KR840000656B1 - The manufacture of condensing of filamentary fiber - Google Patents

Abstract

Filament fiber fluxes are prepd. from a thermoplastic synthetic polymer melt using extrusion from a number of yarning orificies in small spacing. Melt, extruded through the small spacing, is cooled by a cooling medium and converted to a number of separate fibrous fine streams. Convex part is installed discretely between the two adjacent narrow spaces, and the melt extruded from two orificies contacts itself through the concave part. Suitable polymere are polycarbonate having a very high melting viscosity, polyester, polyurethane or polyolefin elastomer.

Description

Manufacturing method of filamentary fiber aggregate

1 is a scanning electron micrograph of a cross section of an arbitrary portion of the filamentary fiber concentrator obtained in the first embodiment of the present invention.

Figure 2a is an enlarged cross-sectional view of the plain weave mesh lock used in the second radiation embodiment of the present invention.

FIG. 2b is an enlarged top view of the plain weave mesh lock shown in FIG.

FIG. 2C is an enlarged view showing the “island-sea” structure of the spinneret in which the polymer melt from the plain weave gilt is adjacent to an adjacent portion and a portion of the plain weave gilt is forming an island.

FIG. 3A is a scanning electron micrograph of a cross section of an arbitrary portion of the filamentary fiber aggregate obtained in Example 2 of the present invention. FIG.

3B is a scanning electron micrograph of a cross section of an arbitrary portion of the filamentary fiber concentrator obtained in Example 3 of the present invention.

4 is a scanning electron micrograph of a cross section of any part of the filamentary fiber aggregate obtained in Example 5 corresponding to the fourth radiation embodiment of the present invention.

FIG. 5 is a scanning electron micrograph of a cross section of an arbitrary portion of the filamentary fiber aggregate obtained in Example 6 of the present invention. FIG.

Figure 6 is an illustration of a sawtooth stacking device used in the sixth radiation aspect of the present invention.

FIG. 7 is a scanning electron micrograph of the cross section at any part of the filamentary fiber concentrator obtained in Example 7. FIG.

8 is a perspective view showing an outline of the implementation of the molding apparatus in the case of manufacturing the filamentary fiber aggregate of the present invention.

9 is an enlarged view of a cross section of the molding region for geometrically explaining the main points of the fiber forming region of the present invention.

FIG. 10 is a graph showing the cross-sectional area variation at intervals of 1 mm in the fiber axis direction for one fiber selected arbitrarily from among non-drawn yarns of the filamentary fiber aggregate obtained in Example 3. FIG.

FIG. 11 is a graph showing the cross-sectional area variation in every 1 mm interval in the fiber axis direction for one fiber selected arbitrarily from among the drawn yarns of the filamentary fiber aggregate obtained by stretching the filamentary fiber aggregate mentioned in FIG. .

12A is an optical micrograph of a cross section at intervals of 1 mm in the fiber axis direction for one fiber selected arbitrarily from among the filamentary fiber bundles obtained in Example 2. FIG.

12B is an optical micrograph of a cross section at intervals of 1 mm in the fiber axis direction for one fiber arbitrarily selected from among the filamentary fiber concentrators obtained in Example 10. FIG.

13 is an exemplary view illustrating a method of measuring the fiber cross-sectional release coefficient defined in the text.

FIG. 14 is an optical micrograph showing a crimped state in 4 mm unstretched yarns continuously by selecting any one from three kinds of filamentary fiber aggregates obtained in Examples 10, 3 and 14. FIG.

Figure 15 is an enlarged photograph of the crimped state of the unstretched yarn of the filamentary fiber aggregate obtained in Example 10.

FIG. 16 is an enlarged photograph showing the crimped state after non-aqueous treatment of the filamentary fiber aggregate obtained in Example 13. FIG.

FIG. 17 is an enlarged photograph showing the crimped state that appears when the filamentary fiber aggregate after the stretching treatment obtained in Example 10 is subjected to non-aqueous treatment. FIG.

18A and 18B are both scanning electron micrographs taken at 45 degrees with respect to the fiber axis of the right angled cross section of the filamentary fiber concentrator obtained in Example 28. FIG.

19 is a wide-angle X-ray diffraction diagram of the filamentary fiber concentrator obtained in Example 3. FIG.

20 is a picture taken in a state in which the radial tension is applied to the filamentary fiber bundle obtained in Example 3 of the present invention.

FIG. 21 is a scanning electron micrograph of the cross section at any part of the filamentous fiber concentrator obtained in Example 30.

FIG. 22 is an optical microscope photograph of a cross section of a beard filamentous fiber aggregate obtained in Example 31. FIG.

The present invention relates to a method for producing a novel filamentary fiber bundle formed from a thermoplastic synthetic polymer.

In summary, the novel filamentary fiber of the present invention, the filamentary fiber (filament) has a change in the cross-sectional area size at irregular intervals along its longitudinal direction, the cross-sectional area variation coefficient in the filament [CV (F )] Is in the range of 0.08 to 1.0. CV (F) means that when the filament is cut in the longitudinal direction, for example, at 1 mm intervals, the size of each cross-section is randomly varied, and an irregular period is caused by the variation of the cross-sectional size. It also means that the variation is in a statistically constant range. When the new filamentary fiber (filament) is described in detail, the cross section is non-circular, and has a change in the cross-sectional area at irregular intervals along the length direction of the filament, and accompanied by a change in the cross-sectional area. .

According to the filamentary fiber assembly of the present invention, when the filamentary fibers have the above characteristics and the cutting body is cut in a direction perpendicular to the fiber axis, the cross-sectional size of each filament is substantially randomly different. It features.

According to the present invention, it has been found that the novel filamentary fiber aggregate having the above-described features can be produced using a spinning method that is completely different from the conventional known methods.

Conventionally, a number of methods for producing fibrous materials from thermoplastic polymers are known. However, from the principle of manufacture, they can be separated into orifice molding type and phase separation molding type described later. The former is a method of discharging a polymer from a uniform and regular tubular hole (i.e., an orifice) provided at regular intervals in a spinneret, cooling and solidifying it while drafting to obtain a fibrous material. According to the orifice geometry, uniform and constant fibers are obtained.

On the other hand, the latter phase-separated molding type is described, for example, in US Pat. Nos. 3,954,928, 3,227,664, and J. Venter, "Industrial and Engineering Chemistry 48, No. 8, page 1342 (1956)". Explosive force of an inert gas mixed and dispersed in a molten polymer, a melt or solution of a polymer from a circular nozzle or a slit-like nozzle by a jet or flash of high temperature or a phase separation method. This is a method of obtaining fibrous water with phase separation so that a fine aggregate phase is formed. According to this method, a large amount of nonwoven fabric aggregates are obtained, but the fibers forming the fiber aggregate have cross-sectional shapes and large size, respectively. There is a feature in that they are different and not uniform.

All of these prior art manufactures of the fibrous material are carried out industrially and serve as a market to provide the fibrous material in large quantities to the market. However, when viewed from the aptitude and fish properties of the fibrous material, they have the following problems. In addition, if these problems are improved, it is possible not only to provide a superior new type of fiber material, but also to provide a fiber material at a lower cost.

That is, in the case of the former orifice molding type, the first problem is that if a plurality of orifices are provided in one spinneret for the purpose of forming a large amount of high-density fiber concentrators and the orifice spacing is narrowed, melting affects the orifice discharge. Due to the barus effect and melt facture of the polymer, problems such as filamentary polymer melt discharged from the orifice are fused and cut together, so an accident occurs between the orifices. Industrially, it can only be narrowed down to about 2-3 mm at most. At this interval, the number of fibers formed from the detention is only about 10 to 20 minutes per 1 cm ² , and it is impossible to form a large amount of the high-density fiber bundle. In other words, in this technique, in order to increase productivity, the molding speed is inevitably increased, usually about 1000 m / min.

The second problem of the orifice forming type is that it becomes a constant monotonous shape since the geometry of the fiber depends on the orifice shape. This is not particularly suitable when used as a material for textile products such as woven fabrics and knitwear.

It is well known that the physical properties of a fiber product depend not only on the properties of the matrix polymer of the fibers constituting it, but also on the geometry of the fiber, ie, the cross-sectional shape or size. For example, the substrate of a product made of natural fibers largely depends on the cross-sectional shape and the irregularities of denier, but it is very difficult to obtain such irregularities from the thermogas polymer by orifice molding. In addition, it is very difficult to directly mold the ultra fine denier fiber which is important for the characteristics of artificial leather and suede, and it is possible to form a composite fiber by using a conventional heteropolymer to dissolve and remove one side or both. It is carried out by the method of splitting the fiber of a polymer, etc., and of course these are expensive fibers because a process is complicated.

On the other hand, in the case of the latter phase-separated molding type, if the method of molding with a slit-shaped nozzle is taken, it is possible to mold the fiber bundle in a larger amount than the former, but in this case, only a two-dimensional bundle is obtained. As for the geometrical shape of the fibers, the fiber cross sections of the fiber aggregates obtained by this technique are heterogeneous without exception, and although the deniers are different, the shape and size of the cross sections and the irregularities of the deniers of the fibers are very large. It is very difficult to adjust, and since the average denier is also difficult to control, its application range is limited by itself. In addition, the fiber connectors obtained by such a phase-separation type method are all remarkable mesh-like fiber assemblies or branched short-fiber aggregates, and the fiber length between the gathering points of the meshes or branches is, for example, several millimeters to It is a few centimeters long and has an extremely short flaw. Therefore, the fiber assembly having a function as an aggregate of a plurality of filaments of at least 30 cm, preferably at least 50 cm or more, on the average of the distances between the junction points of the fibers, is a method of producing the above-described phase separation type fiber assembly. It is impossible to manufacture by.

