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    • 专利摘要:
    polyethylene blend composition suitable for blown film, blown film, article and container device. The present invention provides a polyethylene blend composition suitable for blown (expanded) films, and films made therefrom. the polyethylene blend composition suitable for blown films comprises the molten blend product of: (a) from 0.5 to 4 percent by weight of a low density polyethylene having a density in the range of 0.915 to 0.935 g/cm 3 . and a melt index (i2) in the range of 0.8 to a value less than or equal to 5 g/10 min, and a molecular weight distribution (mw/mn) in the range of 6 to 10; (b) an amount greater than or equal to 90 percent by weight of an ethylene/(alpha)-olefin interpolymer composition having a comonomer distribution constant (cdc) in the range of 75 to 200, a vinyl unsaturation of less than 0 .15 vinyl per 1000 carbon atoms present in the main chain of the ethylene-based polymer composition, a zero shear viscosity ratio (zsvr) in the range of 2 to 20, a density in the range of 0.903 to 0.950 g/cm3, a melt index (i2) in the range of 0.1 to 5 g/10 min, a molecular weight distribution (mw/mn) in the range of 1.8 to 3.5; (c) optionally a neutralizing agent based on hydrotalcite; (d) optionally one or more nucleating agents; and (e) optionally one or more antioxidants.
    公开号:BR112014031191B1
    申请号:R112014031191-9
    申请日:2013-05-22
    公开日:2021-08-24
    发明作者:Mehmet Demirors；Nilesh R. Savargaonkar；Jian Wang；John W. Garnett
    申请人:Dow Global Technologies Llc；
    IPC主号:
    专利说明:

    field of invention
    [0001] The present invention relates to a polyethylene blend composition suitable for blown (expanded) films, and films made with the same. Invention history
    [0002] It is well known to use polymeric materials such as ethylene-based compositions in a blown film extrusion process. The blown film extrusion process employs an extruder that heats, melts, and transports the molten polymeric material and forces it through an annular die. The ethylene-based film is pulled from the die and molded into a tubular shape and eventually passed through a pair of traction or lamination rolls. Afterwards, compressed air is introduced inside the mandrel causing an increase in the diameter of the tube, forming a bubble of the desired size. Thus, the blown film is stretched in two directions, namely, in the axial direction, that is by the use of forced air that expands the diameter of the bubble, and in the longitudinal direction of the bubble, that is, by the action of a winding element that pulls the bubble through the machinery. External air is also introduced around the circumference of the bubble to cool the melt as it exits the die. The film width is varied by introducing more or less internal air into the bubble, thereby increasing or decreasing the bubble size. Film thickness is controlled primarily by increasing or decreasing the speed of the traction roll or the lamination roll to control the rate of section reduction.
    [0003] Then, the bubble is folded into two double layers of film immediately after passing through the traction or laminating roller. The cooled film can then be further processed by cutting or sealing to produce a variety of consumer products.
    [0004] The document WO2011109563 describes a mixture of LDPE and LLDPE suitable for blown films. However, the document WO2011109563 does not suggest that a mixture of the components, observing the respective ranges for their quantities, allows for improved production rates.
    [0005] The document WO2010144784 describes LDPE polymers which, especially when mixed with LLDPE, can have improved processability, especially in terms of increased production due to increased bubble stability. However, WO2010144784 does not suggest a blown film comprising a polyethylene blend composition as defined in the present invention.
    [0006] Despite research efforts to produce the appropriate materials for blown or expanded films, there is still a need for a polyethylene blend composition for blown (or expanded) film, providing improved output rates. Furthermore, there is a need for a method to produce polyethylene blend composition suitable for blown film providing improved output rates. Invention Summary
    [0007] The present invention provides a polyethylene blend composition suitable for blown (expanded) films, and films made with the same.
    [0008] In one embodiment, the present invention provides a polyethylene blend composition suitable for blown films comprising the melt blended product of: (a) from 0.5 to 4 weight percent of a low density polyethylene having a density in the range of 0.915 to 0.935 g/cm3, and a melt index (I2) in the range of 0.8 to a value less than or equal to 5 g/10 min, and a molecular weight distribution (Mw/Mn) in the range from 6 to 10; (b) an amount greater than or equal to 90 percent by weight of an ethylene/α-olefin interpolymer composition having a comonomer distribution constant (CDC) in the range of 75 to 200, a vinyl unsaturation of less than 0.15 vinyl per 1000 carbon atoms present in the main chain of the ethylene-based polymer composition, a zero shear viscosity ratio (ZSVR) in the range of 2 to 20, a density in the range of 0.903 to 0.950 g/cm3, an index of melting (I2) in the range of 0.1 to 5 g/10 min, a molecular weight distribution (Mw/Mn) in the range of 1.8 to 3.5; (c) optionally a neutralizing agent based on hydrotalcite; (d) optionally one or more nucleating agents; and (e) optionally one or more antioxidants.
    [0009] In an alternative embodiment, the present invention provides a blown film comprising the polyethylene blend composition described above.
    In an alternative embodiment, the present invention further provides an article comprising one or more films comprising the polyethylene blend composition described above.
    [0011] In another alternative embodiment, the present invention further provides a container device comprising: (a) one or more substrates; and (b) one or more layers comprising one or more blown films comprising the polyethylene blend composition as described above.
    [0012] In an alternative embodiment, the present invention provides a blend composition suitable for blown film, blown film, article and/or container device, in accordance with any of the foregoing embodiments, except when molding said blend composition of polyethylene in a film via the blown film process, the output rate improves by at least 3 percent over a similar linear low density polyethylene.
    [0013] In an alternative embodiment, the present invention provides a blend composition suitable for blown film, blown film, article and/or container device, in accordance with any of the foregoing embodiments, except that the polyethylene blend composition has a peak at 32.7 ppm measured via 13C NMR, indicating the presence of C3 carbon from C5 branching in the LDPE component.
    [0014] In an alternative embodiment, the present invention provides a blend composition suitable for blown film, blown film, article and/or container device, in accordance with any of the foregoing embodiments, except when molding said blend composition of polyethylene in a film via the blown film process, the total haze improves by at least 15 percent over a blown film consisting essentially of a linear low density polyethylene.
    [0015] In an alternative embodiment, the present invention provides a blend composition suitable for blown film, blown film, article and/or container device, in accordance with any of the foregoing embodiments, except when molding said blend composition of polyethylene in a film via the blown film process, gloss improves by at least 10 percent over a blown film consisting essentially of a linear low density polyethylene. Brief description of the figures
    [0016] For the purpose of illustrating the invention, a form that is exemplary is shown in the drawing; however, it is understood that this invention is not limited to the precise arrangements and instruments shown.
