Producing blown film and blends from bimodal high density high molecular weight film resin using magnesium oxide-supported Ziegler catalyst

A blend for blown film which exhibits improved MD/TD tear balance. The blend is a bimodal molecular weight ethylene resin containing two fractions of different molecular weight. The weight fraction of a higher molecular weight component of the blend is about 0.35 to 0.75.

FIELD OF THE INVENTION 
This invention relates to the production of film grade polyethylene, 
processable in high stalk extrusion. The resins are high density 
polyethylene (HDPE) produced in a process which relies upon a particular 
catalyst. The high density polyethylene is a bimodal ethylene polymer 
composition comprising a mixture of relatively high and relatively lower 
molecular weight polymers blended together which exhibits optimal MD/TD 
balance. 
Preferably, the resins are produced in a gas-phase, fluidized bed 
polymerization in a multi stage process wherein the blending occurs in 
situ. 
BACKGROUND OF THE INVENTION 
High density polyethylene (HDPE) is one of the most versatile of the 
thermoplastic resins and offers a broad spectrum of uses. The properties 
of finished goods made from HDPE are strongly influenced by the 
polymerization and processing conditions and the properties of the polymer 
and the resin. 
Physical and mechanical properties of Ziegler HDPE can be summarized as 
follows: low to medium stiffness and hardness; medium to extremely high 
toughness; no reduction in toughness to -40.degree. C.; unrestricted usage 
in contact with food; no restriction for disposal, burning, or recycling; 
high resistance against solvents and chemicals at ambient temperature; and 
easy and safe to process. 
Molecular weights of polyethylenes are customarily evaluated by measuring 
their melt indexes in accordance with ASTM D-1238. Three melt indexes are 
cited below, those measured with the weights of 21.6 kg (I.sub.21 or 
high-load melt index, HLMI), 5.0 kg (I.sub.5) and 2.16 kg (I.sub.2 or melt 
index, MI). All these numbers vary inversely with resins' molecular 
weight. 
Strength, as well as impact, stress and puncture resistance, together with 
toughness, are attributed to high molecular weight resins. 
However, as the molecular weight of the resin increases, the 
processabiliity of the resin usually does decrease. By providing a blend 
of polymers, the properties characteristic of high molecular weight resins 
can be retained and processability, particularly extrudability, can be 
improved. 
Various approaches have been examined for production of such blends. 
Physical blending suffers the disadvantage brought on by the requirement 
of complete homogenization and attendant high cost. Direct synthesis with 
one catalyst, although theoretically possible and most desirable, is 
difficult to achieve. The third strategy is a multi-stage polymerization 
which involves different staging of variables, usually in multi reactor 
set ups, sometimes referred to as tandem, which provide the possibility of 
diversity in molecular weight. The products exhibit good ESCR and 
stiffness. 
However, the tandem produced products have not received universal domestic 
market acceptance because the tandem produced products exhibit different 
swell and melt fracture characteristics from the Phillips type resins, 
requiring downstream equipment modification, with high attendant costs. 
In accordance with the invention, it is an object to provide bimodal film 
with the desired physical properties of the tandem products but with 
improved bubble stability and film MD and TD tear properties. 
SUMMARY OF THE INVENTION 
The invention relates to blends exhibiting excellent bubble stability and a 
good balance in the MD and TD tear properties. The invention relates to 
blends which exhibit excellent bubble stability in high stalk extrusion. 
The invention relates to forming a bimodal MWD blend of a high HLMI 
ethylene resin containing catalyst particles and/or residues of said 
catalyst particles, with a low molecular weight ethylene polymer or 
copolymer. The high HLMI resin is formed in the presence of an MgO 
containing catalyst defined below, which produces a high molecular weight 
component with a high MFR, which is characteristic of broad molecular 
weight distribution. MFR is the ratio, HLMI/MI. 
The bimodal MWD (molecular weight distribution) resin blends can be 
prepared by using a family of magnesium-oxide-supported Ziegler catalyst 
modified with aliphatic acid and high alkanol, as described in U.S. Pat. 
No. 4,863,886, which is relied upon and incorporated by reference herein. 
These catalysts are useful for preparing the relatively higher molecular 
weight component of the bimodal blend for ultimate application in high 
density high molecular weight film applications. These catalysts produce 
high molecular weight components of broad molecular weight distribution 
and higher activity under high H.sub.2 /C.sub.2 ratios. The catalysts had 
the advantage of requiring higher hydrogen to ethylene ratios of about 
0.067 in the first stage of the gas-phase tandem process to give 0.41 HLMI 
(MI.sub.21) resin. The tolerance for the higher hydrogen/ethylene ratios 
can facilitate control of the HLMI of the first stage reactor product in 
tandem process in which the relatively higher molecular weight component 
is produced in a first gas phase in a first fluid bed reactor and then 
transferred to a second fluid bed reactor for production of the relatively 
lower molecular weight component to produce a bimodal blend. 
Preferably, formation of the low molecular weight polymer or copolymer is 
by in situ polymerization of the low molecular weight component in the 
presence of the HLMI component containing an active MgO catalyst. The 
blending can be undertaken by a process including the steps of 
polymerizing gaseous monomeric compositions comprising a major proportion 
of ethylene in at least two gas phase, under the following conditions. In 
the first stage, a gas comprising monomeric composition and, optionally, a 
small amount of hydrogen, is contacted under polymerization conditions 
with the MgO containing catalyst comprising a transition metal compound 
component and a reducing agent (cocatalyst) such as an organometallic 
compound or metal hydride as cocatalyst, at a hydrogen/ethylene molar 
ratio of no higher than about 0.3 and an ethylene partial pressure no 
higher than about 100 psia such as to produce a relatively high molecular 
weight (HMW) polymer powder wherein the polymer is deposited on the 
catalyst particles. The HMW polymer powder containing the catalyst is then 
subjected to a second stage with, optionally, additional cocatalyst which 
may be the same or different from the cocatalyst utilized in the first 
stage, together with a gaseous mixture comprising hydrogen and monomeric 
composition wherein additional polymerization is carried out at a 
hydrogen/ethylene molar ratio of at least about 0.9, the ratio being 
sufficiently high such that it is at least about 8.0 times that in the 
first reactor, and an ethylene partial pressure at least 1.7 times that in 
the first reactor, to produce a relatively low molecular weight (LMW) 
polymer much of which is deposited on and within the HMW polymer/catalyst 
particles from the first, such that the fraction of HMW polymer in the 
bimodal polymer leaving the second reactor is at least about 0.35. 
