Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond

Definitions

• This invention relates to a new transition metal-magnesium catalyst precursor used to prepare catalysts which are useful for the polymerization of olefins. More particularly, this invention relates to a new method for the preactivation of a transition metal catalyst wherein the catalyst precursor is preactivated by adding a preformed magnesium source or compound to a solution containing transition metal compound(s) and an alkyl halide. As used herein, the term "preactivation” means contacting the transition metal with a magnesium compound and one or more alkyl halide(s) .
• olefins such as ethylene can be polymerized by means of a solid catalyst which comprises: a compound of -a transition metal such as titanium in the trivalent or tetravalent state, and a co-catalyst comprising a reducing agent, such as an organo-metallic or, more specifically, an organo-aluminum compound.
• a solid catalyst which comprises: a compound of -a transition metal such as titanium in the trivalent or tetravalent state, and a co-catalyst comprising a reducing agent, such as an organo-metallic or, more specifically, an organo-aluminum compound.
• MgCl 2 such as MgCl 2 . See, for example, Barbe, P.C., Cecchin, G. ,
• a quantity of MgCl 2 and one or more titanium 10 procatalysts are mixed together in a nonpolar solvent to
• the magnesium is used 34 in a reactive form which is substantially devoid of impurities due in particular to oxidation of the metal.
• Avaro et al. state that, in practice, the magnesium in the industry is activated before being introduced into the medium in which preactivation is effected.
• previous activation of the magnesium can, for example, comprise grinding the metal in an inert atmosphere or in an inert liquid such as an aliphatic solvent. This preliminary operation can also be effected by treating the magnesium with iodine. It is stated to be more convenient, however, to activate the magnesium within the medium in which preactivation is effected.
• the catalyst may be preactivated by
• R is an alkyl radical which may contain from 2 to
• alkylmagnesium halide is first prepared by reacting powdered H magnesium in a flask with an alkyl halide in heptane with an I 5 iodine crystal. A solution of titanium compounds is added lfi to the resulting suspension of alkylmagnesium halide over a
• catalyst precursor is prepared by the process comprising:
• M is at least one transition metal from Group IVB and Group VB of the Periodic Table of the Elements;
• R' is an alkyl group having from 1 to 8 carbon atoms, an alkenyl group having from 2 to 8 carbon atoms, or an aryl group having from 6 to 12 carbon atoms;
• X' is halide;
• t is 3 or 4; and
• s is an integer between 0 and 4, inclusive.
• a catalyst precursor as described above with the limitation that when q is 1 and when M comprises titanium, s is at least one and (t-s) is at least one.
• Also provided in accordance with the present invention is a method for the preparation of a catalyst precursor, useful to make catalysts useful in the polymerization of olefins, comprising adding a preformed magnesium source to a liquid solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined in (b) (2) above.
• a catalyst precursor having the limitation that when q is 1 and when M consists essentially of titanium, s is at least one and (t- s) is at least one.
• the present invention also provides a catalyst precursor, useful to make catalysts useful in the polymerization of olefins, comprising the product obtained by reacting a preformed magnesium source with a solution comprising a solvent having dissolved therein (a) a transition metal compound; and (b) an alkyl halide, said catalyst precursor being comprised of hollow and approximately spheroidal particles.
• a polymerization catalyst useful for the polymerization of olefins, prepared by a process comprising adding an organoaluminum compound, preferably tri-n-octyl-aluminum or triethylaluminum, to the product obtained by adding a preformed magnesium source to a solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined above.
• Also provided in accordance with the present invention is an improved process for the polymerization of olefins in the presence of a polymerization catalyst, wherein the improvement comprises employing a catalyst made from a catalyst precursor comprising the product obtained by adding a preformed magnesium compound to a liquid solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined above.