It is an object and an advantage of the present invention to provide a method for producing a novel fiber bundle.

It is an object and advantage of the present invention to provide a novel manufacturing method (spinning method) capable of spinning filamentous fibers of 100 to 600 or more yarns per 1 cm ² of fiber discharge surface of spinnerets, for example. .

Objects and advantages of the present invention are, for example, thermoplastic polymers having a very high melt viscosity, such as polycarbonate, or thermoplastic polymers exhibiting complex viscoelastic behavior such as, for example, polyester elastomers, polyurethane elastomers, and polyolefin elastomers. It is to provide a method for producing these fiber aggregates easily and inexpensively using thermoplastic polymers that have been industrially considered difficult or virtually impossible to produce.

Still other objects of the present invention will become apparent from the following description.

Hereinafter, the manufacturing method of the filamentary fiber aggregate of this invention is demonstrated in more detail based on this invention.

As a typical example, the filamentary fiber concentrator of the present invention has a plurality of narrowly spaced discharge sides for extruding a melt of a thermoplastic synthetic polymer, and a non-continuous convex (acid) is provided between adjacent narrow spaces. It can be produced using a spinneret characterized in that it has a structure capable of coming and going with each other and the molten liquid extruded at a narrow interval through the narrow gap or recesses (valley) present between the iron portions.

In more detail, the manufacturing method of the present invention, in the extrusion of the melt of the thermoplastic synthetic polymer from the spinneret having a plurality of narrow intervals to produce a filamentary fiber focus, the narrow adjacent to the melt discharge side of the spinneret Between the gaps there is a discontinuous convexity, and the melt, which is extruded from any narrow gap through narrow gaps or recesses existing between the convex (acids), is extruded from another narrow gap adjacent thereto And extruding the molten liquid from the spinneret which is allowed to travel to and from each other.At this time, by supplying a cooling fluid to the molten liquid discharge surface of the spinneret and its vicinity, the molten liquid extruded through the narrow gap is extracted and a plurality of separated Characterized by converting into a fibrous trickle It is a manufacturing method of a filamentary fiber aggregate.

As described above, in the method of the present invention, the spinning surface of the melt of the conventionally known polymer is a smooth surface, and the ejection holes (orifices) of the molten liquid are independently laid in a regular and correct arrangement. It is fundamentally different from the manufacturing method of the fibers which extrude the melt from the mold.

The present inventors plan to develop a method for producing fibers that spin a plurality of fibers (filaments) per unit area (e.g., 1 cm ² ) of spinnerets, with a higher density than that of conventional spinnerets. An orifice was laid down and the extrusion of the melt of a thermoplastic polymer was attempted from these orifices. As one of these attempts, the inventors melted using spinnerets (1000 orifice totals) that laid out orifices with a hole diameter of 0.5 mm at equal intervals at a rate of 10 vertically and 100 horizontally at a pitch interval of 1 mm. Polymers For example, filamentary polymers extruded through the orifices as a result of discharging a melt of crystalline polypropylene from the orifices are fused to each other under normal spinning conditions due to the Barus effect or bending phenomenon to produce fibers. Was not possible.

Thus, the present inventors attempted to solidify the fiber by discharging the melt aggregate discharged from each orifice by quenching the fiber discharge surface of the spinneret and the lower portion thereof in the above-described method, so that the orifice discharge surface is supercooled, resulting in melt fracture phenomenon. Many of these occurred, and the filaments were cut at a large number of orifices, making it impossible to continuously perform a stable spinning operation.

Thus, the present inventors make grooves having a V-shaped cross section (about 0.7 mm in width and about 0.7 mm in depth) on the polymer discharge surface of the spinneret such that they are at an angle of about 45 ° and about 135 ° with respect to the arrangement of the orifices. As a result of extruding the melt of the polymer using spinnerets having convex portions (mountains) and recesses (valleys) between the orifices (narrow spaces) of the discharge surface thus obtained and intersected, they were initially discharged. Although it flows out as if it covers the whole, in this case, the melt of the polymer was drawn out while blowing air appropriately by quenching the polymer discharge surface of the spinneret and its vicinity, and the molten liquid was gradually divided so that the iron part of the spinneret gradually became an island shape. It appeared on the surface of a melt as island, and many filamentous fibers were stabilized and drawn out continuously (the above spinning aspect is called 1st spinning aspect of this invention below).

The detailed conditions of the first radiation embodiment are described in Example 1 described later. In addition, a cross-sectional photograph of part of the filamentary fiber bundle thus obtained is shown in FIG. 1 (this will be described later).

As a result of the high density spinning of the fiber according to the first spinning aspect, the present inventors attempted to spin the polymer melt using a plain weave mesh shown in FIG. 2 as described in Example 2 below. . That is, about 31% of porosity made of stainless steel wire having a diameter of about 0.21mm, the number of narrow gaps per 1cm ² is about 590, 2cm wide and 16cm long (32cm ² area). As a result of extruding the same polymer melt as in Example 1 from the gold screen, as shown in Example 1, the polymer melt first flowed out as if covering the entire gold screen. When appropriately cooled by an air stream, the melt is gradually divided, and the iron portions indicated by M in FIGS. 2a and 2b of the gold mesh appear as islands of the same shape as the diagonal section in FIG. 2c. By converting and solidifying into a plurality of separate fibrous trickle, a plurality of filamentous fibers can be stably drawn out continuously. This spinning aspect is hereinafter referred to as the second spinning aspect of the present invention.

A partial cross section of the fiber bundle obtained in the above embodiment is shown in FIG. 3A. Further, the gold mesh may be of any woven structure. For example, if the gold mesh of the twill tissue shown in Example 3 described later is used to radiate in the same manner as in Example 2, the special mesh as shown in FIG. A filamentary fiber bundle having a cross-sectional shape is obtained.

The present inventors, having a diameter of about 0.38mm in a stainless steel ball of curvature about 46%, 1cm ² each made of a steel wire narrow gap can hanging one narrow gap with respect to the plain weave geummang about 96 protrudes, as shown in Example 4 described later When the polymer melt was extruded using a spinneret with a pin protruding to a height of about 2 mm (width: about 30 mm, length: about 50 mm), the melt initially covered the front surface of the plurality of fins in the gold wire. In the case of drawing out by blowing air to cool the polymer discharging surface and its vicinity, the melt was first drawn out by the trickle at the tip of the fin, but after a while, the melt was drawn out by the divided trickle at the recess below the fin. After cooling, a plurality of filamentary fiber bundles are stably and continuously formed.

In such a case, the polymer melt is divided into islands with multiple fins in the sea, and the melt of the polymer is divided in the narrow zone where the island and the island are approaching, so that the melt is divided into numerous fibrous forms directly from the sea. Withdrawn. It was surprising to be able to form a large number of split filamentous fibers continuously in this form directly from the sea. Said aspect is called 3rd radiation aspect of this invention.

The inventors again attempted high density spinning of the polymer melt using a variety of different spinnerets. Details of these different radiation embodiments are described in the Examples below, which are representative of the following.

Fourth Radiation Embodiment

A plurality of micro metal spheres are densely packed and arranged in at least the surface layer, and the polymer molten liquid is extruded through a narrow gap of the porous plate-shaped body by using a porous plate-shaped body which is sintered and fixed. A method of producing a filamentary fiber aggregate of (see Example 5 to be described later). A partial cross section of the filamentary fiber bundle obtained in this method is shown in FIG.

[Fifth Radiation Embodiment]

As shown in Example 6 to be described later, for example, a densely arranged and stacked horizontal plain gold network having a diameter of about 0.2 mm and a porosity of about 30% is used as a spinneret, and is parallel to the lamination surface of the gold network. A method for producing a plurality of filamentous fiber aggregates by extruding a polymer melt. In this case, the transverse wires forming the gold mesh form protrusions (mountains) between the narrow gaps in the same manner as the plurality of fins in the above-described third radiation embodiment.

A partial cross section of the filamentary fiber bundle formed by this method is shown in FIG.

[Sixth Radiation Embodiment]

)인 다수의 금속판을 제6도에 나타낸 바와 같이 각각 일정한 미소 간격을 두고 가로로 적층한 것을 방사구금으로 사용하여 당해 톱니모양부를 토출측으로 하여 다수의 판면과 평행하게 중합체 용융액을 압출하여 다수의 필라멘트상 섬유집합체를 제조하는 방법.As shown in Example 7 described later, the distal end portion is sawtooth shaped (

As shown in FIG. 6, a plurality of metal plates, each of which are horizontally laminated at regular intervals as shown in FIG. 6, are used as spinnerets, and the toothed portion is discharged to extrude the polymer melt in parallel with the plurality of plate surfaces to form a plurality of filaments. A method of making a phase fiber assembly.