The foregoing conditions provide for a process wherein the production of 
fines (polymer particles) tending to foul compressors and other equipment 
is kept to a relatively low level. Moreover, such conditions provide for 
an inhibited level of productivity in the first reactor with a resulting 
increased level of productivity in the second reactor to produce a bimodal 
polymer blend having a favorable melt flow ratio (MFR, an indication of 
molecular weight distribution) and a high degree of homogeneity (indicated 
by low level of gels and low heterogeneity index) caused by a substantial 
degree of blending of HMW and LMW polymer in each final polymer particle 
inherently resulting from the process operation. The bimodal blend is 
capable of being processed without undue difficulty into films and 
containers for household industrial chemicals having a superior 
combination of mechanical properties.

DETAILED DESCRIPTION OF THE INVENTION 
The gaseous monomer entering both reactors may consist wholly of ethylene 
or may comprise a preponderance of ethylene and a minor amount of a 
comonomer such as a 1-olefin containing 4 to about 10 carbon atoms. 
Comonomeric 1-olefins which may be employed are, for example, 1-butene, 
1-pentene, 1-hexene, 4-methyl-1-pentene, 1-octene, 1-decene, and mixtures 
thereof. The comonomer may be present in the monomeric compositions 
entering either or both reactors. 
In many cases, the monomer composition will not be the same in both 
reactors. For example, in making resin intended for high density film, it 
is preferred that the monomer entering the first reactor contain a minor 
amount of comonomer such as 1-hexene so that the HMW component of the 
bimodal product is a copolymer, whereas the monomer fed to the second 
reactor consists essentially of ethylene so that the LMW component of the 
product is substantially an ethylene homopolymer. When a comonomer is 
employed so as to obtain a desired copolymer in either or both reactors, 
the molar ratio of comonomer to ethylene may be in the range, for example, 
of about 0.005 to 0.7, preferably about 0.04 to 0.6. 
Hydrogen may or may not be used to modulate the molecular weight of the HMW 
polymer made in the first reactor. Thus, hydrogen may be fed to the first 
reactor such that the molar ratio of hydrogen to ethylene (H.sub.2 
/C.sub.2 ratio) is, for example, up to about 0.3, preferably about 0.005 
to 0.2. In the second reactor it is necessary to produce a LMW polymer 
with a low enough molecular weight and in sufficient quantity so as to 
produce a bimodal resin which can be formed, with a minimum of processing 
difficulties, into end use products such as containers for household 
industrial chemicals having a superior combination of mechanical 
properties. For this purpose, hydrogen is fed to the second reactor with 
the ethylene containing monomer such that the hydrogen to ethylene mole 
ratio in the gas phase is at least about 0.9, preferably in the range of 
about 0.9 to 5.0 and most preferably in the range of about 1.0 to 3.5. 
Moreover, to provide a sufficient difference between the molecular weights 
of the polymers in the first and second reactor so as to obtain a bimodal 
resin product having a wide enough molecular weight distribution necessary 
for the desired levels of processability and mechanical properties, the 
hydrogen to ethylene mole ratios in the two reactors should be such that 
the ratio in the second reactor is at least about 8.0 times the ratio in 
the first reactor, for example in the range 8.0 to 10,000 times such 
ratio, and preferably 10 to 200 times the ratio in the first reactor. 
In accordance with the invention, a catalyst is employed which tolerates 
high hydrogen/ethylene ratios. Accordingly, the process of the invention, 
allowing higher hydrogen/ethylene ratios in the first reactor provides 
greater control of the first stage product HLMI. 
Utilizing the hydrogen to ethylene ratios set out previously to obtain the 
desired molecular weights of the HMW and LMW polymers produced in the 
first and second stages (and/or reactors) respectively tends to result in 
relatively high polymer productivity in the first reactor and relatively 
low productivity in the second reactor. This tends to result in turn in a 
bimodal polymer product containing too little LMW polymer to maintain 
satisfactory processability. For this purpose, the ethylene partial 
pressure employed in the first stage is no higher than about 100 psia, for 
example in the range of about 15 to 100 psia, preferably in the range of 
about 20 to 80 psia and the ethylene partial pressure in the second stage 
is, for example in the range of about 26 to 170 psia, preferably about 70 
to 120 psia, with the ethylene partial pressures in any specific process 
being such that the ratio of ethylene partial pressure in the second to 
that in the first stage is at least about 1.7, preferably about 1.7 to 
7.0, and more preferably about 2.0 to 4.0. 
If desired for any purpose, e g., to control superficial gas velocity or to 
absorb heat of reaction, an inert gas such as nitrogen may also be present 
in one or both reactors in addition to the monomer and hydrogen. Thus the 
total pressure in both stages may be in the range, for example, of about 
100 to 600 psig, preferably about 200 to 350 psig. 
The temperature of polymerization in the first stage may be in the range, 
for example, of about 60.degree. to 130.degree. C., preferably about 
60.degree. to 90.degree., while the temperature in the second stage may be 
in the range, for example, of about 80.degree. to 130.degree. C., 
preferably about 90.degree. to 120.degree. C. For the purpose of 
controlling molecular weight and productivity in both stages, it is 
preferred to increase the temperature in the second stage compared to the 
first stage temperature, preferably by at least about 10.degree. C. 
higher, sometimes by about 30.degree. to 60.degree. C. higher than that in 
the first reactor. 
The residence time of the catalyst in each stage is controlled so that the 
productivity is suppressed in the first stage reactor and enhanced in the 
second stage reactor, consistent with the desired properties of the 
bimodal polymer product. Thus, the residence time may be, for example, 
about 0.5 to 6 hours, preferably about 1 to 3 hours in the first reactor, 
and, for example, about 1 to 12 hours, preferably about 2.5 to 5 hours in 
the second reactor, with the ratio of residence time in the second reactor 
to that in the first reactor being in the range, for example, of about 5 
to 0.7, preferably about 2 to 1. 
The superficial gas velocity through both reactors is in a tandem series 
for conducting the process sufficiently high to disperse effectively the 
heat of reaction so as to prevent the temperature from rising to levels 
which could partially melt the polymer and shut the reactor down, and high 
enough to maintain the integrity of the fluidized beds. Such gas velocity 
is in the range, for example, of about 40 to 120, preferably about 50 to 
90 cm/sec. 
The productivity of the process in the first stage reactor in terms of 
grams of polymer per gram atom of transition metal in the catalyst 
multiplied by 10.sup.6, may be in the range, for example, of about 1.6 to 
16.0, preferably about 3.2 to 9.6; in the second stage, the productivity 
may be in the range, for example, of about 0.6 to 9.6, preferably about 
1.6 to 3.5, and in the overall process, the productivity is in the range, 
for example, of about 2.2 to 25.6, preferably about 4.8 to 16.0. The 
foregoing ranges are based on analysis of residual catalyst metals in the 
resin product. 
The polymer produced in the first stage reactor has a flow index (HLMI, FI 
or I.sub.21, measured at 190.degree. C. in accordance with ASTM D-1238, 
Condition F), for example, of about 0.05 to 5, preferably about 0.1 to 3 
grams/10 min. and a density in the range, for example, of about 0.890 to 
0.960, preferably about 0.900 to 0.940 grams/cc. 
