CA2124732C - Chromium catalyst compositions and polymerization processes therewith - Google Patents
Chromium catalyst compositions and polymerization processes therewithInfo
- Publication number
- CA2124732C CA2124732C CA002124732A CA2124732A CA2124732C CA 2124732 C CA2124732 C CA 2124732C CA 002124732 A CA002124732 A CA 002124732A CA 2124732 A CA2124732 A CA 2124732A CA 2124732 C CA2124732 C CA 2124732C
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- CA
- Canada
- Prior art keywords
- support
- chromium
- per gram
- ethylene
- titania
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
Abstract
Chromium catalyst compositions are provided. These chromium catalyst compositions comprise at least two chromium catalyst systems that have a certain amount of chromium and a support that comprises silica and titania. the supports halve certain pore volumes and surface areas. These catalyst compositions are useful for homopolymerizing ethylene or copolymerizing ethylene with a comonomer. The resins produced are useful in film applications.
Description
CHROMIUM CATALYST COMPOSITIONS AND POT.YMERIZATION PROCESSES THEREWITH
This invention is related to the field of chromium catalyst compositions. This invention is also related to the fields of polymerizing ethylene, or copolymerizing ethylene and a comonomer, with a chromium catalyst composition.
The high molecular weight-high density ethylene polymer film market, in the U.S., is dominated by multicomponent ethylene polymers (colloquially referred to as "bimodal" or "multimodal" polymers) that are produced by mixtures of titflnium halide catalysts. These multicomponent ethylene polymers offer good impact resistance and thus, good down gauging capability, along with fl high modulus. The sdvent of these multicomponent ethylene polymers hRs opened up markets previously covered by other materia~s such ~s pR~er, thicker gauge ethylene polymers, and lower density ethylene polymers. However, these multicomponent ethylene polymers are produced commercially using cascade reactor systems in which two reactors flre ]inked in series so that a two stage polymerization can take place with different polymerization condltions in each reactor. This is fl more expensive production method than a single stage reactor system.
This invention is related to the field of chromium catalyst compositions. This invention is also related to the fields of polymerizing ethylene, or copolymerizing ethylene and a comonomer, with a chromium catalyst composition.
The high molecular weight-high density ethylene polymer film market, in the U.S., is dominated by multicomponent ethylene polymers (colloquially referred to as "bimodal" or "multimodal" polymers) that are produced by mixtures of titflnium halide catalysts. These multicomponent ethylene polymers offer good impact resistance and thus, good down gauging capability, along with fl high modulus. The sdvent of these multicomponent ethylene polymers hRs opened up markets previously covered by other materia~s such ~s pR~er, thicker gauge ethylene polymers, and lower density ethylene polymers. However, these multicomponent ethylene polymers are produced commercially using cascade reactor systems in which two reactors flre ]inked in series so that a two stage polymerization can take place with different polymerization condltions in each reactor. This is fl more expensive production method than a single stage reactor system.
2 212 ~732 SUMMARY OF THE INVENTION
In order to compete with these multicomponent ethylene polymers it is important for 8 resin to have good impaçt strength, tear resistsnce in the transverse direction, appearance, and processing behavior. To date, chromium catslysts hflve not been competitive in the high molecular weight-high density ethylene polymer film market. For example, one chromium catalyst may produce 8 resin that has good film properties, but poor bubble stability at high production rates and thin gauges. On the other hand, another chromium catalyst may produce a resin that has a good bubble stability at high production rates flnd thin gauges, but poor film properties. However, making a chromium catalyst that produces an high molecular weight-high density ethylene polymer film resin that has good film properties and good bubble stability at high production rates and thin gauges has, until this invention, not been flccomplished.
It is an object of this invention to provide chromium catalyst compositions.
It is another object of this invention to provide chromium catalyst compositions that are useful for polymerizing ethylene or copolymerizing ethylene with a comonomer.
It is yet another object of this invention to provide chromium catalyst compositlons that are usefu] for polymerizing ethylene or copolymerizing ethylene with a comonomer~ thereby producing a high molecular weight-high density ethylene polymer that is useful for making a film that has good film properties and that can be processed at high production rates and thin gauges.
In order to compete with these multicomponent ethylene polymers it is important for 8 resin to have good impaçt strength, tear resistsnce in the transverse direction, appearance, and processing behavior. To date, chromium catslysts hflve not been competitive in the high molecular weight-high density ethylene polymer film market. For example, one chromium catalyst may produce 8 resin that has good film properties, but poor bubble stability at high production rates and thin gauges. On the other hand, another chromium catalyst may produce a resin that has a good bubble stability at high production rates flnd thin gauges, but poor film properties. However, making a chromium catalyst that produces an high molecular weight-high density ethylene polymer film resin that has good film properties and good bubble stability at high production rates and thin gauges has, until this invention, not been flccomplished.
It is an object of this invention to provide chromium catalyst compositions.
It is another object of this invention to provide chromium catalyst compositions that are useful for polymerizing ethylene or copolymerizing ethylene with a comonomer.
It is yet another object of this invention to provide chromium catalyst compositlons that are usefu] for polymerizing ethylene or copolymerizing ethylene with a comonomer~ thereby producing a high molecular weight-high density ethylene polymer that is useful for making a film that has good film properties and that can be processed at high production rates and thin gauges.
- In accordance with one embodiment of this invention a chromium catalyst composition is provided. This chromium cfltalyst composition comprises at least two chromium catfllyst systems:
(a) One of these chromium catalyst systems comprises chromium and a support. The amount of chromium in this catfllyst system is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system. The support comprises silica snd titania. The support has a pore volume from about 2 to flbout 3 cubic centimeters per gram and a surface area from about 400 to about 600 square meters per gram.
(b) Another one of these chromium catalyst systems also comprises chromium and a support. The amount of chromium in this catalyst system is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system. The support also comprises silica and titania. The support has a pore volume from about 0.7 to about 1.4 cubic centimeters per gram, and a surface area from about 300 to about 400 square meters per gram.
