RU2808962C2 - Method and device for forming elementary thread with change of direction - Google Patents

Abstract

FIELD: cellulose production.

SUBSTANCE: invention relates to a method for producing solid cellulose filaments from a cellulose fluid by extruding the fluid through several extrusion holes, resulting in flowable filaments, and curing the filaments in a coagulation bath, wherein the filaments in the coagulation bath are tied into a bundle and in the form of a bundle their direction is changed and pulled out of the coagulation bath above the level of the coagulation bath, wherein the bundle of filaments receives a direction change width L on the direction change device.

EFFECT: new method.

32 cl, 4 dwg, 2 tbl

Description

The invention relates to the formation and processing of extruded synthetic fiber after curing.

State of the art

Cellulose can be dissolved in aqueous solutions of amine oxides, in particular in solutions of N-oxide-N-methylmorpholine (NMMO), to produce knitting products from the resulting spinning solution, such as filaments, staple fibers, films, etc. This occurs by precipitation of extrudates in water or in dilute solutions of amine oxide, after the extrudates from the extruder are passed through the gas gap into the precipitation bath. Typically, cellulose solutions are used in the range of 4% to 23% for processing into extrusion products. Subsequently, the deposited extrudates are transported in the form of a film bundle or filament, with roller drawing mechanisms applying the necessary drawing forces (in the gas gap). This method is also called the lyocell fiber production method or the resulting cellulose filaments are called lyocell filaments.

Patent document US 4,416,698 relates to an extrusion method or spinning method for cellulose solutions for spinning cellulose into filaments. In it, the flowable spinning material - a solution of cellulose and NMMO (N-methylmorpholine N-oxide) or other tertiary amines - is extruded and placed in a settling bath to cure and stretch.

Patent documents US 4,246,221 and DE 2913589 describe a method for producing cellulose filaments or cellulose films, wherein the cellulose is drawn in a fluid form.

Patent document WO 94/28218 A1 describes a method for the production of cellulose filaments, in which a cellulose solution is spun into several strands using a spinneret. These bundles, through a gap washed by gas, are placed in a precipitation bath and are continuously released from it.

Patent document CA 2057133 A1 describes a process for the production of cellulose filaments, wherein the spinning stock is extruded and fed through an air gap into a cooled NMMO (N-methylmorpholine N-oxide) water bath.

Patent document WO 03/014432 A1 describes a settling bath with a central thread removal device below the sealing film.

Patent document EP 1 900 860 A1 describes a two-stage coagulation bath of a molding device, the baths having different H ₂ S0 ₄ compositions.

Patent document WO 97/33020 A1 relates to a method for the production of cellulose fibers, in which a solution of cellulose is extruded in tertiary amine oxide through the spinning holes of a spinneret, the extruded filaments are passed through an air gap, a settling bath and a drawing device by which the filaments are drawn, drawn The filaments are processed into cellulose fibers, and the drawn filaments are subjected during processing to a tensile force in the longitudinal direction of no more than 5.5 CH/tex.

Patent document DE 10200405 A1 describes a device for the production of faceol fibers with a blowing device in a gas gap. A settling bath device is mentioned in which a web of filaments is immersed in the settling bath, its direction is changed in the settling bath, and then it exits the settling bath again at an upward angle to the bundling device. Since bundling is done on a single strand, strong bundling should be expected when changing direction.

Patent document WO 02/12600 describes a spinning process where the maximum economical spinning speed is calculated with reference to a formula based on the linear density of the fiber, the number of rows of spinning holes and varying operating parameters.

Patent document WO 02/12599 describes a spinning process in which the direction of a web of threads is changed in a coagulation bath and then brought together point by point.

Patent document WO 96/20300 describes filament direction change angles in a method for producing lyocell fibers according to a claim reference.

The problem of damage to the filament during drawing is raised in the patent document WO 2008/019411 A1 and is approached by using a mechanical drawing device installed in the settling bath, wherein this drawing device also applies part of the drawing forces during operation. In addition to the costly construction, the danger of individual very fine filaments becoming entangled in the mechanical structure and thereby having a negative impact on the molding process but also on the function of the mechanical device should not be underestimated.

Patent document WO 2014/057022 describes sequential precipitation baths with different media.

Disclosure of the Invention

In previous methods for producing faceol fiber, all individual filaments (individual extrudates) immediately adjacent to the redirection device (eg, a round rod) are pressed against the redirection device by perpendicular forces arising from the tensile force of the overall bundle. Due to the frictional resistance that arises, this can lead to ruptures and breaks of the thread. In particular, with strong bundling, the perpendicular forces resulting from the total pulling force act only on a few individual filaments in direct contact with the direction changing device. These few individual filaments can be severely damaged by high loads of frictional forces, particularly at high drawing speeds. Another aggravating factor is that the filaments in the coagulation bath swell and, in addition, are still in a hot state, which is why the mechanical ability to withstand the load is low.

The purpose of the present invention is to minimize the friction load of each individual filament at the points of change of direction and to provide, in particular, higher productivity and higher spinning speeds. This frictional force occurs in settling baths in which, due to the operating environment, stationary direction changers or also direction changers with driven or freely rotating rollers must be used, as for example in a filament drafting mechanism.

The present invention allows the user to evaluate his system in a computational manner regarding the load of frictional forces acting on the filaments and to adjust the system by suitable measures so as to maintain a minimum frictional load on all filaments in direct contact with the redirection device.

Another object of the present invention is to provide manual handling of the filament web and the ability to access the redirection point in the processing zone between the spinneret and the drafting mechanism, without the need for expensive and often malfunctioning auxiliary threading devices or drafting devices.

The invention provides a method for producing solid cellulose filaments from a cellulose fluid, extruding the fluid through a plurality of extrusion holes, thereby producing flowable filaments; the flowing filaments preferably pass through the gas gap and solidify the filaments in the coagulation bath, wherein the filaments in the coagulation bath are tied into a bundle and, as a bundle, change their direction and are pulled out of the coagulation bath, above the level of the coagulation bath, wherein the bundle of filaments receives width L of the direction change on the direction change device, determined by formula 1:

L> (2 x LZ x cos (B/2) xv ^2.5 ) / (10 xc _cell ^0.5 x Q). Formula 1,

where L denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second, c _cell is the cellulose concentration of the extruded fluid in % by weight, Q is the dimensionless load factor, where Q = 15 or less. In Formula 1, ">" means "greater than";"x" is the multiplication sign and "cos" means cosine.