A partial cross section of the filamentary fiber aggregate obtained in this method is shown in FIG.

As shown in the above first to sixth aspects, according to the present invention, in manufacturing a filamentary fiber bundle by extruding a melt of a thermoplastic synthetic polymer from a plurality of narrowly spaced spinnerets, The discontinuous convex portions are provided between the narrow gaps adjacent to the melt discharge side, and the melt liquid extruded from a narrow gap through the narrow gaps or recesses existing between the convex portions (mountains) is adjacent to the other. The melt is extruded from the spinneret which is allowed to come and go with the melt extruded from the narrow gap. At this time, the melt is extruded through the narrow gap while cooling by supplying a cooling fluid to the discharge surface and the vicinity of the melt of the spinneret. Withdrawal of the molten liquid and turning the molten liquid into a plurality of separated fibrous trickles By ring and solidification, the filamentary fiber bundle of the number of bones per unit area of the spinneret can be produced.

Further, according to the present invention, for example, the above-mentioned third radiation aspect (a large number of needles are used as convex parts), the fifth radiation aspect (a gold wire is used as convex parts), and sixth radiation As is apparent from the spinning method such as the embodiment (using the sawtooth as the convex portion), according to the present invention, the melt of the spinneret is produced by extruding the melt of the thermoplastic synthetic polymer from the spinneret to produce a filamentary fiber aggregate. On the discharge side, the molten liquid forms a continuous phase (sea), and a plurality of isolated pieces in the continuous phase (sea) of the molten liquid are formed by a plurality of projections protruding the continuous phase (sea) of the melt on the discharge side. It forms a non-continuous non-polymeric phase (island), and the molten liquid from the continuous phase (sea) is cooled by supplying cooling fluid to the molten liquid discharge surface of the spinneret and its vicinity, and a plurality of types of fibrous trickle ( ) To write because the withdrawal and solidified can be made the filamentous fiber bundling body continuously.

According to the present invention, for example, if the average fineness per 1 cm ^{2 of} spinnerets is a thick denier such as about 30 to 100 denier, and if it is about 50 to 150 bones, and the average fineness is about 1 to 5 denier, it is about 100 Filamentary fiber aggregates of 600 to 1500 or more or more water can be continuously produced as long as 600 to 1, and an average fineness of about 1 denier or less.

According to the conventional melt spinning method, it was impossible to continuously and stably spin more than 30, especially more than 50, filamentary fiber bundles per 1 cm 2 of fiber forming area of the spinneret. You can not say that.

Further, according to the present invention, filamentary fiber bundles having various average fineness ranging from ultrafine fibers having an average fineness of 0.01 denier, preferably 0.05 denier to tadenier of 300 denier can be produced.

According to the manufacturing method of the present invention, furthermore, in order to uniformly and efficiently cool the polymer melt discharged from a narrow gap as a fiber forming region of the spinneret, that is, a region where the fibers are substantially formed, an object, in particular a rectangle, It is preferable to set it as the fiber forming region of. It is preferable that such a rectangle has a width of about 6 cm or less, particularly about 5 cm or less, and the length may be any length, and the air flow is discharged from the narrow gap between slits on the slits substantially parallel to the longitudinal direction. It is preferable to cool the molten liquid of the polymer to be blown toward the surface to allow the air flow to flow substantially parallel to the discharge surface in the vicinity of the discharge surface.

Such a cooling fluid uses, for example, air at room temperature as the air flow, and at this speed as the speed immediately after passing the fiber concentrator at a position 5 mm away from the discharge surface (end face of the mountain) of the spinneret. It is advantageous to determine the flow rate so that is about 4 to 40 m / sec, preferably about 6 to 30 m / sec.

According to the present invention, as the rectangular fiber forming region, for example, a filamentous phase of, for example, 3,000 to 120,000 denier, preferably 5,000 to 100,000 denier, for example, an area of ² cm in width and 10 cm in length (total area 20 cm ² ). A fiber bundle can be produced, and a filamentary fiber bundle can be produced continuously at once, while increasing the width, particularly the length, of the rectangle. In fact, the length of the rectangle constituting the fiber forming region may be any length as long as there is no inconvenience in practical operation, and may be, for example, 2 m or 3 m or more.

The total discharging amount per 1 cm 2 of the fiber forming area is preferably 0.1 to 10 g / min and 0.2 to 7 g / min.

The polymer may be any thermoplastic synthetic polymer capable of forming a fiber, but in particular, when the melting point is expressed in absolute temperature (° K), the melt viscosity of the melt at 200 times the temperature (° K) of the melting point is 200. It is advantageously used to have from 30,000 poises, preferably from 300 to 25,000 poises, particularly preferably from 500 to 15,000 poises (wherein the melt viscosity of the polymer is defined as Tm (° K) The viscosity at a temperature (° K) corresponding to x 1.1 is stated, except that the method of measuring this viscosity is based on the flow test method according to ASTM D-1238-52T).

On the other hand, the polymer is preferably in the range of 70 ° C to 350 ° C, particularly 90 to 300 ° C, but is not limited to this temperature method.

The discharge point polymer temperature (T ₀ ) when the polymer melt is discharged from the narrow gap on the discharge side of the spinneret is calculated by the following equation (1).

T ₀ (° K) = (5 _t-2 −2 _t-5 ) 1/3 + 273... … (One)

Provided that t-2 is the actual measurement temperature (° C.) of the molten polymer at the inner position of the 2 mm spinneret from the distal end face of the spinneret.

t-5 is an actual measurement temperature (degreeC) of a molten polymer in the inner position of 5 mm spinneret from the above-mentioned convex front end surface.

In the present invention, the ratio (T ₀ / T _m ) between the discharge point polymer temperature (T ₀ ) and the melting point (Tm; expressed in degrees K-absolute temperature) of the polymer calculated from Equation (1) is 0.85 to 1.25, In particular, it is preferable to discharge the melt of the polymer from the narrow gap of the spinneret so that it is 0.9 to 1.2, most preferably 0.95 to 1.15.

The withdrawal rate (V _L ) in the spinneret of the formed fiber bundle is most preferably 100 to 10,000 cm / min, in particular 300 to 7,000 cm / min, among which 500 to 5,000 cm / min.

The apparent draft ratio D _a of the polymer melt discharged from the spinneret can be represented by the following formula (2).

D _a = V _L / V _O ... … (2)

In the above formula

V _L is the actual withdrawal speed of the fiber bundle (cm / min),

V _O is the average linear velocity (cm / min) in the discharge direction when the polymer melt is discharged while covering the entire discharge surface of the fiber forming region of the spinneret.

On the other hand, the following formula (3) holds about _VO approximately.

V _O = W / S _O ... … (3)

However, W is the discharge amount (g / min) of the entire melt when the polymer melt is discharged while covering the entire discharge surface of the fibrous region of the spinneret,

S _O is the total area of the discharge surface (cm ² ) of the fibrous region,

ρ is the density (g / cm ³ ) of the polymer at room temperature.

Thus, it can be calculated by the following formula (4) the apparent drive soft ratio (D _a) of the polymer melt is injected through the spinneret.

In the present invention, it is most suitable to control the apparent draft ratio D _a obtained from the above formula (4) to 10 to 10,000, particularly 100 to 5,000, more preferably 200 to 4,000.

The reciprocal of the apparent drive soft ratio (D _a) of the above shows the packing fraction (P _f).

P _f = 1 / D _a . … (5)

This packing fraction P _f represents the total of the total fiber cross-sectional area of the fiber concentrator formed per fiber forming area of the spinneret, and is a measure of the density of the fiber spun (ejected) from the fiber forming area, that is, the high density radioactivity. Becomes

In this regard, in the case of conventional polymer melt spinning, the packing fraction P _f is only about 10 ⁻⁵ , but in the case of the present invention P _f is 10 ⁻⁴ to 10 ⁻¹ , preferably 2 ×. It is on the order of 10 ^-4 to 10 ^-2 , and from this point of view, it is clear that the method of the present invention is greatly different from the conventional polymer melting method.

The total denier (ΣD) of the fiber assembly of the fiber assembly produced from the fiber forming region of the spinneret according to the present invention can be obtained by the following formula (6).

Σ De = (W / V _L ) x 9 x 165. … (6)

In the above formula,

V _L and W are the same as defined in the formulas (2) and (3).

_e라 하면, 하기식(7)에서 구할 수 있다.The total number of fibers (N) of the fiber assembly measures any partial average fineness (average denier) of the cluster, and this value is measured.

_{If it is e} , it can obtain | require from following formula (7).

_e……(7)N = ΣD _e /

_e … … (7)

In addition, the number of fibers (n) per unit area (cm ² ) of the spinneret can be obtained by the following equation (8).

=N/S_O……(8)

= N / S _O ... … (8)

However, the definition of S _O is the same as in the case of the equation (7) of the definition of the same in the case of the above formula (3), N.

는 0.2n(m) 내지 0.98n(m)이 된다.In this regard, according to the present invention, when the number of meshes per 1 cm ² of the plain weave mesh described in the second radiation mode (this number is expressed as the product of the horizontal and vertical strong bows per 1 cm ² ) is n (m),

Is 0.2n (m) to 0.98n (m).