• Also provided in accordance with the present invention is an improved process for the polymerization of olefins in the presence of a polymerization catalyst, wherein the improvement comprises employing a catalyst made from a catalyst precursor comprising the product obtained by reacting a preformed magnesium compound and a liquid solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined above; wherein said catalyst is comprised of hollow particles.
• a prepolymer useful for the polymerization of olefins, obtained by the process comprising: (i) reacting a catalyst precursor formed by adding a preformed magnesium compound to a solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined above; with (2) an activator, such as triethylaluminum or tri-n-octylaluminum; and (3) contacting the product of step (2) with a sufficient amount of olefin (preferably ethylene) , under olefin polymerization conditions, such that the product obtained has a melt index in the range of about 0.1 to about 5.
• the present invention involves a process for the polymerization of olefins, the process comprising: (a) making a preformed magnesium compound in a solvent;
• step (c) adding the product of step (a) to the solution of step (b) ;
• step (d) adding trialkylaluminum to the product obtained from step (c) ;
• step (e) reacting the product of step (d) with a sufficient amount of olefin, under olefin polymerization conditions, such that the product formed has a melt index in the range of about 0.1 to about 5;
• step (f) reacting the product of step (e) with sufficient olefin, under olefin polymerization conditions, to produce polyolefin resin.
• the present invention is based on the discovery that a better catalyst is made by reversing the traditional order of addition of reactants in a transition metal-magnesium catalyst precursor synthesis. More particularly, the present invention is based on the discovery that the catalyst precursor made by adding a preformed magnesium compound to a solution comprising a solvent having dissolved therein: (a) an alkyl halide; and (b) at least one transition metal compound as defined above produces olefin polymerization catalysts which are surprisingly more advantageous than catalysts obtained from catalyst precursors made by adding the solution of transition metal compounds to the preformed magnesium compound.
• Some of the advantages of the present invention over the prior art are: the surprisingly high hydrogen response of the catalyst, production of fewer fine particles at the synthesis stage using raw catalyst and prepolymers, the catalysts' unique morphology, which is different from prior catalysts in that the present invention's catalysts are comprised of hollow particles, and the ability of catalyst of this invention to incorporate more comonomer than similar prior-art catalyst.
• Figure 1 is a graph depicting melt index of polymers made in accordance with the present invention as a function of hydrogen pressure.
• Figure 2 is a bar graph showing the effect of catalyst type on the production of polyethylene fine particles.
• the terms "normal addition” and “reverse addition” will be used herein to describe the prior art method and the method of the present invention for making transition metal-magnesium olefin polymerization catalyst precursors.
• the "normal addition” a solution of transition metal compound(s) and alkyl halide is added to a magnesium compound(s) .
• the "reverse addition” preformed magnesium compound(s) is added to a solution of transition metal compound(s) and alkyl halide.
• catalyst precursor refers to the transition metal-magnesium product obtained by reacting a transition metal compound(s) , a magnesium source, and alkyl halide.
• the catalyst precursor is not an olefin polymerization catalyst, but can be activated to become one.
• the present invention is a process for the polymerization of olefins, preferably alpha-olefins, more preferably ethylene.
• Preferred olefins are alpha-olefins wherein at least one of A or A' is hydrogen.
• the olefins are contacted with a polymerization catalyst.
• the polymerization catalyst comprises a catalyst precursor that has been activated by an activator molecule.
• the catalyst precursor of the present invention comprises the product obtained by:
• R' is an alkyl group having
• the catalyst precursor 1 4 between 0 and 4, inclusive. 15 l fi
• the catalyst precursor 1 4 between 0 and 4, inclusive.
• the catalyst precursor is activated with an
• activator compound typically, the activator is an
• activator is an organoaluminum compound, more preferably an 26 alkylaluminum compound.
• activators include, but
• 29 activator compound may be used in neat form, or it may be
• a carrier If a carrier is employed, it may be
• the catalyst precursor may be activated prior to
• the catalyst precursor and activator compound may be added to the polymerization reactor separately.