The invention also relates to a device suitable for carrying out this method, with an extrusion plate with several extrusion holes, a receiving tank for the coagulation bath, preferably with a gas gap between the extrusion holes and the receiving tank, a device for changing direction in the receiving tank to change the direction of the beam of elementary threads from the receiving reservoir and a device for tying into a bundle, setting the width L of the change in the direction of the bundle of filaments on the device for changing the direction, and the bundle of filaments on the device for changing the direction receives a width L of the change in direction, satisfying the already indicated formula 1, where L, LZ , B, v, c _cell and Q have the above value, Q = 15 or less, and v is at least 0.58 m/s (35 m/min), for which the device is therefore designed.

According to the invention, a large change in direction width L is generally obtained, so the invention also relates to a method for producing solid cellulose filaments from a cellulose fluid by extruding the fluid through a plurality of extrusion holes, whereby fluid filaments are produced, preferably by passing the fluid filaments through a gas gap, and solidification of the filaments in the coagulation bath, wherein in the coagulation bath the filaments are tied into a bundle and change direction in the form of a bundle to be pulled above the level of the coagulation bath from the coagulation bath, wherein the extrusion holes are located at a length LL, and the bundle of filaments The threads on the direction change device receive a change direction width L of at least 70% of the length LL. Accordingly, the invention also relates to a device suitable for carrying out this method, with an extrusion plate with several extrusion holes, a receiving tank for the coagulation bath, preferably with a gas gap between the extrusion holes and the receiving tank, a device for changing the direction in the receiving tank for changing the direction filament bundle from the receiving reservoir, and a bundle tying device setting a direction change width L of the filament bundle on the direction changer, wherein the extrusion holes are located at a length LL, and the filament bundle on the direction change device receives a direction change width L at least 70% of the length LL.

The further detailed description applies equally to the devices and the method, for example, the preferred features of the method also correspond to the properties or suitability of the device or its corresponding component parts, and the preferred features of the device also correspond to the means used in the method according to the invention. All advantageous features can be combined with each other unless this is expressly excluded. All features of the method, including those mentioned above, can be combined with each other. All features of the device, including the above, can be combined with each other.

Brief description of drawings

The drawings show:

in fig. 1 - image of the liquid processing zone in the form of a spinning funnel (6);

in fig. 2a - a system of precipitation baths combined with a rectangular die;

in fig. 2b - a system of precipitation baths, combined with a ring-shaped die (5) and a direct device (2) for changing direction;

in fig. 2c - a system of precipitation baths combined with a ring-shaped die, wherein the change in direction of the ring-shaped fluid extrudate occurs by means of a toroidal device for changing direction with an angle (B') of rotation and the rotated extrudate web is directed along the central axis of the annular die vertically upward from the precipitation bath;

in fig. 3a - bath system with device for changing direction and tying into a bundle. In the bundling device, the spinning fabric, with a width L and a turning angle B, changes direction;

in fig. 3b shows a bath system with two devices for changing direction, whereby, in contrast to FIG. 3a, the second change in direction does not result in bundling. With the second change in direction, the direction of the spinning web with width L and turning angle B changes;

in fig. 3c shows a reservoir system with three spinning webs changing direction in a common direction changer in the reservoir and in separate direction changers at the edge of the reservoir, from which the bundles indicated by arrows are drawn;

in fig. 4 - change of direction in the exhaust mechanism, which has drive rollers marked with the letter “M”, in top view and in side view (right). All rollers can be driven (Fig. 4a) or some of them (Fig. 4b). The supply of filament bundles is shown with an arrow. In rollers, the beams change direction at angle B (from 0° to 150°). Under “L” the width of the filament bundle on the roller is shown.

Carrying out the invention

The invention relates to changing the direction of the webs of filament threads or at least to a bundle of filament threads connected on one side. The change in direction occurs in the coagulation bath to re-lead the filaments from the bath to the outside. When changing direction, the filaments are brought perpendicular to the axis of the change in direction, so that the filaments in the first layer overlap the device for changing direction, and in other layers - on each other. This leads to stress on the material, as already mentioned, in particular at high speeds. According to the invention, the change of direction width is increased to draw filaments at any speed, even at high speeds, for example 0.58 m/s (35 m/min) or higher.

The filaments are guided with the change of direction proposed according to the invention in the form of a wide ribbon. Therefore, the term “bundle of complex threads” contains ribbons of elementary threads brought together, having a cross-section of width and height, and the width is greater than the height.

The above-mentioned formula 1 with a Q of 15 or less refers in particular to the change of direction in the coagulation bath, in which the belts, due to thermal control and swelling conditions, are particularly susceptible to the frictional influences mentioned in the abstract. The coagulation bath is an element of the processing zone for extruded filaments. When implementing the method of processing lyocell fibers, the filaments, in this case, have not yet reached their final structure and strength. The structure and strength first change during stretching (mainly in the gas gap) and diffusion of the solvent (mainly in the coagulation bath). Changes in the material may still be detectable even after exiting the coagulation bath, so the path of the filaments/extrudates between the exit of the spinneret and the leaching of solvent from the filaments/extrudates, including the draft mechanism, is called the processing zone. Since the extruded filaments do not yet have their final shape, they are also called “extrudates” in the processing area. The drafting mechanism is a device that applies the necessary drawing forces to form the filaments and to the resulting frictional forces on the filaments/extrudates during feeding from the spinneret to the drafting mechanism. Inside the coagulation bath, due to hydrodynamic conditions, the danger of windings in the driven or freely rotating direction-changing rollers is very high, so that fixed direction-changing rollers are preferably used inside the coagulation bath. From the outside of the coagulation bath, only small changes of direction should be carried out with fixed direction change mechanisms, or freely rotating or driven devices for change of direction should be used. With freely rotating or driven devices for changing direction, the filaments/extrudates are less susceptible to frictional effects, so that smaller values of the changing direction width L are used than those calculated by formula 1. However, a certain width continues to be maintained, in particular for changing direction in the exhaust mechanism, since friction effects also occur there. The task of the drawing mechanism is to provide the required drawing speed depending on the throughput of the hole (per extrusion hole). The drawing mechanism transmits the drawing speed to the filaments/extrudates by means of drive or multiple direction changing devices such as rollers or rollers. In this case, the reversing force of the roller is first transmitted to the filaments/extrudates located inside, which in turn transmits the force to the filaments/extrudates located outside. Therefore, the filaments/extrudates located inside are subject to higher stress than the external ones; According to the invention, the disparity is minimized by maintaining the width of the change of direction, generally so that the filaments/extrudates located inside are covered only by a limited number of filaments/extrudates located outside, which maintains fast and efficient operation. Extrusion holes can be drills or holes in the extrusion plate, as well as capillaries. For all of these options, the number of extrusion holes is also called the number of holes. The drawing can be carried out in a gas chamber into which the filaments enter after leaving the coagulation bath.

