Synthetic resins or natural rubbers -- part of the class 520 ser – Synthetic resins – Polymerizing in tubular or loop reactor
Reexamination Certificate
2000-03-14
2001-10-09
Wu, David W. (Department: 1713)
Synthetic resins or natural rubbers -- part of the class 520 ser
Synthetic resins
Polymerizing in tubular or loop reactor
C526S065000, C526S066000, C526S073000, C526S227000, C526S319000, C526S348200, C526S348500, C526S348600
Reexamination Certificate
active
06300430
ABSTRACT:
The present invention relates to a process for copolymerizing ethylene with vinyl esters and, if desired, further vinylic comonomers in a tube reactor at pressures at from 500 to 4000 bar and at not more than 220° C.
The present invention additionally relates to copolymers obtainable by this process, to the use of the copolymers for producing pigment concentrates for coloring plastics, and to pigment concentrates comprising such copolymers.
Copolymers of ethylene and vinyl esters, especially vinyl acetate, with or without further comonomers are generally known and are used, for example, to produce pigment concentrates, known as masterbatches, for coloring plastics. Copolymers that are to be used for this purpose must firstly be able to be mixed very homogeneously with the pigment products in order to achieve a high coloring power and uniform coloration. For this purpose the copolymer itself must be extremely homogeneous. Secondly, the copolymer is required to have good thermal stability, since plastics are generally colored by extrusion at high temperatures.
The literature discloses various processes for preparing ethylene-vinyl acetate copolymers. For instance, DE 15 20 227 describes a process of synthesizing ethylene-vinyl acetate copolymers in a tube reactor. To maximize the completeness and uniformity of the monomer reaction, oxygen as initiator is fed into the tube at two or more locations. The reaction temperature is said to be from 200 to 250° C. Apart from this, nothing is said about the temperature profile along the tube reactor.
U.S. Pat. No. 3,917,577 describes a method of homopolymerizing ethylene in a tube reactor. The polymerization is initiated by feeding the reaction mixture—comprising ethylene, a peroxide initiator and a polymerization regulator—into the tube reactor at from two to three successive locations. The reaction mixtures are fed into the reactor at from 160 to 210° C. All that is said about the temperature progression in the reactor is that the temperature can be from 160 to 350° C.
EP-A 0 475 124 describes ethylene-vinyl acetate copolymers. Preparation takes place by high-pressure polymerization at from 180 to 240° C. Nothing is said either about the possibility of multiple initiation or about the temperature profile within the reactor.
The known ethylene-vinyl acetate copolymers still leave much to be desired in terms of their homogeneity and their thermal stability.
It is an object of the present invention to find a process for preparing ethylene-vinyl ester copolymers that leads to copolymers which have good homogeneity and thermal stability and which lend themselves well to producing pigment concentrates.
We have found that this object is achieved by a process for copolymerizing ethylene with vinyl esters and, if desired, with further vinylic comonomers in a tube reactor at pressures of from 500 to 4000 bar and at not more than 220° C., which comprises initiating the free-radical polymerization at at least two locations of the tube reactor by adding a catalyst/initiator and adjusting the temperature profile within the reactor such that the temperature maxima downstream of the initiation locations are from 150 to 220° C. and differ by less than ±10° C. from one another.
We have also found novel copolymers having improved properties that are obtainable by this process, and the use of these copolymers for producing pigment concentrates for coloring plastics, and such pigment concentrates themselves.
The process of the invention is a typical high-pressure tube reactor process.
The process can be performed using the customary, continuous tubular high-pressure polymerization systems (tube reactors). By tube reactors are meant tubular polymerization vessels in which the length-to-diameter ratio of the pressuretight tubes is generally from 10,000 to 60,000:1. Details of ethylene high-pressure polymerization processes in which tube reactors are utilized are given, for example, in Ullmanns Encyklopädie der technischen Chemie”, 1980, 4th edition, Volume 19, pages 167 to 178, Verlag Chemie GmbH, D-6940 Weinheim.
The supercritical mixture of ethylene and vinyl ester with or without regulators and further comonomer is supplied to the reactor in accordance with known methods at the inlet location and, if desired, simultaneously at a further location downstream of the inlet location along the tube reactor in the flow direction of the polymerizing ethylene, where the reaction temperature has exceeded a maximum. By inlet location is meant generally the beginning of the tubular reactor. The principle stream is fed in at the beginning of the reactor, while subsidiary streams can be supplied to the reactor at other locations in a known manner.
In accordance with the process of the invention it is preferred to prepare copolymers in which the proportion of ethylene units is from 80 to 95% by weight, the proportion of vinyl ester units from 5 to 20% by weight and the proportion of further vinylic comonomer units from 0 to 10% by weight, based in each case on the overall mass of the copolymer.
It is optional to operate in the presence of polymerization regulators. These make it possible to adjust the melt index of the resulting ethylene copolymers. Examples of suitable regulators are hydrogen, ketones, aldehydes, alcohols, ethers or linear or branched hydrocarbons. Preference is given to the use of propane, propylene, methyl ethyl ketone or propionaldehyde. The polymerization regulators are generally employed in amounts of from 0.2 to 5 mol percent, based on the ethylene to be polymerized. In one particular embodiment no additional regulators are employed since the vinyl esters used possess regulator properties.
The copolymerization is generally conducted in the absence of a solvent. The small amounts of an inert solvent, such as benzene, mineral oil or other inert solvent, in which the polymerization initiators are dissolved can be disregarded in relation to the other starting materials. If oxygen is employed as polymerization initiator, there is no need for any solvent at all.
Appropriate vinyl esters are all vinyl esters which can be copolymerized with ethylene under the stated temperature and pressure conditions. Examples of such comonomers are vinyl esters of carboxylic acids having 1 to 8, preferably 1 to 6 carbon atoms. Particular preference is given to vinyl acetate. Mixtures of different vinyl esters can also be employed.
The ethylene is copolymerized with the vinyl esters in the presence of free-radical initiators. By free-radical polymerization initiators are meant those catalysts which are also used for the high-pressure homopolymerization of ethylene. A suitable example is oxygen, judiciously in amounts of from 2 to 100 mol-ppm, based on the ethylene to be polymerized. Also suitable are peroxides and other free-radical initiators, and mixtures of peroxides having different decomposition points, and hydroperoxides and also mixtures of oxygen and peroxides and/or hydroperoxides. Examples of peroxides and hydroperoxides are tert-butyl peroxypivalate, di-tert-butyl peroxide, tert-butyl hydroperoxide, tert-butyl perbenzoate, p-menthane hydroperoxide and dilauroyl peroxide. Free-radical polymerization initiators also mean compounds such as azoisobutyronitrile. Mixtures of oxygen and one or more peroxides can also be used. The copolymerization of ethylene with vinyl esters is preferably initiated by means of one or more peroxide compounds.
In minor amounts the reaction mixture may also include further comonomers such as propene, butene, pentene, hexene and higher olefins and also mixtures of olefins.
Copolymerization preferably takes place at pressures of from 1000 to 3000 bar, with particular preference from 1500 to 2500 bar. The temperature should not exceed 220° C., since otherwise the vinyl ester is cleaved in detectable amounts and the corresponding acid is liberated. This impairs the thermal stability of the copolymers. The temperature maxima are preferably from 180 to 220° C., with particular preference from 200 to 220° C.
The free-radical polymeriz
Annen Ulrich
Deckers Andreas
Weber Wilhelm
BASF - Aktiengesellschaft
Cheung William
Keil & Weinkauf
Wu David W.
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