    [0017] Figure 1 shows the 13C NMR spectrum between 32.6 and 32.9 ppm for a low density polyethylene;
    [0018] Figure 2 shows a plot of the residual 1H signal from TCE to 100; and
    [0019] Figure 3 shows the pulse sequences modified for unsaturation with Bruker's AVANCE 400 MHz spectrometer. Detailed description of the invention
    [0020] The present invention provides a polyethylene blend composition suitable for blown films, and films made with the same. As used herein, the term "polyethylene blend-composition" refers to a physical blend of at least one low density polyethylene and one linear low density polyethylene, as described herein.
    [0021] The polyethylene blend composition suitable for blown film according to the present invention comprises the molten blend product of: (a) from 0.5 to 4 percent by weight of a low density polyethylene having a density in the range from 0.915 to 0.935 g/cm3, and a melt index (I2) in the range of 0.8 to a value less than or equal to 5 g/10 min, and a molecular weight distribution (Mw/Mn) in the range of 6 to 10; (b) an amount greater than or equal to 90 percent by weight of an ethylene/α-olefin interpolymer composition having a comonomer distribution constant (CDC) in the range of 75 to 200, a vinyl unsaturation of less than 0.15 vinyl per 1000 carbon atoms present in the main chain of the ethylene-based polymer composition, a zero shear viscosity ratio (ZSVR) in the range of 2 to 20, a density in the range of 0.903 to 0.950 g/cm3, an index of melting (I2) in the range of 0.1 to 5 g/10 min, a molecular weight distribution (Mw/Mn) in the range of 1.8 to 3.5; (c) optionally a neutralizing agent based on hydrotalcite; (d) optionally one or more nucleating agents; and (e) optionally one or more antioxidants.
    [0022] The polyethylene blend composition has a density in the range of 0.903 to 0.950 g/cm3. All individual values and sub-ranges from 0.903 to 0.950 g/cm3 are included and disclosed herein; for example, the density can be from a lower limit of 0.903, 0.905, 0.910, 0.915 g/cm3 to an upper limit of 0.925, 0.930, 0.940, 0.945, or 0.950 g/cm3. For example, the polyethylene blend composition can have a density in the range of 0.917 to 0.925 g/cm3; or alternatively, from 0.918 to 0.922 g/cm3; or alternatively, from 0.919 to 0.922 g/cm3.
    [0023] The polyethylene blend composition has a melt index (I2) in the range of 0.1 to 5 g/10 min. All individual values and subranges from 0.1 to 5 g/10 min here are included and disclosed; for example, the melt index (I2) can be from a lower limit of 0.1, 0.2, 0.5, or 0.8 g/10 min, to an upper limit of 1, 2, 3, 4 , or 5 g/10 min. For example, the polyethylene blend composition may have a melt index (I 2 ) in the range of 0.2 to 5 g/10 min; or alternatively, from 0.2 to 3 g/10 min; or alternatively, from 0.5 to 2 g/10 min.
    [0024] The inventive polyethylene blend compositions provide greater melt strength, better bubble stability and higher output rate as well as improved optical properties.
    In one embodiment, the polyethylene blend composition has a peak at 32.7 ppm measured via 13 C NMR indicating the presence of C3 branch carbon C5 or amyl in the component LDPE.
    [0026] In another embodiment, when molding the polyethylene blend composition into a film via a blown film process, the total haze improves by at least 15 percent, e.g., from 15 percent to 45 percent over a blown film consisting essentially of a linear low density polyethylene.
    [0027] In another embodiment, when molding the polyethylene blend composition into a film via a blown film process, the gloss improves by at least 10 percent, for example, from 10 percent to 30 percent relative to a film blown consisting essentially of a linear low density polyethylene.
    [0028] In another embodiment, when molding the polyethylene blend composition into a film via a blown film process, the throughput improves by at least 3 percent, e.g., from 3 percent to 10 percent over a linear low density polyethylene. Low Density Polyethylene (LDPE) component
    [0029] The polyethylene blend composition suitable for blown film according to the present invention comprises an amount less than or equal to 4 percent by weight of a low density polyethylene (LDPE); for example, from 0.5 to 4 percent by weight; or alternatively, from 0.5 to 3 percent by weight; or alternatively, from 1 to 3.5 percent by weight. Low density polyethylene has a density in the range of 0.915 to 0.935 g/cm3; for example, from 0.915 to 0.925 g/cm3; or alternatively, from 0.918 to 0.922 g/cm3. Low density polyethylene has a melt index (I2) of a value greater than 0.8 at less than or equal to 5 g/10 min; for example 1 to 3 g/10 min; or alternatively from 1.5 to 2.5 g/10 min. Low density polyethylene has a molecular weight distribution (Mw/Mn) in the range of 6 to 10; for example, from 6 to 9.5; or alternatively from 6 to 9; or alternatively from 6 to 8.5; or alternatively from 7.5 to 9. Such low density polyethylene compositions are commercially available, for example, from The Dow Chemical Company.
    [0030] LDPE has a long chain branch of at least 2 per 1000 carbons and/or up to 4 per 1000 carbons. LLDPE component
    [0031] The polyethylene blend composition suitable for blown (expanded) film according to the present invention comprises an amount greater than or equal to 90 percent by weight of the ethylene/α-olefin (linear low density polyethylene) interpolymer composition (LLDPE)); for example, from 96 to 99.5 percent by weight; or alternatively, from 97 to 99.5 percent by weight; or alternatively, from 96.5 to 99 percent by weight. The ethylene/α-olefin (linear low density polyethylene (LLDPE)) interpolymer composition comprises (a) an amount less than or equal to 100 percent by weight, for example, at least 70 percent by weight, or at least 80 percent by weight, or at least 90 percent by weight of the ethylene-derived units; and (b) less than 30 percent by weight, for example, less than 25 percent by weight, or less than 20 percent by weight, or less than 10 percent by weight of units derived from one or more comonomers of α -olefins. As used herein, the term "ethylene/α-olefin interpolymer composition" refers to a polymer that contains more than 50 mole percent polymerized ethylene monomer (based on the total amount of polymerizable monomers) and, optionally, can contain at least one comonomer.
    [0032] Typically, α-olefin comonomers have a maximum of 20 carbon atoms. For example, α-olefin comonomers can preferably have from 3 to 10 carbon atoms, and more preferably from 3 to 8 carbon atoms. Exemplary α-olefin comonomers include, but are not limited to, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, and 4-methyl-1 -pentene. For example, the one or more α-olefin comonomers can be selected from the group consisting of propylene, 1-butene, 1-hexene, and 1-octene; or alternatively from the group consisting of 1-hexene and 1 octene.
    [0033] The ethylene/α-olefin interpolymer composition is characterized by having a comonomer distribution constant in the range of more than 45 to 400, for example, from 75 to 300, or from 75 to 200, or from 85 to 150, or from 85 to 125.