According to the invention, a direction changing device is a machine part that provides a change in direction of individual extrudates, extrudate webs or extrudate bundles, while preferably the direction changing device itself does not affect the direction change width L of the rotated web.

As such, such direction changing devices may be configured as a fixed direction changing device or a rotating direction changing device. Rotating devices for changing direction can be designed with or without a drive. The advantage of rotating direction changers is that low friction forces occur between the extrudate and the changer and therefore extremely gentle changeovers can be carried out - with the exception of direction changes in the traction mechanism when forces are transferred from the changer directions to filaments/extrudates. In any case, a disadvantage of rotating redirection devices is that due to the stickiness of the individual extrudates, they can stick to the rotating redirection device, causing windings, breaks and other malfunctions. Also problematic is the use of rotating devices for changing direction in liquids (in a coagulation bath), since due to hydrodynamic turbulence in the section of the changing direction of the roll, there is a very high danger that individual extrudates will be captured by these vortices around the perimeter of the device for changing direction, which can initiate windings, breakage and other malfunctions.

For use in settling bath liquids, as well as sticky, wet or otherwise sticky extrudate webs or bundles, fixed redirection devices, such as rods, coils, box-shaped redirection rolls, or any other form, are preferred.

As materials for stationary devices for changing direction, all materials having the lowest sliding friction coefficient values are taken into account. In addition to coated and uncoated metals, textile ceramics or polymer materials are also possible.

Preferably, the redirection device is used in a coagulation bath. It is also possible to use two or more direction changing devices in the coagulation bath, whereby there is a large selection of (large) rotation angles B for each direction changing device. According to the invention, formula 1 is carried out by the first, preferably also the second or also each device for changing direction in the coagulation bath. "First", "second", etc. refer in this sense to the technological proximity to the extrusion process and the sequence in which the filaments/extrudates pass through the redirection devices.

After the coagulation bath in the processing zone, the filaments/extrudates are also maintained with a certain width of change of direction as a belt, since here too, in particular in the drafting mechanism, frictional forces act, which can cause damage when changing direction. However, the width of the change in direction after a coagulation bath may be smaller than in a coagulation bath, since there may be fewer negative effects on filament strength due to temperature and swelling. According to the invention, it is preferable if the outside of the coagulation bath changes direction, at least with a width L _outside the change of direction, which corresponds to L according to formula 1 (with Q less than or equal to 15), divided by 30, preferably divided by 20, preferably divided by 10, in particular preferably divided by 5, and/or the bundle of filament threads is supported at this width L _{from the outside} (also between changes of direction) - at least up to the suction mechanism and/or the washing device. Alternatively, L _outside can be calculated using formula 1, and a higher value can be used for Q, in particular Q in this case can be given a value of up to 300 or up to 250, for example 10-300 or 40-250. In the washing device, the bundle of filament threads is usually deployed even wider to favor the washing process. L _outside can also be at least L according to formula 1 (from Q to 15), for example, during the washing process.

L _outside (the width of the change of direction or the width of the tape outside the coagulation bath) can also be determined independently of L using formula 1. It is preferable if L _outside is chosen such that, at a given drawing speed, the filament density per millimeter of the width of the change of direction is a maximum of 7000 dtech/mm , preferably a maximum of 6000 dtech/mm, a maximum of 5000 dtech/mm, in particular preferably a maximum of 4000 dtech/mm.

This change of direction width or belt width, L _outside, is maintained outside the coagulation bath, preferably at the immediate next change of direction after the filaments/extrudates exit the coagulation bath, since here the filaments/extrudates are even more sensitive and/or retained in traction mechanism, since in it the elementary threads/extrudates are especially damaged due to the transmission of force. It is advantageous if the filament bundles, after leaving the coagulation bath, throughout the entire processing zone or during the entire filament/extrudate processing process prior to cutting and/or winding of the final products, are constantly maintained at least with a width L _outside . The processing process generally comprises the following sections: forming in a coagulation bath (as described above), removing from the coagulation bath, drawing through a draft mechanism, washing, drying, winding and/or cutting the filaments as the final product.

Alternatively or additionally, the forming process, including processing, may have the following steps: extrusion through a spinneret, passing filaments/extrudates through a gas gap (into which a gas stream is preferably injected, see below) into a coagulation bath (precipitation bath), change of direction filaments/extrudates in the settling bath, preferably by means of a redirection device mounted opposite the spinneret, withdrawing the coagulated filaments/extrudates from the coagulation bath, redirecting the filaments/extrudates outside the coagulation bath and without subsequent bundling with other coagulated filaments /extrudates, supplying the filaments/extrudates to the drawing mechanism (also called draw-off mechanism or stretching device) and/or to the stretching device, as well as passing to the receiving unit of the filaments and/or to the drawing rollers, washing, drying and, if necessary, other steps depending on your desire. The device according to the invention has appropriate apparatus for this purpose. In another embodiment, the method may have the following steps: extrusion through a die, passing the filaments/extrudates through a gas gap (into which a gas stream is preferably injected, see below) into the coagulation bath, reversing the direction outside the coagulation bath, bundling or mixing with other filaments/extrudates, supplying filaments/extrudates to one or more exhaust mechanisms, washing, drying and, if necessary, other stages, or devices for this, depending on desire.

Some stages can be combined: in particular, washing can be carried out in the exhaust mechanism. At each of the stages, the detailed or preferred embodiments of the invention specified in the application and described in detail can be used. The drawing mechanism can also combine driven rollers or rollers with non-driven ones, as for example described in patent document CN 105887226 (A). A thermal treatment such as drying, as described for example in patent document CN 205133803 U, can also be carried out in the drafting mechanism. When starting the process, the piecing aid described in patent document CN 205258674 U can be used; however, it is only necessary as an aid and is not necessarily indispensable.

Additional steps or devices may be provided for this purpose. Thus, for example, after washing, drying may be carried out, or after the washing installation, a dryer may be provided, and one or more other processing steps may be provided before the drying/drying, such as, for example, a filament/extrudate priming treatment or a priming device. Additionally, before drying Other process steps may also be carried out, such as coloring, structuring, sonication, or devices or apparatus for this purpose may be provided.

At any stage of the process prior to drying, a cutting device (for cutting) or a winding device (for winding) may be intermediately connected to produce staple fibers or endless yarn from the endless filaments.

