Title of Invention	DUAL REACTOR ETHYLENE POLYMERIZATION PROCESS
Abstract	A dual reactor process for the solution and (co)polymerization of ethylene uses two different types of catalysts in the two reactors, A catalyst having a phosprttnimine ligand is used in the first reactor. A Ziegler Nafta catalyst is used in the second reactor. The process of this invention is comparatively easy to control and may be used to produce polyethylene products having a broad molecular weight distribution. Linear tow density produced according to this invention is well suited for the manufacture of molded goods and plastic films.

Title of Invention

DUAL REACTOR ETHYLENE POLYMERIZATION PROCESS

Abstract

A dual reactor process for the solution and (co)polymerization of ethylene uses two different types of catalysts in the two reactors, A catalyst having a phosprttnimine ligand is used in the first reactor. A Ziegler Nafta catalyst is used in the second reactor. The process of this invention is comparatively easy to control and may be used to produce polyethylene products having a broad molecular weight distribution. Linear tow density produced according to this invention is well suited for the manufacture of molded goods and plastic films.

Full Text	DUAL REACTOR ETHYLENE POLYMERIZATION PROCESS TECHNICAL HELD This invention relates to the solution polymerization of ethylene in two reactors using two different catalyst systems. BACKGROUND ART The use of so-called "single-site" catalysts such as metallocene catalysts to prepare polyethylene having a narrow molecular weight distribution is well known. The "linear low density polyethylene" (or "LLDPE", a copolymer of ethylene and a higher alpha olefin) prepared with such catalysts typically exhibits a very uniform composition distribution (i.e. the comonomer is very uniformly distributed within the polymer chains). The combination of narrow molecular weight distribution and uniform composition distribution distinguishes these polymers from "conventional" LLDPE which is commercially manufactured with a Ziegler Natta catalyst or a chromium catalyst. In particular, the conventional LLDPE products have a broader molecular weight distribution and a broader composition distribution. These compositional differences are manifested in the form of differences in the physical properties of the two types of LLDPE polymers. Most notably, LLDPE prepared with a single site catalyst has improved impact strength and optical properties in comparison to "conventional" LLDPE. However, one advantage of the "conventional" LLDPE is that it is usually easier to "process" in its existing mixers and extruders. Accordingly, it would be highly desirable to prepare LLDPE products which possess the improved physical properties offered by single site catalysts and retain the broad molecular weight distribution (for improved processability) which is associated with conventional LLDPE. One approach which has been used to achieve this object is the use of mixed catalyst systems. For example, United States Patent (USP) 4,530,914 (Ewen et al, to Exxon) teaches the use of two different metallocenes and USP 4,701,432 (Welborn, to Exxon) teaches the use of a supported catalyst prepared with a metallocene catalyst and a Ziegler 2 Natta catalyst. Many others have subsequently attempted to use similar mixed catalyst systems as may be quickly ascertained by reviewing the patent literature. However, the use of "mixed" catalyst systems is often associated with operability problems. For example, the use of two catalysts on a single support (as taught by Welborn in USP 4,701,432) may be associated with a reduced degree of process control flexibility (e.g. If the polymerization reaction is not proceeding as desired when using such a catalyst system, it is difficult to establish which corrective action should be taken as the corrective action will typically have a different effect on each of the two different catalyst components). Moreover, the two different catalyst/cocatalyst systems may interfere with one another - for example, the organoaluminum component which is often used in Ziegler Natta or chromium catalyst systems may "poison" a metallocene catalyst. Accordingly, a "mixed catalyst" process which mitigates some of these difficulties would be a useful addition to the art. DISCLOSURE OF INVENTION The present invention provides a medium pressure solution polymerization process characterized by: A) polymerizing ethylene, optionally with one or more C3-12 alpha olefins, in solvent in a first polymerization reactor at a temperature of from 80 to 200°C and a pressure of from 500 to 8,000 pounds per square inch gauge ("psi") in the presence of (a) a first catalyst which is an organometallic complex of a group 4 or 5 metal that is characterized by having at least one phosphinimine ligand; and (b) a first cocatalyst; and B) passing said first polymer solution into a second polymerization reactor and polymerizing ethylene, optionally with one or more C3.12 alpha olefins, in said second stirred polymerization reactor at a higher polymerization temperature than that of said first reactor in the presence of a Ziegler Natta catalyst, wherein said Ziegler Natta catalyst comprises a transition metal compound of a transition metal selected from 3 groups 3, 4 or 5 of the Periodic Table (using IUPAC nomenclature) and an organoaluminum component which is defined by the formula: AI(X')a(OR)b (R)c wherein: X' is a halide (preferably chlorine); OR is an alkoxy or aryloxy group; R is a hydrocarbyl (preferably an alkyl having from 1 to 10 carbon atoms); and a, b, or c are each 0, 1, 2 or 3 with the provisos that a+b+c=3 and b+c>1. Thus, the process of the present invention requires two solution polymerization reactors and two distinct catalyst systems. The first catalyst must have a phosphinimine ligand (and, hence, is sometimes referred to herein as a "phosphinimine catalyst" or "PIC"). The first reactor uses the "phosphinimine catalyst". Conventional process control techniques may be used to operate the first reactor as there is only one catalyst to deal with. Preferred phosphinimine catalysts for use in the first reactor are titanium species which contain one cyclopentadienyl ligand, one phosphinimine ligand and two chloride ligands. It is particularly preferred that the concentration of titanium in the first reactor be less that 1 part per million (ppm) especially less that 0.5 ppm (based on the weight of titanium divided by the weight of the reactor contents). Exemplary cocatalysts for the phosphinimine catalyst are alumoxanes and/or ionic activators. Preferred cocatalysts for the phosphinimine catalyst are a combination of: 1) an alumoxane (in which the Al/Ti molar ratio, based on the alumoxane and the titanium in the phosphinimine catalyst is between 10/1 and 200/1, most preferably from 40/1 to 120/1); and 2) a boron-containing ionic activator (in which the B/Ti ratio, based on the boron in the ionic activator to the titanium in the phosphinimine catalyst is between 0.5/1 and 1.5/1). 4 The polymer solution from the first reactor is transferred to the second solution polymerization reactor. A Ziegler Natta catalyst is used ir the second reactor. It is preferred that the Ziegler Natta catalyst contains at least one transition metal selected from titanium and vanadium, and that the molar concentration of titanium/vanadium which is added to the second reactor is at least 10 times greater than the titanium concentration in the first reactor. Thus, the second polymerization reactor must use a Ziegler Natta catalyst. Additionally, the second polymerization reactor must be operatet at a higher temperature from the first - most preferably, at least 30°C higher than the first. While not wishing to be bound by any particular theory, it is believed that the reactor conditions in the second reactor "overwhelm" the catalyst from the first reactor (i.e. for process control purposes, any residual catalyst from the first reactor is not a concern in the second reactor). This is desirable from a process operability perspective as it reduces the number of variables which need to be considered when controlling the polymerization reaction in the second reactor. BEST MODE FOR CARRYING OUT THE INVENTION Part 1. Description of First Catalysts The catalyst used in the first reactor of the process of this invention ("first catalyst") is an organometallic complex of a group 4 or 5 metal which is characterized by having at least one phosphinimine ligand (where the term phosphinimine is defined in section 1.2 below). Any such organometallic having a phosphinimine ligand which displays catalytic activity for ethylene polymerization may be employed. Preferred first catalysts are defined by the formula: wherein M is a transition metal selected from Ti, Hf and Zr (as described in section 1.1 below); PI is a phosphinimine ligand (as described in section 5 1.2 below); L is a monanionic ligand which is a cyclopentadienyl-type Ijgand or a bulky heteroatom ligand (as described in section 1.3 below); X is an activatable ligand which is most preferably a simple monanionic ligand such as alkyl or a halide (as described in section 1.4 below); m is 1 or 2, n is 0 or 1, and p is fixed by the valence of the metal M. The most preferred first catalysts are group 4 metal complexes in the highest oxidation state. For example, a preferred catalyst may be a bis (phosphinimine) dichloride complex of titanium, zirconium or hafnium. However, it is particularly preferred that the first catalyst contain one phosphinimine ligand, one "L" ligand (which is most preferably a cyclopentadienyl - type ligand) and two "X" ligands (which are preferably both chloride). 1.1 Metals The first catalyst is an organometallic complex of a group 4 or 5 metal (where the numbers refer to columns in the Periodic Table of the Elements using IUPAC nomenclature). The preferred metals are from group 4, (especially titanium, hafnium or zirconium) with titanium being most preferred. 1.2 Phosphinimine Liqand The first catalyst must contain a phosphinimine ligand which is covalently bonded to the metal. This ligand is defined by the formula: wherein each R is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical, and a silyl radical of the formula: -Si-(R2)3 6 wherein each R2 is independently selected from the group consisting of hydrogen, a C1-8 alkyl or alkoxy radical, C6-10 aryl or aryloxy radicals, and a germanyl radical of the formula: Ge-(R2)3 wherein R2 is as defined above. The preferred phosphinimines are those in which each R1 is a hydrocarbyl radical. A particularly preferred phosphinimine is tri-(tertiary butyl) phosphinimine (i.e. where each R1 is a tertiary butyl group). 1.3 Ligand L Preferred first catalysts are group 4 organometallic complexes which contain one phosphinimine ligand (as described in section 1.2 above) and one ligand L (as described in sections 1.3.1 to 1.3.6) which is either a cyclopentadienyl-type ligand or a heteroligand. 1.3.1 Cvclopentadienvl-type Liqands As used herein, the term cyclopentadienyl-type ligand is meant to convey its conventional meaning, namely a ligand having a five carbon ring which is bonded to the metal via eta-5 bonding. Thus, the term "cyclopentadienyl-type" includes unsubstituted cyclopentadienyl, substituted cyclopentadienyl, unsubstituted indenyl, substituted indenyl, unsubstituted fluorenyl and substituted fluorenyl. An exemplary list of substituents for a cyclopentadienyl ligand includes the group consisting of C1-10 hydrocarbyl radical (which hydrocarbyl substituents are unsubstituted or further substituted); a halogen atom, C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical; an amido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; a phosphido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; silyl radicals of the formula -Si-(R)3 wherein each R is independently selected from the group consisting of hydrogen, a C1-8 alkyl or alkoxy radical C6-10 aryl or aryloxy radicals; germanyl radicals of the formula Ge-(R2)3 wherein R is as defined directly above. 7 1.3.2 Heteroliqand As used herein, the term "heteroligand" refers to a ligand which contains at least one heteroatom selected from the group consisting of boron, nitrogen, oxygen, phosphorus or sulfur. The heteroligand may be sigma or pi-bonded to the metal. Exemplary heteroligands are described in sections 1.3.2.1 to 1.3,2.6 below. 1.3.2.1 Ketimide Liqands As used herein, the term "ketimide ligand" refers to a ligand which: (a) is bonded to the transition metal via a metal-nitrogen atom bond; (b) has a single substituent on the nitrogen atom, (where this single substituent is a carbon atom which is doubly bonded to the N atom); and (c) has two substituents (Sub 1 and Sub 2, described below) which are bonded to the carbon atom. Conditions a. b and c are illustrated below: The substituents "Sub 1 and Sub 2" may be the same or different. Exemplary substituents include hydrocarbyls having from 1 to 20 carbon atoms; silyl groups, amido groups and phosphido groups. For reasons of cost and convenience it is preferred that these substituents both be hydrocarbyls, especially simple alkyls and most preferably tertiary butyl. 1.3,2.2 Silicone-Containinq Heteroliqands These ligands are defined by the formula: - (p)SiRxRyRz where the - denotes a bond to the transition metal and u is sulfur or oxygen. The substituents on the Si atom, namely Rx, Ry and Rz are required in order to satisfy the bonding orbital of the Si atom. The use of any particular substituent Rx, Ry or Rz is not especially important to the 8 success of this Invention. It is preferred that each of Rx, Ry and Rz is a C1-2 hydrocarbyl group (i.e. methyl or ethyl) simply because such materials are readily synthesized from commercially available materials). 