Homogeneous ethylene polymers having a density less than 0.910 g/cm3, particularly less than 0.900 g/cm3, preferably less than 0.890 g/cm3, and most preferably less than 0.880 g/cm3, have good elongation properties, that is, such as a high elongation at break and the ability to withstand high degrees of stress before breaking, with the degree of elongation properties increasing as the density of the polymer decreases. However, homogeneous ethylene polymers having such elongation properties lack a highly crystalline fraction that imparts increased upper use temperature and favorably high onset of crystallization temperatures.

To compensate for the poor upper use temperature and low onset of crystallization temperature characteristic of homogeneous ethylene polymers having a density less than 0.910 g/cm3, it may be desirable to blend therewith a higher crystallinity material, such as a higher density homogeneous ethylene polymer or a traditional wax. However, while the addition of such a higher crystallinity material may increase the upper use temperature and provide a higher onset of crystallization temperature, it causes a highly deleterious loss of elongation properties.

Those in industry would find great advantage in polymer compositions which have favorable upper use temperatures and high onset of crystallization temperatures, but which retain favorable elongation at break and the ability to withstand high degrees of stress before breaking which is characteristic of homogeneous ethylene polymers having a density less than 0.910 g/cm3.

Hot melt adhesives comprising homogeneous linear or substantially linear ethylene polymers are further known. See, for instance, WO 97/33921, WO 92/12212,. and WO 94/10256. While such hot melt adhesive formulations exhibit many commercially attractive attributes, it would be desirable for certain formulations to improve the elongation at break of these compositions. Those in industry would further find great advantage in hot melt adhesive formulations for use in formulations which require a high elongation at break, without incurring a detrimental effect on yield or break stress, such as, for instance, in bookbinding adhesives.

Accordingly, the subject invention provides a polymer composition comprising: (a) a homogeneous ethylene/a-olefin interpolymer; (b) a wax; and (c) a nucleating agent, wherein the nucleating agent is provided in an effective amount such that the percent elongation at break of the polymer composition is at least fifty percent greater than the percent elongation at break of a comparative composition which lacks the nucleating agent.

In preferred embodiments, the homogeneous ethylene/a-olefin interpolymer will be a homogeneous linear or substantially linear ethylene/a-olefin interpolymer, which in turn preferably has a density less than 0.910 g/cm3, more preferably less than 0.900 g/cm3, even more preferably less than 0.890 g/cm3, and most preferably less than 0.880 g/cm3.

In preferred embodiments, the wax will be a paraffin wax, microcrystalline wax, Fischer-Tropsch wax, polyethylene or polyethylene by-product wax, or homogenous wax, which is preferably characterized as having a Mw of no more than 3000, and which has a density greater than that of the homogeneous ethylene polymer of component (a).

In preferred embodiments, the nucleating agent will be provided in an amount of at least 0.01 weight percent, more preferably at least 0.05 weight percent, even more preferably at least 0.1 weight percent, and most preferably at least 0.2 weight percent; preferably no more than 10 weight percent, more preferably no more than 5 weight percent, even more preferably no more than 1 weight percent, and most preferably less than 0.5 weight percent.

Preferred polymer compositions of the invention will exhibit a percent elongation at break which is at least four times greater than the percent elongation at break of a comparative composition which lacks the nucleating agent.

The subject invention further provides a hot melt adhesive composition comprising: (a) an olefin polymer; (b) a nucleating agent; and (c) optionally, one or more of a tackifier, plasticizer or wax.

These and other embodiments are more fully described in the following detailed description, wherein: FIGURE 1 is a bar chart representation of the elongation properties of polymer compositions of the invention and comparative compositions lacking a nucleating agent The polymer compositions of the invention comprise at least one homogeneous ethylenela-olefin interpolymer which is an interpolymer of ethylene and at least one C3-C20 a-olefin. The term "interpolymer" is used herein to indicate a copolymer, or a terpolymer, or a higher order polymer. That is, at least one other comonomer is polymerized with ethylene to make the interpolymer.

The homogeneous ethylenela-olefin interpolymer is a homogeneous linear or substantially linear ethylene/a-olefin interpolymer. By the term "homogenous", it is meant that any comonomer is randomly distributed within a given interpolymer molecule and substantially all of the interpolymer molecules have the same ethylene/comonomer ratio within that interpolymer. The melting peak of homogeneous linear and substantially linear ethylene polymers, as obtained using differential scanning calorimetry, will broaden as the density decreases and/or as the number average molecular weight decreases. However, unlike heterogeneous polymers, when a homogeneous polymer has a melting peak greater than 115"C (such as is the case of polymers having a density greater than 0.940 g/cm3), it does not additionally have a distinct lower temperature melting peak.

In addition or in the alternative, the homogeneity of the polymer may be described by the SCBDI (Short Chain Branching Distribution Index) or CDBI (Composition Distribution Breadth Index), which are defined as the weight percent of the polymer molecules having a conomomer content within 50 percent of the median total molar comonomer content. The SCBDI of a polymer is readily calculated from data obtained from techniques known in the art, such as, for example, temperature rising elution fractionation (abbreviated herein as "TREF"), which is described, for example, in Wild et al., Journal of Polymer Science, Poly. Phys. Ed., Vol. 20, p. 441 (1982), in U.S. Patent 4,798,081 (Hazlitt et al.), or in U.S. Patent 5,089,321 (Chum et al.). The SCBDI or CDBI for the homogeneous ethylene/a-olefin interpolymers useful in the invention is preferably greater than 50 percent, more preferably greater than 70 percent, with SCBDI's and CDBI of greater than 90 percent being easily attained.

The homogeneous ethylene/a-olefin interpolymers useful in the invention are characterized as having a narrow molecular weight distribution (Mw/Mn). For the homogeneous ethylene/a-olefins useful in the polymer compositions of the invention, the MW/Mn is from 1.5 to 2.5, preferably from 1.8 to 2.2, most preferably 2.0.

Substantially linear ethylene interpolymers are homogeneous interpolymers having long chain branching. Due to the presence of such long chain branching, substantially linear ethylene interpolymers are further characterized as having a melt flow ratio (I 10/I2) which may be varied independently of the polydispersity index, that is, the molecular weight distribution MW/Mn. This feature accords substantially linear ethylene polymers with a high degree of processability despite a narrow molecular weight distribution.

It is noted that substantially linear interpolymers useful in the invention differ from low density polyethylene prepared in a high pressure process. In one regard, whereas low density polyethylene is an ethylene homopolymer having a density of from 0.900 to 0.935 g/cm3, the homogeneous linear and substantially linear interpolymers useful in the invention require the presence of a comonomer to reduce the density to the range of from 0.900 to 0.935 g/cm3.

The long chain branches of substantially linear ethylene interpolymers have the same comonomer distribution as the interpolymer backbone and can be as long as the same length as the length of the interpolymer backbone. When a substantially linear ethylene/a-olefin interpolymer is employed in the practice of the invention, such interpolymer will be characterized as having an interpolymer backbone substituted with from 0.01 to 3 long chain branches per 1000 carbons.

Methods for determining the amount of long chain branching present, both qualitatively and quantitatively, are known in the art.

For qualitative methods for determining the presence of long chain branching, see, for example, U.S. Patent Nos. 5,272,236 and 5,278,272. As set forth therein, a gas extrusion rheometer (GER) may be used to determine the rheological processing index (PI), the critical shear rate at the onset of surface melt fracture, and the critical shear stress at the onset of gross melt fracture, which in turn indicate the presence or absence of long chain branching as set forth below,

The gas extrusion rheometer useful in the determination of rheological processing index (PI), the critical shear rate at the onset of surface melt fracture, and the critical shear stress at the onset of gross melt fracture, is described by M. Shida, R. N. Shroff, and L. V. Cancio in Polymer Engineering Science, Vol. 17, No. 11, p. 770 (1977), and in "Rheometers for Molten Plastics" by John Dealy, published by Van Nostrand Reinhold co. (1982) on pp. 97-99. GER experiments are performed at a temperature of 1900C, at nitrogen pressures between 250 and 5500 psig (between 1.72 and 37.9 MPa) using a 0.0754 mm diameter, 20:1 L/D die with an entrance angle of 180 degrees.

For substantially linear ethylene interpolymers, the PI is the apparent viscosity (in kpoise) of a material measured by GER at an apparent shear stress of2.15 x 106 dynes/cm2 (0.215 MPa). Substantially linear ethylene interpolymers useful in the invention will have a PI in the range of 0.01 kpoise to 50 kpoise, preferably 15 kpoise or less. Substantially linear ethylene interpolymers have aPI which is less than or equal to 70 percent of the PI of a linear ethylene interpolymer (either a Ziegler polymerized polymer or a homogeneous linear ethylene interpolymer) having the same comonomer or comonomers, and having an I2, MW/Mn, and density, each of which is within 10 percent of that of the substantially linear ethylene interpolymer.

An apparent shear stress versus apparent shear rate plot may be used to identify the melt fracture phenomena and to quantify the critical shear rate and critical shear stress of ethylene polymers. According to Ramamurthy, in the Journal of Rheology, 30(2), 1986, pp. 337-357, above a certain critical flow rate, the observed extrudate irregularities may be broadly classified into two main types: surface melt fracture and gross melt fracture.

Surface melt fracture occurs under apparently steady flow conditions and ranges in detail from loss of specular film gloss to the more severe form of "sharkskin." Herein, as determined using the above- described gas extrusion rheometer, the onset of surface melt fracture is characterized as the beginning of losing extrudate gloss at which the surface roughness of the extrudate can only be detected by magnification at 40 times. The critical shear rate at the onset of surface melt fracture for a substantially linear ethylene interpolymer is at least 50 percent greater than the critical shear rate at the onset of surface melt fracture for a linear ethylene polymer having the same comonomer or comonomers and having an I2, MW/Mn and density within ten percent of that of the substantially linear ethylene polymer.

Gross melt fracture occurs at unsteady extrusion flow conditions and ranges from regular (alternating rough and smooth, helical, etc.) to random distortions. The critical shear stress at the onset of gross melt fracture of substantially linear ethylene interpolymers, especially those having a density greater than 0.910 g/cm3, is greater than 4 x 106 dynes/cm2 (0.4 MPa)..

The presence of long chain branching may further be qualitatively determined by the Dow Rheology Index (DRI), which expresses a polymer's "normalized relaxation time as the result of long chain branching." (See, S. Lai and G. W. Knight, ANTEC '93 Proceedings, INSITETM Technology Polyolefins (SLEP)- New Rules in the Structure/Rheology Relationship of Ethylene a-Olefin Copolymers, New Orleans, La., May 1993. DRI values range from 0 for polymers which do not have any measurable long chain branching, such as TafmerTM products available from Mitsui Petrochemical Industries and ExactTM

products available from Exxon Chemical company) to 15, and are independent of melt index. In general, for low to medium pressure ethylene polymers, particular at lower densities, DRI provides improved correlations to melt elasticity and high shear flowability relative to correlations of the same attempted with melt flow ratios. Substantially linear ethylene interpolymers will have a DRI of preferably at least 0.1, more preferably at least 0.5, and most preferably at least 0.8.

DRI may be calculated from the equation: DRI = (3.652879 * Tol 00649/o~l)/1° where To is the characteristic relaxation time of the interpolymer and nO is the zero shear viscosity of the interpolymer. Both To and nO are the "best fit" values to the Cross equation, that is, #/#0= = 1/(1 + (r * To)l-n) in which n is the power law index of the material, and n andy are the measured viscosity and shear rate, respectively. Baseline determination of viscosity and shear rate data are obtained using a Rheometric Mechanical Spectrometer (RMS-800) under dynamic sweep mode from 0.1 to 100 radians/second at 1600C and a gas extrusion rheometer (GER) at extrusion pressures from 1,000 to 5,000 psi (6.89 to 34.5 MPa), which corresponds a shear stress of from 0.086 to 0.43 MPa, using a 0.0754 mm diameter, 20:1 L/D die at 190°C. Specific material determinations may be performed from 140 to 1900C as required to accommodate melt index variations.

For quantitative methods for determining the presence of long chain branching, see, for example, U.S. Patent Nos. 5,272,236 and 5,278,272; Randall (Rev. Macromol. Chem. Phys., C29 (2&3), p. 285-297), which discusses the measurement of long chain branching using 13C nuclear magnetic resonance spectroscopy, Zimm, G.H. and Stockmayer, W.H., J. Chem. Phys., 17, 1301 (1949); and Rudin, A., Modern Methods of Polymer Characterization, John Wiley & Sons, New York (1991) pp. 103-112, which discuss the use of gel permeation chromatography coupled with a low angle laser light scattering detector (GPC- LALLS) and gel permeation chromatography coupled with a differential viscometer detector (GPC-DV).