Preferably, a tensile force of less than or equal to 3 cN/dtex, preferably less than or equal to 2 cN/dtex, or less than or equal to 1.5 cN/dtex, is applied to the filaments/extrudates in the drawing mechanism.

Bundles of filaments from several spinning places can be combined into a twisted single bundle. Typically, such a connection is made immediately after or upon exiting the coagulation bath to apply downstream device elements such as pulling or washing to a single bundle. The width L or L _outside is specified in the application in most cases relative to the spinning position and increases accordingly after joining. For example, L _outside can be at least 8 mm per spinning position, for example from 8 mm to 100 mm, preferably from 12 mm to 70 mm.

A bundling device is a machine part that narrows the direction change width of an extrudate web in accordance with the geometric shape of the bundling device and thereby forms an extrudate bundle from a flat or hose-shaped or also round or otherwise shaped web of extrudates. Additionally, the bundling device also initiates a change in direction of the formed extrudate bundle. Thus, the bundling device can also be a device for changing direction, for which the rules proposed according to the invention and, preferably, the embodiments of the invention are valid. Devices for tying into a bundle can be made similarly to the description of the device for changing direction - stationary or rotating. The same materials may be used. For use in settling bath liquids, as well as sticky, wet or otherwise sticky extrudate webs or extrudate bundles, fixed bundle bundling devices are used, preferably in the form of rods, coils, box-shaped reversing rolls, hooks, eyes, or in any other form of device.

The load factor Q is an empirical value for the superimposed filaments in a direction changing device. The lower it is, the more gentle the process. The larger L should be selected. Q should be 15 or less in the coagulation bath, preferably Q is 12 or less, preferably 8 or less, or 5 or less. In this regard, Q is equal to 2 or more, preferably 3 or more, or 4 or 5 or more, and in particular preferably Q is from 2 to 15 or more, preferably from 4 to 12. Possible values for Q are: 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15 or any value in between. As stated above, Q may be larger outside the bathroom. In this case, L is symbolized by L _outside with Q to 300. Unless otherwise specified, Q refers to the change in direction in the coagulation bath.

The number of extrusion holes (also called the number of holes, abbreviated as “LZ”) determines the number of filaments that must change direction. The method proposed according to the invention is designed, in particular, for large volumes used in industry. Preferably, the number LZ of extrusion holes is 2000 or more, preferably 5000 or more, or 10,000 or more. Independently or in conjunction with this, LZ 500,000 may be equal to or less than 5,000,000, preferably 200,000 or less, 100,000 or less, or 50,000 or less. If it is necessary to simultaneously produce large volumes of product, and at the same time a larger number of filaments, several extrusion devices according to the invention can be used to produce several parallel bundles of filaments or webs, if necessary in a common coagulation bath or even with one common device for direction changes. The above numbers of holes refer to a bundle or a group of filaments changing direction together and gathering into a bundle.

The direction change angle B is determined by the angle enclosed by the filaments and filaments with a changed direction supplied to the device for changing direction (see figures). At a sharper angle, greater shear and friction forces are applied to the filaments. The sharper the angle, the more L should increase (with other parameters of formula 1 remaining unchanged). Preferably, the direction change angle B is an angle from 10° to 90°, preferably from 20° to 60° or from 25° to 45°. If nothing else is specified, angle B refers to the change in direction in the coagulation bath. Externally, for example in the suction mechanism and/or during washing, the angle of change of direction can be from 0 to 150°, in particular any angle in this range, for example specified for the angle in the coagulation bath.

According to the invention, large values of the direction change width L provide high drawing speeds. The filaments are pulled, in most cases, using a traction mechanism through a coagulation bath. The suction mechanism itself is usually located outside the coagulation bath, after the redirection device and, if necessary, also the bundling device. According to the pulling speed, select the appropriate direction change width L. Preferably, the pulling speed (in the direction changing device) is at least 0.58 m/s (35 m/min). The pulling speed v can be 0.6 m/s (36 m/min) or more, preferably 0.67 m/s (40 m/min) or more or 0.75 m/s (45 m/min) , or 0.83 m/s (50 m/min) or more. Independently or in combination, the drawing speed v may be 3.33 m/s (200 m/min) or less or 2.5 m/s (150 m/min) or less.

In the method proposed according to the invention, an extrusion medium is used as the working medium. It is preferably a solution or mixture of cellulose and other components of the working medium, for example solvents. The cellulose concentration for the processing of lyocell fibers is chosen at a normal value. Thus, the concentration of _cellulose extruded fluid is from 4% to 23%, preferably from 6% to 20%, in particular from 8% to 18% or from 10% to 16%, (all data in % by weight ). The extrusion working medium in the process of processing lyeol fibers is, as a rule, a solution of cellulose or a melt of cellulose with NMMO (N-methylmorpholine N-oxide) and water, described at the beginning. Other cellulose solutions, particularly ionic cellulose solvents, can also be used. Ionic solvents are described, for example, in patent document WO 2006/000197 A1 and preferably contain organic cations, such as, for example, ammonium, pyrimidium or imidazolium, preferably 1, 3 dialkylimidazolium halides. Water is also used, in this case, preferably, as an additive to the solvent. Particularly preferred is a solution of cellulose and butyl-3-methylimidazolium (BMIM), for example with chloride as the counterion (BMIMC1), or 1-ethyl-3-methylimidazolium (also preferably as chloride) and water.

The step of passing the flowing filaments through the gas gap according to the method of the invention, or through the gas gap in the device according to the invention, is additional, i.e. may be implemented/existed or not. At this stage/means a distinction is made between wet molding and dry-wet molding. In wet spinning, the filaments are directly introduced into the coagulation bath. In dry-wet spinning, there is a gas gap and the filaments first pass through it before they are fed into the coagulation bath.

A gas flow is optionally (and preferably in large, industrially relevant installations) injected into the gas gap, in particular in large, industrially relevant installations) or a blower is provided for this purpose in the apparatus. The injected gas stream preferably has a temperature of from 5°C to 65°C, preferably from 10°C to 40°C. The material fluid can be extruded at temperatures from 75°C to 160°C. Preferably, the gas gap has a lower temperature than the extruded material fluid. In particular, the gas flow is directed in the gas gap at a lower temperature than the extruded fluid of the material.

