Patent Publication Number: US-2012046429-A1

Title: Sequential Formation of Ziegler-Natta Catalyst Using Non-blended Components

Description:
FIELD 
     Embodiments of the present invention generally relate to methods of brining Ziegler-Natta type catalyst compositions for olefin polymerization. 
     BACKGROUND 
     As reflected in the patent literature, many processes for forming Ziegler-Nana catalyst systems utilize blends of components. Unfortunately, such blends generally are specialty chemicals having a high production cost. In an effort to reduce cost, the use of cheaper raw (non-blended) components can undesirably produce catalysts with lower activity and smaller D 50  particle size, which may not only slow catalyst synthesis but also yield polymer with poor morphology. 
     Therefore, to reduce production costs, a need exists to develop processes that use cheaper components and/or fewer processing steps for the formation of Ziegler-Nana catalysts capable of producing polymers having similar properties and production throughput as compared to polymers produced from catalysts formed from expensive blends. 
     SUMMARY 
     Embodiments of the present invention include methods of forming catalysts. The methods generally include contacting an alkyl magnesium compound with a viscosity modifier prior to contact with an alcohol to form a magnesium dialkoxide compound; contacting the magnesium dialkoxide compound with a first titanium alkoxide and a first agent to form a first solution reaction product “A”, wherein the titanium alkoxide and the first agent are non-blended individual components prior to contacting, the magnesium dialkoxide; contacting the first solution reaction product “A” with a second titanium alkoxide to form a second solution reaction product “B”; contacting the second solution reaction product “B” with a second agent to form a first solid reaction product “C”; contacting the first solid reaction product “C” with a third agent to form a second solid reaction product “D”; and contacting the second solid reaction product “D” with a reducing agent to form a catalyst component. 
     One or more embodiments include the method of the preceding paragraph, wherein the alkyl magnesium compound is represented by the formula MgR 1 R 2 , wherein R 1  and R 2  are independently selected from C 1  to C 10 , alkyls. 
     One or more embodiments include the method of any preceding paragraph, wherein the alkyl magnesium compound is selected from butyl ethyl magnesium, diethyl magnesium, dipropyl magnesium, dibutyl magnesium, and combinations thereof. 
     One or more embodiments include the method of any preceding paragraph, wherein the viscosity modifier is represented by the formula AlR 3   3 , wherein R 3  is selected from C 1  to C 10  alkyl compounds. 
     One or more embodiments include the method of any preceding paragraph, wherein the viscosity modifier is selected from trimethyl aluminum, triisobutyl aluminum, triethyl aluminum, n-octyl aluminum, n-hexyl aluminum, and combinations thereof. 
     One or more embodiments include the method of any preceding paragraph, wherein the viscosity modifier comprises triethyl aluminum. 
     One or more embodiments include the method of any preceding paragraph, wherein the viscosity modifier contacts the alkyl magnesium compound in an equivalent of from about 0.01 to about 0.6. 
     One or more embodiments include the method of any preceding paragraph, wherein the alcohol is represented by the formula R 4 OH, wherein R 4  is selected from C 2  to C 20  alkyls. 
     One or more embodiments include the method of any preceding paragraph, wherein the alcohol is selected from butanol, isobutanol, 2-ethylhexanol, and combinations thereof. 
     One or more embodiments include the method of any preceding paragraph, wherein the alcohol contacts the alkyl magnesium compound in an equivalent of from about 0.5 to about 6. 
     One or more embodiments include the method of any preceding paragraph, wherein the first titanium alkoxide is represented by the formula Ti(OR 5 ) 4 , wherein R 5  is selected from C 2  to C 20  alkyl groups. 
     One or more embodiments include the method of any preceding paragraph, wherein the first titanium alkoxide is selected from titanium 2-ethylhexyl alkoxide, titanium isopropoxide, titanium n-butoxide, and combinations thereof. 
     One or more embodiments include the method of any preceding paragraph, wherein the first titanium alkoxide contacts the magnesium dialkoxide compound in an equivalent of from about 0.25 to about 3. 
     One or more embodiments include the method of any preceding paragraph, wherein the first agent includes a metal halide. 
     One or more embodiments include the method of any preceding paragraph, wherein the first agent includes titanium halide. 
     One or more embodiments include the method of any preceding paragraph, wherein the first agent contacts the magnesium dialkoxide compound in an equivalent of from about 0.05 to about 2. 
     One or more embodiments include the method of any preceding paragraph, wherein the second titanium alkoxide is represented by the formula Ti(OR 6 ) 4 , wherein R 6  is selected from C 2  to C 20  alkyl groups. 
     One or more embodiments include the method of any preceding paragraph, wherein the second titanium alkoxide is selected from titanium 2-ethylhexyl alkoxide, titanium isopropoxide, titanium n-butoxide, and combinations thereof. 
     One or more embodiments include the method of any preceding paragraph, wherein the second titanium alkoxide contacts the first solution reaction product “A” in a molar equivalent of from about 0.05 to about 3. 
     One or more embodiments include the method of any preceding paragraph, wherein the second agent includes a metal halide. 
     One or more embodiments include the method of any preceding paragraph, wherein the second agent contacts the second solution reaction product “B” in an equivalent of from about 0.5 to about 5. 
     One or more embodiments include the method of any preceding paragraph, wherein the third agent includes a metal halide. 
     One or more embodiments include the method of any preceding paragraph, wherein the third agent contacts the first solid reaction product “C” in an equivalent of from about 0.5 to about 5. 
     One or more embodiments include the method of any preceding paragraph, wherein the reducing agent is selected from an organolithium compound, an organomagnesium compound, an organoaluminum compound, and combinations thereof: 
     One or more embodiments include a catalyst component formed by the method of any preceding paragraph. 
     One or more embodiments include a method for polymerizing olefin monomers. The method generally includes contacting olefin monomer with a catalyst to form a polyolefin, wherein the catalyst is formed by a process comprising: contacting an alkyl magnesium compound with a viscosity modifier prior to contact with an alcohol to form a magnesium dialkoxide compound; contacting the magnesium dialkoxide compound with a first titanium alkoxide and a first agent to form a first solution reaction product “A”, wherein the titanium alkoxide and the first agent are non-blended individual components prior to contacting the magnesium dialkoxide; contacting the first solution reaction product “A” with a second titanium alkoxide to form a second solution reaction product “B”; contacting the second solution reaction product “B” with a second agent to form a first solid reaction product “C”; contacting the first solid reaction product “C” with a third agent to form a second solid reaction product “D”, and contacting the second solid reaction product “D” with a reducing agent to form a catalyst component. 
     One or more embodiments include the method of the preceding paragraph, wherein the polyolefin is high density polyethylene. 
     One or more embodiments include a polyethylene polymer formed by the method of any preceding paragraph. 
    