    [0034] The ethylene/α-olefin interpolymer composition is characterized by having a zero shear viscosity ratio (ZSVR) in the range of 2 to 20, for example, from 2 to 10, or from 2 to 6, or from 2.5 to 4.
    [0035] The ethylene/α-olefin interpolymer composition according to the present invention has a density in the range of 0.903 to 0.950 g/cm3. For example, the density can be from a lower limit of 0.903, 0.905, 0.908, 0.910, or 0.912 g/cm3 to an upper limit of 0.925, 0.935, 0.940, 0.945, 0.950 g/cm3.
    [0036] The ethylene/α-olefin interpolymer composition has a molecular weight distribution (Mw/Mn) in the range of 1.8 to 3.5. For example, the molecular weight distribution (Mw/Mn) can be from a lower limit of 1.8, 2, 2.1, or 2.2 to an upper limit of 2.5, 2.7, 2.9 , 3.2, or 3.5.
    [0037] The ethylene/α-olefin interpolymer composition has a melt index (I2) in the range of 0.1 to 5 g/10 min. For example, the melt index (I2) can be from a lower limit of 0.1, 0.2, 0.5, or 0.8 g/10 min to an upper limit of 1.2, 1.5, 1.8, 2.0, 2.2, 2.5, 3.0, 4.0, 4.5 or 5.0 g/10 min.
    [0038] The ethylene/α-olefin interpolymer composition has a molecular weight (Mw) in the range of 50,000 to 250,000 Dalton. For example, the molecular weight (Mw) can be from a lower limit of 50,000, 60,000, 70,000 Dalton to an upper limit of 150,000, 180,000, 200,000 or 250,000 Dalton.
    [0039] The ethylene/α-olefin interpolymer composition has a molecular hair distribution (Mz/Mw) in the range of values less than 4, for example, in the range of values less than 3, or from 2 to 2.8 .
    [0040] The ethylene/α-olefin interpolymer composition has a vinyl unsaturation of less than 0.15 vinyl per 1000 carbon atoms present in the backbone of the ethylene-based polymer composition.
    [0041] The ethylene/α-olefin interpolymer composition has a long chain branching frequency in the range of 0.02 to 3 long chain branches (LCB) per 1000C.
    [0042] In an embodiment, the ethylene/α-olefin interpolymer composition comprises an amount less than or equal to 100 parts, for example, less than 10 parts, less than 8 parts, less than 5 parts, less than 4 parts, less than 1 part, less than 0.5 part, or less than 0.1 part by weight of metal complex residues remaining from a catalytic system comprising a metal complex of a polyvalent aryloxy ether per one million parts of the polymeric composition based on ethylene. One can measure the remaining metal complex residues of the catalytic system comprising a metal complex of a polyvalent aryloxy ether in the ethylene-based polymer composition by X-ray fluorescence (XRF), which is calibrated to reference standards. The polymer resin beads were high temperature compression molded into slabs having a thickness of about 0.95 cm (3/8 inch) for X-ray measurement in a preferred method. At very low metal complex concentrations, such as below 0.1 ppm, ICP-AES would be an appropriate method to determine metal complex residues present in the ethylene-based polymer composition.
    [0043] The ethylene/α-olefin interpolymer composition may further comprise additional components such as one or more other polymers and/or one or more additives. Such additives include, but are not limited to, antistatic agents, color enhancers, dyes, lubricants, fillers such as TiO2 or CaCO3, opacifiers, nucleants, processing aids, pigments, primary antioxidants, secondary antioxidants, UV stabilizers, nonsticks, slip agents, tackifiers, flame retardants, antimicrobial agents, odor reducing agents, fungicides, and combinations thereof. The ethylene-based polymer composition can contain from about 0.1 to about 10 percent combined by weight of such additives, based on the weight of the ethylene-based polymer composition including such additives.
    [0044] In one embodiment, ethylene/α-olefin interpolymer composition has a comonomer distribution profile comprising a monomodal distribution or a bimodal distribution in the temperature range of 35°C to 120°C, excluding purge.
    [0045] Any conventional ethylene (co)polymerization reaction processes can be employed to produce the ethylene-based polymer composition. Such conventional ethylene (co)polymerization reaction processes include, but are not limited to, gas phase polymerization process, slurry phase polymerization process, solution phase polymerization process, and combinations thereof using a or more conventional reactors, for example, gas phase fluidized bed reactors, closed loop reactors, stirred tank reactors, batch reactors in parallel, in series, and/or any combinations thereof.
    [0046] In one embodiment, the ethylene/α-olefin interpolymer composition is prepared via a process comprising the steps of: (a) polymerizing ethylene and optionally one or more α-olefins in the presence of a first catalyst to form a polymer the semi-crystalline ethylene base in a first reactor or in a first part of a multi-part reactor; and (b) reacting freshly supplied ethylene and optionally one or more α-olefins in the presence of a second catalyst comprising an organometallic catalyst thereby forming an ethylene/α-olefin interpolymer composition in at least one other reactor or in a later part of a multi-part reactor, at least one of the catalytic systems in step (a) or (b) comprising a metal complex of a polyvalent aryloxy ether corresponding to the formula:
    in which M3 is Ti, Hf or Zr, preferably Zr; at each occurrence Ar4 is independently a substituted C9-20 aryl group, at each occurrence the substituents are independently selected from the group consisting of alkyl; cycloalkyl; and aryl groups; and derivatives thereof substituted with halogen, trihydrocarbyl silyl and halohydrocarbyl, with the proviso that at least one substituent lacks coplanarity with the aryl group to which it binds; at each occurrence, T4 is independently a C2-20 alkylene, cycloalkylene or cycloalkenylene group, or an inertly substituted derivative thereof; in each occurrence, R21 is independently hydrogen, halogen, hydrocarbyl group, trihydrocarbyl silyl, trihydrocarbyl silyl hydrocarbyl, alkoxy or di(hydrocarbyl)amino of up to 50 atoms not containing hydrogens; at each occurrence, R3 is independently hydrogen, halogen, hydrocarbyl, trihydrocarbyl silyl, trihydrocarbyl silyl hydrocarbyl, alkoxy or amino of up to 50 atoms not containing hydrogens, or two R3 groups together on the same arylene ring or one R3 and one R21 group together on the same arylene ring or in different arylene rings form a bivalent linking group attached to the arylene group at two positions or join two different arylene rings; and in each occurrence, RD is independently a halogen or hydrocarbyl or trihydrocarbyl silyl group of up to 20 atoms not containing hydrogens, or 2 RD groups together were a hydrocarbylene, hydrocarbadiyl, diene or poly(hydrocarbyl)xylylene group.
