Synthetic resins or natural rubbers -- part of the class 520 ser – Synthetic resins – Polymers from only ethylenic monomers or processes of...
Reexamination Certificate
1999-03-31
2001-05-15
Wu, David W. (Department: 1713)
Synthetic resins or natural rubbers -- part of the class 520 ser
Synthetic resins
Polymers from only ethylenic monomers or processes of...
C526S347000, C526S347100, C526S347200, C526S348300, C526S943000, C502S152000
Reexamination Certificate
active
06232415
ABSTRACT:
FIELD OF THE INVENTION
This invention is related to the field of polymers.
BACKGROUND OF THE INVENTION
One of the most important processes for the production of homopolymers of ethylene or copolymers of ethylene/monoolefin is called the slurry polymerization process. Usually, this process employs a diluent, such as, for example, isobutane. However, while this process is very versatile in producing these polymers, it has long been desirable to produce other polymers using this process. This is because of the cost saving that can be realized by utilizing the same commercial operating equipment to produce different polymers.
The invention herein is a step towards this direction.
SUMMARY OF THE INVENTION
It is an object of this invention to provide a process to produce a monovinylaromatic/monoolefin polymer.
It is another object of this invention to provide a monovinylaromatic/monoolefin polymer.
In accordance with this invention a process to produce a monovinylaromatic/monoolefin polymer is provided. Said process comprises polymerizing at least one monovinylaromatic and at least one monoolefin to form a monovinylaromatic/monoolefin polymer, wherein said polymerizing:
(1) is conducted using at least one M-catalyst;
(2) is conducted under polymerization conditions, where said polymerization conditions comprise a temperature from about 0° C. to about 300° C. and a pressure from about 100 kPa to about 10000 kPa;
(3) is conducted in a polymerization zone; and
(4) is conducted in the presence of isobutane.
In accordance with this invention a monovinylaromatic/monoolefin polymer is provided. Said monovinylaromatic/monoolefin polymer is produced by said process.
These objects and other objects of this invention are further disclosed in the following.
DETAILED DESCRIPTION OF THE INVENTION
The monovinylaromatic monomers that can be used in this invention contain from about 8 to about 20 carbon atoms. However, it is more preferred when these monomers contain about 8 to about 12 carbon atoms. Suitable examples of such monomers are styrene, alpha-methyl styrene, 2-methylstyrene, 3-methylstyrene, 4-methylstyrene, 2-ethylstyrene, 3 -ethylstyrene, 4-ethylstyrene, 4-n-propylstyrene, 2-t-butylstyrene, 2,4-dimethylstyrene, and 4-cyclohexylstyrene. Styrene is currently most preferred.
The monoolefin monomers that can be used in this invention contain from about 2 to about 20 carbon atoms. However, it is more preferred when these monomers contain about 2 to about 10 carbon atoms. It is most preferred when these monomers have 2 to 6 carbon atoms. Suitable examples of such monomers are ethylene, propylene, butene, pentene, and hexene. Ethylene is currently most preferred.
These monomers are polymerized using at least one M-catalyst. For the purposes of this invention M-catalyst is defined as those catalysts disclosed in U.S. Pat. No. 5,498,581, where said catalysts are made by the claimed methods. This patent is entitled “METHOD FOR MAKING AND USING A SUPPORTED METALLOCENE CATALYST SYSTEM” and issued on Mar. 12, 1996. The entire disclosure of U.S. Pat. No. 5,498,581, is hereby incorporated by reference. A suitable, and preferred, metallocene to use to produce the M-catalyst is ((9-fluorenyl) (cyclopentadienyl) (methyl) (3-butenyl) methane) zirconium dichloride.
The polymerizing is conducted under polymerization conditions. These polymerization conditions comprises a temperature and a pressure.
The temperature is from about 0° C. to about 300° C. However, it is more preferred when the temperature is from about 20° C. to about 200° C. and it is most preferred when the temperature is from 50° C. to 112° C.
The pressure is from about 100 kPa to about 10000 kPa. However, it is more preferred when the pressure is from about 500 kPa to about 6000 kPa and it is most preferred when the pressure is from 500 kPa to 5000 kPa.
The polymerizing is conducted in a polymerization zone. Currently, any reactor can be used for this polymerization. However, it is more preferred to use a loop slurry reactor. This reactors are well known in the polyethylene polymerization art.
It is most desirable to conduct the polymerization in the presence of isobutane which is the diluent in a slurry polymerization.
The monovinylaromatic/monoolefin polymer produced by this process comprises about 0.1 to about 90 weight percent polymerized monovinylaromatic based on the weight of the monovinylaromatic/monoolefin polymer. However, it is more preferred when the monovinylaromatic/monoolefin polymer produced by this process comprises about 0.5 to about 80 weight percent polymerized monovinylaromatic based on the weight of the monovinylaromatic/monoolefin polymer and it is most preferred when the monovinylaromatic/monoolefin polymer produced by this process comprises 1 to 80 weight percent polymerized monovinylaromatic based on the weight of the monovinylaromatic/monoolefin polymer.
The monovinylaromatic/monoolefin polymer produced by this process comprises about 10 to about 99.9 weight percent polymerized monoolefin based on the weight of the monovinylaromatic/monoolefin polymer. However, it is more preferred when the monovinylaromatic/monoolefin polymer produced by this process comprises about 20 to about 99.5 weight percent polymerized monoolefin based on the weight of the monovinylaromatic/monoolefin polymer and it is most preferred when the monovinylaromatic/monoolefin polymer produced by this process comprises 20 to 99 weight percent polymerized monoolefin based on the weight of the monovinylaromatic/monoolefin polymer.
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Ahmed Iqbal
Kuang Jianxin
Moczygemba George A.
Palackal Syriac J.
Welch M. Bruce
Bowman Edward L.
Harlan R.
Phillips Petroleum Company
Wu David W.
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