Extrusion method

Abstract

A method is provided for producing solid cellulose filaments or films from a solution of cellulose, NMMO (N-methylmorpholine-N-oxide) and water, including pressure-extruding the solution by one or more extrusion openings and by solidifying the filaments or films in a precipitation bath. The solution is guided between the extrusion opening and the precipitation bath by an air gap, the temperature of the solution on the extrusion opening being lower than 105 C. and the pressure difference in the air gap between the pressure of the solution immediately prior to extrusion and after extrusion is between 8 and 40 bar.

Claims

1. A method for producing solid cellulosic shaped articles, or films, from a solution of cellulose, NMMO (N-methylmorpholine N-oxide) and water, comprising: extruding the solution through one or more extrusion openings under pressure and solidifying said articles, or films, in a collecting bath, wherein a length of the solution extends between the extrusion openings and the collecting bath; and guiding the solution through an air gap with a gas flow between the extrusion openings and the collecting bath, the temperature of the solution at the extrusion openings is below 105 C. and the pressure difference between the pressure of the solution immediately before extrusion and after extrusion in the air gap is between 8 and 40 bar, wherein the gas flow is guided against the entire length of the solution extending between the extrusion openings and the collecting bath by a fan and an additional flow guide element.

2. The method according to claim 1, wherein the temperature of the solution is between 80 C. and 98 C.

3. The method according to claim 1, wherein the pressure difference is between 16 bar and 38 bar.

4. The method according to claim 1, wherein the pressure immediately before extrusion is between 13 and 50 bar.

5. The method according to claim 1, wherein the pressure after extrusion in the air gap is between 0.5 bar and 3 bar.

6. The method according to claim 1, further comprising guiding a lateral gas flow in the air gap.

7. The method according to claim 6, wherein the gas flow is between 30 to 300 liters/h of gas per mm of length of the region of the extrusion openings in the gas flow direction or is between 0.15 and 20 liters/h of gas per mm.sup.3 of spinning field volume in the air gap.

8. The method according to claim 6, wherein the region between the extrusion openings and the collecting bath is flushed substantially completely by the gas flow.

9. The method according to claim 6, wherein the gas flow is laminar.

10. The method according to claim 6, further comprising a plurality of extrusion openings provided in the direction of the gas flow.

11. The method according to claim 6, wherein a partial flow of the gas flow is heated by one of an extrusion plate comprising the extrusion openings or by a heating element in the fan.

12. The method according to claim 1, wherein said articles are selected from cellulose filaments, cellulose staple fibres, cellulose non-woven articles or cellulose films.

13. The method according to claim 1, wherein one or more components solubilising the cellulose are separated from the extruded solution by the gas flow.

14. The method according to claim 13, wherein the components separated by means of the gas flow are discharged from the spinning field on a flow-off side.

15. The method according to claim 14, wherein the components discharged from the spinning field on the flow-off side are crystallised.

16. A method for producing solid cellulosic shaped articles, or films, from a solution of cellulose, NMMO (N-methylmorpholine N-oxide) and water, comprising: extruding the solution through one or more extrusion openings under pressure and solidifying said articles, or films, in a collecting bath, wherein a length of the solution extends between the extrusion openings and the collecting bath; and guiding the solution through an air gap with a gas flow directed toward the entire length of the solution extending between the extrusion openings and the collecting bath by a fan and an additional flow guide element, the temperature of the solution at the extrusion openings is below 105 C. and the pressure difference between the pressure of the solution immediately before extrusion and after extrusion in the air gap is between 8 and 40 bar so that NMMO particle formation in the air gap is reduced.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The present invention will be illustrated further by the following figures and examples without being limited to these specific embodiments of the invention.

(2) FIG. 1 shows an extrusion device with extrusion openings 1 and a fan 2 with gas flow discharge openings 3. The extrusion openings 1 are provided on an extrusion plate 6 that is curved in the direction of the gas flow. The entry into a collecting bath is denoted by point 8. The extrusion device further has flow-guiding elements 7, which can be provided on the onflow side (a) and/or on the flow-off side (b). The flow-guiding element, besides the gas flow guidance, has a second purpose, specifically the covering of the collecting bath, such that the transfer of moisture of the collecting bath into the spinning field is reduced. FIG. 1b shows different alternative positions for the flow-guiding element 7b.

(3) FIG. 2 shows a three-dimensional illustration of a spinning field of an extrusion device with an air gap.

