DE1918057B - Process for the production of polyethylene 1,2 diphenoxyathane p, p dicarboxylate fibers - Google Patents

Description

The invention relates to a method of manufacture of polyethylene-1 ^ -diphenoxyethane-p ^ '- dicarboxylate fibers by spinning the molten polymer and taking up the resulting fibers.

In the production of fibers from spinnable linear, high molecular weight polymers in melt spin η method, the procedure so far has been that the undrawn fibers with low strength, high elongation, low crystallinity and low orientation has drawn to their crystallinity and improve orientation. In the known processes, there were two stages, namely that Spinning or drawing, necessary. However, such two-step processes are of concern the amount of work, the necessary facilities and the achievable production capacity are undesirable.

When you can get usable fibers with high strength and low elongation simply by spinning then it is necessary to give the fibers the necessary crystallinity and orientation during to impart their migration from the spinneret to a pick-up point. Try extruded threads record at such high speeds as more than 4700 m per minute and 2700 to 4700 m / min, have already been described in U.S. Patents 2,604,667 and 2,604,689, respectively.

Such high recording speeds are not only accompanied by mechanical difficulties, but also from the fact that the threads picked up at such high speeds are relatively have large permanent deformation and a low elastic limit. This is due to that the threads obtained in practical use in the subsequent process stages, for example in weaving, bring many difficulties. Besides, this is the problem

- O —C

caused a certain irregularity of the tissues.

The invention therefore has the object of providing a process for the direct spinning of polyethylene-1,2-diphenoxyethane-p.p'-dicarboxylate fibers to create in which the previous deficiencies and evils can be switched off.

This object is achieved according to the invention in that a molten polyethylene> lenl.2-diphenoxyethane-p, p'-dicarbo. \ Ylat with an intrinsic viscosity of 0.4 to 1.3 and a proportion of residual carboxyl groups of less than 20 eq / 10 "g of the polymer is used and that the fibers obtained are processed at speeds of 1000 up to 3500 m, min with the proviso that the titers of the monofilaments (single titers) from 0.3 to 1.5 den the recording speeds 1000 to 1800 m-min and for single titers of more than 1.5 den the take-up speed 1800 to 3500 m / min amounts to.

It has been shown that one made of polyethylene-1 ^ -diphenoxyethane-p ^ -dicarboxylate, which satisfies certain conditions. Threads with extremely good properties can be obtained by using the Picks up threads at a speed that is far lower. than one usually considers them pulls. The invention is therefore directed to a new direct spinning process of polyethylene-1,2-diphenoxyethane-p.p'-dicarboxylate fibers, which consists in the fact that with a conventional spinning device from the certain conditions are satisfied named material takes up endless yarns.

The polymers used according to the invention are polyethylene-1 ^ -diphenoxyethane-p ^ '- dicarboxylate, which is at least 70 mole percent of the repeating unit having the formula

CH ₂ -CH ₁ -O

C - O - CH,

CH ₂

contain whose intrinsic viscosity (ι,) is higher than 0.4 and less than 1.3 and contains less than 20 eq / 10 ⁶ g of residual carboxy radicals in the polymer. An intrinsic viscosity (»,) of the polymers of less than 0.4 and more than 1.3 is not advisable, since yarn breaks often occur in these cases.

With proportions of residual carboxyl groups in the polymers of more than 20 eq / 10 ⁶ g and when the threads are taken up at the low speed mentioned, only threads with a low elastic limit can be obtained. On the other hand, if the proportions are less than 20 eq / 10 ⁶ g, excellent fibers having a high elastic limit are obtained even if the filaments are taken up at a relatively low take-up speed. Furthermore, the spinnability in the spinning process is extremely good, which can then be obtained at spinning temperatures of 255 to 32O ⁰ C threads with high production output with a very high stability even when working with high recording speed.

The values should be referred to as intrinsic viscosity (/;) be that at 35 ° C in a solvent mixture of tetrachloroethane and phenol in a weight ratio can be measured at a rate of 2: 1. The remaining carboxyl groups are the measured values those when titrating with a solution of caustic soda and benzyl alcohol using benzyl alcohol as a solvent and phenol red as an indicator (cf. H. H. Po h I, Annal.