Similarly, in the case of twill gold mesh, n is usually about 0.2n (m) to 0.9n (m).

As described above, according to the present invention, n can be variously changed in the range of 0.2n (m) to 0.98n (m) by adjusting the type or spinning condition of the polymer by using a gold mesh of various types of tissue. Thus, the size and / or shape of each fiber cross section can be changed.

In the first radiation aspect of the present invention, n is (0.7 to 0.95) n (m) when the number of orifices per cm ² is n (m).

In addition, in the third to sixth embodiments of the present invention, when the number of convex portions (acids) per 1 cm ² is n (m),

n ranges from 0.3 n (m) to almost n (m) and the same number.

In the method of the present invention, the polymer melt is extruded through a narrow gap provided on the discharge side of the spinneret, converted to a plurality of separate fibrous trickles, and solidified, i.e., the fiber diameter of which the trickle is constant from the convex surface. When the distance until reaching a diameter of 1.1 times is L _f (hereinafter referred to as coagulation field), L _f is about 10 to 100 cm in the case of the conventional melt spinning method, but less than 2 cm in the present invention. , Very advantageously less than 1 cm.

This L _f is, for example, in the step of stably producing the filamentary fiber bundle according to the present invention, dry carbonic acid gas cooled to a part of the surface of the fiber forming region of the spinneret, for example, below freezing point. It can be measured by blowing a cooling fluid such as an air stream, freezing and solidifying the fibrous stream of the polymer melt discharged from a narrow gap as it is, leaving it from the spinneret and irradiating it under microscope.

In the present invention, it is preferable that the coagulation coefficient K defined by the following formula (9) is in the range of 10 to 500, particularly 30 to 300, and most advantageously 50 to 200.

_L……(9)K = L _f / √

_L … … (9)

In the above formula,

_L는고화가 종료된 미연신 필라멘트의 평균 단면적이며,

_{L is} the average cross-sectional area of the unstretched filament at the end _of solidification,

L _f represents the coagulation field.

_L은 하기식(10)에서 산출될 수 있다.Also, the above

_L may be calculated by the following equation (10).

In the above formula,

e의 정의는 섬유집속체의 임의의 일부를 실측하여 구한 당해 섬유의 평균섬도(데니어)이며,

The definition of e is the average fineness (denier) of the fiber obtained by measuring any part of the fiber bundle,

ρ is the density of the polymer (g / cm ³ ) at room temperature.

Conventionally, while the known coagulation field coefficient K is in the range of about 10 ⁴ to 10 ⁵ , in the case of the present invention, the coagulation field coefficient K is 500 or less, particularly 300, as described above. In view of the present invention, it is apparent that the polymer melt is solidified in an extremely short period, and it will be understood that it is very different from the conventional melt spinning method.

In this invention, as a tension (g / denier) at the time of taking out a filamentary fiber concentrator, the range of 0.001-0.2, normally 0.02-0.1 / denier is suitable.

)와 방사구금의 용융액 토출측의 좁은 간격수 또는 철부수[n(m)]의 관계등으로부터 명백한 바와 같이, 본 발명의 방사방법에 있어서는, 당해 좁은 간격 또는 다른 바다부의 용융액과 연락될 수 있도록 되어 있으며, 이와 같은 좁은 간격 또는 바다부로부터 당해 용융액이 섬유상 세류로 분할되면서 인출되므로 어떤 일부의 좁은 간격 또는 바다부에서 인출되는 섬유상 세류가 절단되면, 인접하는 다른 좁은 간격 또는 바다부에서 인출되는 섬유상 세류와 바로 합류하여 신속하게 섬유화되고, 더구나 합류된 세류는 재차 분류하여 분리된 필라멘트상 섬유를 형성한다. 이와같은 용융액의 세류간의 상호간의 협조에 의하여 전체적으로 본 경우에 섬유형성 영역에서 연속적으로 매우 다수의 필라멘트상 섬유를 다발모양(束狀)으로 제조할 수 있다.According to the present invention, the first to the sixth spinning aspect, moreover, the number of fibers per unit area of the spinneret (

In the spinning method of the present invention, it is possible to be in contact with the molten liquid of the narrow gap or other sea portions, as is apparent from the relationship between the narrow gap number or the convex number [n (m)] on the melt discharge side of the spinneret. The molten liquid is drawn out from such a narrow gap or sea part into fibrous trickles so that when some of the narrow gap or fibrous trickle is drawn from the sea part, the fibrous trickle is drawn from another adjacent narrow gap or sea part. And immediately fibrous, and the joined trickle again sorts to form a separate filamentous fiber. By mutual cooperation between such trickles of the melt, a very large number of filamentary fibers can be continuously bundled in the fiber-forming region as a whole in this case.

In the present invention, as described above, the discharge side has a plurality of narrow gaps for extruding the molten liquid of the thermoplastic synthetic polymer, and a non-continuous iron portion is provided between adjacent narrow gaps, and the recess area existing between the iron portions is formed. The filamentary fiber bundle can be formed by using a spinneret having a structure such that the melt extruded from a narrow gap therebetween can communicate with the melt extruded at another narrow gap adjacent thereto. .

The above-described method of the present invention may also be referred to as a melt (polymer melt) forming method using a mold having a fine concavo-convex surface, in consideration of other aspects, and stably forming fine molten concavo-convex on the surface of the melt to allow fusion between the molten iron parts. While suppressing, it is going to preform a fiber mainly from a molten iron convex part.

Therefore, as a molding apparatus of the fiber bundle of the present invention

A) using spinnerets having fine uneven melt surface formation capacity;

B) having a quenching device for the surface of the detention for showing a fine uneven melt surface,

C) It is important to have a device for styling at the convex portions of the uneven melt surface.

)가 0.03 내지 4mm의 범위에 있는 것이 적합하다.As a molding apparatus of the fiber assembly of the present invention, it is a spinneret having the above-described structure, and the melt of the polymer is formed on the surface of the molding region by the average distance between the discharge sections (

) Is suitably in the range of 0.03 to 4 mm.

In particular, according to the definition described below the molding region

)가 0.03 내지 4mm의 범위,(1) Average discharge section distance (

) Ranges from 0.03 to 4 mm,

)가 0.01 내지 3.0mm의 범위,(2) average mountain height (

) Ranges from 0.01 to 3.0 mm,

)이 0.02 내지 1.5mm의 범위,(3) average mountain width (

) Ranges from 0.02 to 1.5 mm,

)와 평균산 폭(

)이 (

)/(

)로 표시하여 0.3 내지 5.0인 범위를 만족시키는 미세요철 및 다수의 중합체 토출구를 갖는 토출면을 가지며, 당해 토출면의 표면을 냉각하기 위한 냉각장치 및 형성된 섬유집속체를 인출하기 위한 인출장치를 갖는 것을 특징으로 하는 성형장치를 사용하는 것이 유리하다.(4) average mountain height (

) And average width (

) This (

) / (

Has a discharge surface having a fine unevenness and a plurality of polymer discharge holes, which satisfy the range of 0.3 to 5.0, and has a cooling device for cooling the surface of the discharge surface and a take-out device for taking out the formed fiber concentrator. It is advantageous to use a molding apparatus which is characterized by the above-mentioned.

), 평균산 높이(

), 평균산폭(

) 및 토출구는 각각 하기의 설영에 의하여 정의된다.Above molding area, average discharge section distance (

), Average height (

), Average mountain width (

) And the discharge port are each defined by the following settings.

), 평균산 높이(

), 평균산폭(

) 등은 모두 기하학적 확률론의 개념에 의거하여 정해지는 값이며, 성형영역 표면의 형상이 기하학적으로 명백한 것에 대해서는 수학적으로 적분 기하학의 정의와 방법에 의하여 산출된다.Average discharge section distance defined in the present invention (

), Average height (

), Average mountain width (

) Are all determined based on the concept of geometric probability, and the shape and shape of the surface of the molding region are mathematically calculated by the definition and method of integral geometry.

For example, theoretically p = √3r and d = πr / 2 for the molding region of the mold in which the spherical body sintered body of radius r is densely packed.

,

,

를 정할 수 있다. 실측에 있어서는 미세하고 균일한 성형 영역표면에 한하여 성형영역의 중심부에 원점을 정하고 그 주위에 30°마다 6개의 단면을 취하여 측정하면 근사적으로

,

,

를 구할 수 있고 실용적으로는 이것으로 충분하다.As such, it can be theoretically determined that the surface of the detention is constituted by a collection of fine and uniform geometric formations, but when it comes to having a fine and non-uniform surface shape, the detention is cut into several orthogonal cross-sections or cuts. This easy material takes the shape of the surface of the cap and cuts it

,

,

Can be determined. In actual measurement, only the fine and uniform surface of the molding area is defined as the origin at the center of the molding area, and 6 cross-sections are taken every 30 ° around it to measure approximately.

,

,

Can be obtained and this is sufficient in practice.

As illustrated in FIG. 8, the shaping region is a region of the briquettes in which a fiber aggregate having a substantially uniform density is formed in the mold 5 for ejecting the molten polymer from the spinneret 4 to spin-mold the fiber assembly. Say

In the molding apparatus of the present invention, the discharge port of the polymer is used to cut the molding region of the mold at right angles to the average surface (a flat virtual surface taken macroscopically by averaging fine irregularities) (hereinafter, this cross section is referred to as a molding region cross section). ), Refers to the first extremely visible flow width when viewed at right angles to the average surface from the surface of the molding area of the flow path through which the polymer can flow.