(4) Extrusion openings are illustrated by points, from which spinning fibres (not illustrated) exit. A spinning gas volume of which the nature is measured and influenced in accordance with the invention is defined around the fibres.

(5) FIG. 3 shows a device for particle measurement comprising a spinneret 1, the indicated direction of flow of the spinning material 1, a sampling probe 3 and a particle counter 4.

(6) FIG. 4 shows the measured particle size distribution (Dp) as a function of the number of particles. The individual superimposed curves show the distribution from the largest distance between the probe and the collecting bath (upper curve) to the smallest distance (lowermost curve). The frequency of the particles increases with greater distance from the spinneret.

(7) FIG. 5 shows examinations of the heat tone of cellulose/amine oxide/water mixtures, as also occur in the spinning field, at different temperatures and pressures. An exothermic decomposition reaction is initiated at all pressures from a temperature of approximately 190 C. Surprisingly, an endothermic process, which is absent at higher pressures, appears at 1 bar in the range from 60 C. to 150 C. with a maximum at 105 C. to 110 C. This can be attributed to rearrangements in the crystal structure of the spinning solution and to evaporation processes, which indicate a delivery or absorption of heat from/into the polymer solution and the substances released respectively.

DETAILED DESCRIPTION

EXAMPLE

(8) In accordance with this example, an extrusion device as illustrated in FIG. 1 is used. In this form, an extrusion device contains an extrusion plate 6, which is curved in the direction of the gas flow, with a profile at extrusion openings 1 which reproduces the profile of the surface of a water bath as a collecting bath when the material fluid flows thereinto. As a result of extrusion under pressure, the material fluid is shaped by the shape of the extrusion openings, for example into filaments, and is drawn further by passing through the gas flow. As a result of cooling, the tackiness is reduced in order to prevent adhesion upon entry into the water bath.

(9) During operation, an extrusion device according to FIG. 1 was tested when spinning cellulose filaments with a cellulose-NMMO-water solution.

Example 1

Analysis of the Conditions in the Air Gap

(10) A spinning solution (cellulose: 12.9%, NMMO 76.3%, water 10.8%, all % in % by weight) is produced by mixing an aqueous amine oxide solution and cellulose by removing excess water in an evaporation process upstream of the spinning process, wherein the cellulose (the polymer) dissolves in the concentrated solvent to form a polymer material. Already during this solution production process, which is carried out at negative pressure, it was established that NMMO, NMM (N-methylmorpholine=decomposition product of NMMO) and M (morpholine=decomposition product of NMMO and NMM, NMMO=N-methylmorpholine N-oxide) and also water can be separated in the evaporation process via the gas phase.

(11) The spinning process results in expansion evaporation as a result of the extrusion of the spinning material because the spinning material fed to the extrusion nozzle is under a suitable conveying and extrusion pressure and this extrusion pressure is decreased to the ambient pressure of the system once the respective melt particle has exited from the spinneret bore. Spinning pressures up to 250 bar are usual in a spinning method, depending on the composition (cellulose concentration of the spinning solution). Due to the previously mentioned expansion evaporation or due to the pressure relief of the spinning solution from the high pressure level, at temperatures from 90 to 110 C., to a low pressure level (lower ambient temperature), a violent bubbling movement of the solubilising components (NMMO and H.sub.2O) is produced in the filament. The vapour bubbles forming rise from the cellulose solution (flash vaporisation). The escaping particles therefore enter the air gap space in a highly accelerated manner.

(12) Due to the expansion (evaporation of the solubilising components), the energy necessary to evaporate the solubilising components is removed from the spinning solution flow, wherein the filament cools by itself as a result of the energy withdrawal. It has surprisingly been found that not only water (Simon, Int. J. Heat Mass Transfer. Vol. 37, No. 7, pp. 1133-1142, 1994), but also NMMO, NMM and M are evaporated from the spinning solution.

(13) Since the composition of the solubilising component in the spinning solution (NMMO hydrate) is at such a ratio that the evaporated solubilising component (NMMO hydrate) transitions into the crystal form at temperature conditions below 75 C., the particle formation was observed during and after the spinning process and an attempt was made to control this by modifying the process parameters in order to provide a microclimate in the air gap region for an optimally progressing spinning process.