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         FIG. 1  illustrates the particle size distribution D50 of various catalyst samples. 
         FIG. 2  illustrates the molecular weight distribution of various catalyst samples. 
         FIG. 3  illustrates that H 2 /C 2  feed ratio for polymerization with various catalyst samples. 
     
    
    
     DETAILED DESCRIPTION 
     Introduction and Definitions 
     A detailed description will now be provided. Each of the appended claims defines a separate invention, which for infringement purposes is recognized as including equivalents to the various elements or limitations specified in the claims. Depending on the context, all references below to the “invention” may in some cases refer to certain specific embodiments only. In other cases it will be recognized that references to the “invention” will refer to subject matter recited in one or more, but not necessarily all, of the claims. Each of the inventions will now be described in greater detail below, including specific embodiments, versions and examples, but the inventions are not limited to these embodiments, versions or examples, which are included to enable a person having ordinary skill in the art to make and use the inventions when the information in this patent is combined with available information and technology. 
     Various terms as used herein are shown below. To the extent a term used in a claim is not defined below, it should be given the broadest definition skilled persons in the pertinent art have given that term as reflected in printed publications and issued patents at the time of filing. Further, unless otherwise specified, all compounds described herein may be substituted or unsubstituted and the listing of compounds includes derivatives thereof. 
     Further, various ranges and/or numerical limitations may be expressly stated below. It should be recognized that unless stated otherwise, it is intended that endpoints are to be interchangeable. Further, any ranges include iterative ranges of like magnitude falling within the expressly stated ranges or limitations. 
     The term “activity” refers to the weight of product produced per weight of catalyst used in a process per hour of reaction at a standard set of conditions (e.g. grams product/gram catalyst/hr). 
     The term “substituted” refers to an atom, radical or group that replaces a hydrogen in a chemical compound. 
     The term “blend” refers to a mixture of compounds that are blended and/or mixed prior to contact with another compound. 
     The term “equivalent” refers to a molar ratio of a component to a starting material. 
     As used herein, the term “room temperature” means that a temperature difference of a few degrees does not matter to the phenomenon under investigation, such as a preparation method. In some environments, room temperature may include a temperature of from about 20° C. to about 28° C. (68° F. to 82° F.), while in other environments, room temperature may include a temperature of from about 50° F. to about 90° F., for example. However, room temperature measurements generally do not include close monitoring of the temperature of the process and therefore such a recitation does not intend to bind the embodiments described herein to any predetermined temperature range. 
     Catalyst Systems 
     Ziegler-Natta Catalysts systems are generally formed from the combination of a metal component (e.g. a catalyst precursor) with one or more additional components, such as a catalyst support, a cocatalyst and/or one or more electron donors, for example. 
     A specific example of a Ziegler-Natta catalyst includes a metal component generally represented by the formula: 
       MR x ; 
     wherein M is a transition metal; R is a halogen, an alkoxy, or a hydrocarboxyl group; and x is the valence of the transition metal. For example, x may be from 1 to 4. 
     The transition metal may be selected from Groups IV through VIB (e.g. titanium, vanadium, or chromium), for example. R may be selected from chlorine, bromine, carbonates, esters, or an alkoxy groups in one embodiment. Examples of catalyst components include TiCl 4 , TiBR 4 , Ti(OC 4 H 9 ) 3 Cl, Ti(OC 4 H 9 ) 2 Cl 2 , Ti(OC 3 H 5 ) 3 Cl, Ti(OC 3 H 7 ) 2 Cl 2 , Ti(OC 6 H 13 ) 2 Cl 2 , Ti(OC 2 H 5 ) 2 Br 2  and Ti(OC 12 H 25 )Cl 3 , for example. 
     Those skilled in the art will recognize that a catalyst may be “activated” in some way before it is useful for promoting polymerization. As discussed further below, activation may be accomplished by contacting the catalyst with an activator, which is also referred to in some instances as a “cocatalyst”. Embodiments of Ziegler-Natta activators include organoaluminum compounds, such as trimethyl aluminum (TMA), triethyl aluminum (TEAl) and triisobutyl aluminum (TiBAl), for example. 
     The Ziegler-Natta catalyst system may further include one or more electron donors, such as internal electron donors and/or external electron donors. Internal electron donors may be used to reduce the atactic form of the resulting polymer, thus decreasing the amount of xylene soluble material in the polymer. The internal electron donors may include amines, amides, esters, ketones, nitriles, ethers, thioethers, thioesters, aldehydes, alcoholates, salts, organic acids, phosphines, diethers, succinates, phthalates, malonates, maleic acid derivatives, dialkoxybenzenes or combinations thereof, for example. (See. U.S. Pat. No. 5,945,366 and U.S. Pat. No. 6,399,837, which are incorporated by reference herein.) 
     External electron donors may be used to further control the amount of atactic polymer produced. The external electron donors may include monofunctional or polyfunctional carboxylic acids, carboxylic anhydrides, carboxylic esters, ketones, ethers, alcohols, lactones, organophosphorus compounds and/or organosilicon compounds, for example. In one embodiment, the external donor may include diphenyldimethoxysilane (DPMS), cyclohexylmethyldimethoxysilane (CMDS), diisopropyldimethoxysilane (DIDS) and/or dicyclopentyldimethoxysilane (CPDS), for example. The external donor may be the same or different from the internal electron donor used. 
     The components of the Ziegler-Matta catalyst system (e.g., catalyst, activator and/or electron donors) may or may not be associated with a support, either in combination with each other or separate from one another. The Ziegler-Naha support materials may include a magnesium dihalide, such as magnesium dichloride or magnesium dibromide, silica, or alumina, for example. 
     Specific, non-limiting examples of formation processes for Ziegler-Natty catalysts are described in U.S. Pat. No. 6,734,134 and U.S. Pat. No. 6,174,971, which are incorporated by reference herein. 
     Embodiments of the invention generally include utilizing non-blended components during catalyst formation. A representative, non-limiting, illustration of a possible reaction scheme for use in embodiments of the invention may be illustrated as follows: 
       MgR 1 R 2 /AlR 3   3 +2R 4 OH→Mg(OR 4 ) 2   1)
 
