Note: Descriptions are shown in the official language in which they were submitted.
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FIELD OF THE INVENTION
The present invention relates to supported Ziegler-Natta catalysts
which are useful in olefin polymerization, and more particularly in the
fluidized gas phase polymerization of alpha-olefins.
BACKGROUND OF THE INVENTION
Ziegler-Natta type catalysts are well known and have been used
since the early 1950's. Generally the catalyst comprises a transition metal
compound, typically titanium in the 3 or 4 valence state (e.g. TiCI3 or TiCI4)
together with at least one activator, typically an aluminum compound such
as a trialkyl aluminum (e.g. triethylaluminum (TEAL)) or an alkyl aluminum
halide (e.g. diethylaluminum chloride (DEAC)) and the like. The catalysts
may contain magnesium chloride which may be generated from a dialkyl
magnesium compound and active chloride. Typically, the catalysts are
prepared in conjunction with an electron donor which tends to narrow the
molecular weight distribution in the resulting polymer. A good description
of these types of catalysts is contained in United States Patent 4,302,566
issued November 24, 1981 to Karol et al., assigned to Union Carbide
Corporation. Karol teaches that it is essential to use an electron donor in
the preparation of the catalyst. The use of an electron donor has been
eliminated from the catalysts of the present invention.
United States Patent 5,633,419 issued May 27, 1997 to The Dow
Chemical Company discloses a supported Ziegler-Natta type catalyst or
catalyst precursor. However, it is a limitation of the reference that the
halide is used in the form of a hydrogen halide (e.g. HCI). The reference
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teaches away from the subject matter of the present invention which is
limited to the use of alkyl halides as the halide source. Additionally, the
reference appears to teach the use of a support such as silica, which has
been treated either thermally or chemically, but not both, which is contrary
to the method for preparing the support of the present invention.
European Patent Application 0 744 416 published November 27,
1996 in the name of BP Chemicals Limited (BP) teaches supported
catalysts and catalyst precursors. The reference teaches that the support
is reacted with either the aluminum compound or the magnesium
compound but not a concurrent treatment with a mixture of aluminum and
magnesium (e.g. MAGALAT"", a mixture sold by Akzo). The reference
teaches against the addition of a second aluminum compound.
Additionally, in view of the examples, the BP patent strongly suggests that
an electron donor needs to be used in the preparation of the catalyst, a
feature that has been eliminated from the present invention. This
reference also teaches that the halogenating agent must be used in a
molar ratio such that all of the Mg and Al compounds are converted to their
respective halides, a limitation which is not put on the present invention.
That is, in accordance with the present invention, there is an excess of
aluminum and magnesium over reactive halide so that not all of the
aluminum and magnesium is precipitated.
BP patent EP 0 595 574 B1 granted on January 2, 1997 requires
that the catalyst be prepared on a support treated with an organosilicon
compound. The supports used in accordance with the present invention
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are treated thermally and chemically (aluminum alkyls) but not with
organosilicon.
BP patent EP 0 453 088 B1 granted on July 31, 1997 teaches that
the catalyst be made on dehydrated silica and that the catalyst needs to
be pre-polymerized to obtain a useful catalyst for the synthesis of linear
low density polyethylene (LLDPE). The catalysts of the present invention
do not need to be pre-polymerized to be useful for the polymerization of
ethylene to LLDPE. The patent teaches about washing the catalyst to
remove excess Mg compounds which is not relevant to our catalyst. This
patent also teaches about the need for high Ti:(Mg+Al) ratios, a restriction
which is removed in the present invention.
The present invention seeks to provide a supported Ziegler-Natta
type catalyst which is prepared preferably in the absence of an electron
donor, and provides a polymer having a broad molecular weight
distribution. The present invention relates to supported Ziegler-Natta
catalysts which are useful in olefin polymerization, and more particularly in
the fluidized gas phase polymerization of alpha-olefins.