In the generalized molding region of the present invention, a schematic enlarged view of an arbitrary cross section is shown in FIG. In Fig. 9, portions A _i and A _i + 1 are discharge ports.

In addition, the distance between the centerlines of the arbitrary discharge ports A _i and A _i + 1 adjacent to each other is called the discharge section distance P _i , and the average P _i in all cross sections is defined as the average discharge section distance p. .

Moreover, in the cross section adjacent to the right side of the arbitrary discharge port A _i of an arbitrary cross section, the mountain (Hi) which attaches the surface area part of the shaping | molding area | region to A _i from the A _i part is called, and the vertex and the average plane of A _i perpendicular direction The interval h _i is called the mountain height of H _i , and the average of h _i in all cross sections is defined as the mountain height h.

In addition, the width parallel to the average surface of the mountains H _i sandwiched between the discharge ports A _i and A _i +1 is called the acid width d _i , and the average of d _i in all the cross sections is defined as the average acid width d.

According to each of the above definitions, the molding apparatus of the present invention has a molding region of a molten polymer.

)가 0.03 내지 4mm의 범위, 바람직하게는 0.03 내지 1.5mm, 특히 0.06 내지 1.0mm의 범위,(1) Average discharge section distance (

) Ranges from 0.03 to 4 mm, preferably from 0.03 to 1.5 mm, in particular from 0.06 to 1.0 mm,

)가 0.01 내지 3.0mm의 범위, 바람직하게는 0.02 내지 1.0mm의 범위,(2) average mountain height

) Ranges from 0.01 to 3.0 mm, preferably from 0.02 to 1.0 mm,

(3) the average acid width d is in the range of 0.02 to 1.5 mm, preferably in the range of 0.04 to 1.0 mm and

)와 평균산폭(

)이

/

로 표시하여 0.3 내지 5.0의 범위, 바람직하게는 0.4 내지 3.0의 범위를 만족시키는 미세 요철 표면과 다수의 중합체 토출구를 갖는 것이 유리하다.(4) average mountain height (

) And average mountain width

)this

Of

It is advantageous to have a fine uneven surface and a plurality of polymer ejection openings that satisfy the range of 0.3 to 5.0, preferably 0.4 to 3.0.

As described above, the values of p, h, d and h / d are set to be in the range of (1) to (4), and the value expressed in (pd) / p is in the range of 0.02 to 0.8, preferably It is further advantageous to set the structure of the surface of the detention so as to be in the range of 0.05 to 0.7. The value of (p-d) / p is a value which shows the area ratio in the shaping | molding area | region of a discharge port when it reduces.

A molten polymer is ejected from the ejection opening having such a fine ejection surface structure to cool the ejection surface, and the ejection of the molten polymer is carried out under suitable conditions to form a network fiber concentrator.

According to the present invention, a filamentary fiber aggregate can be produced from many thermoplastic synthetic polymers as described below.

i) polyolefin-based or polyvinyl-based polymers;

For example, polyethylene, polypropylene, polybutylene, polystyrene, polyvinyl chloride, polyvinyl acetate, polyacrylonitrile, polyacrylic esters, or cross-copolymers thereof.

ii) polyamides;

For example, poly ε-caprolactam, polyhexamethylene adipamide, polyhexamethylene sebacamide.

iii) polyester;

For example, Aromatic dicarboxylic acid, such as phthalic acid, isophthalic acid, terephthalic acid, diphenyl dicarboxylic acid, naphthalin dicarboxylic acid; Aliphatic carboxylic acids such as adipic acid, sebacic acid and decandicarboxylic acid; Or an alicyclic dicarboxylic acid such as hexahydroterephthalic acid as a dibasic acid component, and an ethylene glycol, propylene glycol, trimethylene glycol, tetramethylene glycol, decamethylene glycol, diethyl glycol, 2,2-dimethylpropanediol, hexahydroxyylene Polyesters having aliphatic, cycloaliphatic, or aromatic glycols such as glycol and xylene glycol as glycol components are advantageous. These dibasic acid components or glycol components may be polyesters of one kind or a combination of two or more kinds, respectively. Particularly preferred examples are the polyester elastomers described in polyethylene terephthalate, polytetramethylene terephthalate, polytrimethylene terephthalate, US Patent Nos. 3,763,109, 3,023,192, 3,651,014 and 3,766,146.

iv) other polymers;

Polycarbonate using various bisphenols other than the polymer of said (i)-(iii); Polyacetal; Various polyurethanes, polyfluorides, copolyethylene fluorides.

The thermoplastic synthetic polymers described above may be used alone or as a mixture of two or more thereof. Moreover, you may add a plasticizer, a viscosity increasing agent, etc. in order to increase the plasticity and melt viscosity of a polymer. In the polymer, an optical stabilizer, a pigment, a thermal stabilizer, a flame retardant, a lubricant, a chlorine agent, and the like, which are usually used as additives of fibers, may be added.

In addition, the polymer is not limited to the linear polymer, and may be a polymer having a three-dimensional structure in which a part is crosslinked as long as the thermoplastic is not impaired.

On the other hand, when manufacturing the filamentary fiber aggregate of the present invention, the molten polymer may contain a part of the soluble liquid, and an inert gas or gas generator may be added. In particular, when the production method of the present invention is carried out by adding a volatile liquid medium, an inert gas or a gas generating agent, the liquid medium or the gas may be exploded on the surface of the cap, thereby forming a fiber aggregate having a more detailed fiber cross-sectional structure. have. As the gas in this case, nitrogen, carbon dioxide gas, argon, helium and the like are suitable.

As described above, the production method of the present invention is a polymer conventionally used for melt spinning, for example, polyethylene terephthalate, poly ε-caprolactam, polyhexamethylene adimidamide polyethylene, polypropylene, polystyrene, polytetramethylene Not only polymers such as terephthalate are advantageously applied, but also polymers such as polycarbonate, polyester elastomer, and the like, which have conventionally been difficult to be melt-reflected industrially, can be easily fiberized without any trouble. In this way, according to the production method of the present invention, any of crystalline or amorphous polymers can obtain a fiber bundle.

According to the present invention described above, by adjusting the type of the polymer, the structure of the spinneret, the spinning conditions, and the like, the filamentary fiber aggregate ranging from about 30 cm on average to about 10 m or several 100 m It becomes possible to manufacture by a continuous stable operation. The filament constituting this fiber assembly,

A) This filament has a cross-sectional size change at irregular intervals along its length,

B) The cross-sectional area coefficient of variation [CV (F)] in the filament is characterized by a range of 0.05 to 1.0, which is different from any conventionally known artificial filaments or fibers.

The cross-sectional area coefficient of variation [CV (F)] here refers to the fluctuation of the fineness of the filament in the longitudinal direction (axial direction). For any one filament of the fiber bundle, 3 cm is selected at any one place. This can be calculated from the following equation (11) by measuring the cross-sectional area size at intervals of 1 mm by microscopic observation to obtain 30 cross-sectional mean values (A) and 30 cross-sectional standard deviations (A).

CV (F) = σA√A... … (11)

The filaments constituting the fiber assembly of the present invention are those in which the CV (F) is in the range of 0.05 to 1.0, and particularly preferably in the range of 0.08 to 0.7, of which 0.1 to 0.5.

FIG. 10 and FIG. 11 show graphs plotting the measured values of the cross-sectional area sizes at intervals of 1 mm for two different filaments of the present invention. As is apparent from these graphs, the filaments of the present invention are characterized by having irregular size changes in the cross-sectional area at irregular intervals along the longitudinal direction, even when observed for 5 mm unit length, for example.

Such a feature is considered to be formed by the manufacturing method of the fiber bundle body of this invention completely different from the conventional melt spinning method mentioned above.

Moreover, the filaments constituting the fiber bundle of the present invention are characterized in that the cross section is non-circular as shown in FIGS. 1, 3, 4, 5, and 7.

Another feature of the present invention is that, as shown in FIG. 12, the cross section is non-circular, has an irregular size change in the cross-sectional area at irregular cycles along the longitudinal direction of the filament, and also has a change in cross-sectional shape with it. will be.

The degree of non-circularity of the cross-sectional shape of the filament is expressed as a ratio (D / d) of the maximum distance (D) of two parallel lines to circumscribe and the minimum distance (d) of two parallel lines to circumscribe as shown in FIG. It can be expressed as a coefficient. The filament of the present invention has a release coefficient (D / d) of at least 1.1 and almost 1.2.

In addition, the filament of the present invention is characterized in that the release coefficient D / d changes along the longitudinal direction of the filament, as apparent from FIG. 12.

In addition, this filament is the maximum release coefficient [(D / d) _max ] and the minimum release coefficient [(D / d) _min ] in an arbitrary range of 30 mm along the longitudinal direction. / d) _max- (D / d) _min ] is at least 0.05, preferably at least 0.1.

Filamentary fibers having the above characteristics are not known at all in the prior art, and have morphologically similar characteristics to natural fibers such as silk, for example.