    [0047] The ethylene/α-olefin interpolymer composition can be produced via a solution polymerization according to the following exemplary process.
    [0048] All raw materials (ethylene, 1-octene) and the process solvent (a high purity isoparaffinic solvent with a narrow boiling range commercially obtainable under the trade name ISOPAR E from ExxonMobil Corporation) are purified with molecular sieves before introduction into the reaction environment. Hydrogen is supplied in pressurized cylinders to a high purity grade and is not further purified. The monomer (ethylene) feed stream into the reactor is pressurized via a mechanical compressor to a pressure that is above the reaction pressure, approximately 5.17 MPag (750 psig). The solvent and comonomer (1-octene) feed is pressurized via a positive displacement mechanical pump to a pressure that is above the reaction pressure, approximately 5.17 MPag (750 psig). The individual catalytic components are manually batch diluted to specified component concentrations with purified solvent (ISOPAR E) and pressurized to a pressure that is above the reaction pressure, approximately 5.17 MPag (750 psig). All reaction feed flows are measured with independently controlled flowmeters with automatic computerized valve control systems.
    [0049] The continuous solution polymerization reactor system can consist of two closed loops filled with liquid, non-adiabatic, isothermal, circulating, and independently controlled operating in a series configuration. Each reactor has independent control of all new solvent, monomer, comonomer, hydrogen, and catalytic component feeds. The combined feed temperature of solvent, monomer, comonomer and hydrogen to each reactor is independently controlled somewhere between 5°C and 50°C and typically 40°C by passing the feed stream through a heat exchanger. The new comonomer feed to the polymerization reactors can be manually aligned to add comonomer to one of three choices: the first reactor, the second reactor, or the common solvent and then split between both reactors proportional to the solvent feed split. Total fresh feed for each polymerization reactor is injected into the reactor at two locations per reactor with approximately equal volumes of reactor between each injection site. Typically, fresh feed is controlled with each injector receiving half of the total fresh feed mass flow. The catalytic components are injected into the polymerization reactor through specially designed injection stingers and each of them is injected into the same relative location in the reactor with no contact time before the reactor. The main catalyst component feed is computer controlled to maintain the monomer concentration in the reactor at a specified value. The two cocatalyst components are fed based on specific molar ratios calculated for the main catalyst component. Immediately after each new injection site (either feed or catalyst), feed streams are mixed with the polymerization reactor circulating contents with static mixing elements. The contents of each reactor are continuously circulated through heat exchangers responsible for removing most of the reaction heat and with the refrigerant side temperature responsible for maintaining an isothermal reaction environment at the specified temperature. Circulation around each reactor loop is provided by a spiral pump. The effluent from the first polymerization reactor (containing solvent, monomer, comonomer, hydrogen, catalytic components, and molten polymer) leaves the closed circuit of the first reactor and passes through a control valve (responsible for maintaining the pressure of the first reactor at a value specific) and is injected into the second polymerization reactor of similar design. When the current leaves the reactor, it is contacted with a deactivating agent, eg water, to stop the reaction. Also, various additives such as antioxidants can be added at this point. The stream then passes through another set of static mixing elements to evenly disperse the catalyst deactivating agent and additives.
    [0050] After the addition of additives, the effluent (containing solvent, monomer, comonomer, hydrogen, catalyst components, and molten polymer) passes through a heat exchanger to raise the current temperature in preparation for separating the polymer from the others minor boiling reaction components. The stream then enters a two-stage separation and devolatilization system where the polymer is removed from the solvent, hydrogen, and unreacted monomer and comonomer. The recycled stream is purified before re-entering the reactor. The separated, devolatilized polymer melt is pumped through a specially designed die for underwater pelletizing, cut into uniform solid pellets, dried and transferred to a hopper. Additions
    [0051] The polyethylene blend composition may further comprise one or more additional additives. Such additives include, but are not limited to, one or more hydrotalcite-based neutralizing agents, one or more nucleating agents, one or more antistatic agents, one or more color enhancers, one or more dyes, one or more lubricants, one or more fillers, one or more pigments, one or more primary antioxidants, one or more secondary antioxidants, one or more processing aids, one or more UV stabilizers, and/or combinations thereof. The polyethylene blend composition can comprise any amounts of such additives. The polyethylene blend composition can comprise from about 0 to about 10 weight percent combined of such additives, based on the total weight of the polyethylene blend composition. Production
    [0052] The polyethylene blend composition is prepared via any conventional melt blending process such as extrusion via an extruder, e.g. a single or twin screw extruder. The LDPE, LLDPE, and optionally one or more additives can be melt blended in any order via one or more extruders to form a uniform polyethylene blend composition. applications
    [0053] The polyethylene blend composition can be cast into a film via, for example, a blown (expanded) film process. In one embodiment, when molding the polyethylene blend composition into a film via a blown film process, the output rate is improved by at least 3 percent over a similar linear low density polyethylene; or alternatively, the total haze is improved by at least 15 percent relative to a blown film consisting essentially of linear low density polyethylene; or alternatively, gloss is improved by at least 10 percent over a blown film consisting essentially of linear low density polyethylene. In one embodiment, the polyethylene blend composition can be molded into a multi-layer blown film structure. In another embodiment, one can cast the polyethylene blend composition into a single-layer or multi-layer blown film structure associated with one or more substrates. The blown (expanded) films prepared in accordance with the present invention can be used as lamination films where the blown (expanded) polyethylene film is adhesively laminated to a substrate such as biaxially oriented polypropylene (BOPP) films or poly(ethylene) films. ethylene terephthalate) biaxially oriented (BOPET), coating films, sealing webs, shrinking films, stretching films, etc. Blown films in accordance with the present invention have a thickness in the range of 0.008 to 0.127 mm (0.3 to 5 milliinch), for example 0.013 to 0.127 mm (0.5 to 5 milliinch). Examples
    [0054] The following examples illustrate the present invention, but are not intended to limit the scope of the invention. The examples of the present invention demonstrate that when molding the polyethylene blend composition into a film via a blown film process, the output rate is improved by at least 3 percent over a similar linear low density polyethylene; or alternatively, the total haze is improved by at least 15 percent relative to a blown film consisting essentially of linear low density polyethylene; or alternatively, gloss is improved by at least 10 percent over a blown film consisting essentially of linear low density polyethylene. Inventive Composition 1