Chem., 26, 1614 [1954]).

The elastic limit are the values that are determined from the stress-deformation curves, where 20 cm long samples are stretched at a stretching rate of 100% per minute.

If the samples do not give a clear endpoint, then this is the intersection of two intrapolated Lines determined both from the lower stretch side and from the higher stretch side.

The above polymers can be prepared by adding 1,2-bis (para-carbomethoxy) phenoxyethane or subjecting its ester-forming derivatives and ethylene glycol to an ester interchange reaction in the presence of a catalyst, whereby the bisglycol of 1,2-bis- (para-carbomethoxy) -phenoxyethane is formed. The latter is in the present a polymerization catalyst at an elevated temperature and a reduced pressure of a condensation polymerization subject, with the

Excess glycol formed during condensation is removed.

In the preparation of the polyester ethers described above, one can use a small amount of one or add several comonomers. Glycols other than ethylene glycol, for example, can be used as such as well as dicarboxylic acids and hydroxycarboxylic acids into consideration. Thus, what is suitable for the invention can be Starting material, which consists essentially of Polyäth} -len-1.2-diphenoxyethane-p, p'-dicarboxylate consists of up to 30 mole percent of another glycol. like diet valve glycol. Tetramethvlenghkol. Hexamethylenglyko 'od. like. included. In addition, the molecule can contain up to 30 mole percent of another acid. Such copolymerizable acids are, for example, hexahydroterephthalic acid, Terephthalic acid, isophthalic acid, bibenzolic acid, adipic acid, sebacic acid, azelaic acid, Naphthalic acid, 2,5-dimethyl-terephthalic acid.

These third components can be used together with during the polymerization or before the reaction can be added to the original starting materials. On the other hand, it is also possible to do so separately polymerize and then by fusing the mixture with the Pol \ älhylen-1,2-diphenoxvethane-p.p'-dicarboxylate to undertake.

According to the invention, fibers with an elastic limit of more than 1.0 g / d, a Young's modulus of elasticity of more than 70 g / d, a breaking strength of more than 3.0 g / d and a permanent deformation of less than 80% obtained when molten polyethylene-1,2-diphenoxyethane-p.p'-dicarboxylate with an intrinsic viscosity of 0.4 to 1.3 and a proportion of residual carboxyl groups of less than 20 eq IO ^h g of the polymer is used and the obtained Fibers at speeds of 1000 to 3500 m / min takes up with the proviso that with titers of the mono- (filaments of 0.3 to 1.5 den the take-up speed 1000 to 1800 m / min and with titers of more than 1.5 den the take-up speed 1800 to 3500 m / min.

It must be regarded as quite surprising that in the method according to the invention, which is characterized by the uptake of the threads at relatively low speeds, the lower limit of take up almost up to conventional spinning speed at Spinning fine threads can be reduced. This is because it is possible when using monofilaments with titers in the range of less than 0.5 and greater than 0.2 fibers produce the high strength and have good performance properties even when the take-up speed is 100nvmin. If the titer of the monofilaments is around 1.0 d, then threads with great strength and with practical utility value can be obtained even at take-up speeds of 1500 m / min.

The use of the conventional one, consisting of the two stages of spinning and drawing Production methods for synthetic fibers for the production of such ultrafine threads as above is because of the various problems associated with it, such as yarn breakage and flaky, difficult. In contrast, the method of the invention has manufacture made such ultra-fine threads with extremely high performance possible. For threads with less however, than 0.2 denier, it is not preferable because of the increase in thread breaks.

As already stated, have those produced by the process of the invention Fibers properties similar to those obtained by conventional direct spun methods Threads are superior. However, it is possible to make a manufacturing method extremely practical to make usable fibers available, which have even better properties if you have different Conditions relating to the polymers used, the spinneret, the temperature of the extruded threads up to the pick-up point surrounding air, the pick-up methods for the threads and taking into account their appropriate limits. First of all, the following are the conditions regarding of the polymer are described in more detail.