1.3.2.3 Amido Liqands The term "amido" is meant to convey its broad, conventional meaning. Thus, these ligands are characterized by (a) a metal-nitrogen bond, and (b) the presence of two substituents (which are typically simple alkyl or silyl groups) on the nitrogen atom. 1.3.2.4 Alkoxy Liqands The term "alkoxy" is also intended to convey its conventional meaning. Thus, these ligands are characterized by (a) a metal oxygen bond, and (b) the presence of a hydrocarbyl group bonded to the oxygen atom. The hydrocarbyl group may be a ring structure and/or substituted (e.g. 2, 6 di-tertiary butyl phenoxy). 1.3.2.5 Boron Heterocvclic Liqands These ligands are characterized by the presence of a boron atom in a closed ring ligand. This definition includes heterocyclic ligands which also contain a nitrogen atom in the ring. These ligands are well known to those skilled in the art of oleffn polymerization and are fully described in the literature (see, for example, USPs' 5,637,659; 5,554,775 and the references cited therein). 1.3.2,6 Phosphole Liqands The term "phosphole" is also meant to convey its conventional meaning. "Phospholes" are cyclic dienyl structures having four carbon atoms and one phosphorus atom in the closed ring. The simplest phosphole is C4PI14 (which is analogous to cyclopentadiene with one carbon in the ring being replaced by phosphorus). The phosphole ligands may be substituted with, for example, C1-20 hydrocarbyl radicals (which may, optionally, contain halogen substituents); phosphido radicals; amido radicals; silyl or alkoxy radicals. Phosphoie ligands are also well known to those skilled in the art of olefin polymerization and are described as such in USP 5,434,116. 9 1.4 Activatable Liqand The term "activatable ligand" refers to a ligand which may be activated by a cocatalyst, (also referred to as an "activator"), to facilitate olefin polymerization. Exemplary activatable ligands are independently selected from the group consisting of a hydrogen atom, a halogen atom, a C1-10 hydrocarbyl radical, a C1-10 atkoxy radical, a C5-10 aryl oxide radical; each of which said hydrocarbyl, alkoxy, and aryl oxide radicals may be unsubstituted by or further substituted by a halogen atom, a C1-8 alkyl radical, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; a phosphido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals. The number of activatable ligands depends upon the valency of the metal and the valency of the activatable ligand. The preferred first catalyst metals are group 4 metals in their highest oxidation state (i.e. 4+) and the preferred activatable ligands are monoanionic (such as a halide - especially chloride or a alkyl - especially methyl). Thus, the preferred first catalyst contains a phosphinimine ligand, a cyclopentadienyl ligand and two chloride (or methyl) ligands bonded to the group 4 metal. In some instances, the metal of the first catalyst component may not be in the highest oxidation state. For example, a titanium (III) component would contain only one activatable ligand. 1.5 Summary Description of Preferred Catalyst As previously noted, the preferred first catalyst is a group 4 organometallic complex in its highest oxidation state having a phosphinimine ligand, a cyclopentadienyl-type ligand and two activatable ligands. These requirements may be concisely described using the following formula for the preferred catalyst: 10 wherein: (a) M is a metal selected from Ti, Hf and Zr; (b) PI is a phosphinimine ligand defined by the formula: wherein each R1 is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryI or aryloxy radical, an amido radical, a silyl radical of the formula: -Si-(R2)3 wherein each R2 is independently selected from the group consisting of hydrogen, a C1-8 alky! or alkoxy radical, C6-10 aryl or aryloxy radicals, and a germanyl radical of the formula: Ge-(R2)3 wherein R2 is as defined above; (c) L is a ligand selected from the group consisting of cyclopentadienyl, substituted cyclopentadienyl, indenyl, substituted indenyl, fluorenyl, or substituted fluorenyl; and (d) X is an activatable ligand, and wherein: m is 1, n is 1 and p is 2. 2. Description of First Cocatalvst The catalyst components described in part 1 above are used in combination with at least one cocatalyst (or "activator") to form an active catalyst system for olefin polymerization as described in more detail in sections 2.1, 2.2 and 2.3 below. 2.1 Alumoxanes The alumoxane may be of the formula: (R4)2AIO{R4AIO)mAI(R4)2 wherein each R4 is independently selected from the group consisting of C1-20 hydrocarbyl radicals and m is from 0 to 50, preferably R4 is a C1-4 alkyl radical and m is from 5 to 30. Methylalumoxane (or "MAO") in which each R is methyl is the preferred alumoxane. 11 Alumoxanes are well known as cocatalysts, particularly for metallocene-type catalysts. Alumoxanes are also readily available articles of commerce. The use of an alumoxane cocatalyst generally requires a molar ratio of aluminum to the transition metal in the catalyst from 20:1 to 1000:1. Preferred ratios are from 50:1 to 250:1. 2.2 "Ionic Activators" as Cocatalvsts So-called "ionic activators" are also well known for metallocene catalysts. See, for example, USP 5,198,401 (Hlatky and Turner) and USP 5,132,380 (Stevens and Neithamer). Whilst not wishing to be bound by any theory, it is thought by those skilled in the art that "ionic activators" initially cause the abstraction of one or more of the activatable ligands in a manner which ionizes the catalyst into a cation, then provides a bulky, labile, non-coordinating anion which stabilizes the catalyst in a cationic form. The bulky, non-coordinating anion coordinating anion permits olefin polymerization to proceed at the cationic catalyst center (presumably because the non-coordinating anion is sufficiently labile to be displaced by monomer which coordinate to the catalyst). Preferred ionic activators are boron-containing ionic activators described in (i) - (iii) below: (i) compounds of the formula [R5]+ [B(R7)4] wherein B is a boron atom, R5 is a aromatic hydrocarbyl (e.g. triphenyl methyl cation) and each R7 is independently selected from the group consisting of phenyl radicals which are unsubstituted or substituted with from 3 to 5 substituents selected from the group consisting of a fluorine atom, a C1-4 alkyl or alkoxy radical which is unsubstituted or substituted by a fluorine atom; and a silyl radical of the formula -Si-(R9)3; wherein each R9 is independently selected from the group consisting of a hydrogen atom and a C1-4 alkyl radical; and (ii) compounds of the formula [(R8)tZH]+[B(R7)4] wherein B is a boron atom, H is a hydrogen atom, Z is a nitrogen atom or 12 phosphorus atom, t is 2 or 3 and R8 is selected from the group consisting of C1-8 alkyl radicals, a phenyl radical which is unsubstituted or substituted by up to three C1-4 alkyl radicals, or one R8 taken together with the nitrogen atom may form an anilinium radical and R7 is as defined above; and (iii) compounds of the formula B(R7)3 wherein R7 is as defined above. In the above compounds preferably R7 is a pentafluorophenyl radical, and R5 is a triphenylmethyl cation, Z is a nitrogen atom and R8 is a C1-4 alkyl radical or R8 taken together with the nitrogen atom forms an anilium radical which is substituted by two C1-4 alkyl radicals. The "ionic activator" may abstract one or more activatable ligands so as to ionize the catalyst center into a cation but not to covalently bond with the catalyst and to provide sufficient distance between the catalyst and the ionizing activator to permit a polymerizable olefin to enter the resulting active site. Examples of ionic activators include: triethylammonium tetra(phenyl)boron, tripropylammonium tetra(phenyl)boron, tri(n-butyl)ammonium tetra(phenyl)boron, trirnethylamrnoniurn tetra(p-tolyl)boron, trimethylammonium tetra(o-tolyl)boron, tributylammonium tetra(pentafluorophenyl)boron, tripropylammonium tetra(o,p-dimethylphenyl)boron, tributylammonium tetra(m,m-dimethyiphenyl)boron, tributylammonium tetra(p-trifluoromethylphenyl)boron, tributylammonium tetra(pentafluorophenyl)boron, tri(n-butyl)ammonium tetra(o-tolyl)boron, N,N-dimethylanilinium tetra(phenyl)boron, N.N-diethylanilinium tetra(phenyl)boron, N.N-diethylanilinium tetra(phenyl)n-butylboron, 13 N,N-2,4,6-pentamethylanJIiniumtetra(phenyl)boron" di-(isopropyl)ammonium tetra(pentafluorophenyl)boron, dicyciohexytammoniumtetra(phenyl)boron, triphenylphosphonium tetra(phenyl)boron, tri(methyiphenyl)phosphoniumtetra(phenyl)boron, tri(dimethylphenyl)phosphoniumtetra{phenyl)boron, tropitlium tetrakispentafluorophenyl borate, triphenyimethyliurn tetrakispentafluorophenyl borate, benzene (diazonium) tetrakispentafluorophenyl borate, tropillium phenyltrispentafluorophenyl borate, triphenyimethyliurn phenyltrispentafluorophenyl borate, benzene (diazonium) phenyltrispentafluorophenyl borate, tropillium tetrakis (2,3,5,6-tetrafluorophenyf) borate, triphenylmethyiium tetrakis (2,3,5,6-tetrafluorophenyl) borate, benzene (diazonium) tetrakis (3,4,5-trifluorophenyl) borate, tropillium tetrakis (3,4,5-trifIuorophenyt) borate, benzene {diazonium) tetrakis {3,4,5-trifluorophenyl) borate, tropiliium tetrakis (1,2,2-trifluoroethenyl) borate, triphenyimethyliurn tetrakis (1,2,2-trifluoroethenyl) borate, benzene (diazonium) tetrakis (1,2,2-trifluoroethenyl) borate, tropillium tetrakis (2,3,4,5-tetrafluorophenyl) borate, triphenylmethyiium tetrakis (2,3,4,5-tetrafluorophenyl) borate, and benzene (diazonium) tetrakis (2,3,4,5-tetrafluorophenyl) borate. Readily commercially available ionic activators include; N,N- dimethylaniliniumtetrakispentafluorophenyl borate; triphenylmethylium tetrakispentafluorophenyl borate; and trispentafluorophenyl borane. 3. Description of Zieqler Natta Catalyst The term "Ziegler Natta catalyst" is well known to those skilled in the art and is used herein to convey its conventional meaning, A Ziegler Natta catalyst must be used in the second (hot) reactor of this invention. Ziegler Natta catalysts comprise at least one transition metal compound of 14 a transition metal selected from groups 3, 4, or 5 of the Periodic Table (using IUPAC nomenclature) and an organoaluminum component which is defined by the formula: AI(X')a (OR)b (R)c wherein: X' is a halide (preferably chlorine); OR is an alkoxy or aryloxy group; R is a hydrocarbyl (preferably an alkyl having from 1 to 10 carbon atoms); and a,b, or c are each 0, 1, 2, or 3 with the provisos text a+b+c=3 and b+c>1. It is highly preferred that the transition metal compounds contain at least one of titanium or vanadium. Exemplary titanium compounds include titanium halides (especially titanium chlorides, of which TiCI4 is preferred); titanium alkyls; titanium alkoxides (which may be prepared by reacting a titanium alkyl with an alcohol) and "mixed ligand" compounds (i.e. compounds which contain more than one of the above described halide, alkyl and alkoxide ligands). Exemplary vanadium compounds may also contain halide, alkyl or alkoxide ligands. In addition vanadium oxy trichloride ("VOCI3") is known as a Ziegler Natta catalyst component and is suitable for use in the present invention. It is especially preferred that the Ziegler Natta catalyst contain both of a titanium and a vanadium compound. The Ti/V mole ratios may be from 10/90 to 90/10, with mole ratios between 50/50 and 20/80 being particularly preferred. The above defined organoaluminum compound is an essential component of the Ziegler Natta catalyst. The mole ratio of aluminum to transition metal {for example, aluminum/(titanium + vanadium)} is preferably from 1/1 to 100/1, especially from 1.2/1 to 15/1. As will be appreciated by those skilled in the art of ethylene polymerization, conventional Ziegler Natta catalysts may also incorporate additional components such as an electron donor- for example an amine; or a magnesium compound - for example a magnesium alkyl such as butyl ethyl magnesium and a halide source (which is typically a chloride such as tertiary butyl chloride). 15 Such components, if employed, may be added to the other catalyst components prior to introduction to the reactor or may be directly added to the reactor. The Ziegler Natta catalyst may also be "tempered" (i.e. heat treated) prior to being introduced to the reactor (again, using techniques which are well known to those skilled in the art and published in the literature). 