SUMMARY OF THE INVENTION
The present invention provides a process conducted in a
hydrocarbon solvent at a temperature from 0 C to 100 C for preparing a
catalyst for the gas phase polymerization of alpha-olefins comprising:
a. contacting a dehydrated silica support containing from 0.1 to 3
weight % aluminum having the formula AI'(R')aXb wherein each R'
is independently selected from the group consisting of C,_,o alkyl
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radicals, X is selected from the group consisting of Cl and Br, a and
b are 0 or an integer from 1 to 3 provided the sum of a+b=3 with;
b. carbon tetrachloride (CCI4) or a secondary or tertiary alkyl halide of
the formula R4CI wherein R4 is selected from the group consisting of
C3_6 alkyl radicals. The halide is added to the support in a quantity
of 2 to 30 weight %, preferably from 5 to 20 weight %, based on the
weight of silica and contacting the resulting product with;
c. in any order or in combination; (i) a mixture of an aluminum
compound of the formula AI2(R2)nXm wherein each R 2 is
independently selected from the group consisting of C,-,o alkyl
radicals, X is selected from the group consisting of CI and Br, m
and n are 0 or an integer from 1 to 3 provided the sum of n+m=3,
and (ii) Mg(R3)2 wherein each R3 is independently selected from the
group consisting of C,_,o alkyl radicals wherein the molar ratio of
Mg:A12 in said mixture is from 0.5:1 to 25:1 to provide from 0.25 to
8.0 weight % of Mg based on the weight of the silica, a molar ratio
of Cl:Mg from 1:1 to 8:1 in the resulting product and contacting the
resulting product with;
d. a titanium compound of the formula Ti(R5)y(CI)Z wherein each R5 is
selected from the group consisting of C1_10 alkyl and alkoxide
radicals and phenyl radicals which are unsubstituted or substituted
by a C1_4 alkyl radical, y and z are 0 or an integer from 1 to 4 and
the sum of y+z=4 to provide from 0.1 to 1.5 weight % of Ti based
on the silica.
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In a further embodiment of the present invention in the above
process after step d there is added from 0 up to 0.3 mmol of electron
donor per g of silica.
The present invention also provides a gas phase process for the
polymerization, at a pressure from 10 to 500 psi, of a mixture comprising
from 0 to15 mole % hydrogen, from 0 to 30 mole % of one or more C3-e
alpha-olefins, from 15 to 100 mole % of ethylene and from 0 to 75 mole %
of an inert gas such as N2, conducted at a temperature from 50 C to
120 C in the presence of a catalyst as described above preferably in the
absence of an electron donor.
The present invention further provides a polymer comprising from 0
to 15 mole % of one or more C3_8 alpha-olefins, from 85 to 100 mole % of
ethylene having a molecular weight (Mw) greater than 50,000 and a
polydispersity (Mw/Mn) from 3.5 to 7 prepared according to the above
process.
BEST MODE
The supports useful in accordance with the present invention
typically comprise a substrate of alumina or silica having a pendant
reactive moiety. The reactive moiety may be a siloxy radical or more
typically is a hydroxyl radical. The preferred support is silica or alumina.
The support should have a particle size from about 10 to 250 microns,
preferably from about 30 to 150 microns. The support should have a large
surface area typically greater than about 3 m2/g, preferably greater than
about 50 mZ/g, most preferably from 100 m2/g to 1,000 m2/g. The support
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will be porous and will have a pore volume from about 0.3 to 5.0 ml/g,
typically from 0.5 to 3.0 ml/g. Supports, which are specifically designed to
be an agglomeration of subparticies, while useful, are not required.
It is important that the support be dried prior to the initial reaction
with an aluminum compound. Generally the support may be heated at a
temperature of at least 200 C for up to 24 hours, typically at a temperature
from 500 C to 800 C for about 2 to 20 hours. The resulting support will be
free of adsorbed water and should have a surface hydroxyl content from
about 0.1 to 5 mmol/g of support, preferably from 0.5 to 3 mmol/g.
The first aluminum (AI') is deposited upon the support by contacting
the support, preferably silica, with an anhydrous solution of an aluminum
alkyl of the formula AI'(R')aXbwherein each R' is independently selected
from the group consisting of C,-,o alkyl radicals, preferably C1_6 alkyl
radicals, X is selected from the group consisting of Cl and Br, preferably Cl
and a and b are 0 or an integer from 1-3 provided the sum of a+b=3. Most
preferably, R' is selected from the group consisting of methyl, ethyl and
butyl radicals. Preferably, b is 0. From a commercial viewpoint, the most
available compound is triethylaluminum (TEAL).