       Mg(OR 4 ) 2 +Ti(OR 5 ) 4 +TiCl 4 →“A” (soln.)   2)
 
       “A” (soln.) +Ti(OR 6 ) 4 →“B” (soln.)   3)
 
       “B” (soln) +TiCl 4 →“C” (solid)   4)
 
       “C” (solid) +TiCl 4 →“D” (solid)   5)
 
       “D” (solid) +AlR 7   3 →Catalyst  6)
 
     Note that while the primary reaction components are illustrated above, additional components may be reaction products or used in such reactions and not illustrated above. Further, while described herein in terms of primary reaction steps, it is known to those skilled in the art that additional steps may be included in the reaction schemes and processes described herein (e.g. washing, filtering, drying, stirring, agitating, decanting steps), while it is further contemplated that other steps may be eliminated in certain embodiments. In addition, it is contemplated that any of the agents described herein may be added in combination with one another so long as the order of addition complies with the spirit of the invention. 
     As illustrated by the reaction scheme above, embodiments of the invention include methods of forming Ziegler-Natta catalysts. The methods generally include the formation and/or providing of a magnesium dialkoxide compound represented by the formula Mg(OR 4 ) 2 . In one embodiment, the magnesium dialkoxide compound may be formed by contacting a magnesium containing compound with an alcohol to form the magnesium dialkoxide compound. In one or more embodiments, this reaction is conducted at a reaction temperature of from room temperature to about 90° C. or from room temperature to about 85° C. for a time of up to about 10 hours, for example. 
     The magnesium containing compound may be represented by the formula: 
       MgR 1 R 2 ; 
     wherein R 1  and R 2  are independently selected from C 1  to C 10  alkyl groups. Non-limiting illustrations of magnesium containing compounds include butyl ethyl magnesium (BEM), diethyl magnesium, dipropyl magnesium and dibutyl magnesium, for example. 
     The alcohol may be represented by the formula: 
       R 4 OH; 
     wherein R 4  is selected from C 2  to C 20  alkyl groups. Non-limiting illustrations of alcohols include butanol, isobutanol and 2-ethylhexanol, for example. The alcohol may be added to the magnesium containing compound in an equivalent (i.e. per mole of [Mg]) of from about 0.5 to about 6 or from about 1 to about 3, for example. 
     The method may further include contacting or blending the magnesium containing compound with a viscosity modifier to make the resultant solution more amenable for controlled, larger catalyst particle size precipitation. The viscosity modifier may include organoaluminum compounds represented by the formula: 
       AlR 3   3 ; 
     wherein R 3  is selected from C 1  to C 10  alkyl compounds. Non-limiting illustrations of the aluminum alkyl compounds generally include trimethyl aluminum (TMA), triisobutyl aluminum (TiBAl), triethyl aluminum (TEAl), n-octyl aluminum and n-hexyl aluminum, for example. In one specific embodiment, the viscosity modifier includes TEAl. In general, an increase in the amount of viscosity modifier added increases the catalyst D 50  particle size and improves fluff morphology. Thus, depending upon the desired catalyst particle size and fluff morphology, the viscosity modifier may be added to the magnesium-containing compound in a molar equivalent of from about 0.01 to about 0.6, or from about 0.05 to about 0.4 or tram about 0.1 to about 0.3, for example. 
     In preparing the resultant magnesium dialkoxide compound, the amount of alcohol R 4 OH added to the magnesium-containing compound may be adjusted to convert substantially all metal alkyls to non-reducing metal alkoxides. For example, the alcohol may be added to the magnesium containing compound/viscosity modifier in a molar equivalent of from about 1 to about 6, or from about 1 to about 3 or from about 2 to about 3, for example. 
     In subsequent steps, prior efforts to sequentially form the Ziegler-Matta catalyst generally utilized blends of specialty chemicals having a high production cost. Conversely, the various embodiments of the present invention generally include replacing blended agents with cheaper non-blended components, thereby substantially reducing catalyst production cost by as much as about 75% while retaining one or more of the beneficial properties (e.g. polymer activity, fluff particle size distribution) of catalysts obtained via blends. 
     In particular, embodiments include a subsequent step of contacting the magnesium dialkoxide compound with a second compound and a third compound to form a reaction product “A”. The resulting reaction product “A” is a solution product. As used herein, “solution” refers to homogenous mixture of two or more compounds. 
     This reaction may occur in the presence of an inert solvent. A variety of hydrocarbons can be used as the inert solvent, but any hydrocarbon selected should remain in liquid form at all relevant reaction temperatures and the ingredients used to form the supported catalyst composition should be at least partially soluble in the hydrocarbon. Accordingly, the hydrocarbon is considered to be a solvent herein, even though in certain embodiments the ingredients are only partially soluble in the hydrocarbon. Suitable hydrocarbon solvents include substituted and unsubstituted aliphatic hydrocarbons and substituted and unsubstituted aromatic hydrocarbons. For example, the inert solvent may include hexane, heptane, octane, decane, toluene, xylene, dichloromethane, chloroform, 1-chlorobutane or combinations thereof, for example. 
