High-density linear polyethylene with high tenacity and high resistance to environmental stress cracking (ESCR)

Abstract

An interpolymer product comprising: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 250,000 and a density less than 0.930 g / cm³, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm³; and wherein the interpolymer product comprises an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 90 hours. The interpolymer product can be manufactured in a continuous solution polymerization process using at least two reactors employing at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation.

Description

High-density linear polyethylene with high tenacity and high resistance to environmental stress cracking (ESCR) Field of Invention This description generally relates to an interpolymer product manufactured in a continuous solution polymerization process using at least two reactors employing at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation, as well as methods for manufacturing and using the same. Background of the Invention Rotational molding (rotational molding) involves adding material to a mold in a rotational molding machine, heating and rotating the mold so that the material coats the mold walls, cooling the mold to produce a rotomolded item, and releasing the rotomolded item from the mold. Examples of rotational molding machines include reciprocating machines, chest-type machines, vertical or up-and-over rotary machines, shuttle-type machines, swing-arm machines, and carousel machines. Rotational molding machines come in a wide range of sizes. Examples of rotomolded items include, but are not limited to, toys, wastebaskets, containers, helmets, boats, and large tanks. zoofrnn / zznz / E / YiAi Ref. 332695 Ethylene interpolymer products are widely used in rotomolding applications to produce rotomolded articles. There is a need to improve the Environmental Stress Cracking Resistance (ESCR) of rotomolded articles while maintaining or increasing stiffness and impact properties, for example, low-temperature (-40°C) ARM impact resistance. A person skilled in the art would appreciate that the stiffness of conventional ethylene interpolymers can be increased by increasing the density of the ethylene interpolymer, and that ESCR typically decreases as density increases. Consequently, it may be desirable to provide rotomolded articles that have an improved ESCR while maintaining or increasing stiffness and / or impact properties. Summary of the Invention This description generally describes rotomolded articles that have an improved ESCR while maintaining or increasing stiffness and / or impact properties. An interpolymer product comprising: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) of more than 250,000 and a density of less than 0.930 g / cm³, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw of less than 70,000 and a density greater than 0.930 g / cm³; and wherein the interpolymer product includes an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, 10% IGEPAL® CO-630, of more than 90 hours. The interpolymer product can be manufactured in a continuous solution polymerization process using at least two reactors employing at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation. Brief Description of the Figures The rotomolded articles described in this document can be better understood by considering the following description together with the attached figures; it being understood that this description is not limited to the attached figures. Figure 1 illustrates the IZOD impact strength (ft.lb / in) versus the ambient stress cracking strength (ESCR) (hr) of ethylene interpolymer polymers according to the present description and comparative examples. Figure 2 illustrates the crystallinity at 23°C versus the molecular weight of an ethylene interpolymer polymer according to the data published in the literature by Tung and Buckser Effect of molecular weight on the crystallinity of polyethylene (1958) J. Phys. Chem., vol 62, p.1520. Figure 3 illustrates the molecular weight distribution zoofrnn / zznz / E / YiAi obtained by GPC measurement of an ethylene interpolymer polymer according to the present description (Example 1 described) and the deconvolution results based on multiple Flory molecular weight distribution functions. The first ethylene interpolymer is modeled using a single Flory distribution function. The second ethylene interpolymer is estimated using a four-distribution model. Figure 4 illustrates the molecular weight distribution obtained by GPC measurement of an ethylene interpolymer polymer according to the present description (Example 1) and the deconvolution results based on three idealized Flory molecular weight distribution functions. Figure 5 illustrates the cumulative weight fraction of an ethylene interpolymer polymer according to the present description (Example 1 and Example 2) and comparative examples 1, 2, 5, and 6. Figure 6 illustrates the cumulative weight fraction of an ethylene interpolymer polymer according to the present description (Example 1 and Example 2) and comparative examples 7 and 8. Detailed Description of the Invention This description outlines features, aspects, and advantages of rotomolded articles that include at least one ethylene interpolymer product manufactured in a continuous solution polymerization process using at least two reactors employing at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation. However, it is understood that this description also encompasses numerous alternative features, aspects, and advantages that can be achieved by combining any of the various features, aspects, and / or advantages described herein in any combination or subcombination that a person skilled in the art may find useful. Such combinations or subcombinations are intended to be included within the scope of this description.As such, the claims may be amended to list any feature, aspect, and advantage expressly or inherently described in, or otherwise expressly or inherently supported by, this description. Furthermore, any feature, aspect, and advantage that may be present in the prior art may be affirmatively disclaimed. Accordingly, this description may comprise, consist of, essentially consist of, or be characterized by one or more of the features, aspects, and advantages described herein. All numerical quantities stated herein are approximate unless otherwise stated. Accordingly, the term "approximately" may be inferred where not expressly stated. The numerical quantities described herein should be understood as not being strictly limited to the exact numerical values ​​listed. Instead, unless otherwise stated, each numerical value stated herein is intended to mean both the value stated and a functionally equivalent interval surrounding that value. At a minimum, and not as an attempt to limit the application of the doctrine of equivalents to the scope of the claims, each numerical value should be interpreted at least in light of the number of significant digits reported and by applying ordinary rounding techniques.Despite the approximations of numerical quantities stated in this document, the numerical quantities described in specific examples of actual measured values ​​are reported to the greatest extent possible. Any numerical value, however, inherently contains certain errors that necessarily result from the standard deviation found in its respective test measurements. All numerical intervals established in this document include all subintervals within them. For example, an interval from 1 to 10 or 1-10 is intended to include all subintervals between and including the minimum value of 1 and the maximum value of 10 because the numerical intervals described are continuous and include every value between the minimum and maximum values. Any maximum numerical limit stated in this document is intended to include all lower numerical limits. Any minimum numerical limit stated in this document is intended to include all higher numerical limits. All composition ranges stated herein are limited in total and do not exceed 100 percent (e.g., percent by volume or percent by weight) in practice. Where multiple components may be present in a composition, the sum of the maximum amounts of each component may exceed 100 percent, it being understood, and as will be readily understood by those skilled in the art, that the amounts of the components may be selected to achieve the maximum of 100 percent. The following description provides certain details to enhance understanding of various features, aspects, and advantages of the description. However, a person skilled in the art will understand that these features, aspects, and advantages can be practiced without such details. In other cases, well-known structures, methods, and / or techniques associated with practicing the various features, aspects, and advantages may not be shown or described in detail to avoid unnecessarily obscuring the descriptions of other details of the zoofrnn / zznz / E / YiAi description. Definitions As generally used in this document, the articles the, a and one refer to one or more of what is claimed or described. As generally used in this document, the terms include, includes, and that includes are intended to be non-limiting. As generally used in this document, the terms have, has and that has are not intended to be limiting. As generally used in this document, the term characterized by is not intended to be limiting. As generally used in this document, the term monomer refers to a small molecule that can react chemically and chemically bond with itself or with other monomers to form a polymer. As generally used herein, the term comonomer(s) refers to one or more additional monomers and often includes α-olefins. As generally used in this document, the term α-olefin refers to a monomer having a linear hydrocarbon chain containing 3 to 20 carbon atoms that has a double bond at one end of the chain. As generally used in this document, the term zQOfrnn / zznz / E / YiAi homopolymer refers to a polymer that includes only one type of monomer. As generally used in this document, the term ethylene polymer refers to macromolecules produced from ethylene monomers and, optionally, one or more additional monomers, regardless of the specific catalyst or process used to manufacture the ethylene polymer. Common ethylene polymers include high-density polyethylene (HDPE), medium-density polyethylene (MDPE), linear low-density polyethylene (LLDPE), very low-density polyethylene (VLDPE), ultra-low-density polyethylene (ULDPE), plastomers, and elastomers. Ethylene polymers include polymers produced in high-pressure polymerization processes, such as low-density polyethylene (LDPE), ethylene-vinyl acetate (EVA) copolymers, ethylene-alkyl acrylate copolymers, ethylene-acrylic acid copolymers, and ethylene-acrylic acid metal salts (commonly referred to as ionomers).Ethylene polymers also include block copolymers comprising 2 to 4 comonomers. Ethylene polymers include combinations or blends of the ethylene polymers described herein. As generally used in this document, the term ethylene interpolymer refers to a subset of ethylene polymers that excludes ethylene polymers produced in high-pressure polymerization processes, such as LDPE and EVA, for example. As generally used in this document, the term heterogeneous ethylene interpolymers refers to a subset of ethylene interpolymers produced using a heterogeneous catalyst formulation, such as Ziegler-Natta catalysts and chromium catalysts, for example. As generally used in this document, the term heterogeneous ethylene interpolymers refers to a subset of ethylene interpolymers produced using a heterogeneous catalyst formulation, such as Ziegler-Natta or chromium catalysts, for example. In general, heterogeneous ethylene interpolymers can have larger molecular weight distributions than the molecular weight distributions of homogeneous ethylene interpolymers. As generally used in this document, the term homogeneous ethylene interpolymer refers to a subset of ethylene interpolymers produced using metallocene formulations or single-site catalysts. In general, homogeneous ethylene interpolymers can have narrow molecular weight distributions, for example, gel permeation chromatography (GPC) Mw / Mnde values ​​less than 2.8, and narrow comonomer distributions, i.e., each macromolecule within the molecular weight distribution has a similar comonomer content. Those skilled in the art know that homogeneous ethylene interpolymers can be subdivided into linear homogeneous ethylene interpolymers and substantially linear homogeneous ethylene interpolymers. These two subgroups generally differ in the amount of long-chain branching. More specifically, linear homogeneous ethylene interpolymers have fewer than 0.01 long-chain branches per 1000 carbon atoms, while substantially linear ethylene interpolymers have more than 0.01–3.0 long-chain branches per 1000 carbon atoms. A long-chain branch is macromolecular in nature, meaning it is of a similar length to the macromolecule to which it is attached.As generally used herein, the term homogeneous ethylene interpolymer refers to both linear homogeneous ethylene interpolymers and substantially linear homogeneous ethylene interpolymers. As generally used in this document, the term polyolefin includes ethylene polymers and propylene polymers. Examples of propylene polymers include isotactic, syndiotactic, and atactic propylene homopolymers, random propylene copolymers containing at least one comonomer, and impact polypropylene copolymers or heterophasic polypropylene copolymers. As generally used in this document, the term thermoplastic refers to a polymer that becomes liquid when heated, flows under pressure, and solidifies when cooled. Examples of thermoplastic polymers include ethylene polymers, as well as other polymers commonly used in the plastics industry, such as barrier resins (EVOH), bonding resins, polyethylene terephthalate (PET), and polyamides, for example. As commonly used here, the term monolayer refers to a rotomolded article where the wall structure includes a single layer. As commonly used in this document, the terms hydrocarbyl, hydrocarbyl radical, and hydrocarbyl group refer to linear or cyclic, aliphatic, olefinic, acetylenic, and aryl (aromatic) radicals that include hydrogen and carbon that are deficient in one hydrogen. As generally used in this document, the term alkyl radical refers to linear, branched, and cyclic paraffin radicals that are deficient in a hydrogen radical, such as methyl (-CH3) and ethyl (-CH2CH3) radicals, for example. The term alkenyl radical refers to linear, branched, and cyclic hydrocarbons that have at least one carbon-carbon double bond that is deficient in a hydrogen radical. As generally used in this document, the term R1 and its superscript R1 refer to a first reactor in a continuous solution polymerization process; it being understood that R1 is clearly different from the symbol R1, which may be used in chemical formulas to represent a hydrocarbyl group. Similarly, the term R2 and its superscript R2 refer to a second reactor, and the term R3 and its superscript R3 refer to a third reactor. Catalysts Organometallic catalyst formulations that are effective in the polymerization of defins are well known in the art. In general, at least two catalyst formulations can be employed in a continuous solution polymerization process. The first catalyst formulation is a single-site catalyst formulation that produces a first ethylene interpolymer. The second catalyst formulation is a heterogeneous catalyst formulation that produces a second ethylene interpolymer. Optionally, a third ethylene interpolymer is produced using the heterogeneous catalyst formulation that was used to produce the second ethylene interpolymer, zoofrnn / zznz / E / YiAi, or a different heterogeneous catalyst formulation can be used to produce the third ethylene interpolymer. In the continuous solution process, the catalyst formulations can be mixed in solution to produce an ethylene interpolymer product. Single-site catalyst formulation The catalyst components of a single-site catalyst formulation can include a wide variety of catalyst components. A single-site catalyst formulation may include the following three or four components: (i) a bulky metal-ligand complex; (ii) an alumoxane cocatalyst; (iii) an ion activator; and optionally, (iv) a hindered phenol. As generally used herein: (i) refers to the amount of component (i), i.e., the bulky metal-ligand complex added to R1; (ii) refers to component (ii), i.e., the alumoxane cocatalyst; (iii) refers to component (iii), i.e., the ion activator; and (iv) refers to component (iv), i.e., the optional hindered phenol. The component (i) can be represented by Formula (I): (LA)aM (PI)b(Q)nen where (LA) represents a bulky ligand; M represents a metal atom; PI represents a phosphinimine ligand; Q represents a leaving group; a is 0 or 1; b is 1 or 2; (a+b)=2; n is 1 or 2; and the sum of (a+b+n) is equal to the valency of metal M. The bulky ligand LA in formula (I) may include substituted or unsubstituted cyclopentadienyl ligands or cyclopentadienyl-type ligands, cyclopentadienyl-type ligands substituted with heteroatoms and / or containing heteroatoms. For example, cyclopentaphenanthreneyl ligands, unsubstituted or substituted indenyl ligands, benzidenyl ligands, unsubstituted or substituted fluorenyl ligands, octahydrofluorenyl ligands, cyclooctatetraendiyl ligands, cyclopentacyclododecene ligands, azenyl ligands, azulene ligands, pentalene ligands, phosphoyl ligands, phosphinimine, pyrrolyl ligands, carbazolyl ligands, borbenzene ligands and the like, including hydrogenated versions thereof, for example, tetrahydroindenyl ligands.The bulky ligand LA may include any other ligand structure capable of forming η bonds with metal M, including η3 and η5 bonds with metal M. The bulky ligand LA may include one or more heteroatoms, for example, nitrogen, silicon, boron, germanium, sulfur, and phosphorus, in combination with carbon atoms to form an open, acyclic, or fused ring or ring system, for example, a heterocyclopentadienyl auxiliary ligand. The bulky ligand LA may include bulky amides, phosphides, alkoxides, aryloxides, imides, carbolides, borolides, porphyrins, phthalocyanines, corrins, and other polyazomacrocycles. The metal M in Formula (I) can include Group 