The support is reacted with an aluminum compound such that the
amount of aluminum on the support is from about 0.1 to about 3 weight %,
preferably from about 0.5 to about 2 weight %, based on the weight of the
silica.
The resulting treated support may then be reacted with the
remaining components in the specified order.
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The halide in the catalyst is provided by CCI4 or a secondary or
tertiary halide of the formula R4CI wherein R4 is selected from the group
consisting of C3-6 alkyl radicals. Suitable chlorides include sec-butyl
chloride, t-butyl chloride and sec-propyl chloride. The halide is added to
the support in a quantity of 2 to 30 weight %, preferably from 5 to 20
weight % based on the weight of silica.
The second aluminum component in the catalyst is of the formula
AI2(R2)nXm wherein each R2 is independently selected from the group
consisting of C,_,o alkyl radicals, preferably C1-6 alkyl radicals, X is
selected
from the group consisting of Cl and Br, preferably Cl and n and m are 0 or
an integer from 1 to 3 provided the sum of n+m=3. Most preferably, R2 is
selected from the group consisting of methyl, ethyl and butyl radicals.
Preferably, m is 0. The second aluminum compound may be the same or
different from the first aluminum compound. The amount of the second
aluminum (e.g. AI2) is such that it will provide from about 0.20 to 4.0 weight
% of the catalyst based on the weight of the silica.
The magnesium component in the catalyst will have the formula
Mg(R3)2 wherein each R3 may be independently selected from the group
consisting of C1-10 alkyl radicals, preferably C,_6 alkyl radicals. More
preferably, R3 is selected from the group consisting of ethyl and butyl
radicals. Some suitable magnesium compounds include dibutyl-
magnesium and butyl-ethyl-magnesium. The magnesium is used in an
amount to provide from 0.25 to 8.0 weight % based on the weight of the
silica, preferably from 0.5 to 4.0 weight % based on the weight of the
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silica. The Mg is also used to provide a CI:Mg molar ratio from 1:1 to 8:1,
preferably from 1.5:1 to 6:1. The molar ratio of Mg:A12 may range from
0.5:1 to 25:1, preferably from 0.5:1 to 16:1.
The AIZ and Mg may be added as a mixed compound (such as the
commercially available MAGALA, a product supplied by Akzo) or
sequentially in any order. That is to say, AI2 can be added first followed by
the Mg compound or the Mg compound can be added first followed by AIZ.
The titanium in the catalyst is provided by a compound of the
formula Ti(RS)YCIZ wherein each R5 is independently selected from the
group consisting of C1_10 alkyl and alkoxide radicals and phenyl radicals
which are unsubstituted or substituted by a C,-4 alkyl radical, and y and z
are 0 or an integer from 1 to 4 provided that the sum of y+z=4. Preferably,
R5 is selected from the group consisting of C2_6 alkyl and alkoxy radicals
and phenyl and benzyl radicals. The titanium compound is added in an
amount to provide from 0.1 to 1.5 weight % of titanium based on the
weight of the silica. Preferably, the titanium is present in an amount from
0.25 to 1.0 weight % based on the weight of the silica. In one
embodiment of the invention, y is 0.
The catalysts of the present invention will have: a molar ratio of
total aluminum (AI'+AI2):Mg from 0.1:1 to 3:1, preferably from 0.4:1 to 3:1;
preferably a molar ratio of halide (CI) to 2Mg +3(AI'+AI2) from 0.25:1 to
4:1; an amount of organic halide from 0.2 to 5 mmol per g of silica; an
amount of Mg from 0.1 to 3.5 mmol per g of silica; a total amount of
aluminum to provide from 0.3 to 3.0 mmol of aluminum per g of silica; a
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molar ratio of titanium to aluminum and magnesium (e.g. Ti:(AI+Mg)) from
0.01:1 to 0.15:1 preferably from 0.02:1 to 0.085:1; an amount of Ti to
provide from 0.02 to 0.32 mmol of Ti per g of silica; a molar ratio of Ti:Mg
from 0.04:1 to 0.4:1.