In the preparation of polymers, any known combination of a Esteraustauschkalalysators and polymerization catalyst may be used, the other polymerization conditions such as Polymerisationszeil and temperature, the remaining carboxyl groups in the polymers provided by appropriate selection of less than 20 eq ΊΟ 'be ¹ g. However, if a combined system consisting of a special ester exchange catalyst and polymerization catalyst is used in the production of the polymer and the fibers are produced therefrom by means of a high-speed spinning process.

then the fibers obtained have particularly good properties, such as greater elastic limit, greater strength wedge, lower permanent set, etc. As preferred combinations of ester interchange catalysts and polymerization catalysts, for example, combinations of a barium compound and a tin compound, a Barium compound and an antimony compound and a calcium compound and an antimony compound to be named. Suitable compounds for the ester interchange catalyst include the elemental ones Metals and the carbonates, oxides, hydroxides. Acetates and borates of barium or calcium.

Suitable antimony compounds for the polymerization catalyst are, for example, the salts of antimony with inorganic or organic acids, the double salts, such as potassium antimony tartrate, the salts of antimonic acid (e.g. ammonium pyroantimonate), the oxides. Glycoside c. Catechol complex salts and so on. Organic tin compounds are suitable as tin compounds, which by the general formula

are characterized. In this formula, in an integer from 1 to 4, rv a valence of the X atom. 4 - m / vx is an integer from 0 to 3. R is an aliphalic group with 1 to 18 carbon atoms, a cyclic radical with 3 to 6 rings or an aromatic group. X isl

- R —OR -OH -SnR.,

Il

- O - C - R

Halogen - O -
or

- Ο —C-R '- C —Ο -

(where R is as defined above and R 'is a divalent radical R as defined above Meaning is).

The ester interchange catalyst is used in amounts of 0.005 to 0.5 percent by weight, preferably 0.01 up to 0.3 percent by weight, the polymerization catalyst in amounts of 0.005 to 0.5 percent by weight, preferably 0.01 to 0.5 percent by weight, based in each case on the polymer formed, is used.

The further addition of a phosphorus compound, such as triphenyl phosphite, phosphoric acid, as a color stabilizer and TiO ₂ as a matting agent does not interfere with the effectiveness of the invention.

When using a catalyst system which consists of the specific combination described above to produce the polymer, the rate of crystallization of the obtained polymer extraordinary big.

The half crystallization time was measured by determining the temperature of the molten-at 29o ⁰ C polymers after 10 minutes was changed to 220 C for directly and the polymers at this temperature using a differential scanning calorimeter of Perkin Elmer Co. were maintained, is within 2 minutes. Presumably, this high rate of crystallization has an advantageous effect on the drawing. the orientation and crystallization at the time of recording at high speed. It must be regarded as surprising that such small amounts of the catalyst system exert a beneficial influence on the properties of the fibers. This circumstance can greatly enhance the suitability of the method of the invention.

In the following, the conditions present in the spinneret will be considered in more detail. It is it is preferable to use a spinneret with a hole diameter greater than 0.25 mm and not more than 0.9 mm to use. If the values in question are within this range, then the stability is extremely good at spinning. With hole lengths of the spinnerets of more than 1.5 mm and at most 10 mm, extremely uniform fibers can be obtained. There is a slope below 1.5 mm to the appearance of irregular physical properties, which is due to the non-uniform flow of the molten material. On the other hand, there is no need to change the length of the hole to be chosen larger than 10 mm.

With regard to the conditions of the atmosphere can be stated as follows: It has proved to be advantageous, the extruded filaments at a distance from the spinneret of more than 30 cm and less than 2 m before recording by a maintained at 10 to 18O ⁰ C hot atmosphere to direct. It is not practical to extrude the molten material in a cold atmosphere at temperatures below 10 ° C or to carry out the extrusion in a manner that is directed to the spinning nozzle, a gas stream or a jet of liquid at temperatures below 10 ⁰ C, since then the elastic limit of fibers is decreased. A lowering of the orientation of the molecular chain of the threads, which leads to a deterioration in the physical properties, then also occurs. if the threads are allowed to pass through an atmosphere at more than 180 ° C. Furthermore, it is not advisable to provide a heating area of less than 30 cm or more than 2 m. When controlling the hot atmosphere, as well as controlling the rate of cooling, which occurs when polyester fibers are spun in the conventional manner by means of a dried, hot air stream, control becomes easier and better results are obtained using a hot air stream which is greater than that has been humidified as 65% relative humidity.