A. Willem deGroot and P. Steve Chum, both of The Dow Chemical Company, at the October 4, 1994 conference of the Federation of Analytical Chemistry and Spectroscopy Society (FACSS) in St. Louis, Missouri, presented data demonstrating that GPC-DV is a useful technique for quantifying the presence of long chain branches in substantially linear ethylene polymers. In particular, deGroot and Chum found that the presence of long chain branches in substantially linear ethylene polymers correlated well with the level of long chain branches measured using 13C NMR.

Further, deGroot and Chum found that the presence of octene does not change the hydrodynamic volume of the polyethylene samples in solution and, as such, one can account for the molecular weight increase attributable to octene short chain branches by knowing the mole percent octene in the sample. By deconvoluting the contribution to molecular weight increase attributable to 1 -octene short chain branches, deGroot and Chum showed that GPC-DV may be used to quantify the level of long chain branches in substantially linear ethylene/octene copolymers.

deGroot and Chum also showed that a plot of log(I2, melt index) as a function of log(GPC weight average molecular weight), as determined by GPC-DV, illustrates that the long chain branching aspects (but not the extent of long chain branching) of substantially linear ethylene polymers are comparable to those of high pressure, highly branched low density polyethylene (LDPE) and are clearly distinct from heterogeneously branched ethylene polymers produced using Ziegler-type catalysts (such as linear low density polyethylene and ultra low density polyethylene) as well as from homogeneous linear ethylene polymers (such as TafmerTM products available from Mitsui Petrochemical Industries and ExactTM products available from Exxon Chemical Company).

The first polymer will be an interpolymer of ethylene with at least one comonomer selected from the group consisting of C3-C20 a-olefins, non-conjugated dienes, and cycloalkenes. Exemplary C3-C20 a- olefins include propylene, isobutylene, I-butene, 1 -hexene, 4-methyl-1-pentene, 1 -heptene, and 1-octene.

Preferred C3-C20 a-olefrns include 1-butene, 1-hexene, 4-methyl-l-pentene, 1-heptene, and 1-octene, more preferably 1 -hexene and l-octene. Exemplary cycloalkenes include cyclopentene, cyclohexene, and cyclooctene. The non-conjugated dienes suitable as comonomers, particularly in the making of ethylene/a- olefin/diene terpolymers, are typically non-conjugated dienes having from 6 to 15 carbon atoms.

Representative examples of suitable non-conjugated dienes include: (a) Straight chain acyclic dienes such as 1,4-hexadiene; 1,5-heptadiene; and 1,6-octadiene; (b) Branched chain acyclic dienes such as 5-methyl-l,4-hexadiene; 3,7-dimethyl-1,6- octadiene; and 3,7-dimethyl- I ,7-octadiene; (c) Single ring alicyclic dienes such as 4-vinylcyclohexene; 1-allyl-4-isopropylidene cyclohexane; 3-allylcyclopentene; 4-allylcyclohexene; and 1-isopropenyl-4- butenylcyclohexene; (d) Multi-ring alicyclic fused and bridged ring dienes such as dicyclopentadiene; alkenyl, alkylidene, cycloalkenyl, and cycloalkylidene norbornenes, such as 5-methylene-2- norbornene; 5-methylene-6-methyl-2-norbornene; 5-methylene-6,6-dimethyl-2- norbornene; 5-propenyl-2-norbornene; 5-(3-cyclopentenyl)-2-norbornene; 5-ethylidene-2- norbornene; and 5-cyclohexylidene-2-norbornene.

One preferred conjugated diene is piperylene. The preferred dienes are selected from the group consisting of 1,4-hexadiene; dicyclopentadiene; 5 -ethylidene-2-norbornene; 5 -methylene-2-norbornene; 7- methyl-1,6 octadiene; piperylene; and 4-vinylcyclohexene.

The homogeneous ethylene polymer useful as component (a) of the polymer composition of the invention may further be an ultra-low molecular weight ethylene polymer.

Ultra-low molecular weight polymers may be made in accordance with the Examples herein and with the procedures set forth below. Ultra-low molecular weight polymers are disclosed and claimed in WO 97/26287.

The homogeneous ethylene polymer may be suitably prepared using a single site metallocene or a constrained geometry metal complex. Constrained geometry metal complexes are disclosed in U.S.

Application Serial No. 545,403, filed July 3, 1990 (EP-A-416,815); U.S. Application Serial No. 702,475, filed May 20, 1991 (EP-A-514,828); as well as US-A-5,470,993, 5,374,696, 5,231,106, 5,055,438, 5,057,475, 5,096,867, 5,064,802, and 5,132,380. In U.S. Serial Number 720,041, filed June 24, 1991, (EP- A-5 14,828) certain borane derivatives of the foregoing constrained geometry catalysts are disclosed and a method for their preparation taught and claimed. In US-A 5,453,410 combinations of cationic constrained geometry catalysts with an alumoxane were disclosed as suitable olefin polymerization catalysts.

Exemplary constrained geometry metal complexes in which titanium is present in the +4 oxidation <BR> <BR> 5<BR> state include but are not limited to the following: (n-butylamido)dimethyl(#@- tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (n-butylamido)dimethyl(#5- <BR> <BR> 5<BR> tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (t-butylamido)dimethyl(ll5- <BR> <BR> 5<BR> tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (t-butylamido)dimethyl(ll5- tetramethylcyclopentadienyl)silane-titanium (IV) dibenzyl; (cyclododecylamido)dimethyl(#5- tetramethylcyclo-pentadienyl)silanetitanium (IV) dibenzyl; (2,4,6-trimethylanilido)dimethyl-(# 5tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (1-adamantyl-amido)dimethyl(#- tetramethylcyclopentadienyl) silanetitanium (IV) dibenzyl; (t-butylamido)dimethyl(#5- tetramethylcyclopentadienyl) silanetitanium (IV) dimethyl; (t-butylamido)dimethyl(#5- tetramethylcyclopentadienyl) silanetitanium (IV) dibenzyl; (1-adamantylamido)dimethyl(#5- tetramethylcyclo-pentadienyl)silanetitanium (IV) dimethyl; (n-butylamido)diisopropoxy(#5-tetramethyl- cyclopentadienyl)silanetitanium (IV) dimethyl; (n-butylamido)diisopropoxy(#5- <BR> <BR> 5<BR> tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (cyclododecylamido)-diisopropoxy(#@- tetramethylcyclopentadienyl)-silanetitanium (IV) dimethyl; (cyclododecylamido)diisopropoxy(#5- tetramethylcyclopentadienyl)-silanetitanium (IV) dibenzyl; (2,4,6-trimethylanilido)diisopropoxy(#5- <BR> <BR> 5<BR> tetramethylcyclopentadienyl)-silanetitanium (IV) dimethyl; (2,4,6-trimethylanilido)diisopropoxy(rl tetramethyl-cyclopentadienyl)silanetitanium (IV) dibenzyl; (cyclododecylamide)dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (cyclododecylamido)-dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (1-adamantylamido)diisopropoxy(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (1-adamantylamido)diisopropoxy(#5- <BR> <BR> 5<BR> tetramethylcyclopentadienyl)-silanetitanium (IV) dibenzyl; (n-butylamido)dimethoxy(#@-tetramethylcyclo- pentadienyl)silanetitanium (IV) dimethyl; (n-butylamido)dimethoxy-(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (2,4,6-trimethylanilido) dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (2,4,6-trimethylanilido)dimethoxy(#5- tetramethylcyclopentadienyl)silane-titanium (IV) dibenzyl; (1-adamantylamido)dimethoxy(#5- tetramethylcyclo-pentadienyl)silanetitanium (IV) dimethyl; (1-adamantylamido)dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dibenzyl; (n-butylamido)-ethoxymethyl(#5- tetramethylcyclopentadienyl silanetitanium (IV) dimethyl; (n-butylamido)ethoxymethyl(#5-

tetramethylcyclopenta-dienyl)silanetitanium (IV) dibenzyl; (cyclododecylamido)ethoxymethyl(#5- <BR> <BR> 5 <BR> tetramethylcyclopentadienyl)-silanetitanium (IV) dimethyl; (cyclododecylamido) ethoxymethyl(#@- tetramethyl-cyclopentadienyl)silanetitanium (IV) dibenzyl; (2,4,6-trimethylanilido)ethoxymethyl-(#5- tetramethylcyclopentadienyl)silanetitanium (IV) dimethyl; (2,4,6-trimethylanilido)ethoxymethyl(#5- tetramethylcyclopentadienyl) silanetitanium (IV) dibenzyl; (cyclododecylamido)dimethyl(#5- <BR> <BR> 5<BR> tetramethylcyclopenta-dienyl)silane-titanium (IV) dimethyl; (1 -adamantylamido)-ethoxym ethyl(ll- tetramethylcyclo-pentadienyl)silanetitanium (IV) dimethyl; and (1-adamantylamido) ethoxymethyl(#5- tetramethylcyclo-pentadienyl)silanetitanium (IV) dibenzyl.

Exemplary constrained geometry metal complexes in which titanium is present in the +3 oxidation state include but are not limited to the following: (n-butylamido)dimethyl(#5- tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (t-butylamido)dimethyl( 5-tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (cyclododecylamido)dimethyl(#5-tetramethylcyclopentadienyl) silanetitanium (III) 2-(N,N- dimethylamino)benzyl; (2,4,6-trimethylanilido)dimethyl(#5-tetramethylcyclopentadie nyl)silanetitanium <BR> <BR> 5<BR> (III) 2-(N,N-dimethylamino)benzyl; (1 -adamantylamido)dimethyl(rl - tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (t-butylamido)dimethyl( 5<BR> -tetramethylcyclopentadienyl) silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (n-<BR> <BR> 5<BR> butylamido)diisopropoxy(#@-tetramethylcyclopentadienyl)silan etitanium (III) 2-(N,N- dimethylamino)benzyl; (cyclododecylamido)diisopropoxy(#5-tetramethylcyclopentadien yl)-silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (2,4,6-trimethylanilido)diisopropoxy(#5-2-methylindenyl) silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (1-adamantylamido)diisopropoxy(#@- tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (n-butylamido)dimethoxy( 1 -tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; 5<BR> (cye lododecylamido)dim ethoxy(ll -tetramethylcyclopentadienyl silanetitanium (III) 2-(N,N-<BR> <BR> 5<BR> dimethylamino)benzyl; (l-adamantylamido)dimethoxy(r) -tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (2,4,6-trimethylanilido)dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (n- butylamido)ethoxymethyl(#5-tetramethylcyclopentadienyl) silanetitanium (III) 2-(N,N- dimethylamino)benzyl; (cyclododecylamido)ethoxymethyl(#5-tetramethylcyclopentadien yl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; (2,4,6-trimethylanilido)ethoxymethyl(#5- tetramethylcyclopentadienyl)silanetitanium (III) 2-(N,N-dimethylamino)benzyl; and (1 - adamantylamido)ethoxymethyl(ll -tetramethyl-cyclopentadienyl)silanetitanium (III) 2-(N,N- dimethylamino)benzyl.

Exemplary constrained geometry metal complexes in which titanium is present in the +2 oxidation state include but are not limited to the following: (n-butylamido)-dimethyl-(#5- tetramethylcyclopentadienyl)silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (n-butylamido)dimethyl(#5-