In accordance with another embodiment of this invention the above embodiment of the invention can he contacted with ethylene or with ethylene and another comonomer, under polymerization conditions, to produce a homopolymer or a copolymer.
The invention as disclosed in this application can be suitably practiced in the absence of any steps, components, compounds, or ingredients not disclosed herein.
(a) One of these chromium catalyst systems comprises chromium and a support. The amount of chromium in this catfllyst system is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system. The support comprises silica snd titania. The support has a pore volume from about 2 to flbout 3 cubic centimeters per gram and a surface area from about 400 to about 600 square meters per gram.
(b) Another one of these chromium catalyst systems also comprises chromium and a support. The amount of chromium in this catalyst system is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system. The support also comprises silica and titania. The support has a pore volume from about 0.7 to about 1.4 cubic centimeters per gram, and a surface area from about 300 to about 400 square meters per gram.
In accordance with another embodiment of this invention the above embodiment of the invention can he contacted with ethylene or with ethylene and another comonomer, under polymerization conditions, to produce a homopolymer or a copolymer.
The invention as disclosed in this application can be suitably practiced in the absence of any steps, components, compounds, or ingredients not disclosed herein.
DETAILED DESCRIPTION OF THE INVENTION
In general, the chromium cfltalyst compositions used in this invention comprise at least two chromium cataly~t systems. These chromium catalyst systems comprise a chromium component and a support component. The support component comprises silica and titanifl. The term "support" is not meant to be construed as an inert component.
The Chromium Catalyst System that has a High Pore Volume Support The amount of chromium in this chromium catalyst system is from about 0.5 weight percent to about 1 weight percent based on the total weight of the catalyst system (hereafter "Catalyst System XX").
If substantially less than 0.5 weight percent of chromium is used, the catalyst system will have an undesirably low activity. If substantially more than 1 weight percent is used, the catalyst system will produce a resin that will have an undesirable amount of long chain branching. A
resin with an undesirable amount of long chain branching would be less desirable for film applications because of lower film properties such as tear resistance in the transverse direction. Additionally, having a substantially higher amount of chromium in the catalyst system could impart an undesired color to the resin.
The support comprises silica and titania. The amount of titania is from about 2 weight percent to about 10 weight percent based on the total weight of the support. If substantially less than 2 weight percent of titanium is used, the molecular weight distribution of a resulting resin will be too narrow. If substantially more than 10 weight percent is used, the catalyst system will have an undesirably low activity. The amount of silica is from about 80 to about 98 weight percent based on the total weight of the support. Other components can 2 1 2 4 7 3~ 33222CA
be present in the support, provided that, they do not adversely affect the properties of the support or adversely affect the properties of the resins produced.
The support should have a pore volume from about 2 cubic centimeters per gram to about 3 centimeters per gram. If the pore volume is substantially less than s 2 cubic centimeters per gram, the melt index of a resulting resin will be undesirably low. If the pore volume is substantially more than 3 cubic centimeters per gram the catalyst system will be to soft to handle.
The support should have a surface area from about 400 square meters per gram to about 600 square meters per gram. If the surface area is substantially less o than about 400 square meters per gram, the catalyst will have an undesirably low polymerization activity and the amount of long chain branching in a resulting resin will be undesirably increased. If the surface area is more than 600 square meters per gram, the catalyst will substantially lose its melt index potential and the catalyst will have an undesirably low polymerization activity.
1 5 These catalyst systems can be produced in accordance with the procedures disclosed in U.S. Patents 3,887,494; 3,900,457; and 4,119,569.
The Chromium Catalyst System that has a Low Pore Volume Support The amount of chromium in this catalyst system is from about 2 o 1 weight percent to about 1.5 weight percent based on the total weight of the catalyst system (hereafter "Catalyst YY"). If substantially less than 1 weight percent of chromium is used, the amount of long chain branching desired in the resulting resin will not be achieved and when 212 ~ 7 3 2 the resin is blown into a film, the bl]bble will be less stable. If substantially more thfln 1.5 weight percent is used, the resulting resin could have an undesirable color imparted to it.
The support comprises silica and titania. The amount of titania is from about 2 weight percent to about lO weight percent based on the total weight of the support. If substantially less than 2 weight percent of titanium is used, the molecular weight distribution of a resulting resin will be too narrow. If substantially more than 10 weight percent is used, the catalyst system will have an undesirably low activity. The amount of silica is from flbout 80 to about 98 weight percent based on the total weight of the support. Other components can be present in the support, provided that, they do not adversely affect the properties of the support or adversely affect the properties of the resins produced.
The support should have a pore volume from about 0.7 cubic centimeters per gram to about 1.4 centimeters per gram. If the pore volume is substantially less than 0.7 cubic centimeters per gram, the catalyst system will have an undesirably low activity. If the pore volume is substantially more than 1.4 cubic centimeters per gram the bulk density of the catalyst will decrease undesirably and the amount of long chain branching in the resulting resin will decrease undesirably.
It is preferable if the pore volume is from about 0.8 to about 1.2 cubic centimeters per gram for best control of long chain branching and film properties.
The support should have a surface area from about 300 square meters per gram to about 400 square meters per gram. If the surface area is substantially less than about 300 square meters per gram, the catalyst will have an undesirably low activity. If the surface area is more than 400 square meters per gram, the resulting resin will have an undesirably low film processability.
These catalyst systems can be produced in accordance with the procedures disclosed in U.S. Patent 4,981,831.
It is plerelled if the amount of titania in each support is substantially the same. If the amount of titania is not substantially the same, the molecular weight distributions of each of the resulting polymers will be undesirably different.
The surface area and pore volume of the supports can be determined by nitrogen sorption by a person with ordinary skill in the art. For example, the following 1 o references can be used "Adsorption, Surface Area and Porosity" by S.J. Gregg and K.S.W. Sing, Academic Press, London (1982); and "Introduction to Powder Surface Area" by S. Lowell, J. Wiley & Sons, New York, NY (1979); the disclosures of which are hereby incorporated by reference. Additionally, a "Quantachrome Autosorb-6 Nitrogen Pore Size Distribution Instrument" can be used to help determine surface areas and pore volumes of the supports. This instrument (or similar instrument) is available from the Quantachrome Corporation, Sysset, New York.
