DE2403516C2 - Process for the production of homo-, co- and terpolymers as well as polymer alloys of ethylene - Google Patents

Description

25th

The invention relates to a method of manufacture of homo-, co- and terpolymerizates of ethylene as well as polymer alloys made from homopolymers, copolymers and / or terpolymers of ethylene in one Multi-zone tubular reactor system.

It is known that polyethylene and copolymers of the Ethylene in Mehrzonennjaktore ^ under high pressure to manufacture.

It is also known to use graft copolymers to produce various advantageous properties in the high pressure reactor, the possibilities of Incorporation of a graft component into a polymer is very limited for procedural reasons. Mixtures of mixed and Graft polymers of the same monomer building blocks.

It is also known to use ethylene polymers with a produce broad molecular weight distribution that in a first reactor or the Monomers are polymerized and this reaction mixture then between the two ends of a Reactor operating under reaction conditions is added, a low molecular weight polymer being formed. This process is suitable for polymers of the same composition with very different molecular weight by a kind of solution mixing to distribute homogeneously in each other. The application of this procedure to the tubular reactor process is not described. It would also be uneconomical as it would lead to a reduction in sales.

It is also known to produce copolymers of ethylene with vinyl esters in a two-zone reactor, with products in the first reaction zone a lower proportion of vinyl esters are produced than in the second zone. It is also known that Polymer alloys by compounding the corresponding polymers in one of the polymerizations downstream operation can be produced. In addition to excellent properties, these compounds often have a lack of homogeneity. Disadvantageous is also that the subsequent compounding of the finished polymers additional costs for the Mixing, melting and homogenizing arise.

Another disadvantage is that the polymers one must be exposed to additional thermal stress, which has a detrimental effect on certain product properties.

The purpose of the invention is to produce homo-, Copolymers and terpolymers of ethylene and of polymer alloys of homo-, co- and or or To develop terpolymers of ethylene in a technically and economically advantageous manner.

There was thus the task of a method develop that allows homo-, co- and terpolymers as well as polymer alloys of homo-, co- and or or to produce terpolymers of ethylene in a tubular reactor system.

This object is achieved in that the production of homopolymers, copolymers and terpolymers and polymer alloys of ethylene in a multi-zone reactor system at pressures above 500 at and temperatures of 100 to 400 ⁰ C in the presence of free radical initiators and optionally chain regulators and / or telegenes according to the invention so is carried out that ethylene or ethylene and vinyl acetate alone or with a further polymerizable compound in a first reaction zone which consists of several tubular reactors arranged in parallel, (»are polymerized that the reaction mixture is then further polymerized in a second reaction zone, the second reaction zone being a mixing section is upstream or downstream, and that the reaction mixture is depressurized after the second reaction zone, optionally, in the case of the downstream mixing section, mixed and fed to the separator.

The first reaction zone expediently consists of two or three parallel tubular reactors. the Further polymerization in the second reaction zone takes place either in a tubular reactor system that consists of consists of several parallel tubular reactors, which is followed by the mixing section, or in a single one Tube reactor upstream of which the mixing section is connected.

The polymerization is carried out at vortefijiafterweise and in the first reaction zone at pressures of from 1200 to 3500 from 150 to 40CC, and in the second reaction zone at pressures of from 1150 to 3450 and at temperatures of 200 to 40O ⁰ C

If the further polymerization is carried out in the second reaction zone in several parallel tubular reactors through, then the reaction mixture of each tubular reactor is expediently separated to 150 to 350 at relaxed, combined 'and fed to the high-pressure separator via a mixing section. This procedure is particularly suitable for homo-, co- and terpolymerization of ethylene, if the starting monomers, -monomer concentrations and the reaction conditions in the continuous parallel tubular reactors of the two reaction zones are the same. In this way, homopolymers, copolymers and terpolymers of ethylene are made obtained economically advantageous, e.g. B. polyethylene or ethylene-vinyl acetate copolymers.

For the production of polymer alloys from copolymers and / or terpolymers of ethylene and optionally polyethylene, the reaction mixtures are already after the first reaction zone combined and over the mixing section of the second reaction zone, which in this case consists of only one There is a tubular reactor, fed in and optionally with renewed feed of further polymerizable Connections further polymerized.