tetramethylcyclopentadienyl)silanetitanium (II) 1,3-pentadiene; (t-butylamido)dimethyl(#5- tetramethylcyclopentadienyl)silane-titanium (II) 1,4-diphenyl-1,3-butadiene; (t-butylamido)dimethyl(#5- tetramethyl-cyclopentadienyl) silanetitanium (II) 1,3-pentadiene; (cyclododecylamido)dimethyl-(#5- tetramethylcyclo-pentadienyl)silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (cyclododecylamido)dimethyl( <BR> <BR> <BR> #5-tetramethylcyclopentadienyl)silanetitanium (II) 1,3-pentadiene; (2,4,6-trimethyl-anilido)dimethyl(#5- tetramethylcyclopentadienyl)-silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (2,4,6- trimethylanilido)dimethyl(#5-tetramethylcyclopentadienyl)sil anetitanium (II) 1,3-pentadiene; (2,4,6- trimethylanilido)dimethyl(#5-tetramethylcyclopentadienyl) silanetitanium (IV) dimethyl; (1- 5<BR> adamantylamido)dimethyl(rl -tetramethylcyclopenta-dienyl)silane-titanium (II) 4-diphenyl- 1,3- butadiene; (1-adamantylamido)dimethyl(#5-tetramethylcyclopentadienyl)si lanetitanium (II) 1,3-pentadiene; (t-butylamido)-dimethyl(#5-tetramethylcyclopentadienyl)silan etitanium (II) 1,4-diphenyl-1,3-butadiene; (t- butyl-amido)dimethyl(#5-tetramethylcyclopentadienyl)silaneti tanium (II) 1,3-pentadiene;; (n- butylamido)diisopropoxy(#5-tetramethylcyclopentadienyl)-sila netitanium (II) 1,4-diphenyl-1,3-butadiene; 5<BR> (n-butylamido)diisopropoxy(#@-tetramethylcyclopentadienyl) silanetitanium (II) 1,3-pentadiene; (cyclododecylamido)-diisopropoxy(#5-tetramethyl-cyclopentadi enyl)silanetitanium (II) 1,4-diphenyl-1,3- butadiene; (cyclododecylamido) diisopropoxy(ll -tetramethylcyclopentadienyl)-silanetitanium (11)1,3- pentadiene; (2,4,6-trimethylanilido)diisopropoxy(#5-2-methyl-indenyl)sil anetitanium (II) 1,4-diphenyl-1,3- butadiene; (2,4,6-trimethylanilido)-diisopropoxy(#5-tetramethylcyclopen tadienyl) silanetitanium (II) 1,3- pentadiene; (1-adamantylamido)diisopropoxy(# -tetramethyl-cyclopentadienyl)silanetitanium (II)1,4- diphenyl-1,3-butadiene; (1-adamantylamido) diisopropoxy(#5-tetramethyl-cyclopentadienyl)silanetitanium 5<BR> (II) 1,3-pentadiene; (n-butylamido)dimethoxy( -tetramethylcyclopentadienyl)silanetitanium (11)1,4- <BR> <BR> 5<BR> diphenyl-1,3-butadiene; (n-butylamido)dimethoxy( -tetramethylcyclopentadienyl)silanetitanium (11)13 - <BR> <BR> 5<BR> pentadiene; (cyclododecylamido)dimethoxy(ll5-tetramethylcyclopentadienyl )-silanetitanium (II) 1,4- diphenyl-1,3-butadiene; (cyclododecylamido)dimethoxy(#5-tetramethylcyclopentadienyl) silanetitanium (II) 1,3-pentadiene; (2,4,6-trimethylanilido) dimethoxy(#5-tetramethylcyclopentadienyl)silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (2,4,6-trimethylanilido)dimethoxy(#5- tetramethylcyclopentadienyl)silanetitanium (II) 1,3-pentadiene; (1-adamantyl-amido)dimethoxy(#5- tetramethylcyclopentadienyl) silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (1- adamantylamido)dimethoxy(#5-tetramethylcyclopentadienyl)-sil anetitanium (II) 1,3-pentadiene; (n- butylamido) ethoxymethyl(#5-tetramethylcyclopentadienyl)silanetitanium (II) 1,4-diphenyl-1,3-butadiene; (n-butylamido)ethoxymethyl(#5-tetramethylcyclopentadienyl)si lanetitanium (II) 1,3-pentadiene; (cyclododecylamido)ethoxymethyl(#5-tetramethylcyclopentadien yl) silanetitanium (II) 1,4-diphenyl-1,3- butadiene; (cyclododecylamido)ethoxymethyl(#5-tetramethylcyclopentadien yl)silanetitanium (II) 1,3- pentadiene; (2,4,6-trimethylanilido) ethoxymethyl(#5-tetramethylcyclopentadienyl)silanetitanium (II) 1,4- 5<BR> diphenyl- 1,3 -butadiene; (2,4,6-trimethylanilido)ethoxymethyl(ll -tetramethylcyclopentadienyl)<BR> <BR> <BR> silanetitanium (II) 1,3-pentadiene; (1-adamantylamido)ethoxymethyl(# -tetramethyl-

cyclopentadienyl)silanetitanium (II) 1,4-diphenyl-1,3-butadiene; and (1 -adamantylamido) ethoxymethyl(Tl 5-tetramethylcyclopentadienyl)silanetitanium 1,3-pentadiene.

The complexes can be prepared by use of well known synthetic techniques. The reactions are conducted in a suitable noninterfering solvent at a temperature from -100 to 300 OC, preferably from -78 to 100 "C, most preferably from 0 to 50 OC. A reducing agent may be used to cause the metal to be reduced from a higher to a lower oxidation state. Examples of suitable reducing agents are alkali metals, alkaline earth metals, aluminum and zinc, alloys of alkali metals or alkaline earth metals such as sodium/mercury amalgam and sodium/potassium alloy, sodium naphthalenide, potassium graphite, lithium alkyls, lithium or potassium alkadienyls, and Grignard reagents.

Suitable reaction media for the formation of the complexes include aliphatic and aromatic hydrocarbons, ethers, and cyclic etchers, particularly branched-chain hydrocarbons such as isobutane, butane, pentane, hexane, heptane, octane, and mixtures thereof; cyclic and alicyclic hydrocarbons such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof; aromatic and hydrocarbyl-substituted aromatic compounds such as benzene, toluene, and xylene, C1 4 dialkyl ethers, C 4 dialkyl ether derivatives of (poly)alkylene glycols, and tetrahydrofuran. Mixtures of the foregoing are also suitable.

Suitable activating cocatalysts and activating techniques have been previously taught with respect to different metal complexes in the following references: EP-A-277,003, US-A-5,153,157, US-A-5,064,802, EP-A-468,651 (equivalent to U. S. Serial No. 07/547,718), EP-A-520,732 (equivalent to U. S. Serial No.

07/876,268), WO 95/00683 (equivalent to U.S. Serial No. 08/82,201), and EP-A-520,732 (equivalent to U.

S. Serial No. 07/884,966 filed May 1, 1992).

Suitable activating cocatalysts for use herein include perfluorinated tri(aryl)boron compounds, and most especially tris(pentafluorophenyl)borane; nonpolymeric, compatible, noncoordinating, ion forming compounds (including the use of such compounds under oxidizing conditions), especially the use of ammonium-, phosphonium-, oxonium-, carbonium-, silylium- or sulfonium- salts of compatible, noncoordinating anions, and ferrocenium salts of compatible, noncoordinating anions. Suitable activating techniques include the use of bulk electrolysis. A combination of the foregoing activating cocatalysts and techniques may be employed as well.

Illustrative, but not limiting, examples of boron compounds which may be used as an activating cocatalysts are: tri-substituted ammonium salts such as: trimethylammonium tetrakis(pentafluoro-phenyl) borate; triethylammonium tetrakis(pentafluorophenyl) borate; tripropylammonium tetrakis(pentafluorophenyl) borate; tri(n-butyl)ammonium tetrakis(pentafluorophenyl) borate; tri(sec- butyl)ammonium tetrakis(pentafluoro-phenyl) borate; N,N-dimethylanilinium tetrakis(pentafluorophenyl) borate; N,N-dimethylanilinium n-butyltris(pentafluorophenyl) borate; N,N-dimethylanilinium benzyltris (pentafluorophenyl) borate; N,N-dimethylanilinium tetrakis(4-(t-butyldimethylsilyl)-2, 3, 5, 6-

tetrafluorophenyl) borate; N,N-dimethylanilinium tetrakis(4-(triisopropylsilyl)-2, 3, 5, 6-tetrafluorophenyl) borate; N,N-dimethylanilinium pentafluorophenoxytris (pentafluorophenyl) borate; N,N-diethylanilinium tetrakis(pentafluorophenyl) borate; N,N-dimethyl-2,4,6-trimethylanilinium tetrakis(pentafluorophenyl) borate; trimethylammonium tetrakis(2,3 ,4,6-tetrafluorophenyl)borate; triethylammonium tetrakis(2 ,3 ,4,6- tetrafluorophenyl) borate; tripropylammonium tetrakis(2,3,4,6-tetrafluorophenyl) borate; tri(n- butyl)ammonium tetrakis(2,3,4,6-tetrafluorophenyl) borate; dimethyl(t-butyl) ammonium tetrakis(2,3,4,6- tetrafluorophenyl) borate; N,N-dimethylanilinium tetrakis(2,3,4,6-tetrafluorophenyl) borate; N,N- diethylanilinium tetrakis(2,3,4,6-tetrafluorophenyl) borate; and N,N-dimethyl-2,4,6-trimethylanilinium tetrakis(2,3,4,6-tetrafluorophenyl) borate; disubstituted ammonium salts such as: di-(i-propyl)ammonium tetrakis (pentafluorophenyl) borate; and dicyclohexylammonium tetrakis(pentafluorophenyl) borate; trisubstituted phosphonium salts such as: triphenylphosphonium tetrakis (pentafluoro-phenyl) borate; tri(o-tolyl)phosphonium tetrakis(pentafluorophenyl) borate; and tri(2,6- dimethylphenyl)phosphonium tetrakis(pentafluorophenyl) borate; disubstituted oxonium salts such as: diphenyloxonium tetrakis(pentafluoro-phenyl) borate; di(o- tolyl)oxonium tetrakis(pentafluorophenyl) borate; and di(2,6-dimethylphenyl)oxonium tetrakis(pentafluorophenyl) borate; and disubstituted sulfonium salts such as: diphenylsulfonium tetrakis (pentafluorophenyl) borate; di(o- tolyl)sulfonium tetrakis(pentafluorophenyl) borate; and bis(2,6-dimethylphenyl)sulfonium tetrakis(pentafluorophenyl) borate.

A most preferred activating cocatalyst is trispentafluorophenylborane.

Alumoxanes, especially methylalumoxane or triisobutylaluminum modified methylalumoxane are also suitable activators and may be used for activating the present metal complexes.

The molar ratio of metal complex: activating cocatalyst employed preferably ranges from 1:1000 to 2 1, more preferably from 1: 5 to 1.5 1, most preferably from 1: 2 to 1:1. In the preferred case in which a metal complex is activated by trispentafluorophenylborane and triisobutylaluminum modified methylalumoxane, the titanium:boron:aluminum molar ratio is typically from 1: : 50 to 1: 0.5 : 0.1, most typically from 1: 3 : 5.

A support, especially silica, alumina, or a polymer (especially poly(tetrafluoroethylene) or a polyolefin) may be employed, and desirably is employed when the catalysts are used in a gas phase polymerization process. The support is preferably employed in an amount to provide a weight ratio of catalyst (based on metal):support from 1:100,000 to 1:10, more preferably from 1:50,000 to 1:20, and most preferably from 1:10,000 to 1:30. In most polymerization reactions the molar ratio of catalyst:polymerizable compounds employed is from lO-12:1 to 10-1:1, more preferably from 10-91 to 10- 5:1

At all times, the individual ingredients as well as the recovered catalyst components must be protected from oxygen and moisture. Therefore, the catalyst components and catalysts must be prepared and recovered in an oxygen and moisture free atmosphere. Preferably, therefore, the reactions are performed in the presence of a dry, inert gas such as, for example, nitrogen.

The polymerization may be carried out as a batchwise or a continuous polymerization process, with continuous polymerizations processes being required for the preparation of substantially linear polymers. In a continuous process, ethylene, comonomer, and optionally solvent and diene are continuously supplied to the reaction zone and polymer product continuously removed therefrom.

In general, the homogeneous linear or substantially linear polymer may be polymerized at conditions for Ziegler-Natta or Kaminsky-Sinn type polymerization reactions, that is, reactor pressures ranging from atmospheric to 3500 atmospheres (350 MPa). The reactor temperature should be greater than 80"C, typically from 100"C to 2500C, and preferably from 100"C to 1500C, with temperatures at the higher end of the range, that is, temperatures greater than 1 000C favoring the formation of lower molecular weight polymers.

In conjunction with the reactor temperature, the hydrogen:ethylene molar ratio influences the molecular weight of the polymer, with greater hydrogen levels leading to lower molecular weight polymers. <BR> <BR> <P>When the desired polymer has an I2 of 1 g/10 min, the hydrogen:ethylene molar ratio will typically be 0: 1.

When the desired polymer has an I2 of 1000 g/10 min., the hydrogen:ethylene molar ratio will typically be from 0.45 1 to 0.7:1. The upper limit of the hydrogen:ethylene molar ratio is typically 2.2-2.5 1.

Generally the polymerization process is carried out with a differential pressure of ethylene of from 10 to 1000 psi (70 to 7000 kPa), most preferably from 40 to 60 psi (30 to 300 kPa). The polymerization is generally conducted at a temperature of from 80 to 250 "C, preferably from 90 to 170 °C, and most preferably from greater than 95 to 1400C.

In most polymerization reactions the molar ratio of catalyst:polymerizable compounds employed is from l0l2:l to 10l:l, more preferably from 10-9:1 to 10-5:1.

Solution polymerization conditions utilize a solvent for the respective components of the reaction.

Preferred solvents include mineral oils and the various hydrocarbons which are liquid at reaction temperatures. Illustrative examples of useful solvents include alkanes such as pentane, iso-pentane, hexane, heptane, octane and nonane, as well as mixtures of alkanes including kerosene and lsoparETM, available from Exxon Chemicals Inc.; cycloalkanes such as cyclopentane and cyclohexane; and aromatics such as benzene, toluene, xylenes, ethylbenzene and diethylbenzene.

The solvent will be present in an amount sufficient to prevent phase separation in the reactor. As the solvent functions to absorb heat, less solvent leads to a less adiabatic reactor. The solvent: ethylene ratio (weight basis) will typically be from 2.5 1 to 12 1, beyond which point catalyst efficiency suffers. The most typical solvent: ethylene ratio (weight basis) is in the range of from 5 1 to 10: 1.