Possible values of the gas gap length, in particular the distance between the extrusion holes and the coagulation bath, or a reservoir for this as a bath, are preferably from 10 mm to 200 mm, in particular from 15 mm to 100 mm, or from 20 mm up to 80 mm. Preferably it is at least 15 mm. The gas in the gas gap is preferably air. The gas flow is preferably an air flow. Other inert gases are also possible. An inert gas is a gas that does not react chemically in the gas gap with flowing filaments and, preferably, also with a solidified medium, such as water or a solution of NMMO (N-methylmorpholine N-oxide) diluted in water or with other solvent components , depending on the extrusion medium used.

In wet molding, the processing area consists essentially of liquid reservoirs, liquid funnels, or liquid troughs. The extrudates leaving the die are directly sent to the settling bath liquid for precipitation and/or cooling. Wet (settled and/or cooled) extrudates are fed through wash baths and/or through a gas or air chamber to a draft mechanism.

In dry-wet molding, the processing zone consists essentially of a gas gap or air gap and downstream liquid reservoirs, liquid funnels or liquid troughs. The extrudates emerging from the extrusion holes flow through a gas gap and subsequently through a coagulation bath, also called a “precipitation bath.” The wet (settled and/or cooled) extrudates are fed through one or more washing baths and/or through a gas or air chamber to an exhaust mechanism.

With the wet molding method or the dry-wet molding method, due to the processes of displacement and drawing between the liquid of the coagulation bath and the extrudates, turbulence and vortices occur at higher speeds. Additionally, in areas where direction is changed using fixed direction change devices, there is also a risk of dry running at the contact points between the extrudate and the direction change device. The danger of dry running is greater the higher the drawing speed and the more strongly the extrudate webs or extrudate bundles are pressed against the device to change direction.

Preferably, the extrusion holes are arranged in an elongated shape to form extruded filaments with a geometry favorable for changing direction and bundling when changing direction. Therefore, the longitudinal direction of the arrangement of the extrusion holes preferably also corresponds to the longitudinal direction of the direction changing device. Therefore, this longitudinal direction of the direction changing device preferably corresponds to the direction changing axis (or follows several direction changing axes in curved direction changing devices). Possible shapes for the extrusion hole arrangement are a rectangular shape, a curved shape, a ring shape, or a ring segment shape. The oblong shape may have a length to width ratio of 100:1 to 2:1, preferably 60:1 to 5:1 or 40:1 to 10:1.

The extrusion holes have a diameter preferably from 30 µm to 200 µm, preferably from 50 µm to 150 µm or from 60 µm to 100 µm. This allows the production of filament yarns for textile products (woven and non-woven).

Preferably, the extrusion throughput is adjusted such that a linear fiber density of the individual fibers of 1.3 dtex is obtained at a given draw speed. +/-50%, preferably +/-25% or +/-10%. The extrusion throughput can be controlled by the pressure of the extruded mass, in particular the cellulose solution. Possible pressure values are, for example, from 0.5 to 10 MPa (5 to 100 bar), preferably from 0.8 to 4 MPa (8 to 40 bar).

Particularly advantageous, also according to a separate main feature of the invention, independent of formula 1, is a generally large direction change width L. Depending on or independently of formula 1, the extrusion holes can be located along the length LL, whereby according to this feature of the invention the direction change width L is at least 70%, preferably at least 80% or also at least 90% of length LL. The direction change width may be equal to the length LL or may be even greater, such as 110% of the length LL or more. L _outside is preferably at least 1%, at least 3%, preferably at least 5% or also at least 10% of the length LL. For bundling purposes, L _outside - preferably a maximum of 50% of the length LL. All method and device adjustment parameters proposed according to the invention can be combined with each other. For example, a particularly preferred combination is a pulling speed v of 0.66 m/s to 2.5 m/s (40 m/min to 150 m/min) and a load factor Q of 4 to 13, or 5 up to 12. Of course, all values described in the application are possible within these ranges or even beyond them.

Examples:

The liquid processing zone for the dry-wet molding method can be designed in different ways, some options are described by means of figures 1, 2a, 2b, 2c, 3a and 3b. Experimental parameters and results are provided in Table 1.

In fig. 1 shows a first embodiment of the invention of a liquid processing zone in the form of a spinning funnel. In this embodiment, the liquid of the settling bath is fed through the loading point (1) into a funnel-shaped reservoir (6). The funnel-shaped tank (6) has a bottom hole at the lower end. Using a bundle-binding device (2) inserted into the bottom hole, part of the supplied precipitation bath is withdrawn along with the extrudates (4) passed from top to bottom through the spinning funnel. The excess part of the precipitation bath is discharged through the overflow edge (3). The overflow edge (3) also serves to adjust the air gap (7). The extrudates emerging from the spinneret (5) are bundled as they flow vertically downwards and removed through the bundling device (2) from the spinning funnel. The cross-section of the device (2) for tying into a bundle can be made round, oval, polygonal or in the form of a slot.

The angle (B) of change in direction is obtained from the vertical distance (H) between the nozzle mouth (5) and the bundling device (2), as well as from the specified geometric parameters of the die (5). The change-of-direction width (L) is the portion of the change-of-direction device to which the extrudates actually contact and change direction or bundle. In the toroidal bundling device (2), the width (L) of the direction change is obtained from the derivative of the bundling diameter (D) and the number π (3.1415...). The angle (B) of direction change is obtained from the selected geometric parameters. The minimum required width (L) of direction change is calculated using Formula 1.

In figures 2a, 2b, 2c, 3a and 3b, the liquid treatment zone is depicted as a precipitation bath. With these options, the liquid of the settling bath (coagulation liquid) is supplied through the loading point (1) into a bath-shaped reservoir (8) formed in any way. The liquid is again drained through the overflow lip (3) from the reservoir. The overflow edge (3) also serves to adjust the air gap (7). A device (2) for changing direction and/or, if necessary, a device for bundling is installed inside the precipitation bath (8). The extrudates (4) coming out of the die (5) are directed vertically down into the bath (8). In the device (2) located in the precipitation bath, the direction of the extrudates (4) is changed to change the direction, and if necessary, they are also tied into a bundle, leading upward from the precipitation bath and fed to other processing steps. The device for changing direction or for tying into a bundle can be made round, oval or polygonal in cross section. For example, the device for changing direction can also be a box-shaped or slat-ribbed roller consisting of several rods, as well as a guide roller with ribs located transverse to the direction of transport of the extrudate. According to another embodiment of the invention, the device (2) for changing the direction can also be made concave in the axial direction to ensure, in addition to changing the direction of the extrudates (4), also binding the extrudate into a bundle. Since elements rotating in the settling bath liquid inevitably lead to turbulence in the settling bath and, as a consequence, to twists, breaks and other malfunctions, devices for changing direction are made in the settling bath mainly, preferably, in the form of stationary devices for changing direction.