As further polymerizable compounds that lead to

Manufacture of Pcäy ^ alloys are suitable, compounds are used that polymerize alternately with ethylene, e.g. maleic anhydride, or compounds that polymerize significantly faster than ethylene, especially those with a ratio the r-values of

'"polyrn. connection

<0.004,

As such are particularly suitable

n-butyl acrylate, vinylidene chloride,

Methyl methacrylate acrylonitrile,

n-butyl methacrylate, n-isopropyl acrylamide,

N-phenyl methacrylan \ id, t-butyl methacrylate, Methacrylic acid, methyl acrylate and Ethyl acrylate

The concentration of these monomers in the reaction mixture should be 0.05 to immediately after the addition 5 mol .-% of the total amount of monomers.

Furthermore, as further polymerizable compounds, more than bifunctional compounds, e.g. B. Those with conjugated double bonds with CO groups and allyl compounds are preferably used to the double bond

Glycol diacrylate, glycol dimethacrylate Hexadiene-1 A diallyladipate or Allyl acrylate

used in the co- and terpolymerization of The concentrations of the more than bifunctional compounds are expediently ethylene 0.005 to 5% by weight of the total amount of monomers.

If ethylene and vinyl acetate are used as components in co- and terpolymerization, this is the case Process according to the invention for the preparation of polymers suitable in the ethylene and vinyl acetate in the Ratio 99: 1 to 50: 50 parts by weight are polymerized.

To control the chain length, you can also use Regulator, e.g. B. propane, butane, alcohols, ketones, aldehydes or hydrogen can be used.

Particular importance is attached to the use of hydrogen and / or telogens, whereby products are made with low molecular weights, e.g. B. in the form of wax compounds or hot melt adhesives are used.

The initiators customary in the radical copolymerization of ethylene are used as initiators in Concentrations from 0.005 to 1 wt% use, e.g. B. peroxides, azo compounds such as azobisisobutyronitrile or oxygen.

The initiators are fed to the reactor in solution separately from the monomers or together with the monomer (s). They can be added at other points along the reactor, except at the beginning of the first zone, especially if the reaction mixtures are combined after the first reaction zone, take place at the mixing section. However, mixtures can also be used which, due to the different initiator fan suspension temperatures of the constituents, are suitable for keeping the polymerization going over the entire area of the reactor,

Show advantages of the method according to the invention themselves, inter alia. in that the effort for the work-up of the residual reaction gas in the production of homo-, co- and terpolymers in the from several parallel tubular reactors existing reaction system through the combined work-up

reduced significantly

Furthermore, polymer alloys can be produced, without subsequent expenses for the compounding being necessary. It is without Meaning in which of the tubular reactors the individual components the polymer alloys are polymerized.

This process can be used to produce compounds made up of components with comparable molecular weights as well as compounds made up of components with very different molecular weights. The latter is particularly easy to obtain when z. B. in a tube reactor a more than bifunctional compound is polymerized, while in one or the other tube reactors a non-crosslinking comonomer z. B. methyl methacrylate or n-butyl acrylate is used.

Another advantage arises from the possibility of using copolymers of ethylene with compounds Produce vinyl acetate of different vinyl acetate content by adding the reaction sintering Fresh ethylene and vinyl acetate differently on the individual tubular reactors - in extreme cases the whole Ethylene in one tubular reactor and all of the vinyl acetate in the other tubular reactor - distributed be that z. B. suitable as a basis for hot melt adhesive are.

It is also particularly advantageous if you work with the Combination of the reaction gas flows from the various reactors after the first reaction zone, fresh ethylene or mixtures of ethylene with others Adding monomers This enables a significant increase in conversion to be achieved.

The method according to the invention is explained in more detail with reference to the drawings (FIG. 1 and FIG. 2):

The feed of the reaction gas is expediently carried out in such a way that the ethylene is brought to reaction pressure by the final pressure compressor (F), (Fig. 1) and is distributed to the individual tubular reactors Au Ai, A3 ... of the first reaction zone via a quantitative ratio control Feedings d 1, a ₂ , a ₃ ... further polymerizable compounds and optionally initiators are added.

The feeding of the monomers, in particular the fresh ethylene, to the individual tubular reactors can, however, also take place upstream of the final pressure compressor (b) if the gas flow is split up beforehand, the compression to reaction pressure is carried out in several lines of the final pressure compressor or with several final pressure compressors and the monomer mixture is individual tubular reactors is fed to the first zone of the reactor.

The reaction mixtures formed in the individual tube reactors of the first Reaktijnäzone are combined in a mixing section (B) and mixed intimately Of course, in this Quarrel: corner (B) and further along the second reaction zone (C) monomer or monomer mixture or initiators for supplying a * to be added.