The polymerization may further be conducted in a slurry polymerization process, using the catalysts as described above as supported in an inert support, such as silica. As a practical limitation, slurry polymerizations take place in liquid diluents in which the polymer product is substantially insoluble.

Preferably, the diluent for slurry polymerization is one or more hydrocarbons with less than 5 carbon atoms.

If desired, saturated hydrocarbons such as ethane, propane or butane may be used in whole or part as the diluent. Likewise the a-olefin monomer or a mixture of different a-olefin monomers may be used in whole or part as the diluent. Most preferably the diluent comprises in at least major part the a-olefin monomer or monomers to be polymerized.

The homogeneous ethylene polymer will typically be present in the composition of flue invention in an amount of at least 5 weight percent, preferably at least 10 weight percent, more preferably at least 20 weight percent, more preferably at least 50 weight percent, and most preferably at least 70 weight percent; typically less than 99 weight percent, preferably less than 95 weight percent, more preferably less than 90 weight percent, and most preferably less than 80 weight percent.

The homogeneous ethylene polymer will typically have a density of at least 0.855 g/cm3, preferably at least 0.860 g/cm3, more preferably at least 0.865 g/cm3, and most preferably at least 0.865 g/cm3; typically no more than 0.910 g/cm3, preferably no more than 0.900 g/cm3, more preferably no more than 0.890 g/cm3, and most preferably no more than 0.880 g/cm3.

The homogeneous ethylene polymer will typically have a melt index (I2) of at least 50 g/10 min., preferably at least 60 g/10 min.; preferably no more than 10,000 g/10 min., more preferably no more than 1500 g/10 min.

While the polymer compositions of the invention may usefully comprise a single homogeneous ethylene polymer, in combination with a wax and a nucleating agent, in exemplary preferred embodiments, two or more homogenous ethylene polymers may be employed, which differ from one another in terms of their density and/or melt index. In one preferred embodiment, the polymer composition will comprise a first homogeneous ethylene polymer and a second homogeneous ethylene polymer differing by at least 20 g/10 min. in terms of melt index. In such embodiments, the first homogeneous ethylene polymer will have a melt index of at least 1 g/10 min., preferably at least 10 g/10 min., more preferably at least 30 g/10 min., and most preferably at least 50 g/10 min.; preferably no more than 200 g/10 min., more preferably no more than 150 g/10 min., even more preferably no more than 100 g/10 min., and most preferably no more than 80 g/10 min. The second homogeneous ethylene polymer will have a melt index of at least 100 g/10 min., preferably at least 120 g/10 min., more preferably at least 170 g/10 min., more preferably at least 220 g/10 min.; preferably no more than 10,000 g/10 min., more preferably no more than 5000 g/10 min., more preferably no more than 3000 g/10 min., and most preferably no more than 1500 g/10 min.

The polymer compositions of the invention will further comprise a wax or other higher melting ethylene polymer (hereinafter collectively "waxes"). Such waxes will increase the upper use temperature

and the onset of crystallization temperature of the polymer compositions. Accordingly, the wax will typically have a crystalline melting point, as determined by differential scanning calorimetry (DSC) which is at least 10"C, preferably at least 200C, and most preferably at least 300C greater than that of the homogeneous ethylene polymer. Waxes useful in the polymer compositions of the present invention include paraffin waxes, microcrystalline waxes, Fischer-Tropsch, polyethylene and by-products of polyethylene wherein the Mw is less than 3000.

Also suitable are ultra-low molecular weight ethylene/a-olefin interpolymers prepared using a constrained geometry catalyst, and may be referred to as homogeneous waxes. Such homogeneous waxes, as well as processes for preparing such homogeneous waxes, are more fully described above in conjunction with the description of ultra-low molecular weight ethylene polymers. Homogeneous waxes lead to a low polymer and formulation viscosity, but are characterized by peak crystallization temperatures which are greater than the peak crystallization temperatures of corresponding higher molecular weight materials of the same density.

Homogeneous waxes will be either ethylene homopolymers or interpolymers of ethylene and a C3- C20 a-olefin. The homogeneous wax will have a number average molecular weight less than 6000, preferably less than 5000. Such homogeneous waxes will typically have a number average molecular weight of at least 800, preferably at least 1300.

Homogeneous waxes, in contrast to paraffinic waxes and crystalline ethylene homopolymer or interpolymer waxes, will have a MW/Mn of from 1.5 to 2.5, preferably from 1.8 to 2.2.

In the case of polyethylene based waxes and homogeneous waxes, the wax will have a density greater than that of the homogeneous ethylene polymer of component (a) of the polymer compositions of the invention, and will typically have a density of at least 0.910 g/cm3, preferably at least 0.915 g/cm3, more preferably at 0.920 g/cm3, and most preferably at least 0.925 g/cm3.

The wax will typically be provided in the polymer composition of the invention in an amount of at least 1 weight percent, preferably at least 5 weight percent, more preferably at least 10 weight percent, and most preferably at least 20 weight percent. The wax will typically be provided in the polymer composition of the invention in an amount of no more than 40 weight percent, preferably no more than 35 weight percent, more preferably no more than 30 weight percent.

The polymer compositions of the invention will further comprise a nucleating agent. The term "nucleating agent", is defined to mean a material useful to control the particle size and process by which crystals are formed from liquids, supersaturated solutions or saturated vapors. Two classes of nucleating agents include: (1) preformed particles which are dispersed into the polymer composition under high shear; and (2) particles which are formed in situ in melt of the other components of the polymer composition, which particles crystallize at a higher temperature than the other components of the polymer composition, forming a fibrous network which serves as a nucleating site for the homogeneous polymer and wax.

Exemplary preformed particles which are dispersed into a polymer system under high shear include organophilic multi-layered particles. Such particles can be prepared from hydrophilic phyllosilicates by methods well known in the art. Illustrative of such materials are smectite clay minerals

such as montmorillonite, nontronite, beidellite, volkonskoite, hectorite, saponite, sauconite, magadiite, kenyaite, and vermiculite. Other useful multi-layered particles include illite minerals such as ledikite and admixtures of illites with the clay minerals named above. Other useful multi-layered particles, particularly useful with anionic polymers, are the layered double hydroxides such as Mg6AI34(OH)18 g(CO3)} 7H2O (see W.T. Reichle, J. Catal., Vol. 94, p. 547 (1985), which have positively charged layers and exchangeable anions in the interlayer spaces. Other multi-layered particles having little or no charge on the layers may be useful in this invention. Such materials include chlorides such as ReCI3 and FeOCI; chalcogenides such as TiS2, MoS2, and MoS3; cyanides such as Ni(CN)2; and oxides such as H2Si2O5, V5O,3, HTiNbO3, CrO 5Vo sS2 W0y28O7, Cr3O8, MoO3(OH)2, VOPO4-2H2O, CaPO4CH3-H2O, MnHAsO4-H2O, and Ag6Mo,0033.

The hydrophilic multi-layered particle can be rendered organophilic by exchange of sodium, potassium, or calcium cations with a suitable material such as a water-soluble polymer, a quaternary ammonium salt, an amphoteric surface-active agent, and a chlorine compound, or the like. Representative examples of exchangeable water-soluble polymers include water-soluble polymers of vinyl alcohol (for example, poly(vinyl alcohol)), polyalkylene glycols such as polyethylene glycol, water-soluble cellulosic polymers such as methyl cellulose and carboxymethyl cellulose, the polymers of ethylenically unsaturated carboxylic acids such as poly(acrylic acid) and their salts, and polyvinyl pyrrolidone.

Representative examples of the quaternary ammonium salts (cationic surface-active agents) which can be employed in this invention include the quaternary ammonium salts having octadecyl, hexadecyl, tetradecyl, or dodecyl groups; with preferred quaternary ammonium salts including dimethyl dihydrogenated tallow ammonium salt, octadecyl trimethyl ammonium salt, dioctadecyl dimethyl ammonium salt, hexadecyl trimethyl ammonium salt, dihexadecyl dim ethyl ammonium salt, tetradecyl trimethyl ammonium salt, and ditetradecyl dimethyl ammonium salt.

Preferred organophilic multi-layered particles are those prepared by ion exchange of quaternary ammonium cations. A more preferred organophilic multi-layered material is a montmorillonite clay treated with a quaternary ammonium salt, most preferably dimethyl dihydrogenated tallow ammonium salt, commercially sold as ClaytoneTM HY (a trademark of Southern Clay Products).

The organophilic multi-layered particles may also be prepared by the exchange of the sodium, potassium, or calcium cations with an inorganic material, a polymeric substance obtained by hydrolyzing a polymerizable metallic alcoholate such as Si(OR)4, Al(OR)3, Ge(OR)4, Si(OC2H5)4, Si(OCH3)4, Ge(OC3H7), or Ge(OC2H5)4, either alone, or in any combination. Alternatively, the inorganic material can be a colloidal inorganic compound. Representative colloidal inorganic compounds which can be used include SiO2, Sub2 03, Fe2O3, Awl203, TiO2, ZrO2, and SnO2, alone, or in any combination.

The organophilic multi-layered material may also be prepared through exchange of functionalized organosilane compounds, as disclosed in WO 93/11190, pp. 9-21.

Exemplary nucleating agents which are particles which are formed in situ in melt of flue other components of the polymer composition include acetals, such as trinaphthylidene sorbitol, tri (4-methyl- 1 - naphthylidene) sorbitol, tri-(4-methyoxy- 1 -naphtylidene)sorbitol, and dibenzylidene zylitol. An example of

these materials is 3,4,-dimethyl dibenzylidene sorbitol, which is available from Milliken Chemical, Inc. as MilladTM 3988, which is further available as a 10 weight percent mixture in 90 weight percent low density polyethylene as MilladTM 5L71-10, as well as MilladTM 3905P dibenzylidene sorbitol.

The concentration of the nucleating agent in the polymer composition of the invention will be in an amount effective to produce the desired improvement in elongation at break, and is application dependent, but is preferably not less than 0.01 weight percent, more preferably not less than 0.05 weight percent, even more preferably not less than 0.1 weight percent, and most preferably not less than 0.2 weight based on the total weight of the polymer composition; and preferably not greater than 10 weight percent, more preferably not greater than 5 weight percent, even more preferably not greater than 1 weight percent, and most preferably no greater than 0.5 weight percent of the total polymer composition.

The polymer composition of the invention will be characterized as having an elongation at break which is at least 50 percent greater, preferably at least 100 percent greater, more preferably at least 200 percent greater, even more preferably at least 400 percent greater than comparative polymer compositions which lack the nucleating agent. As illustrated below in the examples, highly preferred polymer compositions are possible, which exhibit a percent elongation at break which is at least 600 percent, an even at least 700 percent greater than comparative compositions which lack the nucleating agent.

While the hot melt adhesives of the invention will preferably comprise at least one homogeneous ethylene polymer, they may, instead, or in addition, comprise any of a variety of traditional olefin polymers.

The term olefin polymer is in part used herein to refer to C2-C8 a-olefin homopolymers or ethylene/a-olefin interpolymers prepared, for example, with a Ziegler Natta catalyst, low density polyethylene prepared, for example, in a high pressure reaction process. Olefin polymers prepared in a high pressure process are generally known as low density polyethylenes (LDPE) and are characterized by branched chains of polymerized monomer units pendant from the polymer backbone. LDPE polymers generally have a density between 0.910 and 0.935 g/cm3. Ethylene polymers and copolymers prepared by the use of a coordination catalyst, such as a Ziegler or Phillips catalyst, are generally known as linear polymers because of the substantial absence of branch chains of polymerized monomer units pendant from the backbone. High density polyethylene (HDPE), generally having a density of 0.941 to 0.965 g/cm3, is typically a homopolymer of ethylene, and it contains relatively few branch chains relative to the various linear copolymers of ethylene and an a-olefm. HDPE is well known, commercially available in various grades, and may be used in this invention.

Olefin polymers which are linear copolymers of ethylene and at least one a-olefin of 3 to 12 carbon atoms, preferably of4 to 8 carbon atoms, are also well known and commercially available. As is well known in the art, the density of a linear ethylene/a-olefin copolymer is a function of both the length of the a-olefin and the amount of such monomer in the copolymer relative to the amount of ethylene, the greater the length of the a-olefin and the greater the amount of a-olefin present, the lower the density of the copolymer. Linear low density polyethylene (LLDPE) is typically a copolymer of ethylene and an a-olefin of 3 to 12 carbon atoms, preferably 4 to 8 carbon atoms (for example, 1-butene, 1-octene, etc.), that has sufficient a-olefin content to reduce the density of the copolymer to that of LDPE. When the copolymer

contains even more a-olefin, the density will drop below 0.91 g/cm3 and these copolymers are known as ultra low density polyethylene (ULDPE) or very low density polyethylene (VLDPE). The densities of these linear polymers generally range from 0.87 to 0.91 g/cm3.