4 metals, such as titanium, zirconium, and hafnium, for example. The phosphinimine ligand, PI, can be represented by Formula (II): (Rf)3P=Nen where each of the Rp groups is independently selected from: a hydrogen atom; a halogen atom; a C1-20 hydrocarbyl radical that is unsubstituted or substituted with one or more halogen atoms; a Ci-3 alkoxy radical; a Cg-ium aryl radical; a Ce-ium aryloxy radical; an amido radical; a silyl radical of formula -Si(Rs)3, wherein each of the Rs groups is independently selected from a hydrogen atom, a C1-8 alkyl or alkoxy radical, a Ce-ium aryl radical, a Cg-ium aryloxy radical, or a germanyl radical of formula -Ge(RG)3, wherein each of the RG groups is defined as Rs. The leaving group Q can include any ligand that functions as a leaving group to form a catalyst-like structure capable of polymerizing one or more polymers. As generally used herein, the term leaving group is equivalent to the term activatable ligand. The leaving group Q can include a labile monoanionic ligand that has a sigma bond with M. Depending on the oxidation state of the metal, the value of n is either 1 or 2, so that Formula (I) represents a neutral bulky metal-ligand complex. Examples of ligands Q can include a hydrogen atom, halogens, Ci2O hydrocarbyl radicals, Ci2O alkoxy radicals, and C5-10 aryl oxide radicals. These radicals can be linear, branched or cyclic or further substituted by halogen atoms, Ci-10 alkyl radicals, C1-10 alkoxy radicals, Ce-io aryl radicals or aryloxy radicals.Examples of Q ligands can include weak bases, such as amines, phosphines, ethers, carboxylates, dienes, and hydrocarbyl radicals with 1 to 20 carbon atoms, for example. In another example, two Q ligands can be part of a fused ring or ring system. The first catalyst component (i) of the single-site catalytic formulation may include structural, optical, or enantiomeric isomers (meso and racemic isomers) and mixtures thereof of the bulky ligand-metal complexes described in Formula (I). The second catalyst component (ü) of the single-site catalyst formulation may include an alumoxane cocatalyst that activates component (i) to a cationic complex. An equivalent term for alumoxane is aluminoxane; although the exact structure of this cocatalyst is uncertain, those skilled in the art generally agree that it may be an oligomeric species including repeating units represented by Formula (III): (R)2A1O- (Al (R) -O)n-Al (R)2 where each of the R groups can be the same or different and can include linear, branched, or cyclic hydrocarbyl radicals containing 1-20 carbon atoms and n is from 0-50. An example of alumoxane is methyl aluminoxane (or MAO), where each R group in Formula (III) is a methyl radical. The third catalyst component (iii) for single-site catalyst formation may include an ionic activator. In general, ionic activators include a cation and a bulky anion, the latter being substantially non-coordinating. Examples of ionic activators include four coordinated boron ionic activators, each having four ligands attached to the boron atom. Examples of boron ionic activators can be represented by formula (IV): [R5]+[B(R7)4] where B is a boron atom; R5 includes an aromatic hydrocarbyl, for example, a triphenylmethyl cation; and each R7 is independently selected from phenyl radicals that may be unsubstituted or substituted with 3-5 substituents selected from fluorine atoms, C1-4 alkyl radicals, or alkoxy radicals that are unsubstituted or substituted with fluorine atoms; and a silyl radical represented by the formula -Si(R9)3, where each R9 is independently selected from hydrogen atoms and C1-4 alkyl radicals. Examples of boron ionic activators can be represented by formula (V): [ (R8) tZH1 + [B (R7) 4 ] wherein B is a boron atom; H ​​is a hydrogen atom; Z is a nitrogen or phosphorus atom; t is 2 or 3; and R8 is selected from Ci-8 alkyl radicals, phenyl radicals that are either unsubstituted or substituted with up to three C1-4 alkyl radicals, or an R8 taken together with the nitrogen atom to form an anilinium radical; and R7 is as defined above in Formula (IV). In both Formulas (IV) and (V) , an example of R7is a pentafluorophenyl radical. In general, ionic boron activators can be described as tetra (perfluorophenyl)boron salts, for example, anilinium, carbonium, oxonium, phosphonium, and sulfonium salts of tetra (perfluorophenyl)-boron with anilinium and triphil (or triphenylmethyl). Additional examples of ionic activators may include triethylammonium tetra(phenyl)boron, tripropylammonium tetra(phenyl)boron, tri (n-butyl)ammonium tetra(phenyl)boron, trimethylammonium tetra(p-tolyl)boron, trimethylammonium tetra(o-tolyl)boron, tetra(pentafluorophenyl)boron de tributhylammonium, tetra(o,pdimethylphenyl)tripropylammonium boron, tetra(m,mdimethylphenyl)tributhylammonium boron, tetra(ptrifluoromethylphenyl)tributhylammonium boron, tetra (pentafluorophenyl)tributhylammonium boron, tetra(otolyl)tri(n-butyl)ammonium boron, tetra(phenyl)boron of N,Dimethylanilinium, N,N-diethylanilinium tetra(phenyl)boron, N,N-diethylanilinium tetra(phenyl)n-butylboron,tetra(phenyl)boron of N,N-2,4,6-pentamethylanilinium, tetra(pentafluorophenyl)boron of di-(isopropyl)amonium, tetra(phenyl)boron of dicyclohexylamonium, triphenylphosphonium tetra(phenyl)boron, tri(methylphenyl)phosphonium tetra(phenyl)boron, tetra(phenyl)boron of tri(dimethylphenyl)phosphonium, tetrakispentafluorofenil borate of tropilium, tetrakispentafluorofenil borate of triphenylmethylium, tetrakispentafluorofenil borate of benceno(diazonium), tetrakis(2,3,5,6-tetrafluorofenil)borate of tropilium, tetrakis(2,3,5,6-tetrafluorofenil)borate of triphenylmethylium, tetrakis(3,4),5-trifluorofenil)borate of benceno(diazonium), tropyl tetrakis(3,4,5-trifluorophenyl)borate, tropyl tetrakis(3,4,5-trifluorophenyl)benceno(diazonium)borate, tropyl methyl tetrakis(1,2,2-trifluoroethenyl)borate, triphenylmethyl tetrakis(1,2,2-trifluoroethenyl)borate, zQOfrnn / zznz / E / YiAi tetrakis(1,2,2-trifluoroethenyl)borate de benceno(diazonium), tetrakis(2,3,4,5-tetrafluorophenyl)borate de tropillo, tetrakis(2,3,4,5-tetrafluorophenyl) triphenylmethyl borate and tetrakis(2,3,4,5-tetrafluorophenyl) benzene (diazonium) borate. Commercially available ion activators include N,N-dimethylanilinium tetrakispentafluorophenyl borate and triphenylmethyl tetrakispentafluorophenyl borate. The fourth optional catalyst component (iv) for single-site catalyst formation may include a hindered phenol. Examples of hindered phenols may include butylated phenolic antioxidants, butylated hydroxytoluene, 2,4-di-tert-butyl-6-ethylphenol, 4,4'-methylenebis(2,6-di-tert-butylphenol), 1,3,5-trimethyl-2,4,6-tris(3,5-di-tert-butyl-4-hydroxybenzyl)benzene, and octadecyl-3(3',5'-di-tert-butyl-4'-hydroxyphenyl)propionate. To produce a single-active-site catalyst formulation, the quantity and molar ratios of each of the three (i)-(iii) or four (i)-(iv) components can be optimized as described below. Heterogeneous Catalyst Formulations Experts in the technique are well acquainted with various heterogeneous catalyst formulations, including Ziegler-Natta catalysts and chromium catalyst formulations, for example. zoofrnn / zznz / E / YiAi Ziegler-Natta catalysts may include one or more online and batch Ziegler-Natta catalyst formulations. As generally used herein, the term online Ziegler-Natta catalyst formulation refers to the continuous synthesis of a small quantity of active Ziegler-Natta catalyst and the immediate injection of this catalyst into at least one continuously operating reactor, where the catalyst polymerizes ethylene and one or more optional α-olefins to form an ethylene interpolymer. As generally used herein, the terms batch Ziegler-Natta catalyst formulation and batch Ziegler-Natta procatalyst refer to the synthesis of a much larger quantity of catalyst or procatalyst in one or more mixing vessels that are external to, or isolated from, the continuously operating solution polymerization process.Once prepared, the batch Ziegler-Natta catalyst formulation, or the batch Ziegler-Natta procatalyst, can be transferred to a catalyst storage tank. As generally used herein, the term procatalyst refers to an inactive catalyst formulation (inactive with respect to the polymerization of ethylene); the procatalyst can be converted into an active catalyst by adding an alkylaluminum cocatalyst. When desired, the procatalyst can be pumped from the storage tank to at least one continuously operating reactor, where it can be converted into an active catalyst to polymerize ethylene and one or more optional α-olefins to form an ethylene interpolymer. The procatalyst can be converted into an active catalyst either in the reactor or outside of it. A variety of chemical compounds can be used to synthesize, or combined with other chemical compounds to produce, an active formulation of Ziegler-Natta catalyst. Those skilled in the art will understand that the examples described herein are not limited to the specific chemical compounds listed. An active Ziegler-Natta catalyst formulation can be formed from: a magnesium compound, a chloride compound, a metal compound, an alkylaluminum cocatalyst, and an alkylaluminum. As commonly used herein, the magnesium compound may be referred to as component (v) or (v); the chloride compound may be referred to as component (vi) or (vi); the metal compound may be referred to as component (vil) or (vii); the alkylaluminum cocatalyst may be referred to as component (viii) or (viii); and the alkylaluminum may be referred to as component (ix) or (ix). As those skilled in the art will appreciate, Ziegler-Natta catalyst formulations may include additional components, such as an electron donor, for example, amines or ethers. An active formulation of an online Ziegler-Natta catalyst can be prepared as follows. In the first step, a solution of a magnesium compound (component (v)) can be reacted with a solution of the chloride compound (component (vi)) to form a magnesium chloride support suspended in solution. Examples of magnesium compounds include Mg(R1)2, where the R1 groups can be identical or different linear, branched, or cyclic hydrocarbyl radicals containing 1–10 carbon atoms. Examples of chloride compounds include R2C1, where R2 represents a hydrogen atom, or a linear, branched, or cyclic hydrocarbyl radical containing 1–10 carbon atoms. In the first step, the magnesium compound solution can also contain an aluminum alkyl (component (ix)).Examples of alkyl aluminum include Al(R3)3, where the R3 groups can be identical or different linear, branched, or cyclic hydrocarbyl radicals containing 1 to 10 carbon atoms. In the second step, a solution of the metal compound (vile component) can be added to the magnesium chloride solution, and the metal compound can be supported on the magnesium chloride. Examples of suitable metal compounds include M(X)n and MO(X)n, where M represents a metal selected from Group 4 through Group 8 of the Table. Periodic, or mixtures of selected metals from Group 4 to Group 8; O represents oxygen; and X represents chloride or bromide; n is an integer from 3 to 6 that satisfies the oxidation state of the metal. Examples of suitable metal compounds include metal alkyls from Group 4 to Group 8, metal alkoxides (which can be prepared by reacting a metal alkyl with an alcohol), and mixed-ligand metal compounds containing a mixture of halide, alkyl, and alkoxide ligands. In the third step, a solution of an alkylaluminum cocatalyst (component (viii)) can be added to the metal compound supported on magnesium chloride. A wide variety of alkylaluminum cocatalysts are suitable, as expressed in Formula (VI): Al(R4)p(OR5)q(X)r, wherein the R4 groups can be identical or different hydrocarbyl groups having from 1 to 10 carbon atoms; the OR5 groups can be identical or different alkoxy or aryloxy groups, wherein R5 is a hydrocarbyl group having from 1 to 10 carbon atoms bonded to oxygen; X is chloride or bromide, and; (p+q+r)=3, with the condition that p is greater than 0. Examples of alkylaluminum cocatalysts include trimethylaluminum, triethylaluminum, tributylaluminum, dimethylaluminum methoxide, diethylaluminum ethoxide, dibutylaluminum butoxide, dimethylaluminum chloride or aluminum bromide, diethylaluminum chloride or bromide, dibutylaluminum chloride or bromide, and ethylaluminum dichloride or dibromide. The process described in the preceding paragraph for synthesizing an active Ziegler-Natta catalyst formulation online can be carried out in a variety of solvents; non-limiting examples of solvents include linear or branched C5-12 alkanes or mixtures thereof. To produce an active Ziegler-Natta catalyst formulation online, the amounts and molar ratios of the five components, (v) through (ix), can be optimized as described below. Additional forms of heterogeneous catalyst formulations include those in which the metal compound may include a chromium compound, such as silyl chromate, chromium oxide, and chromocene, for example. The chromium compound may be supported on a metal oxide, such as silica or alumina. Heterogeneous catalyst formulations containing chromium may also include cocatalysts, such as trialkylaluminum, alkylaluminoxane, and dialkoxyalkylaluminum compounds, for example. Polymerization process Ethylene interpolymer products can be manufactured using conventional blending systems and processes, including physical blending and in-situ blending via polymerization in multi-reactor systems. For example, the first ethylene interpolymer can be blended with the second ethylene interpolymer by melt blending of the two preformed polymers. In another example, the first, second, and third ethylene interpolymers can be prepared in sequential polymerization steps. Ethylene interpolymer products can be manufactured using both series and parallel reactor processes. Gas-phase reactor systems, suspension-phase reactor systems, and solution-phase reactor systems can all be used. For example, the ethylene interpolymer product can be prepared using solution-phase reaction systems. The ethylene interpolymer products described herein can be produced in a continuous solution polymerization process as described in U.S. Patent No. 8,101,693, issued January 24, 2012, and Canadian Patent Application No. 2,868,640, filed October 21, 2014. A dual-reactor solution process that can be used to produce the ethylene interpolymer products is described in U.S. Patent No. 6,372,864 and the Publication of Application No. US Patent No. 20060247373A1. The continuous solution polymerization process may include a reactor system comprising at least two continuously stirred reactors, R1 and R2, and an optional tubular reactor, R3. The feeds (e.g., solvent, ethylene, at least two catalyst formulations, optional hydrogen, and optional α-olefin) may be continuously fed to the at least two reactors. A single-site catalyst formulation may be injected into R1, and a first heterogeneous catalyst formulation may be injected into R2 and, optionally, into R3. Optionally, a second heterogeneous catalyst formulation may be injected into R3. The single-site catalyst formulation comprises an ionic activator (component (iii)), a bulky metal-ligand complex (component (i)), an alumoxane cocatalyst (component (ii)), and an optional hindered phenol (component (iv)), respectively. The residence time in each reactor may depend on the reactor system design and capacity. The reactors can be operated under conditions that ensure complete mixing of the reactants. Reactors R1 and R2 can operate in series or parallel mode. In series mode, 100% of the effluent from reactor R1 flows directly to reactor R2. In parallel mode, reactors R1 and R2 operate independently, and the effluents from each reactor can be combined downstream of reactors R1 and R2. A heterogeneous catalyst formulation is injected into R2. A first online Ziegler-Natta catalyst formulation can be injected into R2. A first online Ziegler-Natta catalyst formation can be formed within a first heterogeneous catalyst assembly by optimizing one or more of the following molar ratios: (alkylaluminum) / (magnesium compound) or (ix) / (v); (chloride compound) / (magnesium compound) or (vi) / (v); (alkylaluminum cocatalyst) / (metal compound) or (viii) / (vii); and (alkylaluminum) / (metal compound) or (ix) / (vii); as well as the time these compounds have to react and equilibrate. Within the first heterogeneous catalyst assembly, the first retention time (HUT-1) between the addition of the chloride compound and the addition of the metal compound (component (vii)) can be controlled.The second retention time (HUT-2) between the addition of component (vii) and the addition of the alkylaluminum cocatalyst, component (viii), can also be controlled. Furthermore, the third retention time (HUT-3) between the addition of the alkylaluminum cocatalyst and the injection of the Ziegler-Natta catalyst formulation inline into R2 can be controlled. Optionally, 100% of the alkylaluminum cocatalyst can be injected directly into R2. Optionally, a portion of the alkylaluminum cocatalyst can be injected into the first heterogeneous catalyst assembly, and the remaining portion can be injected directly into R2. The amount of in-line heterogeneous catalyst formulation added to R2 can be expressed as parts per million (ppm) of metal compound (component (vii)) in the reactor solution (R2 (vii) (ppm)). Injection of the in-line heterogeneous catalyst formulation into R2 can produce a second ethylene interpolymer in a second outlet stream (exiting R2). Optionally, the second outlet stream can be deactivated by adding a catalyst deactivator. When the second outlet stream is not deactivated, it enters reactor R3, which may include a tubular reactor.Optionally, one or more of the following fresh feeds can be injected into R3: solvent, ethylene, hydrogen, α-olefin, and a first or second heterogeneous catalyst formulation; the latter can be supplied from a second heterogeneous catalyst assembly. The chemical composition of the first and second heterogeneous catalyst formulations can be the same or different; that is, the catalyst components ((v) to (ix)), molar ratios, and retention times can differ in the first and second heterogeneous catalyst assemblies zoofrnn / zznz / E / YiAi. The second heterogeneous catalyst assembly can generate an efficient catalyst by optimizing the holding times and molar ratios of the catalyst components. An additional