Subsequently to the mixing section (B) , the mixture enters the second reaction zone (C). In addition to increasing the conversion, this is particularly important because here the polymerization of any monomers that may still be present, which should not emit into the residual gas, is completed.

You can control the reaction in the individual reactors of the first zone so that in the

individual reactors A \. A2. As ... the polymerization no, -h is not completed and these monomers are only polymerized away in reaction zone C with the formation of a mixed polymer of the components that are added in the individual tubular reactors.

In addition, however, it is also possible to add more monomer or monomer mixtures upstream of the mixing section and to continue the copolymerization in the second reaction zone (C) . Subsequent to the second reaction zone (C) , the reaction mixture is expanded via an expansion valve (C) to about 200 to 350 atm in a high-pressure separator (D) , where the polymer, which is discharged in a known manner via a granulator in (C), from the residual gas, which is fed back to the pressure release compressor via a gas cleaning device (E).

The inert gas level and the pressure of the circulating gas can be regulated through the expansion line (d). However, as shown in FIG. 2, the polymerization can also be carried out in such a way that different or identical monomers are produced in the same way as in FIG. I described, polymerized in the tubular reactors A \, A ₂ , Ai ... and in the subsequent

Tubular reactors G, C2, Cj, if appropriate, under

Addition of further monomers. polymerized further, the reaction mixture through the relief valves Ct. Gi, G> ... are expanded separately to about 250 atm, combined in a mixing section B and fed to the HP separator.

The following polymerization unit is used to carry out the work.

The tubular reactor system consists of 3240 m long tubular reactors, the 1st zones of which are each 120 m long with an inner diameter of 10 mm and whose 2nd zones are also 120 m long and an inner one Have a diameter of 15 mm. The tubular reactors are separate for both reaction zones Hot water coats surrounded. The 3 tubular reactors each have an expansion valve, from where the reaction κ mixture is fed to the high-pressure separator via a common mixing section. The 3 tubular reactors are arranged so that both the possibility exists. 2 or 3 tubular reactors with the 1st and 2nd Operate reaction zone, as well as, after installation of fitting pieces and a mixing section 3.50 m long and 32 mm in diameter. 2 tubular reactors with to operate the 1st zone, to combine the reaction mixture of the 1st zones in the mixing section and through a common 2nd zone to be fed to the high-thickness separator via the expansion valve.

The invention is illustrated by the following examples:

example 1

A tubular reactor system consisting of 3 tubular reactors with 1st and 2nd reaction zones is used for the polymerization. In the first zones of 3 tubular reactors at the input in each case 3! 6 kg / h kg and in the zones 2 in each case 337 / h ethylene and per zone and reactor 2.15 to 2.4 l / h of O, 2gew.- ^o Oigen ho tert-butyl perbenzoate solution fed into paraffin oil. The reaction conditions are set to be equal in all 3 reactors, the polymerization is at at 2950 and a maximum temperature of 251 ⁰ C in the first reaction zones and 245 ° C in the second reaction zones ^ carried out The heating mantle of the reactor is flowed through by hot water in the first reaction zones 202 ° C and in the second reaction zones 200 ⁰ C. to

Regulation of the chain length of the resulting polyethylene is given to ethylene with 4.9% by volume of propane. There are 270 kg of polyethylene per hour with a melt index of 1.5 g / 10 min at 190T and a density of 0.929 g / cm ¹ . The polymer is suitable for the production of films and for melt extrusion.

Example 2

A reactor system consisting of 2 tubular reactors is used for the polymerization. In the I tube reactor, 311 kg / h of ethylene and 144 kg / h of vinyl acetate are fed into the 1st reaction zone and 343 kg / h of ethylene and 160 kg / h of vinyl acetate are fed into the 2nd reactor zone. The other tubular reactor is fed into the first zone with 308 kg / h of ethylene and 143 kg / h of vinyl acetate and into the second zone with 335 kg / h of ethylene and 155 kg / h of vinyl acetate. 2.0 to 2.2 l / h of a 1.8% by weight solution of dilauroyl peroxide in paraffin oil are added as initiators to each reaction zone of the two reactors Set reaction zones and I39T in the 2nd reaction zones as heating and cooling medium for the reactor jacket at a reaction pressure of 2700 at maximum temperatures of 158 ° C. in the 1st zone and 155 ° C. in the 2nd zones. Under these conditions, about 210 kg / h of an ethylene vinyl acetate copolymer with a melt index of 78 g / min at 190T and a density of 0.956 g / cm ³ , which contains 31% by weight of vinyl acetate, is produced. Due to its excellent adhesive properties, the copolymer can be used, inter alia, as a hotmelt adhesive component.