Once the chromium catalyst systems are made they can be combined in any manner known in the art. For example, they can be dry blended together in a mixer or added to a feed stream that leads to a reactor. The weight ratio of Catalyst 2 o XX to Catalyst YY can vary from 99: 1 to 1 :99 depending on the properties desired in the resin. In general, using more of Catalyst XX produces a resin that has better film plol)el~ies, whereas, using more of Catalyst YY produces a resin that has a better bubble stability during film production. It is plerelled if the weight ratio of Catalyst XX to Catalyst YY is from about 6: 1 to about 1: 1; more preferably it is about 5: 1 to about 2: 1 in order to promote the production of resins with good film properties and good film processability.
It should be noted that after the catalyst systems are combined they can be activated together at the same temperature. They can also be separately activated and then combined. However, if they are separately activated the temperature at which each activation takes place should not be substantially different, otherwise, the molecular weight distributions of each of the resulting polymers will be undesirably dirre~
The chromium catalyst compositions used in this invention can be used to homopolymerize ethylene or to copolymerize ethylene with another comonomer.
Suitable comonomers are those olefins having from 3 to about 20 carbon atoms. It is preferable if these olefins are l-olefins. Suitable examples of these olefins include propylene, l-butene, 3-methyl-1-butene, l-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, l-hexene, 3-ethyl-1-hexene, l-octene, l-decene, and mixtures thereof.
Various polymerization schemes are known in the art. For example, U.S.
Patents 2,825,721; 3,152,872; 3,172,737; 3,203,766; 3,225,023; 3,226,205; 3,242,150;
3,248,179; and 4,121,029 disclose several polymerization schemes. A particularly2 o preferred polymerization scheme is the slurry or particle form polymerization method.
This method is disclosed, for example, in U.S. Patent 3,248,179.
The substantially monomodal, high molecular weight-high density ethylene polymer resins produced using the chromium catalyst composIt~ons disclosed herein can be m~de into fi]ms that have competitive film properties and good proces.sflbility. These resins will have a high load melt index from about I to flbout 20 (preferably about 5 to about 15) grams per ten minutes, when measured in accordance with ASTM D-1238 65T. Additionally, these resins will have a density from about 0.94 to about 0.97 (preferably about 0.945 to about 0.955) grams per cubic centimeter, when measured in accordance with ASTH D-1505-85.
EXAMPLE
This example is provided to further assist a person skilled in the art with understanding this invention. This example is intended to be illustrative of the invention and is not meant to be construed as limiting the scope of the invention.
Part One The following chromium catalyst composition was used to copolymerize ethylene and l-hexene:
(1) A chromium catalyst system that had a high pore volume silica-titania (2.5 weight percent titania) support was purchased from the W.R. Grace Corporation. It had a surface area of about 550 square meters per gram and a pore volume of about 2.5 cubic centimeters per gram. It also had a chromium content of about 1 weight percent based on the weight of the chromium catalyst system; and (2) A chromium catalyst system that had a low pore volume silica-titania (2.3 weight percent titflnia) support was purchased from the W.R. Grace Corporation. It had A surface area of about 360 square meters per gram and a pore volume of about 1.1 cubic centimeters per lo 2124732 gram. It also had a chromium content of About l.t weight percent based on the weight of the chromium cfltalyst system.
These two catalyst systems were then mlxed together and activated by subjectlng them to air flt 650 degrees Celsius.
The copolymeri~ation was conducted in an 87 liter, 15.2 centimeter pipe loop reactor. The copotymer was recovered in a flash chamber and a Vulcan dryer was used to dry the copolymer.
Ethylene that hAd been dried over alumina was used as the polymerization monomer. l-hexene that had been dried over alumina was used as the comonomer. Isobutane thst had been degassed by fractionation and dried over aluminfl WAS used as the diluent. The copolymerization was conducted at about 100 degrees Celsius and lasted for about one hour.
The ethylene-l-hexene copolymer produced was then evaluated as a film resin. The film blowing conditions were as follows:
1. a die gap of 0.035 inches;
2. a four to one blow up ratio;
3. a fourteen inch frost line height;
4. a screw speed of 75 revolutions per minute; And 5. an extruder temperature of 220 degrees Celsius.
The resin was blown into a one mil film (except when it was down gauged) and compared to other fi]m resins. The results are presented below.
,l 2124732 TA~LF. t Material A~ -B-2 C3 Sl4 S25 HLMI (dg/min)6 7.5 6.4 8.9 8.7 8.8 MI (dg/min)8 0.07 0.04 0.08 - -Density (gms/cc)3 0.9531 0.9509 0.949 0.953 0.951Screw RPM 75 75 75 75 75 Melt temp. (~C) 242 241 234 242 240 Rate (lb/hr) 38.9 38.9 40.5 34.2 35.1 Extruder (kW) 5.1 5.l 4.9 4.5 4.5 Die pressure (psi) 2950 3100 2700 3400 3400 Line speed (ft/min) 64 64 67 57 57 Gauge (mils) I t Maximum line speed* (ft/min) - - 124s 103s lOOs Gauge @ max. speed (mils) - - 0.5 0.5 0.5 Breathing9 Dancing~~ 2 2 1 2 2 Streaks11 2 2 2 1 2 Surgingl2 Bubble symmetry~ 3 l 1 l 1 2 Gel uniformity'4 3 2 l 2 2 TOTAL1s lO 9 7 8 lO
*s indicates a stable bubble at the maximum line speed shown.