The vertical distance (H) between the mouth of the die (5) and the bundling device (2) is adjusted so that the nozzle draw angle is less than 45°, less than 30°, less than 15°, or preferably less than 10°. This measure allows the extrudates to be pulled out gently and with a slight change in direction from the die channel. Depending on the vertical distance (H) and the angle of extraction from the die, the angle (B) of change in direction is adjusted for given geometric parameters. The redirection width (L) is that portion of the redirection device's length at which the extrudates are directly adjacent and redirected or bundled; Accordingly, with a (concave) device for changing direction, this is the extended length of the contact line occupied by the extrudates. The angle (B) of direction change is obtained from the selected geometric parameters. The minimum width (L) of direction change is calculated using Formula 1.

In fig. Figure 2a shows a settling bath system combined with a rectangular shaped extrusion hole arrangement. Typical for a bath system with a rectangular die are small angles of change of direction (B) with a large width of change of direction (L).

In fig. 2b shows a settling bath system combined with an annular extrusion hole arrangement. In contrast to the rectangular die system (Fig. 2a), this embodiment of the invention has disadvantages. The drawing angle from the die compared to the rectangular die design according to FIG. 2a is significantly larger, as a result of which gentle pulling out of the die channel is no longer ensured. Therefore, in particular with large diameters of annular dies, it is necessary to significantly increase the vertical distance (H) between the die and the device to change direction significantly. Since with large annular dies the required vertical distance (H) can be much greater than 1 meter, manual access to the device for changing direction becomes difficult, in addition, large frictional forces between the extrudates and the coagulation bath negatively affect the overall stress in the elementary bundle threads Another disadvantage of the embodiment according to FIG. 2b is the need for an annular die not only to change the direction in the precipitation bath, but also to bundle it in order to ensure, as possible, the same conditions for all annularly arranged extrudates. For a bath system with an annular die and centric bundling in the settling bath, small angles of change of direction (B) with a small width (L) of change of direction are rather typical.

In fig. 2c shows a system of precipitation baths, in combination with a ring-shaped die, wherein the change of direction of the annular extrudate web is carried out using a toroidal device for changing direction with an angle (B') of the change of direction and the changed direction of the extrudate web is directed vertically upward from the precipitation bath, along the central axis ring die. Above the annular die and thus outside the precipitation bath, the extrudate web is bundled, preferably at a large angle of change of direction. Since the bundling or redirection is carried out outside the settling bath liquid, the bundling or redirection can also be carried out using freely rotating rollers, so that no sliding friction can occur between the extrudate bundle and the redirection device. Another embodiment of the invention for bundling above the annular die, similar to the spinning hopper, provides a toroidal bundle tying device and, if necessary, installation of a freely rotating, direction-changing roller located downstream. With the system of FIG. 2c, it is possible to eliminate many of the disadvantages that the system of FIG. 2b. The drawing angle (A) from the die is significantly reduced compared to the annular die design of FIG. 2b, as a result of which a more gentle drawing from the die is obtained. Even with large dies, the vertical distance (H) can be kept small, thereby ensuring manual access to the device for changing direction. Binding of the extrudate web into a bundle in the precipitation bath is not required. For a bath system with an annular die and a toroidal device for changing direction in the settling bath, rather small angles of change of direction (B) with a large width (L) of change of direction are typical.

In fig. 3a shows a comparative example in the form of a settling bath system in combination with a rectangular die, the extrudate web changing direction twice in the settling bath. The first direction changing process, viewed in the manufacturing direction, is carried out similarly to the embodiment of FIG. 2a, the second change in direction serves to further change the direction and at the same time to bind the extrudate web into an extrudate tow. For the illustrated bundling reversal system, moderate reversal angles (B) with a small reversal width (L) due to the bundling are rather typical. Due to the increased binding into a bundle, it was necessary to choose a large load factor of 20. The spinning and technological properties turned out to be unsatisfactory.

In fig. 3b shows the same precipitation bath system as in FIG. 3a, however, the second change in direction was calculated based on a significantly lower load factor (no or little bundling). Due to the greater length (L) of the direction changing device, in contrast to the embodiment of FIG. 3a, achieve fairly satisfactory spinning properties.

After leaving the coagulation bath, the bundles are pulled out and washed together using a suction mechanism and a washing station, which can also be combined with each other. The first drawing mechanism, after the bath, transmits the speed of drawing the threads during molding. In fig. 4 shows a possible traction mechanism, and it has five rollers, three with a motor (“M” - in a circle, shown schematically). Any number of rollers suitable for the system can be used, for example, from one to sixty. In this case, the beams will change direction in the rollers at an angle B from 0° to 150°. In this case, it is also preferable if the width of the filament bundles is also maintained according to formula 1, and Q can be greater than in the coagulation bath, for example, from 40 to 300. All rollers or only some of the rollers can be driven. All drive rollers can be driven together or individually. When washing simultaneously, different speeds are recommended, at least for the rotation of the surface of the roller; for rollers of the same size, also the speed of rotation of the rollers themselves, since during washing the filaments lose the solvent and shrink. To prevent the elementary threads from breaking, the shrinkage process should be reflected in a decrease in speed. Non-driven rollers can be freely rotating rollers. With drive rollers, contact friction occurs between the filaments and the roller; with non-driven rollers - sliding friction between the filament and the roller.

To produce a cellulose solution, an ionic solution has been prepared as an alternative and parallel to the process for producing lyeol fibers using NMMO/water as a solvent. In this case, the cellulose used, such as eucalyptus cellulose, was suspended in desalinated water. Once the cellulose fibers are completely suspended in the desalinated water, excess water is separated by filtration and the resulting cellulose cake is pressed to a solids concentration of approximately 50% cellulose. After dewatering, the cellulose spun cake is sent to split the fibers through a needle roller and shredder. The resulting finely ground wet cellulose is added in a continuous sequence to the aqueous ionic liquid 1-N-butyl-3-methylimidazolium chloride (BMIMC1) to create a pre-mix. Suitable apparatus for this are circular bed mixers and/or turbulent mixers.

The mixture of water, cellulose and BMIMC1 (1-butyl-3-methylimidazolium chloride) is added later in the process to produce a cellulose solution, into a continuously operating vertical kneading machine of the "Reactotherm" type from Buss-SMS-Canzler GmbH. Similar kneading and reactor technology devices, as well as all types of extruders, high-viscosity thin layer stacker, stirred tank reactor and/or disk reactor can be used to make cellulose solutions individually or in combination in different reactor zones and process steps. In this vertical kneading machine "Reactotherm" with intensive mixing and kneading action it is possible to continuously produce lump-free cellulose solution. Treatment times in individual reactor zones of 20 to 80 minutes result in complete dissolution of cellulose.