ethylene interpolymer may or may not be produced in the tubular reactor R3. A third ethylene interpolymer may not be produced when a catalyst deactivator is added upstream of the tubular reactor R3. A third ethylene interpolymer may be produced when a catalyst deactivator is added downstream of the tubular reactor R3. The optional third ethylene interpolymer can be produced using a variety of operating modes (provided that no catalyst deactivator is added upstream).Examples of operating modes for the tubular reactor R3 may include: (a) supplying waste ethylene, optional waste α-olefin, and waste active catalyst to the tubular reactor R3 to produce the third ethylene interpolymer; (b) supplying fresh process solvent, fresh ethylene, and optionally fresh α-olefin to the tubular reactor R3 and supplying the waste active catalyst to the tubular reactor R3 to produce the third ethylene interpolymer; (c) supplying a second in-line heterogeneous catalyst formulation to the tubular reactor R3 to polymerize the waste ethylene and optional waste α-olefin to produce the third ethylene interpolymer; or (d) supplying fresh process solvent, fresh ethylene, optionally fresh α-olefin, and a second in-line heterogeneous catalyst formulation to R3 to produce an additional ethylene interpolymer. In series mode, R3 produces a third output stream (the stream leaving R3) containing the first ethylene interpolymer, the second ethylene interpolymer, and optionally, a third ethylene interpolymer. A catalyst deactivator can be added to the third output stream to produce a deactivated solution; however, if a catalyst deactivator was added upstream of R3, no catalyst deactivator should be added. The deactivated solution can be passed through a pressure-reducing device and / or a heat exchanger and / or contacted with a passivator to produce a passivated solution. The passivated solution can then be passed through a series of vapor-liquid separators. The ethylene interpolymer can be recovered by one or more polymer recovery operations, such as vapor-liquid separators, a gear pump, a single-screw extruder, and a twin-screw extruder, to force the molten ethylene interpolymer product through a pelletizer. zQOfrnn / zznz / E / YiAi Ethylene interpolymer products can be manufactured using conventional equipment and methods, such as dry-mixing the individual components and subsequently melt-mixing them in a mixer, or mixing the components directly in a mixer, such as a single-screw or twin-screw extruder, which may include a compounding extruder. The ethylene interpolymer product may include one or more additional polymer components besides the first, second, and / or third ethylene interpolymer. These additional polymer components may include polymers manufactured in situ and / or polymers added during the extrusion or compounding step. Optionally, the ethylene interpolymer product may include at least one additive. The additive may be added during an extrusion or compounding step, for example. Additives may also be added to the polymer solution either before the vapor-liquid separators or at some point along the vapor-liquid separation vessels. The additive may be added as is or as part of a separate polymer component (i.e., not as part of the first, second, or third ethylene interpolymers) added during an extrusion or compounding step.Suitable additives are known in the art and may include, but are not limited to, antioxidants, phosphites and phosphonites, nitrones, antacids, UV light stabilizers, UV absorbers, metal deactivators, colorants, fillers and reinforcing agents, nanoscale organic or inorganic materials, antistatic agents, release agents such as zinc stearates, and nucleating agents (including nucleators, pigments, or any other chemical that can provide a nucleating effect to the polyethylene composition). Additives may include up to 20 percent by weight (wt%) of the ethylene interpolymer product. The manufactured articles described herein can also be formed from ethylene interpolymer products synthesized using a batch Ziegler-Natta catalyst. Typically, a first batch of Ziegler-Natta procatalyst is injected into R2, and the procatalyst is activated within R2 by the injection of an alkylaluminum cocatalyst, forming a first batch of Ziegler-Natta catalyst. Optionally, a second batch of Ziegler-Natta procatalyst is injected into R3. Additional Parameters of the Solution Polymerization Process A variety of solvents can be used as the process solvent, such as linear, branched, or cyclic C5 to C12 alkanes, for example. Examples of α-olefins include C3 to C12 α-olefins. It is well known to those skilled in the art that reactor feed streams (e.g., solvent, monomer, α-olefin, hydrogen, catalyst formulation) must be essentially free of catalyst-deactivating poisons, such as trace amounts of oxygenated compounds like water, fatty acids, alcohols, ketones, and aldehydes, for example. Poisons can be removed from reactor feed streams using standard purification practices, such as molecular sieve beds, alumina beds, and oxygen-scavenging catalysts for the purification of solvents, ethylene, and α-olefins, for example. In continuous polymerization processes, the total amount of ethylene supplied to each reactor system can be divided among one or more of the reactors R1, R2, and R3. This operating variable can be called Ethylene Division (ES), where ESR1, ESR2, and ESR3 refer to the weight percentage of ethylene injected into each of the reactors R1, R2, and R3, respectively, with the condition that ESR1 + ESR2 + ESR3 = 100%. The ethylene concentration in each reactor can also be controlled. The ethylene concentration in reactor R1 can be defined as the weight of ethylene in reactor R1 divided by the total weight of everything added to reactor R1; the ethylene concentration of reactor R2 (weight percent) and the ethylene concentration of reactor R3 (weight percent) can be defined similarly. The total amount of ethylene converted in each reactor can also be controlled.The term QR1 refers to the percentage of ethylene added to reactor R1 that can be converted into an ethylene interpolymer by the catalyst formulation. Similarly, QR2 and QR3 represent the percentage of ethylene added to each of reactors R2 and R3 that can be converted into an ethylene interpolymer, respectively. The term QT ​​represents the total or overall ethylene conversion across the entire continuous solution polymerization plant; that is, QT = 100 x [weight of ethylene in the interpolymer product] / ([weight of ethylene in the interpolymer product] + [weight of unreacted ethylene]). Optionally, α-olefin can be added to the continuous solution polymerization process. When added, the α-olefin can be dosed or divided among each of reactors R1, R2, and R3.This operating variable can be called split comonomer (CS), i.e., CSR1, CSR2 and CSR3 refer to the weight percentage of aolefin comonomer that can be injected into each of the reactors R1, R2, and R3, respectively; with the condition that CSR1+CSR2+CSR3=100%. In continuous polymerization processes, polymerization can be terminated by adding a catalyst deactivator. The catalyst deactivator substantially stops the polymerization reaction by changing the active species of the catalyst to inactive forms. Suitable deactivators are well known in the art and may include: amines (e.g., those described in U.S. Patent No. 4,803,259); alkali or alkaline earth metal salts of carboxylic acids (e.g., those described in U.S. Patent No. 4,105,609); water (e.g., those described in U.S. Patent No. 4,731,438); hydrotalcites, alcohols, and carboxylic acids (e.g., those described in U.S. Patent No. 4,379,882); or a combination thereof (e.g., as described in U.S. Patent No. 6,180,730). Before entering the vapor / liquid separator, a passivator or acid scavenger can be added to the deactivated solution. Suitable passivators are well known in the art and may include alkali or alkaline earth metal salts of carboxylic acids or hydrotalcites. In general, the number of solution reactors may not be particularly important; provided that the continuous solution polymerization process includes at least two reactors employing at least one single-site catalyst formulation. As previously stated, the interpolymer can be produced in a process using at least two continuously stirred reactors in series followed by a tubular reactor. Consequently, the gel permeation chromatograph (GPC) of the interpolymer can be mathematically deconvolved into three components. First Ethylene Interpolymer The first ethylene interpolymer can be produced with a single-site catalyst formulation. When the optional aolefin is not added to reactor R1, the ethylene interpolymer produced in reactor R1 is an ethylene homopolymer. When an α-olefin is added to reactor R1, the following weight ratio can be used to control the density of the first ethylene interpolymer: ((α-olefin) / (ethylene))R1. The symbol σ1 refers to the density of the first ethylene interpolymer produced in reactor R1. The upper limit of σ1 can be 0.93 g / cm³ or 0.923 g / cm³. The lower limit of σ1 can be 0.90 g / cm³ or 0.910 g / cm³. Methods for determining the CDBI5q (composition distribution branching index) of an ethylene interpolymer are well known to those skilled in the art. The CDBI50, expressed as a percentage, is defined as the percentage of the ethylene interpolymer whose comonomer composition is within 50% of the median comonomer composition. It is also well known that the CDBI50 of ethylene interpolymers produced with single-site catalyst formulations is higher than the CDBI50 of aolefin-containing ethylene interpolymers produced with heterogeneous catalyst formulations. The upper limit of the CDBI5q of the first ethylene interpolymer (produced with a single-site catalyst formulation) can be 98%, 95%, or 90%. The lower limit of the CDBI50 of the first ethylene interpolymer can be 70%, 75%, or 80%. As is well known to those skilled in the art, the polydispersity (Mw / Mn) of ethylene interpolymers produced with single-site catalyst formulations is lower compared to ethylene interpolymers produced with heterogeneous catalyst formulations. The upper limit of the polydispersity (Mw / Mn) of the first ethylene interpolymer can be 3 or 2.25. The lower limit of the polydispersity (Mw / Mn) of the first ethylene interpolymer can be 1 or 1.75. The first ethylene interpolymer may include catalyst residues that reflect the chemical composition of the single-site catalyst formulation used. Those skilled in the art may understand that the catalyst residues can be quantified in parts per million of metal in the first ethylene interpolymer, where "metal" refers to the metal in component (i), i.e., the metal in the bulk ligand-metal complex, which may be referred to as metal A. Examples of metal A may include Group 4 metals, such as titanium, zirconium, and hafnium. The upper ppm limit of metal A in the first ethylene interpolymer may be 1.0 ppm, 0.9 ppm, or 0.8 ppm. The lower ppm limit of metal A in the first ethylene interpolymer may be 0.01 ppm, 0.1 ppm, or 0.2 ppm. The amount of hydrogen added to each of the R1 reactors can vary over a wide range, allowing the continuous solution process to produce first ethylene interpolymers that differ greatly in melt index, hereafter I21 (the melt index is measured at 190°C using a 2.16 kg charge following the procedures described in ASTM D1238). The amount of hydrogen added to reactor R1 (H2R1(ppm)) can be expressed as parts per million (ppm) of hydrogen in R1 relative to the total mass in reactor R1. The upper limit of H2R1(ppm) can be 100 ppm, and the lower limit of H2R1(ppm) can be 0 or greater than zero. Similarly, the upper and lower limits of H2R1(ppm) for reactors R2 and / or R3 can be independently equal to or different from the upper and lower limits of H2R1(ppm) for reactor R1.Without wishing to be linked to any particular theory, the upper limit zQOfrnn / zznz / E / YiAi of hydrogen added to each of the R1 reactors may depend on the pump capacity, the catalyst type, the catalyst concentration, the comonomer content, and the reactor temperature. The upper limit of the melting index (I21) can be 0.01 g / 10 min or 0.008 g / 10 min. The lower limit of the melting index (I21) can be 0.0001 g / 10 min or 0.001 g / 10 min. Without adhering to any particular theory, hydrogen can be used as a transfer agent. The molecular weight can decrease (and the melting rate can increase) when the amount of hydrogen fed to the reactor increases. As discussed earlier, the amount of hydrogen added to each of the R1 reactors for a particular melting rate can depend on the catalyst type, catalyst concentration, comonomer content, and reactor temperature. The upper limit of the weight percent (wt%) of the first ethylene interpolymer in the ethylene interpolymer product may be 40 wt%, 30 wt%, 25 wt%, or 22 wt%. The lower limit of the weight percent of the first ethylene interpolymer in the ethylene interpolymer product may be 10 wt%, 15 wt%, or 18 wt%. Second ethylene interpolymer The second ethylene interpolymer can be produced with a heterogeneous catalyst formulation. When no optional α-olefin is added to reactor R2, either by adding new α-olefin to reactor R2 or by transferring it from reactor R1, the ethylene interpolymer produced in R2 may include an ethylene homopolymer. When an optional α-olefin is present in reactor R2, the following weight ratio can be used to control the density of the second ethylene interpolymer produced in reactor R2: ((α-olefin) / (ethylene))R2. Hereafter, the symbol o2 refers to the density of the ethylene interpolymer produced in reactor R2. The upper limit of o2 can be 0.98 g / cm³ or 0.96 g / cm³. The lower limit of o2 can be 0.93 g / cm³ or 0.95 g / cm³. When the second ethylene interpolymer contains an α-olefin, the CDBI5q of the second ethylene interpolymer is lower relative to the CDBI50 of the first ethylene interpolymer produced with a single-site catalyst formulation. For example, the upper limit of the CDBI5q of the second ethylene interpolymer (containing an α-olefin) might be 70%, 65%, or 60%. The lower limit of the CDBI50 of the second ethylene interpolymer (containing an α-olefin) might be 45%, 50%, or 55%. When an α-olefin is not added to the continuous solution polymerization process, the second ethylene interpolymer is an ethylene homopolymer. In the case of a homopolymer, which does not contain an α-olefin, a CDBI50 can still be measured using TREF.It is well known to those skilled in the art that as the α-olefin content in the second ethylene interpolymer approaches zero, there is a smooth transition between the CDBI50 limits listed for second ethylene interpolymers (containing an aolefin) and the CDBI50 limits listed for second ethylene interpolymers that are ethylene homopolymers. Typically, the CDBI50 of the first ethylene interpolymer is higher than the CDBI50 of the second ethylene interpolymer. The polydispersity (Mw / Mn) of the second ethylene interpolymer may be greater than the Mw / Mn of the first ethylene interpolymer. The upper limit of the polydispersity (Mw / Mn) of the second ethylene interpolymer may be 4.0 or 2.9. The lower limit of the polydispersity (Mw / Mn) of the second ethylene interpolymer may be 2.0 or 2.5. The second ethylene interpolymer may include catalyst residues that reflect the chemical composition of the heterogeneous catalyst formulation used. Those skilled in the art will understand that heterogeneous catalyst residues are normally quantified by the parts per million of metal in the second ethylene interpolymer, where "metal" refers to the metal originating from component (vii), i.e., the metal compound, which may be referred to as metal B. Examples of metal B include metals selected from Groups 4 through 8 of the Periodic Table, or mixtures of metals selected from Groups 4 through 8. Each of the upper and lower ppm limits for metal B in the second ethylene interpolymer may be described in U.S. Patent No. 9,512,282.While we do not wish to limit ourselves to any particular theory, in series operation mode it is believed that the chemical environment within the second reactor deactivates the single-site catalyst formulation, or in parallel operation mode, the chemical environment within R2 deactivates the single-site catalyst formation. The amount of hydrogen added to reactor R2 can vary over a wide range, allowing the continuous solution process to produce second ethylene interpolymers that differ greatly in melt index, hereafter referred to as I22. The amount of hydrogen added can be expressed as parts per million (ppm) of hydrogen in reactor R2 relative to the total mass in reactor R2; hereafter referred to as H2R2(ppm). The upper limit of H2R2(ppm) can be 100 ppm, and the lower limit of H2R2(ppm) can be 0 or greater than zero. As discussed earlier with respect to H2R1, without wishing to be limited to any particular theory, the upper limit of hydrogen added to each of the R2 reactors can depend on the pump capacity, the type of catalyst, the catalyst concentration, the comonomer content, and the reactor temperature at a particular melt index. The upper limit of the melting index (I22) can be 25 g / 10 min or 22 g / 10 min. The lower limit of the melting index (I22) can be 5 g / 10 min or 10 g / 10 min. The upper limit of the weight percent (wt%) of the second ethylene interpolymer in the ethylene interpolymer product may be 90 wt%, 85 wt%, or 82 wt%. The lower limit of the wt% of the second ethylene interpolymer in the ethylene interpolymer product may be 70 wt%, 75 wt%, or 78 wt%. Ethylene interpolymer product The upper limit of the density of the ethylene interpolymer product can be 0.97 g / cm3, 0.965 g / cm3 or 0.954 g / cm3. The lower limit of the density of the ethylene interpolymer product suitable for rotomolded articles can be 0.94 g / cm3, 0.945 g / cm3 or 0.950 g / cm3. The upper CDBI50 limit for an ethylene interpolymer product may be 90%. The lower CDBI50 limit for an ethylene interpolymer may be 70%. The polydispersity (Mw / Mn) of the ethylene interpolymer product can be 3-6. The upper limit of Mw / Mn of the ethylene interpolymer product can be 6, 5 or 4.7. The lower limit of Mw / Mn of the ethylene interpolymer product can be 3, 4 or 4.4. The catalyst residues in the ethylene interpolymer product reflect the chemical compositions of the single-site catalyst formulation used in R1 and the heterogeneous