     In one or more embodiments, this reaction is conducted at a temperature of from about 0° C. to about 100° C. or from about 20° C. to about 90° C. for a time of from about 0.2 hours to about 24 hours or from about 1 hour to about 4 hours, for example. 
     The second compound is a titanium alkoxide generally represented by the formula: 
       Ti(OR 5 ) 4 ; 
     wherein R 5  is selected from C 2  to C 20  alkyl groups. Non-limiting illustrations of the second compound include titanium alkoxides, such as titanium 2-ethylhexyl alkoxide, titanium isopropoxide Ti(OiPr) 4 , titanium n-butoxide Ti(OBu) 4 , and combinations thereof. The titanium alkoxide may be added to the magnesium alkoxide compound in a molar equivalent of from about 0.25 to about 3, or from about 0.5 to about 2 or from about 0.5 to about 1, for example. 
     The third compound is a first metal halide. In one example, the first metal halide may be added to the magnesium dialkoxide compound in a molar equivalent of from about 0.05 to about 2, or from about 0.1 to about 1 or from about 0.1 to about 0.5, for example. 
     The first metal halide may include any metal halide known to one skilled in the art, such as titanium tetrachloride (TiCl 4 ), for example. 
     The method further includes contacting the reaction product “A” with a titanium alkoxide to form reaction product “B”. The resulting reaction product “B” is also a solution product. The titanium alkoxide may generally be represented by the formula: 
       Ti(OR 6 ) 4 ; 
     wherein R 6  is selected from C 2  to C 20  alkyl groups. Non-limiting illustrations of titanium alkoxides include titanium 2-ethylhexyl alkoxide, titanium n-butoxide Ti(OBu) 4 , titanium isopropoxide Ti(OiPr) 4 , and combinations thereof. The titanium alkoxide may be added to the reaction product “A” in a molar equivalent of from about 0.05 to about 3, or from about 0.1 to about 1.0 or from about 0.25 to about 0.75, for example. 
     The method may then include contacting reaction product “B” with a second metal halide to form a solid reaction product “C”. This reaction may occur in the presence of an inert solvent. The inert solvents may include any of those solvents previously discussed herein, for example. 
     In one or more embodiments, this reaction is conducted at a temperature of from about 0° C. to about 100° C. or from about 20° C. to about 90° C. for a time of from about 0.2 hours to about 36 hours or from about 1 hour to about 4 hours, for example. 
     The second metal halide may be added to reaction product “B” in an amount sufficient to precipitate solid reaction product “C” out of solution. The second metal halide may include any metal halide known to one skilled in the art, such as titanium tetrachloride (TiCl 4 ), for example. The second metal halide may contact reaction product “B” in a molar equivalent of from about 0.5 to about 5, or from about 1 to about 4 or from about 1.5 to about 2.5, for example. 
     The method may then include contacting solid reaction product “C” with a third metal halide to form solid reaction product “D”. This reaction may occur in the presence of an inert solvent, for example. The inert solvents may include any of those solvents previously discussed herein, for example. Further, in one or more embodiments, the reaction is conducted at room temperature. 
     The third metal halide may include any metal halide known to one skilled in the art, such as TiCl 4 , for example. The third metal halide may contact reaction product “C” in a molar equivalent of from about 0.5 to about 5, or from about 1 to about 4 or from about 1.5 to about 2.5, for example. 
     The method then includes reducing the reaction product “D” to form an active catalyst. In one embodiment, reaction product “D” is reduced by contacting the reaction product “D” with a reducing agent AlR 7   3 . The reducing agent may be added to the reaction product “D” in a molar equivalent of from about 0.02 to about 2, or from about 0.05 to about 0.5 or from about 0.1 to about 0.25, for example. 
     The reducing agent may be selected from organolithium compounds, organomagnesium compounds, organoaluminum compounds, and combinations thereof, for example. In one, non-limiting embodiment, the organoaluminum compound is represented by the formula: 
       AlR 7   3    
     wherein R 7   3  is selected from C 1  to C 10  alkyl compounds. Non-limiting illustrations of the aluminum alkyl compounds generally include trimethyl aluminum (TMA), triisobutyl aluminum (TIBAl), triethyl aluminum (TEAl), n-octyl aluminum and n-hexyl aluminum, for example. In one specific embodiment, the reducing agent includes TEAl. The resulting catalyst is suitable for the polymerization of olefins. 
     As previously described, upon formation of a first solid reaction product “C”, only one subsequent precipitation step is needed to form a second solid reaction product “D” prior to the reducing step to form a catalyst component of the present invention. In contrast, prior efforts to sequentially form the Ziegler-Matta catalyst generally utilized several precipitation steps subsequent to the initial formation of a solid reaction product and prior to a reducing step to form a catalyst. The use of fewer precipitation processing steps described herein for the formation of Ziegler-Matta catalysts capable of producing polymers having similar properties to polymers produced from catalysts formed from expensive blends and/or with additional precipitation steps advantageously enhances production throughput which also further reduces production and/or labor costs. 