The further description should now be directed to the recording method. Under the name "Recording" is to be understood as a device that controls the running speed of the extruded threads determined after cooling and solidification. You should not use a device for winding the Threads restricted to bobbins that are used in conjunction with a common drive mechanism but also includes entire devices that contain devices that implement the Conveying threads at a considerably high speed, such as devices using working from air currents, etc.

When carrying out the method according to the invention, one or more materials with the threads result in friction, inserted into the part between the spinneret and the receiving point without adverse effects occurring.

The invention is illustrated in the examples. All information regarding the parts and the percentages are based on weight.

example 1

Polyethylene -1,2 -diphenoxvä than - pp '-dicarboxylate with an intrinsic viscosity of the polymer of 0.65 and a proportion of residual catboxyl groups of the polymer of 16eq.10 ⁶ g, which is obtained by polymerization using 0.03 part of manganese acetate as an ester exchange catalyst and 0.01 part of germanium dioxide was obtained as a polymerization catalyst, was extruded through a spinneret having 2 mm long holes, the diameter of which was 0.35 mm, at a spinning temperature of 290 "C and spun under various spinning conditions. The results obtained are shown in Table I put together.

Table I.

admission Titcr Elastic fracture fracture Young speed limit of activity strength strain module age (Denier) (g / d) <& d) (%) (S'd) (mmin) 1.9 0.75 2.7 110 54.4 1600 2.0 1.1 3.1 80 78.0 1800 3.3 1.05 3.0 90 73.0 1800 0.8 3.7 51 110.0 2500 2.1 3.5 57 100.2 2500 5.2 3.2 63 93.0 2500 1.8 3.6 50 111.0 3000 3.3 3.3 54 101.0 3000 2.3 , 4 4.2 45 153.2 3500 3.1 , 2 3.8 47 109.8 3500 5.0 , 0 3.5 54 105.0 3500 1.8 , 5 2.8 2.4 \ > 0

Comparative example 1

Polyethylene-1.2-diphenox_ \ athan-p.p'-dicarbo \ ylate with an intrinsic viscosity of 0.61 and a proportion of residual carboxyl radicals of the polynes of 33 eq K) ' ¹ g, which is obtained by polymerization using 0.03 parts of manganese acetate as ester exchange catalyst and 0.01 part of germanium dioxide as polymerization catalyst, was extruded through a spinneret with 2 mm long holes, the diameter of which was 0.35 mm, at a spinning temperature of 285 ° C. The properties obtained under different spinning conditions are summarized in Table II below.

Pickup speed
age

(in now)

1600
1800
1800
2500
2500
2500
3000
3000
3500
3500
3500

Ti t he
(The ic!

2.0
2.3
3.0
1.0
1.9
5.1
2.2
3.3
2.0
3.4
5.2

Table Il

Γ ~ "" "Ί

Ll.isu / i- Bruchl.ilsgien / e strength

(gd) (gd)

Elongation at break

Young module

(gd)

0.53 2.6 119 53.3 0.69 2.9 92 75.0 0.51 2.7 99 61.0 1.0 3.3 60 105.0 0.77 3.1 64 93.3 0.69 2.9 80 80.1 1.2 3.5 53 109.4 1.0 3.3 57 98.6 2.6 4.0 47 118.2 2.1 3.4 49 105.5 2.0 3.4 56 100.1

Example 3

Polyethylene 1,2-diphenoxyethane-p.p'-dicarboxylate with an intrinsic viscosity of the polymer of 0.73 and a proportion of residual carboxyl radicals of the polymer of 14eq / 10 ⁽ 'g, which is produced by polymerization using manganese acetate as ester exchange catalyst and germanium dioxide as a polymerization catalyst was extruded from a spinneret with 3 mm long holes, the diameter of which was 0.5 mm, at a spinning temperature of 295 C. The properties of the fibers obtained under various spinning conditions are shown in Table III.