• enough activator is present to make a prepolymer having a bulk density of about 0.28 - 0.32. This typically requires a mole ratio of activator metal to transition metal present in the catalyst of greater than about 0.5.
• the olefin polymerization catalyst is contacted with an olefin, under polymerization conditions, to produce a prepolymer.
• a sufficient amount of olefin is used such that the prepolymer obtained has a melt index in the range of about 0.1 to about 5.
• melt index refers to the unit of measure described in ASTM Procedure No. D-1238, which is incorporated by reference herein.
• the prepolymer is then used as a catalyst for the polymerization of the olefin. Polymerization is accomplished by adding more olefin to the prepolymer under polymerization conditions.
• the catalyst precursors of the present invention are prepared by adding a preformed magnesium source or compound to a solution containing transition metal compound(s) and an alkyl halide.
• the magnesium source can be represented by the formula MgR q X (2 . q) - R is an alkyl radical, preferably C 2 to C 8 , more preferably butyl; an alkenyl radical, preferably c 2 to C 8 , more preferably butenyl; and/or an aryl radical, preferably C 6 to C 12 , more preferably phenyl.
• the radicals are preferably nonfunctionalized.
• X is a halide, preferably chloride or bromide, and q is a number between 0 and 2, inclusive. Preferably, q is between 0.1 and 1.9, inclusive, and most preferably, q is about 1.
• the magnesium source may be added to the transition metal solution in solid powdered form or as a solid suspended in an organic liquid such as hexane or heptane.
• the preformed magnesium source is slowly added as a solid or slurry to a solution comprising a solvent having dissolved therein: (1) an alkyl halide; and (2) at least one transition metal compound represented by the formula M(OR') ⁇ X' (t . 6) or MO(OR') s X' (t . s) where M is at least one transition metal from Group IVB and Group VB of the Periodic Table of the Elements; R' is an alkyl group having from 1 to 8 carbon atoms, an alkenyl group having from 2 to 8 carbon atoms, or an aryl group having from 6 to 12 carbon atoms; X' is halide; t is 3 or 4; and s is an integer between 0 and 4, inclusive.
• the transition metal compound used is as described above, with the proviso that when q is 1 and when M comprises titanium, s is at least one and (t-s) is at least one.
• M is preferably vanadium, titanium, or a blend of vanadium and titanium.
• the vanadium compounds may be tetravalent or pentavalent.
• the vanadium compounds are preferably vanadium halides such as vanadium tetrabromide and, more preferably, vanadium tetrachloride.
• the vanadium compounds are also preferably vanadium oxyhalides, with vanadium oxytrichloride being preferred.
• vanadium tetraalkoxide compounds are preferred, including vanadium tetra-n- butoxide.
• the titanium compounds may contain trivalent or preferably tetravalent titanium, having the formula TiX' n or Ti(OR') m , wherein n and m each is 3 or 4, preferably 4, and X and R' are as defined above.
• the titanium compounds are preferably alkoxytitanium halides, such as titanium tri-n- propoxychloride.
• the titanium compounds are preferably alkoxytitanium halides as above, titanium halides, titanium alkoxides, or a mixture of these compounds.
• the preferred titanium halide is titanium tetrachloride
• the preferred titanium alkoxide is titanium tetraisopropoxide or titanium tetra-n-propoxide.
• the mole ratio of magnesium to transition metal should preferably be in the range of about 2:1 to about 10:1, and more preferably is about 4: 1 to about 5:1.
• the alkyl halide is defined by the formula R''X wherein R' ' is an alkyl radical, preferably C 2 to C 8 alkyl, more preferably butyl or propyl, and X is as defined above.
• transition metal compound(s) is dissolved in an appropriate amount of solvent together with an alkyl halide such that the molar ratios are:
• transition metal compound to alkyl halide is about 0.01:1 to about 0.20:1, preferably about 0.05:1 to about 0.10:1; and
• magnesium to alkyl halide is about 1:1, preferably about 0.8:1 to about 1:1.