The process to prepare the catalyst may be conducted at
temperatures from 0 C to 100 C, typically at temperatures from 5 C to
80 C. The individual components (e.g. silica comprising aluminum
compound, magnesium compound, second aluminum compound, halide
(chloride) compound and titanium compound) are suspended or dissolved
in a hydrocarbon medium. The solvent used in the preparation of the
catalyst is an inert C5_10 hydrocarbon which may be unsubstituted or
substituted by a C, alkyl radical, such as a hydrocarbon that is inert with
respect to the catalyst. Such solvents are known and include for example:
pentane, hexane, heptane, octane, cyclohexane, methylcyclohexane and
hydrogenated naphtha.
The drying steps may be conducted in a number of different
manners. During the synthesis of the catalyst, it is preferred that the
solvent not be removed between the halide and Mg addition sequence.
The drying step or steps may be conducted by maintaining the reactants
at a temperature from 5 C to 80 C, preferably from 30 C to 80 C, by
passing or purging a dry inert gas such as nitrogen through the reactants.
The drying may also be conducted at a reduced pressure under vacuum
at a temperature from 10 C to 50 C and at a pressure from 0.1 to 500 mm
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Hg (torr), preferably less than 400 torr (66.65 kPa, preferably less than
53.33 kPa).
The catalyst is recovered as a free flowing powder. The catalyst is
then used in combination with a cocatalyst, typically an aluminum
compound such as an aluminum alkyl, in the gas phase polymerization of
a gaseous mixture comprising from 0 to 15 mole % of hydrogen, from 0 to
30 mole % of one or more C3-8 alpha-olefins, from 15 to 100 mole % of
ethylene, and from 0 to 75 mole % of an inert gas at a temperature from
50 C to 120 C, preferably from 75 C to about 110 C, and at pressures
typically not exceeding 3447 kPa (about 500 psi), preferably not greater
than 2414 kPa (about 350 psi). Preferably, the catalyst is used in the
absence of an electron donor. If present the electron donor may be used
in amounts from 0 up to 0.3 mmol per g of silica. Suitable electron donors
are well known to those skilled in the art and include tetrahydrofuran
(THF), dimethyl formamide (DMF), ethyl acetate, methyl isobutyl ketone
and the like.
The catalyst may be used in a fluidized bed gas phase reactor or in
a stirred bed gas phase reactor. These processes are well known to
those skilled in the art. A broad general description of these types of
processes is set out in the paper "Gas Phase Ethylene Polymerization:
Production Processes, Polymer Properties, and Reactor Modeling" by
Tuyu Xie, Kim B. McAuley, James C. C. Hsu, and David W. Bacon, Ind.
Eng. Chem. Res., 1994, 33, 449-479.
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Generally, a monomer feed comprising at least ethylene and one or
more C3_6 alpha-olefins is fed to a gas phase fluidized bed or stirred bed
reactor. The monomer mixture optionally together with hydrogen and/or
an inert gas are fed to the fluidized bed. In a fluidized bed reactor, the
velocity of the gas is sufficient to suspend the bed in the fluid flow of
monomer and other components. In a stirred bed reactor mechanical
agitation serves to help suspend the bed. Generally a fluid bed reactor is
vertical and a stirred bed reactor is horizontal. Concurrently with the
monomers a supported catalyst is fed to the bed. The monomer passing
over the catalyst polymerizes on the catalyst and in the pores of the
catalyst causing the particle to increase in size and to break. The
resulting particle of polymer on catalyst grows as it resides in the catalyst
bed. In a stirred tank reactor the bed is stirred to a discharge section and
leaves the reactor. In a fluidized bed the reactor typically has a narrower
section to keep the fluid velocity sufficiently high to fluidize the bed.
There
is an expanded zone at the top of the reactor to reduce the speed of the
gas passing through the reactor so the polymer/catalyst particles fall back
into the bed. The discharge is from the bed zone in the reactor.
In both the fluidized bed and stirred bed the polymer particles
removed from the reactor are degassed to remove any volatile material
and the resulting polymer (with entrained catalyst) may then be further
treated (e.g. stabilizers added and pelletized if necessary).
Typically the resulting polymer will comprise from 85 to 100 mole %
of ethylene and from 0 to 15 mole % of one or more C3_6 alpha-olefins.