Table III Example 2

90 parts of 1.2-bis- (para-carboxymethoxy) -phenoxyäthan, 75 parts of ethylene glycol, 0.01 part of calcium acetate as Esteraustauschkatalysator were mixed and the resulting mixture heated for 4 hours at 220 C ^c. The methanol formed was removed. Then 10 parts of adipic acid, 0.01 part of antimony trioxide, 0.01 part of TiO ₂ and, as a stabilizer, 0.01 part of triphenyl phosphite were added and the whole was placed in a polymerization vessel and at a reduced pressure of less than 0.1 mm Hg to 280 ° C heated, the ethylene glycol formed was removed. The intrinsic viscosity and the residual carboxyl group content of the polymer were 0.84 and 13 eq / 10 ⁶ g, respectively. The polymer obtained was isolated from a 24löchrigen spinneret having 2 mm long holes, the diameter of 0.45 mm, was spun at a spinning temperature of 300 C and an extrusion speed ^c of 12 g / min extruded. The fibers obtained were taken up at a speed of 2500 m / min. In this way, excellent fibers having a strength of 3.6 g / d, an elongation of 38%, an initial elastic modulus of 114 g / d and an elastic limit of 1.3 g / d were obtained.

Pickup speed
age

(m.min)

Titer

(Denier)

25th

30th

1500

2000

2500

3000

40 0.36

1.3

0.41

1.4

2.1

0.51

1.3

2.6

0.43

1.5

2.4

0.62

1.6

3.4

Elastic fracture fracture Young limit of activity strength strain module (g / d) (g-d) (%) (g / d) U 3.0 63 88.8 0.7 2.7 74 64.3 1.3 3.3 57 91.1 1.2 3.1 67 86.4 0.7 2.6 71 76.5 1.8 3.7 46 98.3 1.4 3.2 52 99.9 1.2 3.1 58 103.2 1.9 4.0 41 103.1 1.4 3.6 49 106.3 1.3 3.4 54 105.6 2.1 4.1 36 112.1 1.9 3.7 50 109.5 1.8 3.2 53 100.0

Example 4

90 parts of 1,2-bis (p-carbomethoxyphenoxy) ethane and 75 parts of ethylene glycol were heated to 220 ° C. for 4 hours in the presence of an ester exchange catalyst, the methanol formed being removed. Thereafter, the resulting mixture under reduced pressure below 1 mm Hg in a polymerization vessel in the presence of a polymerization catalyst, 0.03 parts of TiO ₂ as a matting agent and 0.1 part of triphenyl phosphite as a stabilizer heated to 28O ⁰ C, wherein the ethylene glycol formed was removed . The Instrinsic viscosities of the polymer and the proportions of residual carboxyl groups in the polymer formed in the presence of various ester interchange catalysts and polymerization catalysts are shown in Table IV. These polymers were melt-spun using a spinneret having holes 2 mm long and 0.35 mm in diameter. The threads obtained were taken up at a take-up speed of 2400 m / min. In this way, fibers whose single denier was 2 denier were obtained. The physical properties of the fibers obtained are given in the sixth and subsequent columns of Table IV.