4. Description of Dual Reactor Solution Polymerization Process Solution processes for the (co)polymerization of ethylene are well known in the art. These processes are conducted in the presence of an inert hydrocarbon solvent typically a C5-12 hydrocarbon which may be unsubstituted or substituted by a C1-4 alkyl group, such as pentane, methyl pentane, hexane, heptane, octane, cyclohexane, methycyclohexane and hydrogenated naphtha. An example of a suitable solvent which is commercially available is "Isopar E" (C8-12 aliphatic solvent, Exxon Chemical Co.). . The solution polymerization process of this invention must use at least two polymerization reactors. The first polymerization reactor must operate at a lower temperature ("cold reactor") using a "phosphinimine catalyst" described in Part 1 above. The polymerization temperature in the first reactor is from about 80°C to about 180°C (preferably from about 120°C to 160°C) and the hot reactor is preferably operated at a higher temperature (up to about 300°C). Both reactors are preferably "stirred reactors" (i.e. the reactors are well mixed with a good agitation system). Preferred pressures are from about 500 psi to 8,000 psi. The most preferred reaction process is a "medium pressure process", meaning that the pressure in each reactor is preferably less than about 6,000 psi (about 42,000 kiloPascais or kPa), most preferably from about 1,500 psi to 3,000 psi (about 14,000-22,000 kPa) Suitable monomers for copolymerization with ethylene include C3-20 mono- and di- olefins. Preferred comonomers include C3-12 alpha olefins which are unsubstituted or substituted by up to two C1-6 alkyl radicals, C8-12 16 vinyl aromatic monomers which are unsubstituted or substituted by up to two substituents selected from the group consisting of C1-4 alkyl radicals, C4-12 straight chained or cyclic diolefins which are unsubstituted or substituted by a C1-4 alkyl radical. Illustrative non-limiting examples of such alpha-olefins are one or more of propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, and 1-decene, styrene, alpha methyl styrene and the constrained-ring cyclic olefins such as cyclobutene, cyclopentene, dicyclopentadiene norbornene, alkyl-substituted norbornes, alkenyl-substituted norbornes and the like (e.g. 5-methylene-2-norbomene and 5-ethylidene-2-norbornene, bicyclo-(2,2,1 )-hepta-2,5-diene). The polyethylene polymers which may be prepared in accordance with the present invention are LLDPE's which typically comprise not less than 60, preferably not less than 75 weight % of ethylene and the balance one or more C4-10 alpha olefins, preferably selected from the group consisting of 1-butene, 1-hexene and 1-octene. The polyethylene prepared in accordance with the present invention may be LLDPE having a density from about 0.910 to 0.935 g/cc or (linear) high density polyethylene having a density above 0.935 g/cc. The present invention might also be useful to prepare polyethylene having a density below 0.910 g/cc - the so-called very low density polyethylene and ultra low density polyethylenes (or "plastomers"). Generally the alpha olefin may be present in an amount from about 3 to 30 weight %, preferably from about 4 to 25 weight %. The present invention may also be used to prepare co- and ter-polymers of ethylene, propylene and optionally one or more diene monomers. Generally, such polymers will contain about 50 to about 75 weight % ethylene, preferably about 50 to 60 weight % ethylene and correspondingly from 50 to 25 weight % of propylene. A portion of the monomers, typically the propylene monomer, may be replaced by a conjugated diolefin. The diolefin may be present in amounts up to 10 weight % of the polymer although typically is present in amounts from about 3 to 5 weight %. The resulting polymer may have a composition 17 comprising from 40 to 75 weight % of ethylene, from 50 to 15 weight % of propylene and up to 10 weight % of a diene monomer to provide 100 weight % of the polymer. Preferred but not limiting examples of the dienes are dicyclopentadiene, 1,4-hexadiene, 5-methylene-2-norbornene, 5-ethylidene-2-norbomene and 5-vinyl-2-norbornene, especially 5-ethylidene-2-norbornene and 1,4-hexadiene. The monomers are dissolved/dispersed in the solvent either prior to being fed to the first reactor (or for gaseous monomers the monomer may be fed to the reactor so that it will dissolve in the reaction mixture). Prior to mixing, the solvent and monomers are generally purified to remove potential catalyst poisons such as water, oxygen or metal impurities. The feedstock purification follows standard practices in the art, e.g. molecular sieves, alumina beds and oxygen removal catalysts are used for the purification of monomers. The solvent itself as well (e.g. methyl pentane, cyclohexane, hexane or toluene) is preferably treated in a similar manner. The feedstock may be heated or cooled prior to feeding to the first reactor. Additional monomers and solvent may be added to the second reactor, and it may be heated or cooled. Generally, the catalyst components may be premixed in the solvent for the reaction or fed as separate streams to each reactor. In some instances premixing it may be desirable to provide a reaction time for the catalyst components prior to entering the reaction. Such an "in line mixing" technique is described in a number of patents in the name of DuPont Canada Inc (e.g. USP patent 5,589,555, issued December 31, 1996). The residence time in each reactor will depend on the design and the capacity of the reactor. Generally the reactors should be operated under conditions to achieve a thorough mixing of the reactants. In addition, it is preferred that from 20 to 60 weight % of the final polymer is polymerized in the first reactor, with the balance being polymerized in the second reactor. In a highly preferred embodiment, the first polymerization reactor has a smaller volume than the second polymerization reactor. On 18 leaving the reactor system the solvent is removed and the resulting polymer is finished in a conventional manner. Further details of the invention are illustrated in the following, non limiting, examples. EXAMPLES Continuous Solution Polymerization All the polymerization experiments described below were conductec using a continuous solution polymerization system. The process is continuous in all feed streams (solvent, monomers and catalyst) and in the removal of product. All feed streams were purified prior to the reactors by contact with various absorption media to remove catalyst killing impurities such as water, oxygen and polar materials as is known to those skilled in the art. All components were stored and manipulated under an atmosphere of purified nitrogen. The polymerization system included two reactors connected in series. The first reactor had an internal volume of 51 mL and was connected via tubing to a second reactor having an internal volume of 71.5 mL. It was possible to add monomers, solvent and/or catalysts to each of the reactors. The catalyst used in the first reactor was a titanium complex having one cyclopentadienyl ligand, one tri (tertiary butyl) phosphinimine ligand and two chloride ligands (i.e. "CpTi NP(tBu)3 Cl2"). This catalyst was used in all inventive experiments and is identified in Table 1 as "PIC" (for phosphinimine catalyst) The Ziegler Natta catalyst used in the second reactor was a mixed titanium/vanadium system using titanium tetrachloride ("TiCI4") and vanadium oxy trichloride ("VOCI3"). Triethyl aluminum ("AIEt3") was used as part of the Ziegler Natta catalyst system. The cocatalyst used in the first reactor was a combination of a boron-containing ionic activator and an alumoxane. (Note: the ionic activator used in experiments 1, 2, 3, 4, 5 and 6 was triphenylmethylium tetrakispentafluorophenyl borate or "Ph3CB(C6F5)4". The ionic activator 19 used in the remaining experiments was trispentafluorophenyl borane or "B(C6F5)3". The atumoxane used in all other experiments was a commercially available isobutyfalumtnoxane sold under the trademark "IBAO-65" by AKZO-Nobef). Catalysts and cocatalysts used in the first reactor were added independently by way of xytene solutions. The polymerizations were carried out in cyclohexane at a pressure of about 1,500 pounds per square inch gauge ("psi"). The pressure in the second reactor was slightly lower than that of the first to facilitate transfer of the polymer solution between the reactors. Ethylene was supplied to the reactors by a calibrated thermal mass flow meter and was dissolved in the reaction solvent prior to the polymerization reactor. If comonomer was used it was also premixed with the ethylene before entering the polymerization reactor. Under these conditions the ethylene conversion is a dependent variable controlled by such variables as the catalyst concentration, reaction temperature and catalyst activity. The internal reactor temperatures were monitored by a thermocouple in the polymerization medium and can be controlled at the required set point to +/- 0.5°C. Downstream of the second reactor the pressure was reduced from the reaction pressure (about 1,500 psi) to atmospheric pressure. The solid polymer was then recovered from the discharge of the second reactor as a slurry in the condensed solvent and was dried by evaporation before analysts. The accompanying tables illustrate flow rates to the reactors, catalyst concentrations and ethylene conversions. The flow rate of ethylene ("C2" in the tables) and octene {"C8" in the tables) is expressed in grams per minute. The monomers were dissolved in solvent and flow rates were adjusted to provide average reactor residence times (also referred to as "hold up times" or "HUT") of 1.5 minutes in the first reactor and 1.74 minutes in the second reactor (for all experiments). The concentration of catalyst in each reactor is reported on a transition metal 20 basis. Likewise, the mole ratio of cocatalysts (in comparison to the catalysts) is reported for all experiments in the tables. The ethylene conversions ("Q", in the tables) in each reactor were determined by gas chromatography. The results are shown in the tables under the heading "%Q-R1" and "%Q-R2" for the first and second reactor, respectively. The experiments of Table 1 were completed using Ph3CB(C6F5)4 as the ionic activator at reactor temperatures of 160°C in the first reactor and 230°C in the second reactor. Table 2 illustrates the effect of using a different ionic activator, namely B(C6F5)3. The reactor temperatures were again 160°C for the first reactor and 230°C for the second reactor. Table 3 illustrates the effect of using different first reactor temperatures while keeping the second reactor temperature at 230°C. Experiments 1, 2, 4, 5, 7 and 9 are comparative and are provided to illustrate comparative products produced using single reactor/single catalyst systems. Polymer Analysis Molecular weights were determined by gel permeation chromotography ("GPC"). GPC analysis was carried out using a Waters 150C GPC using 1,2,4-trichlorobenzene as the mobile phase at 140°C. The samples were prepared by dissolving the polymer in the mobile phase solvent in an external oven at 0.1% (w/v) and were run without filtration. Molecular weights are expressed as polyethylene equivalents with a relative standard deviation of 2.9% and 5.0% for the number average molecular weight "Mn" and weight average molecular weight "Mw" respectively. Molecular weight distribution ("MWD") is obtained by dividing Mw by Mn. Melt index (Ml) measurements were conducted according to ASTM method D-1238-82. 21 Polymer densities were measured using pressed plaques (ASTM D-1928-90) with a densitometer. The amount of comonomer was determined by Fourier transform infra red ("FTIR") analysis and reported in the tables. INDUSTRIAL APPLICABILITY This invention may be applied to the preparation of ethylene polymers, especially linear low density polyethylene. The ethylene polymers produced according to this invention are suitable for a wide variety of applications, including films; extruded goods such as profiles, hoses and cable coverings; blow molded parts such as toys; rotomolded parts such as storage containers and injection molded parts such as drinking cups and food packages. 22 23 24 25 We Claim: 1. A medium pressure solution polymerization process characterized by: A) polymerizing ethylene, optionally with one or more C3-12 alpha oleflns, In an Inert hydrocarbon solvent which comprises a C5 to C12 hydrocarbon in a first polymerization reactor at a temperature of from 80 to 200°C and a pressure of from 500 to 8,000 psi fn the presence of (a) a first catalyst which is an organometaitic complex of a group 4 or 5 metal that is characterized by having at least one phosphinimine ligand; and (b) a first cocatatyst, and B) passing said first polymer solution into a second polymerization reactor and polymerizing ethylene, optionally with one or more C3-12 alpha oleflns, In said second stirred polymerization reactor at a higher polymerization temperature than that of said first reactor in the presence of a Ziegler Natta catalyst, wherein said Ziegfer Natta catalyst comprises a transition metal compound of a transition metal selected from groups 3, 4 or 5 transition metals and an organoaiumlnum component which is defined by the formula: AI(X')a (OR)b (R)c wherein: X' Is a hailde; OR is an alkoxy or aryloxy group; R Is a hydrocarbyl; and a, b, or c are each 0, 1, 2 or 3 with the provisos that a+b+c=3 and b+c >1. wherein: (a) M is a metal selected from Ti, Hf and Zr; (b) PI is a phosphinimine ligand defined by the formula; 2. The process of claim one wherein said first catalyst is defined by the formula: 26 wherein each R1 is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical, a silyl radical of the formula: -Si-(R2)3 wherein each R2 is independently selected from the group consisting of hydrogen, a C1-8 alkyl or alkoxy radical, C6-10 aryl or aryloxy radicals, and a germanyl radical of the formula: Ge-(R2)3 wherein R2 is as defined above; (c) L is a ligand selected from the group consisting of cyclopentadienyl, substituted cyclopentadienyl, indenyl, substituted indenyl, fluorenyl or substituted fluorenyl; and (d) X is an activatable ligand, and wherein: m is 1 or 2, n is 0 or 1, with the proviso that n is 1 when m is 1 and p is fixed by the valence of said metal M. 3. The process of claim 2 wherein said first catalyst is defined such that said m is one and PI is a trialkyl phosphinimine; n is one and L is selected from unsubstituted cyclopentadienyl, substituted cyclopentadienyl, unsubstituted indenyl and substituted indenyl; and p is 2 and each X is independently selected from (a) an alkyl having from one to ten carbon atoms; and (b) a halide. 4. The process according to claim 3 wherein said first catalyst is cyclopentadienyl titanium (tri (tertiary butyl) phosphinimine) dichloride. 5. The process according to claim 2 wherein said metal is titanium and wherein the concentration of said titanium in said first reactor is less that one part per million. 6. The process of claim 5 wherein said first cocatalyst contains an alumoxane with the further proviso that the Al/Ti mole ratio, based upon aluminum in said alumoxane and titanium in said first catalyst is from 10/1 to 200/1. 27 7, The process of claim 6 wherein said first cocatatysl further.includes an Ionic boron cocatalyst, with the proviso that the B/Ti mole ratio, based on boron contained In said Ionic cocatalyst and titanium contained In said first catalyst is from 0.5/1 to 1.5/1. A dual reactor process for the solution and (co)polymerization of ethylene uses two different types of catalysts in the two reactors, A catalyst having a phosprttnimine ligand is used in the first reactor. A Ziegler Nafta catalyst is used in the second reactor. The process of this invention is comparatively easy to control and may be used to produce polyethylene products having a broad molecular weight distribution. Linear tow density produced according to this invention is well suited for the manufacture of molded goods and plastic films.