catalyst formulation used in R2. These residues can be quantified by measuring the parts per million (ppm) of catalytic metal in the ethylene interpolymer products. Additionally, the elemental amounts (ppm) of magnesium, chlorine, and aluminum can be quantified. The catalytic metals can originate from two sources: (a) metal A originating from reactor R2; and (b) metal B originating from reactor R2.As generally used in this document, the term total catalyst metal means the sum of the catalytic metals A+B, and the terms first total catalyst metal and second total catalyst metal refer to the first ethylene interpolymer product and a comparative polyethylene composition that can be produced using different catalyst formulations, respectively. The upper limit of the melting rate of the ethylene interpolymer product may be greater than 0.5 g / 10 min or from 0.5 to 8 g / 10 min. The lower limit of the melting rate of the ethylene interpolymer product may be 0.5 g / 10 min or 0.8 g / 10 min. zQOfrnn / zznz / E / YiAi The upper limit of the melt flow ratio (I21 / I2) of the ethylene interpolymer product can be 60 or 70. The lower limit of the melt flow ratio (T21 / T2) of the ethylene interpolymer product can be 30 or 35. The upper limit of the ESCR for the ethylene interpolymer product may be greater than 90 hours or 500 hours. The lower limit of the ESCR for the ethylene interpolymer product may be 90 hours. The upper limit of the IZOD of the ethylene interpolymer product may be greater than 0.13 mkg / cm (2.5 ft.lb / in) or 0.54 m-kg / cm (10 ft.lb / in). The lower limit of the IZOD of the ethylene interpolymer product may be 0.13 mkg / cm (2.5 ft.lb / in). Examples Testing methods Prior to testing, each sample was conditioned for at least 24 hours at 23 ± 2 °C and 50 ± 10% relative humidity. Testing was performed at 23 ± 2 °C and 50 ± 10% relative humidity. As generally used in this document, the term ASTM conditions refers to a laboratory maintained at 23 ± 2 °C and 50 ± 10% relative humidity. ASTM refers to the American Society for Testing and Materials. Materials. The molded plates from the polyethylene compositions were tested according to the following ASTM methods: Environmental Stress Cracking Resistance (ESCR) of bent strip in condition B in 10% IGEPAL at 50°C, ASTM D1693; Noted IZOD impact properties, ASTM D 256; Flexural properties, ASTM D 790; Tensile properties, ASTM D 638. Density The densities of the ethylene interpolymer products were determined using ASTM D792-13 (November 1, 2013). fusion index The melting index of the ethylene interpolymer product was determined using ASTM D1238 (August 1, 2013). The melting indices, I2, l1, and θI21, were measured at 190°C using weights of 2.16 kg, 6.48 kg, 10 kg, and 21.6 kg, respectively. As generally used in this document, the term strain exponent, or its acronym S.Ex., is defined by the following relationship: S . Ex . = (I6 / I2) / log (6480 / 2160) where Iβ and I2 are the melting rates measured at 190°C using loads of 6.48 kg and 2.16 kg, respectively. In this description, the melting index was expressed using the units of g / 10 min or dg / min; these units are equivalent. Environmental stress cracking resistance (ESCR) The ESCR of the ethylene interpolymer product was determined in accordance with ASTM D1693-13 (November 1, 2013). Both ESCR conditions A and B were used. In Condition A, the sample thickness was within the range of 3.00–3.30 mm (0.120–0.130 in) and the notch depth was within the range of 0.50–0.65 mm (0.020–0.025 in). Condition A was carried out using 100% IGEPAL CO-630 (nonylphenoxypolyoxyethylene nonylphenyl ether). In Condition B, the sample thickness was within the range of 1.841.97 mm (0.0725–0.0775 in) and the notch depth was within the range of 0.30–0.40 mm (0.012–0.015 in). The Condition B experiments were performed using either 100% IGEPAL CO-630 or a 10% solution of IGEPAL CO-630 in water. Gel permeation chromatography (GPC) The molecular weights of the ethylene interpolymer product, Mn, Mwy, Mz (g / mol), as well as the polydispersity (Mw / Mn), were determined by high-temperature gel permeation chromatography (GPC) with differential refractive index (DRI) detection using universal calibration (e.g., ASTM-D6474-99). GPC data were obtained using a Waters zQOfrnn / zznz / E / YiAi model 150 gel permeation chromatography (GPC) apparatus equipped with a differential refractive index detector with 1,2,4-trichlorobenzene as the mobile phase at 140°C. Samples were prepared by dissolving the polymer in this solvent and processed without filtration. Molecular weights are expressed as polyethylene equivalents with a relative standard deviation of 2.9% for number-average molecular weight (Mn) and 5.0% for weight-average molecular weight (Mw). The molecular weight distribution (MWD) is weight-average molecular weight divided by number-average molecular weight, Mw / Mn. The z-weight distribution is Mz / Mn. Sample solutions of ethylene interpolymer product (1–2 mg / ml) were prepared by heating the interpolymer in 1,2,4-trichlorobenzene (TCB) and rotating a wheel for 4 hours at 150°C in an oven. The antioxidant 2,6-di-tert-butyl-1,4-methylphenol (BHT) was added to the mixture to stabilize the polymer against oxidative degradation. The BHT concentration was 250 ppm. The sample solutions were subjected to chromatography at 140°C in a PL 220 high-temperature chromatography unit equipped with four Shodex columns (HT803, HT804, HT805, and HT806) using TCB as the mobile phase at a flow rate of 1.0 ml / min, with a differential refractive index (DRI) detector. BHT was added to the mobile phase at a concentration of 250 ppm to protect the columns from oxidative degradation. The sample injection volume was 200 microliters. Raw GPC data were processed using CIRRUS GPC software.The GPC columns were calibrated using narrow-distribution polystyrene standards. The molecular weights of polystyrene were converted to molecular weights of polyethylene using the Mark-Houwink equation, as described in ASTM D6474 standard test method. GPC-FTIR was used to determine comonomer content as a function of molecular weight. After polymer separation by GPC, an online FTIR measured the polymer concentration and the methyl end groups. The methyl end groups were used in branching frequency calculations. Conventional calibration allowed for the calculation of a molecular weight distribution. Mathematical deconvolutions were performed to determine the relative polymer quantity, molecular weight, and comonomer content of the component produced in each reactor. Estimates were first obtained from predictions derived using fundamental kinetic models as described in U.S. Patent No. 9,695,309 (with specific kinetic constants for each catalyst formulation), as well as the feed and reactor conditions. The simulation was based on the solution pilot plant configuration described below, which was used to produce the ethylene interpolymer product examples described herein. The kinetic model predictions were used to establish estimates of the short-chain branching distribution between the first and second interpolymer components.In some cases indicated in Table 2, the fit between the simulated molecular weight distribution profile and the data obtained from GPC chromatography was improved by modeling the molecular weight distribution as a sum of components having molecular weight distributions described using multi-site idealized Flory distributions. During deconvolution, the total Mn, Mwy, and Mz are calculated using the following relationships: Mn = 1 / Σ (wi / (Mn) i) , Mw = Σ (wi x (Mw)i), Mz = Σ (wi x (Mz)i2 / ^(wi x (Mzi) ), where i represents the i-th component and wz represents the relative weight fraction of the i-th component in the composition. The following equations were used to calculate the densities and the I2 fusion index: px- 0.978863 - 5.94808 x 10“3(----) - 3.83133 x 10-'[log10(M„ )]35.77986 x 10'6+ 5.57395 x 10“3Equation (1) ^ = (^-^^) / ^2 Equation (2) logI0[fusion index I2) = 7.900 — 3.909 [logie— 0.2799 f—}Equation (3) where Mn, Mw, Mzy SCB / 1000C are the deconvoluted values ​​of the individual components of the ethylene polymer, obtained from the results of the deconvolution described above, while p is the density of the overall ethylene copolymer composition and is determined experimentally. Equations (1) and (2) were used to estimate pl and p2, the densities of the first and second ethylene copolymers, respectively. Equation (3) was used to estimate the melting index I2. See Duncan E. Thompson, Kim B. McAuley, and P. James McLellan. Exploring reaction kinetics of a multi-site Ziegler-Natta catalyst using deconvolution of molecular weight distributions for ethylene-hexene copolymers. Macromolecular Reaction Engineering, 1(2):264-274, 2007. doi:10.1002 / mren.200600028; Duncan E. Thompson, Kim B. McAuley, and P. James McLellan.A simplified model for prediction of molecular weight distributions in ethylene-hexene copolymerization using Ziegler-Natta catalysts. Macromolecular Reaction Engineering, 1(5):523-536, 2007. doi:10.1002 / mren.200700018 ; Alfred Rudin, The elements of polymer Science and engineering, 2nd edition, Academic Press, 1999. Ver también la Patente Estadounidense No. 8,022,143. zQOfrnn / zznz / E / YiAi Contenido de insaturación The number of unsaturated groups, i.e., double bonds, in an ethylene interpolymer product was determined according to ASTM standards D3124-98 (vinylidene unsaturation, published March 2011) and ASTM D6248-98 (vinyl and trans unsaturation, published July 2012). An ethylene interpolymer sample was: a) first subjected to carbon disulfide extraction to remove additives that may interfere with the analysis; b) the sample (in pellet, film, or granular form) pressed onto a plate of uniform thickness (0.5 mm); and c) the plate was analyzed by FTIR. Short String Branching Frequency (SCBF) The short-chain branching frequency (SCB per 1000 carbon atoms) of the copolymer samples was determined by Fourier transform infrared spectroscopy (FTIR) according to ASTM D6645-01. A Thermo-Nicolet 750 Magna-IR spectrophotometer equipped with OMNIC software version 7.2a was used for the measurements. Comonomer content can be measured using 13C NMR techniques as discussed in Randall, Rev. Macromol. Chem. Phys., C29 (2&3), p. 285; U.S. Patent 5,292,845 and International Publication No. WO 2005 / 121239. zQOfrnn / zznz / E / YiAi Differential scanning calorimetry (DSC) The melting behavior, including the maximum melting point (Tm), number of peaks, heat of fusion (J / g), and percentage crystallinity of the copolymers, can be determined using a TA Instrument Q1000 DSC thermal analyzer at a rate of 10°C / min in accordance with ASTM D3418-12. In a DSC measurement, the instrument was calibrated with indium; after calibration, the sample was equilibrated to 0°C and then the temperature was increased to 200°C at a heating rate of 10°C / min; the melt was then held isothermally at 200°C for five minutes; the melt was then cooled to 0°C at a cooling rate of 10°C / min and held at 0°C for five minutes; the sample was then heated to 200°C at a heating rate of 10°C / min.The melting point, heat of fusion, and percentage of crystallinity are determined by the main maximum temperature and the total area under the DSC curve, respectively, from the second heating data. The peak melting temperature (Tmes) is the highest temperature peak; when two peaks are present in a bimodal DSC profile, they also typically have the greatest peak height. Primary structure parameter (PSP2) The calculation of PSP2 is described by DesLauriers and zQOfrnn / zznz / E / YiAi Rohlfing in Macromolecular Symposia (2009), 282 (Polyolefin Characterization--ICPC 2008), pages 136-149. The calculation of PSP2 can generally be described as a multi-step process. The first step is to estimate the homopolymer (or low comonomer polymer) density of a sample from the sample's molecular weight distribution as described in Equation (4): 1 / p = Σ (w± / pi) = f 1 / p (dw / dLog M)dLog M Equation (4), where: p = 1.0748(0.0241) Log M. The first step takes into account the effects of molecular weight on the sample density. Density values ​​at molecular weights below 720 g / mol are equal to 1.006 g / cm3 according to this method. In the second step, to better account for the added contributions to density suppression from short-chain branching for each molecular weight (MW) segment, the difference between the measured bulk density of the copolymer and the calculated density of the homopolymer is divided by the total short-chain branching (SCB) level (measured by size-exclusion chromatography-Fourier transform infrared spectroscopy or by 13C-NMR) and then applied to the SCB level in each MW segment. The original observed bulk density of the copolymer (up to 0.852 g / cm³) is obtained by summing the MW portions as described above. The calculations have been simplified by assuming that all SCB levels will have the same effect on density suppression.However, it should be understood that the effectiveness of a particular level of SCB in suppressing density will vary (i.e., the ability of SCB to alter crystallinity decreases as the level of SCB increases). Alternatively, if the copolymer density is unknown, then the effects of SCB on the sample density can be estimated in the second step using Equation 2 as described in U.S. Patent Application Publication No. 2007 / 0298508, now U.S. Patent No. 7,803,629, wherein the change in density Δρ refers to the value that is subtracted from the value given in Equation (5) on a molecular segment by segment basis: Ap=Ci (SCB / PDIn)c2-C3 (SCB / PDIn)c4(Equation 5), wherein Ci=1.25E-02, C2=0.5, C3=7.51E-05, O4=0.62 and n=0.32.The third step is to calculate the amount of 2 lc+laen where lces is the estimated thickness of the crystal lamina (in nm) and laes is the estimated thickness (in nm) of the amorphous material at a particular molecular weight given by the following equations (Equations (6) and (7)):. zoofrnn / zznz / E / YiAi T„(° CJ = (20587.5149640828 )p3- (63826.2771547794 )pz+Equation 6(65965.7028912473) - 22585.2457979131 0.624 nm-7»(K) Equation 7 K c NN In Equation 6, assigned values ​​of 20°C and 142.5°C are given for density values ​​of 0.852 g / cm³ and 1.01 g / cm³, respectively. Equation 7 is a form of the well-accepted Gibbs-Thompson equation. The thickness of the amorphous layer (la) is calculated using Equations (8A) and (8B): C ca σ N Equation 8A Equation 8B where, wc=weight fraction of crystallinity, p=calculated density of the MW segment, pc=density of the 100% crystalline sample (assigned 1.006 g / cm3) and pa=density of the amorphous phase (0.852 g / cm3). The fourth step calculates the bonding probability of the molecule (P) for each molecular weight and the respective 2(lc+la) value according to Equations (9A) and (9B): 4b3r2exp(—b^r^dr í00r2exp(- b2r2)dr •J u 4^3 -> 3 , If 4b3CL2 2 2where b — y Γ={Dul—X 1 ,— if ^Xp( — b Γ )dr The symbols above have the following meanings: P = Probability of bond chain formation, L = Critical distance (nm) = 2 lc+la, D = Chain extension factor at melting = 6.8 for polyethylene, n = Number of bonds = Mw / 14 for polyethylene, and 1 = The bond length = 0.153 nm for polyethylene. Finally, the PSP2 values ​​are calculated from Equations (9A) and (9B) by treating this value essentially as a weighting factor (Pi) for each portion of the MWD, where Pi is arbitrarily multiplied by 100 and subsequently defined as PSP2i. As in all the calculations mentioned above, this value in each segment is multiplied by the respective weight fraction (wí) of the MWD profile to obtain a value for the bulk polymer. Composition Distribution Branching Index (CDBI) The compositional distribution amplitude index (CDBI) is frequently used to quantify how the comonomer is distributed within an ethylene interpolymer, as well as to differentiate ethylene interpolymers produced with different catalysts or processes. CDBI50 is defined as the percentage of ethylene interpolymer whose composition is within 50% of the median comonomer composition; this definition is consistent with that described in U.S. Patent No. 5,206,075. The CDBI5q of an ethylene interpolymer can be calculated from TREF (temperature-raising elution fractionation) curves; the TREF method is described in Wild, et al., J. Polym. Sci., Part B, Polym. Phys., vol. 20 (3), pages 441-455. Typically, the CDBI50 of homogeneous ethylene interpolymers is greater than 70%. Conversely, the CDBI50 of heterogeneous ethylene interpolymers containing α-olefin is generally lower than the CDBI50 of homogeneous ethylene interpolymers. The compositional distribution of a polymer can be characterized by the short chain distribution index (SCDI) or the compositional distribution amplitude index (CDBI). The definition of the compositional distribution amplitude index (CDBI) can be found in Pub. International No. WO 93 / 03093 and U.S. Patent No. 5,206,075. The CDBI was determined using a commercially available crystal-TREF unit from Polymer Char (Valencia, Spain). The acronym TREF stands for temperature-elevated elution fractionation. A sample of ethylene interpolymer product (80–100 mg) was placed in the reactor of the Polymer Char crystal-TREF unit, the reactor was filled with 35 mL of 1,2,4-trichlorobenzene (TCB), heated to 150°C, and held at this temperature for 2 hours to dissolve the sample. Next, an aliquot of the TCB zoofrnn / zznz / E / YiAi solution was loaded (1.5 mL of TCB solution was placed in a Polymer Char TREF column packed with stainless steel beads and equilibrated for 45 minutes at 110°C. The ethylene interpolymer product was then crystallized from the TCB solution in the TREF column by slowly cooling the column from 110°C to 30°C at a cooling rate of 0.09°C per minute. The TREF column was then equilibrated at 30°C for 30 minutes. The crystallized ethylene interpolymer product was then eluted from the TREF column by passing pure TCB solvent through the column at a flow rate of 0.75 mL / minute while slowly increasing the column temperature from 30°C to 120°C at a heating rate of 0.25°C per minute.Using Polymer Char software, a TREF distribution curve was generated as the ethylene interpolymer product eluted from the TREF column. A TREF distribution curve is a graph of the amount (or intensity) of ethylene interpolymer eluting from the column as a function of the TREF elution