009 584/344

Table IV

10

Catalyst system and amount,
Ester exchange analyzer
Polymerization calculator Intrinsic
Viscosity Share of rest
lichen carboxyl
radical HaIb-
crystalline
salion line Spinning
learn pcratur Tiler Elastic
limit of activity Firm
speed Deh
tion Young
module A% 10 "g (C) (Denier) (g d) (possibly <%) (g / d) Ba acetate / dibutyltin oxide
(0.04 part / 0.03 part) .... 0.85 18th 1'33 " 300 2.0 2.0 4.0 45 114.1 Barium acetate / antitnon
trioxide (0.04 part /
0.03 parts) -0.78 16 1 '30 " 300 1.9 1.8 3.9 46 112.1 Ca acetate / antimony trioxide
(0.03 part / 0.03 part) .... 0.76 15th 1 '20 " 300 2.0 1.7 3.9 46 111.0 Ca acetate / dibutyltin oxide
(0.03 part / 0.03 part) .... 0.77 13th 4'30 " 300 1.8 1.3 3.4 59 102.1 Ba acetate / germanium dioxide
(0.04 part / 0.01 part) 0.74 15th 3'3O " 295 1.9 1.1 3.2 61 100.1 Mn acetate / germanium
dioxide
(0.03 part / 0.01 part) 0.79 10 3'40 " 300 2.0 1.4 3.4 57 105.6 Mn acetate / antimony trioxide
(0.03 part / 0.03 part) .... 0.78 11th 4'30 " 300 2.0 1.4 3.5 56 107.2

Example 5

The polymer used in Example 1 was melt-extruded from a spinneret having 2 mm long holes of different diameter at a spinning temperature of 29o C ^0.

At a take-up speed of 3000 m / min, fibers with a single denier of 2 den receive. The spinning conditions are in Table V below, the number of fiber breaks compared with continuous spinning over 8 hours. The physical properties of the Fibers that are of different lengths under the same conditions and when using a spinneret Holes of different diameters obtained are shown in Table VI as deviations from the arithmetic mean values given 50 times measurement.

45 Table V

Table VI

Diameter of the spinning holes Number of breaks in the fibers 0.15 5.6 0.2 3.1 0.25 0.9 0.3 0.5 0.4 0.4 0.5 0.5 0.7 0.4 0.9 0.6 1.0 1.7 1.2 2.9

length Titer Unequal Unequal diameter (mm) Unequal moderation moderation the
Spinning hole cr 1.0 moderation the
Fixed wedge the stretch 1.5 (± denier) <± g / d) (±%) 0.35 2.0 0.2 1.5 13th 3.0 0.1 1.0 7th 5.0 0.15 0.6 6th 1.0 0.1 0.7 5 2.0 0.2 0.3 5 0.5 3.0 0.2 1.5 14th 5.0 0.2 0.9 8th 1.0 0.15 0.9 6th 2.0 0.2 0.4 5 0.7 3.0 0.2 2.3 21 5.0 0.2 2.0 7th 9.0 0.1 0.9 6th 13.0 0.15 0.6 5 0.2 0.5 4th 0.15 0.5 5

Example 6

The polymer used in Example 1 was melt-extruded from a spinneret having 2 mm long holes whose diameter was 0.35 mm at a temperature of 29o C ^0. The temperature of the zone, which was 5 to 90 cm away from the spinneret, was kept at a preselected value, which was done by installing a 1 m long heating or cooling pipe immediately below the spinneret. In another case, a stream of cooling was - 10 ⁰ C from a compressor directly blown onto the spinneret. The physical properties of the fibers, the single denier of which was 2 den, and which had been taken up at a take-up speed of 3000 m / min, are summarized in Table VII.

Table VII

Temperaiui Eljsti / iuits- Kcstigkeil the
the atmosphere gren / e Hedgehog) (C) (g dl 3.0 -10 0.7 3.0 + 5 0.9 3.1 10 1.3 3.4 20th 1.7 3.5 80 1.8 3.6 100 2.0 3.5 160 2.1 3.4 180 1.8 3.2 200 0.9 3.0 -10 0.6

strain

68 63 56 51 47 43 46 50 64 69

Young-M od u I

(g d)

99.0 102.1 105.6 110.0

113.5 116.3 115.0

113.6 101.0

93.6

(Cooling with a cold stream of air).

Long the
Heating zone Elasticity
border strength strain Young
module (cm) (g d | (g'd) 1%) <g.d) 25th 0.8 3.0 62 96.4 30th 1.5 3.2 50 107.3 100 2.0 3.5 45 115.0 200 1.9 3.4 46 116.3 250 2.1 3.5 43 115.0

Elasticity limit of 2.4 g / d, a strength of 4.2 g / d, an elongation of 38% and a Young's modulus from 118 g / d up. Their uniformity was excellent. In an approximately 11 m thick roll of cloth the plain woven fabric made with these fibers did not become unevenly colored observed.