AAAAAAbAA,SAAAhbAAAA~S,SAA~S,SAA~S,S,SAAAAAAAAAAAAAAAAA.SAA~SA,SAAAAAAAAAAAAA~SAAAAA
12 212 l732 Table Notes:
1. This is a film produced from a resin that was made by copolymerizing ethylene and l-hexene with only Catalyst XX.
2. This is a film produced from fl resin that was made by copolymerizing ethylene and l-hexene with only Catalyst YY.
3. This is the inventive film produced from the inventive resin that was made from the inventive catalyst composition.
4. This is an industry standflrd film resin.
5. This is another industry standard film resin.
In general, the chromium cfltalyst compositions used in this invention comprise at least two chromium cataly~t systems. These chromium catalyst systems comprise a chromium component and a support component. The support component comprises silica and titanifl. The term "support" is not meant to be construed as an inert component.
The Chromium Catalyst System that has a High Pore Volume Support The amount of chromium in this chromium catalyst system is from about 0.5 weight percent to about 1 weight percent based on the total weight of the catalyst system (hereafter "Catalyst System XX").
If substantially less than 0.5 weight percent of chromium is used, the catalyst system will have an undesirably low activity. If substantially more than 1 weight percent is used, the catalyst system will produce a resin that will have an undesirable amount of long chain branching. A
resin with an undesirable amount of long chain branching would be less desirable for film applications because of lower film properties such as tear resistance in the transverse direction. Additionally, having a substantially higher amount of chromium in the catalyst system could impart an undesired color to the resin.
The support comprises silica and titania. The amount of titania is from about 2 weight percent to about 10 weight percent based on the total weight of the support. If substantially less than 2 weight percent of titanium is used, the molecular weight distribution of a resulting resin will be too narrow. If substantially more than 10 weight percent is used, the catalyst system will have an undesirably low activity. The amount of silica is from about 80 to about 98 weight percent based on the total weight of the support. Other components can 2 1 2 4 7 3~ 33222CA
be present in the support, provided that, they do not adversely affect the properties of the support or adversely affect the properties of the resins produced.
The support should have a pore volume from about 2 cubic centimeters per gram to about 3 centimeters per gram. If the pore volume is substantially less than s 2 cubic centimeters per gram, the melt index of a resulting resin will be undesirably low. If the pore volume is substantially more than 3 cubic centimeters per gram the catalyst system will be to soft to handle.
The support should have a surface area from about 400 square meters per gram to about 600 square meters per gram. If the surface area is substantially less o than about 400 square meters per gram, the catalyst will have an undesirably low polymerization activity and the amount of long chain branching in a resulting resin will be undesirably increased. If the surface area is more than 600 square meters per gram, the catalyst will substantially lose its melt index potential and the catalyst will have an undesirably low polymerization activity.
1 5 These catalyst systems can be produced in accordance with the procedures disclosed in U.S. Patents 3,887,494; 3,900,457; and 4,119,569.
The Chromium Catalyst System that has a Low Pore Volume Support The amount of chromium in this catalyst system is from about 2 o 1 weight percent to about 1.5 weight percent based on the total weight of the catalyst system (hereafter "Catalyst YY"). If substantially less than 1 weight percent of chromium is used, the amount of long chain branching desired in the resulting resin will not be achieved and when 212 ~ 7 3 2 the resin is blown into a film, the bl]bble will be less stable. If substantially more thfln 1.5 weight percent is used, the resulting resin could have an undesirable color imparted to it.
The support comprises silica and titania. The amount of titania is from about 2 weight percent to about lO weight percent based on the total weight of the support. If substantially less than 2 weight percent of titanium is used, the molecular weight distribution of a resulting resin will be too narrow. If substantially more than 10 weight percent is used, the catalyst system will have an undesirably low activity. The amount of silica is from flbout 80 to about 98 weight percent based on the total weight of the support. Other components can be present in the support, provided that, they do not adversely affect the properties of the support or adversely affect the properties of the resins produced.
The support should have a pore volume from about 0.7 cubic centimeters per gram to about 1.4 centimeters per gram. If the pore volume is substantially less than 0.7 cubic centimeters per gram, the catalyst system will have an undesirably low activity. If the pore volume is substantially more than 1.4 cubic centimeters per gram the bulk density of the catalyst will decrease undesirably and the amount of long chain branching in the resulting resin will decrease undesirably.
It is preferable if the pore volume is from about 0.8 to about 1.2 cubic centimeters per gram for best control of long chain branching and film properties.
The support should have a surface area from about 300 square meters per gram to about 400 square meters per gram. If the surface area is substantially less than about 300 square meters per gram, the catalyst will have an undesirably low activity. If the surface area is more than 400 square meters per gram, the resulting resin will have an undesirably low film processability.
These catalyst systems can be produced in accordance with the procedures disclosed in U.S. Patent 4,981,831.
It is plerelled if the amount of titania in each support is substantially the same. If the amount of titania is not substantially the same, the molecular weight distributions of each of the resulting polymers will be undesirably different.
The surface area and pore volume of the supports can be determined by nitrogen sorption by a person with ordinary skill in the art. For example, the following 1 o references can be used "Adsorption, Surface Area and Porosity" by S.J. Gregg and K.S.W. Sing, Academic Press, London (1982); and "Introduction to Powder Surface Area" by S. Lowell, J. Wiley & Sons, New York, NY (1979); the disclosures of which are hereby incorporated by reference. Additionally, a "Quantachrome Autosorb-6 Nitrogen Pore Size Distribution Instrument" can be used to help determine surface areas and pore volumes of the supports. This instrument (or similar instrument) is available from the Quantachrome Corporation, Sysset, New York.
Once the chromium catalyst systems are made they can be combined in any manner known in the art. For example, they can be dry blended together in a mixer or added to a feed stream that leads to a reactor. The weight ratio of Catalyst 2 o XX to Catalyst YY can vary from 99: 1 to 1 :99 depending on the properties desired in the resin. In general, using more of Catalyst XX produces a resin that has better film plol)el~ies, whereas, using more of Catalyst YY produces a resin that has a better bubble stability during film production. It is plerelled if the weight ratio of Catalyst XX to Catalyst YY is from about 6: 1 to about 1: 1; more preferably it is about 5: 1 to about 2: 1 in order to promote the production of resins with good film properties and good film processability.