(14) Aerosols and crystals transported away can be easily determined in the flow-off region of the spinneret and are not present in the onflow region of the nozzle. These aerosols, besides the gaseous components, such as air (O.sub.2 and CO.sub.2), CO, NMM and M, also consist of the NMMO hydrate compound formed (monohydrate). It is known that there are various forms of NMMO in the form of adsorbed crystallisation water.

(15) Sampling from the Spinneret Flushing Gas:

(16) The spinning gas was sampled as representatively and loss-free as possible on the exhaust air side, which is charged with aerosols. This was achieved using a measuring probe, wherein the probe was designed in accordance with VDI2066. The design was implemented individually so that isokinetic sampling was ensured.

(17) The sampling line was introduced beneath the spinneret, wherein the positioning of the probe was varied over the height of the air gap and over the distance between the sampling probe and the nozzle midpoint. FIG. 3 shows the measuring arrangement.

(18) Carrying Out the Measurement:

(19) The measurement of the aerosol ejected from the spinning process was carried out using an optical particle counter of the SMPS type (Scanning Mobility Particle Sizer Spectrometer) by TSI.

(20) With this method, the particles are electrically charged and are then fractionated in a differential mobility analyser (DMA). The fraction is counted using a condensation core counter. In principle, any fractions can be isolated from the aerosol and counted by varying the control voltage at the DMA. The entire distribution is thus obtained gradually.

(21) The condensation core counter can detect particles from approximately 3 nanometers in diameter. With regard to particle size, the system is limited upwardly to approximately 1 micrometre of particle diameter.

(22) Sampling was performed in accordance with VDI 2066 using a probe which was fabricated from steel (1.4301) and which was encased and designed as a counterflow heat exchanger. Temperatures between 0 C. and 60 C. were able to be set, wherein the drawn spinning gas volume flow rate was set between 3 m/s and 4 m/s.

(23) The air feed at the spinneret was arranged closely along the longitudinal side of the nozzle and screened the spinneret from the side so that transverse flows by drag could be excluded.

(24) The precipitation bath surface was also covered laterally and on top on the onflow side and also on the flow-off side so that no moisture could be drawn during the measurement.

(25) Filter measurements were also performed for the chemical analysis of the drawn aerosol product in order to analyse the particles in terms of mass in addition to the size analysis. PTFE membranes with pore diameters from 200 to 300 nanometers were used for the filter measurements.

(26) The temperature of the measuring probe was set to 18 C., and in any case so high that no crystallisation of water contained in the air was possible, so that the measurement result could not be falsified. In this case, the spinning gas temperature was approximately 60 C. The probe was not cooled any lower in order to avoid condensate and crystallisation formation as detailed above as a result of drawn moisture from the ambient air, since, in accordance with the thesis forming the basis of the invention (separation of NMMO monohydrate crystals from the spinning polymer solution), a feed of moisture via condensate formation would have led to the dissolution of the NMMO monohydrate crystals and it would not have been possible to measure the particle size and number.

(27) FIG. 4 shows a particle size distribution for various positions of the aerosol measurement. It can be derived from FIG. 4 that the frequency of particles in the aerosol increases with greater distance from the nozzle. From this, it can be derived that the particles must originate from a condensation/crystallisation process, wherein the crystallisation or the frequencies of particles increases with greater distance from the nozzle.

(28) Since the probe was cooled to 18 C., as a result of which no water crystals could form, the measurement results clearly indicate the presence of aerosols that can be condensed or crystallised. The crystallisation product is to be attributed to an NMMO hydrate compound. The proportion of water in the NMMO monohydrate compound is only approximately 13%.

(29) Due to the arrangement according to the invention of the treatment zones of the spinning fibres in the air gap and supply with corresponding flushing gas, the microclimate can be influenced and set in such a way that the nucleation or crystallisation of the NMMO hydrate compound (crystal compound) can be prevented or delayed in the region of the extrusion openings.

(30) Severe cooling in the region of the air gap, but particularly immediately after the shaping, results in increased crystallisation of the previously evaporated NMMO hydrate immediately after the exit from the extrusion opening, whereby the crystallisation heat is introduced into the gas space and the released heat heats the gas space or consequently negatively influences the spinning process.

(31) Results of the Aerosol Filter Sampling

(32) It was found during the measurements that the material filtered from the spinning gas quickly blocks the filter pores of the PTFE filter membrane.