The polymer produced in the second reactor has a melt index (MI or I.sub.2, 
measured at 190.degree. C. in accordance with ASTM D-1238, Condition E) in 
the range, for example, of about 10 to 4000, preferably about 15 to 2000 
grams/10 min. and a density in the range, for example, of about 0.890 to 
0.976, preferably about 0.930 to 0.976 grams/cc. These values are 
calculated based on a single reactor process model using steady state 
process data. 
The final granular bimodal blend will exhibit balanced MD tear and TD tear 
values. 
The final granular bimodal polymer from the second reactor has a weight 
fraction of HMW polymer of at least about 0.35, preferably in the range of 
about 0.35 to 0.75, more preferably about 0.45 to 0.65, a flow index in 
the range, for example, of about 3 to 200, preferably about 6 to 100 
grams/10 min., a melt flow ratio (MFR, calculated as the ratio of flow 
index to melt index) in the range, for example, of about 60 to 250, 
preferably about 80 to 150, a density in the range, for example, of about 
0.89 to 0.965, preferably about 0.910 to 0.960, an average particle size 
(APS) in the range, for example, of about 127 to 1270, preferably about 
380 to 1100 microns, and a fines content (defined as particles which pass 
through a 120 mesh screen) of less than about 10 weight percent, 
preferably less than about 3 weight percent. With regard to fines 
content, it has been found that a very low amount of fines are produced in 
the first (HMW) reactor and that the percentage of fines changes very 
little across the second reactor. This is surprising since a relatively 
large amount of fines are produced when the first or only reactor in a gas 
phase, fluidized bed system is used to produce a relatively low molecular 
weight (LMW) polymer as defined herein. A probable explanation for this is 
that in the process of this invention, the LMW polymer formed in the 
second reactor deposits primarily within the void structure of the HMW 
polymer particles produced in the first reactor, minimizing the formation 
of LMW fines. This is indicated by an increase in settled bulk density 
(SBD) across the second reactor while the APS stays fairly constant. 
When pellets are formed from granular resin which was stabilized and 
compounded with two passes on a Brabender extruder to ensure uniform 
blending, such pellets have a flow index in the range, for example, of 
about 3 to 200, preferably about 6 to 100 grams/10 min., a melt flow 
ratio in the range, for example, of about 60 to 250, preferably about 80 
to 150, and a heterogeneity index (HI, the ratio of the FI's of the 
granular to the pelleted resin) in the range for example of about 1.0 to 
1.5, preferably about 1.0 to 1.3. HI indicates the relative degree of 
inter-particle heterogeneity of the granular resin. 
The catalysts used herein are MgO catalysts treated to contain transition 
metal so that the amount of transition metal ranges from 0.5 to 20, 
preferably 1.0 to 1.6 mmole/gram of catalyst. Preferably, the transition 
metal is titanium. In contrast, silica supported Mg and titanium produce 
products with a FR of about 9.5 to 10.5 at the same flow index range, 
which is too narrow to give acceptable products. These MgO catalysts are 
activated with activators, or cocatalysts comprising trialkylaluminum, 
dialkylaluminum hydrides and dialkylaluminum halides, in each of which the 
alkyl contains 1 to 12 carbon atoms and can be selected from the group 
consisting of methyl, ethyl propyl, isopropyl, butyl, isobutyl, t-butyl, 
pentyl, iso-pentyl (the isoamyl isomers), the hexyl and hexyl isomers, and 
admixtures thereof. The activity of the catalyst may be enhanced by using 
as a cocatalyst diisobutylaluminum hydride (DIBAH) or triisobutylaluminum 
(TIBA) and by feeding isopentane into the first reactor with the catalyst. 
The amount of activator, (cocatalyst) ranges from 0.5 to 2.0, preferably 
1.0 to 1.6, preferably about 1 millimole/gram catalyst. 
The general preparation of these catalysts involves treating MgO support 
with an organic acid, reacting the treated support with Ti tetrahalide 
(e.g. TiCl.sub.4) and pre-reducing the catalyst with an aluminum alkyl. 
Suitable in carrying out the process of this invention are catalysts 
prepared by pre-treating a dried magnesium oxide (MgO) support with an 
organic acid, e.g. 2-ethoxybenzoic acid, and contacting the resulting 
pre-treated support material with a titanium compound which is the 
reaction product of titanium tetrachloride and an alkanol having 5 to 12 
carbon atoms. The initial treatment of the MgO support with organic acid 
is conducted with a molar excess of MgO. Preferably, the ratio of organic 
acid to MgO is from 0.001 to 0.5 most preferably from 0.005 to 0.1. After 
drying, the acid-treated MgO support is again treated in a similar mannner 
with the product of an alkanol or polyhydroxy alkanol having 5 to 12 
carbon atoms in a ratio of about 0.5 to 1.5, preferably about 0.8 to 1.2, 
moles of the alkanol per mole of TiCl.sub.4. The material is then treated 
with a hydrocarbylaluminum, e.g., tri-n-hexylaluminum to obtain the 
supported catalyst, which may be utilized with additional amounts of a 
hydrocarbyl aluminum cocatalyst, e.g., di-n-hexylaluminum hydride, 
(DIBAH), as described previously in connection with the process of this 
invention. The catalysts are described more fully in U.S. Pat. No. 
4,863,886, the entire disclosure of which is incorporated herein by 
reference. 
Another group of catalysts suitable for the process of this invention are 
those prepared by treating a magnesium oxide (MgO) support with an organic 
acid, e.g., 2-ethyoxybenzoic acid, acetic acid, or octanoic acid (caprylic 
acid), reacting the treated support with titanium tetrachloride, and 
pre-reducing the catalyst with an aluminum alkyl, e.g., triethylaluminum, 
tri-n-hexylaluminum, diisobutylaluminum hydride, or trimethylaluminum; the 
amount of this reagent can range from 0.25 to 1 millimole/gram catalyst. 
During polymerization, a cocatalyst is used which may also be an aluminum 
alkyl such as any of those in the foregoing list of pre-reducing agents or 
cocatalysts. Use of these catalysts produces a high molecular weight 
component with broad molecular weight distribution and produces a resin 
which exhibits excellent bubble stability in high stalk extrusion to 
produce blown film. Because of the high activity of the catalyst, it can 
be employed in the first stage with higher hydrogen ethylene ratios than 
actually used heretofore; higher tolerance for hydrogen, allows control of 
HLMI in the first stage product of the process. For example, this catalyst 
allows for hydrogen to ethylene ratios of about 0.067 to give a 0.41 HLMI 
(MI.sub.21) resin. The blends resulting from the catalysis improves the MD 
tear (g/mil) while maintaining TD tear properties. 
An independent catalyst system can be used to make the low molecular weight 
component. One suitable class of catalysts for this purpose, comprises: 
(i) a catalyst precursor complex or mixture of complexes consisting 
essentially of magnesium, titanium, a halogen, and an electron donor; and 
(ii) at least one hydrocarbyl aluminum cocatalyst. 