Full Text

DUAL REACTOR ETHYLENE POLYMERIZATION PROCESS
TECHNICAL HELD
This invention relates to the solution polymerization of ethylene in two reactors using two different catalyst systems.
BACKGROUND ART
The use of so-called "single-site" catalysts such as metallocene catalysts to prepare polyethylene having a narrow molecular weight distribution is well known. The "linear low density polyethylene" (or "LLDPE", a copolymer of ethylene and a higher alpha olefin) prepared with such catalysts typically exhibits a very uniform composition distribution (i.e. the comonomer is very uniformly distributed within the polymer chains). The combination of narrow molecular weight distribution and uniform composition distribution distinguishes these polymers from "conventional" LLDPE which is commercially manufactured with a Ziegler Natta catalyst or a chromium catalyst. In particular, the conventional LLDPE products have a broader molecular weight distribution and a broader composition distribution. These compositional differences are manifested in the form of differences in the physical properties of the two types of LLDPE polymers. Most notably, LLDPE prepared with a single site catalyst has improved impact strength and optical properties in comparison to "conventional" LLDPE. However, one advantage of the "conventional" LLDPE is that it is usually easier to "process" in its existing mixers and extruders. Accordingly, it would be highly desirable to prepare LLDPE products which possess the improved physical properties offered by single site catalysts and retain the broad molecular weight distribution (for improved processability) which is associated with conventional LLDPE.
One approach which has been used to achieve this object is the use of mixed catalyst systems. For example, United States Patent (USP) 4,530,914 (Ewen et al, to Exxon) teaches the use of two different metallocenes and USP 4,701,432 (Welborn, to Exxon) teaches the use of a supported catalyst prepared with a metallocene catalyst and a Ziegler