To reliably control the process, other stabilizers are added to the aqueous mixture of ionic liquid and cellulose before transferring it from the preliminary mixture into the cellulose solution to stabilize the solvent and to prevent the destruction (destruction) of cellulose. The continuously produced pre-mixture is converted by applying temperature and reduced pressure (vacuum) and shear into a viscoelastic solution. The temperatures used at the individual stages of the process varied from 85°C to 150°C, with the removal of excess water carried out at a reduced pressure between 0.001 and 0.015 MPa (10 and 150 mbar). To homogenize the premix, the applied shear rates were varied from 0.33 to 3.33 rps (20 to 200 rpm), while maintaining the set shear power and torque. This ensured the dissolution of cellulose in the ionic liquid. The highly viscous cellulose solution thus obtained was subjected to additional process steps such as degassing and filtration before spinning. To adjust the quality of the spinning mass corresponding to the cellulose, the solution was additionally fed through one or more high-viscosity heat exchangers of the Sulzer SMR/SMXL type, adapted to the process steps. In addition to temperature control, they primarily also serve to regulate the desired viscosity of the spinning solution as well as the degree of polarization of the cellulose. Therefore, these heat exchangers served for effective temperature control, in particular cooling or heating of a highly viscous cellulose solution, since they provided efficient mixing and controlled heat transfer.

Spinning of the cellulose solution into filaments, as well as further processing, was carried out according to the invention, the spinning solution being fed by means of a spinning pump into a heated knitting package consisting of a pre-spun, distribution plates and a spinneret. The spinning temperatures were distributed in the range from 85°C to 150°C, preferably in the range from 95°C to 115°C. After the solution preparation step, attention was paid to a short residence time at elevated temperatures in the process complex to adapt the cellulose solution to the processing speed and unwanted destruction of the cellulose.

The molding method that has found application is described according to the invention and is usually called the dry-wet molding method, with an adjustable, height-adjustable air gap located between the die and the aqueous coagulation bath containing the ionic liquid. The gas flow supplied into the air gap and thereby passing through the filaments passes in a state corresponding to the standard and can be either air or another inert forming gas corresponding to the standard. According to the invention, the filaments are passed through a coagulation bath, removed from the bath and supplied as described above for subsequent processing. Parameters and product properties from experiments with BMIMCl (1-butyl-3-methylimidazolium chloride) and NMMO (N-methylmorpholine N-oxide) as solvents are summarized in Table 2.

table 2

Ionic liquid -N-methylmorpholine N-oxide (BMIMCl) (NMMO) Cellulose Eucalyptus Eucalyptus Average degree of polymerization of copper-ammonium complex [-] 535 646 α. Cellulose content. [%] 95.2 94.8 Content of carboxyl groups [µmol/g] 17 27 Content of divalent groups [µmol/g] 23 29 Ash content [%] 0.4 0.2 Whiteness level WClE [-] 82 84 Fiber Characteristics Cellulose solids content of ionic liquid [%] 13.27 12.8 Average degree of polymerization of the copper-ammonium complex [-] 521 584 Zero shear viscosity at 85°C. [Pass] 39-720 19.250 Spinning mass temperature [WITH] 102 95 Die hole diameter [µm] 90 90 Spinning mass pressure before the spinneret [bar] 37 27 Air gap [mm] 43 38 Temperature of the precipitation bath [WITH] 20 18 Linear fiber density [dtex] 1.63 1.71 Breaking load according to standard [sN/tex] 51.2 41.0 Stretch to standard [%] 13.9 15.2 Wet material module [sN/tex] 297 185 Number of wet cleanings [E] 54 38

Claims (48)