temperature. A CDBI5q was calculated from the TREF distribution curve for each ethylene interpolymer product analyzed. The CDBI5q is defined as the percentage of ethylene interpolymer whose composition is within 50% of the median comonomer composition (25% on either side of the median comonomer composition); it is calculated from the TREF composition distribution curve and the normalized cumulative integral of the TREF composition distribution curve.Those skilled in the art will understand that a calibration curve is required to convert a TREF elution temperature into comonomer content, that is, the amount of comonomer in the ethylene interpolymer fraction that elutes at a specific temperature. The generation of such calibration curves is described, for example, in Wild et al., J. Polym. Sci., Part B, Polym. Phys., vol. 20 (3), pages 441–455. Generally, Ziegler-Natta catalysts produce ethylene copolymers with a CDBI of less than approximately 50%, consistent with a heterogeneously branched copolymer. In contrast, metallocenes and other single-site catalysts will more frequently produce ethylene copolymers with a CDBI of more than approximately 55%, consistent with a homogeneously branched copolymer. To determine the composition's distribution width index, CDBI50, a solubility distribution curve for the polyethylene composition is first generated. This is achieved using data acquired from the Temperature-Raising Elution Fractionation (TREF) technique. This solubility distribution curve is a graph of the weight fraction of the copolymer that dissolves as a function of temperature. This is converted into a cumulative distribution curve of weight fraction versus comonomer content, from which the CDBI50 is determined by establishing the weight percent of a copolymer sample that has a comonomer content within 50% of the median comonomer content on either side of the median. (See International Publication No. WO 93 / 03093 and U.S. Patent No. 5,376,439). The specific TREF method used here was as follows. Polymer samples (50–150 mg) were introduced into the reactor vessel of a crystallization TREF unit (Polymer Char). The reactor vessel was filled with 20–40 mL of 1,2,4-trichlorobenzene (TCB) and heated to the desired dissolution temperature (e.g., 150°C) for 1–3 hours. The solution was then charged (0.5–1.5 mL) into the TREF column filled with stainless steel beads. After equilibration at a predetermined stabilization temperature (e.g., 110°C) for 30–45 minutes, the polymer solution was allowed to crystallize with a temperature drop from the stabilization temperature to 30°C (at a rate of 0.1 or 0.2°C / minute). After equilibrating at 30°C for 30 minutes, the crystallized sample was eluted with TCB (0.5-0.75 ml / minute) with a temperature ramp from 30°C to the stabilization temperature (0.25-1.0°C / minute).The TREF column was cleaned at the end of the run for 30 minutes at the dissolution temperature. Data were processed using PolymerChar software, Excel spreadsheets, and the internally developed TREF software. Rheological Measurements of Dynamic Mechanical Analysis (DMA) Dynamic Mechanical Analysis (DMA) rheological measurements (e.g., small strain (10%) oscillatory shear measurements) were performed on a Rheometrics Dynamic Spectrometer (RDS-II), Rheometrics SR5, or Stresstech ATS on compression-molded samples in a nitrogen atmosphere at 190°C, using a 25 mm diameter cone and plate geometry. The polymer samples were adequately stabilized with antioxidant additives and then inserted into the test device for at least one minute of preheating to ensure that the normal force returned to zero. DMA experiments were conducted at a 10% strain, from 0.05 to 100 rad / s, and at 190°C. Orchestrator software was used to determine viscoelastic parameters, including the storage modulus (G) and loss modulus (G).The storage modulus G' values ​​were estimated at a constant loss modulus G at 500 Pa at 190 °C (G' to G (500 Pa)). This is to characterize and discriminate the viscoelastic properties of the comparative and described copolymers. This test technique provides the opportunity to study the various characteristics of a molten polymer where the elastic and viscous moduli (G' and G), viscosity (η*), and tangent δ as a function of dynamic oscillation (frequency) are generated to provide information on rheological behavior in correlation with molecular architecture. Dilution index (Yd) measurements A series of small-amplitude frequency sweep tests were performed on each sample using an Anton Paar MCR501 rotational rheometer equipped with the TruGap™ parallel plate measurement system. A gap of 1.5 mm and a strain amplitude of 10% were used throughout the tests. Frequency sweeps ranged from 0.05 to 100 rad / s at intervals of seven points per decade. Test temperatures were 170°C, 190°C, 210°C, and 230°C. Master curves at 190°C were constructed for each sample using Rheoplus / 32 V3.40 software via the standard TTS (time and temperature superposition) procedure, with horizontal and vertical offset enabled. The dilution index (Yd) and the dimensionless modulus (Xd) are then defined. In addition to having molecular weights, molecular weight distributions, and branched structures, ethylene interpolymer blends can exhibit a hierarchical structure in the melt phase. In other words, the components of the ethylene interpolymer may or may not be homogeneous down to the molecular level, depending on the interpolymer's miscibility and the physical history of the blend. Such a hierarchical physical structure in the melt is expected to have a strong impact on flow and, therefore, on processing and conversion, as well as the end-use properties of the manufactured articles. The nature of this hierarchical physical structure among the interpolymers can be characterized. The hierarchical physical structure of ethylene interpolymers can be characterized using melt rheology. A convenient method can be based on small-amplitude frequency sweep tests. Such rheological results are expressed as the phase angle δ as a function of the complex modulus G*, called van Gurp-Palmen plots (as described in M. Van Gurp, J. Palmen, Rheol. Bull. (1998) 67(1): 5-8, and Dealy J, Plazek D. Rheol. Bull. (2009) 78(2): 16-31). For a typical ethylene interpolymer, the phase angle δ increases toward its upper limit of 90°, and G* becomes sufficiently low. VGP plots are a signature of resin architecture. The increase of δ toward 90° is monotonic for an ideally linear monodisperse interpolymer. The δ (G*) for a branched interpolymer or a mixture containing a branched interpolymer may show an inflection point that reflects the topology of the branched interpolymer (see S. Trinkle, P.Walter, C. Friedrich, Rheo. Acta (2002)) 41: 103-113). The deviation of the phase angle δ from the monotonic increase may indicate a deviation from the ideal linear interpolymer due to the presence of long chain branching if the inflection point is low (e.g., δ 20°) or a mixture containing at least two interpolymers that have a different branching structure if the inflection point is high (e.g., δ b 70°). For commercially available linear low-density polyethylenes, inflection points are not observed, with the exception of some commercial polyethylenes containing a small amount of long-chain branching (LCB). To use VGP charts independently of the presence of LCB, an alternative is to use the point where the frequency is two decades below the crossover frequency ω, i.e., mc = 0.01ωχ. The crossover point is taken as a reference because it is known to be a characteristic point that correlates with the MI, density, and other specifications of an ethylene interpolymer. The crossover modulus is related to the plateau modulus for a given molecular weight distribution (see S. Wu. J Polym Sci, Polym Phys Ed zQOfrnn / zznz / E / YiAi (1989) 27:723; M.R. Nobile, F. Cocchini. Rheol Acta (2001) 40:111).The two-decade shift in phase angle δ is to find comparable points where the individual viscoelastic responses of the components can be detected. The complex modulus Gc* for this point is normalized to the crossover modulus, Gx / t (δ), as (δ;2)Gδ / Gx, to minimize the variation due to molecular weight, molecular weight distribution, and short-chain branching. As a result, the coordinates on the VGP charts for this low-frequency point at ω0 = 0.01ωχ, i.e., (δ;2)Gδ / Gxy, characterize the contribution due to the blend. Similar to inflection points, the closer the point {(δ;2)GC / Gδ} is to the upper limit of 90, the more the blend behaves as if it were an ideal single component. As an alternative way to avoid interference due to molecular weight, molecular weight distribution and short branching of the ingredients of the ethylene interpolymer 5C, the coordinates (G*c, 5C) are compared with a reference sample of interest to form the following two parameters: dilution index (Yd) represented by Yd= 5C- (Cq - Ciec2lnGc*) , and dimensionless modulus (Xd) represented by Xd =G*o.oiUc / Gr*, in which the constants Cq, Cd and C2 are determined by fitting the VGP data δ (G*) of the reference sample to the following equation: ó=Co-Ciec2lnG*, where Gr* zQOfrnn / zznz / E / YiAi is the complex modulus of this reference sample in its 5C= δ (0.01ωχ) . When an ethylene interpolymer, synthesized with an online Ziegler-Natta catalyst using a solution reactor, which has a density of 0.920 g / cm3 and a melting index (MI or I2) of 1.0 dg / min, is taken as a reference sample, the constants are: Co = 93.43°, Ci = 1.316°, C2 = 0.2945 and Gr* = 9432 Pa. The values ​​of these constants may be different if the rheology test protocol differs from the one specified here. These regrouped coordinates (Xd, Yd) of (Gc*, 5C) allow for comparison between the ethylene interpolymer products described herein and comparative examples. The dilution index (Yd) reflects whether the blend behaves as a simple mixture of linear ethylene interpolymers (without hierarchical structure in the melt) or exhibits a distinct response reflecting a hierarchical physical structure within the melt. The lower the Yd, the more the sample exhibits separate responses from the ethylene interpolymers included in the blend; the higher the Yd, the more the sample behaves as a single component or a single ethylene interpolymer. The dimensionless modulus (Xd) reflects the differences (relative to the reference sample) that are related to the overall molecular weight, the molecular weight distribution (Mw / Mn), and short-chain branching. Without wishing to limit itself to any particular theory, it is believed that the dimensionless modulus (Xd) can be considered related to the Mw / Mn ratio and the radius of gyration ( <rg>2) The increase in Xd and the ethylene interpolymer in the melt may have similar effects to those of increasing Mw / Mny / o <rg>2, without the risk of including a lower molecular weight fraction and sacrificing certain related properties. Tensile Properties The following tensile properties were determined using ASTM D638: tensile breaking strength (MPa), yield elongation (%), yield strength (MPa), maximum elongation (%), ultimate strength (MPa), and secant modulus at 1 and 2% (MPa). Flexural properties The flexural properties, i.e., the 2% secant flexural modulus, were determined using ASTM D790-10 (published in April 2010). ARM impact tests The ARM impact test was performed in accordance with ASTM D5628 at a test temperature of -40°C. This test was adapted from the International Association of Rotational Molders' Low Temperature Impact Test, Version 4.0, dated July 2003. The purpose of this test was to determine the impact properties of the rotomolded parts. ARM impact test specimens, 12.7 cm x 12.7 cm (5 in x 5 in), were cut from a side wall of the cubic rotomolded part that was 3.18 mm (0.125 in) thick. The test specimens were thermally equilibrated in a refrigerated test laboratory maintained at -40°C ± 2°C (40 ± 3.5°F) for at least 24 hours prior to the impact test. The testing technique used is commonly called the Bruceton ladder method or the up-and-down method.The procedure establishes the specific dart height that will cause 50% of the specimens to fail. The test (dar falling on the specimens) was performed until a minimum of 10 passes and 10 failures occurred. Each failure was characterized as either ductile or brittle. Ductile failure was characterized by the dart penetrating the specimen, with the impact area elongated and thinned, leaving a hole with fibrous fibers at the point of failure. Brittle failure was evident when the test specimen cracked, with cracks radiating outward from the point of failure and the specimen showing little to no elongation at the point of failure. The percentage of ductility (ARM) was calculated as follows: 100 x [(number of ductile failures) / (total number of all failures)]. The average ARM failure energy (ft-lbs) was calculated by multiplying the drop height (ft) by the nominal dart weight (lbs). The samples were subjected to impact testing using a weight drop impact tester; the available impact darts consisted of 10 lb (4.54 kg), 15 lb (6.80 kg), 20 lb (9.07 kg) or 30 lb (13.6 kg) darts. All impact darts had a rounded dart tip with a diameter of 1.0 ± 0.005 inches (2.54 cm), the dart tip was transformed into a lower cylindrical shaft (diameter of 1.0 inch), the length of the lower cylindrical shaft (to the dart tip) was 4.5 inches (11.4 cm). Impact darts included an upper cylindrical shaft with a diameter of 5.08 cm (2.0 in). The length of the upper cylinder shaft varied according to the desired dart weight; for example, 26.7 cm (10.5 in) or 41.9 cm (16.5 in) for the 10 lb or 20 lb dart, respectively. Preferably, a dart weight is selected so that the drop height is between 2.5 ft and 7.5 ft (0.8 m to 2.3 m).The test specimens were oriented in the impact tester so that the falling dart impacted the surface of the part in contact with the mold (when molded). If the specimen did not fail at a given height and weight, the height or weight was gradually increased until partial failure occurred. Once failure occurred, the height or weight was reduced by the same increment, and the process was repeated. The average failure energy of the ARM was calculated by multiplying the drop height (in feet) by zQOfrnn / zznz / E / YiAi. 40,000, which favors an increase in the total comonomer content. A molecular weight value of 40,000 was identified as a threshold value below which crystallinity (density) becomes exponentially dependent on changes in molecular weight. The ethylene interpolymer products described in the Examples section were produced in a continuous solution polymerization pilot plant with reactors arranged in series. Methylpentane (a commercial mixture of methylpentane isomers) was used as the process solvent. The volume of the first CSTR (R1) was 3.2 gallons (12 L), the volume of the second CSTR (R2) was 5.8 gallons (22 L), and the volume of the tubular reactor (R3) was 4.8 gallons (18 L). Examples of ethylene interpolymer products were produced using a pressure of R1 from approximately 14 MPa to approximately 18 MPa; R2 was operated at a lower pressure to facilitate continuous flow from R1 to R2. R1 and R2 operated in series, with the first outlet stream from R1 flowing directly into R2. Both CSTRs were stirred to ensure that the reactor contents were well mixed.The process was made to work continuously by feeding fresh process solvent, ethylene, 1-octene, and hydrogen to the reactors. The single-site catalyst components used (Catalyst Formulation 1) were: component (i), cyclopentadienyl tri(butyl tertiary)phosphinimine titanium dichloride, (Cp[(t-Bu)3PN]TICl2), hereinafter PIC-1; component (ii), methylaluminoxane (MMIOO-07); component (iii), triphyll tetrakis(pentafluorophenyl)borate; and component (iv), 2,6-di-tert-butyl-4-ethylphenol. The single-site catalyst component solvents used were methylpentane for components (ii) and (iv) and xylene for components (i) and (iii). The amount of PIC-1 added to R1, R1(i) (ppm) is shown in Table 1. The molar ratios of the single-site catalyst components used to produce Examples 1-3 are shown in the following table. zQOfrnn / zznz / E / YiAi Example 1 Example 2 Example 3 Molar ratio Rl (ii) / (i) [ (MMAO-07) / (PIC-1) ] 100 100 100 Molar ratio Rl (iv) / (ii) [(2,6-di-tert-butyl-4ethylphenol) / (MAMO-07)] 0 0 0.4 Molar ratio Rl (iii) / (i) [(tetrakis(pentafluoropheni)borate)tripyl / (PIC-1)] 1.2 1.1 1.1 The single-site catalyst formulation was injected into Rl using a process solvent; the flow rate of this solvent containing catalyst was approximately 30 kg / h. The online Ziegler-Natta catalyst formulation was prepared from the following components: component (v), butylethylmagnesium; component (vi), tert-butyl chloride; component (vii), titanium tetrachloride; component (viii), diethylaluminum ethoxide; and component (ix), triethylaluminum. Methylpentane was used as the solvent component of the catalyst. The online Ziegler-Natta catalyst formulation was prepared using the following steps.In step one, a triethylaluminum / dibutylmagnesium solution ((triethylaluminum) / (dibutylmagnesium) in a molar ratio of 20:1) was combined with a tertiary butyl chloride solution and allowed to react for approximately 30 seconds (HUT-1). In step two, a titanium tetrachloride solution was added to the mixture formed in step one and allowed to react for approximately 14 seconds (HUT-2). In step three, the mixture formed in step two was allowed to react for an additional 3 seconds (HUT-3) before injection into R2. The inline Ziegler-Natta procatalyst formulation was injected into R2 using a process solvent; the flow rate of the solvent containing the catalyst was approximately 49 kg / h. The inline Ziegler-Natta catalyst formulation was formed in R2 by injecting a diethylaluminum ethoxide solution into R2.The amount of titanium tetrachloride R2 (vii) (ppm) zQOfrnn / zznz / E / YiAi added to reactor 2 (R2) is shown in Table 1. In Examples 1-3, the following molar ratios shown in the table below were used to synthesize the Ziegler-Natta Catalyst online. Example 1 Example 2 Example 3 Molar ratio R2 (vi) / (v) 1.58 1.58 1.98 Molar ratio R2 (viii) / (vii) 1.35 1.35 1.35 Molar ratio R2 (ix) / (vii) 0.35 0.35 0.35 In all the examples described, 100% of the diethylaluminum ethoxide was injected directly into R2. Table 1 provides additional information on the manufacturing conditions for the comparative