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Natta catalyst. Many others have subsequently attempted to use similar mixed catalyst systems as may be quickly ascertained by reviewing the patent literature.
However, the use of "mixed" catalyst systems is often associated with operability problems. For example, the use of two catalysts on a single support (as taught by Welborn in USP 4,701,432) may be associated with a reduced degree of process control flexibility (e.g. If the polymerization reaction is not proceeding as desired when using such a catalyst system, it is difficult to establish which corrective action should be taken as the corrective action will typically have a different effect on each of the two different catalyst components). Moreover, the two different catalyst/cocatalyst systems may interfere with one another - for example, the organoaluminum component which is often used in Ziegler Natta or chromium catalyst systems may "poison" a metallocene catalyst. Accordingly, a "mixed catalyst" process which mitigates some of these difficulties would be a useful addition to the art.
DISCLOSURE OF INVENTION
The present invention provides a medium pressure solution polymerization process characterized by:
A) polymerizing ethylene, optionally with one or more C3-12
alpha olefins, in solvent in a first polymerization reactor at a temperature of
from 80 to 200°C and a pressure of from 500 to 8,000 pounds per square
inch gauge ("psi") in the presence of (a) a first catalyst which is an
organometallic complex of a group 4 or 5 metal that is characterized by
having at least one phosphinimine ligand; and (b) a first cocatalyst; and
B) passing said first polymer solution into a second
polymerization reactor and polymerizing ethylene, optionally with one or
more C3.12 alpha olefins, in said second stirred polymerization reactor at a
higher polymerization temperature than that of said first reactor in the
presence of a Ziegler Natta catalyst, wherein said Ziegler Natta catalyst
comprises a transition metal compound of a transition metal selected from

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groups 3, 4 or 5 of the Periodic Table (using IUPAC nomenclature) and an organoaluminum component which is defined by the formula:
AI(X')a(OR)b (R)c
wherein: X' is a halide (preferably chlorine); OR is an alkoxy or aryloxy group; R is a hydrocarbyl (preferably an alkyl having from 1 to 10 carbon atoms); and a, b, or c are each 0, 1, 2 or 3 with the provisos that a+b+c=3 and b+c>1.
Thus, the process of the present invention requires two solution polymerization reactors and two distinct catalyst systems. The first catalyst must have a phosphinimine ligand (and, hence, is sometimes referred to herein as a "phosphinimine catalyst" or "PIC").
The first reactor uses the "phosphinimine catalyst". Conventional process control techniques may be used to operate the first reactor as there is only one catalyst to deal with.
Preferred phosphinimine catalysts for use in the first reactor are titanium species which contain one cyclopentadienyl ligand, one phosphinimine ligand and two chloride ligands.
It is particularly preferred that the concentration of titanium in the first reactor be less that 1 part per million (ppm) especially less that 0.5 ppm (based on the weight of titanium divided by the weight of the reactor contents).
Exemplary cocatalysts for the phosphinimine catalyst are alumoxanes and/or ionic activators. Preferred cocatalysts for the phosphinimine catalyst are a combination of:
1) an alumoxane (in which the Al/Ti molar ratio, based on the
alumoxane and the titanium in the phosphinimine catalyst is
between 10/1 and 200/1, most preferably from 40/1 to
120/1); and
2) a boron-containing ionic activator (in which the B/Ti ratio,
based on the boron in the ionic activator to the titanium in the
phosphinimine catalyst is between 0.5/1 and 1.5/1).

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The polymer solution from the first reactor is transferred to the second solution polymerization reactor. A Ziegler Natta catalyst is used ir the second reactor. It is preferred that the Ziegler Natta catalyst contains at least one transition metal selected from titanium and vanadium, and that the molar concentration of titanium/vanadium which is added to the second reactor is at least 10 times greater than the titanium concentration in the first reactor.
Thus, the second polymerization reactor must use a Ziegler Natta catalyst. Additionally, the second polymerization reactor must be operatet at a higher temperature from the first - most preferably, at least 30°C higher than the first.
While not wishing to be bound by any particular theory, it is believed that the reactor conditions in the second reactor "overwhelm" the catalyst from the first reactor (i.e. for process control purposes, any residual catalyst from the first reactor is not a concern in the second reactor). This is desirable from a process operability perspective as it reduces the number of variables which need to be considered when controlling the polymerization reaction in the second reactor.
BEST MODE FOR CARRYING OUT THE INVENTION
Part 1. Description of First Catalysts
The catalyst used in the first reactor of the process of this invention ("first catalyst") is an organometallic complex of a group 4 or 5 metal which is characterized by having at least one phosphinimine ligand (where the term phosphinimine is defined in section 1.2 below).
Any such organometallic having a phosphinimine ligand which displays catalytic activity for ethylene polymerization may be employed. Preferred first catalysts are defined by the formula:

wherein M is a transition metal selected from Ti, Hf and Zr (as described in section 1.1 below); PI is a phosphinimine ligand (as described in section

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1.2 below); L is a monanionic ligand which is a cyclopentadienyl-type Ijgand or a bulky heteroatom ligand (as described in section 1.3 below); X is an activatable ligand which is most preferably a simple monanionic ligand such as alkyl or a halide (as described in section 1.4 below); m is 1 or 2, n is 0 or 1, and p is fixed by the valence of the metal M.
The most preferred first catalysts are group 4 metal complexes in the highest oxidation state. For example, a preferred catalyst may be a bis (phosphinimine) dichloride complex of titanium, zirconium or hafnium. However, it is particularly preferred that the first catalyst contain one phosphinimine ligand, one "L" ligand (which is most preferably a cyclopentadienyl - type ligand) and two "X" ligands (which are preferably both chloride).
1.1 Metals
The first catalyst is an organometallic complex of a group 4 or 5 metal (where the numbers refer to columns in the Periodic Table of the Elements using IUPAC nomenclature). The preferred metals are from group 4, (especially titanium, hafnium or zirconium) with titanium being most preferred.
1.2 Phosphinimine Liqand
The first catalyst must contain a phosphinimine ligand which is covalently bonded to the metal. This ligand is defined by the formula:

wherein each R is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20
hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical, and a silyl radical of the formula:
-Si-(R2)3

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wherein each R2 is independently selected from the group consisting of
hydrogen, a C1-8 alkyl or alkoxy radical, C6-10 aryl or aryloxy radicals, and a
germanyl radical of the formula: Ge-(R2)3
wherein R2 is as defined above.
The preferred phosphinimines are those in which each R1 is a
hydrocarbyl radical. A particularly preferred phosphinimine is tri-(tertiary
butyl) phosphinimine (i.e. where each R1 is a tertiary butyl group).
1.3 Ligand L
Preferred first catalysts are group 4 organometallic complexes which contain one phosphinimine ligand (as described in section 1.2 above) and one ligand L (as described in sections 1.3.1 to 1.3.6) which is either a cyclopentadienyl-type ligand or a heteroligand.
1.3.1 Cvclopentadienvl-type Liqands
As used herein, the term cyclopentadienyl-type ligand is meant to convey its conventional meaning, namely a ligand having a five carbon ring which is bonded to the metal via eta-5 bonding. Thus, the term "cyclopentadienyl-type" includes unsubstituted cyclopentadienyl, substituted cyclopentadienyl, unsubstituted indenyl, substituted indenyl, unsubstituted fluorenyl and substituted fluorenyl. An exemplary list of substituents for a cyclopentadienyl ligand includes the group consisting of C1-10 hydrocarbyl radical (which hydrocarbyl substituents are unsubstituted or further substituted); a halogen atom, C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical; an amido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; a phosphido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; silyl radicals of the formula -Si-(R)3 wherein each R is independently selected from the group consisting of hydrogen, a C1-8 alkyl or alkoxy radical C6-10 aryl or aryloxy radicals; germanyl radicals of the formula Ge-(R2)3 wherein R is as defined directly above.