The titanium based complex or mixture of complexes is exemplified by an 
empirical formula Mg.sub.a Ti(OR).sub.b X.sub.c (ED).sub.d wherein R is an 
aliphatic or aromatic hydrocarbon radical having 1 to 14 carbon atoms or 
COR' wherein R' is an aliphatic or aromatic hydrocarbon radical having 1 
to 14 carbon atoms; each OR group is alike or different; X is Cl, Br, or 
I, or mixtures thereof; ED is an electron donor, which is a liquid Lewis 
base in which the precursors of the titanium based complex are soluble; a 
is 0.5 to 56; b is 0,1, or 2; c is 1 to 116, particularly 2 to 116; and d 
is 2 to 85. 
The titanium compound, which can be used in the above preparations, has the 
formula Ti(OR).sub.a X.sub.b wherein R and X are as defined for component 
(i) above; a is 0, 1 or 2; b is 1 to 4; and a+b is 3 or 4. Suitable 
compounds are TiCl.sub.3, TiCl.sub.4, Ti(OC.sub.6 H.sub.5)Cl.sub.3, 
Ti(OCOCH.sub.3)Cl.sub.3 and Ti(OCOC.sub.6 H.sub.5)Cl.sub.3. 
The magnesium compound has the formula MgX.sub.2 wherein X is as defined 
for component (i) above. Suitable examples are MgCl.sub.2, MgBr.sub.2, and 
MgI.sub.2. Anhydrous MgCl.sub.2 is a preferred compound. About 0.5 to 56, 
and preferably about 1 to 10, moles of the magnesium compound are used per 
mole of titanium compound. 
The electron donor used in the catalyst composition is an organic compound, 
liquid at temperatures in the range of about 0.degree. C. to about 
200.degree. C. It is also known as a Lewis base. The titanium and 
magnesium compounds are both soluble in the electron donor. 
Electron donors can be selected from the group consisting of alkyl esters 
of aliphatic and aromatic carboxylic acids, aliphatic ketones, aliphatic 
amines, aliphatic alcohols, alkyl and cycloalkyl ethers, and mixtures 
thereof, each electron donor having 2 to 20 carbon atoms. Among these 
electron donors, the preferred are alkyl and cycloalkyl ethers having 2 to 
20 carbon atoms; dialkyl, diaryl, and alkyaryl ketones having 3 to 20 
carbon atoms; and alkyl, alkoxy, and alkylalkoxy esters of alkyl and aryl 
carboxylic acids having 2 to 20 carbon atoms. The most preferred electron 
donor is tetrahydrofuran. Other examples of suitable electron donors are 
methyl formate, ethyl acetate, butyl acetate, ethyl ether, dioxane, 
di-n-propyl ether, dibutyl ether, ethyl formate, methyl acetate, ethyl 
anisate, ethylene carbonate, tetrahydropyran, and ethyl propionate. 
The cocatalyst may, for example, have the formula AlR".sub.e X'.sub.f 
H.sub.g wherein X' is Cl or OR"; R" and R" are saturated aliphatic 
hydrocarbon radicals having 1 to 14 carbon atoms and are alike or 
different; f is 0 to 1.5; g is 0 or 1; and e +f+g=3. Examples of suitable 
R, R', R", and R" radicals are: methyl, ethyl, propyl, isopropyl, butyl, 
isobutyl, tert-butyl, pentyl, neopentyl, hexyl, 2-methylpentyl, heptyl, 
octyl, isooctyl, 2-ethyhexyl, 5,5-dimethylhexyl, nonyl, isodecyl, undecyl, 
dodecyl, cyclohexyl, cycloheptyl, and cyclooctyl. Examples of suitable R 
and R' radicals are phenyl, phenethyl, methyloxyphenyl, benzyl, tolyl, 
xylyl, naphthal, and methylnaphthyl. Some examples of useful cocatalyst 
are triisobutylaluminum, trihexyaluminum, di-isobutylaluminum, hydride, 
dihexylaluminum hydride, di-isobutylhexylaluminum, trimethylaluminum, 
triethylaluminum, diethylaluminum chloride, Al.sub.2 (C.sub.2 
H.sub.5).sub.3 Cl.sub.3, and Al(C.sub.2 H.sub.5).sub.2 (OC.sub.2 H.sub.5). 
While it is not necessary to support the complex or catalyst precursors 
mentioned above, supported catalyst precursors do provide superior 
performance and are preferred. Silica is the preferred support. Other 
suitable inorganic oxide supports are aluminum phosphate, alumina, 
silica/alumina mixtures, silica pretreated with an organoaluminum compound 
such as triethyaluminum, and silica modified with diethylzinc, such 
modifier being used in a quantity sufficient to react with the hydroxyl 
groups on the support which otherwise tend to react with and deactivate 
part of the titanium in the catalyst, but not in sufficient quantity to 
function as a cocatalyst. A typical support is a solid, particulate 
material essentially inert to the polymerization. It is used as a dry 
powder having an average particle size of about 10 to 250 microns and 
preferably about 30 to about 100 microns; a surface area of at least about 
3 square meters per gram and preferably at least about 50 square meters 
per gram; and a pore size of at least about 80 Angstroms and preferably at 
least about 100 Angstroms. Generally, the amount of support used is that 
which will provide about 0.01 to about 0.5, and preferably about 0.2 to 
about 0.35 millimole of transition metal per gram of support. Impregnation 
of the abovementioned catalyst precursor into, for example, silica is 
accomplished by mixing the complex and silica gel in the electron donor 
solvent followed by solvent removal under reduced pressure and/or elevated 
temperature. 
Broad, exemplary ranges and preferred ranges of molar ratios of various 
components of the foregoing catalyst systems utilizing titanium/magnesium 
complexes are as follows: 
TABLE I 
______________________________________ 
Broad Exemplary 
Preferred 
Catalyst Components 
Range Range 
______________________________________ 
1. Mg:Ti 0.5:1 to 56:1 1.5:1 to 5:1 
2. Mg:X 0.005:1 to 28:1 
0.075:1 to 1:1 
3. Ti:X 0.01:1 to 0.5:1 
0.05:1 to 0.2:1 
4. Mg:ED 0.005:1 to 28:1 
0.15:1 to 1.25:1 
5. Ti:ED 0.01:1 to 0.5:1 
0.1:1 to 0.25:1 
6. Cocatalyst used as 
0:1 to 50:1 0:1 to 5:1 
Partial Activator:Ti 
7. Total Cocatalyst:Ti 
0.6:1 to 250:1 
11:1 to 105:1 
8. ED:Al 0.05:1 to 25:1 
0.2:1 to 5:1 
______________________________________ 
Specific examples of the described catalysts comprising a 
titanium/magnesium complex, and methods for their preparation are 
disclosed, for example, in U.S. Pat. Nos. 3.989,881; 4,124,532, 4,174,429; 
4,349,648; 4,379,759; 4,719,193; and 4,888,318; and European Patent 
application Publication Nos. 0 012 148; 0 091 135; 0 120 503; and 0 369 
436; and the entire disclosures of these patents and publications 
pertaining to catalysts are incorporated herein by reference. 