(33) NMMO monohydrate as a crystallised produce could also be determined via tests carried out by light microscopy. These observations also correspond in so far as NMMO monohydrate crystallises and forms deposits, in the case of a continuously operating spinning device, in the flow-off region, but also in an onflow region not constructed optimally, particularly with use of open jet blasting. In any case, the deposition of crystals could be detected by conducting the spinning exhaust gas flow past a cooled metal surface, since the NMMO crystal forms can deposit on the cooled surface.

Example 2

Polymer Expansion Effects at Different Pressures

(34) Flash evaporation of the spinning material occurs, at least for the water content of the pre-heated spinning solution at boiling temperature, due to the pressure reduction during the extrusion process.

(35) It is assumed, based on the test results, that a certain segregation or separation of the homogeneous mixing phase at least at the polymer solution surface (extrudate surface) occurs as a result of the pressure relief during the spinning process caused by an expansion of the polymer. Two heterogeneous mixing phases, specifically the extrudate core formed from a homogeneous mixture of cellulose/amine oxide/water and the extrudate surface formed from an enrichment of amine oxide and water, for example in the form of crystallisation water, and/or water vapour mixed with thermal decomposition products (from amine oxide=NMM (N-methylmorpholine, M=morpholine)) are formed. This segregation may lead to the formation of a second phase in the extrudate. Due to nucleation and growth of crystal nuclei, this may lead to spinodal decomposition or the enrichment of polymer solution constituents at the boundaries of the dissolved polymer. It is in any case to be assumed that, due to this expansion process of the polymer solution jet, the fibrillary structure of the filaments formed in a fibre-like manner has already formed upon entry into the solvent-containing collecting bath (spinning bath) and the fibrils are only loosely connected via cellulose chains. A further segregation process therefore takes place in the spinning bath, since, due to the incompatibility with excess water supply, the polymer solution in the spinning bath experiences spontaneous spinodal decomposition and the looser cross-linking network of cellulose molecules formed additionally by the expansion evaporation is ripped open under the spinning bath swelling. Even with extrusion products such as filaments and staple fibres from a solution of cellulose/amine oxide/water, an increased fibrillation tendency can typically be detected on the finished, dry product, which can be attributed to the segregation and enrichment during the extrusion process.

(36) In any case, the spinning solution is heated to a temperature above the boiling point in the air gap. The throttling of the overheated spinning solution flow introduced by the spinneret and expansion causes the spontaneous evaporation of NMMO/NMM/N/water at the filament surface in the gas space.

(37) The flash evaporation observed in the spinning solution occurs since the pre-heated spinning material enters an environment of lower pressure, wherein the released quantity of solvent (mixture) implicitly functions on the one hand to cool the polymer flow exiting from the nozzle relief device. In other words, the pressure drop of the polymer flow (cellulose solution) from, for example, 20-50 bar to ambient pressure leads to an overheating of the polymer solution. The new pressure set in the shaped polymer solution spreads at high speed over the polymer material expanding in the air gap environment. At the same time, the pressure relief is accompanied by a change to the specific volume.

(38) The temperature change is slowed by material transfers, such as heat transfers, at the phase boundary, with the result that it is to be assumed that a thermodynamic equilibrium of the polymer solution or spinning solution is no longer present in the spun fibre.

(39) In thermodynamics, the direct transition of a material from the gaseous state of matter to the solid state of matter is also referred to as resublimation.

(40) No liquid state of matter exists with the pressure and temperature conditions under which resublimation occurs. These conditions are also referred to, independently of the direction of the phase conversion, as sublimation pressure and sublimation temperature, or as the sublimation point.

(41) Any substance, during the course of its resublimation, releases what is known as sublimation heat, which is equal to the sum of melting heat and evaporation heat.

(42) The pressure relief and change to the thermal economy (heat tone effects) of the spinning solution were examined experimentally as follows.

(43) To examine the heat tone effects, the spinning solution was passed through a pressure DSC equipped with sensors and liquid nitrogen cooling in a perforated crucible and was subjected to the following temperature program.

(44) Heating: 30 C. to 300 C., heating rate 10 C./min; atmosphere nitrogen, test pressure: 1, 25, 50, 100 and 150 bar.

(45) The test results at various test pressures are illustrated in FIG. 5. It can be seen from FIG. 5, carried out at a measuring pressure of 1 bar, that a process progressing endothermically occurs from approximately 58-60 C. The peak temperature of the endothermic process lies between 105 and 110 C.