Moreover, according to the present invention, filaments having irregular periods of irregular crimps along the longitudinal direction of the filaments as undrawn yarns are obtained as shown in FIG. 14 using many polymers.

The filamentary fiber focusing body of the present invention is a filamentous focusing body formed of a plurality of filaments made of at least one thermoplastic synthetic polymer, and (1) each filament constituting the focusing body has a cross-sectional size at irregular intervals along its longitudinal direction. Has a change of,

(2) The filament has a cross-sectional variation coefficient (CV (F)) in the range of 0.05 to 1.0 in filament,

(3) The cross-sectional area size of each filament in the case of cutting the focusing body in a direction perpendicular to the filament axis at any position of the connecting body is characterized by being substantially random.

The feature 3 can be clearly understood in FIGS. 1, 3, 4, 5 and 7.

In addition, the cross-sectional area variation of each filament when the focusing body is cut at right angles to the filament axis at any position of the present invention is expressed in the range of the filament cross-sectional area variation coefficient [CV (A)] in the range of 0.1 to 1.5, In particular, it is most suitable that CV (A) exists in the range of 0.2-1.

This CV (A) extracts 100 partial focus bodies randomly from the said focusing body, and measures the magnitude | size of each cross section by microscopic observation of the cross section in arbitrary positions, and the average value (B) and 100 The standard deviation (σB) of the cross-sectional area of the dog can be obtained and calculated from the following equation (12).

CV (A) = σ B / B. … (12)

In the filamentary fiber concentrator of the present invention, when the converging member is cut in a direction perpendicular to the filament axis at any position of the concentrator, the cross section of each filament is substantially different in size and shape. Doing. This is evident in FIGS. 1, 3, 4, 5 and 7 and 12 above.

In the filamentary fiber concentrator of the present invention, when the converging member is cut in a direction perpendicular to the filament axis at any position, the cross section of each filament is non-circular, and each cross section has a release coefficient (D / d) of at least 1.1. And nearly 1.2.

In addition, at least a release coefficient maximum difference represented by the difference between the maximum release factors and maximum release coefficient in the case where the aforementioned fiber cross-section is extracted to more than 30 randomly _{[(D / d) max -} (D / d) min] Is at least 0.05, and preferably has at least 0.1.

In addition, the fiber bundle of the present invention has irregular crimps as an aggregate of unstretched yarns obtained from many polymers, and each filament constituting the fiber bundle has a randomly different crimp. This fact becomes apparent, for example, from FIG.

Each different irregular crimp of each of these filaments becomes more prominent by non-aqueous treatment or non-aqueous treatment of unstretched fiber aggregates as shown in FIGS. 16 and 17.

The filamentary fiber aggregates of the present invention are a plurality of fiber bundles made of thermoplastic synthetic polymers, and the cross-sections of the fibers when the fibers forming the bundle are cut at right angles to the fiber axis have different shapes and sizes. And, according to the definitions described in the text,

i) the average fineness (D) in the focusing body of the fibers forming the fiber focusing range is 0.01 to 100d _e ,

ii) the filament cross-sectional variation coefficient [CV (A)] of the fineness of the fibers forming the fineness concentrator is in the range of 0.1 to 1.5,

iii) It is preferable that the coefficient of variation in cross-sectional area [CV (F)] in the filament in the longitudinal direction of the fibers forming the fiber bundle ranges from 0.05 to 1.0.

The average fineness (average denier D _e ) in the above-mentioned focusing body may randomly extract 10 100 sub-focusing bodies from the focusing body (it may be three if it is easy to carry out. Almost unchanged from the case of dog extraction) One spot in the fiber axis direction of each sub-collector is randomly selected and cut in a right angle direction. The sum of the weights of the cross-sections and the weights of the cross sections are divided by the bow of the cross-section photograph, averaged, and the value [m (A)] is converted into denier (d _e ).

Therefore, the average fineness D _e in this aggregate is computed from the following formula.

D _e = Km (A)

However, in the above formula

m (A) is the weight average value of the fiber cross section of the cut-out photograph, K is a denier (d _e ) conversion coefficient, and is calculated | required by Formula K = 9 * 10 <^5> * (rho) / (alpha) * (beta). Where α is the unit area weight (g) of the photograph, β is the area magnification of the photograph, and ρ is the specific gravity of the thermoplastic polymer, all of which are expressed in CGS units.

For example, when the filamentary fiber bundle of the present invention is made by mixing two or more polymers, or when the gas or gas generating material is mixed with the polymer melt and spun as a foamable melt, In the case of producing from the melt, a plurality of stripe shapes continuous along the fiber axis are formed on the filamentary fiber surface constituting the focusing body. "Multiple stripe shapes along the fiber axis on the fiber surface" is confirmed by observation by the following method.

As shown in Figs. 18A and 18B, the fiber assembly is cut at right angles to the fiber axis, and the cut section is photographed at a magnification of 1,000 to 3,000 times with a scanning electron microscope at a 45 ° angle to the fiber axis. From this picture, it is possible to recognize a number of consecutive stripes along the fiber axis on the fiber surface.

However, in the case of forming a fibrous material by extruding a thermoplastic polymer from a nozzle having a geometric shape, a release such as a release cross-section fiber [eg, star, triangle, etc.] resulting from the shape of the nozzle The horizontal stripe resulting from the cross section is not referred to as the "stripe pattern" above, and the stripes in the fiber axis direction that can be recognized in the relatively smooth surface portion of the side of the fiber axis in the photograph are referred to as the "stripe pattern" in the invention. do.

In particular, the fiber concentrator of the present invention is capable of identifying a continuous stripe shape along the fiber axis in at least 30% of the visible surface (preferably in at least 40%) of the fiber surface of at least 50% by the above-described photographic observation. It is best to have one.

Using a fiber bundle having such a stripe pattern on the surface of the fiber, for example, when the fabric is formed, the surface appearance of smooth, cold texture, gloss, etc. together with the cross-sectional shape and longitudinal fluctuations described above is the natural silk fabric. It becomes very similar to, and also in the functionality and the like can be obtained that the advantages of the synthetic polymer is superior to the added natural products.

Thus, the stripe shape does not mean that it exists on all the fiber surfaces forming the fiber concentrator of the present invention, and the presence or absence of the stripe shape and the amount thereof are combined with the type of the thermoplastic polymer to cool the surface of the molten polymer and the surface of the metal surface. It depends on the conditions.

According to the research of the present inventors, in the case of a mixture of two or more kinds of polymers, a stripe pattern occurs more easily than in the case of a single polymer, and the ratio of irregularities in the discharge surface of the molten polymer (that is, the value of the h / p) It was found that the larger the value), the easier it is to obtain a stripe-shaped fiber, and moreover, the smaller the discharge surface relative temperature ratio θ, that is, the stronger the cooling of the surface, the easier the stripe-like fiber can be obtained. In combination with these types of polymers, the ratio of irregularities on the discharge surface and the cooling conditions on the discharge surface are not absolute conditions for obtaining streaked fibers, but are affected by various conditions in addition to each other, and the factors interact with each other. A stripe shape is formed.

In particular, (a) two kinds of polymers (particularly two kinds of polymers having different physical properties) are mixed at a ratio of 30/70 to 70/30 wt%, and (b) the h / d value at the discharge surface is 0.5 or more. , (c) When the discharge surface relative temperature ratio θ is 1.03 or less, it is possible to obtain a fiber bundle having a large stripe pattern on the surface. Of course, the requirements of (a), (b) and (c) above do not have to satisfy all three of these requirements, and even when one or both of the requirements are satisfied, the stripe-shaped fiber aggregate It goes without saying that there are cases in which it can be obtained.

Furthermore, according to the present invention, as clearly shown in FIG. 22 (Example 31), the filamentary fiber bundle of the present invention is cut in an arbitrary direction in a part of a plurality of cross sections which can be seen when the filamentary fiber bundle is cut perpendicular to the fiber axis. A fiber bundle comprising a fiber having a cross-sectional shape having protruding beard-like protrusions can be obtained. Thus, a fiber bundle having a cross section in which a part of the fiber has a protrusion is not as typical as in FIG. 22, but can also be seen in FIG.

In the case where the base polymer of the filamentary fiber aggregate of the present invention is a hard and a cultured polymer, as shown in FIG. 19, in many cases, it has some degree of crystallinity and culture in an unstretched state. The degree of crystallinity and culture can be further increased by stretching or heat treating the aggregate.

As described above, even when the unfocused fiber bundle is stretched or stretch heat treated, the aforementioned CV (F) and CV (A) do not depart from the above ranges.

Of course, by stretching, physical properties such as strength, young's modulus of the fiber assembly can be improved.

Moreover, when extending the fiber assembly of this invention, it has the following characteristics not seen with the general fiber assembly. In the case of a general long-fiber convergence (tow) obtained by ordinary orifice spinning, the focusing body is cut at about the same place at the same time when the stretching range is exceeded (maximum drawing ratio), but the fiber focusing material of the present invention Due to the weak irregularity in the longitudinal direction, the focusing body is not abruptly cut at the same place even when the maximum draw ratio is exceeded, and the fiber can be produced by partially cutting the fiber because the acid is cut in the focusing body. Do.

By coagulating this phenomenon, it is possible to easily produce the same focusing body as the sliver in spinning or a bulky filament having the same properties as the spinning yarn.