Both the materials made by the free radical catalysts and by the coordination catalysts are well known in the art, as are their methods of preparation. Heterogeneous linear ethylene polymers are available from The Dow Chemical Company as DowlexTM LLDPE and as AttaneTM ULDPE resins. Heterogeneous linear ethylene polymers can be prepared via the solution, slurry or gas phase polymerization of ethylene and one or more optional a-olefin comonomers in the presence of a Ziegler Natta catalyst, by processes such as are disclosed in U.S. Patent No. 4,076,698 to Anderson et al. Preferably, heterogeneous ethylene polymers are typically characterized as having molecular weight distributions, M+/Mn, in the range of from 3.5 to 4.1. Relevant discussions of both of these classes of materials, and their methods of preparation are found in U.S. Patent No. 4,950,541 and the patents to which it refers.

Likewise suitable as olefin polymers are ethylene polymers having at least one comonomer selected from the group consisting of vinyl esters of a saturated carboxylic acid wherein the acid moiety has up to 4 carbon atoms, unsaturated mono- or dicarboxylic acids of 3 to 5 carbon atoms, a salt of the unsaturated acid, esters of the unsaturated acid derived from an alcohol having 1 to 8 carbon atoms, and mixtures thereof. Terpolymers of ethylene and these comonomers are also suitable. Ionomers, which are completely or partially neutralized copolymers of ethylene and the acids described above, are discussed in more detail in U.S. Patent 3,264,272. In addition, terpolymers of ethylene/vinyl acetate/carbon monoxide or ethylene/methyl acrylate/carbon monoxide containing up to 15 weight percent carbon monoxide may also be employed.

The ethylene to unsaturated carboxylic comonomer weight ratio is preferably from 95:5 to 40:60, more preferably from 90:10 to 45:50, and even more preferably from 85:15 to 60:40. The melt index (I2 at 1900C) of these modifying interpolymers of ethylene may range from 0.1 to 150, preferably from 0.3 to 50, and more preferably from 0.7 to 10 g/10 min. Physical properties, principally elongation, are known to decline to lower levels when the ethylene copolymer melt index is above 30 g/10 min.

Suitable ethylene/unsaturated carboxylic acid, salt and ester interpolymers include ethylene/vinyl acetate (EVA) including, but not limited to, the stabilized EVA described in U.S. Patent 5,096,955; ethylene/acrylic acid (EEA) and its ionomers; ethylene/methacrylic acid and its ionomers; ethylene/methyl acrylate; ethylene/ethyl acrylate; ethylene/isobutyl acrylate; ethylene/n-butyl acrylate; ethylene/isobutyl acrylate/methacrylic acid and its ionomers; ethylene/n-butyl acrylate/methacrylic acid and its ionomers; ethylene/isobutyl acrylate/acrylic acid and its ionomers; ethylene/n-butyl acrylate/acrylic acid and its ionomers; ethylene/methyl methacrylate; ethylene/vinyl acetate/methacrylic acid and its ionomers ethylene/vinyl acetate/acrylic acid and its ionomers; ethylene/vinyl acetate/carbon monoxide; ethylene/methacrylate/carbon monoxide; ethylene/ n-butyl acrylate/carbon monoxide; ethylene/isobutyl acrylate/carbon monoxide; ethylene/vinyl acetate/monoethyl maleate; and ethylene/methyl acrylate/monoethyl maleate. Particularly suitable copolymers are EVA; EAA; ethylene/methyl acrylate; ethylene/isobutyl acrylate; and ethylene/methyl methacrylate copolymers and mixtures thereof. Certain

properties, such as tensile elongation, are taught to be improved by certain combinations of these ethylene interpolymers, as described in U.S. Patent 4,379,190. The procedures for making these ethylene interpolymers are well known in the art and many are commercially available.

When an ethylene interpolymer is used in additional to a homogeneous ethylene polymer, the ethylene interpolymer will typically be added in an amount of up to 25 percent by weight to increase the cohesive strength, improve the sprayability, modify the open time, increase the flexibility, etc. This modifying polymer may be any compatible elastomer, such as a thermoplastic block copolymer, a polyamide, an amorphous or crystalline polyolefin such as polypropylene, polybutylene or polyethylene wherein Mw is greater than 3000; an ethylenic copolymer such as ethylene-vinyl acetate (EVA), ethylene- methyl acrylate, or a mixture thereof. Surprisingly, the homogeneous ethylene/a-olefin interpolymers are also compatible with polyamides, resulting in plasticizer resistant pressure sensitive adhesives. The modifying polymer will typically be used in a relatively low concentration, so as not to detract from the improved properties of the homogeneous ethylene/a-olefin interpolymer. A preferred modifying polymer for increasing the open time and heat resistance is a polybutene-l copolymer such as DuraflexTM 8910 (Shell).

In the embodiment of the invention which provides a hot melt adhesive formulation, such hot melt adhesive formulation will preferably comprise a homogeneous ethylene polymer, a wax, a nucleating agent, and a tackifier.

In the inventive hot melt adhesive formulations, the homogeneous ethylene polymer, as described above, will preferably be provided in an amount of at least 5 weight percent, preferably at least 10 weight percent, more preferably at least 20 weight percent, more preferably at least 50 weight percent, and most preferably at least 70 weight percent; typically less than 99 weight percent, preferably less than 95 weight percent, more preferably less than 90 weight percent, and most preferably less than 80 weight percent.

In the inventive hot melt adhesive formulations, the wax will typically be provided in an amount of at least 1 weight percent, preferably at least 5 weight percent, more preferably at least 10 weight percent, and most preferably at least 20 weight percent. The wax will typically be provided to the hot melt adhesive formulation in an amount of no more than 40 weight percent, preferably no more than 35 weight percent, more preferably no more than 30 weight percent.

In the inventive hot melt adhesive formulations, the nucleating agent will typically be provided in an amount of not less than 0.01 weight percent, more preferably not less than 0.05 weight percent, even more preferably not less than 0.1 weight percent, and most preferably not less than 0.2 weight based on the total weight of the hot melt adhesive formulation; and preferably not greater than 10 weight percent, more preferably not greater than 5 weight percent, even more preferably not greater than 1 weight percent, and most preferably no greater than 0.5 weight percent of the hot melt adhesive formulation.

In the inventive hot melt adhesive formulations, the tackifier will typically be provided in an amount of at least 1 weight percent, more preferably at least 5 weight percent, and most preferably at least

10 weight percent; and typically no more than 80 weight percent, preferably no more than 60 weight percent, more preferably no more than 45 weight percent of the hot melt adhesive formulation.

In general terms, the tackifiers useful in the hot melt adhesives of the invention comprise resins derived from renewable resources such as rosin derivatives including wood rosin, tall oil, gum rosin; rosin esters, natural and synthetic terpenes, and derivatives of such. Aliphatic, aromatic or mixed aliphatic- aromatic petroleum based tackifiers are also useful in the adhesives of this invention.

Representative examples of useful hydrocarbon resins includes alpha-methyl styrene resins, branched and unbranched C5 resins, C9 resins, C,0 resins, as well as styrenic and hydrogenated modifications of such. Tackifiers range from being a liquid at 370C to having a ring and ball softening point of 135"C.

Solid tackifying resins with a softening point greater than 100"C, more preferably with a softening point greater than 130"C are particularly useful to improve the cohesive strength of the adhesives of the present invention.

For the adhesives of the invention, the preferred tackifying resin is predominantly aliphatic.

However, tackifying resins with increasing aromatic character are also useful, particularly when a second tackifier or mutually compatible plasticizer is employed.

Exemplary tackifiers include EastotacE H-100, H-115 and H-130 from Eastman Chemical Co. in Kingsport, TN which are partially hydrogenated cycloaliphatic petroleum hydrocarbon resins with softening points of 100"C, 115"C and 130"C, respectively. These are available in the E grade, the R grade, the L grade and the W grade indicating differing levels of hydrogenation with E being the least hydrogenated and W being the most hydrogenated. The E grade has a bromine number of 15, the R grade a bromine number of 5, the L grade a bromine number of 3 and the W grade has a bromine number of 1. There is also an Eastotac(D H-142R from Eastman Chemical Co. which has a softening point of 140"C. Other useful tackifying resins include EscorezB 5300 and 5400, partially hydrogenated cycloaliphatic petroleum hydrocarbon resins, and EscorezO 5600, a partially hydrogenated aromatic modified petroleum hydrocarbon resin all available from Exxon Chemical Co. in Houston, TX; WingtackE Extra which is an aliphatic, aromatic petroleum hydrocarbon resin available from Goodyear Chemical Co. in Akron, OH; HercoliteB 2100, a partially hydrogenated cycloaliphatic petroleum hydrocarbon resin available from Hercules, Inc. in Wilmington, DE; and ZonatacB 105 and 501 Lite, which are styrenated terpene resins made from d-limonene and available from Arizona Chemical Co. in Panama City, FL.

There are numerous types of rosins and modified rosins available with differing levels of hydrogenation including gum rosins, wood rosins, tall-oil rosins, distilled rosins, dimerized rosins and polymerized rosins. Some specific modified rosins include glycerol and pentaerythritol esters of wood rosins and tall-oil rosins. Commercially available grades include, but are not limited to, SylvatacB 1103, a pentaerythritol rosin ester available from Arizona Chemical Co., Unitac(E) R-100 Lite, a pentaerythritol rosin ester from Union Camp in Wayne, NJ, Permalyn(D 305, a erythritol modified wood rosin available from Hercules and Foral 105 which is a highly hydrogenated pentaerythritol rosin ester also available from

Hercules. SylvatacB R-85 and 295 are 85"C and 95"C melt point rosin acids available from Arizona Chemical Co. and Foral AX is a 70"C melt point hydrogenated rosin acid available from Hercules, Inc.

Nirez V-2040 is a phenolic modified terpene resin available from Arizona Chemical Co.

The hot melt adhesive of the invention may optionally comprise a plasticizer. When a plasticizer is employed, it will typically be provided to the hot melt adhesive formulation in an amount of at least 1 weight percent, preferably at least 5 weight percent, and more preferably at least 10 weight percent; and typically in an amount of no more than 30 weight percent, preferably no more than 25 weight percent, and most preferably no more than 20 weight percent of the hot melt adhesive formulation.

A plasticizer is broadly defined as a typically organic composition that can be added to thermoplastics, rubbers and other resins to improve extrudability, flexibility, workability, or stretchability.

The plasticizer may be either a liquid or a solid at ambient temperature. Exemplary liquid plasticizers include hydrocarbon oils, polybutene, liquid tackifying resins, and liquid elastomers. Plasticizer oils are primarily hydrocarbon oils which are low in aromatic content and which are paraffinic or napthenic in character. Plasticizer oils are preferably low in volatility, transparent and have as little color and odor as possible. The use of plasticizers in this invention also contemplates the use of olefin oligomers, low molecular weight polymers, vegetable oils and their derivatives and similar plasticizing liquids.

When a solid plasticizing agent is employed, it will preferably have a softening point above 60"C.

It is believed that by combining the homogeneous ethylene/a-olefin interpolymer with a suitable tackifying resin and a solid plasticizer such as a cyclohexane dimethanol dibenzoate plasticizer, the resulting adhesive composition may be applied at temperatures below 1200C, preferably below 100"C. Although a 1,4- cyclohexane dimethanol dibenzoate compound commercially available from Velsicol under the trade name BenzoflexTM 352 is exemplified, any solid plasticizer that will subsequently recrystallize in the compounded thermoplastic composition is suitable. Other plasticizers that may be suitable for this purpose are described in EP 0422 108 B1 and EP 0 410 412 B1, both assigned to H.B. Fuller Company.

In the embodiments of the invention which further comprise a plasticizer, preferably a solid plasticizer will be employed.

The hot melt adhesives of the invention will be characterized as having a percent elongation at break which is at least 25 percent greater, preferably at least 50 percent greater, and more preferably at least 100 percent greater than a comparative hot melt adhesive which lacks the nucleating agent.

Additives such as antioxidants (for example, hindered phenolics (for example, IrganoxTM 1010, IrganoxTM 1010), phosphites (for example, lrgafosTM 168)), cling additives (for example, polyisobutylene), antiblock additives, colorants, pigments, extender oils, fillers, and tackifiers can also be included in the present compositions, to the extent that they do not detrimentally affect the elongation properties which are characteristic of the polymer compositions of the invention. In the case of antioxidants, cling additives, antiblock additives, colorants, etc., such optional components will typically be present in the polymer compositions of the invention in an amount less than 5 weight percent, preferably less than 3 weight

percent, more preferably less than 1 weight percent. In the case of extender oils and tackifiers, such components may be provided in substantially greater amounts. Except as otherwise provided above, in the case of the hot melt adhesive formulations of the invention which are discussed in more detail above, when it is desirable to include such components, they will typically be provided in an amount greater than 5 weight percent, preferably at least 10 weight percent, more preferably at least 20 weight percent; preferably no more than 70 weight percent, more preferably no more than 60 weight percent.