     In one or more embodiments, it has been found that catalysts produced from the reaction scheme disclosed herein may exhibit somewhat smaller D 50  particle size and a lower fluff bulk density, while concomitantly demonstrating a higher activity, as compared to Ziegler-Natta catalyst formed from expensive blends. Furthermore, the catalysts produced from the reaction scheme disclosed may herein exhibit no fines and similar fluff particle size distribution as compared to Ziegler-Natta catalyst formed from expensive blends. 
     In yet another aspect, introducing the viscosity modifier AlR 3   3  in such step of the catalyst synthesis scheme may also advantageously lead to faster solid particle settling rate during synthesis. In one or more embodiments, the solids (e.g., intermediates) settling time is less than 15 minutes, for example. 
     Controlling the precipitation steps of the catalyst synthesis scheme by adjustments to either the concentration of the soluble catalyst precursor (i.e. [Mg]) or the precipitating agent (e.g., [TiCl 4 ]), or both, provides an effective means of adjusting the morphology of the solid catalyst component that results. For example, decreasing the concentration of the [Mg] in the catalyst synthesis solution may result in increased average particle size of the resulting catalyst component. 
     To increase batch yield and further reduce production cost, it may be desirable to reduce the amount of solvent at precipitation; however prior efforts have generally resulted in unacceptably small catalyst D 50  particle size due to a concomitant increase in [Mg]. It has been found that utilizing the viscosity modifier AlR 3   3  results in sufficiently large catalyst D 50  particle size even while utilizing additional cost saving measures, such as reducing the quantity of solvent at precipitation. 
     Polymerization Processes 
     As indicated elsewhere herein, catalyst systems are used to form polyolefin compositions. Once the catalyst system is prepared, as described above and/or as known to one skilled in the art, a variety of processes may be carried out using that composition. The equipment, process conditions, reactants, additives and other materials used in polymerization processes will vary in a given process, depending on the desired composition and properties of the polymer being formed. Such processes may include solution phase, gas phase, slurry phase, bulk phase, high pressure processes or combinations thereof, for example. (See. U.S. Pat. No. 5,525,678; U.S. Pat. No. 6,420,580; U.S. Pat. No. 6,380,328; U.S. Pat. No. 6,359,072; U.S. Pat. No. 6,346,586; U.S. Pat. No. 6,340,730; U.S. Pat. No. 6,339,134; U.S. Pat. No. 6,300,436; U.S. Pat. No. 6,274,684; U.S. Pat. No. 6,271,323; U.S. Pat. No. 6,248,845; U.S. Pat. No. 6,245,868; U.S. Pat. No. 6,245,705; U.S. Pat. No. 6,242,545; U.S. Pat. No. 6,211,105; U.S. Pat. No. 6,207,606; U.S. Pat. No. 6,180,735 and U.S. Pat. No. 6,147,173, which are incorporated by reference herein.) 
     In certain embodiments, the processes described above generally include polymerizing one or more olefin monomers to form polymers. The olefin monomers may include C 2  to C 30  olefin monomers, or C 2  to C 12  olefin monomers (e.g. ethylene, propylene, buten, pentene, 4-methyl-1-pentene, hexene, octene and decene), for example. The monomers may include olefinic unsaturated monomers, C 4  to C 18  diolefins, conjugated or nonconjugated dienes, polyenes, vinyl monomers and cyclic olefins, for example. Non-limiting examples of other monomers may include norbornene, norbornadiene, isobutylene, isoprene, vinylbenzycyclobutane, styrene, alkyl substituted styrene, ethylidene norbornene, dicyclopentadiene and cyclopentene, for example. The formed polymer may include homopolymers, copolymers or terpolymers, for example. 
     Examples of solution processes are described in U.S. Pat. No. 4,271,060, U.S. Pat. No. 5,001,205, U.S. Pat. No. 5,236,998 and U.S. Pat. No. 5,589,555, which are incorporated by reference herein. 
     One example of a gas phase polymerization process includes a continuous cycle system, wherein a cycline gas stream (otherwise known as a recycle stream or fluidizing medium) is heated in a reactor by heat of polymerization. The heat is removed from the cycling gas stream in another part of the cycle by a cooling system external to the reactor. The cycling gas stream containing one or more monomers may be continuously cycled through a fluidized bed in the presence of a catalyst under reactive conditions. The cycling gas stream is generally withdrawn from the fluidized bed and recycled back into the reactor. Simultaneously, polymer product may be withdrawn from the reactor and fresh monomer may be added to replace the polymerized monomer. The reactor pressure in a gas phase process may vary from about 100 psig to about 500 psig, or from about 200 psig to about 400 psig, or from about 250 psig to about 350 psig, for example. The reactor temperature in a gas phase process may vary from about 30° C. to about 120° C. or from about 60° C. to about 115° C., or from about 70° C. to about 110° C. or from about 70° C. to about 95° C., for example. (See, for example, U.S. Pat. No. 4,543,399; U.S. Pat. No. 4,588,790; U.S. Pat. No. 5,028,670; U.S. Pat. No. 5,317,036; U.S. Pat. No. 5,352,749; U.S. Pat. No. 5,405,922; U.S. Pat. No. 5,436,304; U.S. Pat. No. 5,456,471; U.S. Pat. No. 5,462,999; U.S. Pat. No. 5,616,661; U.S. Pat. No. 5,627,242; U.S. Pat. No. 5,665,818; U.S. Pat. No. 5,677,375 and U.S. Pat. No. 5,668,228, which are incorporated by reference herein.) 