    [0055] Inventive composition 1 is a polyethylene blend composition comprising the molten blend product of (a) 3 weight percent of a low density polyethylene (LDPE) component having a melt index (I2) of approximately 1 .85 g/10 min, and a density of 0.919 g/cm3 as further defined in Table 1, provided by The Dow Chemical Company; and (b) 97 percent by weight of a 1 component linear low density polyethylene (LLDPE 1) (including 900 parts DHT-4A per million parts LLDPE 1), which is a linear low density polyethylene (LLDPE) prepared via solution polymerization process in a configuration of two reactors connected in series in the presence of a catalyst comprising a metal complex of a polyvalent aryloxy ether, described above, having a melt index (I2) of approximately 0.91 g/10 min and a density of approximately 0.918 g/cm3, and further described in Table 1. The properties of Inventive Composition 1 are measured, and reported in Table 2. Comparative Composition A
    [0056] Comparative Composition A is a linear low density polyethylene 1 (LLDPE 1), which is a linear low density polyethylene (LLDPE) prepared via a solution polymerization process in a configuration of two reactors connected in series in the presence of one catalyst comprising a metal complex of a polyvalent aryloxy ether, described above, having a melt index (I2) of approximately 0.91 g/10 min and a density of approximately 0.918 g/cm3, and further described in Table 1. The properties of Comparative Composition A are measured, and reported in Table 2. Inventive Film 1
    [0057] Inventive Composition 1 is cast into Inventive Film 1 via a blown film process based on the process conditions reported in Table 3. Inventive Film 1, a single layer film, was tested for its properties, and the results are reported in Table 4. The film properties reported in Table 4 are for films made at a maximum rate of 173.27 kg/h (approximately 15.3 lbs/hr/inch or 382 lbs/hr). Comparative Film A
    [0058] Comparative Composition A is cast into Comparative Film A via a blown film process based on the process conditions reported in Table 3. Comparative Film A, a single-layer film, was tested for its properties, and the results are reported in Table 4. The film properties reported in Table 4 are for films made at a maximum rate of 167.82 kg/h (approximately 14.8 lbs/hr/inch or 370 lbs/hr). Test Methods
    [0059] Test methods include the following: Melt Index
    The melt indexes (I2 and I10) were measured according to ASTM D-1238 at 190°C and load of 2.16 kg and 10 kg, respectively. Their values are reported in g/10 min. Density
    Samples for density measurement were prepared in accordance with ASTM D4703. Measurements were made within 1 hour of sample pressing using ASTM D792, Method B. Dynamic Shear Rheology
    Samples were compression molded into circular plates 3 mm thick by 25 mm in diameter at 177°C for 5 minutes under a pressure of 10 MPa in air. Afterwards, the sample was removed from the press and placed on the counter to cool.
    [0063] Frequency sweep measurements were performed at constant temperature in an ARES controlled strain rheometer (TA Instruments) equipped with 25 mm parallel plates, in nitrogen purge. For each measurement, the rheometer was thermally balanced for at least 30 minutes before resetting the interval. The sample was placed on the plate and allowed to melt for five minutes at 190°C. The samples were then closed to 2 mm, the sample rectified, and then the test started. The method of a preset additional five minute delay to allow for temperature balance. The experiments were carried out at 190°C across a frequency range of 0.1-100 rad/s at five points per ten interval. The deformation amplitude was constant at 10%. The voltage response was analyzed in terms of amplitude and phase, from which storage modulus (G'), loss modulus (G”), complex modulus (G*), dynamic viscosity (n*), and tg delta or tg (δ). Cast strength
    Melt strength measurements were performed Rheotens Gottfert 71.97 (Goettfert Inc., Rock Hill, SC) attached to a Rheotester 2000 Gottfert capillary rheometer. A polymer melt is extruded through a capillary matrix having a flat entry angle (180°) with a capillary diameter of 2.0 mm and an aspect ratio (capillary length/capillary diameter) of 15.
    [0065] After equilibrating the samples at 190°C for 10 minutes, the piston is operated at a constant speed of 0.265 mm/s. The standard test temperature is 190°C. The sample is taken uniaxially to a set of accelerator clamps located 100 mm below the matrix with an acceleration of 2.4 mm/s2. Traction force is recorded as a function of the tightening speed of the compression cylinders. The melt strength is recorded as the plateau force (cN) before the course breaks. The following conditions are used in melt strength measurements: Plunger velocity = 0.265 mm/s; wheel acceleration = 2.4 mm/s2; capillary diameter = 2.0 mm; capillary length=30 mm; and drum diameter = 12 mm. Determination of crystallinity by DSC
    [0066] One can use differential scanning calorimetry (DSC) to measure the crystallinity of a sample at a given temperature over a wide range of temperatures. For the Examples, a TA model Q1000 DSC (TA Instruments, New Castle, DE) equipped with an RSC (Refrigerated Cooling System) cooling accessory and an autosampler module is used to perform the tests. During testing, a nitrogen purge gas flow of 50 mL/min is used. Each sample is compressed into a thin film and melted in the press at about 175°C; the molten sample is then air cooled to room temperature (~25°C). A 3-10 mg sample of the cooled material is cut into a 6 mm diameter disk, weighed, placed in a lightweight aluminum pan (approximately 50 mg), and crimped closed. Afterwards, the sample is tested for its thermal behavior.
    [0067] The thermal behavior of the sample is determined by changing the temperature of the sample up and down to create a response against temperature profile. First, the sample is rapidly heated to 180°C and held in an isothermal state for 3 minutes to remove any previous thermal history. The sample is then cooled to -40°C at a cooling rate of 10°C/min and held at -40°C for 3 minutes. Then, the sample is heated to 150 °C at a heating rate of 10 °C/min. The cooling and second heating curves are recorded. The values determined are the maximum melting temperature (Tm), the maximum crystallization temperature (Tc), the heat of melting (Hf), and the % crystallinity for polyethylene samples calculated using the following equation:

    [0068] The heat of fusion (Hf) and the maximum fusion temperature are reported from the second heating curve. The maximum crystallization temperature of the cooling curve is determined. High Temperature Gel Permeation Chromatography
    [0069] The gel permeation chromatography (GPC) system consists of a Waters (Milford, Mass) 150°C high temperature chromatograph (other high temperature GPC instruments include the Model 210 and Model 220 from Polymer Laboratories (Shropshire, UK)) equipped with a differential refractometer (RI) in the instrument (other suitable concentration detectors may include an IR4 infrared detector from PolymerChar (Valencia, Spain) Data collection is performed using TriSEC software from Viscotek, version 3, and a 4-channel DM400 data manager from Viscotek.The system is also equipped with a solvent degassing device in the line from Polymer Laboratories (Shropshire, UK).
    Appropriate high temperature GPC columns can be used such as four 30 cm long HT803 Shodex 13 micron columns or four 30 cm long Polymer Labs 20 micron mixed pore size thickened columns (MixA LS , Polymer Labs). The sample carousel compartment is operated at 140°C and the column compartment is operated at 150°C. Samples are prepared at a concentration of 0.1 g polymer in 50 ml solvent. The chromatographic solvent and sample preparation solvent contain 200 ppm trichlorobenzene (TCB). Both solvents are sparged with nitrogen. Polyethylene samples are gently shaken at 160°C for four hours. The injection volume is 200 μL. The flow rate through the GPC is adjusted to 1 mL/min.