Likewise, the compositions of the invention may further optionally comprise other polymeric components, including but not limited to polypropylene, styrene-butadiene block copolymers, and conventional polyolefins (such as, for instance, linear low density polyethylene, low density polyethylene, and ethylene vinyl acetate copolymers).

The compositions of the present invention are compounded by any convenient method, including dry blending the individual components and subsequently melt mixing, either directly in the extruder used to make the finished article, or by pre-melt mixing in a separate extruder or mixer such as, for example, a Haake unit or a Banbury mixer.

The polymer compositions of the invention will find utility in applications requiring high elongation at break, while maintaining a high onset of crystallization temperature, such as in the high-speed coating of fabrics, carpet backing, floor tile and sheeting, and adhesives.

Examples Preparation of Polymer Compositions. The ingredients utilized in the polymer compositions of the invention and of the comparative examples are set forth in the following Table One. The homogeneous ethylene polymers are prepared in accordance with the procedures of U.S. Patent Nos. 5,272,236 and 5,278,272, and in accordance with the procedures for preparing ultra-low molecular weight ethylene polymers and homogeneous waxes set forth in WOl97/26287.

The compositions of the examples and comparative examples were prepared in accordance with the following procedure. The homogeneous polymer was added in the amount indicated in the following Table Two to a Haake mixer which was preheated to 130"C and which was operated at 20 revolutions per minute.

After the polymer melted, the mixing speed was increased to 200 revolutions per minute, and the polymer was mixed for 2 minutes. The nucleating agent was then added in the amount indicated in Table Two, and the resultant material was mixed for two minutes. The wax was added in the amount indicated in Table Two, and the resultant materials was mixed for two minutes. After cooling to 950C, the sample was removed from the mixture.

Plaque Preparation. Plaque-shaped samples were made by compression forming using the following procedure. Fifteen (15) grams of the sample indicated in Table Two was placed between two polytetrafluoroethylene coated-fiber glass cloths, and was pressed at 200 psig (1.38 MPa) for 2 to 3 minutes at a temperature of 130"C. The pressure was increased to 20,000 psig (138 MPa), and the sample was maintained at this pressure for 2 to 3 minutes. The sample was cooled to 250C, and was allowed to equilibrate for at least 12 hours. In accordance with ASTM D-1708, a punch press equipped with a micro- tensile die was used to cut dumbbell-shaped micro-tensile specimens from the plaques, which were evaluated for elongation at break, break stress, and peak stress. The nominal stress-strain diagram for each sample was determined using an InstronTM 4507 Materials Testing System (available from Instron Corporation). The crosshead speed was 4 inches/minute (10 cm/minute).

Table One: Ingredients Identification Descriptive Information Company of Orgin Polymer A Homogeneous ethylene/1-octene interpolymer having a density of 0.870 g/cm3 and an I2 of 70 g/10 min. (additives The Dow Chemical Company include 1250 ppm calcium stearate, 800 ppm PEPQ (tetrakis(2,4-di-t-butylphenyl)-4,4'-biphenylene diphosphonite) (available from Clariant Corporation), and 2000 ppm IrganoxTM 1010) Polymer B Homogeneous ethylene/1-octene interpolymer having a density of 0.890 g/cm3 and an I2 of 2200 g/10 min. The Dow Chemical Company (melt viscosity at 350°F of 5000 centipoise) (additives include 2000 ppm IrganoxTM 1010) Polymer C Homogeneous ethylene/1-octene interpolymer having a density of 0,870 g/cm3 and an I2 of 190 g/10 min. The Dow Chemical Company (additives include 2000 ppm IrganoxTM 1010) Polymer D Homogeneous ethylene/1-octene interpolymer having a density of 0,860 g/cm3 and an I2 of 10 g/10 min. (additives The Dow Chemical Company include 2000 ppm IrganoxTM 1010). Polymer E Homogeneous ethylene/1-octene interpolymer having a density of 0.880 g/cm3 and an I2 of 1000 g/10 min. The Dow Chemical Company Wax A R-7152 fully refined paraffin wax having a melting point of 151°F Moore and Munger Marketing, Inc Wax B Bareco C-1035 Fischer Tropsch wax having a melting point of 205°F Bareco, Inc. Wax C Bareco PX-100 Fischer Tropsch Wax Bareco, Inc. Wax D Paraflint H1 Fischer Tropsch wax having a congealing point of 208°F Moore and Munger Marketing, Inc. Wax E Paraflint C-80 Fischer Tropsch wax having a congealing point of 176°F Moore and Munger Marketing, Inc. Wax F 180 microcrystalline wax Shell Chemical Company Nucleating MilladTM 5L71-10 Concentrate (10 weight percent Millad TM 3988 3,4-dimethyl dibenzylidene sorbitol is Milliken Chemicals Agent A dispersed in 90 weight percent low density polyethylene, and is provided at 92 weight percent in conjunction with 4 weight percent IrganoxTM 1076 and 4 weight percent IrgafosTM 168) Nucleating MilladTM 3905 (3,4-dimethyl dibenzylidene sorbitol) Milliken Chemicals Agent B Tackifier A Escorez 5615 Exxon Chemical Company Table Two: Polymer Compositions Ex. 1 Comp. Ex. Ex. 3 Comp. Ex. Ex. 5 Comp. Ex. Ex. 7 Comp. Ex. Ex. 9 Comp. Ex. 2 4 6 8 10 Polymer A 52.3 52.6 52.3 52.6 52.3 52.6 52.3 52.6 52.3 52.6 Polymer B 22.4 22.4 22.4 22.4 22.4 22.4 22.4 22.4 22.4 22.4 Wax A 25.0 25.0 Wax B 25.0 25.0 Wax C 25.0 25.0 Wax D 25.0 25.0 Wax E 25.0 25.0 Nucleating Agent A 0.3 0 0.3 0 0.3 0 0.3 0 0.3 0

The percent strain at break, peak stress, and break stress of the compositions of Examples and Comparative Examples 1-10 are set forth in Figure 1. As illustrated therein, the subject invention provides compositions exhibiting at least four times greater percent strain at break (in the case of Examples 1, 3, 6, 7, and 9), at least six times greater percent strain at break (in the case of Examples 1, 7, and 9), and at least fifteen times greater percent strain at break (in the case of Example 9), than comparative compositions lacking the nucleating agent.

As further illustrated in Figure 1, the subject invention provides compositions exhibiting a percent strain at break which is at least 120 percent (in the case of Examples 1, 3, 5, 7, and 9), preferably at least 200 percent (in the case of Examples 1, 7, and 9), and more preferably at least 400 percent (in the case of Example 9).

As further illustrated in Figure 1, the subject invention provides compositions exhibiting a break stress which is at least 7 times greater (in the case of Examples 1, 3, 5, 7, and 9) than that of the comparative compositions lacking the nucleating agents. As further illustrated, the subject invention provides compositions exhibiting a break stress of at least 500 psi (3.4 MPa) (in the case of Examples 1, 3, 5, 7, and 9), with Example 7 exhibiting a break stress of nearly 600 psi (4.1 MPa).

As further illustrated in Figure 1, the compositions of the invention exhibit a peak stress which is at least 10 percent greater (in the case of Examples 1,3, 5, 7, and 9), preferably at least 20 percent greater (in the case of Examples 1, 3, 5, and 9), and most preferably at least 30 percent greater (in the case of Examples 3 and 9) than that of comparative compositions lacking the nucleating agents. As further illustrated, the subject invention provides compositions exhibiting a peak stress which is at least 650 psi (4.5 MPa) (in the case of Examples 1, 3, 5, 7, and 9).

Formulations Containing a Single Homogeneous Ethylene Polymer Example 11 is prepared in accordance with the procedure described with respect to Examples and Comparative Examples 1-10. Example 11 contains 69.85 weight percent Polymer C, 29.85 weight percent Wax A, and 0.3 weight percent Nucleating Agent A. Comparative Example 12 contains 70 weight percent Polymer C and 30 weight percent Wax A. Example 11 exhibits a percent elongation at break, peak stress, and break stress which is improved over that of Comparative Example 12.

Preparation of Hot Melt Adhesive Formulations The hot melt adhesive formulations were blended with a Haake mixer using the following procedure. First, the mixer was heated to 1300C. The mixer was started, and, when it achieved a speed of 20 revolutions per minute, the polymer portion of the formulation was added. After the polymer had melted, the speed was raised to 200 revolutions per minute, and the molten polymer was mixed for two minutes. The nucleating agent (when used) was added, and the mixture was mixed for two minutes. The wax and tackifier were then added, and the formulation was mixed for two minutes. The formulation was cooled to 95"C, and was removed from the mixer. The formulations prepared are set forth in the following Table Three.

Table Three Ingredient HMA-A (weight percent) Comparative HMA-B (weight percent) Polymer D 17.5 16.0 Polymer E 17.5 16.0 Nucleating Agent B 3.0 0 Wax F 25.0 25.0 Tackifier A 39.5 39.5 HMA-A is characterized as having a percent strain at break which is at least 800 percent, as compared to the Comparative HMA-B which has a percent strain at break of 420 percent. HMA-A has a yield stress which is within 10 percent of the yield stress of Comparative HMA-B. HMA-A further has a break stress which is within 10 percent of the break stress of Comparative HMA-B.

Preparation of Homogeneous Ethylene Polymers, Ultralow Molecular Weight Ethylene Polymers, and Homogeneous Waxes for Use in the Polymer Compositions of the Invention The following provides procedures and conditions useful to make homogeneous ethylene polymers, ultra-low molecular weight ethylene polymers and homogeneous waxes for use in the polymer compositions of the invention: Catalyst Preparation One Part 1: Preparation of TiCl3(DME)1 5 The apparatus (referred to as R- 1) was set-up in the hood and purged with nitrogen; it consisted of a 10 L glass kettle with flush mounted bottom valve, 5-neck head, polytetrafluoroethylene gasket, clamp, and stirrer components (bearing, shaft, and paddle). The necks were equipped as follows: stirrer components were put on the center neck, and the outer necks had a reflux condenser topped with gas inlet/outlet, an inlet for solvent, a thermocouple, and a stopper. Dry, deoxygenated dimethoxyethane (DME) was added to the flask (approx. 5 L). In the drybox, 700 g of TiC13 was weighed into an equalizing powder addition funnel; the funnel was capped, removed from the drybox, and put on the reaction kettle in place of the stopper. The TiC13 was added over 10 minutes with stirring. After the addition was completed, additional DME was used to wash the rest of the TiC13 into the flask. The addition funnel was replaced with a stopper, and the mixture heated to reflux. The color changed from purple to pale blue. The mixture was heated for 5 hours, cooled to room temperature, the solid was allowed to settle, and the supernatant was decanted from the solid. The TiC13(DME) 5 was left in R- 1 as a pale blue solid.

Part 2: Preparation of r(Me4Cs)SiMeN-t-BulrMgCllv The apparatus (referred to as R-2) was set-up as described for R-1, except that flask size was 30 L.

The head was equipped with seven necks; stirrer in the center neck, and the outer necks containing condenser topped with nitrogen inlet/outlet, vacuum adapter, reagent addition tube, thermocouple, and stoppers. The flask was loaded with 4.5 L of toluene, 1.14 kg of(Me4C5H)SiMe2NH-t-Bu, and 3.46 kg of 2 M i-PrMgCl in Et2O. The mixture was then heated, and the ether allowed to boil off into a trap cooled to -78 OC. After four hours, the temperature of the mixture had reached 75 °C. At the end of this time, the heater was turned off and DME was added to the hot, stirring solution, resulting in the formation of a white solid. The solution was allowed to cool to room temperature, the material was allowed to settle, and the supernatant was decanted from the solid. The [(Me4C5)SiMe2N-t-Bu][MgCl]2 was left in R-2 as an off- white solid.

Part 3: Preparation of l(n -Me4~)SiMesN-t-BulTiMev The materials in R-1 and R-2 were slurried in DME (3 L of DME in R-l and 5 L in R-2). The contents of R- 1 were transferred to R-2 using a transfer tube connected to the bottom valve of the 10 L flask and one of the head openings in the 30 L flask. The remaining material in R-l was washed over using additional DME. The mixture darkened quickly to a deep red/brown color, and the temperature in R-2 rose from 21 °C to 32 °C. After 20 minutes, 160 mL of CH2C12 was added through a dropping funnel, resulting in a color change to green/brown. This was followed by the addition of 3.46 kg of 3 M MeMgCl in THF, which caused a temperature increase from 22 °C to 52 °C. The mixture was stirred for 30 minutes, then 6 L of solvent was removed under vacuum. Isopar E (6 L) was added to the flask. This vacuum/solvent addition cycle was repeated, with 4 L of solvent removed and 5 L of Isopar E added. In the final vacuum step, an additional 1.2 L of solvent was removed. The material was allowed to settle overnight, then the liquid layer decanted into another 30 L glass kettle (R-3). The solvent in R-3 was removed under vacuum to leave a brown solid, which was re-extracted with Isopar E; this material was transferred into a storage cylinder. Analysis indicated that the solution (17.23 L) was 0.1534 M in titanium; this is equal to 2.644 moles of [(#5-Me4C5)SiMe2N-t-Bu]TiMe2. The remaining solids in R-2 were further extracted with Isopar E, the solution was transferred to R-3, then dried under vacuum and re-extracted with Isopar E. This solution was transferred to storage bottles; analysis indicated a concentration of 0.1403 M titanium and a volume of 4.3 L (0.6032 moles [(#5-Me4C5)SiMe2N-t-Bu]TiMe2). This gives an overall yield of 3.2469 moles of [(#5-Me4C5]SiMe2N-t-Bu]TiMe2, or 1063 g. This is a 72 percent yield overall based on the titanium added as TiC13.