     Slurry phase processes generally include forming a suspension of solid, particulate polymer in a liquid polymerization medium, to which monomers and optionally hydrogen, along with catalyst, are added. The suspension (which may include diluents) may be intermittently or continuously removed from the reactor where the volatile components can be separated from the polymer and recycled, optionally after a distillation, to the reactor. The liquefied diluent employed in the polymerization medium may include a C 3  to C 7  alkane (e.g. hexane or isobutane), for example. The medium employed is generally liquid under the conditions of polymerization and relatively inert. A hulk phase process is similar to that of a slurry process with the exception that the liquid medium is also the reactant (e.g., monomer) in a bulk phase process. However, a process may be a bulk process, a slurry process or a bulk slurry process, for example. 
     In a specific embodiment, a slurry process or a hulk process may be carried out continuously in one or more loop reactors. The catalyst, as slurry or as a dry free flowing powder, may be injected regularly to the reactor loop, which can itself be filled with circulating slurry of growing polymer particles in a diluent, for example. Optionally, hydrogen (or other chain terminating agents, for example) may be added to the process, such as for molecular weight control of the resultant polymer. The loop reactor may be maintained at a pressure of from about 27 bar to about 50 bar or from about 35 bar to about 45 bar and a temperature of from about 38° C. to about 121° C., for example. Reaction heat may be removed through the loop wall via any suitable method, such as via a double-jacketed pipe or heat exchanger, for example. 
     Alternatively, other types of polymerization processes may be used, such as stirred reactors in series, parallel or combinations thereof, for example. Upon removal from the reactor, the polymer may be passed to a polymer recovery system for further processing, such as addition of additives and/or extrusion, for example. 
     Polymer Product 
     The polymers (and blends thereof) formed via the processes described herein may include, but are not limited to, linear low density polyethylene, elastomers, plastomers, high density polyethylenes, low density polyethylenes, medium density polyethylenes, polypropylene and polypropylene copolymers, for example. 
     Unless otherwise designated herein, all testing methods are the current methods at the time of filing. 
     In one or more embodiments, the polymers include ethylene based polymers. As used herein, the term “ethylene based” is used interchangeably with the terms “ethylene polymer” or “polyethylene” and refers to a polymer having at least about 50 wt. %, or at least about 70 wt. %, or at least about 75 wt. %, or at least about 80 wt. %, or at least about 85 wt. %, or at least about 90 wt. % polyethylene relative to the total weight of polymer, for example. 
     The ethylene based polymers may have a density (as measured by ASTM D-792) of from about 0.86 g/cc to about 0.98 g/cc, or from about 0.88 g/cc to about 0.965 g/cc, or from about 0.90 g/cc to about 0.965 g/cc, or from about 0.925 g/cc to about 0.97 g/cc, for example. 
     The ethylene based polymers may have a melt index (MI 2 ) (as measured by ASTM D-1238) of from about 0.01 dg/min to about 100 dg/min., or from about 0.01 dg/min. to about 25 dg/min. or from about 0.03 dg/min. to about 15 dg/min., or from about 0.05 dg/min. to about 10 dg/min, for example. 
     In one or more embodiments, the polymers include low density polyethylene. 
     In one or more embodiments, the polymers include linear low density polyethylene. 
     In one or more embodiments, the polymers include medium density polyethylene. As used herein, the term “medium density polyethylene” refers to ethylene based polymers having a density of from about 0.92 g/cc to about 0.94 g/cc, or from about 0.926 Wee to about 0.94 g/cc, for example. 
     In one or more embodiments, the polymers include high density polyethylene. As used herein, the term “high density polyethylene” refers to ethylene based polymers having a density of from about 0.94 g/cc to about 0.97 g/cc, for example. 
     Product Application 
     The polymers and blends thereof are useful in applications known to one skilled in the art, such as forming operations (e.g. film, sheet, pipe and fiber extrusion and co-extrusion as well as blow molding, injection molding and rotary molding). Films include blown, oriented or cast films formed by extrusion or co-extrusion or by lamination useful as shrink film, cling film, stretch film, sealing films, oriented films, snack packaging, heavy duty bags, grocery sacks, baked and frozen food packaging, medical packaging, industrial liners, and membranes, for example, in food-contact and non-food contact application. Fibers include slit-films, monofilaments, melt spinning, solution spinning and melt blown fiber operations for use in woven or non-woven torn to make sacks, bags, rope, twine, carpet backing, carpet yarns, filters, diaper fabrics, medical garments and geotextiles, for example. Extruded articles include medical tubing, wire and cable coatings, sheets, such as thermoformed sheets (including profiles and plastic corrugated cardboard), geomembranes and pond liners, for example. Molded articles include single and multi-layered constructions in the form of bottles, tanks, large hollow articles, rigid food containers and toys, for example. 
     EXAMPLES 
     Two catalysts were synthesized for comparison (via the catalyst synthesis method described below), Catalyst 1 via Scheme 1 below and Catalyst 2 via Scheme 2 below. It was observed that Catalyst 1 exhibited a smaller catalyst D50 than that of Catalyst 2 (see,  FIG. 1 ). 
     Scheme 1 
     Comparative 
       BEM+2.2equiv.2-ethylhexanol(2-EHOH)→Mg(2-EHO)2
 