polyethylene compositions described. For examples 1, 2, and 3, the volume of the first reactor was 12 liters and the volume of the second reactor was 22 liters. These are pilot plant scales. The first reactor was operated at a pressure of 10,500–35,000 kPa, and the second reactor was operated at a lower pressure to facilitate continuous flow from the first reactor to the second. The solvent was methylpentane. The process operates using continuous feed streams. For comparative examples 1–5, the volume of the first reactor was 12 liters and the volume of the second reactor was 22 liters. These are pilot plant scales. The first reactor was operated at a pressure of 10,500–35,000 kPa, and the second reactor was operated at a lower pressure to facilitate continuous flow from the first reactor to the second.The solvent was methylpentane. The process operates using continuous feed streams. Comparative example 6 is a commercial rotomolding grade. Comparative example 7 is a commercial product from NOVA Chemicals. Comparative example 8 is a commercial DOW product sold under the CONTINUUM™ DMDC-1250 label. Table 2 illustrates a computer-generated version of an ethylene interpolymer product (using the methods described in U.S. Patent No. 9,695,309) for the purpose of estimating the properties of the first and second ethylene interpolymers produced in each of the first (R1) and second (R2) polymerization reactors. This simulation was based on fundamental kinetic models (with kinetic constants specific to each catalyst formulation), as well as the feed and reactor conditions presented in Table 1 and used for the production of Examples 1, 2, and 3 described above. The simulation was further based on the solution pilot plant configuration described above that was used to produce the ethylene interpolymer products. The simulated version of Examples 1, 2, and 3 was synthesized using a single-site catalyst formulation in R1 and an in-line Ziegler-Natta catalyst formulation in R2. The properties of the polyethylene composition described and compared are outlined in Tables 3, 4, and 5. The ethylene interpolymer product described herein has a density of 0.948, a melt index of 1.0–1.4 g / 10 min, a polydispersity (Mw / Mn) of less than 5, and an inverse comonomer distribution. The ethylene interpolymer product comprises a blend of a high-density, low-molecular-weight component made with a Ziegler-Natta (ZN) catalyst—that is, a heterogeneous catalyst formulation—and a low-density, high-molecular-weight component made with a single-site catalyst (SSC) formulation. The ethylene interpolymer product described herein exhibits excellent ESCR performance (ESCR B10 > 90 hours, ESCR A100 > 1000 hours) and a polydispersity (Mw / Mn) of less than 5.Toughness is evaluated using the IZOD impact strength of compression-molded plates. Toughness is greater than 0.19 m-kg / cm (3.5 ft.lb / in). The ethylene interpolymer product described herein has a balance of toughness and ESCR that is unmatched by commercial products with comparable density / melt index specifications, such as the high-density commercial products listed here as comparative examples 7 and 8. The ethylene interpolymer product described herein may have improved rotomolding processability, as demonstrated by the ductile impact failure mode of the rotomolded part tested at low temperatures (e.g., -40°C). Rotomolding Rotational molding tests were carried out on the described examples. Additives were incorporated into the preparation of each evaluated example for rotational molding performance using melt extrusion and fine powder grinding (35 mesh). Example 1, described, was prepared by mixing additives in the molten state, as a master batch, using a Leistritz LSM 30.34 twin-screw extruder.The composition shown in Example 1 described contained the following additives (All amounts shown in parts per million by weight of polyethylene): Hindered Phenol (Irganox 1076): 574 ppm total; Phosphite (CAS Registry Number 31570-04-4): 912 ppm; Diphosphite (CAS Registry Number 154862-43-8): target amount of 450 ppm; Hydroxylamine (CAS Registry Number 143925-92-2): target amount of 250 ppm; Hindered Amine Light Stabilizer (HALS Chimassorb 944): target amount of 750 ppm; Hindered Amine Light Stabilizer (HALS Tinuvin 622): target amount of 750 ppm; Zinc Oxide: target amount of 750 ppm. Example 3 described was prepared by mixing molten additives in the form of a master batch using a Coperion ZSK26 twin-screw extruder.The composition shown in Example 3 described contained the following additives (All amounts are shown in parts per million by weight of polyethylene): Hindered Phenol (IRGANOX® 1076): 561 ppm total; Phosphite (CAS Registry Number 31570-04-4): 813 ppm; Diphosphite (CAS Registry Number 154862-43-8): target amount of 429 ppm; Hydroxylamine (CAS Registry Number 143925-92-2): target amount of 250 ppm; Hindered Amine Light Stabilizer (HALS Chimassorb 944): target amount of 750 ppm; Hindered Amine Light Stabilizer (HALS Tinuvin 622): target amount of 750 ppm; Zinc Oxide: target amount of 750 ppm. Rotational molding tests were conducted on the comparative examples. Additives were incorporated into the preparation of each evaluated example for rotational molding performance using melt extrusion. Example 7 was prepared by blending additives in the melt, as a masterbatch, using a Coperion ZSK26 twin-screw extruder. The composition shown in Example 7 contained the following additives (all quantities are shown in parts per million by weight of polyethylene): Hindered Phenol (Irganox 1010): target amount of 500 ppm; Phosphite (CAS Registry Number 31570-04-4): 1550 ppm; Diphosphite (CAS Registry Number 154862-43-8): target amount of 450 ppm; Hydroxylamine (CAS Registry Number 143925-92-2): target amount of 250 ppm. Hindered Amine Light Stabilizer (HALS Chimassorb 944): Target amount of 750 ppm; Hindered Amine Light Stabilizer (HALS Tinuvin 622): Zinc Oxide: Target amount of 750 ppm.Example 8 was prepared by blending additives in the melt, in the form of a master batch using a Coperion ZSK26 twin-screw extruder. The composition shown in Example 8 contained the following additives (All quantities are shown in parts per million by weight of polyethylene): Phosphite (CAS Registry Number 31570-04-4): 1824 ppm; Diphosphite (CAS Registry Number 154862-43-8): 508 ppm; Hydroxylamine (CAS Registry Number 143925-92-2): target amount of 250 ppm; Hindered Amine Light Stabilizer (HALS Chimassorb 944): Hindered Amine Light Stabilizer (HALS Tinuvin 622): minimum target amount of 750 ppm; Zinc Oxide: minimum target amount of 750 ppm. Figure 1 illustrates the IZOD impact strength (ft.lb / in) versus the ambient stress cracking strength (ESCR) (hr) of ethylene interpolymer polymers according to the present description and comparative examples. zoofrnn / zznz / E / YiAi Figure 2 illustrates the crystallinity at 23°C versus the molecular weight of an ethylene interpolymer polymer. See Tung and Buckser, Effect of molecular weight on the crystallinity of polyethylene (1958), J. Phys. Chem., vol. 62, p. 1520. Figure 3 illustrates the molecular weight distribution obtained by GPC measurement of an ethylene interpolymer polymer according to the present description (Example 1 described) and the deconvolution results based on multiple Flory molecular weight distribution functions. The first ethylene interpolymer is modeled using a single Flory distribution function. The second ethylene interpolymer is estimated using a four-distribution model. Figure 4 illustrates the molecular weight distribution obtained by GPC measurement of an ethylene interpolymer polymer according to the present description (Example 1) and the deconvolution results based on three idealized Flory molecular weight distribution functions. Figure 5 illustrates the cumulative weight fraction of an ethylene interpolymer polymer according to the present description (Example 1 and Example 2) and comparative examples 1, 2, 5, and 6. Without wishing to be tied to any particular theory, it is believed that the Ziegler-Natta component provides continuity in the interpolymer product. The interpolymer product described herein has been shown to be beneficial in maintaining better toughness and ESCR performance compared to conventional compositions. The interpolymer product having improved ESCR and toughness according to the present description may include linker molecules, which are favored with an increase in molecular weight combined with an increase in comonomer incorporation. With reference to Tables 2, 3 and 5, without wishing to limit oneself to any particular theory, it is believed that molecular weight and molecular weight distribution have a minimal effect on ESCR and toughness; however, the molecular weight of the high-density fraction and the overall comonomer incorporation affect ESCR performance. While comonomer content can influence density, the effect of molecular weight becomes exponentially important at values ​​below 50,000. The interpolymer product according to the present description may include a low molecular weight component that has a higher density than normally expected based solely on the composition (component R2) To achieve the desired overall composition density, the amount of comonomer in the high molecular weight fraction can be increased. This results in an interpolymer product with an inverse comonomer distribution and improved ESCR and toughness. However, there are limits to the amount of low molecular weight fraction that can be included in the interpolymer product to avoid plasticizing effects and deposition problems during and after the conversion process. The interpolymer product according to the present description was prepared by selecting reactor conditions that (1) force the molecular weight of the high-density component to remain below a threshold of 40,000; (2) minimize the incorporation of comonomers into the high-density component; and (3) increase the incorporation of comonomers into the high molecular weight component; (4) maintain the polydispersity index of the overall composition below 5. The interpolymer product described herein may include ethylene copolymers with a density greater than 0.948 g / cm³, which may be suitable for rotational molding applications with high ESCR requirements. The interpolymer product may be manufactured using a single-site catalyst (SSC) and a Ziegler-Natta (ZN) catalyst in a dual reactor technology. The SSC technology provides better control over molecular weight and comonomer distribution. The ZN component provides continuity in the overall molecular composition, contributing to rotomolability and toughness. The interpolymer product described herein has a high molecular weight and high comonomer content, which improves both toughness and ESCR performance.When compared to conventional interpolymer products, the interpolymer product described herein has an unusually high toughness-ESCR balance with comparable melt index and density. Without wishing to be bound to any particular theory, it is believed that the suitability of the high-density interpolymer product described herein for rotational molding applications may be related to increasing the total comonomer content while maintaining the desired density. This can be achieved by keeping the molecular weight of the high-density component below 40,000 because crystallinity (density) becomes exponentially dependent on changes in molecular weight below this value. The improved toughness and ESCR performance may be related to controlling the low-molecular-weight component. ζοοίτηη / ζζηζ / Ε / γίΛΐ The following aspects are described in this description: Aspect 1. An interpolymer product comprising: a first ethylene interpolymer comprising ethylene and an aolefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer comprising an Mw less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product comprising an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, 10% IGEPAL CO-630, greater than 90 hours. Aspect 2. The interpolymer product of any of the preceding claims, wherein the density of the interpolymer product is 0.94-0.97 g / cm3; the density of the interpolymer product is 0.945-0.965 g / cm3; or the density of the interpolymer product is 0.947-0.955 g / cm3. Aspect 3. The interpolymer product of any of the above aspects, wherein the ESCR of the interpolymer product is 90 to 500 hours; or the ESCR of the interpolymer product is 100 to 400 hours. Aspect 4. The interpolymer product of any of the above aspects, wherein the impact resistance zQOfrnn / zznz / E / YiAi The IZOD of the interpolymer product is greater than 0.10 m-kg / cm (2 ft.Lb / in); the IZOD impact strength of the interpolymer product is from 0.10 m-kg / cm to 0.54 m-kg / cm (2 to 10 ft.Lb / in); or the IZOD impact strength of the interpolymer product is from 0.10-0.27 m-kg / cm (2-5 ft.Lb / in). Aspect 5. The interpolymer product of any of the above aspects, including a tensile impact greater than 3.0 m-kg / cm2 (140 ft.lb / in2); or a tensile impact of 3.0-7.5 m-kg / cm2 (140-350 ft.lb / in2). Aspect 6. The interpolymer product of any of the above aspects that includes a melt index (I2) greater than 0.5 g / 10 min; a melt index (I2) of 0.88 g / 10 min; or a melt index (I2) of 0.8-5 g / 10 min. Aspect 7. The interpolymer product of any of the above aspects that includes a melt flow ratio, I21 / I2, of 30-70; or a melt flow ratio, I21 / I2 / ·, of 35-60. Aspect 8. The interpolymer product of any of the above aspects that includes a flexural modulus (1% secant) of at least 1000 MPa; or a flexural modulus (1% secant) of 1,100-1,500 MPa. Aspect 9. The interpolymer product of any of the above aspects including a total vinyl unsaturation greater than 0.02 vinyl groups per 1,000 carbon atoms; or a total vinyl unsaturation of 0.02-1.0 vinyl groups per 1,000 carbon atoms. Aspect 10. The interpolymer product of any of the above aspects that includes a long-chain branching frequency of 0. Aspect 11. The interpolymer product of any of the above aspects including a short-chain branching frequency of 0.5-5.0; a short-chain branching frequency of 0.5 to 2.9; or a short-chain branching frequency of 3.0-4.0. Aspect 12. The interpolymer product of any of the above aspects, which includes a CDBI5o greater than 70%; or a CDBI50 of 70-90%. Aspect 13. The interpolymer product of any of the above aspects, wherein the α-olefin includes a C3-C12 α-olefin or a combination thereof; the α-olefin includes an α-olefin selected from 1-hexene, 1-octene, or a mixture thereof; the α-olefin includes 1-hexene; or the α-olefin includes 1-octene. Aspect 14. The interpolymer product of any of the above aspects, wherein the α-olefin includes 0.05-5 mol% of the interpolymer product; the α-olefin includes 0.1-5 mol% of the interpolymer product; the α-olefin includes 0.5-3.0 mol% of the interpolymer product; the α-olefin includes 0.5-1.5 mol% of the interpolymer product; the α-olefin includes 0.1-0.5 mol% of the interpolymer product; the α-olefin includes 2.7 mol% of the interpolymer product; or the α-olefin includes 0.7 mol% of the interpolymer product. Aspect 15. The interpolymer product of any of the above aspects including a number average molecular weight (Mn) of 12,000 to 45,000; a number average molecular weight (Mn) of 15,000 to 40,000; or a number average molecular weight (Mn) of 20,000-30,000. Aspect 16. The interpolymer product of any of the above aspects including an average molecular weight z (Mz) of 280,000-500,000; or an average molecular weight z (Mz) of 305,000-400,000. Aspect 17. The interpolymer product of any of the above aspects including a polydispersity (Mw / Mn) of 3-7; a polydispersity (Mw / Mn) of 4-7. Aspect 18. The interpolymer product of any of the above aspects, including a dilution index, Yd, >-1.0; a dilution index, Yd, less than 0; or a dilution index, Yd, from -10 to 0. Aspect 19. The interpolymer product of any of the above aspects, which includes a primary structure parameter (PSP2) of 2 to 8.9 as determined by the GPC-FTIR branching distribution profile; a primary structure parameter (PSP2) of 4 to 8 as determined by the GPC-FTIR branching distribution profile; a primary structure parameter (PSP2) of 2 to 8.9 determined by the branching content (FTIR); or a primary structure parameter (PSP2) of 4 to 8 determined by the branching content (FTIR). Aspect 20. The interpolymer product of any of the above aspects including, based on the total weight percentage of the interpolymer product: 10-45% by weight of the first interpolymer; and 55-90% by weight of the second interpolymer. Aspect 21. The interpolymer product of any of the above aspects including, based on the total weight percentage of the interpolymer product: 10-40% by weight of the first interpolymer; and 60-90% by weight of the second interpolymer. Aspect 22. The interpolymer product of any of the above aspects including, based on the total weight percentage of the interpolymer product: 15-30% by weight of the first interpolymer; and 70-85% by weight of the second interpolymer. Aspect 23. The interpolymer product of any of the above aspects, wherein the first interpolymer includes 10-45% by weight of the interpolymer product; 10-35% by weight of the interpolymer product; or 15-30% by weight of the interpolymer product. Aspect 24. The interpolymer product of any of the above aspects, wherein the first interpolymer includes an Mwde 200,000-500,000; an Mwde 230,000-450,000; or an Mwde 250,000-400,000. Aspect 25. The interpolymer product of any of the above aspects, wherein the first interpolymer includes an Mnde 100,000-200,000; or an Mnde 120,000-180,000. Aspect 26. The interpolymer product of any of the above aspects, wherein the first interpolymer includes an Mz from 320,000 to 650,000; or an Mz from 350,000 to 545,000. Aspect 27. The interpolymer product of any of the above aspects, wherein the first interpolymer includes a polydispersity (Mw / Mn) of 1.0-3.0; or a polydispersity (Mw / Mn) of 1.75-2.7. Aspect 28. The interpolymer product of any of the above aspects, wherein the first interpolymer includes a short-chain branching frequency of 1.0-5.0; or a short-chain branching frequency of 1.3-3.5. Aspect 29. The interpolymer product of any of the above aspects, wherein the first interpolymer includes a melt index (I2) of up to 0.4 g / 10 min; or a melt flow index (I2) of 0.0001-0.4 g / 10 min; or a melt index (I2) of 0.001-0.1 g / 