• the amount of solvent to transition metal solution should be a volume ratio of about 20-50:1, preferably about 30-35:1.
• the solvent may be any liquid which dissolves the transition metal compound(s) and alkyl halide, and does not interfere with the reaction which produces the catalyst precursor.
• the solvent will typically be an organic solvent, preferably a hydrocarbon solvent. Examples of suitable solvents include, but are not limited to, C 5 to C 10 hydrocarbons. Hexane and heptane are preferred solvents.
• the catalyst precursors of this invention may be produced by reaction at a temperature of from about 60 * to about 90°C, preferably from about 75 * to about 85 * C.
• the liquid solution containing the transition metal compound(s) and alkyl halide is heated to about 80-85 * C.
• a preformed magnesium source is then added to the liquid solution by a controlled addition, i.e., the magnesium source is added to the transition metal solution slowly over time. Once all of the magnesium source has been added to the liquid solution, the resulting mixture is cooled to room temperature and filtered to recover the catalyst precursor in the form of a powder.
• the preformed magnesium source be slowly added to the solution of transition metal compound(s) and alkyl halide by a controlled addition over a relatively long period of time. While the period of time over which the magnesium source is added to the solution will depend on such factors as the size of the reaction mixture, typically that period of time will be about 1 to about 5 hours, preferably about 2 to about 4 hours. This manner and order of addition is necessary to allow small concentrations of preformed magnesium source to react with excess transition metal in the beginning of the reaction.
• a catalyst precursor which is synthesized by the reverse addition method of this invention will contain particles having a unique morphology, i.e., the catalyst precursor will contain hollow particles. These hollow particles are different from the solid, compact particles obtained by the normal addition process. This difference may be observed using a scanning electron microscope such as a JEOL JSM-820 instrument equipped with a Tracor Northern 5500 Energy dispersive X-ray detector.
• a catalyst or prepolymer which is synthesized by using precursors made by the reverse addition method of this invention will contain substantially less fines than prior-art catalysts or prepolymers made using the normal addition method.
• Prior-art normal addition titanium magnesium catalyst products and prepolymer products made using them have contained a significant amount of fine particles.
• Fine particles are particles of less than 20 microns in diameter for catalyst, less than 80 microns in diameter for prepolymer, and less than 180 microns in diameter for polymer.
• Catalyst particle sizes may be determined by using a Malvern 2600 Particle Size Analyzer or by standard sieving techniques, and prepolymer and polymer particle sizes can be determined by the method of ASTM procedure D1921, which is incorporated by reference in its entirety herein.
• Fine particles are especially disadvantageous in gas phase olefin polymerization reactions.
• the fine particles are easily carried beyond the disengaging zone of the reactor bed and into areas of the reactor where polymerization is not intended to occur.
• fine particles may electrostatically affix to metal surfaces such as the reactor wall, yielding growing sheets of active polymer which can break away from the wall and at least partially plug the gas inlet.
• the fine particles must be removed prior to polymerization. This is typically done via a catalyst elutriation procedure, like the one described in U.S. Patent No. 4,931,193, which is incorporated herein by reference. This procedure involves first having to prepare a homogeneous suspension of the particles in an elutriation liquid, then elutriating the catalyst by filtering the suspension through one or two elutriation columns.
• the present invention provides catalysts and prepolymers with fewer fine particles, the aforementioned elutriation procedure can be avoided. This simplifies the catalyst preparation by eliminating one preparative step while also significantly improving the catalyst yield.
• the catalyst precursor becomes the polymerization catalyst upon activation.
• the catalyst precursor is activated by contacting it with an activator compound such as an organoaluminum compound, as discussed above.
• Preferred activators are trialkylaluminum compounds, especially triethylaluminum, tributylaluminum and tri-n-octylaluminum.