It should be noted that after the catalyst systems are combined they can be activated together at the same temperature. They can also be separately activated and then combined. However, if they are separately activated the temperature at which each activation takes place should not be substantially different, otherwise, the molecular weight distributions of each of the resulting polymers will be undesirably dirre~
The chromium catalyst compositions used in this invention can be used to homopolymerize ethylene or to copolymerize ethylene with another comonomer.
Suitable comonomers are those olefins having from 3 to about 20 carbon atoms. It is preferable if these olefins are l-olefins. Suitable examples of these olefins include propylene, l-butene, 3-methyl-1-butene, l-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, l-hexene, 3-ethyl-1-hexene, l-octene, l-decene, and mixtures thereof.
Various polymerization schemes are known in the art. For example, U.S.
Patents 2,825,721; 3,152,872; 3,172,737; 3,203,766; 3,225,023; 3,226,205; 3,242,150;
3,248,179; and 4,121,029 disclose several polymerization schemes. A particularly2 o preferred polymerization scheme is the slurry or particle form polymerization method.
This method is disclosed, for example, in U.S. Patent 3,248,179.
The substantially monomodal, high molecular weight-high density ethylene polymer resins produced using the chromium catalyst composIt~ons disclosed herein can be m~de into fi]ms that have competitive film properties and good proces.sflbility. These resins will have a high load melt index from about I to flbout 20 (preferably about 5 to about 15) grams per ten minutes, when measured in accordance with ASTM D-1238 65T. Additionally, these resins will have a density from about 0.94 to about 0.97 (preferably about 0.945 to about 0.955) grams per cubic centimeter, when measured in accordance with ASTH D-1505-85.
EXAMPLE
This example is provided to further assist a person skilled in the art with understanding this invention. This example is intended to be illustrative of the invention and is not meant to be construed as limiting the scope of the invention.
Part One The following chromium catalyst composition was used to copolymerize ethylene and l-hexene:
(1) A chromium catalyst system that had a high pore volume silica-titania (2.5 weight percent titania) support was purchased from the W.R. Grace Corporation. It had a surface area of about 550 square meters per gram and a pore volume of about 2.5 cubic centimeters per gram. It also had a chromium content of about 1 weight percent based on the weight of the chromium catalyst system; and (2) A chromium catalyst system that had a low pore volume silica-titania (2.3 weight percent titflnia) support was purchased from the W.R. Grace Corporation. It had A surface area of about 360 square meters per gram and a pore volume of about 1.1 cubic centimeters per lo 2124732 gram. It also had a chromium content of About l.t weight percent based on the weight of the chromium cfltalyst system.
These two catalyst systems were then mlxed together and activated by subjectlng them to air flt 650 degrees Celsius.
The copolymeri~ation was conducted in an 87 liter, 15.2 centimeter pipe loop reactor. The copotymer was recovered in a flash chamber and a Vulcan dryer was used to dry the copolymer.
Ethylene that hAd been dried over alumina was used as the polymerization monomer. l-hexene that had been dried over alumina was used as the comonomer. Isobutane thst had been degassed by fractionation and dried over aluminfl WAS used as the diluent. The copolymerization was conducted at about 100 degrees Celsius and lasted for about one hour.
The ethylene-l-hexene copolymer produced was then evaluated as a film resin. The film blowing conditions were as follows:
1. a die gap of 0.035 inches;
2. a four to one blow up ratio;
3. a fourteen inch frost line height;
4. a screw speed of 75 revolutions per minute; And 5. an extruder temperature of 220 degrees Celsius.
The resin was blown into a one mil film (except when it was down gauged) and compared to other fi]m resins. The results are presented below.
,l 2124732 TA~LF. t Material A~ -B-2 C3 Sl4 S25 HLMI (dg/min)6 7.5 6.4 8.9 8.7 8.8 MI (dg/min)8 0.07 0.04 0.08 - -Density (gms/cc)3 0.9531 0.9509 0.949 0.953 0.951Screw RPM 75 75 75 75 75 Melt temp. (~C) 242 241 234 242 240 Rate (lb/hr) 38.9 38.9 40.5 34.2 35.1 Extruder (kW) 5.1 5.l 4.9 4.5 4.5 Die pressure (psi) 2950 3100 2700 3400 3400 Line speed (ft/min) 64 64 67 57 57 Gauge (mils) I t Maximum line speed* (ft/min) - - 124s 103s lOOs Gauge @ max. speed (mils) - - 0.5 0.5 0.5 Breathing9 Dancing~~ 2 2 1 2 2 Streaks11 2 2 2 1 2 Surgingl2 Bubble symmetry~ 3 l 1 l 1 2 Gel uniformity'4 3 2 l 2 2 TOTAL1s lO 9 7 8 lO
*s indicates a stable bubble at the maximum line speed shown.
AAAAAAbAA,SAAAhbAAAA~S,SAA~S,SAA~S,S,SAAAAAAAAAAAAAAAAA.SAA~SA,SAAAAAAAAAAAAA~SAAAAA
12 212 l732 Table Notes:
1. This is a film produced from a resin that was made by copolymerizing ethylene and l-hexene with only Catalyst XX.
2. This is a film produced from fl resin that was made by copolymerizing ethylene and l-hexene with only Catalyst YY.
3. This is the inventive film produced from the inventive resin that was made from the inventive catalyst composition.
4. This is an industry standflrd film resin.
5. This is another industry standard film resin.
6. This is the High Load Melt Index meflsured in accordance with ASTM
D-1238 65T.
D-1238 65T.
7. This is the Melt Index measured in accordance with ASTM D-1238 65T.
8. This is the Density measured in accordance with ASTM D-1505-85.
Items 9-15 are qualitative observations of the bubble during film production. The range in results is from 1 to 4. A "1" means that the defect is not detectable or barely visible. A "2" means that the defect is visible but it is not serious. A "3" means that the defect is not acceptable but the resin could be processed. A "4" means that the defect is so bad that it would shut down the line.