Catalyst Preparation Two Part 1: Preparation of TiCl3 (DME) 1.5 The apparatus (referred to as R-1) was set-up in the hood and purged with nitrogen; it consisted of a 10 L glass kettle with flush mounted bottom valve, 5-neck head, polytetrafluoroethylene gasket, clamp, and stirrer components (bearing, shaft, and paddle). The necks were equipped as follows: stirrer components were put on the center neck, and the outer necks had a reflux condenser topped with gas inlet/outlet, an inlet for solvent, a thermocouple, and a stopper. Dry, deoxygenated dimethoxyethane (DME) was added to the flask (approximately 5.2 L). In the drybox, 300 g of TiC13 was weighed into an equalizing powder addition funnel; the funnel was capped, removed from the drybox, and put on the reaction kettle in place of the stopper. The TiC13 was added over 10 minutes with stirring. After the addition was completed, additional DME was used to wash the rest of the TiC13 into the flask. This process was then repeated with 325 g of additional TiC13, giving a total of 625 g. The addition funnel was replaced with a stopper, and the mixture heated to reflux. The color changed from purple to pale blue. The mixture was heated for 5 hours, cooled to room temperature, the solid was allowed to settle, and the supernatant was decanted from the solid. The TiC13(DME)1 5 was left in R-1 as a pale blue solid.

Part 2: Preparation of r(MeaCg)SiMe3N-t-Bul TMlzC112 The apparatus (referred to as R-2) was set-up as described for R-1, except that flask size was 30 L.

The head was equipped with seven necks; stirrer in the center neck, and the outer necks containing condenser topped with nitrogen inlet/outlet, vacuum adapter, reagent addition tube, thermocouple, and stoppers. The flask was loaded with 7 L of toluene, 3.09 kg of 2.17 M i-PrMgC1 in Et2O, 250 mL of THF, and 1.03 kg of (Me4CsH)SiMe2NH-t-Bu. The mixture was then heated, and the ether allowed to boil off into a trap cooled to -78 "C. After three hours, the temperature of the mixture had reached 80 "C, at which time a white precipitate formed. The temperature was then increased to 90 OC over 30 minutes and held at this temperature for 2 hours. At the end of this time, the heater was turned off, and 2 L of DME was added to the hot, stirring solution, resulting in the formation of additional precipitate. The solution was allowed to cool to room temperature, the material was allowed to settle, and the supernatant was decanted from the solid. An additional wash was done by adding toluene, stirring for several minutes, allowing the solids to settle, and decanting the toluene solution. The [(Me4Cs)SiMe2N-t-Bu][MgCI]2 was left in R-2 as an off- white solid.

Part 3: Preparation of [(#5-Me4C5]SiMe2N-t-Bu]Ti(#4-1,3-pentadiene) The materials in R-1 and R-2 were slurried in DME (the total volumes of the mixtures were approx. 5 L in R-1 and 12 L in R-2). The contents of R-l were transferred to R-2 using a transfer tube connected to the bottom valve of the 10 L flask and one of the head openings in the 30 L flask. The remaining material in R-1 was washed over using additional DME. The mixture darkened quickly to a deep

red/brown color. After 15 minutes, 1050 mL of 1,3-pentadiene and 2.60 kg of 2.03 M n-BuMgC1 in THF were added simultaneously. The maximum temperature reached in the flask during this addition was 53 "C.

The mixture was stirred for 2 hours, then approx. 11 L of solvent was removed under vacuum. Hexane was then added to the flask to a total volume of 22 L. The material was allowed to settle, and the liquid layer (12 L) was decanted into another 30 L glass kettle (R-3). An additional 15 liters of product solution was collected by adding hexane to R-2, stirring for 50 minutes, again allowing to settle, and decanting. This material was combined with the first extract in R-3. The solvent in R-3 was removed under vacuum to leave a red/black solid, which was then extracted with toluene. This material was transferred into a storage cylinder. Analysis indicated that the solution (11.75 L) was 0.255 M in titanium; this is equal to 3.0 moles of [(n5-Me4Cs)SiMe2N-t-Bu]Ti(P4-1,3-pentadiene) or 1095 g. This is a 74 percent yield based on the titanium added as TiC13.

Preparation of Polymers A-E Polymer A was produced in accordance with the procedure of U.S. 5,272,236 and 5,278,272. The polymer products of Examples B-E (the polymer components, in the case of Polymer D, which was a melt blend of two polymer components), were prepared in a solution polymerization process using ISOPAR E as a solvent, using ethylene and octene as comonomers, and using the reactor conditions indicated in the following Table Four. In Example A, the catalyst employed was that of Catalyst Description One, while in each of Examples B-E, the catalyst employed was the catalyst of Catalyst Description Two. In each of preparations A-E, the cocatalyst was tris(pentafluorophenyl)borane, available as a 3 weight percent solution in IsoparTM~E mixed hydrocarbon, from Boulder Scientific, and aluminum was provided in the form of a solution of modified methylalumoxane (MMAO Type 3A) in heptane, which is available at a 2 weight percent aluminum concentration from Akzo Nobel Chemical Inc. Each of Examples B-E utilized 35 ppm deionized water as a catalyst kill.

In the case of Polymer B, the octene flow was 2.3 lbs/hr (5.06 kg/hr), the hydrogen flow was 60 SCCM, and the solvent flow was 19.06 Ibs/hr (41.93 kg/hr).

Table Four B C D (First D (Second Component)* Component)* Ethylene feed 44.4 47.6 45.4 47.6 (kg/hr) Comonomer: olefin ratio 21 19.5 18.1 (mole percent) Hydrogen: ethylene ratio 0.182 0.061 0.443 (mole percent) Diluent: ethylene ratio 6 6 6 (weight basis) Catalyst metal concentration (ppm) 4 40 70 66 Catalyst flow rate 0.713 kg/hr 1.12 0.318 0.585 (kg/hr) Co-catalyst concentration (ppm) 87.9 3000 2070 1990 Co-catalyst flow rate (kg/hr) 1.04 kg/hr 0.561 0.342 0.827 Aluminum concentration (ppm) 9.77 400 215 1-70 Aluminum flow rate (kg/hr) 0.99 kg/hr 0.318 0.290 0.826 Reactor temperature ("C) 110.4 120 91 120 Reactor pressure (MPa) 3.3 3.7 3.7 3.7 Ethylene concentration in reactor 1.68 1.22 1.45 exit stream (weight percent) Polymer density (g/cm ) 0.890 0.8721 0.8620 0.8789 Polymer melt viscosity at 3500F 4900 50,448 746,660 8,177 (1 770C) (centipoise) Polymer melt index 1600 200 9.7 1000 (12 at 1900C) Polymer Mw 31200 70900 18000 Polymer Mn 17300 35800 10000 Polymer Mw/Mn 1.803 1.98 1.88

* Polymer D is a melt blend formed from 50 weight percent of each of the first and second components identified.

Preparation of Polymers A1-R1 The polymer products of Examples Al - R1 are produced in a solution polymerization process using a continuously stirred reactor. Additives (for example, antioxidants, pigments, etc.) can be incorporated into the interpolymer products either during the pelletization step or after manufacture, with a subsequent re-extrusion. Examples Al-Il were each stabilized with 1250 ppm calcium stearate, 500 ppm IrganoxTM 1076 hindered polyphenol stabilizer (available from Ciba-Geigy Corporation), and 800 ppm PEPQ (tetrakis(2,4-di-t-butylphenyl)-4,4'-biphenylene diphosphonite) (available from Clariant Corporation). Examples J1-R1 were each stabilized with 500 ppm IrganoxTM 1076, 800 ppm PEPQ, and 100 ppm water (as a catalyst kill agent).

The ethylene and the hydrogen were combined into one stream before being introduced into the diluent mixture, a mixture of C8-C10 saturated hydrocarbons, for example, Isopar-E hydrocarbon mixture (available from Exxon Chemical Company) and the comonomer. In Examples A l-O1 the comonomer was 1-octene; in Examples Q1 and R1, the comonomer was 1-butene; and Example P1 had no comonomer. The reactor feed mixture was continuously injected into the reactor.

The metal complex and cocatalysts were combined into a single stream and were also continuously injected into the reactor. For Examples Al-Il, the catalyst was as prepared in Catalyst Description One set forth above. For Examples J1-R1, the catalyst was as prepared in Catalyst Description Two set forth above.

For Examples Al -Rl, the co-catalyst was tris(pentafluorophenyl)borane, available as a 3 weight percent solution in IsoparTM.E mixed hydrocarbon, from Boulder Scientific. Aluminum was provided in the form of a solution of modified methylalumoxane (MMAO Type 3A) in heptane, which is available at a 2 weight percent aluminum concentration from Akzo Nobel Chemical Inc.

Sufficient residence time was allowed for the metal complex and cocatalyst to react prior to introduction into the polymerization reactor. For the polymerization reactions of Examples A1-R1, the reactor pressure was held constant at 475 psig (3380 kPa). Ethylene content of the reactor, in each of Examples Al -Rl, after reaching steady state, was maintained at the conditions specified in Table Five.

After polymerization, the reactor exit stream is introduced into a separator where the molten polymer is separated from the unreacted comonomer(s), unreacted ethylene, unreacted hydrogen, and diluent mixture stream. The molten polymer is subsequently strand chopped or pelletized, and, after being cooled in a water bath or pelletizer, the solid pellets are collected. Table Five describes the polymerization conditions and the resultant polymer properties.