Example 3

A tubular reactor system with 2 two-onigen tubular reactors is used. An ethylene vinyl acetate copolymer is produced in the 1st reactor, while a terpolymer consisting of ethylene, vinyl acetate and N-isopropyl acrylamide is produced in the 2nd reactor. After the expansion valves, the reaction products are fed to a separator system via a shared mixing section and discharged via a 30D discharge machine with good homogenizing performance. In the 1st tube reactor 312 kg / h of ethylene and 38 kg / h of vinyl acetate are fed into the 1st reaction zone and 340 kg / h of ethylene and 42 kg / h of vinyl acetate are fed into the 2nd reaction zone. 1.8 to 2 l / h of a 1.8% by weight dilauroyl peroxide solution are added as initiator per reaction zone, the amount being measured so that under a reaction pressure of 2900 atm and at hot water temperatures of 138T in the jacket of the 1st reaction zone and set in the shell of the second reaction zone maximum temperatures of 173 ^C C in the first reaction zone and 172 ⁰ C in the second reaction zone 140 ° ".

The 1st reaction zone of the 2nd tubular reactor is at 312 kg / h of ethylene. 38 kg / h of vinyl acetate and 2.25 kg / h of N-isopropyl acrylamide are charged. 346 kg / h of ethylene are fed into the second reaction zone of the second tubular reactor. 42.5 kg / h of vinyl acetate and 2.6 kg / h of N-isopropyl acrylamide are fed. 2.0 to 22 l / h of a 1.8% by weight solution of dilauroyl peroxide in paraffin oil are used as initiator per reaction zone in the reaction zone I. 160 ° C and in the reaction zone Z 161 ⁰ C Maximaitemperaturen of set in! .Zone 190 ° C and 188 ° C derZZone.

In the polymerization of about 170 kg / h are formed of a polymer alloy having a Schmclzindex of 8.7 g / 10 min at 19O ⁰ C and a density of 0.930 g / cm ". 11% by weight of vinyl acetate and 2.8% by weight of N-isopropyl acrylate can be detected in the polymer.

The polymers produced by this process can be processed by blowing, casting, extrusion and injection molding. The hergeri- from the polymers: llten finished parts exhibit compared with pure ethylene vinyl acetate copolymers improved Zähig- \ i resistance and rigidity.

Example 4

A tubular reactor system as shown in FIG. I used, the 1st reaction zone | - ne consists of 2 parallel tubular reactors, which are followed by a mixing zone and a common 2nd reaction zone. The two tubular reactors of the I. reaction / c me have an inner diameter of 10 mm iinr) Hir J RpaliΙίηης7ηηρ has pinrn innprpn Dilrrhmp *: - ™

ser of 15 mm. The reaction zones are each 120 m long.

An ethylene-vinyl acetate mixture is polymerized. In the 1st reactor of the 1st reaction zone, 324 kg / h of ethylene and 148 kg / h of vinyl acetate are polymerized using 1.7 to 1.8 l / h of a 1.25% by weight dilauroal peroxide solution in paraffin oil at 2700 atm. The heating jacket of the reactor tube is charged with hot water of 140 ^0C. The amount of peroxide is calculated so that a maximum temperature of 163 ° C. is established in this reaction tube.

The 2nd reactor of the 1st reaction zone is fed with 326 kg / h of ethylene. 168 kg / h vinyl acetate and 1.6 to 1.8 l / h a 1.25 wt .-% dilauroyl peroxide solution charged, j-,

The polymerization is carried out using hot water of 138 ° C in a heating mantle at 2700 atm and a maximum temperature of 16PC. The reaction mixture of the two reactors is combined in a mixing section and the polymerization after the addition of 98 kg / h of ethylene, 48 kg / h of vinyl acetate and 1.9 to 2.2 l / h of a 2.5% strength by weight solution of dilauroyl peroxide in Paraffin oil continued. In this case, a maximum temperature of 160 ⁰ C is adjusted using hot water of 140 ° C. r,

The polymerization produces 180 kg / h of an ethylene-vinyl acetate copolymer with a melt index of 72 g / 10 min at 190 ° C. and a density of 0.956 g / cm ³ . The polymer contains approx. 33% by weight vinyl acetate. The polymer is suitable for use as a hotmelt adhesive component.