• the aluminum to transition metal mole ratio is about 0.50:1 to about 2.0:1, preferably about 0.8:1 to about 1.2:1.
• the catalyst precursor is activated by the activator compound by methods conventional in the art.
• PREPOLYMERIZATION AND POLYMERIZATION Prepolymerization is generally carried out under a pressure of less than about 70 psi and at a temperature from about 40 * to about 150 * C. This operation may be performed by introducing the monomer(s) comprising, e.g., ethylene (and possibly other olefins) , into a liquid diluent such as a saturated aliphatic hydrocarbon or, in the absence of diluent, by direct contact between the monomer(s) in the gaseous condition and the constituents of the catalyst system.
• a liquid diluent such as a saturated aliphatic hydrocarbon or, in the absence of diluent
• Prepolymerization is carried out in the presence of a chain growth limiter, generally comprising hydrogen, whose proportion by volume with respect to the monomer(s) introduced into the polymerization medium is from about 1 to about 80%, so as to produce a polymer having the desired melt index.
• a chain growth limiter generally comprising hydrogen, whose proportion by volume with respect to the monomer(s) introduced into the polymerization medium is from about 1 to about 80%, so as to produce a polymer having the desired melt index.
• the catalyst may be introduced into the polymerization reactor directly or in the form of a prepolymer produced by preliminary polymerization of one or more olefins within an inert liquid such as an aliphatic hydrocarbon and in the presence of a catalyst of the present invention.
• the prepolymer contains about 1000 parts by weight of olefin per part by weight of transition metal. It may or may not be filtered prior to polymerization.
• the prepolymer has a melt index in the range of about 0.1 to about 5.
• the catalyst may be used in any polymerization method known in the art.
• the catalyst is particularly effective in the "low pressure" polymerization of olefins, although the catalyst may also be used in gas phase, in slurry phase, or in "high pressure” polymerization.
• the temperature in a "low pressure” polymerization is typically maintained between 40 and 150°C, and preferably is between 70 and 110°C.
• the pressure is typically maintained between 100 and 1000 psi, and preferably is between 250 and 500 psi. Hydrogen may be used to control the molecular weight of the polymer.
• EXAMPLE 2 Preparing a Vanadium Reverse Addition Catalyst Precursor
• a total of 300 mL heptane, 3.0 L (28 mmol) VC1 4 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85°C.
• Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85"C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 3 Preparing a Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 2.6 mL (28 mmol) V0C1 3 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85'C. Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85 "C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 4 Preparing a Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 9.6 g (28 mmol) V(0-CH 2 CH 2 CH 2 CH 3 ) 4 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85 * C. Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85 * C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 5 Preparing a Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 4.8 g (14 mmol) V(0-CH 2 CH 2 CH 2 CH 3 ) 4 , 2.7 g (14 mmol) VC1 4 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85 C.
• Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85"C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 6 Preparing a Titanium/Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 3.1 mL (28 mmol) TiCl 4 , 0.1 L (1 mmol) VC1 4 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85 * C. Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85 * C.
• a total of 300 mL heptane, 1.8 mL (16 mmol) TiCl 4 , 3.4 mL (12 mmol) Ti(0-CH 2 CH 2 CH 3 ) 4 , 0.3 mL (3 mmol) V0C1 3 , and 21 mL (201 mmol) n-butylchloride is added to a 1000 mL flask and heated to 85 * C.
• Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85 * C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85"C for an additional 0.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 9 Preparing a Titanium/Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 1.0 g (3 mmol) V(0-CH 2 CH 2 CH 2 CH 3 ) 4 , 8.5 g (25 mmol) Ti(0-CH 2 CH 2 CH 2 CH 3 ) 4 , and 21 mL (201 mmol) n- butylchloride is added to a 1000 mL flask and heated to 85 * C. Organomagnesium support precursor from Example 1 (15.7 g) is added via a powder addition funnel over 1.5 hours. The slurry is maintained at 85 * C for an additional o.5 hour, washed with 3 x 100 mL aliquots of heptane, and dried.