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1.3.2 Heteroliqand
As used herein, the term "heteroligand" refers to a ligand which
contains at least one heteroatom selected from the group consisting of
boron, nitrogen, oxygen, phosphorus or sulfur. The heteroligand may be
sigma or pi-bonded to the metal. Exemplary heteroligands are described
in sections 1.3.2.1 to 1.3,2.6 below.
1.3.2.1 Ketimide Liqands
As used herein, the term "ketimide ligand" refers to a ligand which: (a) is bonded to the transition metal via a metal-nitrogen atom bond; (b) has a single substituent on the nitrogen atom, (where this single substituent is a carbon atom which is doubly bonded to the N atom); and (c) has two substituents (Sub 1 and Sub 2, described below) which are bonded to the carbon atom.
Conditions a. b and c are illustrated below:

The substituents "Sub 1 and Sub 2" may be the same or different.
Exemplary substituents include hydrocarbyls having from 1 to 20 carbon
atoms; silyl groups, amido groups and phosphido groups. For reasons of
cost and convenience it is preferred that these substituents both be
hydrocarbyls, especially simple alkyls and most preferably tertiary butyl.
1.3,2.2 Silicone-Containinq Heteroliqands
These ligands are defined by the formula:
- (p)SiRxRyRz
where the - denotes a bond to the transition metal and u is sulfur or oxygen.
The substituents on the Si atom, namely Rx, Ry and Rz are required in order to satisfy the bonding orbital of the Si atom. The use of any particular substituent Rx, Ry or Rz is not especially important to the

8
success of this Invention. It is preferred that each of Rx, Ry and Rz is a C1-2 hydrocarbyl group (i.e. methyl or ethyl) simply because such materials are readily synthesized from commercially available materials).
1.3.2.3 Amido Liqands
The term "amido" is meant to convey its broad, conventional meaning. Thus, these ligands are characterized by (a) a metal-nitrogen bond, and (b) the presence of two substituents (which are typically simple alkyl or silyl groups) on the nitrogen atom.
1.3.2.4 Alkoxy Liqands
The term "alkoxy" is also intended to convey its conventional meaning. Thus, these ligands are characterized by (a) a metal oxygen bond, and (b) the presence of a hydrocarbyl group bonded to the oxygen atom. The hydrocarbyl group may be a ring structure and/or substituted (e.g. 2, 6 di-tertiary butyl phenoxy).
1.3.2.5 Boron Heterocvclic Liqands
These ligands are characterized by the presence of a boron atom in a closed ring ligand. This definition includes heterocyclic ligands which also contain a nitrogen atom in the ring. These ligands are well known to those skilled in the art of oleffn polymerization and are fully described in the literature (see, for example, USPs' 5,637,659; 5,554,775 and the references cited therein).
1.3.2,6 Phosphole Liqands
The term "phosphole" is also meant to convey its conventional meaning. "Phospholes" are cyclic dienyl structures having four carbon atoms and one phosphorus atom in the closed ring. The simplest phosphole is C4PI14 (which is analogous to cyclopentadiene with one carbon in the ring being replaced by phosphorus). The phosphole ligands may be substituted with, for example, C1-20 hydrocarbyl radicals (which may, optionally, contain halogen substituents); phosphido radicals; amido radicals; silyl or alkoxy radicals. Phosphoie ligands are also well known to those skilled in the art of olefin polymerization and are described as such in USP 5,434,116.

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1.4 Activatable Liqand
The term "activatable ligand" refers to a ligand which may be activated by a cocatalyst, (also referred to as an "activator"), to facilitate olefin polymerization. Exemplary activatable ligands are independently selected from the group consisting of a hydrogen atom, a halogen atom, a C1-10 hydrocarbyl radical, a C1-10 atkoxy radical, a C5-10 aryl oxide radical; each of which said hydrocarbyl, alkoxy, and aryl oxide radicals may be unsubstituted by or further substituted by a halogen atom, a C1-8 alkyl radical, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals; a phosphido radical which is unsubstituted or substituted by up to two C1-8 alkyl radicals.
The number of activatable ligands depends upon the valency of the
metal and the valency of the activatable ligand. The preferred first catalyst
metals are group 4 metals in their highest oxidation state (i.e. 4+) and the
preferred activatable ligands are monoanionic (such as a halide -
especially chloride or a alkyl - especially methyl). Thus, the preferred first
catalyst contains a phosphinimine ligand, a cyclopentadienyl ligand and
two chloride (or methyl) ligands bonded to the group 4 metal. In some
instances, the metal of the first catalyst component may not be in the
highest oxidation state. For example, a titanium (III) component would
contain only one activatable ligand.
1.5 Summary Description of Preferred Catalyst
As previously noted, the preferred first catalyst is a group 4 organometallic complex in its highest oxidation state having a phosphinimine ligand, a cyclopentadienyl-type ligand and two activatable ligands. These requirements may be concisely described using the following formula for the preferred catalyst:

10
wherein: (a) M is a metal selected from Ti, Hf and Zr; (b) PI is a phosphinimine ligand defined by the formula:

wherein each R1 is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryI or aryloxy radical, an amido radical, a silyl radical of the formula:
-Si-(R2)3
wherein each R2 is independently selected from the group consisting of hydrogen, a C1-8 alky! or alkoxy radical, C6-10 aryl or aryloxy radicals, and a germanyl radical of the formula:
Ge-(R2)3
wherein R2 is as defined above; (c) L is a ligand selected from the group
consisting of cyclopentadienyl, substituted cyclopentadienyl, indenyl,
substituted indenyl, fluorenyl, or substituted fluorenyl; and (d) X is an
activatable ligand, and wherein: m is 1, n is 1 and p is 2.
2. Description of First Cocatalvst
The catalyst components described in part 1 above are used in
combination with at least one cocatalyst (or "activator") to form an active
catalyst system for olefin polymerization as described in more detail in
sections 2.1, 2.2 and 2.3 below.
2.1 Alumoxanes
The alumoxane may be of the formula:
(R4)2AIO{R4AIO)mAI(R4)2
wherein each R4 is independently selected from the group consisting of C1-20 hydrocarbyl radicals and m is from 0 to 50, preferably R4 is a C1-4 alkyl radical and m is from 5 to 30. Methylalumoxane (or "MAO") in which each R is methyl is the preferred alumoxane.

11
Alumoxanes are well known as cocatalysts, particularly for metallocene-type catalysts. Alumoxanes are also readily available articles of commerce.
The use of an alumoxane cocatalyst generally requires a molar ratio
of aluminum to the transition metal in the catalyst from 20:1 to 1000:1.
Preferred ratios are from 50:1 to 250:1.
2.2 "Ionic Activators" as Cocatalvsts
So-called "ionic activators" are also well known for metallocene catalysts. See, for example, USP 5,198,401 (Hlatky and Turner) and USP 5,132,380 (Stevens and Neithamer).
Whilst not wishing to be bound by any theory, it is thought by those skilled in the art that "ionic activators" initially cause the abstraction of one or more of the activatable ligands in a manner which ionizes the catalyst into a cation, then provides a bulky, labile, non-coordinating anion which stabilizes the catalyst in a cationic form. The bulky, non-coordinating anion coordinating anion permits olefin polymerization to proceed at the cationic catalyst center (presumably because the non-coordinating anion is sufficiently labile to be displaced by monomer which coordinate to the catalyst). Preferred ionic activators are boron-containing ionic activators described in (i) - (iii) below:
(i) compounds of the formula [R5]+ [B(R7)4] wherein B is a boron atom, R5 is a aromatic hydrocarbyl (e.g. triphenyl methyl cation) and each R7 is independently selected from the group consisting of phenyl radicals which are unsubstituted or substituted with from 3 to 5 substituents selected from the group consisting of a fluorine atom, a C1-4 alkyl or alkoxy radical which is unsubstituted or substituted by a fluorine atom; and a silyl radical of the formula -Si-(R9)3; wherein each R9 is independently selected from the group consisting of a hydrogen atom and a C1-4 alkyl radical; and (ii) compounds of the formula [(R8)tZH]+[B(R7)4] wherein B is a boron atom, H is a hydrogen atom, Z is a nitrogen atom or

12
phosphorus atom, t is 2 or 3 and R8 is selected from the group consisting of C1-8 alkyl radicals, a phenyl radical which is unsubstituted or substituted by up to three C1-4 alkyl radicals, or one R8 taken together with the nitrogen atom may form an anilinium radical and R7 is as defined above; and (iii) compounds of the formula B(R7)3 wherein R7 is as defined
above. In the above compounds preferably R7 is a pentafluorophenyl
radical, and R5 is a triphenylmethyl cation, Z is a nitrogen atom and R8 is a
C1-4 alkyl radical or R8 taken together with the nitrogen atom forms an
anilium radical which is substituted by two C1-4 alkyl radicals.
The "ionic activator" may abstract one or more activatable ligands
so as to ionize the catalyst center into a cation but not to covalently bond
with the catalyst and to provide sufficient distance between the catalyst
and the ionizing activator to permit a polymerizable olefin to enter the
resulting active site.
Examples of ionic activators include:
triethylammonium tetra(phenyl)boron,
tripropylammonium tetra(phenyl)boron,
tri(n-butyl)ammonium tetra(phenyl)boron,
trirnethylamrnoniurn tetra(p-tolyl)boron,
trimethylammonium tetra(o-tolyl)boron,
tributylammonium tetra(pentafluorophenyl)boron,
tripropylammonium tetra(o,p-dimethylphenyl)boron,
tributylammonium tetra(m,m-dimethyiphenyl)boron,
tributylammonium tetra(p-trifluoromethylphenyl)boron,
tributylammonium tetra(pentafluorophenyl)boron,
tri(n-butyl)ammonium tetra(o-tolyl)boron,
N,N-dimethylanilinium tetra(phenyl)boron,
N.N-diethylanilinium tetra(phenyl)boron,
N.N-diethylanilinium tetra(phenyl)n-butylboron,