1. A method of making cured cellulose filaments from a cellulose fluid, comprising the steps of extruding the fluid through a plurality of extrusion holes thereby forming flowable filaments, and curing the filaments in a coagulation bath, wherein the filaments in the coagulation bath are bundled and in the form of a bundle, their direction is changed and pulled out of the coagulation bath above the level of the coagulation bath, characterized in that the bundle of filaments takes on the direction change width L on the direction change device, adjusted according to the formula L>(2×LZ×cos(B/2)×v ^2.5 )/(10×s _cell ^0.5 ×Q), where L denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second, c _cell is the cellulose concentration of the extruded fluid in % by weight, Q is the dimensionless load factor, where Q=15 or less. 2. The method according to claim 1, characterized in that it includes the step of passing flowing filaments through a gas gap before curing the filaments in a coagulation bath. 3. Method according to claim 1 or 2, characterized in that Q is from 2 to 15. 4. Method according to any one of paragraphs. 1-3, characterized in that the number LZ of extrusion holes is from 2000 to 500,000. 5. Method according to any one of paragraphs. 1-4, characterized in that the angle B of the direction change is an angle from 10 to 90°. 6. Method according to any one of paragraphs. 1-5, characterized in that the pulling speed v is from 0.6 m/s (36 m/min) to 3.33 m/s (200 m/min). 7. Method according to any one of paragraphs. 1-6, characterized in that _{the cell} cellulose concentration of the extruded fluid is from 4 to 23%, all data in % by weight, and the extruded fluid contains cellulose, NMMO (N-methylmorpholine N-oxide) and water or cellulose , organic cationic solvent and water. 8. Method according to any one of paragraphs. 2-7, characterized in that a gas flow is injected into the gas gap; a blower is provided in the device for this purpose, and the gas flow has a temperature from 5 to 65°C. 9. Method according to any one of paragraphs. 1-8, characterized in that the extrusion holes are arranged in an oblong shape, a rectangular shape, a curved shape, an annular shape or an annular segment shape, wherein the oblong shape has a length to width ratio of 100:1 to 2:1. 10. Method according to any one of paragraphs. 1-9, characterized by the following additional steps: removing the coagulated filaments from the coagulation bath, changing the direction of the filaments outside the coagulation bath, supplying the filaments to the traction mechanism and/or stretching device, as well as carrying the filaments/extrudates to the receiving unit, washing and drying of the filaments, optionally including additional steps: priming, dyeing, structuring, sonication, cutting and/or winding of the corresponding filaments/extrudates. 11. The method according to claim 10, characterized in that when the direction of the filaments outside the coagulation bath changes, they are additionally tied into a bundle with other coagulated filaments. 12. Method according to any one of paragraphs. 1-11, characterized in that the extrusion holes have a diameter from 30 to 200 microns. 13. Method according to any one of paragraphs. 1-12, characterized in that the extrusion holes are located along the length LL and the width L of the direction change is at least 80% of the length LL. 14. Method according to any one of paragraphs. 1-13, characterized in that the bundle of filaments receives, on a direction change device located outside the coagulation bath, a width L _outside the direction change, adjusted according to the formula L _outside >(2×LZ×cos(B/2)×v ^2.5 )/(10×c _cell ^0.5 ×Q), where L _outside denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second , c _cell is the cellulose concentration of the extruded fluid in % by weight and Q is the dimensionless load factor, where Q=300 or less; at least upon the first change of direction after the filaments leave the coagulation bath and/or at least upon a change of direction in the traction mechanism. 15. A device for changing the direction of a bundle of filaments for implementing the method according to claim 1, containing an extrusion plate with a plurality of extrusion holes, a receiving tank for a coagulation bath, a device for changing the direction in the receiving tank for changing the direction of a bunch of filaments from the receiving tank, and a device for tying into a bundle that sets the direction change width L of the filament bundle on the direction change device, wherein the filament bundle on the direction change device takes on the direction change width L satisfying the formula L>(2×LZ×cos(B/2)×v ^2.5 )/(10×c _cell ^0.5 ×Q), where L denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second, c _cell is the cellulose concentration of the extruded fluid in % by weight, Q is the dimensionless load factor, with Q=15 or less, and v is at least 0.58 m/s (35 m/min). 16. The device according to claim 15, characterized in that it contains a gas gap between the extrusion holes and the receiving tank. 17. Device according to claim 15 or 16, characterized in that Q is from 2 to 15. 18. Device according to any one of paragraphs. 15-17, characterized in that the number LZ of extrusion holes is from 2000 to 500,000. 19. The device according to any one of paragraphs. 15-18, characterized in that the angle B of the direction change is an angle from 10 to 90°. 20. The device according to any one of paragraphs. 15-19, characterized in that the pulling speed v is from 0.6 m/s (36 m/min) to 3.33 m/s (200 m/min). 21. The device according to any one of paragraphs. 15-20, characterized in that _{the cellulose} concentration of the extruded fluid is from 4 to 23%, all data in % by weight, and the extruded fluid contains cellulose, NMMO (N-methylmorpholine N-oxide) and water or cellulose , organic cationic solvent and water. 22. The device according to any one of paragraphs. 16-21, characterized in that a gas flow is injected into the gas gap; a supercharger is provided in the device for this purpose. 23. The device according to any one of paragraphs. 15-22, characterized in that the extrusion holes are arranged in an oblong shape, a rectangular shape, a curved shape, an annular shape or an annular segment shape, wherein the oblong shape has a length to width ratio of 100:1 to 2:1. 24. The device according to any one of paragraphs. 15-23, characterized in that it is designed to carry out the following additional steps: removing coagulated filaments from the coagulation bath, changing the direction of the filaments outside the coagulation bath, supplying the filaments to the traction mechanism and/or to the stretching device, as well as passing them to the receiving filament/extrudate unit, washing and drying the filaments. 25. The device according to claim 24, characterized in that it is designed to change the direction of the filaments outside the coagulation bath with additional binding into a bundle with other coagulated filaments. 26. The device according to any one of paragraphs. 15-25, characterized in that the extrusion holes have a diameter from 30 to 200 microns. 27. The device according to any one of paragraphs. 15-26, characterized in that the extrusion holes are located along the length LL and the width L of the direction change is at least 80% of the length LL. 28. The device according to any one of paragraphs. 15-27, characterized in that the bundle of filaments receives, on a direction change device located outside the coagulation bath, a width L _outside the direction change, adjusted according to the formula L _outside >(2×LZ×cos(B/2)×v ^2.5 )/(10×c _cell ^0.5 ×Q), where L _outside denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second , c _cell is the cellulose concentration of the extruded fluid in % by weight and Q is the dimensionless load factor, where Q=300 or less; at least upon the first change of direction after the filaments leave the coagulation bath and/or at least upon a change of direction in the traction mechanism. 29. A method of making cured cellulose filaments from a cellulose fluid, comprising the steps of extruding the fluid through a plurality of extrusion holes thereby forming flowing filaments, passing the flowing filaments through a gas gap, and curing the filaments in a coagulation bath, wherein the filaments in the coagulation bath they are tied into a bundle and in the form of a bundle they change their direction and are pulled out of the coagulation bath above the level of the coagulation bath, characterized in that the extrusion holes are located along the length LL, and the bundle of filaments on the direction change device takes on the direction change width L, amounting to at least 80% of the length LL. 30. The method according to claim 29, characterized in that the bundle of filaments receives a width L outside the direction change on the direction change device _outside the coagulation bath, adjusted according to the formula L _outside >(2×LZ×cos(B/2)×v ^2.5 )/(10×c _cell ^0.5 ×Q), where L _outside denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second , c _cell is the cellulose concentration of the extruded fluid in % by weight and Q is the dimensionless load factor, where Q=300 or less; at least upon the first change of direction after the filaments leave the coagulation bath and/or at least upon a change of direction in the traction mechanism. 31. A device for changing the direction of a bundle of filaments for implementing the method according to claim 29, containing an extrusion plate with a plurality of extrusion holes, a receiving tank for a coagulation bath, a gas gap between the extrusion holes and the receiving tank, a device for changing direction in the receiving tank for changing the direction a bundle of filaments from the receiving reservoir and a device for tying into a bundle, setting the width L of the direction change of the filament bundle on the device for changing the direction, characterized in that the extrusion holes are located along the length LL, and the bundle of filaments on the direction change device receives the width L of the change direction, constituting at least 80% of the length LL. 32. The device according to claim 31, characterized in that the bundle of filaments receives a width L _outside the direction change on the device for changing direction outside the coagulation bath, adjusted according to the formula L _outside >(2×LZ×cos(B/2)×v ^2.5 )/(10×c _cell ^0.5 ×Q), where L _outside denotes the beam reversal width in millimeters, LZ is the number of extrusion holes, B is the redirection angle calculated from 180° minus the angle of filament wrapping around the redirection device in degrees, v is the filament drawing speed in meters per second , c _cell is the cellulose concentration of the extruded fluid in % by weight and Q is the dimensionless load factor, where Q=300 or less; at least upon the first change of direction after the filaments leave the coagulation bath and/or at least upon a change of direction in the traction mechanism.