    [0071] The set of GPC columns is calibrated by operating 21 polystyrene standards of narrow molecular weight distribution. The molecular weight (Mw) of the standards ranges from 580 to 8,400,000, and the standards are contained in 6 “cocktail” blends. Each mixture of standards has at least a dozen separations between individual molecular weights. Standard mixes are purchased from Polymer Laboratories. Polystyrene standards are prepared in 0.025 g in 50 mL solvent for molecular weights greater than or equal to 1,000,000 and 0.05 g in 50 mL solvent for molecular weights less than 1,000,000. Polystyrene standards were dissolved at 80°C with gentle agitation for 30 minutes. Narrow standard mixtures are used first and in order to lower maximum molecular weight component to minimize degradation. Standard polystyrene maximum molecular weights are converted to polyethylene molecular weights using Equation 2 (described in Williams and Ward, J. Polym. Sci., Polym. Letters, 6, 621 (1968)):
    where M is the molecular weight of polyethylene or polystyrene (as marked), and B equals 1.0. Those skilled in the art know that A can range from about 0.38 to about 0.44 and is determined at the time of calibration using a broad polyethylene standard. The use of this polyethylene calibration method to determine molecular weight values, such as molecular weight distribution (MWD or Mw/Mn), and related statistics (generally referred to as conventional GPC or GPC-cc results), is defined herein. as modified Williams and Ward method. 13C NMR
    Samples were prepared by adding approximately 2.7 g of a 50/50 mixture of tetrachloroethane-d2/ortho-dichlorobenzene containing 0.025M Cr(AcAc)3 to 0.4 g of sample in a 10 mm Norell NMR tube 1001-7, and then purging in a box of N2 for 2 hours. The samples were dissolved and homogenized by heating the tube and its contents to 150°C using a heat block and torch. Each sample was visually inspected to ensure homogeneity. Data were collected using a Bruker 400 MHz spectrometer equipped with a double Bruker DUL high temperature cryogenic probe. Data were acquired at 57-80 hours per data file, a pulse repetition delay of 7.3 s (6 s delay + 1.3 s acquisition time), 90° excitation angles, and decoupling inverse batch with a sample temperature of 120°C. All measurements are performed on non-rotating specimens in locked mode. Samples were homogenized immediately prior to insertion into the heated NMR sample converter (125°C), and were thermally equilibrated on the probe for 7 minutes prior to data acquisition. The number of branches was calculated from the integral of the peak region at 32.7 ppm and their relative peak ratio of pure LDPE. Elution and crystallization fractionation method (CEF)
    [0073] Comonomer distribution analysis with fractionation by elution and crystallization (CEF) is performed (PolymerChar, Spain) (B. Monrabal et al., Macromol. Symp. 257, 71-79 (2007)). It is used as a solvent ortho-dichlorobenzene (ODCB) with 600 ppm of the antioxidant butylated hydroxy toluene (BHT). Sample preparation is done with an automatic feeding system at 160°C with 2 hours under agitation at 4 mg/mL (unless otherwise specified). The injection volume is 300 μL. The CEF temperature profile is: crystallization at 3°C/min at 110°C to 30°C, thermal equilibrium at 30°C for 5 minutes, elution at 3°C /min from 110°C to 30°C, thermal equilibrium at 30°C for 5 minutes, elution at 3°C/min from 30°C to 140°C. The flow rate during crystallization is 0.052 ml/min. The flow rate during elution is 0.50 ml/min. Data is collected at one data point/second.
    [0074] The CEF column is loaded by The Dow Chemical Company with glass beads at 125 µm ± 6% (MO-SCI Specialty Products) with 0.32 cm (1/8 inch) steel tubing. Glass beads are acid washed by MO-SCI Specialty on request from The Dow Chemical Company. Column volume is 2.06 ml. Column temperature calibration is performed using a linear polyethylene mixture of NIST 1475a standard reference material (1.0 mg/mL) and eicosan (2 mg/mL) in ODCB. The temperature is calibrated by adjusting the heat elution rate so that linear polyethylene NIST 1475a has a maximum temperature of 101.0°C, and eicosan has a maximum temperature of 30.0°C. Column resolution of CEF is calculated with a mixture of linear polyethylene NIST 1475a (1.0 mg/ml) and hexacontane (Fluka, purity >97.0%, 1 mg/ml). A baseline separation of hexacontane and NIST 1475a linear polyethylene is achieved. The hexacontane area (from 35.0 to 67.0°C) for the area of linear polyethylene NIST 1475a (from 67.0 to 110.0°C) is 50 to 50, the amount of soluble fraction below 35 ,0°C is less than 1.8% by weight. The CEF column resolution is defined in the following equation:
    where column resolution is 6.0. Comonomer Distribution Constant Method (CDC)
    [0075] The comonomer distribution constant (CDC) is calculated from the comonomer distribution profile by CEF. CDC is defined as the comonomer distribution index divided by the comonomer distribution form factor multiplied by 100 as shown in the following equation: Comonomer distribution index Comonomer distribution index

    [0076] The comonomer distribution index represents the total weight fraction of polymer chains with the comonomer content ranging from 0.5 of the average comonomer content (Cmedium) and 1.5 of Cmedium from 35.0 to 119°C. Comonomer distribution form factor is defined as the ratio of the comonomer distribution profile half-width divided by the maximum temperature (Tp) comonomer distribution profile standard deviation.
    [0077] CDC is calculated from the comonomer distribution profile by CEF, and CDC is defined as the comonomer distribution index divided by comonomer distribution form factor multiplied by 100 as shown in the following equation: Index comonomer distribution index comonomer distribution
    where the comonomer distribution index represents the total weight fraction of polymeric chains with the comonomer content ranging from 0.5 of the average comonomer content (Caverage) and 1.5 of Cmedium from 35.0 to 119°C, where the comonomer distribution form factor as the ratio of the comonomer distribution profile semi-amplitude divided by the maximum temperature comonomer distribution profile standard deviation (Tp).