10 min. Aspect 30. The interpolymer product of any of the above aspects, wherein the first interpolymer includes a density of 0.90-0.93; or a density of 0.9100.929 g / cm3. Aspect 31. The interpolymer product of any of the above aspects, wherein the second interpolymer includes 55-90% by weight of the interpolymer product; or 65-90% by weight of the interpolymer product; or 70-85% by weight of the interpolymer product. Aspect 32. The interpolymer product of any of the above aspects, wherein the second interpolymer includes an Mwde 30,000-70,000; or an Mwde 40,000-60,000. Aspect 33. The interpolymer product of any of the above aspects, wherein the second interpolymer includes an Mnde 10,000-30,000; an Mnde 12,000-25,000. Aspect 34. The interpolymer product of any of the above aspects, wherein the second interpolymer includes an Mzde 70,000 to 125,000; or an Mzde 80,000 to 115,000. Aspect 35. The interpolymer product of any of the above aspects, wherein the second interpolymer zQOfrnn / zznz / E / YiAi includes a polydispersity (Mw / Mn) of 2.0-7.0; or a polydispersity (Mw / Mn) of 2.5-5.0. Aspect 36. The interpolymer product of any of the above aspects, wherein the second interpolymer includes a short-chain branching frequency of 0.01-1.5; a short-chain branching frequency of 0.01 to 1.0; or a short-chain branching frequency of 0.1-1.5. Aspect 37. The interpolymer product of any of the above aspects, wherein the second interpolymer includes a melt index of 1-500 g / 10 min; or a melt index of 5-200 g / 10 min; a melt index of 1-50 g / 10 min; or a melt index of 10-100 g / 10 min. Aspect 38. The interpolymer product of any of the above aspects, wherein the second interpolymer includes a density of 0.93-0.98; or a density of 0.95 to 0.97. Aspect 39. An interpolymer product of any of the above aspects comprising: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) of 300,000 to 450,000 and a density of 0.900 to 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw of zoofrnn / zznz / E / YiAi 30,000 to 70,000 and a density of 0.930 to 0.980; and wherein the interpolymer product has: an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, 10% IGEPAL CO-630, of more than 90 hours; an IZOD impact strength of 0.16 to 0.27 mkg / cm (3.0 to 5.0 ft.Lb / in); a density of 0.945-0.960; a melt index of 0.9-3.0; and a melt flow ratio, I2i / l2z, of 35-65. Aspect 40. An interpolymer product of any of the above aspects comprising: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 210,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an MK less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product includes: an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 200 hours; an IZOD impact strength of 0.27 to 0.43 m-kg / cm (5.0 to 8.0 ft-lb / in); a density of 0.945-0.955; a melting index of 0.9 to 5.0; and a melting flux ratio, I21 / I2, of 40-65. Aspect 41. An interpolymer product of any of the above aspects including: an environmental stress cracking (ESCR) resistance, measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, of more than 300 hours; an IZOD impact strength of 0.27 to 0.43 mkg / cm (5.0 to 8.0 ft.Lb / in); a density of 0.945-0.953; a melt index of 1.0-2.0; and a melt flow ratio, I21 / I2L, of 45-60. Aspect 42. An interpolymer product of any of the above aspects including: an environmental stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, of more than 90 hours; an IZOD impact strength of 0.16 to 0.27 mkg / cm (3.0 to 5.0 ft.lb / in); a density of 0.947-0.960; a melt index of 0.9-3.0; and a melt flow ratio, I21 / I2 / of 35-65. Aspect 43. A rotomolded article of any of the above aspects including a wall structure including at least one layer including an ethylene interpolymer product including: a first ethylene interpolymer including ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer including ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product has an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 90 hours. Aspect 44. The rotomolded article of any of the above aspects selected from a toy, wastebasket, container, helmet, boat, or large tank. Aspect 45. A closure for a bottle, wherein the closure includes: a first ethylene interpolymer including ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3; and a second ethylene interpolymer including ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm3, and wherein the interpolymer product includes an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, of more than 90 hours. Aspect 46. The closure of any of the above aspects carried out by compression molding or injection molding. Aspect 47. The closure of any of the above aspects including a screw cap. Aspect 48. A composition as substantially described in the accompanying description and figures. zQOfrnn / zznz / E / YiAi Aspect 49. A polymer mixture composition as substantially described in the accompanying description and figures. Aspect 50. A bimodal polyethylene copolymer composition as substantially described in the accompanying description and figures. Aspect 51. An interpolymer product as substantially described in the accompanying description and figures. Aspect 52. An article that includes the composition as substantially described in the accompanying description and figures. Aspect 53. A rotomolded article including the composition as substantially described in the accompanying description and figures. Aspect 54. A rotomolded article including a wall structure comprising the composition as substantially described in the accompanying description and figures. Aspect 55. A single-layer film comprising the composition as substantially described in the accompanying description and figures. Aspect 56. A multi-layered film including the composition as substantially described in the accompanying description and figures. zQOfrnn / zznz / E / YiAi Aspect 57. A method for preparing the composition as substantially described in the accompanying description and figures. Aspect 58. A method for manufacturing the interpolymer product as substantially described in the accompanying description and figures. Aspect 59. A method for manufacturing the article as substantially described in the accompanying description and figures. Aspect 60. A method for manufacturing the film as substantially described in the accompanying description and figures. All documents cited herein are incorporated herein by reference, but only to the extent that the incorporated material does not conflict with the definitions, statements, or other existing documents set forth herein. To the extent that any meaning or definition of a term in this document conflicts with any meaning or definition of the same term in a document incorporated by reference, the meaning or definition assigned to that term in this document shall prevail. The citation of any document should not be construed as an admission that it is prior art with respect to this application. References: Publication of Application for Patent zoofrnn / zznz / E / YiAi 100 US Patent No. 7,153,909; US Patent No. 8,076,421; US ​​Patent No. 8,791,205; US Patent No. 9,102,819; US Patent No. 9,758,653. Although they are private, it would be 2018 / 230,298; Patent American No. 7,396,881; Patent American No. 8,492,498; Patent American No. 9,056,970; Patent American No. 9,695,309; and Patent have illustrated yd( obvious to the experts American No. 7,307,126; US Patent No. 8,101,687; US Patent No. 8,829,115; US Patent No. 9,512,283; US Patent No. The described methods in the art described herein may be modified or altered in any way without departing from the spirit and scope of the description. Those skilled in the art will recognize, or be able to determine through routine experimentation, numerous equivalents to the specific apparatus and methods described herein, including alternatives, variants, additions, deletions, modifications, and substitutions. Therefore, this application, including the appended claims, purports to cover all changes and modifications that are within the scope of this application. zoofrnn / zznz / E / YiAi Table 1: Reactor Conditions Example (1) Example (2) Example (3) Comparative Example 1 (Ex. 73 of US 9,695,309) Comparative Example 2 (Ex. 71 of US 9,695,309) Comp. Example 3 Comp. Example 4 (Ex. #3 in US 9,982,077) Comp. Example 5 Ethylene divided between first reactor (R1), second reactor (R2) 22 / 78 22 / 78 30 / 70 30 / 70 35 / 65 20 / 80 0.35 / 0.65 0.35 / 0.65 Octene divided between first reactor (R1) and second reactor (R2) and third reactor (R3) 1 / 0 1 / 0 1 / 0 1 / 0 1 / 0 1 / 0 1 / 0 1 / 0 Octene to ethylene ratio in fresh feed 0.030 0.037 0.038 0.043 0.052 0.016 0.021 0.028 Hydrogen in reactor 1 (ppm) 0.3 0.2 0.9 0.9 1.2 0.3 0.8 1.2 Hydrogen in reactor 2 (ppm) 22.0 31.9 30.0 24.0 34.0 18.5 4.5 6.0 Reactor 1 temperature (°C) 133 131 136 140 135 137 143 144 Reactor 2 temperature (°C) 219 219 210 217 217 216 208 211 Ethylene conversion of reactor 1 (%) 88.6 89.2 83.6 91.0 90.0 89.0 Ethylene conversion of reactor 2 (%) 75.6 80.1 80.2 89.8 Ethylene conversion of reactor 2 (%) 86.6 86.1 87.5 90.1 90.9 PIC-1 (ppm) 0.14 0.13 0.09 0.15 0.13 0.10 0.10 PIC-1 (ppm) 0 0 0 0 0 0.22 0.38 R2 (vil) (ppm) 3.1 2.6 7.4 4.3 4.9 0 0 Production rate of polyethylene (kg / h) 75.8 78.0 83.5 92.7 94.6 91.3 86.1. 102 Table 2A: Deconvolution Results for Described Examples ζοοίτηη / ζζηζ / Ε / γίΛΐ Example (1) Example (2) Example (3) 1st ETHYLENE POLYMER (R1- Deconvolution Studies) Kinetic Model (R1) Kinetic Model (R2) Kinetic Model (R1) Kinetic Model (R1) Single Site Single Site Single Site Weight Fraction (%) 20% 27% 21% 27% Mn 161,500 125,000 178,377 133,330 Mw 323,000 250,000 356,754 266,660 Mz 484,500 375,000 535,131 399,990 Polydispersity Index (Mw / Mn) 2.0 2.0 2.0 2.0 Branching Frequency / 1000C (SCB1) 1.9 2.4 1.4 Estimated density (g / cm3) (1 eq.) 0.9218 0.9191 09261 Estimated melting index I2 (g / 10 min) (3 eq.) 0.0089 0.01 0.02 2nd ETHYLENE POLYMER (R2- Deconvolution studies) Kinetic model (R2) Deconv. study (Florv Dist.) Kinetic Model (R2) Kinetic Model (R2) Ziegler-Natta Ziegler-Natta Ziegler-Natta Weight Fraction (%) 80% 28% 79% 73% Mn 19,200 10,000 18,839 17,424 Mw 58,500 20,000 51,676 42,794 Mz 123,600 30,000 110,475 81,666 Polydispersity Index (Mw / Mn) 3.0 2.0 2.7 2.5 Branching Frequency / 1000C (SCB2) 0.6 0.4 0.9 Estimated Density (g / cm3) (eq. 1) 0.9618 0.9559 0.9594 Estimated Melting Index I2 (g / 10 min) (eq. 3) 8.0 12.6 25.6 3rd ETHYLENE POLYMER (AFT+Trim simulation) Deconversion Study (Flory Dist.) Weight Fraction (%) 45% Mn 31,000 Mw 62,000 Mz 93,000 Polydispersity Index (Mw / Mn) 2.0 Branching Frequency / 1000C (SCB2) Estimated Density (g / cm3) (eq. 1) Estimated Melting Index I2 (g / 10 min). 103 Table 2B: Deconvolution Results for Examples Comparatives 1, 2, 3, 4, and 5 zoofrnn / zznz / E / YiAi Comparative Example 1 (Ex. 73 of US 9,695,309) Comparative Example 3 (Ex. 71 of US 9,695,309) Comparative Example 3 Comparative Example 4 (Ex. #3 in US 9,982,077) Comparative Example 5 1st ETHYLENE POLYMER (R1 Deconvolution Studies) Kinetic Model (R1) Kinetic Model (R1) Kinetic Model (R1) Kinetic Model (R1) Kinetic Model (R1) Single Site Single Site Single Site Single Site Single Site Single Site Weight Fraction (%) 31% 36% 17% 29% 33% Mn 88,100 84,900 166,500 111,200 83,500 MW 181,500 174,400 333,000 222,400 167,000 Mz 499,400 333,600 250,500 Polydispersity index (Mw / Mn) 2.1 2.1 2.0 2.0 2.0 Branching Frequency / 1000C (SCB1) 2.3 2.2 1.1 2.0 2.3 Estimated density (g / cm2) (eq. 2) 0.9276 0.9283 0.9240 0.9264 0.9291 Estimated melting index b ^10min)(eq3) 0.07 0.09 0.01 0.04 0.12 2nd ETHYLENE POLYMER (R2 Deconvolution Studies) Kinetic Model (R2) Kinetic Model (R2) Kinetic Model (R2) Kinetic Model (R2) Kinetic Model (R2) Ziegler-Natta Ziegler-Natta Ziegler-Natta Single Site Single Site Weight Fraction (%) 61% 57% 73% 71% 67% Mn 19,000 17,600 18,400 23,700 19,700 Mw 52,500 45,000 48,800 47,400 39,400 Mz 114,000 90,700 99,800 71,100 59,100 Polydispersity Index (Mw / Mn) 2.8 2.6 2.7 2.0 2.0 Branching Frequency / 1000C (SCB2) 0.7 0.9 0.4 0.0 0.0 Estimated Density (g / cm3) (eq. 2) 0.9628 0.9568 0.9579 Melting Index I2 (eq. 3) 11.9 21.3 15.6 16.2 33.4 3rd ETHYLENE POLYMER (R2 Simulation -AFT+Trim) Kinetic Model (R3) Kinetic Model (R3) Ziegler-Natta Ziegler-Natta Weight Fraction (%) 8% 7% Mn 16,100 14,800 Mw 40,400 34,700 Mz Polydispersity Index (Mw / Mn) 2.5 2.3 Branching Frequency / 1000C (SCB2) 0.0 0.0 Estimated Density (g / cm3) 0.9515 0.9522. 104 zQOfrnn / zznz / E / YiAi Table 3: Resin Characteristics Example (1) Example (2) Example (3) Comparative Example 1 (Ex. 73 of US 9,695,309) Comparative Example 2 (Ex. 71 of US 9,695,309) Comp. Example 3 Freq. Branching / 1000C (FTIR) 0.9 3.4 1.1 2.0 2.0 0.6 Comonomer ID octene octene octene octene octene octene Molar % of comonomer 0.2 0.7 0.2 0.4 0.4 0.1 Weight % of comonomer 0.7 2.7 0.8 1.6 1.6 0.5 Internal Unsaturation / 100C (FTIR) 0.001 0.001 0.001 0.001 0.001 0.001 Side Chain Unsaturation / 100C 0.002 0.001 0.002 0.002 0.001 0.002 Terminal Unsaturation / 100C (FTIR) 0.061 0.064 0.047 0.047 0.048 0.06 Total unsaturation / 100C (FTIR) 0.064 0.066 0.050 0.050 0.050 Mn (GPC) 22,983 24,268 19,684 26,026 26,051 24,828 Mw(GPC) 105,018 109,673 106,535 100,009 94,966 96,786 Mz(GPC) 314,217 384,584 335,419 274,043 265,760 301,876 Polydispersity index (Mw / Mn) 4.6 4.5 5.4 3.8 3.6 3.9 index (Mz / Mw) 3.0 3.5 3.1 2.7 2.8 3.1 C-TREF CDBI (50) 77.7 74.9 82.5 80.2 83.2 PSP2 (Buck et al. CPChem) based on the distribution profile of 6.4 7.8 3.1 3.7 PSP2 (Buck et al. CPChem) based on Branching content (FTIR) 5.7 5.6 4.6 4.5 Dilution index Yd -2.60 -3.98 -0.61 -0.68 Dimensionless Modulus Xd = log(Gc / Gr) -0.18 -0.19 -0.11 -0.16. 105 zQOfrnn / zznz / E / YiAi Table 3 continued Example Comp. 4 (Ex. #3 in US 9,982,077) Example Comp. 5 Example Comp. 6 Example Comp. 7 Example Comp. 8 Branching Frequency / 1000C (FTIR) 1.2 1.9 2.7 2.4 2.5 Comonomer ID octene octene octene octene hexene Comonomer Molal % 0.2 0.4 0.5 0.5 0.5 Comonomer Weight % 0.9 1.5 2.1 1.9 1.5 Internal Unsaturation / 100C (FTIR) 0.11 0.14 0.12 0 Side Chain Unsaturation / 100C 0 0 0 0 Terminal Unsaturation / 1000C (FTIR) 0.08 0.11 0.08 0.02 Unsaturation total / 100C (FTIR) 0.19 0.25 0.20 0.02 Mn (GPC) 35,000 27,000 28,500 10,375 10,189 Mw (GPC) 102,000 86,000 89,500 94,834 105,947 Mz (GPC) 264,000 221,500 250,000 283,975 499,610 Polydispersity index (Mw / Mn) 2.9 3.2 3.1 9.1 10.4 index (Mz / Mw) 2.6 2.6 2.8 3.0 4.7 C-TREF CDBI (50) 92.6 87.6 88.2 71.6 PSP2 (Buck et al. CPChem) based on the Branching Distribution Profile GPC-FTIR 2.8 4.8 5.7 8.2 PSP2 (Buck et al. CPChem) based on the Branching Content (FTIR) 4.5 4.1 6.2 7.8 Dilution index Yd -4.76 0.02 Dimensionless Module Xd = log(Gc / Gr) -0.27 -0.11. 106 zQOfrnn / zznz / E / YiAi Table 4: Results of GPC Measurements Example (1) Example (2) Example (3) Comparative Example 1 (Ex. 73 of US 9,695,309) Comparative Example 2 (Ex. 71 of 9,695,309) Comp. Example 3 GPC-RI TEST RESULTS Mn 22,983 24,268 19,684 26,026 26,051 24,828 Mw 105,018 109,673 106,535 100,009 94,966 96,786 Mz 314,217 384,584 335,419 274,043 265,760 301,876 Polydispersity Index (Mw / Mn) 4.6 4.5 5.4 3.8 3.7 3.9 Index (Mz / Mw) 3.0 3.5 3.1 2.7 2.8 3.1 Weight fraction with logMW < 4 9.4% 9.4% 8.8% 8.6% 8.6% 8.9% Weight fraction with logMW > 5 29.6% 27.9% 28.8% 30.3% 28.1% 25.2% Table 4 Results of GPC Measurements - Continued Example Comp. 4 (Ex. #3 in US 9,982,077) Example Comp. 5 Example Comp. 6 Example Comp. 7 GPC-RI TEST RESULTS Mn 35,108 26,927 28,464 10,375 Mw 102,082 86,123 89,339 94,834 Mz 264,139 221,664 250,256 283,975 Polydispersity Index (Mw / Mn) 2.9 3.2 3.1 9.1 Index (Mz / Mw) 2.6 2.6 2.8 3.0 Weight fraction with logMW < 4 4.1% 6.8% 5.9% 25.2% Weight fraction with logMW > 5 28.6% 25.1% 25.1% 32.2% 107 zoofrnn / zznz / E / YiAi Table 5 Example (1) Example (2) Example (3) Comparative Example 1 (Ex. 73 of US 9,695,309) Comparative Example 2 (Ex. 71 of 9,695,309) Comp. Example 3 Flexural Properties Seq. Mod. of Flexure at 1% (MPa) 1271 1191 1154 1292 Dev. of Seq. Mod. of Flexure at 1% (MPa) 23 12 12 12 Environmental Stress Cracking Resistance Cond. ESCR A10 (hrs) 10% CO-630 99-163 104 83 103 49 Cond. ESCR B10 (hrs) 10% CO-630 92 343 92 79 84 30 Cond. ESCR A100 (hrs) 100% CO-630 >1000 >1000 568 > 1000 >1000 163 Cond. ESCR B100 (hrs) 100% CO-630 556 >1000 860 > 1000 > 1000 97 Impact Performance (plate test) IZOD Impact m-kg / cm (ft.lb / in) 0.1905 (3.5) 0.3647 (6.7) 0.1905 (3.5) 0.1034 (1.9) Tensile Impact m-kg / cm2 (ft.lb / in2) 4.009 (187.1) 3.131 (146.2) 4.401 (205.4) 2.229 (104) Low Temperature ARM Impact Performance not evaluated Average Failure Energy m-kg (ft.lb) under optimum conditions 23.71- 23.09 (171.5- 167.0) 14.83- 9.77 (107.3- 70.7) 19.08-24.33 (138-176) 21.84(158) Ductility (%) under optimum conditions 100-82 90-91 90-70 100 As is the density (g / cm3) under optimum conditions 0.950- 0.954 0.948 - 0.954 0.946 - 0.949 0.9463 Oven time at oven temperature of 293.33°C (560°F) (minutes) 24-26 24-26. 108 Table 5 Continued Example Comp. 4 (Ex. #3 in US 9,982,077) Example Comp. 5 Example Comp. 6 Example Comp. 7 Example Comp. 8 Flexural Properties Secondary Modulus of Flexure at 1% (MPa) 1202 1057 1005 1399 Deviation of Secondary Modulus of Flexure at 1% (MPa) 24 25 20 33 Environmental Stress Cracking Resistance Cond. ESCR A10 (hrs) 10% CO-630 800 Cond. ESCR B10 (hrs) 10% CO-630 176 189 Cond. ESCR A100 (hrs) 100% CO-630 120 80 >1000 Cond. ESCR B100 (hrs) 100% CO-630 112 141 >1000 Impact Performance (plate test) IZOD Impact nvkg / cm (ft.lb / in) 0.1469 (2.7) 0.0925 (1.7) 0.0762 (1.4) Tensile Impact nvkg / cm2 (ft.lb / in2) 4.854 (226.5) 4.796 223.8 2.623 (122.4) Low Temperature ARM Impact Performance Average Failure Energy nvkg (ft.lb) under optimum conditions 25.577(185) 25.577 (185) 25.991 (188) 9.954 - 5.046 (72.0- 36.5) 0-0 Ductility (%) under optimum conditions 92 100 100 0-0 0-0 As is the density (g / cm3) under optimum conditions 0.952 0.9488 0.9464 0.953- 0.956 0.957 - 0.958 Oven time at oven temperature of 293.33°C (560°F) (minutes) 22-24 24-26. 109 INDUSTRIAL APPLICABILITY High-density linear polyethylene with high tenacity and high resistance to environmental stress cracking. It is hereby stated that, as of this date, the best method known to the applicant for putting the aforementioned invention into practice is the one that is clear from the present description of the invention.< / rg> < / rg>