Items 9-15 are qualitative observations of the bubble during film production. The range in results is from 1 to 4. A "1" means that the defect is not detectable or barely visible. A "2" means that the defect is visible but it is not serious. A "3" means that the defect is not acceptable but the resin could be processed. A "4" means that the defect is so bad that it would shut down the line.
9. This is a qualitative measure of the vertical instability in the frost line position.
10. This is a qualitative measure of the horizontal instability in the bubble.
11. This is a qualitative measure of the streaks present in the film, especially along port lines.
12. This is a qualitative measure of the stabi]ity of the resin through the extruder.
13 212~732 13. This is a qualitative measure of the ~symmetry of the bubble in three dimensions.
14. This is a qualitative measure of the imperfections in the film such as, chars, gels, applesauce, or other non-uniform appearance.
15. This is the total of the qualltative mea.sures.
AAAAAAbAhAAhAhhhhAhh,shbAAAAAA:hAAAAAhAAA:AAhAAAAAAAAAAAAAAhAAhhAAhAAhAAA
As can been seen from table one, inventive resin C processed extremely well. The bubble was stable flt high line speeds as well.
Furthermore, when the film was downgauged to a 0.5 mil thickness the line speed was 124 ft/min. with no .significant instabilities. Also, the out put rate was higher than the industry standards by about 5 lbs/hr which is a fairly significant difference on in this particular extrusion process.
Part Two:
Several more sample lots of the inventive resin were made according to the procedure in part one. These sample lots and an industry standard sample were then made into film on the same extrusion line. They were processed under different conditions in order to find the range of film properties each sflmple possessed. The results are presented below in table two.
TABLF. 2 Industry Inventive Samples Stflndard Several Lots Sample Total Energy Dart Drop ASTMD-4272 0.8-1.8 1.3-2.9 Elemendorf Tear (g) Tensile at Yleld (psi) Elastic Mod. (psi) hAAAAhAAAhAAAAAAAAAAAAAAbAA~SA,:A~SAAAAAAAA,::AAA,SAAAS,SAAhAA,:AAAAhAAAAAAAAAA
As can be seen from the flbove results the properties of the monomodal inventive resins are competitive with the multicomponent industry standard resin.
AAAAAAbAhAAhAhhhhAhh,shbAAAAAA:hAAAAAhAAA:AAhAAAAAAAAAAAAAAhAAhhAAhAAhAAA
As can been seen from table one, inventive resin C processed extremely well. The bubble was stable flt high line speeds as well.
Furthermore, when the film was downgauged to a 0.5 mil thickness the line speed was 124 ft/min. with no .significant instabilities. Also, the out put rate was higher than the industry standards by about 5 lbs/hr which is a fairly significant difference on in this particular extrusion process.
Part Two:
Several more sample lots of the inventive resin were made according to the procedure in part one. These sample lots and an industry standard sample were then made into film on the same extrusion line. They were processed under different conditions in order to find the range of film properties each sflmple possessed. The results are presented below in table two.
TABLF. 2 Industry Inventive Samples Stflndard Several Lots Sample Total Energy Dart Drop ASTMD-4272 0.8-1.8 1.3-2.9 Elemendorf Tear (g) Tensile at Yleld (psi) Elastic Mod. (psi) hAAAAhAAAhAAAAAAAAAAAAAAbAA~SA,:A~SAAAAAAAA,::AAA,SAAAS,SAAhAA,:AAAAhAAAAAAAAAA
As can be seen from the flbove results the properties of the monomodal inventive resins are competitive with the multicomponent industry standard resin.
Claims (16)
1. A process to produce an ethylene homopolymer or an ethylene copolymer said process comprising polymerizing ethylene or copolymerizing ethylene and at least one comonomer, wherein said comonomer is an olefin having from 3 to about 20 carbon atoms, with a chromium catalyst composition that comprises at least two chromium catalyst systems wherein:
(a) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 0.7 to about 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram.
(a) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 0.7 to about 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram.
2. A process according to claim 1 wherein said supports in (a) and (b) consist essentially of silica and titania.
3. A process according to claim 1 wherein said supports in (a) and (b) consist of silica and titania.
4. A process according to claim 1 wherein said support in (b) has a pore volume from about 0.8 to about 1.2 cubic centimeters per gram.
5. A process according to claim 4 wherein said supports in (a) and (b) consist essentially of silica and titania.
6. A process according to claim 4 wherein said supports in (a) and (b) consist of silica and titania.
7. A process to produce an ethylene homopolymer or ethylene copolymer said process comprising polymerizing ethylene or copolymerizing ethylene and at least one comonomer, wherein said comonomer is an olefin having from 3 to about 20 carbon atoms, with a chromium catalyst composition that consists essentially of two chromium catalyst systems wherein:
(a) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 0.7 to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram.
(a) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 0.7 to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram.
8. A process according to claim 7 wherein said supports in (a) and (b) consist of silica and titania.
9. A process according to claim 7 wherein said supports in (a) and (b) has a pore volume from about 0.8 to about 1.2 cubic centimeters per gram.
10. A process according to claim 9 wherein said supports in (a) and (b) consist of silica and titania.
11. A process to produce an ethylene homopolymer or ethylene copolymer said process comprising polymerizing ethylene or copolymerizing ethylene and at least one comonomer, wherein said comonomer is an olefin having from 3 to about 20 carbon atoms, with a chromium catalyst composition that comprises at least two chromium catalyst systems wherein:
(a) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 0.7 but less than or equal to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram wherein said ethylene homopolymer or said ethylene copolymer has a high load melt index from about 1 but equal to or less than 15 grams per 10 minutes.
(a) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) at least one of said chromium catalyst systems comprises chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support comprises silica and titania, and wherein said support has a pore volume from about 0.7 but less than or equal to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram wherein said ethylene homopolymer or said ethylene copolymer has a high load melt index from about 1 but equal to or less than 15 grams per 10 minutes.
12. A process according to claim 11 wherein said ethylene homopolymer or said ethylene copolymer has a density from about 0.94 grams per cubic centimeter but less than 0.957 grams per cubic centimeter.