13
N,N-2,4,6-pentamethylanJIiniumtetra(phenyl)boron" di-(isopropyl)ammonium tetra(pentafluorophenyl)boron, dicyciohexytammoniumtetra(phenyl)boron, triphenylphosphonium tetra(phenyl)boron, tri(methyiphenyl)phosphoniumtetra(phenyl)boron, tri(dimethylphenyl)phosphoniumtetra{phenyl)boron, tropitlium tetrakispentafluorophenyl borate, triphenyimethyliurn tetrakispentafluorophenyl borate, benzene (diazonium) tetrakispentafluorophenyl borate, tropillium phenyltrispentafluorophenyl borate, triphenyimethyliurn phenyltrispentafluorophenyl borate, benzene (diazonium) phenyltrispentafluorophenyl borate, tropillium tetrakis (2,3,5,6-tetrafluorophenyf) borate, triphenylmethyiium tetrakis (2,3,5,6-tetrafluorophenyl) borate, benzene (diazonium) tetrakis (3,4,5-trifluorophenyl) borate, tropillium tetrakis (3,4,5-trifIuorophenyt) borate, benzene {diazonium) tetrakis {3,4,5-trifluorophenyl) borate, tropiliium tetrakis (1,2,2-trifluoroethenyl) borate, triphenyimethyliurn tetrakis (1,2,2-trifluoroethenyl) borate, benzene (diazonium) tetrakis (1,2,2-trifluoroethenyl) borate, tropillium tetrakis (2,3,4,5-tetrafluorophenyl) borate, triphenylmethyiium tetrakis (2,3,4,5-tetrafluorophenyl) borate, and benzene (diazonium) tetrakis (2,3,4,5-tetrafluorophenyl) borate.
Readily commercially available ionic activators include; N,N- dimethylaniliniumtetrakispentafluorophenyl borate; triphenylmethylium tetrakispentafluorophenyl borate; and trispentafluorophenyl borane. 3. Description of Zieqler Natta Catalyst
The term "Ziegler Natta catalyst" is well known to those skilled in the art and is used herein to convey its conventional meaning, A Ziegler Natta catalyst must be used in the second (hot) reactor of this invention. Ziegler Natta catalysts comprise at least one transition metal compound of

14
a transition metal selected from groups 3, 4, or 5 of the Periodic Table (using IUPAC nomenclature) and an organoaluminum component which is defined by the formula:
AI(X')a (OR)b (R)c
wherein: X' is a halide (preferably chlorine); OR is an alkoxy or aryloxy group; R is a hydrocarbyl (preferably an alkyl having from 1 to 10 carbon atoms); and a,b, or c are each 0, 1, 2, or 3 with the provisos text a+b+c=3 and b+c>1.
It is highly preferred that the transition metal compounds contain at least one of titanium or vanadium. Exemplary titanium compounds include titanium halides (especially titanium chlorides, of which TiCI4 is preferred); titanium alkyls; titanium alkoxides (which may be prepared by reacting a titanium alkyl with an alcohol) and "mixed ligand" compounds (i.e. compounds which contain more than one of the above described halide, alkyl and alkoxide ligands). Exemplary vanadium compounds may also contain halide, alkyl or alkoxide ligands. In addition vanadium oxy trichloride ("VOCI3") is known as a Ziegler Natta catalyst component and is suitable for use in the present invention.
It is especially preferred that the Ziegler Natta catalyst contain both of a titanium and a vanadium compound. The Ti/V mole ratios may be from 10/90 to 90/10, with mole ratios between 50/50 and 20/80 being particularly preferred.
The above defined organoaluminum compound is an essential component of the Ziegler Natta catalyst. The mole ratio of aluminum to transition metal {for example, aluminum/(titanium + vanadium)} is preferably from 1/1 to 100/1, especially from 1.2/1 to 15/1.
As will be appreciated by those skilled in the art of ethylene polymerization, conventional Ziegler Natta catalysts may also incorporate additional components such as an electron donor- for example an amine; or a magnesium compound - for example a magnesium alkyl such as butyl ethyl magnesium and a halide source (which is typically a chloride such as tertiary butyl chloride).

15
Such components, if employed, may be added to the other catalyst components prior to introduction to the reactor or may be directly added to the reactor.
The Ziegler Natta catalyst may also be "tempered" (i.e. heat
treated) prior to being introduced to the reactor (again, using techniques
which are well known to those skilled in the art and published in the
literature).
4. Description of Dual Reactor Solution Polymerization Process
Solution processes for the (co)polymerization of ethylene are well known in the art. These processes are conducted in the presence of an inert hydrocarbon solvent typically a C5-12 hydrocarbon which may be unsubstituted or substituted by a C1-4 alkyl group, such as pentane, methyl pentane, hexane, heptane, octane, cyclohexane, methycyclohexane and hydrogenated naphtha. An example of a suitable solvent which is commercially available is "Isopar E" (C8-12 aliphatic solvent, Exxon Chemical Co.). .
The solution polymerization process of this invention must use at least two polymerization reactors. The first polymerization reactor must operate at a lower temperature ("cold reactor") using a "phosphinimine catalyst" described in Part 1 above.
The polymerization temperature in the first reactor is from about 80°C to about 180°C (preferably from about 120°C to 160°C) and the hot reactor is preferably operated at a higher temperature (up to about 300°C). Both reactors are preferably "stirred reactors" (i.e. the reactors are well mixed with a good agitation system). Preferred pressures are from about 500 psi to 8,000 psi. The most preferred reaction process is a "medium pressure process", meaning that the pressure in each reactor is preferably less than about 6,000 psi (about 42,000 kiloPascais or kPa), most preferably from about 1,500 psi to 3,000 psi (about 14,000-22,000 kPa)
Suitable monomers for copolymerization with ethylene include C3-20 mono- and di- olefins. Preferred comonomers include C3-12 alpha olefins which are unsubstituted or substituted by up to two C1-6 alkyl radicals, C8-12

16
vinyl aromatic monomers which are unsubstituted or substituted by up to two substituents selected from the group consisting of C1-4 alkyl radicals, C4-12 straight chained or cyclic diolefins which are unsubstituted or substituted by a C1-4 alkyl radical. Illustrative non-limiting examples of such alpha-olefins are one or more of propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, and 1-decene, styrene, alpha methyl styrene and the constrained-ring cyclic olefins such as cyclobutene, cyclopentene, dicyclopentadiene norbornene, alkyl-substituted norbornes, alkenyl-substituted norbornes and the like (e.g. 5-methylene-2-norbomene and 5-ethylidene-2-norbornene, bicyclo-(2,2,1 )-hepta-2,5-diene).
The polyethylene polymers which may be prepared in accordance with the present invention are LLDPE's which typically comprise not less than 60, preferably not less than 75 weight % of ethylene and the balance one or more C4-10 alpha olefins, preferably selected from the group consisting of 1-butene, 1-hexene and 1-octene. The polyethylene prepared in accordance with the present invention may be LLDPE having a density from about 0.910 to 0.935 g/cc or (linear) high density polyethylene having a density above 0.935 g/cc. The present invention might also be useful to prepare polyethylene having a density below 0.910 g/cc - the so-called very low density polyethylene and ultra low density polyethylenes (or "plastomers").
Generally the alpha olefin may be present in an amount from about 3 to 30 weight %, preferably from about 4 to 25 weight %.
The present invention may also be used to prepare co- and ter-polymers of ethylene, propylene and optionally one or more diene monomers. Generally, such polymers will contain about 50 to about 75 weight % ethylene, preferably about 50 to 60 weight % ethylene and correspondingly from 50 to 25 weight % of propylene. A portion of the monomers, typically the propylene monomer, may be replaced by a conjugated diolefin. The diolefin may be present in amounts up to 10 weight % of the polymer although typically is present in amounts from about 3 to 5 weight %. The resulting polymer may have a composition

17
comprising from 40 to 75 weight % of ethylene, from 50 to 15 weight % of propylene and up to 10 weight % of a diene monomer to provide 100 weight % of the polymer. Preferred but not limiting examples of the dienes are dicyclopentadiene, 1,4-hexadiene, 5-methylene-2-norbornene, 5-ethylidene-2-norbomene and 5-vinyl-2-norbornene, especially 5-ethylidene-2-norbornene and 1,4-hexadiene.
The monomers are dissolved/dispersed in the solvent either prior to being fed to the first reactor (or for gaseous monomers the monomer may be fed to the reactor so that it will dissolve in the reaction mixture). Prior to mixing, the solvent and monomers are generally purified to remove potential catalyst poisons such as water, oxygen or metal impurities. The feedstock purification follows standard practices in the art, e.g. molecular sieves, alumina beds and oxygen removal catalysts are used for the purification of monomers. The solvent itself as well (e.g. methyl pentane, cyclohexane, hexane or toluene) is preferably treated in a similar manner.
The feedstock may be heated or cooled prior to feeding to the first reactor. Additional monomers and solvent may be added to the second reactor, and it may be heated or cooled.
Generally, the catalyst components may be premixed in the solvent for the reaction or fed as separate streams to each reactor. In some instances premixing it may be desirable to provide a reaction time for the catalyst components prior to entering the reaction. Such an "in line mixing" technique is described in a number of patents in the name of DuPont Canada Inc (e.g. USP patent 5,589,555, issued December 31, 1996).
The residence time in each reactor will depend on the design and the capacity of the reactor. Generally the reactors should be operated under conditions to achieve a thorough mixing of the reactants. In addition, it is preferred that from 20 to 60 weight % of the final polymer is polymerized in the first reactor, with the balance being polymerized in the second reactor. In a highly preferred embodiment, the first polymerization reactor has a smaller volume than the second polymerization reactor. On