TABLE FIVE A1 B1 C1 D1 E1 F1 G1 H1 I1 J1 Ethylene feed (lb/hr) 2.0 2.0 2.0 2.0 2.0 2.0 3.0 3.0 3.0 3.0 (kg/hr) (0.91) (0.91) (0.91) (0.91) (0.91) (0.91) (1.4) (1.4) (1.4) (1.4) Comonomer: olefin ratio 18.00 18.10 12.40 12.50 12.50 8.50 4.40 0.40 0.40 11.80 (mole percent) Hydrogen: ethylene ratio 0.00 1.22 0.26 0.48 1.26 0.66 0.68 0.72 1.60 0.34 (mole percent) Diluent: ethylene ratio 10.20 9.80 10.60 11.10 11.10 9.30 5.90 5.90 5.90 9.99 (weight basis) Catalyst metal concentration (ppm) 4 4 4 4 4 2 5 5 5 3 Catalyst flow rate (lb/hr) 0.280 0.313 0.272 0.316 0.428 0.386 0.417 0.441 0.626 0.449 (kg/hr) (0.127) (0.142) (0.123) (0.143) (0.194) (0.175) (0.189) (0.200) (0.284) (0.203) Co-catalyst concentration (ppm) 88 88 88 88 88 44 353 353 353 88 Co-catalyst flow rate (lb/hr) (kg/hr) 0.408 0.455 0.396 0.460 0.624 0.561 0.190 0.200 0.284 0.490 (0.185) (0.206) (0.180) (0.209) (0.283) (0.254) (0.086) (0.091) (0.129) (0.222) Aluminum concentration (ppm) 10 10 10 10 10 5 20 20 20 9.8 Aluminum flow rate (lb/hr) 0.385 0.431 0.375 0.438 0.590 0.528 0.357 0.376 0.534 0.461 (kg/hr) (0.174) (0.196) (0.170) (0.199) (0.268) (0.240) (0.162) (0.171) (0.242) (0.209) Reactor temperature (°C) 110 110 110 110 110 110 140 140 140 110 TABLE FIVE CONTINUED A1 B1 C1 D1 E1 F1 G1 H1 I1 J1 Ethylene concentration in reactor exit 2.17 2.48 1.80 1.69 1.65 2.99 4.44 4.14 4.41 1.75 stream (weight percent) Polymer density (g/cm3) 0.858 0.855 0.875 0.871 0.870 0.897 0.929 0.963 0.968 0.872 Polymer melt viscosity at 350°F 309000* 350 39000* 4200 355 5200 5600 5200 395 15,000 (centipoise) Polymer melt index 32 16200* 246 1800* 16000* 1500* 1400* 1500* 14500* 583* (I2 at 190°C) Polymer Mw 60,400 8,700 30,100 16,500 7,900 15,600 15,800 15,800 7,300 23,200 Polymer Mn 29,100 4,600 17,100 9,100 4,300 8,700 8,900 8,000 3,700 11,900 Polymer Mw/Mn 2.08 1.89 1.76 1.81 1.84 1.79 1.78 1.98 1.97 1.95 Peak crystallization temperature byDSC 23.73 27.13 55.73 55.44 59.05 78.57 102.76 116.01 114.76 55.73 (°C) Peak melting temperature by DSC 45.63 57 68 67 67 91.04 112.22 129.23 127.6 68 (°C) Total percent crystallinity by DSC 7.46 9.98 18.94 17.78 19.55 36.3 38.42 76.03 79.62 18.94 TABLE FIVE CONTINUED K1 L1 M1 N1 O1 P1 Q1 R1 Ethylene feed (lb/hr) 3.0 3.0 3.0 3.0 3.0 3.0 3. 3.0 (kg/hr) (1.4) (1.4) (1.4) (1.4) (1.4) (1.4) (1.4) (1.4) Comonomer : olefin ratio 9.10 7.40 7.40 7.30 1.24 0.00 17.10 12.70 (mole percent) Hydrogen : ethylene ratio 0.54 0.42 0.56 0.76 2.14 2.14 0.54 0.62 (mole percent) Diluent : ethylene ratio 9.99 8.59 8.59 8.59 7.69 7.70 9.99 9.00 (weight basis) Catalyst metal concentration (ppm) 3 3 3 3 32 32 8 8 Catalyst flow rate (lb/hr) 0.450 0.466 0.555 0.713 0.304 0.294 0.392 0.207 (kg/hr) (0.204) (0.211) (0.252) (0.323) (0.138) (0.133) (0.178) (0.094) Co-catalyst concentration (ppm) 88 88 88 88 1430 1430 353 353 Co-catalyst flow rate (lb/hr) 0.490 0.500 0.605 0.777 0.219 0.211 0.278 0.150 (kg/hr) (0.222) (0.227) (0.274) (0.352) (0.099) (0.096) (0.126) (0.068) TABLE FIVE CONTINUED K1 L1 M1 N1 O1 P1 Q1 R1 Aluminum concentration (ppm) 9.8 9.8 9.8 9.8 120.0 120.0 39.8 39.8 Aluminum flow rate (lb/hr) 0.468 0.480 0.574 0.731 0.323 0.311 0.260 0.141 (kg/hr) (0.212) (0.218) (0.260) (0.332) (0.147) (0.141) (0.118) (0.064) Reactor temperature (°C) 110 120 110 110 110 110 110 110 Ethylene concentration in reactor 1.71 1.41 2.17 2.48 1.80 1.69 1.65 2.99 exit stream (weight percent) Polymer density (g/cm3) 0.883 0.898 0.897 0.894 0.948 0.960 0.868 0.887 Polymer melt viscosity at 350°F 5000 15,000 5200 2500 350 512 5290 5000 (centipoise) Polymer melt index 1500* 580* 1500* 2900* 16000* 11600* (I2 at 190°C (g/10 min.)) Polymer Mw 16,200 20,300 16,100 12,000 6,900 7,400 Polymer Mn 8,200 10,400 8,900 5,800 3,200 3,200 Polymer Mw/Mn 1.98 1.95 1.81 2.07 2.16 2.31 Peak crystallization temperature by 69.27 79.85 78.57 81.22 109.88 116.39 47.15 65.65 DSC (°C) Peak melting temperature by DSC 81.97 92.62 91.04 92.43 120.5 131.11 55 78.06 (°C) Total percent crystallinity by DSC 28.18 36.76 36.3 37.81 72.81 72.84 13.06 26.39 *Calculated on the basis of melt viscosity correlations in accordance with the formula:<BR> I2 = 3.6126(10 log(#)-6.6928)/-1.1363)-9.3185,<BR> where #=melt viscosity at 350°F (177°C)

The polymer products of Examples S1, T1, and Ul were produced in a solution polymerization process using a well-mixed recirculating loop reactor. Each polymer was stabilized with 2000 ppm IRGANOXTM 1076 hindered polyphenol stabilizer (available from Ciba-Geigy Corporation) and 35 ppm deionized water (as a catalyst kill agent).

The ethylene and the hydrogen (as well as any ethylene and hydrogen which were recycled from the separator, were combined into one stream before being introduced into the diluent mixture, a mixture of Cg-C1o saturated hydrocarbons, for example, ISOPARTM-E (available from Exxon Chemical Company) and the comonomer 1-octene.

The metal complex and cocatalysts were combined into a single stream and were also continuously injected into the reactor. The catalyst was as prepared in Catalyst Description Two set forth above; the primary cocatalyst was tri(pentafluorophenyl)borane, available from Boulder Scientific as a 3 weight percent solution in ISOPAR-E mixed hydrocarbon; and the secondary cocatalyst was modified methylalumoxane (MMAO Type 3A), available from Akzo Nobel Chemical Inc. as a solution in heptane having 2 weight percent aluminum.

Sufficient residence time was allowed for the metal complex and cocatalyst to react prior to introduction into the polymerization reactor. The reactor pressure was held constant at 475 psig (3380 kPa).

After polymerization, the reactor exit stream was introduced into a separator where the molten polymer was separated from the unreacted comonomer(s), unreacted ethylene, unreacted hydrogen, and diluent mixture stream, which was in turn recycled for combination with fresh comonomer, ethylene, hydrogen, and diluent, for introduction into the reactor. The molten polymer was subsequently strand chopped or pelletized, and, after being cooled in a water bath or pelletizer, the solid pellets were collected.

Table Six describes the polymerization conditions and the resultant polymer properties. TABLE SIX S1 T1 U1 Ethylene fresh feed rate (Ibs/hr) 140 140 140 (kg/hr) (63.5) (63.5) (63.5) Total ethylene feed rate (Ibs/hr) 146.2 146.17 146.5 (kg/hr) (66.32) (66.30) (66.45) Fresh octene feed rate (lbs/hr) 45.4 49.5 12.67 (kg/hr) (20.6) (22.4) (5.75) Total octene feed rate (Ibs/hr) Not determined 112 32.9 (kg/hr) (50.8) (14.9) Total octene concentration (weight percent) Not determined 11.4 3.36 Fresh hydrogen feed rate (standard cmj/min) 4025 5350 16100 Solvent and octene feed rate (Ibs/hr) 840 839.4 840 (kg/hr) (381) (380.8) (381) Ethylene conversion rate (wt percent) 90.7 90.3 88.26 Reactor temperature (°C) 109.86 119.8 134.3 Feed temperature (°C) 15 15 15.3 Catalyst concentration (ppm) 70 70 70 Catalyst flow rate (Ibs/hr) 0.725 1.265 4.6 (kg/hr) (0.329) (0.5738) (2.1) Primary cocatalyst concentration (ppm) 1200 2031 1998 Primary cocatalyst flow rate (Ibs/hr) 2.96 1.635 5.86 (kg/hr) (1.34) (0.7416) (2.66) Primary cocatalyst to catalyst molar ratio (B:Ti) 2.96 3.48 2.897 Secondary cocatalyst concentration (ppm) 198 198 198 Secondary cocatalyst flow rate (Ibs/hr) 0.718 1.258 3.7 (kg/hr) (0.326) (0.571) (1.7) Secondary cocatalyst to catalyst molar ratio (Al:Ti) 5 4.986 4.037 Product density (g/cmj) 0.8926 0.8925 0.9369 Product melt viscosity at 3500F (centipoise) 12,500 4,000 400 Polymer melt index (12 at 1900C)* 686* 1,900* 14,000* Polymer Mn 12,300* 8,900* 4,700* * Calculated on the basis of melt viscosity correlations in accordance with the formulas: 12 = 3.6126(10 log(rl)-6.6928)l-l.l363) 9 9.3185, Mn = lO[(logrl + 10.46)/3.56)] where TI = melt viscosity at 350°F (177°C).

Except as noted, Examples V1, W1, and Xl were prepared in accordance with the procedure set forth above with respect to Examples Al - Rl. In particular, Examples Vl and Wl were prepared using a catalyst prepared in accordance with Catalyst Procedure 2. The additives employed were 1000 ppm Irganox TM 1076 hindered polyphenol stabilizer (available from Ciba-Giegy Corporation) and 100 ppm water. In the case of Example Wi, ethylbenzene, rather than IsoparTM E mixed hydrocarbon, was utilized as the solvent.

Example Xl was prepared using a catalyst prepared in accordance with Catalyst Procedure 1. The additives employed were 1250 ppm calcium stearate, 500 ppm IrganoxTM 1076 hindered polyphenol stabilizer (available from Ciba-Giegy Corporation), and 800 ppm PEPQ (tetrakis(2,4-di-t-butylphenyl)-4,4'- biphenylene diphosphonite) (available from Clariant Corporation).

The run conditions employed and a description of the resultant polymers is set forth in the following Table Seven: TABLE SEVEN Vl Wl Xl Ethylene fresh feed rate (Ibs/hr) 2.5 3.5 3.02 (kg/hr) (1.1) (1.6) (1.37) Total ethylene feed rate (Ibs/hr) 2.5 3.5 3.02 (kg/hr) (1.1) (1.6) (1.37) Fresh octene feed rate (Ibs/hr) 1.9 1.52 1.1 (kg/hr) (0.86) (0.689) (0.50) Total octene feed rate (Ibs/hr) 1.9 1.52 1.1 Total octene concentration (weight percent) 11.44 6.47 5.52 Fresh hydrogen feed rate (standard cm3/min) 199.9 292.4 124.9 Solvent and octene feed rate (Ibs/hr) 14.1 20.04 16.9 (kg/hr) (6.40) (9.253) (7.66) Ethylene conversion rate (wt percent) 75.2 85.5 69.3 Reactor temperature (OC) 119.8 136.3 140.4 Feed temperature (OC) 26.9 33.93 40 Catalyst concentration (ppm) 12 2.4 5 Catalyst flow rate (Ibs/hr) 0.4543 0.60717 0.4174 (kg/hr) (0.2061) (0.27541) (0.1893) Primary cocatalyst concentration (ppm) 92 92 393 Primary cocatalyst flow rate (Ibs/hr) 0.67 0.3664 0.18967 (kg/hr) (0.30) (0.1662) (0.08603) Primary cocatalyst to catalyst molar ratio (B:Ti) - 2.16 3.3 Secondary cocatalyst concentration (ppm) - 21.74 19.78 Secondary cocatalyst flow rate (Ibs/hr) - 0.302 0.3569 (kg/hr) (0.137) (0.1619) Secondary cocatalyst to catalyst molar ratio 8 6 (Al:Ti) Product density (g/cm3) 0.890 0.930 0.920 Product melt viscosity at 3500F (1770C) 350 400 5620 (centipoise) Polymer melt index (I2 at 1900C)* 16,000 14,000 1400 Polymer Mn* 4500 4700 9800

* Calculated on the basis of melt viscosity correlations in accordance with the formulas: 12 = 3.6126(10 log(r1)-6.6928) /-1.1363) - 9.3185, Mn = 10[(log# + 10.46)/3.56)] where TI melt viscosity at 3500F (1770C).

To a 4 liter autoclave stirred reactor, 865.9 g of ISOPARTME hydrocarbon (available from Exxon Chemical Company) and 800.4 g l-octene were charged. The reactor was heated to 1200C and hydrogen was added from a 75 cc cylinder. Hydrogen was added to cause a 250 psig (1800 kPa) pressure drop in the cylinder. The reactor was then pressurized to 450 psig (3200 kPa) of ethylene. Catalyst was added at the rate of 1 cc/min. The catalyst was as prepared in the Catalyst One Preparation set forth above and was mixed with other co-catalysts at a ratio of 1.5 mL of a 0.005 M of Catalyst Preparation One, 1.5 mL of a

0.015 M solution of tris(pentafluorophenyl) borane in ISOPAR-E hydrocarbon mixture (a 3 wt percent solution of tris(pentafluorophenyl)borane in ISOPAR-E hydrocarbon mixture is available from Boulder Scientific), 1.5 mL of a 0.05 M solution of modified methylalumoxane in ISOPAR-E hydrocarbon mixture (MMAO Type 3A) (a solution of MMAO Type 3A in heptane with a 2 wt percent aluminum content is available from Akzo Nobel Chemical Inc.), and 19.5 mL of ISOPAR-E hydrocarbon mixture. Ethylene was supplied on demand. The reactor temperature and pressure were set at 1200C and 450 psig (3200 kPa), respectively. The reaction continued for 23.1 minutes. At this time, the agitation was stopped and the reactor contents transferred to a glass collection kettle. The reactor product was dried in a vacuum oven overnight.

The ethylene/octene product thus prepared had a density of 0.867 g/cm3, and an I2 at 1 900C of 842 g/10 min.