(46) This endothermic effect clearly describes the fact that shifts in the crystal structure of the spinning solution occur in the range from 60 C. or evaporation processes are also introduced, which indicate heat delivery and absorption from/into the polymer solution and the released substances respectively. As a result of a further heat feed, the exothermic decomposition of the spinning material is initiated from 190 C.

(47) At the higher pressures of 25, 50, 100 and 150 bar, it can be seen that the endothermic effect of the spinning solution is supressed in the temperature range 60 to 150 C. and is shifted to higher temperatures. A reason for this behaviour can be clearly cited as the pressure with the evaporation of the components located in the spinning solution. It is also interesting that the exothermic reactions of the spinning solution introduced at higher measuring temperatures occur to a smaller extent than with the 1 bar measurement.

(48) Since the spinning process, due to the generated spinning pressure (function of the spinning solution concentration, the molecular weight (DP value, degree of polymerisation, average degree of polymerisation of the cellulose) of the mass throughput, the viscosity, the temperature, the spinneret diameter, the spinneret length), is necessarily relieved of pressure to ambient pressure upon discharge (usual pressure range of 15-100 bar), it is clear from the measured enthalpy curve that, with the relief pressure difference before and after extrusion, the polymer solution is subjected to an endothermic effect. This effect is strongest at the peak maximum at 105 C. to 110 C. In accordance with the invention, this teaching is reversed in order to operate the extrusion spinning process at lower temperatures.

Example 3

Spinning Device

(49) An NMMO spinning material consisting of a mixture of pulps of the MoDo Crown Dissolving-DP 510-550 and Sappi Saiccor DP 560-580 type was produced continuously in the following composition: cellulose 12.9%, amine oxide (NMMO-N-methylmorpholine N-oxide) 76.3%, water 10.8%.

(50) The solution was produced following aqueous enzymatic pretreatment and suspension production by evaporating off excess water under vacuum in a reaction vessel subject to continuous flow at a temperature of 97-103 C. Known stabilisers were added in order to stabilise the NMMO/water solvent. As is known, the cellulose solution was stabilised using gallic acid propyl ester in alkaline spinning material and solvent. For safety-relevant solution production, it is advantageous for the heavy metal ion content to be controlled and not to exceed a value of 10 ppm as a cumulative parameter (of metal ions and non-ferrous metal ions). A pulp having a cellulose (alpha) content of greater than 90% is preferably used for the solution production ( content determined as unsoluble fraction in 17.5% NaOH). The carbonyl group content of the used pulp was <0.1%. The carboxyl group content of the pulp likewise fluctuated in the region of <0.1%. It should be noted that the alkaline and alkaline earth ion content in the pulp is <350 ppm. The density of the produced solution was 1,200 kg/m.sup.3 at room temperature. The zero shear viscosity of the spinning material, set via the pulp mixing components, may be up to 15,000 Pas, measured at 75 C. Depending on the processing temperature selected in the spinning process, the zero shear viscosity may fluctuate in the range from 500 to 15,000 Pas. Due to the shear-thinning behaviour of the spinning solution, the viscosity at spinning shear rates falls, depending on the selected processing temperature, to a range below 100 Pas and is likewise highly dependent on the cellulose concentration in the spinning solution.

(51) An NMMO solution was used as the spinning bath necessary for the spinning process, wherein the NMMO concentration was held in the range between 18 and 23% and at a temperature from 15 to 28 C. by the addition of aqueous condensate. The metal cations and non-ferrous metal cations located in the spinning bath had a concentration of <0.25 mg/l. The alkaline and earth alkaline concentration in the spinning bath ranged from 30 to 50 mg/l.

(52) The spun spinning solution as described above was subjected to a test program in accordance with accompanying Table 1.

(53) A rectangularly drilled nozzle metal sheet (material high-grade steel) of different thickness was used as a spinneret. The spinneret openings were formed in the manner of capillary bores in the nozzle metal sheet. A geometry for the bore hole form was used with which the spinning solution runs in a conical part into the spinning hole and, after the conical part, is conducted into a cylindrical part of the bore hole before the spinning material is pressed out into the air gap with simultaneous drawing, was used as the bore hole form. The material drawn into fibrils was then dipped into the spinning bath for solidification and ultimate fibre formation.

(54) The spinneret openings were held at a temperature, as stated in example Table 1.

(55) The air gap between the spinneret openings and the spinning bath surface constitutes the spinning gas volume. The spinning gas volume is formed from the spinning field and the gas gap height associated with the spinning field.