• EXAMPLE 10 Preparing a Titanium/Vanadium Reverse Addition Catalyst Precursor A total of 300 mL heptane, 2.6 mL (24 mmol) TiCl 4 , 0.2 mL (2 mmol) VC1 4 , 0.2 mL (2 mmol) V0C1 3 , and 21 mL (201 mmol) n- butylchloride is added to a 1000 mL flask and heated to
• EXAMPLE 11 Preparing Reverse Addition Catalyst Precursor
• This apparatus was charged with 200 mL heptane, 3.6 mL (12 mmol) titanium tetraisopropoxide, 1.8 mL (16 mmol) titanium tetrachloride, 21 mL (200 mmol) butylchloride, and a Teflon stir bar under argon.
• the mixture was heated to 85 * C and 15.7 g (134 mmol) butylmagnesium chloride was evenly added to the mixture via the powder addition funnel over 1.5 hrs.
• Figure 2 is a bar graph depiction of the percentage of fine particles of polyethylene produced using catalysts made from the magnesium powder catalyst precursor of Comparative Example A, the normal addition catalyst precursor of Comparative Example B, and the reverse addition catalyst precursor of Example 11 wherein the catalysts used were in raw form and in prepolymer form.
• a catalyst used in raw form is one which does not go through a prepolymerization stage.
• the graph shows that normal addition catalyst and reverse addition catalyst produce about the same percentage of fine particles in the raw form. However, when using the catalysts in prepolymer form, the reverse addition catalyst produces significantly less fine particles.
• the graph also shows that powdered magnesium catalysts have the lowest production of fine particles.
• Comparative Example A catalyst was elutriated to remove fine particles. The elutriation procedure is undesirable because it reduces catalyst yield and increases the equipment and time required to process the catalyst, thereby increasing operating costs.
• EXAMPLE 12 General Laboratory Procedure for Prepolymerization for Catalyst Precursor of Examples 2-11 and Comparative Examples A and B
• An 810 mL Fisher-Porter bottle is charged with 350 mg of the polymerization catalyst precursor, 50 mL heptane, alkylaluminum compound, and a Teflon stir bar.
• the bottle is connected to an ethylene cylinder, and the assembly is evacuated. Dihydrogen is added as required.
• the bottle is pressurized as required with ethylene and heated to 80"C. As ethylene is consumed, the pressure falls, and the bottle is repressurized to original pressure after the gauge pressure has fallen 10 psig. A total of 300 psi of ethylene is added in this way.
• Figure 1 shows the hydrogen response for the catalyst of this invention and comparative catalysts.
• the catalyst of the present invention gives higher melt index polymers at any given hydrogen concentration.
• the melt index is about 10 when the catalyst of this invention is used, while the melt index is only about 4 for the comparative example.
• the melt index is about 35 when the catalyst of this invention is used, compared to about 12 for the comparative catalyst.
• the catalyst of this invention has a surprisingly high hydrogen response, that is, relatively small amounts of hydrogen can be used to alter the polymer molecular weight.
• This high hydrogen response is advantageous, as it is often desirable to adjust polymer molecular weight during a polymerization run depending on the melt index of the polyolefin product desired and its planned applications or uses.
• the high hydrogen response of the catalyst of this invention also means that less hydrogen is used. As it is difficult to remove catalyst poisons from hydrogen, less hydrogen means fewer introduced catalyst poisons. Also, there are operating pressure limits on most ethylene polymerization vessels; these limit the amount of hydrogen that can be added. Moreover, added hydrogen generally displaces ethylene in the polymerization vessel and, thus, decreases the ethylene concentration in the vessel. This can impact the reaction kinetics.