Example 5

The polymerization is carried out in the tubular reactor system described in Example 4

For the polymerization, ethylene and n-butyl acrylate are used in the 1st tubular reactor in the 1st reaction zone and in the 2nd reaction zone. After the tubular reactor of the 1st reaction zone, a mixture of ethylene and methacrylic acid is used Mixing of the two reaction mixtures, the ω polymerization with the addition of ethylene in the 2. Reaction zone continued

The polymerization is carried out at 1600 atm. A 1.75% by weight solution of tert-butyl perbenzoate is used as the initiator in paraffin oil! used

In the 1st tubular reactor of the 1st reaction zone, 298 kg / h of ethylene, 3.8 kg / h of n-butyl acrylate and 2.15 to Given 2.4 l / h peroxide solution. The amount of peroxide solution so that, using hot water at 185 "C, a maximum temperature of 219 "C is reached.

In the 2nd tubular reactor of the 1st reaction zone, at a hot water inlet temperature of 219 ° C. and catalyst injections of 2.2 to 2.5 l / h at temperatures with a maximum of 258 ° C., 306 kg / h of ethylene and 0.83 kg / h Methacrylic acid copolymerized. After the reaction mixtures of the two tubular reactors have been combined, the polymerization is continued in the 2nd reaction zone with the addition of 95 kg / h of ethylene and 2.4 to 2.7 l / h of initiator solution. Using hot water of 216C as a cooling medium produced a maximum temperature of 216 ⁰ C. It will be about 126 kg / h of a polymer alloy having a melt index of 1.5 g / 10 min at I9O ° C and a density of 0.924 g / cm ¹ educated. The alloy contains 3% by weight of n-butyl acrylate and 0.65% by weight of methacrylic acid. As a result of the manufacturing process, which is an intense

present a very homogeneous alloy that can be used for extrusion processing. Particularly it is suitable for the coextrusion of films and for the production of flexible moldings.

Example 6

The polymerization is carried out in the polymerization unit described in Example 4.

326 kg / h of ethylene alone and are used for the polymerization in the 1st tubular reactor of the 1st reaction zone in the 2nd tubular reactor of the 1st reaction zone 298 kg / h of ethylene mixed with 3.6 kg / h of methyl methacrylate.

The reaction mixture leaving the two tubular reactors is combined in the mixing section and polymerized further with the addition of a mixture consisting of 102 kg / h of ethylene and 2.7 kg / h of methacrylic acid.

The polymerization is carried out at 2280 atm. 2.8 to 3.1 l / h are used as initiator for the 1st tubular reactor 0.5% strength by weight solution of tert-butyl perbenzoate in paraffin oil, the 2nd tubular reactor of the 1st reaction zone 2.4 up to 2.6 l / h of the same solution and in the 2nd reaction zone 2.5 to 2.8 l / h of a 1.2% strength by weight t-butyl perbenzoate solution added. To regulate the molecular weight of the resulting polymer 3% by volume of propane were also added to the monomer.

By means of the amounts of initiator solution, the individual tubular reactors are operated in such a way that under Use of hot water of 215 ° C in the 1st reactor of the 1st zone, 185 ° C in the 2nd reactor of the 1st zone and in the 2nd zone 219 ° C maximum temperatures of 255 ° C in the 1st reactor of the 1st zone, 219 ° C in the 2nd reactor of the 1st zone and set 258 ° C in the 2nd zone.

206 kg / h of a polymer alloy with a melt index of 0.8 g / 10 min at 190 ^° C. and a density of 0.925 g / cm ³ are obtained, which contains 1.75% by weight of methyl methacrylate and 1.2% by weight. % Contain polymerized methacrylic acid.

The polymer, which can have a very good homogeneous distribution of the alloy components z. B. processed into films and molded articles by the extrusion process. The manufactured Films and moldings have sufficient transparency and improved transparency compared to polyethylene Can be printed and glued on.

Example 7

The polymerization is carried out in the tubular reactor system described in Example 4.

330 kg / h of ethylene are used in the 1st tube reactor of the 1st reaction zone for the polymerization Mixture with 153 kg / h vinyl acetate and in the 2nd tubular reactor the 1st reaction zone 311 kg / h ethylene, 144 kg / h vinyl acetate and 1.5 kg / h maleic anhydride. To After leaving the first reaction zone, the reaction mixtures are in a common mixing section given and then with the addition of a mixture of 110 kg / h of ethylene and 51 kg / h of vinyl acetate in the 2. The reaction zone continues to polymerize.