Although it depends on the draw ratio by drawing the fiber assembly of the present invention, the filament junction point is cut and the distance between the average junction points is further increased to obtain a filamentary fiber assembly having a very long distance between the junction points, in which case there is almost no junction point. It is possible to obtain a fiber aggregate such as formed substantially from long fibers.

On the other hand, the fiber bundle having few junction points between the filaments can be obtained by giving the fiber bundle a physical stress in the axial direction of the fiber, such as stretching, but by developing the other fiber bundle in a direction perpendicular to the fiber axis. The junction point may be cut to obtain a continuous filamentary fiber bundle having almost no junction point.

In the fiber concentrator of the present invention, any one of a relatively large or small number of joining points can be cut into a suitable length in a direction perpendicular to the fiber axis to form a short fiber. Even such aggregates of short fibers fall within the scope of the fiber aggregate of the present invention as long as the requirements as the fiber aggregates specified in the present invention described above are satisfied. Such short fibers are preferably 200 mm or less in average length of the fiber, preferably 150 mm or less. The fiber concentrator of the present invention, which is preferable as short fibers, may be used as it is, or may be used by mixing with other fibers. In this case, if at least 10% by weight, preferably at least 20% by weight is the fiber aggregate of the present invention, the characteristics of the fiber aggregate of the present invention can be expressed. The short fibers may also be mixed with these or other short fibers to be used as a weaving yarn.

The fiber assembly of the present invention has a certain range of fluctuations in fiber cross-section along its cross-sectional shape, size, distribution and fiber axis direction, and such fiber bundles cannot be obtained from a known fiber manufacturing method. As a focusing body, structural properties and various interesting things that can not be obtained from the conventionally known ones are expressed.

As the cross-sectional shape, size, distribution, and fluctuation range of the fiber cross section along the fiber axis direction are partially similar to natural silk or wool, the fiber assembly of the present invention uses synthetic fibers having similar characteristics and characteristics to such natural products. It can be said that it can provide.

Thus, the fiber assembly of the present invention can be used as a material of all textile products such as woven fabrics, knitted fabrics, and other nonwoven fabrics.

The fiber bundle of the present invention expresses highly crimped by heat treatment in many cases due to moderate irregularities in the fiber cross section and the longitudinal direction and cooling effect in different directions imparted at the time of fiber forming, and this property increases the entanglement of fiber cross-linking. It can be applied to things.

The fiber connecting body of the present invention can be easily applied to the above-mentioned parallel arrangement sheet, orthogonal nonwoven fabrics bonded by orthogonal bonding thereof, random structure nonwoven fabrics randomized by applying electricity or air, and artificial leather.

Hereinafter, an Example demonstrates this invention. However, the following examples are described to facilitate understanding of the present invention, and do not limit the present invention in any way.

Example 1

In an apparatus as shown in FIG. 8 using a polypropylene (grade for fiber made by Ubegosansha, melting point 440 ° K) chip, the spinneret 7 has a one-piece molding area, just below the spinneret. The filament yarn fiber concentrator is molded by the same molding apparatus as shown in FIG. 8, except that the cooling apparatus 8 has a single-slit nozzle.

That is, the chip is kneaded and melted at a temperature range of 200 to 300 ° C. while continuously supplying the chip to the extruder 2 having an internal diameter of 30 mm, and the molten polymer of 12 gr per minute is sent to the spinning head 6 by the gear pump 5. The molding area area S _O is discharged from a rectangle of approximately 11 cm ² .

In addition, as described in the text on the surface of the spinneret used for spinning a conventional orifice having 1,000 linear holes having a diameter of 0.5 mm, the cross section is V-shaped (about 0.7 mm wide and about 0.7 mm deep). A groove of radial aspect 1 is used by intersecting the grooves with crosses at an angle of about 45 ° and about 135 ° with respect to the arrangement of the orifice holes.

The molding conditions of the filamentary fiber connecting body are as shown in Table 1-1, and the polymer ejection surface of the spinneret and the cooling in the vicinity of the filamentary fiber connecting body are formed in the filamentary phase from the cooling apparatus having the gas injection nozzle immediately below the nozzle. The cooling wind velocity passing through the fiber bundle is 7 m per second to obtain a filamentary fiber connecting body having a total denier of 14,000 denier at a speed of 8 m per minute and having a cross-sectional shape as shown in FIG.

The filament cross-sectional area variation coefficient CV (F) and the filament release coefficient (D / d) F of the filamentary fiber connecting body were measured by the methods described below, and the results are as shown in Table 2-1. 0.18 and 1.22. The cross-sectional area variation coefficient CV (F) in the filament of the filamentary fiber converging member elects the filament of any of the filamentary converging fibers, and any one of them is buried in an ester-based hardening resin for fiber fixing (manufactured by Reich Hold Japan). The microtome (Ultramicrotome manufactured by Nippon Microtome Research Institute) was cut into thin films of 15μ, taken with an optical microscope (manufactured by Nikon), taken with an optical microscope (made by Nikon). The individual cross-sectional area of the fiber is measured.

The cross-sectional area of 1 fiber every 1 mm interval is used for the sample fixed in the resin of 3 cm length, and the cross-sectional area of every fiber 2 mm interval of 1 fiber is used for the sample fixed in the resin of 6 cm length, and also 1 fiber The cross-sectional area for every 10 mm interval was calculated from Formula (11) described in the text from 30 cross-sectional area values, respectively, using samples fixed in a 30 cm long resin.

Releasing factor (D / d) and a release coefficient maximum difference between the fiber cross-section [(D / d) _max - (D / d) _min] (hereinafter, DIF hereinafter) is a method described in the text by using the art to enlarge Measure

Example 2

Except for spinneret, the same molding apparatus as that used in Example 1 was used, and the same polypropylene chip (hereinafter, abbreviated as p and p) as used in Example 1 was taken out by melt extrusion and cooled, A filamentary fiber aggregate having the same fiber cross-sectional shape is obtained.

As the spinneret, a plain weave mesh with an average discharge section distance [p], an average peak height [h], and an average peak width [d] of 0.321 mm, 0.117 mm and 0.220 mm, respectively, and having irregularities on the surface are used. The spinning method corresponds to the spinning mode (2) described in the text. Specific measurements of the values of [p], [h], and [d] were obtained by cutting six cross sections every 30 ° around an arbitrary point of the plain weave mesh, and photographing these cut sections with an optical microscope. A plurality of photographs are analyzed and performed.

Spinning conditions are as shown in Table 1-1, and extremely weak network filamentary fiber aggregates having a total denier of 13,000 deniers and a distance of 6 m between the joint points per filament were obtained.

The measurement of the distance between the junction point was cut at 10 cm test length at any place of the obtained filamentary fiber concentrator, and 200 fibers were carefully scraped with one tweezers and two fibers were welded. The number of junction points which existed was dismissed and computed by the following formula.

0.1 (m) × 200 / (number of junctions) = distance between junctions

The average single yarn denier (D _e ) of the filamentary fiber aggregate obtained in this example was 1.4 denier, and the coagulation cross-sectional area (A ₁ ) was 0.17 × 10 ^-5 cm ² , and the coagulation field was measured by optical microscope observation. 0.2 cm.

The average single yarn denier (D _e ) of the filamentary fiber aggregates shown here is obtained by cutting the cross-sectional photographs of the filamentary fiber aggregates, which were taken in magnified photographs using the JSM-U ₃ format manufactured by Nippon Electronics Co., Ltd. It measured and estimated the cross-sectional area conversion using the formula described in the text. The coagulation cross section [A ₁ ] shown here was computed using said Formula (10) described in the text by the said average single yarn denier [D _e ] measured. In addition, the above-mentioned coagulation field stably blows dry carbon dioxide gas cooled below freezing point to a part of the surface end of the fiber forming region of the spinneret in the step of stably producing the filamentary fiber bundle according to the present invention. The fibrous flow of the polymer melt discharged from the narrow gap was freeze-solidified in the state as it was, to be released from the spinneret, and the filamentary fiber concentrator having a fine portion thereof attached to the terminal was collected for 20 minutes or more.

From the denier obtained by measuring the thinning sections of the obtained fibers of each single fiber at an interval of 100 mu in the fiber length direction using an optical microscope, the fine curves of the fibers of each yarn were obtained, and the fiber coordination was carried out from the analysis thereof. Faults were determined and the coagulation field [L _f ] was measured as these average values.

In the present embodiment, the number of the number of the fibrillated fiber per unit area (1 cm ² ) per unit area (1 cm ² ) at a distance away from the spinneret is 290, much more than the number of fibers corresponding to the conventional orifice melt spinning method. .

As in Example 1, the cross-sectional variation coefficient CV (F) (1 mm interval) of the filamentary fiber aggregate of this example was selected by randomly selecting three fibers, and each 3 cm at each end of 0.5 m, 1 m, and 1.5 m intervals, respectively. When six CV (F) were measured in the part of length, all were in the range of 0.15-0.35 and there was no bogie. In these six places, even if the release coefficient and the maximum coefficient of release coefficient of the fiber cross section were measured as in Example 1, they did not deviate much from the values shown in Table 2-1.