• EXAMPLE 14 Preparation of Magnesium Chloride Precursor io g of finely divided Mg powder (411 mmol) was added to a 1000 mL flask equipped with a condenser. After 3 evacuation/argon refill cycles, 350 mL heptane, 0.1 g (0.4 mmol) iodine and 50 ml (479 mmol) n-butylchloride were added and heated to reflux for 4 hours. The product was washed with 3 X 100 mL aliquots heptane and dried in vacuo , yielding a gray/white powder. The total yield was 39 g with an elemental composition of 24.5% Mg, 47.3% Cl, 18.2% C and 3.4% H.
• EXAMPLE 15 Preparing a Ti Reverse Addition Catalyst Precursor A 1000 mL flask was charged with 300 mL dry heptane, 3.4 mL (12 mmol) Ti(0-n-CH 2 CH 2 CH 3 ) 4 , 1.8 mL (16 mmol) TiCl 4 , and 21 mL (201 mmol) n-butylchloride and heated to 85°C. A total of 15.7 g of dry product from Ex. 14 was then added over 2 hours via a powder addition funnel, followed by an additional hour of heating. The resulting brown slurry was washed with 3 X 100 mL heptane and dried in vacuo, yielding 21.8 g of product. The resulting elemental analysis showed 17.2% Mg and 7.0% Ti.
• EXAMPLE 16 Preparing a Vanadium Reverse Addition Catalyst Precursor 300 mL dry heptane, 2.6 mL (28 mmol) VOCl 3 , and 17.4 mL (167 mmol) n-butylchloride were added to a 1000 mL flask under argon and heated to 85°C. A total of 13 g of dry product from Ex. 14 was then added over 2 hours via a powder addition funnel, followed by an additional hour of heating. The resulting brown slurry was washed with 3 X 100 mL heptane and dried in vacuo , yielding 15.59 g of product. The resulting elemental analysis showed 15.4% Mg and 6.2% V.
• EXAMPLE 17 Preparing a Vanadium and Titanium Reverse Addition Catalyst Precursor 300 mL dry heptane, 1.3 mL (13.8 mmol) V0C1 3 , 1.5 mL (13.6 mmol) TiCl 4 , and 21 mL (201 mmol) n-butylchloride were added to a 1000 L flask under argon and heated to 85°C. A total of 15.7 g of dry product from Ex. 14 was then added over 2 hours via a powder addition funnel, followed by an additional hour of heating. The resulting slurry was washed with 3 X 100 L heptane and dried in vacuo, yielding 15.59 g of product. The resulting elemental analysis showed 13.2% Mg, 3.7% V, and 2.6% Ti.
• a catalyst was prepared essentially by the method of U.S. Pat. No. 3,878,124 Ex. 4 (Durand et al.). Over the course of two hours, a 15.7 g aliquot of magnesium chloride precursor prepared in Example 14 above was stirred into a 01 solution of 300 L heptane, 27 mmol (3 mL) TiCl 4 and 201
• the amount 34 of l-hexene comonomer listed in Table II was also added to the funnel.
• the funnel was emptied into an evacuated 2 L Autoclave Engineers reactor maintained at a temperature of 80°C, and the stirrer was turned on.
• Argon was added to a pressure of about 125 psig, and hydrogen was added to a pressure of 150 psig.
• Ethylene was added until the pressure in the reactor was 300 psi and was allowed to polymerize for i hour. Polymer properties are summarized in Table II.
• the reverse addition catalyst of Example 15 surprisingly incorporated more comonomer than the catalyst of Comparative Example C.
• prior art catalyst produced a copolymer having only about 26-27 short-chain side-branches per 1000 carbon atoms, as measured by NMR.
• Reverse addition catalyst produced a copolymer having about 42-45 short-chain side-branches per 1000 carbon atoms, a substantial increase in the number of side-branches present in the copolymer.
• Catalyst precursor of Comparative Ex. C exhibited a wide range of sizes and shapes, with the precursor appearing to be relatively amorphous honeycombed particles.