       Mg(2-EHO)2+ClTi(OiPr)3→solution A
 
       Solution A+2TiCl4/TNBT→solid B
 
       Solid B+2equiv.TiCl4→solid C
 
       Solid C+0.16equiv.TEAl→1277-017
 
     Scheme 2 
       BEM+2.2equiv.2-ethylhexanol(2-EHOH)→Mg(2-EHO)2
 
       Mg(2-EHO)2+0.75equiv.Ti(OiPr)4+0.25equiv.TiCl4→solution A
 
       Solution A+0.5equiv.TNBT→solution B
 
       Solution B+2equiv.TiCl4→solid C
 
       Solid C+2equiv.TiCl4→solid D
 
       Solid D+0.16equiv.TEAl→Catalyst
 
     Catalyst 1 Syntheses: MAGALA BEM (16.8 wt % BEM and 0.12 wt % Al in TEAl in heptane) and TEAl (25 wt % in heptane), 2-EHOH, TNBT, TiCl4, ClTi(OiPr)3 (1.0 M in hexane), and Ti(OiPr) 4  were purchased and used as received. Hexane used for catalyst preparation and polymerization was purchased and purified by passing through molecular sieves and copper catalyst purification columns. Catalysts were synthesized in a 500 mL glass reactor with Morton-type indentation. An overhead agitator consisting of a metal shaft with two sets of three-blades impeller and an addition funnel were used. Catalysts were prepared under plant nitrogen at room temperature with an agitation speed of 250 RPM unless otherwise stated. 
     54.7 g (84 mmol) BEM diluted by hexane to 100 mL was transferred to a reactor via cannular with positive nitrogen. 20 mL hexane was added to rinse the cannular and the graduated cylinder. The agitation was started and 28.16 g (216 mmol) 2-EHOH diluted by hexane to a 50 mL solution was drop wise added to the reactor. After the addition, the solution was stirred for an hour. 50 mL 2.0 M ClTi(OiPr) 3  (100 mmol) hexane solution was further diluted by hexane to 100 mL and transferred slowly to the reactor via cannular. After the addition, the solution was further stirred for one hour. Pre-prepared 300 mL hexane solution of TiCl 4 /TNBT (TiCl 4 =37.04 g. 200 mmol and TNBT=34.4 g, 100 mmol) was drop wise added to the stirring solution over two hours. After the addition, the slurry was further stirred for one hour. The solid was washed three times with hexane, each with 200 mL. 100 mL hexane was added and the agitation resumed. 100 mL hexane solution of 37.04 g (200 mmol) TiCl 4  was slowly added to the slurry. After the addition, the slurry was further stirred for one hour. The solid was then washed live times, each with 200 mL hexane. Another 100 mL hexane was added. 50 mL hexane solution of TEAl (7.39 g. 16 mmol) was slowly added. The slurry became dark brown. The slurry was further stirred for one hour and collected for catalyst characterization. 
     Catalyst 2 Syntheses: Catalyst 2 was synthesized similar to that of Catalyst 1 except that 1) ClTi(OiPr) 3  was replaced by first adding 20.68 g (75 mmol) Ti(OiPr) 4  followed by one hour stirring, and then 4.70 g (25 mmol) TiCl 4 , and 2) instead of using pre-prepared TiCl 4 /TNBT. 17.02 g (50 mmol) TNBT was added and the solution was stirred for 1 hour, then 37.04 g (200 mmol) TiCl 4  was dropwise added to form the solid. 
     Reference catalyst elemental components and those of Catalyst 1 and 2 are illustrated in Table 1 below. 
     