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The polymer should have a molecular weight (weight average Mw) greater
than 50,000. The polymers prepared according to the present invention
will have a polydispersity (Mw/Mn) from 3.5 to 7, preferably from 3.75 to 6.
The polymers may be compounded with the usual additives such as
heat and light stabilizers (typically hindered phenol type stabilizers such as
those sold by Ciba Geigy) and ultraviolet light stabilizers (such as the
hindered amine stabilizers sometimes referred to as HALS also sold by
Ciba Geigy), processing aids such as the fluoroelastomers optionally in
combination with waxes such as low molecular weight esters of
polyethylene glycol (i.e. CarbowaxTM ) as sold by 3M and by DuPont .
The resulting polymers, depending on polymer properties, may be
used in a number of applications such as film, injection molding and
rotomolding.
The present invention will now be illustrated by the following non-
limiting examples.
Catalyst Synthesis
Support Preparation
Silica (200 g) was pre-dried at 150 C for a day prior to heating it to 200 C
under a flow of air for 2 hours. After this time the air was turned off and
nitrogen was slowly passed over the silica and the temperature was
increased to 600 C for 6 hours. The oven was then turned off and the
silica was allowed to cool to room temperature. The silica was then
transferred to a reaction vessel and hexane (1 L) was added. With stirring,
triethylaluminum (TEAL) (71.4 mL of a 25 weight % TEAL in n-
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hexane) was added over 10 minutes at room temperature. After stirring
the slurry for 15 minutes at room temperature the solvent was removed
under vacuum. After the silica reached a free-flowing state, it was dried
thoroughly under a high vacuum (0.1 mm of Hg) at 60 C for 2 hours.
Catalyst Preparation
To a slurry of a prepared support (15 g) in pentane (100 mL) at 0 C
was added t-butyl chloride (3.24 g diluted with 10 mL of pentane) over 10
minutes. After the addition was complete the cold bath was removed and
the reaction mixture was stirred for 2 hours. The slurry was then cooled
again to 0 C and MAGALA (24.3 g, 1.75 weight % Mg, 0.24 weight % Al in
heptane) was added over 10 minutes. After removing the cold bath and
stirring for 2 hours the solvent was removed under vacuum at room
temperature. The solid was then slurried again in pentane (100 mL) and
cooled to 0 C at which time TiCl4 (0.42 g diluted with 10 mL pentane) was
added over 10 minutes. After removing the cold bath and stirring for 2
hours, the solvent was removed under vacuum leaving the catalyst as a
white solid which was stored in a glove box.
Polymerization of the Above Catalyst
In a 75 L stirred bed catalytic reactor at 88 C containing hydrogen,
nitrogen, ethylene and hexene (as described in Table 1) the above
catalyst was added at a rate of 0.67 g per hour. The Al, in the cocatalyst
(TEAL):Ti ratio was maintained at approximately 40:1. Under these
conditions an LLPDE was formed whose properties are shown in Table 1.
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TABLE I
C6H12/C2H4 molar flow ratio 0.077
H2/C2H4 molar gas ratio 0.084
Nitrogen (mole %) 53.3
M12.16 0.65
MFR 36.5
Bulk density (Ib/ft3) 20.3
Comparative Example
For comparative purposes a catalyst prepared following United
States Patent 4,302,566 was used to produce an LLDPE. In a 75 L stirred
bed catalytic reactor at 88 C containing hydrogen, nitrogen, ethylene and
hexene (as described in Table 2) the above catalyst was added at a rate
of 0.17 g per hour. The Al, in the cocatalyst (TEAL):Ti ratio was
maintained at approximately 40:1. Under these conditions an LLPDE was
formed whose properties are shown in Table 2.
TABLE 2
C6H12/C2H4 molar flow ratio 0.077
H2/C2H4 molar gas ratio 0.19
Nitrogen (mole %) 48.4
MI216 0.97
MFR 26.5
Bulk density (Ib/ft3) 24.7
When the melt flow ratio (MFR) in Table 1 (36.5) is compared to the
MFR in Table 2 (26.5) it is evident that the molecular weight distribution of
the polymer prepared in accordance with the present invention is
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significantly broader than the molecular weight distribution for the polymer
prepared with the catalyst of the prior art.
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