Claims

1. An interpolymer product, characterized in that it comprises: a first ethylene interpolymer including ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer including ethylene and an α-olefin wherein the second ethylene interpolymer includes an Mw less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product includes an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 90 hours.

2. The interpolymer product according to any of the preceding claims, characterized in that the density of the interpolymer product is 0.940.97 g / cm3; the density of the interpolymer product is 0.945-0.965 g / cm3; or the density of the interpolymer product is 0.947-0.955 g / cm3.

3. The interpolymer product according to claim 1, characterized in that the ESCR of the interpolymer product is 90 to 500 hours; or the ESCR of the interpolymer product is 100 to 400 hours.

4. The interpolymer product according to any of the preceding claims, characterized in that the IZOD impact strength of the interpolymer product is greater than 0.10 m-kg / cm (2 ft.lb / in); the IZOD impact strength of the interpolymer product is 0.10-0.54 m-kg / cm (2 to 10 ft.lb / in); or the IZOD impact strength of the interpolymer product is 0.10-0.27 m-kg / cm (2-5 ft.lb / in).

5. The interpolymer product according to any of the preceding claims, characterized in that it comprises a tensile impact greater than (140 ft.lb / in2); or a tensile impact of (140-350 ft.lb / in2).

6. The interpolymer product according to any of the preceding claims, characterized in that it comprises a melt index (I2) greater than 0.5 g / 10 min; a melt index (I2) of 0.8-8 g / 10 min; or a melt index (I2) of 0.8-5 g / 10 min.

7. The interpolymer product according to any of the preceding claims, characterized in that it comprises a melt flow ratio, I21 / I2Z, of 30-70; or a melt flow ratio, I21 / I2, of 35-60.

8. The interpolymer product according to any of the preceding claims, characterized in that it comprises a flexural modulus (1% secant) of at least 1000 MPa; or a flexural modulus (1% secant) of 1,100-1,500 MPa.

9. The interpolymer product according to any of the preceding claims, characterized in that it comprises a total vinyl unsaturation greater than 0.02 vinyl groups per 1,000 carbon atoms; or a total vinyl unsaturation of 0.02-1.0 vinyl groups per 1,000 carbon atoms.

10. The interpolymer product according to any of the preceding claims, characterized in that it comprises a long-chain branching frequency of 0.

11. The interpolymer product according to any of the preceding claims, characterized in that it comprises a short chain branching frequency of 0.55.0; a short chain branching frequency of 0.5 to zQOfrnn / zznz / E / YiAi 2.9; or 113 a short chain branching frequency of 3.04.

0.

12. The interpolymer product according to any of the preceding claims, characterized in that it comprises a CDBI5q greater than 70%; or a CDBI50 of 70-90%.

13. The interpolymer product according to any of the preceding claims, characterized in that the α-olefin comprises a C3-C12 α-olefin or a combination thereof; the α-olefin comprises an aolefin selected from 1-hexene, 1-octene or a mixture thereof; the α-olefin includes 1-hexene; or the α-olefin includes 1-octene.

14. The interpolymer product according to any of the preceding claims, characterized in that the α-olefin includes 0.05-5 mol% of the interpolymer product; the α-olefin includes 0.1-5 mol% of the interpolymer product; the α-olefin includes 0.5-3.0 mol% of the interpolymer product; the α-olefin includes 0.5-1.5 mol% of the interpolymer product; the α-olefin includes 0.1-0.5 mol% of the interpolymer product; the α-olefin includes 2.7 mol% of the interpolymer product; or the α-olefin includes 0.7 mol% of the interpolymer product.

15. The interpolymer product according to any of the preceding claims, characterized in that it comprises a number-average molecular weight (Mn) of 12,000 to 45,000; a number-average molecular weight (Mn) of 15,000 to 40,000; or a number-average molecular weight (Mn) of 20,000 to 30,000.

16. The interpolymer product according to any of the preceding claims, characterized in that it comprises an average molecular weight z (Mz) of 280,000-500,000; or an average molecular weight z (Mz) of 305,000-400,000.

17. The interpolymer product according to any of the preceding claims, characterized in that it comprises a polydispersity (Mw / Mn) of 3-7; zoofrnn / zznz / E / YiAi 115 a polydispersity (Mw / Mn) of 4-7.

18. The interpolymer product according to any of the preceding claims, characterized in that it comprises a dilution index, Yd, >-1.0; a dilution index, Yd, less than 0; or a dilution index, Yd, from -10 to 0.

19. The interpolymer product according to any of the preceding claims, characterized in that it comprises a primary structure parameter (PSP2) of 2 to 8.9 as determined by the GPC-FTIR branching distribution profile; a primary structure parameter (PSP2) of 4 to 8 determined by the GPC-FTIR branching distribution profile; a primary structure parameter (PSP2) of 2 to 8.9 determined by the branching content (FTIR); or a primary structure parameter (PSP2) of 4 to 8 determined by the branching content (FTIR).

20. The interpolymer product according to any of the preceding claims, characterized in that it comprises, based on the total weight percentage of the interpolymer product: 10-45% by weight of the first interpolymer; and 55-90% by weight of the second interpolymer.

21. The interpolymer product according to any of the preceding claims, characterized in that it comprises, based on the total weight percentage of the interpolymer product: 10-40% by weight of the first interpolymer; and 60-90% by weight of the second interpolymer.

22. The interpolymer product according to any of the preceding claims, characterized in that it comprises, based on the total weight percentage of the interpolymer product: 15-30% by weight of the first interpolymer; and 70-85% by weight of the second interpolymer.

23. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises 10-45% by weight of the interpolymer product; 10-35% by weight of the interpolymer product; or 15-30% by weight of the interpolymer product.

24. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises an Mw of 200,000-500,000; an Mw of 230,000-450,000; or an Mw of 250,000-400,000. zQOfrnn / zznz / E / YiAi 117 25. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises an Mn of 100,000-200,000; or an Mn of 120,000-180,000.

26. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises an Mz of 320,000 to 650,000; or an Mz from 350,000-545,000.

27. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises a polydispersity (Mw / Mn) of 1.0-3.0; or a polydispersity (Mw / Mn) of 1.75-2.

7.

28. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises a short-chain branching frequency of 1.05.0; or a short-chain branching frequency of 1.33.

5.

29. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises zoofrnn / zznz / E / YiAi 118 a melt index (I2) of up to 0.4 g / 10 min; or a melt index (I2) of 0.0001-0.4 g / 10 min; or a melt index (I2) of 0.001-0.1 g / 10 min.

30. The interpolymer product according to any of the preceding claims, characterized in that the first interpolymer comprises a density of 0.90-0.93; or a density of 0.910-0.929 g / cm3.

31. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises 55-90% by weight of the interpolymer product; or 65-90% by weight of the interpolymer product; or 70-85% by weight of the interpolymer product.

32. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises an Mw of 30,000-70,000; or an Mw of 40,000-60,000.

33. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises an Mn of 10,000-30,000; an Mn of 12,000-25,000.

34. The interpolymer product according to zoofrnn / zznz / E / YiAi 119 any of the preceding claims, characterized in that the second interpolymer comprises an Mz of 70,000 to 125,000; or an Mz of 80,000 to 115,000.

35. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises a polydispersity (Mw / Mn) of 2.0-7.0; or a polydispersity (Mw / Mn) of 2.5-5.

0.

36. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises a short-chain branching frequency of 0.011.5; a short-chain branching frequency of 0.01 to 1.0; or a short-chain branching frequency of 0.11.

5.

37. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises a melt rate of 1-500 g / 10 min; or a melt rate of 5-200 g / 10 min; a melt rate of 1-50 g / 10 min; or a melt rate of 10-100 g / 10 min. zQOfrnn / zznz / E / YiAi 120 38. The interpolymer product according to any of the preceding claims, characterized in that the second interpolymer comprises a density of 0.93-0.98; or a density of 0.95 to 0.

97.

39. The interpolymer product according to any of the preceding claims, characterized in that it comprises: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) of 300,000 to 450,000 and a density of 0.900 to 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw of 30,000 to 70,000 and a density of 0.930 to 0.980; and wherein the interpolymer product has: an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, 10% IGEPAL CO-630, of more than 90 hours; an IZOD impact strength of 0.16–0.27 m-kg / cm² (3.0 to 5.0 ft.lb / in²); a density of 0.945–0.960; a melt index of 0.9–3.0; and a melt flow ratio, I₂₁ / I₂₂Z, of 35–65. zQOfrnn / zznz / E / YiAi 121 40. The interpolymer product according to any of the preceding claims, characterized in that it comprises: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 210,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product comprises: an ambient stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 200 hours; an IZOD impact strength of 0.27 to 0.43 m-kg / cm (5.0 to 8.0 ft.lb / in); a density of 0.945-0.955; a melting index of 0.9 to 5.0; and a melting flux ratio, I21 / I2 / of 40-65.

41. The interpolymer product according to any of the preceding claims, characterized in that it comprises: an environmental stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL zQOfrnn / zznz / E / YiAi 122 CO-630 at 10%, of more than 300 hours; an IZOD impact strength of 0.27 to 0.43 m-kg / cm (5.0 to 8.0 ft.lb / in); a density of 0.945-0.953; a melt index of 1.0-2.0; and a melt flow ratio, I21 / I2Z, of 45-60.

42. An interpolymer product according to any of the preceding claims, characterized in that: an environmental stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, of more than 90 hours; an IZOD impact strength of 0.16-0.27 m-kg / cm (3.0 to 5.0 ft.lb / in); a density of 0.947-0.960; a melt index of 0.9-3.0; and a melt flow ratio, I21 / I2, of 35-65.

43. A rotomolded article according to any of the preceding claims comprising a wall structure including at least one layer comprising an ethylene interpolymer product, characterized in that it comprises: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3, and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm3; and wherein the interpolymer product has an environmental stress cracking resistance (ESCR), measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, greater than 90 hours.

44. The rotomolded article according to any of the preceding claims, characterized in that it is selected from a toy, a wastebasket, a container, a helmet, a boat, or a large tank.

45. A closure for a bottle, characterized in that it comprises: a first ethylene interpolymer comprising ethylene and an α-olefin having a weight average molecular weight (Mw) greater than 200,000 and a density less than 0.930 g / cm3; and a second ethylene interpolymer comprising ethylene and an α-olefin wherein the second ethylene interpolymer has an Mw less than 70,000 and a density greater than 0.930 g / cm3, and wherein the interpolymer product comprises an environmental stress cracking resistance (ESCR), zQOfrnn / zznz / E / YiAi 124 measured in accordance with ASTM D1693, Condition B, IGEPAL CO-630 at 10%, of more than 90 hours.

46. ​​The closure in accordance with any of the preceding claims, characterized in that it is 5 made by compression molding or injection molding.

47. The closure in accordance with any of the preceding claims, characterized in that it comprises a screw cap.