       
         
           
               
               
             
               
                   
                 TABLE 1 
               
             
            
               
                   
                   
               
               
                   
                 Catalyst 
               
            
           
           
               
               
               
               
            
               
                   
                 Reference 
                 Catalyst 1 
                 Catalyst 2 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                   
                 Al (wt %) 
                 3.6 
                 2.8 
                 2.1 
               
               
                   
                 Mg (wt %) 
                 13.1 
                 13.6 
                 12.4 
               
               
                   
                 Ti (wt %) 
                 8.8 
                 6.3 
                 9.2 
               
               
                   
                   
               
            
           
         
       
     
     Polymers were formed with the various catalysts via the conditions illustrated in Table 2 (H 2 /C 2 =0.25 and H 2 /C 2  feed ratio of 1.0). 
     
       
         
           
               
               
               
             
               
                   
                 TABLE 2 
               
               
                   
                   
               
             
            
               
                   
                 Cocatalyst [TlBAl] 
                 0.25 mmol/L 
               
               
                   
                 Temperature 
                 80° C. 
               
               
                   
                 Polymerization time 
                 1 hr 
               
               
                   
                 Pressure 
                 125 psi 
               
               
                   
                 Diluent 
                 Hexane 
               
               
                   
                 Ethylene flow rate 
                 8 SLPM 
               
               
                   
                 H2/C2 feed ratios 
                 0.25, 1.0 
               
               
                   
                   
               
            
           
         
       
     
     Targeted polymer properties and those formed from Catalyst 1 and 2 are illustrated in Table 3 below and  FIG. 2 . 
     
       
         
           
               
               
               
               
             
               
                   
                 TABLE 3 
               
               
                   
                   
               
               
                   
                 Reference 
                   
                   
               
               
                   
                 catalyst 
                 Catalyst 1 
                 Catalyst 2 
               
               
                   
                   
               
             
            
               
                   
               
            
           
           
               
               
               
               
            
               
                 Adj. H 2 /C 2   
                 0.49 
                 0.44 
                 0.57 
               
               
                 Mg based Activity (g/g/h) 
                 15000 
                 14000 
                 37000 
               
               
                 B.D. (g/cc) 
                 0.41 
                 0.38 
                 0.33 
               
               
                 D50 (μm) 
                 222 
                 460 
                 497 
               
               
                 Span 
                 0.9 
                 0.9 
                 1.1 
               
               
                 Fines (%) 
                 0 
                 0 
                 0 
               
               
                 Density (g/cc) 
                 0.952 
                 0.950 
                 0.952 
               
               
                 M12 (dg/min) 
                 0.76 
                 1.05 
                 0.81 
               
               
                 M15 (dg/min) 
                 2.57 
                 3.59 
                 2.59 
               
               
                 HLM1 (dg/min) 
                 31.44 
                 47.80 
                 28.96 
               
               
                 SR2 
                 41.2 
                 45.6 
                 35.7 
               
               
                 SR5 
                 12.2 
                 13.3 
                 11.2 
               
               
                 Wax (%) 
                 0.3 
                 0.6 
                 0.2 
               
               
                 Mn (g/mol) 
                 18000 
                 18000 
                 18000 
               
               
                 Mw (g/mol) 
                 137000 
                 145000 
                 130000 
               
               
                 Mz (g/mol) 
                 738000 
                 849000 
                 639000 
               
               
                 Mw/Mn 
                 7.7 
                 8.1 
                 7.1 
               
               
                 Mz/Mw 
                 5.4 
                 5.9 
                 4.9 
               
               
                 Ea (KJ/mol) 
                 25.02 
                 27.9 
                 25.4 
               
               
                 η (Pa * s) 
                 23200 
                 17000 
                 16600 
               
               
                 λ (s) 
                 0.0129 
                 0.0109 
                 0.0109 
               
               
                 a 
                 0.273 
                 0.291 
                 0.301 
               
               
                   
               
            
           
         
       
     
     The polymerization results illustrate that the various catalysts do not produce identical polymers (as further illustrated in  FIG. 3 ). In summary, Catalyst 1 showed similar catalyst characteristic to the reference polymer properties. e.g. catalyst activity, polymer molecular weight distribution, and rheology. However. Catalyst 2 had a higher activity, slightly lower bulk density, narrower molecular weight distribution and lower hydrogen response than either Catalyst 1 or the reference catalyst. All final catalysts and their intermediates were measured by Malvern hydro 2000 μP in hexane slurry forms. Malvern Scirocco 2000 was used for polymer samples. 
     While the foregoing is directed to embodiments of the present invention, other and limiter embodiments of the invention may be devised without departing from the basic scope thereof and the scope thereof is determined by the claims that follow.