(56) The spinning fibres passed transversely through the temperature-layered gas space (spinning volume), wherein they were passed continuously in this gas space through the spinning gas flow 1 and the spinning gas flow 2 during the spinning process. Test 8 and Test 9 were carried out without the feed of a spinning gas flow 2.

(57) The fibre formation or coagulation of the drawn cellulose solution was then performed in the spinning bath, which was attached beneath the spinneret openings.

(58) The drawn fibres exiting from the spinning bath were removed continuously by means of a discharge member.

(59) During the tests, the spinning gas exhaust gas flow was measured on the flow-off side of the spinning field for aerosol particles, wherein the particle size and concentration are illustrated in Table 1 in accordance with each test.

(60) It could surprisingly be determined that it is possible to detect a dependency of the aerosol particles released from the cellulose solution via the variation of the spinning pressure and the spinning temperature. A release of aerosol particles induced by temperature and spinning pressure could thus be determined, wherein a lower aerosol release could be determined in the spinning temperature range between 87 C. and 94 C. at a spinning pressure between 22 and 34 bar (tests 5, 6 and 7).

(61) The spinning behaviour was additionally determined visually, under consideration of the number of spinning errors, such as fibre breaks and adhesions. The spinning behaviour was classified from 1 (best) to 5 (worst), wherein the method according to the invention demonstrated the best behaviour in accordance with tests 5, 6 and 7.

(62) If the spinning solution had the same composition over all tests, but was spun at higher spinning temperatures and spinning pressures, a much higher aerosol particle concentration can be determined in the gas flow through which the spinning material is passed. Since the aerosol particles crystallised already at temperatures of 20 C., the detected particles can only be assumed to be NMMO 2,5 hydrate, NMMO 1 hydrate or pure NMMO discharged during the spinning process as a result of expansion evaporation. The aerosol particles can also be easily detected, besides the aerosol measurement by means of a measuring apparatus, by deposition on a cooled depositing plate arranged after the spinning field. Besides the crystallised amine oxide (NMMO hydrate), NMMO-typical decomposition products (which are produced during production of the spinning material), such as NMM (N-methylmorpholine), M (morpholine) and other solution-specific degradation products, can also be separated from the spinning material.