Referring now to the drawing, catalyst component containing transition 
metal, e.g. titanium, is fed into first reactor 1 through line 2. 
Ethylene, comonomer, e.g., n-hexene, if used, hydrogen, if used, inert gas 
such as nitrogen, if used, and cocatalyst, e.g. triethylaluminum (TEAL), 
are fed through line 3 into recycle line 4 where they are combined with 
recycle gas and fed into the bottom of reactor 1. The gas velocity is high 
enough and the size and density of the particles in reactor 1 are such as 
to form a fluidized or dense bed 5 comprising catalyst particles 
associated with polymer formed by the polymerization of ethylene and, if 
present, comonomer within reactor 1. The conditions in reactor 1, e.g. 
partial pressure of ethylene, hydrogen/ethylene molar ratio, temperature, 
total pressure, etc. are controlled such that the polymer which forms is 
of relatively high molecular weight (HMW). Recycle gas leaving the top of 
reactor 1 through line 4 is recompressed in compressor 6, cooled in heat 
exchanger 7 after passing through valve 8 and are fed to the bottom of 
reactor 1 after being optionally combined with make-up gases and 
cocatalyst from line 3 as described. 
Periodically, when sufficient HMW polymer has formed in reactor 1, the 
polymer and catalyst 1 are transferred to discharge tank 9 by opening 
valve 10 while valves 11, 12 and 13 remain closed. When an amount of the 
HMW polymer and catalyst from reactor 1 which is desired to be transferred 
has been fed to discharge tank 9, the transfer system to second reactor 14 
is activated by opening valve 13 to force the HMW polymer and catalyst 
into transfer hose 15. Valve 13 is then closed to isolate transfer hose 15 
from discharge tank 9 and valve 11 is opened, ensuring that any gases 
leaking through valve 13 are vented and do not back-leak across valve 10 
into reactor 1. Transfer hose 15 is then pressurized with reactor-cycle 
gas from reactor 14 by opening valve 16. To minimize upsets in reactor 14, 
surge vessel 17 is used to store gas for pressuring transfer hose 15. With 
valve 16 still in the open position, valve 18 is opened to convey HMW 
polymer and catalyst into reactor 14. Both valves 16 and 18 are left open 
for a period to sweep transfer hose 15. Valves 18 and 16 are then closed 
sequentially. Transfer hose 15 is then vented by opening valve 13, valve 
11 having remained open during the transfer operation. Discharge tank 9 is 
then purged with purified nitrogen through line 18A by opening valve 12. 
During the transfer, cycle gas comprising hydrocarbons and hydrogen leaves 
reactor 14 through line 19, is compressed by compressor 20, flows through 
valves 21, 22 and 23 in line 24 and through surge tank 17, valve 16 and 
pressurized transfer hose 15 as described, thus effecting the transfer of 
HMW polymer and catalyst to reactor 14. 
After the transfer to reactor 14 is effected, the flow of gas from reactor 
14 to transfer hose 15 is stopped by closing valves 21, 22, 23 and 16. 
Ethylene, hydrogen, comonomer, e.g., n-hexene, if used, inert gas such as 
nitrogen, if used, and cocatalyst or catalyst component, if used, e.g., 
TEAL, are fed to reactor 14 through line 25 after being combined with 
unreacted cycle gas leaving the top of reactor 14 through line 19 which is 
compressed in compressor 20, cooled in heat exchanger 26 and enters the 
bottom of reactor 14 through line 27. The gas velocity and size and 
density of the particles in reactor 14 are such as to form fluidized or 
dense bed 28 of bimodal polymer particles associated with the catalyst, 
including the transition metal primary catalyst component added to reactor 
1. The conditions in reactor 14, e.g., partial pressure of ethylene, 
hydrogen/ethylene ratio and temperature, are controlled such that a 
relatively low molecular weight (LMW) polymer forms primarily within the 
voids of the HMW polymer/catalyst particles transferred from reactor 1. 
After a sufficient amount of LMW polymer has formed resulting in a bimodal 
polymer having a desirable molecular weight distribution and other 
properties, the polymer is transferred to discharge tank 29 by opening 
valve 30 while keeping valve 31 closed. After substantially all the 
polymer has been transferred to discharge tank 29, it is collected by 
closing valve 30 and opening valve 31, resulting in the pressure discharge 
of the final polymer product through line 32. 
The significance of bubble stability of melts of blends of the invention 
can be gleaned from the following discussion of the high stalk extrusion 
manipulations which involve extruding at rates of at least 150 feet per 
minute preferably at greater than 250 feet per minute (line speed.) 
Polyethylene resins prepared in the process of this invention are primarily 
used for the manufacture of biaxially oriented blown film in a high-stalk 
extrusion process. In this process, a polyethylene melt is fed through a 
gap (typically 30-50 mm) in an annular die attached to an extruder and 
forms a tube of molten polymer which is moved vertically upward. The 
initial diameter of the molten tube is approximately the same as that of 
the annular die. Pressurized air is fed to the interior of the tube to 
maintain a constant air volume inside the bubble. This air pressure 
results in a rapid 3-to-9-fold increase of the tube diameter which occurs 
at a height of approximately 5 to 10 times the die diameter above the exit 
point of the tube from the die. The increase in the tube diameter is 
accompanied by a reduction of its wall thickness to a final value ranging 
from approximately 0.5 to 2 mils and by a development of biaxial 
orientation in the film. The expanded tube is rapidly cooled (which 
induces crystallization of the polymer), collapsed between a pair of nip 
rolls and wound onto a film roll. 
Two factors determine suitability of a particular polyethylene resin for 
high stalk extrusion: the maximum attainable rate of film manufacture and 
mechanical properties of the formed film. Different HDPE resins greatly 
vary in their processing stability at high rates of film manufacture. 
Adequate processing stability is desired at throughput rates of up to 15 
lb/hr/inch die and high linespeeds (&gt;200 ft/min) for thin guage 
manufacture on modern extrusion equipment. The resins produced in the 
polymerization process of this invention with the catalyst systems of this 
invention have molecular characteristics which allow them to be processed 
successfully at these high speeds. Mechanical strength of the film is 
different in two film directions, along the film roll (machine direction, 
MD) and in the perpendicular direction (transverse direction, TD). 
Typically, the TD strength in such films is significantly higher than 
their MD strength. The films manufactured from the resins prepared in the 
process of this invention with the catalyst of this invention have a 
favorable balance of the MD and TD strengths. 