18
leaving the reactor system the solvent is removed and the resulting polymer is finished in a conventional manner.
Further details of the invention are illustrated in the following, non limiting, examples. EXAMPLES Continuous Solution Polymerization
All the polymerization experiments described below were conductec using a continuous solution polymerization system. The process is continuous in all feed streams (solvent, monomers and catalyst) and in the removal of product. All feed streams were purified prior to the reactors by contact with various absorption media to remove catalyst killing impurities such as water, oxygen and polar materials as is known to those skilled in the art. All components were stored and manipulated under an atmosphere of purified nitrogen.
The polymerization system included two reactors connected in series. The first reactor had an internal volume of 51 mL and was connected via tubing to a second reactor having an internal volume of 71.5 mL. It was possible to add monomers, solvent and/or catalysts to each of the reactors.
The catalyst used in the first reactor was a titanium complex having one cyclopentadienyl ligand, one tri (tertiary butyl) phosphinimine ligand and two chloride ligands (i.e. "CpTi NP(tBu)3 Cl2"). This catalyst was used in all inventive experiments and is identified in Table 1 as "PIC" (for phosphinimine catalyst)
The Ziegler Natta catalyst used in the second reactor was a mixed titanium/vanadium system using titanium tetrachloride ("TiCI4") and vanadium oxy trichloride ("VOCI3"). Triethyl aluminum ("AIEt3") was used as part of the Ziegler Natta catalyst system.
The cocatalyst used in the first reactor was a combination of a boron-containing ionic activator and an alumoxane. (Note: the ionic activator used in experiments 1, 2, 3, 4, 5 and 6 was triphenylmethylium tetrakispentafluorophenyl borate or "Ph3CB(C6F5)4". The ionic activator

19
used in the remaining experiments was trispentafluorophenyl borane or "B(C6F5)3". The atumoxane used in all other experiments was a commercially available isobutyfalumtnoxane sold under the trademark "IBAO-65" by AKZO-Nobef).
Catalysts and cocatalysts used in the first reactor were added independently by way of xytene solutions.
The polymerizations were carried out in cyclohexane at a pressure of about 1,500 pounds per square inch gauge ("psi"). The pressure in the second reactor was slightly lower than that of the first to facilitate transfer of the polymer solution between the reactors. Ethylene was supplied to the reactors by a calibrated thermal mass flow meter and was dissolved in the reaction solvent prior to the polymerization reactor. If comonomer was used it was also premixed with the ethylene before entering the polymerization reactor. Under these conditions the ethylene conversion is a dependent variable controlled by such variables as the catalyst concentration, reaction temperature and catalyst activity.
The internal reactor temperatures were monitored by a thermocouple in the polymerization medium and can be controlled at the required set point to +/- 0.5°C. Downstream of the second reactor the pressure was reduced from the reaction pressure (about 1,500 psi) to atmospheric pressure. The solid polymer was then recovered from the discharge of the second reactor as a slurry in the condensed solvent and was dried by evaporation before analysts.
The accompanying tables illustrate flow rates to the reactors, catalyst concentrations and ethylene conversions. The flow rate of ethylene ("C2" in the tables) and octene {"C8" in the tables) is expressed in grams per minute. The monomers were dissolved in solvent and flow rates were adjusted to provide average reactor residence times (also referred to as "hold up times" or "HUT") of 1.5 minutes in the first reactor and 1.74 minutes in the second reactor (for all experiments). The concentration of catalyst in each reactor is reported on a transition metal

20
basis. Likewise, the mole ratio of cocatalysts (in comparison to the catalysts) is reported for all experiments in the tables.
The ethylene conversions ("Q", in the tables) in each reactor were determined by gas chromatography. The results are shown in the tables under the heading "%Q-R1" and "%Q-R2" for the first and second reactor, respectively.
The experiments of Table 1 were completed using Ph3CB(C6F5)4 as the ionic activator at reactor temperatures of 160°C in the first reactor and 230°C in the second reactor.
Table 2 illustrates the effect of using a different ionic activator, namely B(C6F5)3. The reactor temperatures were again 160°C for the first reactor and 230°C for the second reactor.
Table 3 illustrates the effect of using different first reactor temperatures while keeping the second reactor temperature at 230°C.
Experiments 1, 2, 4, 5, 7 and 9 are comparative and are provided to illustrate comparative products produced using single reactor/single catalyst systems. Polymer Analysis
Molecular weights were determined by gel permeation chromotography ("GPC"). GPC analysis was carried out using a Waters 150C GPC using 1,2,4-trichlorobenzene as the mobile phase at 140°C. The samples were prepared by dissolving the polymer in the mobile phase solvent in an external oven at 0.1% (w/v) and were run without filtration. Molecular weights are expressed as polyethylene equivalents with a relative standard deviation of 2.9% and 5.0% for the number average molecular weight "Mn" and weight average molecular weight "Mw" respectively. Molecular weight distribution ("MWD") is obtained by dividing Mw by Mn.
Melt index (Ml) measurements were conducted according to ASTM method D-1238-82.

21
Polymer densities were measured using pressed plaques (ASTM D-1928-90) with a densitometer.
The amount of comonomer was determined by Fourier transform infra red ("FTIR") analysis and reported in the tables.
INDUSTRIAL APPLICABILITY
This invention may be applied to the preparation of ethylene polymers, especially linear low density polyethylene. The ethylene polymers produced according to this invention are suitable for a wide variety of applications, including films; extruded goods such as profiles, hoses and cable coverings; blow molded parts such as toys; rotomolded parts such as storage containers and injection molded parts such as drinking cups and food packages.

22

23

24

25 We Claim:
1. A medium pressure solution polymerization process characterized by:
A) polymerizing ethylene, optionally with one or more C3-12 alpha oleflns, In an
Inert hydrocarbon solvent which comprises a C5 to C12 hydrocarbon in a first
polymerization reactor at a temperature of from 80 to 200°C and a pressure of
from 500 to 8,000 psi fn the presence of (a) a first catalyst which is an
organometaitic complex of a group 4 or 5 metal that is characterized by having at
least one phosphinimine ligand; and (b) a first cocatatyst, and
B) passing said first polymer solution into a second polymerization reactor
and polymerizing ethylene, optionally with one or more C3-12 alpha oleflns, In said
second stirred polymerization reactor at a higher polymerization temperature
than that of said first reactor in the presence of a Ziegler Natta catalyst, wherein
said Ziegfer Natta catalyst comprises a transition metal compound of a transition
metal selected from groups 3, 4 or 5 transition metals and an organoaiumlnum
component which is defined by the formula:
AI(X')a (OR)b (R)c
wherein: X' Is a hailde; OR is an alkoxy or aryloxy group; R Is a hydrocarbyl; and a, b, or c are each 0, 1, 2 or 3 with the provisos that a+b+c=3 and b+c >1.
wherein: (a) M is a metal selected from Ti, Hf and Zr; (b) PI is a phosphinimine ligand defined by the formula;

2. The process of claim one wherein said first catalyst is defined by the
formula:

26
wherein each R1 is independently selected from the group consisting of a hydrogen atom, a halogen atom, C1-20 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom, a C1-8 alkoxy radical, a C6-10 aryl or aryloxy radical, an amido radical, a silyl radical of the formula:
-Si-(R2)3
wherein each R2 is independently selected from the group consisting of hydrogen, a C1-8 alkyl or alkoxy radical, C6-10 aryl or aryloxy radicals, and a germanyl radical of the formula:
Ge-(R2)3
wherein R2 is as defined above; (c) L is a ligand selected from the group consisting of cyclopentadienyl, substituted cyclopentadienyl, indenyl, substituted indenyl, fluorenyl or substituted fluorenyl; and (d) X is an activatable ligand, and wherein: m is 1 or 2, n is 0 or 1, with the proviso that n is 1 when m is 1 and p is fixed by the valence of said metal M.
3. The process of claim 2 wherein said first catalyst is defined such
that said
m is one and PI is a trialkyl phosphinimine;
n is one and L is selected from unsubstituted cyclopentadienyl, substituted cyclopentadienyl, unsubstituted indenyl and substituted indenyl; and
p is 2 and each X is independently selected from (a) an alkyl having from one to ten carbon atoms; and (b) a halide.
4. The process according to claim 3 wherein said first catalyst is
cyclopentadienyl titanium (tri (tertiary butyl) phosphinimine) dichloride.
5. The process according to claim 2 wherein said metal is titanium and
wherein the concentration of said titanium in said first reactor is less that
one part per million.
6. The process of claim 5 wherein said first cocatalyst contains an
alumoxane with the further proviso that the Al/Ti mole ratio, based upon
aluminum in said alumoxane and titanium in said first catalyst is from 10/1
to 200/1.

27
7, The process of claim 6 wherein said first cocatatysl further.includes an Ionic boron cocatalyst, with the proviso that the B/Ti mole ratio, based on boron contained In said Ionic cocatalyst and titanium contained In said first catalyst is from 0.5/1 to 1.5/1.
A dual reactor process for the solution and (co)polymerization of ethylene uses two different types of catalysts in the two reactors, A catalyst having a phosprttnimine ligand is used in the first reactor. A Ziegler Nafta catalyst is used in the second reactor. The process of this invention is comparatively easy to control and may be used to produce polyethylene products having a broad molecular weight distribution. Linear tow density produced according to this invention is well suited for the manufacture of molded goods and plastic films.

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Patent Number

207990

Indian Patent Application Number

IN/PCT/2001/00319/KOL

PG Journal Number

27/2007

Publication Date

06-Jul-2007

Grant Date

04-Jul-2007

Date of Filing

20-Mar-2001

Name of Patentee

NOVA CHEMICALS ( INTERNATIONAL) S.A.

Applicant Address

CHEMIN DES MAZOTS 2, 1700 FRIBOURG

Inventors:

#	Inventor's Name	Inventor's Address
1	JABER ISAM	1048-16A STREET NE CALGARY, ALBERTA 12E 4TS
2	BROWN STEPHEN JOHN	157 MOUNT SPARROWHAWKK PLACE SE, CALGARY ALBERTA T2Z 2G7

PCT International Classification Number

C 08 F 10/02

PCT International Application Number

PCT/CA99/00790

PCT International Filing date

1999-08-27

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	2,247,703	1998-09-22	Canada