13. A process according to claim 12 wherein said ethylene homopolymer or said ethylene copolymer has a density from about 0.94 to about 0.955 grams per cubic centimeter.
14. A process to produce an ethylene homopolymer or ethylene copolymer said process comprising polymerizing ethylene or copolymerizing ethylene and at least one comonomer, wherein said comonomer is an olefin having from 3 to about 20 carbon atoms, with a chromium catalyst composition that consists essentially of two chromium catalyst systems wherein:
(a) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 0.7 but less than or equal to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram wherein said ethylene homopolymer or said ethylene copolymer has a high load melt index from about 1 but equal to or less than 15 grams per 10 minutes.
(a) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 0.5 to about 1 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 2 to about 3 cubic centimeters per gram, and wherein said support has a surface area from about 400 to about 600 square meters per gram; and (b) one of said chromium catalyst systems consists essentially of chromium and a support, and wherein the amount of said chromium is from about 1 to about 1.5 weight percent based on the total weight of said catalyst system, and wherein said support consists essentially of silica and titania, and wherein said support has a pore volume from about 0.7 but less than or equal to 1.4 cubic centimeters per gram, and wherein said support has a surface area from about 300 to about 400 square meters per gram wherein said ethylene homopolymer or said ethylene copolymer has a high load melt index from about 1 but equal to or less than 15 grams per 10 minutes.
15. A process according to claim 14 wherein said ethylene homopolymer or said ethylene copolymer has a density from about 0.94 grams per cubic centimeter but less than 0.957 grams per cubic centimeter.
16. A process according to claim 14 wherein said ethylene homopolymer or said ethylene copolymer has a density from about 0.94 to about 0.955 grams per cubic centimeter.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US08/134,765 US5508362A (en) | 1993-10-08 | 1993-10-08 | Chromium catalyst compositions and polymerization processes therewith |
| US08/134,765 | 1993-10-08 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2124732A1 CA2124732A1 (en) | 1995-04-09 |
| CA2124732C true CA2124732C (en) | 1998-09-29 |
Family
ID=22464889
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002124732A Expired - Fee Related CA2124732C (en) | 1993-10-08 | 1994-05-31 | Chromium catalyst compositions and polymerization processes therewith |
Country Status (14)
| Country | Link |
|---|---|
| US (2) | US5508362A (en) |
| EP (1) | EP0647661B2 (en) |
| JP (1) | JPH07188324A (en) |
| KR (1) | KR100340914B1 (en) |
| CN (2) | CN1036523C (en) |
| AU (1) | AU663656B2 (en) |
| CA (1) | CA2124732C (en) |
| DE (1) | DE69409055T3 (en) |
| ES (1) | ES2113593T5 (en) |
| FI (1) | FI944700A (en) |
| HU (1) | HU214900B (en) |
| NO (1) | NO306410B1 (en) |
| TR (1) | TR28158A (en) |
| ZA (1) | ZA945476B (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5714424A (en) * | 1995-01-09 | 1998-02-03 | W. R. Grace & Co.-Conn. | Multi-component polyolefin catalysts |
| US5895770A (en) * | 1995-02-28 | 1999-04-20 | Pq Corporation | Olefin polymerization catalysts with specific silica supports |
| EP0849293A1 (en) * | 1996-12-20 | 1998-06-24 | Fina Research S.A. | Production of polyethylene having a bimodal molecular weight distribution |
| EP0882740A1 (en) | 1997-06-06 | 1998-12-09 | Fina Research S.A. | Titanated chromium-based catalysts to produce polyethylene exhibiting better environmental stress crack resistance |
| EP0882743B1 (en) * | 1997-06-06 | 2003-11-12 | ATOFINA Research | Titanated chromium-based catalysts to produce polyethylene |
| US6204346B1 (en) * | 1998-12-17 | 2001-03-20 | Phillips Petroleum Co. | Polymerization process |
| EP1041089A1 (en) | 1999-03-29 | 2000-10-04 | Fina Research S.A. | Production of polyethylene |
| US6828268B1 (en) * | 1999-11-05 | 2004-12-07 | Phillips Petroleum Company | Polymerization catalyst systems and processes using alkyl lithium compounds as a cocatalyst |
| GB9928176D0 (en) | 1999-11-29 | 2000-01-26 | Borealis Polymers Oy | Polymer |
| DE60121758T2 (en) * | 2000-05-19 | 2006-12-21 | Ineos Europe Ltd., Staines | PROCESS FOR THE GAS PHASE POLYMERIZATION OF OLEFINES |
| KR100476481B1 (en) * | 2002-09-19 | 2005-03-17 | 엘지전자 주식회사 | Method For Transmitting Message Between Signaling Points In No.7 Signaling Network |
| GB0326415D0 (en) * | 2003-11-12 | 2003-12-17 | Solvay | Polymer of ethylene |
| US6982304B2 (en) | 2003-12-22 | 2006-01-03 | Union Carbide Chemicals & Plastics Technology Corporation | Blow molding resins with improved ESCR |
| US8399580B2 (en) | 2010-08-11 | 2013-03-19 | Chevron Philips Chemical Company Lp | Additives to chromium catalyst mix tank |
| WO2016141020A1 (en) * | 2015-03-02 | 2016-09-09 | Equistar Chemicals, Lp | Catalysts and methods of controlling long chain branching in polyolefins |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3135809A (en) * | 1960-07-21 | 1964-06-02 | Southern Res Inst | Isomerization process |