(63) TABLE-US-00001 Test 1 Test 2 Test 3 Test 4 Test 5 Test 6 Test 7 Test 8 Spinning solution temperature C. 105 107 110 109 92 87 94 112 Throughput per hole g/hole min 0.025 0.025 0.050 0.050 0.025 0.034 0.025 0.050 Diameter mm 0.100 0.100 0.100 0.100 0.070 0.080 0.070 0.070 Nozzle length mm 1.00 1.50 1.00 1.50 1.00 1.50 1.50 1.00 Spinning fibre discharge rate Titre dtex 1.40 1.42 1.41 1.39 1.43 1.38 1.40 1.43 Discharge rate m/min 27.9 27.9 55.7 55.7 27.9 38.5 27.9 55.7 spec. hole density fibres/mm.sup.2 3 3 2.5 2.5 3 3 3 2.5 Cross-sectional area of holes (fibres) 0.024 0.024 0.020 0.020 0.012 0.015 0.012 0.010 at the nozzle discharge without the swell per mm.sup.2 of nozzle area Cross-sectional area of the 0.00035 0.00036 0.00035 0.00035 0.00036 0.00035 0.00035 0.00036 filaments at the end of drawing Averaged filament cross-sectional 0.010 0.010 0.008 0.008 0.005 0.006 0.005 0.004 area per mm.sup.2 of nozzle area Volume of the filaments with full 0.589 0.589 0.491 0.491 0.289 0.377 0.289 0.241 discharge area, cylindrical Volume of the filaments with 0.239 0.239 0.199 0.199 0.118 0.154 0.118 0.099 averaged filament cross-sectional area Spinning field volume/per mm of mm.sup.3/mm 25 50 25 25 25 25 25 25 nozzle width Spinning gas volume in the spinning mm.sup.3 24.761 49.761 24.801 24.801 24.882 24.846 24.882 24.901 field = spinning field volume minus volume of filaments with averaged discharge area Ratio of spinning field total factor 104.809 209.581 125.451 125.477 211.096 162.689 211.208 252.048 volume/averaged fibre volume Fibre volume in % of spinning field % 0.954 0.477 0.797 0.797 0.474 0.615 0.473 0.397 total volume Number of spinning fields in the gas 20,000 20,000 20,000 20,000 20,000 20,000 20,000 20,000 flow direction spec. spinning gas flow 1 feed over liters/h 150 250 275 280 60 60 60 250 number of spinning fields per mm of spinneret length spec. spinning gas flow 2 feed over liters/h 125 50 25 30 100 100 100 0 number of spinning fields per mm of spinneret length spec. spinning gas treatment flow 1 liters/h 7.5 12.5 13.8 14.0 3.0 3.0 3.0 12.5 per spinning field spec. spinning gas treatment flow 2 liters/h 6.25 2.50 1.25 1.50 5.00 5.00 5.00 per spinning field Measured particle concentration in g/m.sup.3 2.80E+04 3.20E+04 3.35E+04 3.05E+04 2.98E+04 3.20E+04 3.47E+04 3.38E+04 the spinning exhaust gas flow Spinning gas flow feed per mm.sup.3 liters/h 0.55 0.30 0.60 0.62 0.32 0.32 0.32 0.50 of spinning field volume per mm.sup.3 of spinning field conc. = 15 10 20 19 10 10 11 17 removal in g/h per mm.sup.3 of spinning field Number of air changes in the 5.50E+05 3.00E+05 6.00E+05 6.20E+05 3.20E+05 3.20E+05 3.20E+05 5.00E+05 spinning field Spinning behaviour 2 2 2-3 2-3 1-2 1-2 1-2 2-3 Test 9 Test 10 Test 11 Test 12 Test 13 Spinning solution temperature C. 114 117 119 121 124 Throughput per hole g/hole min 0.050 0.025 0.025 0.050 0.050 Diameter mm 0.070 0.050 0.050 0.050 0.050 Nozzle length mm 1.50 1.00 1.50 1.00 1.50 Spinning fibre discharge rate Titre dtex 1.42 1.40 1.41 1.44 1.42 Discharge rate m/min 55.7 27.9 27.9 55.7 55.7 spec. hole density fibres/mm.sup.2 2.5 3 3 2.5 2.5 Cross-sectional area of holes (fibres) 0.010 0.006 0.006 0.005 0.005 at the nozzle discharge without the swell per mm.sup.2 of nozzle area Cross-sectional area of the 0.00036 0.00035 0.00035 0.00036 0.00036 filaments at the end of drawing Averaged filament cross-sectional 0.004 0.002 0.002 0.002 0.002 area per mm.sup.2 of nozzle area Volume of the filaments with full 0.241 0.147 0.147 0.123 0.123 discharge area, cylindrical Volume of the filaments with 0.099 0.062 0.062 0.052 0.052 averaged filament cross-sectional area Spinning field volume/per mm of mm.sup.3/mm 25 25 25 25 25 nozzle width Spinning gas volume in the spinning mm.sup.3 24.901 24.938 24.938 24.943 24.948 field = spinning field volume minus volume of filaments with averaged discharge area Ratio of spinning field total factor 252.101 404.401 404.265 479.976 480.360 volume/averaged fibre volume Fibre volume in % of spinning field % 0.397 0.247 0.247 0.208 0.208 total volume Number of spinning fields in the gas 20,000 20,000 20,000 20,000 20,000 flow direction spec. spinning gas flow 1 feed over liters/h 275 250 250 275 350 number of spinning fields per mm of spinneret length spec. spinning gas flow 2 feed over liters/h 0 25 25 75 75 number of spinning fields per mm of spinneret length spec. spinning gas treatment flow 1 liters/h 13.8 12.5 12.5 13.8 17.5 per spinning field spec. spinning gas treatment flow 2 liters/h 1.25 1.25 3.75 3.75 per spinning field Measured particle concentration in g/m.sup.3 3.86E+04 3.65E+04 4.50E+04 4.18E+04 4.95E+04 the spinning exhaust gas flow Spinning gas flow feed per mm.sup.3 liters/h 0.55 0.55 0.55 0.70 0.85 of spinning field volume per mm.sup.3 of spinning field conc. = 21 20 25 29 42 removal in g/h per mm.sup.3 of spinning field Number of air changes in the 5.50E+05 5.50E+05 5.50E+05 7.00E+05 8.50E+05 spinning field Spinning behaviour 2-3 3-4 3-4 4 4