In accordance with the invention, a melt of the linear polyethylene is fed 
through a gap in an annular die for extrusion in the form of a tube, which 
is moved vertically upward. The bubble formed is measured in feet to the 
frost line. Pressurized air is fed to the interior of the bubble formed by 
the tube, which blows it to a greatly increased diameter and 
correspondingly reduced wall thickness and results in biaxial orientation 
of the film. Cooling air is supplied to the exterior surface of a bubble, 
while the extruded tube of molten material is being drawn. Further 
handling usually involves collapsing the tube between a pair of rolls to a 
flattened double-wall web at a stage in the cooling at which the wall 
surfaces will not adhere to one another. The flattened tube is wound onto 
a roll and/or further processed. 
Cooling air can be supplied to the exterior surface of a bubble by one or 
more cooling rings, each of which discharges one or more annular streams 
of cooling air for heat exchange engagement with the bubble exterior 
surface. One often used arrangement is to employ a primary ring in the 
immediate neighborhood of the die orifice, and a more powerful secondary 
ring spaced along the path of the bubble at a location at which the melt, 
while still not solidified, has cooled sufficiently to withstand the force 
of the more powerful secondary ring air stream or streams. 
These air rings can be configured, prearranged, not only to cool, but also 
to shape, the tube of molten resin. Controlling the configuration of the 
tube and bubble, by such air rings is described in U.S. Pat. No. 4,118,453 
which is incorporated by reference herein. The internal pressure of the 
tube is maintained by employing pressurized gas (air) during passage of 
the tube through the air rings. The apparatus in which such means are used 
are sometimes referred to as "stalk extruders"; stalk extruders are 
commercially available from Alpine. 
Thus in accordance with the invention the process comprises extruding the 
polyethylene through an annular die to form an extruded tube of molten 
material, cooling the extruded tube while drawing the tube so cooled, 
expanding the tube to attenuate the walls thereof by introducing a gas to 
the interior of the tube, and flowing a cooling gas in contact with the 
outer surface of said tube from a plurality of annular zones about said 
extruded tube spaced along the axis therof and being of increasing 
diameter in the direction away from the point of extrusion; the plurality 
of annular zones can be provided by circular pairs of annular zones about 
said extruded tube. In U.S. Pat. No. 4,118,453, incorporated by reference 
herein, as noted above, additional separate pairs of cooling gas confined 
streams are directed against said film on each side of a shape restricting 
surface which extends beyond the discharge boundaries of the discharged 
confined streams; the said additional cooling gas streams are passed in 
contact with the outer surface of said film tube at each of said shape 
restricting surfaces to produce a positive gas pressure zone between said 
surface and said film material and then said cooling gas is withdrawn from 
such contact between each pair of adjacent cooling gas inlets. 
In accordance with the invention the molten polyethylene, described above, 
is formed into a tube or a bubble having at least two different diameters, 
the smaller of the two diameters being substantially that of the die and 
the second diameter of the bubble exceeding that diameter of the die, with 
a frost height line downstream of the portion of the bubble having said 
smaller diameter and downstream of the portion of the bubble having said 
second diameter. The Frost line is the line where the extruded tube or 
bubble changes from molten to solid character. 
While the diameter of the tube is that of the die, the stresses, as well as 
machine direction (MD) orientation, in the melt relax; this stage of the 
process has been found to be critical to increase in MD tear resistance 
and impact resistance. As the tube diameter increases, the pressure 
increases within the bubble; that is the pressure differential between the 
inside of the tube and the external surface of the tube increases as the 
diameter increases. The increase in diameter can be 3:1 to 5:1 and up to 
7:1 to 9:1 times the die diameter. This expansion in bubble diameter 
occurs before the melt turns into a solid. As suggested above, the frost 
line height is where the film is below its melting point with no more 
expansion in the transverse direction and so no increase in bubble 
diameter. The resulting films have thicknesses of 1 mil gauge or less 
preferably of 0.5 mil and most preferably 0.5 mil or less. 
EXAMPLES 
Catalyst Preparation 
Example 1--Preparation of Catalyst Containing MgO treated with acetic acid: 
A sample of MgO support (Merck-Maglite D) was dried in a 500-ml 3-neck 
flask under nitrogen at 250.degree. C. for 16 hours without stirring. 30.8 
grams of this dry MgO support was then slurried in 200 ml of dry hexane in 
a 500-ml 3-neck flask and refluxed for 16 hours with 0.44 ml glacial 
acetic acid (99.8% pure acetic acid) at 0.01 molar ratio of the acid to 
the MgO. A dilute pentanol solution was prepared by adding 53.5 ml of 
pre-dried 1-pentanol (0.494 mole) to 45 ml of dry hexane in another flask. 
To avoid a rapid isotherm, 54.4 ml of neat TiCl.sub.4 (0.494 mole) was 
added dropwise to the 1-pentanol solution to form the titanium compound 
solution. The (1:1 pentanol/TiCl.sub.4) solution was immediately added to 
the acetic acid-treated MgO at room temperature. The slurry was refluxed 
at 70.degree. C. for 16 hours and allowed to cool. 
The catalyst precursor was washed 6 times with 100 ml of dry hexane. The 
solid was re-slurried with 200 ml of dry hexane, and 12 ml of 25 wt. % 
tri-n-hexylaluminum (TNHAL) solution (7.66 mmole TNHAL) was slowly added 
(about 3 minutes) to form a catalyst having an Al/Ti ratio of 0.23. The 
catalyst was dried for 16 hours at 65.degree. C. under nitrogen purge, to 
give a free-flowing light brown powder. Elemental analysis indicated that 
the finished catalyst contained 1.1 mmoles/g of Ti. 
Example 2--Preparation of Catalyst Containing MgO treated with octanoic 
acid: 
The preparation procedures are similar to Example 1 except octanoic acid 
was used in place of acetic acid to modify the MgO support. 
Example 3--Slurry Polymerization with Example 1 for Low Molecular Weight 
Product: 
The polymerization was conducted in a 1-gallon slurry reactor at 90.degree. 
C. with 2 liters of polymerization grade hexane. 0.138 g of Example 1 
catalyst (0.127 mmole Ti) and 1.8 ml of di-isobutylaluminumhydride (DIBAH) 
solution (25 wt. % in heptane: 2.27 mmole Al), no hexene comonomer, and 
hydrogen were added to the reactor. The polymerization was run at ethylene 
partial pressure of 70 psia to produce the HDPE products. The H.sub.2 
:C.sub.2 molar ratio was maintained at 3:1. The product was stabilized 
with 500 ppm of Irganox 1076, and then it was dried in vacuum oven for 4 
hours at 65.degree. C. The product was 1043 I.sub.2 homopolymer, and the 
productivity of the catalyst was 1875 g/g cat./hr. 
Example 4--Slurry Polymerization with Example 1 Catalyst for High Molecular 
Weight Product: 
The polymerization was conducted in a 2-gallon slurry reactor at 90.degree. 