    [0078] CDC is calculated according to the following steps: (A) Obtain a weight fraction at each temperature (T) (wT(T)) from 35.0°C to 119.0°C with a step increase temperature of 0.200°C of CEF according to the following equation:
    (B) Calculate the average temperature (Tmean) in cumulative weight fraction of 0.500 according to the following equation:
    (C) Calculate the corresponding mean comonomer content in mole % (Cmean) at the mean temperature (Tmean) using the comonomer content calibration curve according to the following equation:
    (D) Construct a comonomer content calibration curve using a series of reference materials with known amount of comonomer content, ie, eleven reference materials with narrow comonomer distribution (monomodal comonomer distribution at CEF 35.0 at 119.0°C) with weight average molecular weight Mw of 35,000 to 115,000 (measured via conventional GPC) at a comonomer content ranging from 0.0% mol to 7.0 mol% are analyzed with CEF under the same experimental conditions specified in experimental sections of CEF; (E) Calculate comonomer content calibration using the maximum temperature (Tp) of each reference material and its comonomer content. The calibration of each reference material is calculated according to the following equation:
    (Equation 7) where R2 is the correlation constant; (F) Calculate the comonomer distribution index of the total weight fraction with a comonomer content ranging from 0.5*Caverage to 1.5*Caverage, and if Tmean is greater than 98.0°C, the distribution index of comonomer will be set to 0.95; (G) Obtain the CEF comonomer distribution profile maximum peak height by searching each data point for the maximum peak of 35.0°C to 119.0°C (if the two peaks are identical, then the smallest peak temperature will be selected); semi-amplitude is defined as the temperature difference between the front temperature and the back temperature at half of the maximum peak height, the front temperature at half of the maximum peak is looked for before 35.0°C, while the back temperature at half of the maximum peak is sought after 119.0°C, in the case of a well-defined bimodal distribution where the difference in peak temperatures is greater than or equal to 1.1 times the sum of the semi-amplitude of each peak, the semi-amplitude of the polymer composition the inventive ethylene base is calculated as the arithmetic mean of the semi-amplitude of each peak; (H) Calculates the standard deviation (Stdev) according to the following equation:
    (Equation 8) Viscosity measurement method with zero shear via strain
    [0079] Zero shear viscosities are obtained via strain tests which were performed in an AR-G2 tension controlled rheometer (TA Instruments, New Castle, Del) using 25 mm diameter parallel plates at 190°C. Set the rheometer oven to test temperature for at least 30 minutes before resetting fixtures. At the test temperature a compression molded sample disc is inserted between the plates and allowed to reach equilibrium for 5 minutes. The top plate is then lowered to 50 μm above the desired test span (1.5 mm). Any unnecessary material is cut and the top plate is lowered to the desired gap. Measurements are made under nitrogen purge at a flow rate of 5 L/min. The deformation absent time is set to 2 hours.
    [0080] A constant low shear stress of 20 Pa is applied to all samples to ensure that the steady state shear rate is low enough to be in the Newtonian region. In this study, the resulting steady-state shear rates are in the range of 10-3 to 10-4 s-1 for the samples. The steady state (steady state) is determined by a linear regression for all data in the last 10% time window of the graph of log(J(t)) against log(t), where J(t) is the deformation length and t is the deformation time. If the slope of the linear regression is greater than 0.97, it is considered that the equilibrium state has been reached, and then the strain test is stopped. In this study, in all cases the slope satisfies the criterion within the 2-hour limits. The steady-state shear rate is determined from the slope of the linear regression of all data points in the last 10% time window of the graph of ε against t, where ε is strain. The zero shear viscosity is determined from the ratio of the applied stress to the steady state (steady state) shear rate.
    [0081] In order to determine whether the sample degrades during the strain test, a small amplitude oscillatory shear test is performed before and after the strain test on the same specimen from 0.1 to 100 rad/s. The complex viscosity values of the two tests are compared. If the difference in viscosity values at 0.1 rad/s is greater than 5%, the sample is considered to have degraded during the strain test, and the result is discarded.
    [0082] Zero shear viscosity ratio (ZSVR) is defined as the ratio of the zero shear viscosity (ZSV) of the branched polyethylene material to the ZSV of the linear polyethylene material in the equivalent weight average molecular weight (Mw-gcp) according to the following equation:
    (Equation 9)
    [0083] The ZSV value of the strain test at 190°C is obtained via the method described above. The Mw-gpc value is determined by the conventional GPC method. The correlation between linear polyethylene ZSV and its Mw-gpc was established based on a series of linear polyethylene reference materials. A description of the ZSV-Mw relationship can be found in the ANTEC process: Karjala, Teresa P.; Sammler, Robert L.; Mangnus, Marc A.; Hazlitt, Lonnie G.; Johnson, Mark S.; Hagen, Charles M., Jr.; Huang, Joe W.L.; Reichek, Kenneth N., “Detection of low levels of long-chain branching in polyolefins”. Annual Technical Conference - Society of Plastics Engineers (2008), 66th, 887-891. 1H NMR Method
    [0084] 3.26 g of stock solution is added to 0.133 g of polyolefin sample in 10 mm NMR tube. The stock solution is a mixture of tetrachloroethane-d2 (TCE) and perchlorethylene (50:50, w:w) with Cr3+ 0.001M. The solution in the tube is purged with N2 for 5 minutes to reduce the amount of oxygen. The capped sample tube is left at room temperature overnight to swell the polymeric sample. The sample is dissolved at 110°C with vibration. The samples are free of additives that can contribute to unsaturation, for example glidants such as erucamide.
    1H NMR is performed with a 10 mm cryogenic probe at 120°C on an AVANCE 400 MHz Bruker spectrometer.
    [0086] Two experiments are performed to obtain the unsaturation: the control experiments and the double pre-saturation.
    [0087] For the control experiment, data is processed with exponential window function with LB= 1 Hz, baseline was corrected from 7 to -2 ppm. The residual 1H TCE signal is adjusted to 100, Itotal from -0.5 to 3 ppm is used as the whole polymer signal in the control experiment. The number of CH 2 group, NCH 2 in the polymer is calculated as follows: NCH 2 = Itotal/2.
    [0088] For the double pre-saturation experiment, data are processed with exponential window function with LB = 1 Hz, baseline was corrected from 6.6 to 4.5 ppm. The residual 1H signal of TCE is adjusted to 100, the corresponding integrals for unsaturations (Ivinylene, Itrissubstituted, Ivinyl and Ivinylidene) were integrated based on the region shown in the graph in Figure 2.
    [0089] The unsaturation unit number for vinylene, trisubstituted, vinyl and vinylidene is calculated:

    [0090] The unit of unsaturation/1,000,000 carbons is calculated as follows:

    [0091] The requirement for NMR analysis of unsaturation includes: quantification level is 0.47 ± 0.02/1,000,000 carbon to Vd2 with 200 scans (data acquisition less than 1 hour including time to run the experiment of control) with 3.9% by weight of sample (for Vd2 structure, see Macromolecules, vol. 38, 6988, 2005), 10 mm high temperature cryogenic probe. The quantization level is defined as the signal to noise ratio of 10.