• Catalyst precursor of Example 11 clearly differed in morphology, having a relatively narrow particle- size distribution of well-defined hollow spherical particles having a diameter of approximately 50-80 microns.
• Prepolymer produced from these well-defined hollow spheres exhibited excellent bulk density (0.28 - 0.32), and the resulting polymer has been observed to be filled (i.e. not hollow) spheres, suggesting that polymerization occurred on both the inner and outer surfaces of the catalyst particles.
• EXAMPLE 20 Preparing Magnesium Chloride Precursor A 50 gallon reactor was charged with 10 gallons of hexane, 333 g (13.7 mol) finely divided Mg powder, and 10 g (39 mmol) iodine. After heating to 70°C, n-butylchloride was added to the reactor at a rate of 29 mL/min. for 57 minutes, totalling 1.7 L (16 mol) n-butylchloride. After maintaining the reactor at 70°C for 4 hours, the product was cooled to ambient temperature and isolated as a hexane slurry. Dried product had 17.2% Mg, 41.4% Cl, 23.8% C and 4.6% H.
• EXAMPLE 21 Preparing a Ti Reverse Addition Catalyst Precursor
• a 250 gallon reactor under N 2 blanket was charged with 30 gallons hexane, 370 L (1.35 mol) Ti(0-n-C 3 H 7 ) 4 , 150 mL (1.37 mol) TiCl 4 , and 1575 mL (15 mol) n-butylchloride.
• This mixture was heated to 85°C, and the slurry of Example 20 was added slowly over a 1 hour time period. A total of 60 additional gallons of hexane were added. The resulting brown slurry was stirred at 85°C for an additional 2 hours, after which time stirring ceased and the product was allowed to settle.
• Example 21 Little settling of catalyst was observed after
• Catalyst precursor losses for Example 21 and Comparative Example D were measured by mass balance by subtracting the mass of transition metal present in the recovered prepolymer from the amount of transition metal originally introduced into the reactor, then dividing this number by the amount of transition metal originally introduced into the reactor.
• COMPARATIVE EXAMPLE E Catalyst was prepared substantially by the method of Comparative Ex. A, substituting titanium tetra-n-propoxide for titanium tetraisopropoxide, and prepolymer was produced in hexane in a 250 gallon reactor at 74°C by reacting about 210 lb. ethylene, about 0.14 lb. hydrogen, and the catalyst of Comparative Ex. B in the presence of enough TNOA to give a molar ratio of about 0.8:1 Al/Ti. The resultant prepolymer was filtered from the slurry, dried with hot nitrogen, and was fed to a gas-phase polymerization reactor substantially like the one disclosed in U.S. Pat. No.
• Example 22 Catalyst of Example 15 was prepolymerized and fed to the gas-phase reactor by the method of Comparative Example E.
• Table III shows the density of the copolymer as a function of the amount of comonomer fed to the reactor.
• Table III shows that reverse addition catalyst of this invention incorporated comonomer into the ethylene copolymer more effectively than prior-art catalyst could.
• Reverse addition catalyst of this invention differs in many regards from prior-art catalysts.
• Reverse addition synthesis provides catalyst precursor that is hollow and spherically-shaped, with few catalyst precursor fines being produced.
• Reverse addition catalyst produces prepolymer having less fines than normal addition catalyst produces.
• Reverse addition catalyst exhibits higher hydrogen response than normal addition catalyst, and reverse addition catalyst incorporates more comonomer into copolymer than normal addition catalyst.

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• 1995
  • 1995-03-09 AU AU21189/95A patent/AU2118995A/en not_active Abandoned
  • 1995-03-09 EP EP95914019A patent/EP0745098A1/de not_active Withdrawn
  • 1995-03-09 WO PCT/US1995/003122 patent/WO1995024432A1/en not_active Application Discontinuation

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