C. with 4 liters of polymerization grade hexane. 0.073 g of Example 1 
catalyst, 3.6 ml DIBAH solution, and 40 ml of 1-hexene were added to the 
reactor. The polymerization was run at 155 psia partial pressure of 
ethylene and the H.sub.2 :C.sub.2 molar ratio was maintained at 0.06 to 
produce the high molecular weight product. The productivity of the 
catalyst was 5877 g/g cat./hr. and the product was 0.35 I.sub.21 
copolymer. 
Examples 3 and 4 indicate that it is possible to generate high and low 
molecular weight polymers in a tandem process to produce bimodal molecular 
weight distribution products using this catalyst. 
Example 5--Slurry Polymerization with Example 2 Catalyst for High Molecular 
Weight Product: 
The polymerization was conducted in a 2-gallon slurry reactor at 90.degree. 
C. with 4 liters of polymerization grade hexane. 0.047 g of Example 2 
catalyst, 2.5 ml TEA solution (25 wt. %), and 10 ml of 1-hexene were added 
to the reactor. The polymerization was run at 110 psia partial pressure of 
ethylene and the H.sub.2 :C.sub.2 molar ratio was maintained at 0.05 to 
produce high molecular weight (HMW). 
The productivity of the catalyst was 4500 g/g cat./hr. and the product was 
3.42 I.sub.21, 0.28 I.sub.5, and 12.2 FR (I.sub.21 /I.sub.5) copolymer 
with a molecular weight distribution suitable for generating HMW component 
for HD HMW Film tandem resins. 
Example 6--Slurry Polymerization with Example 2 Catalyst for High Molecular 
Weight Component to Simulate the Conditions of the First Reactor for a 
Tandem Process: 
The polymerization was conducted in a 500 ml slurry reactor at 90.degree. 
C. with 250 ml of polymerization-grade hexane. Approximately 5 ml of 
1-hexene, 1 ml of triethylaluminum solution (25 wt. % in heptane) as 
cocatalyst 1.5 mmole Al), 2.5 psia hydrogen and 0.0165 g of Example 2 
catalyst were added in sequence to the reactor. The polymerization was run 
at 48.5 psia partial pressure of ethylene for one hour to give 32.3 g of 
polyethylene. The productivity was 1958 g/g cat./hr, and the product was 
3.1 I.sub.21 copolymer. 
Example 7--Slurry Polymerization with Example 2 Catalyst for Low Molecular 
Weight Component to Simulate the Conditions of the Second Reactor for a 
Tandem Process: 
The polymerization was conducted in a 500 ml slurry reactor at 90.degree. 
C. with 250 ml of polymerization-grade hexane. Approximately 5 ml of 
1-hexene, 1 ml of triethylaluminum (25 wt. % in heptane) as cocatalyst 
(1.5 mmole Al), 114 psia hydrogen and 0.0252 g of Example 2 catalyst were 
added in sequence to the reactor. The polymerization was run at 46 psia 
ethylene partial pressure for one hour to give 47 g of polyethylene. The 
productivity of the catalyst was 1865 g/g cat./hr. and the polymer was 288 
I.sub.2 homopolymer. 
Example 6 and Example 7 showed that the productivity of Example 2 catalyst 
is suitable for tandem reactor operations. It suffers less than an 
ordinary catalyst under high hydrogen partial pressure. 
Comparative Example 1--Preparation of the Comparative Catalyst 
491 kg of Davison 955 silica was dehydrated at 600.degree. C. for 4 hours. 
This dry silica was transferred to a mix vessel, and 7.173 liters/kg dry 
silica of isopentane and 0.882 liters/kg dry silica of 11 wt. % 
triethylaluminum (TEA) in isopentane solution were also charged to the mix 
vessel. The slurry was agitated at 60.degree. C. for 1 hour. Under dry 
nitrogen purge, the temperature was raised to 80.degree. C. to evaporate 
the solvent to give "TOS" (TEA on silica). 
The temperature of the precursor solution vessel was set at 45.degree. C. 
Approximately 300 gallons of fresh THF and 45.4 kg of the pre-purged (5 
times with dry nitrogen) MgCl.sub.2 were charged to the vessel. The 
temperature was then raised to 70.degree. C., 31 kg TiCl.sub.3 was added, 
and the precursor solution was stirred for 4 hours. 
The mix vessel was maintained at 70.degree. C. and the precursor solution 
was charged to the TOS while agitating. The agitation was continued for 
one hour at 70.degree. C. and the temperature was raised to 80.degree. C. 
to start the solvent evaporation. Dry nitrogen was purged through the 
bottom of the catalyst mix vessel for about 20 hours to give free-flow 
SIMP catalyst. 
Slurry Polymerization with Comparative Example 1 Catalyst for High 
Molecular Weight Component to Simulate the Conditions of the First Reactor 
for a Tandem Process 
The polymerization was carried out as described in Example 6 except 0.023 g 
of the Comparative-Example 1 catalyst was used in place of Example 2 
catalyst. The productivity was 978 g/g cat./hr and the product was 7.7 
I.sub.21 copolymer. 
Comparative Example 3--Slurry Polymerization with Comparative Example 1 
Catalyst for Low Molecular Weight Component to Simulate the Conditions of 
the Second Reactor for a Tandem Process. 
The polymerization was carried out as described in Example 7 except 0.0235 
g of the Comparative Example 1 catalyst was used in place of Example 2 
catalyst. The productivity was 425 g/g cat./hr and the product was 241 
I.sub.2 homopolymer. 
Comparing Example 6 with Comparative Example 2 and Example 7 with 
Comparative Example 3, as shown in Table 1, it is obvious that the 
activity of Example 2 catalyst is higher and it suffers less under high 
hydrogen partial pressure conditions than the Comparative Example catalyst 
1. 
TABLE 1 
______________________________________ 
Catalyst Ex. 6 Comp. Ex. 2 Ex. 7 Comp. Ex. 3 
______________________________________ 
H2/C2 0.05 0.05 2.5 2.5 
Productivity 
1960 980 1860 425 
(g/g cat./hr) 
MI.sub.2 0.07 0.19 288 241 
MI.sub.21 3.1 7.7 -- -- 
______________________________________ 
Example 7' and Comparative Example 4 
Addition of hydrogen during ethylene polymerization reactions with Ti-based 
catalysts always results in suppression of catalyst activity. However, the 
decrease in activity is catalyst-dependent. Two polymerization experiments 
were conducted at 90.degree. C. in a 500 ml slurry reactor filled with 250 
ml of heptane containing 1.5 mmol of triethylaluminum as cocatalyst. 
Catalyst of Example 2 (0.0285 g) was used in one experiment (Example 7') 
and catalyst of Comparative Example 1 ((0.0257 g) was used in another 
experiment (Comparative example 4). The ethylene partial pressure in each 
experiment was maintained at 90 psi. During each experiment, the hydrogen 
partial pressure was increased from 0 to 90 psi and the resulting decrease 
in the polymerization rate was measured. The results are presented in 
Table 2. 