    [0092] The chemical shift reference is set at 6.0 ppm for the 1H residual proton signal of TCT-d2. The control is carried out with pulse ZG, TD 32768, NS 4, DS 12, SWH 10.000 Hz, AQ 1.64 s, D1 14 s. The double presaturation experiment is performed with a modified pulse sequence, O1P 1.354 ppm, O2P 0.960 ppm, PL9 57db, PL21 70db, TD 32768, NS 200, DS 4, SWH 10,000 Hz, AQ 1.64 s, D1 1 s, D13 13 s. Figure 3 shows the pulse sequences modified for unsaturation with Bruker's AVANCE 400 MHz spectrometer. Film Test Conditions
    [0093] The following physical properties are measured on the produced films: • Total turbidity: Samples measured for total turbidity are prepared in accordance with ASTM D 1746. Hazegard Plus (BYK-Gardner USA, Columbia, MD) is used for testing. • 45° Brightness: ASTM D-2457. • 1% Modulus of Elasticity - MD (machine direction) and CD (cross direction): ASTM D-882. • Elmendorf breaking strength in MD and CD: ASTM D-1922. • Tensile strength in MD and CD: ASTM D-1922. • Dart Impact Resistance: ASTM D-1709, Method A. • Puncture Resistance: Puncture resistance is measured on an Instron Model 4201 with Testworks Sintech software version 3.10. The sample size is 15.23 cm x 15.23 cm (6” x 6”) and 4 measurements are taken to determine an average perforation value. The film is conditioned for 40 hours after film production and for at least 24 hours in a controlled ASTM laboratory. A 100-pound load cell with an 81.37 cm2 (12.56 inch2) round sample clamp is used. The drill rig is a 1.27 cm (0.5 inch) diameter polished stainless steel ball with a maximum displacement length of 19.05 (7.5 inches). There is no gauge length; the probe is as close as possible to the sample, but not touching it. The piston speed is 25.4 cm (10 inches/min). The thickness in the middle of the sample is measured. The film thickness, the distance traveled by the plunger, and the maximum load are used to determine the perforation by the software. The drill probe is cleaned using a tissue after each sample. Determining the maximum blown film output rate
    [0094] Film samples are collected at a controlled rate and at a maximum rate. The controlled rate is 113.40 kg/hr (250 lbs/hr) which is equal to the output rate of 10 lbs/hr/inch die circumference. Note that the matrix diameter used for the output rate experiments is a 20.32 cm (8 inches) matrix such that for the controlled rate, as an example, the conversion between pound/h and pound/h/inch of matrix circumference is shown in Equation 18. Similarly, such an equation can be used for other rates, such as the maximum rate, by replacing the maximum rate in Equation 18 with the standard rate of 113.40 kg/h (250 lbs/h). ) to determine the lb/h/inch of matrix circumference.
    (Equation 18)
    [0095] The maximum rate for a given sample is determined by increasing the output rate to the point where bubble stability is the limiting factor. The extruder profile is maintained for both samples (standard rate and full rate), however the melting temperature is higher for the full rate samples due to the increase in shear rate. The maximum rate is determined by maximizing both internal bubble cooling and external air ring cooling. The maximum bubble stability is determined by bringing the bubble to the point where any of the following are observed: (a) the bubble would not remain supported in the air ring, (b) the bubble began to lose its shape, (c) the bubble has started to breathe in and out, or (d) the freezing line height becomes unstable. At that point the rate is deducted to where the bubble is replaced in the air ring maintaining the bubble shape and a stationary freezing line height and then the sample is collected. The bubble cooling is adjusted by adjusting the air ring and holding the bubble. This is considered with the maximum output rate maintaining bubble stability.
    [0096] Single-layer films were produced. The die diameter is 20.32 cm (8 inches), the die gauge is 1.778 mm (70 milli inches), the burst ratio is 2.5, and internal bubble cooling is used.
    [0097] The present invention may be incorporated in other forms without departing from the spirit and essential attributes thereof, and, consequently, reference should be made to the appended claims, rather than the previous descriptive report, as indicating the scope of the invention .


    权利要求:
    Claims (6)
    [0001]
    1. Polyethylene blend composition suitable for blown film, characterized in that the molten blend product comprises: - from 0.5 to 4 percent by weight of a low density polyethylene having a density in the range of 0.915 to 0.935 g/cm3, and a melt index (I2) in the range of 0.8 to a value less than or equal to 5 g/10 min, and a molecular weight distribution (Mw/Mn) in the range of 6 to 10; - an amount greater than or equal to 90 percent by weight of an ethylene/α-olefin interpolymer composition having a comonomer distribution constant (CDC) in the range of 75 to 200, a vinyl unsaturation of less than 0.15 vinyl per 1000 carbon atoms present in the main chain of the ethylene-based polymer composition, a zero shear viscosity ratio (ZSVR) in the range of 2 to 20, a density in the range of 0.903 to 0.950 g/cm3, a melt index ( I2) in the range of 0.1 to 5 g/10 min, a molecular weight distribution (Mw/Mn) in the range of 1.8 to 3.5; - optionally a neutralizing agent based on hydrotalcite; - optionally one or more nucleating agents; - and optionally one or more antioxidants.
    [0002]
    2. Polyethylene blend composition according to claim 1, characterized in that when said polyethylene blend composition is cast into a film via the blown film process, the output rate is improved by 3 percent over a similar linear low density polyethylene.
    [0003]
    3. Polyethylene blend composition according to any one of claims 1 or 2, characterized in that it has a peak at 32.7 ppm measured via 13C NMR, indicating the presence of C3 carbon from C5 branch in the component LDPE.
    [0004]
    4. Polyethylene blend composition according to any one of claims 1 to 3, characterized in that when it is molded into a film via the blown film process, the total turbidity will improve by at least 15 percent over a blown film consisting essentially of a linear low density polyethylene.
    [0005]
    5. Polyethylene blend composition according to any one of claims 1 to 4, characterized in that when it is molded into a film via the blown film process, the gloss will improve by at least 10 percent over a film blown consisting essentially of a linear low density polyethylene.
    [0006]
    6. Blown film, characterized in that it comprises the polyethylene blend composition as defined by claim 1.
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    法律状态:
    2018-03-06| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2018-03-13| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2018-03-20| B06I| Publication of requirement cancelled [chapter 6.9 patent gazette]|Free format text: ANULADA A PUBLICACAO CODIGO 6.6.1 NA RPI NO 2462 DE 13/03/2018 POR TER SIDO INDEVIDA. |
    2020-02-27| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2021-01-05| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2021-06-08| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-08-24| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 22/05/2013, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US201261664318P| true| 2012-06-26|2012-06-26|
    US61/664,318|2012-06-26|
    PCT/US2013/042141|WO2014003926A1|2012-06-26|2013-05-22|A polyethylene blend-composition suitable for blown films, and films made therefrom|
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