The polymerization is carried out at 2400 atm. 2.5 to 2.6 l / h of the reaction mixture in the first reactor and 2.7 to 2.9 l / h of a 1.8% strength by weight dilauroyl peroxide solution are added as the initiator to the first reaction zone in the first reactor in paraffin oil and in the 2nd reaction zone 2.4 to 2.5 p / h of a 4.1% strength by weight dilauroyl peroxide solution in paraffin oil are added to the reaction mixture. By means of the initiator solution amount to be operated, the individual tube reactors so that by using hot water in the first reactor of the I.Zone 138 ° C. in the 2nd principal of the 1st zone 135 ° C and in the 2nd zone 140 ⁰ C of Miximaltemperaturen In the 1st reactor of the 1st zone IdO ⁰ ° C., in the 2nd reactor of the 1st zone 157 ° C. and in the 2nd zone 178 ° C. are obtained. 146 kg / h of a polymer alloy with a melt index of 85 are produced during the polymerization g / 10 min at 190 ⁰ C and a density of 0.953 g / cm ^3. the polymer contains 31.5 wt .-% vinyl acetate and i, i wt ° / o maleic anhydride in copolymerized form. the constituents of the alloy are distributed homogeneously very The polymer is particularly suitable for use as a hotmelt adhesive component and has improved adhesive properties compared to pure ethylene-vinyl acetate copolymers.

Example 8
The polymerization unit described in Example 4 is used to carry out the polymerization. The following are used for the polymerization in the first tubular reactor ^: reaction zone 298 kg / h of ethylene and 206 kg / h of vinyl acetate;

-, reaction zone 3Cb kg / h ethylene and 210 kg / h vinyl acetate. The reaction mixture leaving the two tubular reactors is combined in the mixing section and with the addition of a mixture consisting of 64 kg / h ethylene, 42 kg / h vinyl acetate and 1.05 kg / h glycol

Hi acrylate, polymerized further in the 2nd reaction zone. the Polymerization is carried out at 3200 atm. The first reaction zone is used as the initiator in the tubular reactors 2.1 to 2.4 l / h each of a 1.25% by weight dilauroyl peroxide solution in paraffin oil and in the 2nd reaction zone 2.3 to

ii 2.4 l / h of a 1.8% strength by weight dilauroyl peroxide solution in Paraffin oil added to the reaction mixture. The tubular reactors become so by means of the amount of initiator solution operated that using hot water of 123 ° C in the 1st reactor of the 1st reaction zone, in the 2nd reactor

.Ό the 1st reaction zone 122 ° C and in the 2nd reaction zone Maximum temperatures of 125 ° C as heating or cooling medium of 145 ° C in the 1st reactor of the 1st zone, 146 ° C in the 2nd reactor of the 1st zone and 135 ° C in the 2nd zone will.

The polymerization produces 123 kg / h of a polymer with a melt index of 146 g / 10 min at 190 ° C. and a density of 0.967 g / cm ³ . The polymer has an ester number of 260 mg of KOH per 1 g of polymer.

κι It has extremely good adhesive properties. In addition to being suitable as a hot-melt adhesive component a polymer can be produced by peroxidic crosslinking, which z. B. as a raw material for the production of PVC impact resistant is suitable.

ü The melt index was determined according to TGL 20 996 »Plastics, test methods, determination of the Melt index of polyethylene and polyethylene compounds «and the determination of the densities according to TGL 14 075 »Testing of plastics, determination of the raw density

te «.

For this purpose 2 sheets of drawings

Claims (1)

Claim: Process for the production of homo-, co- and Terpojymerisaten as well as polymer alloys of Ethylene in a multi-zone reactor system Pressures above 500 at and temperatures from 100 to 400 ° C in the presence of radical initiators and optionally chain carriers and / or junction, characterized in that len or ethylene and vinyl acetate alone or together with another polymerizable Compound are polymerized in a 1st reaction zone, which consists of several parallel Tubular reactors that the reaction mixture consists is then further polymerized in a 2nd reaction zone, the 2nd reaction zone a Mixing section is connected upstream or downstream, and that the reaction mixture after the 2nd reaction zone relaxed, optionally, in the case of the downstream mixing section, then mixed and is deposited.