TABLE 2 
______________________________________ 
Activity depression at 
Catalyst P.sub.H /P.sub.E = 1 
______________________________________ 
Example 7' Example 2 52% 
Comp. Example 7 
Comp. Example 1 
74% 
______________________________________ 
These comparisons show that the catalyst formulations of this invention are 
adversely affected by hydrogen to a lesser degree than the catalyst 
formulation of Comparative Example 1. 
Example 8--Gas-Phase Fluid-Bed Polymerization with Example 2 Catalyst under 
the Conditions of the First Reactor for a Tandem Process: 
In a four cubic foot gas-phase fluid-bed reactor, at 74.degree. C., the 
Example 2 catalyst was run under conditions corresponding to the expected 
conditions in the first reactor of a HMW-first tandem process. As shown in 
Table II, the ethylene partial pressure was kept at 43 psia during the 
entire run. There was no sign of static or fouling of pressure taps. 49 
psia of isopentane was used to further enhance process continuity. 
0.067 hydrogen to ethylene ratio and 0.058 hexene to ethylene in the gas 
phase were maintained. A 0.41 MI.sub.21, 0.9295 (g/cc), 23.5 lb/ft.sup.3, 
and 0.019 inch of average particle size resin was produced. This resin was 
later used in blend studies. 
Example 9--Blend study to simulate tandem-process HD-HMW film-grade resin 
using high molecular weight polymer component (Example 8) prepared with 
the catalyst of this invention. 
Several resin blends were prepared with compositions imitating tandem 
resins. In two cases, the high molecular weight component was prepared 
with the catalyst of Example 2. The density of the resin was 0.931 and its 
I.sub.21 value was 0.47. In other two cases the high molecular weight 
component was prepared with the catalyst of Comparative Example 1. The 
density of the resin was 0.926 and I.sub.21 was 0.38. In all these 
examples, the low molecular weight component was the same. It was prepared 
with the catalyst of Comparative Example 1. It has I.sub.2 =250 and 
density 0.960. It is known that the low molecular weight component in such 
blends does not have significant effect on mechanical properties of the 
blends and is merely used to enhance processability of the blends. The 
components were melt-blended in a Banbury batch mixer under mild 
conditions to prevent tailoring of the resins. Properties of the blends 
are given in Table II. 
TABLE II 
__________________________________________________________________________ 
Catalyst for 
Properties of 
Content of 
Properties of 
Blend No. 
HMW component 
HMW Component 
HMW Component 
Blend 
__________________________________________________________________________ 
1 Example 2 
I.sub.21 = 0.47 
52% I.sub.21 = 10.5 
d = 0.931 MFR = 148 
FR = 18.0 
2 Example 2 
I.sub.21 = 0.47 
58% I.sub.21 = 6.1 
d = 0.931 MFR = 153 
FR = 18.0 
3 Comparative 
I.sub.21 = 0.38 
52% I.sub.21 = 9.9 
Example 1 
d = 0.926 MFR = 115 
FR = 11.4 
4 Comparative 
I.sub.21 = 0.38 
58% I.sub.21 = 5.7 
Example 1 
d = 0.926 MFR = 94 
FR = 11.4 
__________________________________________________________________________ 
As shown in Table II, the blends made with the HMW component produced with 
the catalyst of Example 2 had broader molecular weight distributions 
(higher MFR values) compared to those for the blends made with the HMW 
component produced with the catalyst of Comparative Example 1. 
Films were manufactured from the blends listed in Table II using the Alpine 
Film Line. The blends based on the HMW component produced with the 
catalyst of Comparative Example 1 exhibit very poor bubble stability (&lt;100 
foot/min). These blends could not be processed into 0.5-mil film. On the 
other hand, the blends made with the HMW component produced with the 
catalyst of Example 2 exhibit excellent bubble stability, with a stable 
bubble at line speeds exceeding 300 foot/min. The 0.5-mil film was easily 
manufactured with these blends. Ability to manufacture films from 
untailored resins has a significant cost advantage. 
MD tear value is one of the crucial parameters that characterize HMW HDPE 
films. All 1-mil films which contain the HMW component produced with the 
catalyst of Example 2 have the MD tear values of approximately 29 g, which 
is, on average, 15% higher than the MD tear values of the 1-mil films 
which contain the HMW component produced with the catalyst of Comparative 
Example 1. 
Examples 8' and 9' 
Preparation of polymers under conditions corresponding to tandem process. 
To demonstrate the use of the catalyst formulation of this invention for a 
two-stage synthesis of HDPE resins with broad molecular weight 
distributions, two experiments were carried out in which reaction 
conditions (hydrogen/ethylene ratios and temperature) were changed in the 
course of polymerization reactions. The reactions were carried out in a 50 
ml reactor containing 250 ml heptane and small amounts of 1-hexene. 
Catalyst of Example 2 was used in both reactions (0.0255 g in Example 8' 
and 0.0321 g in Example 9'). Both polymerization reactions were carried 
out in two stages. In the first stages, the reactions were carried out at 
low P.sub.H /P.sub.E ratios and, in the second stages, at high P.sub.H 
/P.sub.E ratios. Polymer yields were 30.8 g in Example 8' and 24.1 g in 
Example 9'. Table 3 gives conditions of these experiments and properties 
of the resins. 
TABLE 3 
__________________________________________________________________________ 
A. Reaction conditions 
Temperature 
P.sub.H /P.sub.E 
Example 
Catalyst 
Cocat. 
Hexene 
1 stage 
2 stage 
1 stage 
2 stage 
__________________________________________________________________________ 
8' Ex. 2 
TEAL 
4 wt. % 
80.degree. C. 
95.degree. C. 
0.04 2.5 
9' Ex. 2 
TEAL 
2 wt. % 
80.degree. C. 
95.degree. C. 
0.006 
2.5 
__________________________________________________________________________ 
B. Resin Properties 
Fraction of resin 
Example 
made in first stage 
I.sub.2 
I.sub.21 
MFR = I.sub.21 /I.sub.2 
__________________________________________________________________________ 
8' 49% 0.064 
6.5 102 
9' 52% 0.164 
26.0 159 
__________________________________________________________________________ 
These examples show that the catalysts of this invention afford synthesis 
of HDPE resins with broad molecular weight distributions (as characterized 
by high MFR values) required for high-strength film applications. 
Thus it is apparent that there has been provided, in accordance with the 
invention, a product and process for its production, that fully satisfies 
the objects, aims, and advantages set forth above. While the invention has 
been described in conjunction with specific embodiments thereof, it is 
evident that many alternatives, modifications, and variations will be 
apparent to those skilled in the art in light of the foregoing 
description. Accordingly, it is intended to embrace all such alternatives, 
modifications, and variations as fall within the spirit and broad scope of 
the appended claims.