In Table IX below is the influence of the various spinning speeds

a) with constant titer and

b) with constant delivery rate

described.

Table IX

A zone more than 5 cm away from the spinneret was kept at 140 ^° C. by installing a heating tube of the same length below the spinneret. The spinning was carried out under the same conditions as in the case described above. The physical properties of the 2den fibers are summarized in Table VIII.

Table VIII

40

Example 7

90 parts of 1,2-bis-p-Carbomethoxyphenoxyäthan and 7.5 parts of ethylene glycol were heated for 4 hours in the presence of 0.04 part of barium acetate as Esteraustauschkatalysator to 220 ⁰ C, whereby the formed methanol has been removed. The mixture obtained was then heated to 280 ° C. at reduced pressure below 1 mm Hg in a polymerization vessel in the presence of a mixture of 0.03 part of dibutyltin _{oxide as a polymerization catalyst and 0.03 part of TiO 2} as a matting agent and 0.1 part of triphenyl phosphite as a stabilizer, whereby the ethylene glycol formed was removed. The polymer thus obtained had an intrinsic viscosity of 0.73 and a residual carboxyl group content of 12 eq / 10 ⁶ g.

The polymer was obtained from a spinneret with 3 mm long holes, the diameter of which was 0.5 mm was melt-extruded at a spinning temperature of 295 ° C. The threads obtained were with a Take-up speed of 3000 m / min recorded, with a 1 m long, held at 160 ° C The heating tube installed below the spinneret ran through it. The so obtained Fibers with a single titer of 2den had a

admission Titer Elaslizi- fracture Fracture- Young speed (Denier tälsgren / e firmly igkci stretchy. module (m / min) fed) (gd) (%) (gd) a) 2.2 1000 1.9 0.4 2.0 220 46.0 1600 2.0 0.75 2.7 110 54.4 1800 2.1 1.1 3.1 80 78.0 2500 1.8 1.2 3.5 57 100.2 3000 2.3 1.8 3.6 50 111.0 3500 2.0 2.8 4.2 45 153.2 4000 3.1 4.1 42 158.0 lots yarn breaks b) 0.5 3000 1.0 2.3 4.1 41 120 3000 1.8 2.1 3.6 46 113 3000 3.3 1.8 3.6 50 111.0 3000 4.9 1.5 3.3 54 101.0 3000 7.1 1.5 3.3 59 98 3000 1.3 3.1 63 90

Claims (4)

Patent claims: 1. A process for the production of polyethylene-1,2 - diphenoxyethane - p, p '- dicarboxylate - fibers by spinning the molten polymer and taking up the fibers obtained, characterized in that a molten polyethylene -1,2 -diphenoxyethane - p, p'-dicarboxylate with an intrinsic viscosity of 0.4 to 1.3 and a proportion of residual carboxyl groups of less than 20 eq / 10 ⁶ g of the polymer is used and that the fibers obtained are taken up at speeds of 1000 to 3500 m / min with the proviso that for monofilaments of 0.3 to 1.5 denier the take-up speed is 1000 to 1800 m / min and for titers of more than 1.5 den the take-up speed is 1800 to 3500 m / min. 2. The method according to claim 1, characterized in that that the product is used as polyethylene-l, 2-diphenoxyethane-p, p'-dicarboxylate, that using a combination of a) a barium compound and a tin compound, b) a barium compound and an antimony compound and c) a calcium compound and an antimony compound as a combination of ester interchange catalyst and polymerization catalyst is. 3. The method according to claim I. characterized in that that the molten polyethylene-1,2-diphenoxyethane-p, p'-dicarboxylate by a Spinneret with 1.5 to 10 mm long holes, the diameter of which is 0.25 to 0.9 mm, extruded. 4. The method according to claim I, characterized in that the extruded polyethylene-1,2-diphenoxyethane-p, p -dicarboxylate after passing at least 30 cm from the spinneret a distant 10 to 180 C warm atmosphere.