| US3165504A (en) † | 1961-02-27 | 1965-01-12 | Phillips Petroleum Co | Catalyst and process for producing olefin polymers |
| US3378536A (en) * | 1964-09-24 | 1968-04-16 | Phillips Petroleum Co | Polymerization process using a catalyst comprising a supported diarene metal and supported chromium oxide |
| US3900457A (en) † | 1970-10-08 | 1975-08-19 | Phillips Petroleum Co | Olefin polymerization catalyst |
| US3887494A (en) * | 1970-11-12 | 1975-06-03 | Phillips Petroleum Co | Olefin polymerization catalyst |
| US3798202A (en) * | 1971-10-12 | 1974-03-19 | Phillips Petroleum Co | Polyolefin production |
| BE789870A (en) † | 1972-10-09 | 1973-04-09 | Nat Petro Chem | Olefins polymn catalyst - consisting of chromium oxide deposited on two silica supports with different pore volumes/sizes |
| US4119569A (en) * | 1973-05-24 | 1978-10-10 | Phillips Petroleum Company | Olefin polymerization catalyst |
| US3959178A (en) * | 1974-03-28 | 1976-05-25 | Phillips Petroleum Company | Mixed hydrocarbyloxide treated catalyst activated at different temperatures |
| US3947433A (en) * | 1974-05-13 | 1976-03-30 | Phillips Petroleum Company | Supported chromium oxide catalyst having mixed adjuvant |
| US4053436A (en) † | 1975-08-26 | 1977-10-11 | Phillips Petroleum Company | Spray dried titanium-containing catalyst for stress crack resistant polymer |
| US4325839A (en) * | 1979-12-21 | 1982-04-20 | Phillips Petroleum Company | Impregnated second valence chromium compound in supported catalyst |
| US4285834A (en) * | 1979-12-31 | 1981-08-25 | The Dow Chemical Company | Dual, independently supported catalyst mixtures |
| US4461873A (en) * | 1982-06-22 | 1984-07-24 | Phillips Petroleum Company | Ethylene polymer blends |
| US4659690A (en) * | 1983-12-23 | 1987-04-21 | Phillips Petroleum Company | Acid agglomeration of refractory gel in polar organic diluent |
| US4672096A (en) * | 1984-04-04 | 1987-06-09 | Mobil Oil Corporation | Catalyst composition for polymerizing alpha-olefins |
| US4806513A (en) * | 1984-05-29 | 1989-02-21 | Phillips Petroleum Company | Silicon and fluorine-treated alumina containing a chromium catalyst and method of producing same |
| US4560733A (en) * | 1984-10-01 | 1985-12-24 | Phillips Petroleum Company | Polymerization and catalyst |
| US4981927A (en) * | 1987-05-20 | 1991-01-01 | National Distillers And Chemical Corporation | Chromium catalyst compositions and polymerization utilizing same |
| CA1307619C (en) * | 1987-05-20 | 1992-09-15 | Louis J. Rekers | Chromium catalyst compositions and polymerization utilizing same |
| US5198400A (en) * | 1987-05-20 | 1993-03-30 | Quantum Chemical Corporation | Mixed chromium catalysts and polymerizations utilizing same |
| CA1309801C (en) * | 1987-09-18 | 1992-11-03 | Elizabeth A. Boggs | Process for olefin polymerization |
| US4981831A (en) * | 1988-07-25 | 1991-01-01 | Phillips Petroleum Company | Twice-aged porous inorganic oxides, catalysts, and polymerization processes |
-
1993
- 1993-10-08 US US08/134,765 patent/US5508362A/en not_active Expired - Lifetime
-
1994
- 1994-05-31 CA CA002124732A patent/CA2124732C/en not_active Expired - Fee Related
- 1994-07-25 ZA ZA945476A patent/ZA945476B/en unknown
- 1994-08-04 AU AU68875/94A patent/AU663656B2/en not_active Ceased
- 1994-08-24 KR KR1019940020948A patent/KR100340914B1/en not_active IP Right Cessation
- 1994-08-25 JP JP6200920A patent/JPH07188324A/en active Pending
- 1994-09-24 CN CN94116495A patent/CN1036523C/en not_active Expired - Fee Related
- 1994-10-07 EP EP94115883A patent/EP0647661B2/en not_active Expired - Lifetime
- 1994-10-07 DE DE69409055T patent/DE69409055T3/en not_active Expired - Fee Related
- 1994-10-07 FI FI944700A patent/FI944700A/en not_active Application Discontinuation
- 1994-10-07 NO NO943812A patent/NO306410B1/en not_active IP Right Cessation
- 1994-10-07 ES ES94115883T patent/ES2113593T5/en not_active Expired - Lifetime
- 1994-10-07 HU HU9402901A patent/HU214900B/en not_active IP Right Cessation
- 1994-10-07 TR TR01048/94A patent/TR28158A/en unknown
-
1995
- 1995-05-25 US US08/450,184 patent/US5654249A/en not_active Expired - Lifetime
-
1996
- 1996-09-19 CN CN96112334A patent/CN1152581A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| FI944700A0 (en) | 1994-10-07 |
| NO306410B1 (en) | 1999-11-01 |
| DE69409055D1 (en) | 1998-04-23 |
| US5508362A (en) | 1996-04-16 |
| HUT70080A (en) | 1995-09-28 |
| CN1106024A (en) | 1995-08-02 |
| EP0647661A1 (en) | 1995-04-12 |
| HU214900B (en) | 1998-07-28 |
| ES2113593T3 (en) | 1998-05-01 |
| KR100340914B1 (en) | 2002-11-29 |
| US5654249A (en) | 1997-08-05 |
| EP0647661B1 (en) | 1998-03-18 |
| KR950011478A (en) | 1995-05-15 |
| FI944700A (en) | 1995-04-09 |
| DE69409055T2 (en) | 1998-07-02 |
| EP0647661B2 (en) | 2002-01-23 |
| ZA945476B (en) | 1995-03-06 |
| HU9402901D0 (en) | 1995-02-28 |
| ES2113593T5 (en) | 2002-05-16 |
| CA2124732A1 (en) | 1995-04-09 |
| JPH07188324A (en) | 1995-07-25 |
| AU663656B2 (en) | 1995-10-12 |
| CN1152581A (en) | 1997-06-25 |
| DE69409055T3 (en) | 2002-08-14 |
| AU6887594A (en) | 1995-04-27 |
| TR28158A (en) | 1996-02-13 |
| NO943812L (en) | 1995-04-10 |
| CN1036523C (en) | 1997-11-26 |
| NO943812D0 (en) | 1994-10-07 |
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