伸度)는 임의로 선출한 30본의 섬유를 텐숀미터(동양측기사제 VTM-11)를 사용하여 반복, 측정하여 평균치를 구하면 각각 0.86g/d_e및 150%였다.Single yarn strength and single yarn elongation of the filamentary fiber aggregate of this embodiment

伸度) is tensyon one of the fibers 30 randomly chosen m (repeated using Oriental Co. instrumental VTM-11), an average value was determined to ask each of 0.86g / d _e and 150%.

The filamentous fiber bundle was immersed in water for 10 minutes, and then dried by wind, and each fiber was selected from the fiber bundle, and the crimp number was observed by an optical microscope, and the average was 6.5 N / 20 mm.

In addition, the filamentary fiber aggregate obtained in this Example was stretched 2.4 times in a bath of 90 to 100 ° C., and the performance of the stretched yarn was measured in the same manner as in the non-stretched yarn, as shown in Table 2-1. Afterwards, natural crimps were expressed, and the fiber strength was sufficient to be applied to various applications.

Example 3

Except spinneret, polypropylene chips were melt-extruded and drawn while cooling using the same molding apparatus as that used in Example 2 to obtain a filamentary fiber aggregate.

As the spinneret, Table 1 was used using a twill weave network (level weave network manufactured by Filcon Japan) having an average discharge section distance [p], an average acid height [h], and an average acid width [d] of 0.380 mm, 0.085 mm, and 0.3000 mm, respectively. The mixture was taken out under cooling under the same spinning conditions as shown in the above to obtain a filamentary fiber aggregate having a total denier of 29,000 denier and an average single yarn denier of 1.8 denier. 3B is a cross-sectional electron microscope photograph at an arbitrary portion of the obtained fiber bundle. The fiber form and fiber performance of the unstretched yarn of the obtained filamentary fiber bundle are as shown in Table 2-1.

In this regard, the X-ray diffraction measurement of the obtained filamentary fiber concentrator was measured under the following conditions by a Ru-3H type X-ray wide-angle apparatus manufactured by Science and Electrical Industry.

Cave P

(KVP): 80mA

Target

(Target): Cu

filter

(Filter): Ni

Pinhole Slit

(pinhole slit): 0.5mmΦ

Exposure: 60 minutes

Camera Radius: 5cm

An X-ray diffraction photograph of FIG. 19 is obtained.

The fiber form and fiber performance of the unstretched yarn and the stretched yarn of the filamentary fiber aggregate obtained in this example are shown in Table 2.

Example 4

Except for spinneret, the polypropylene chip (p.p) was taken out by melting and extruding and cooling by using the same molding apparatus as that used in Example 2 to obtain a filamentary fiber aggregate. As the spinneret, as shown as the third radiation aspect in the text, a projecting pin was formed by cutting through the narrow gap of the mesh of the plain weave mesh net one by one. The average discharge section distance [p], average peak height [h] and average peak width [d] of the spinnerets used were very large as shown in Table 1, but they were stable under the spinning conditions shown in this table. A coarse filamentary fiber aggregate having a denier of 39.0 deniers was obtained. The fiber form and fiber performance of the unstretched yarn of the filamentary fiber aggregate are as shown in the second table.

Example 5

Except for spinneret, polypropylene chips were melt-extruded and drawn while cooling using the same molding apparatus as that used in Example 2 to obtain a filamentary fiber aggregate.

The spinneret is a sintered metal porous plate body in which a plurality of fine bronze metal spheres are densely packed and arranged and sintered and fixed as shown in the fourth spinning mode in the text.

The surface of the spinneret has hemispherical irregularities and the area porosity is about 9%. When viewed under a narrow interval of optical microscope discharged from the molten polymer, the hole diameter and hole shape become very uneven. there was. Nevertheless, withdrawal at a speed of 30 m per minute while cooling under the spinning conditions described in Table 1, a filamentary fiber condenser having a total denier of 1.3 denier is obtained stably. Observation of the cross section at any part of the filamentary fiber assembly with a scanning electron microscope yields a quadrangular filamentary fiber assembly with irregular cross-sectional shapes and a slight deformation as shown in FIG. Thus, the cross-sectional area variation coefficient [CV (F)], which is a feature of the present invention, also in the non-drawn yarn of the filamentary fiber aggregate having a nonuniform cross-sectional area and its shape and a stretched yarn that has been stretched 3.2 times in a bath of 90 to 100 ° C., The release coefficient [D / d] and the release coefficient maximum difference [(D / d) _max -[(D / d) _min ] were as shown in the second table.

Example 6

Except spinneret, polypropylene chips were melt-extruded and drawn out using the same molding apparatus as that used in Example 2 to obtain a filamentary fiber aggregate.

As the water-proof detention, as shown in the fifth radiation mode in the text, a very large number of stainless steel plain weave mesh fabrics woven with a diameter of about 0.2 mm to have a porosity of about 30% are compressed and laminated to have a high density in a longitudinal arrangement. use.

Using this spinneret, the polymer melt is extruded to exude through the lamination intervals of the individual planes of the plain weave mesh to obtain a filamentary fiber aggregate having a cross-sectional shape as shown in the scanning electron micrograph of FIG.

Thus, even if the fiber cross-section is irregular, the cross-sectional variation coefficient [CV (F)] remains within a certain range, and the filamentary fiber aggregate can be stretched 2.9 times in a bath of 90 to 100 ° C. Unique is obtained.

It was 0.9 m when the distance between the junction points of the filamentary fiber aggregates obtained in this example was obtained by the method described in Example 2.

Example 7

Except spinneret, polypropylene chips were melt-extruded and drawn with cooling using the same molding apparatus as that used in Example 2 to obtain a filamentary fiber aggregate.

)인 다수매의 금속판을 제6도에 나타낸 것처럼 각각 약 0.25mm의 간격을 두고 가로로 적충한 것을 사용한다.As the spinneret, as shown in the sixth aspect of radiation in the main body, the distal end portion is sawtooth shaped (

A large number of sheets of metal plates (), which are horizontally stacked with a space of about 0.25 mm each, are used as shown in FIG.

The scanning electron micrograph of the cross section in any part of the filamentary fiber assembly obtained in this example is FIG. 7, and is similar to the cross-sectional picture of the filamentary fiber assembly in Example 6. In some cases, the cross-sectional shape of the filamentary fiber aggregate obtained in the fifth and sixth aspects was different from each other.

The fiber form and fiber performance of the filamentary fiber aggregates obtained in this example were as shown in the second table.

[Examples 8 to 14]

Using a molding apparatus having the same spinneret as in Example 3, melt extrusion was carried out using a variety of the following polymer chips as shown in the first table, and withdrawn while cooling each under the spinning conditions described in the above table suitable for each polymer. A filamentary fiber aggregate of each polymer is obtained.

Polyethylene: high density grade made by Ubegoshan

Melting Point 404 ° K (P.E.)

Polystyrene: Asaida Company, Stylon-666 grade

Melting Point 473 ° K (abbreviated PS _t )

Nylon-6: Made by Teijin Sha, Intrinsic Viscosity η = 1.3

Melting Point 496 ° K (N _y abbreviation)

Polybutylene terephthalate: made by Teijin Sha, intrinsic viscosity η = 1.1

Melting Point 496 ° K (abbreviated PBT)

Polycarbonite: Teijin Shaze

Average molecular weight 24,000

Melting Point 515 ° K (P.C)

Polyethylene terephthalate;

Teijin Shaze, Intrinsic viscosity η = 0.71

Melting Point 540 ° K (PET)

Polyester elastomer;

DuPont Company, HITUEL 5556 Grade

Melting Point 484 ° K (abbreviated as Pes, Elas)

The individual fiber cross-sectional shapes of the respective filamentary fiber aggregates obtained in these examples were approximately the same as those in FIG. 3B and were in the form of non-uniform cocoon.

In addition, the fiber form and fiber performance of the filamentary fiber aggregates of the various polymers obtained in these examples are as shown in Table 2, and are treated under the stretching conditions (stretching temperature and stretching ratio) suitable for the individual polymers. As a result, as shown in Table 2, the filamentary fiber aggregate having the fiber type and fiber performance as shown in Table 2, as a result of treatment under the stretching conditions (drawing temperature and draw ratio) suitable for the individual polymers And the fiber style thereof was good.

Example 15

In addition to the spinneret, the polypropylene chip is melt-extruded and drawn while cooling by using the same molding apparatus as the apparatus used in the case where 2 is carried out to obtain a filamentary fiber aggregate. For spinnerets, the average discharge section distance [p], average peak height [h] and average peak width [d] were 0.443 mm, 0.139 mm and 0.277 mm, respectively. As a result, the filamentary fiber bundle had a coagulation length of 0.11 cm, which was extremely short as a spinning method, with the apparent draft defined as 3800 being cooled down to 3800. The fiber form and fiber performance of the filamentary fiber aggregates obtained were as shown in the second table.

Example 16

Using the same spinneret and molding apparatus as in Example 15, the same polymer melt was used, except that the polymer melt per unit area of the mold forming zone was extruded and cooled at a rate of 32 m per minute while being cooled and extruded to condense filamentous fibers. Obtain a sieve.

The fiber coagulation field at the time of carrying out this example was 0.28 cm, and the fiber thinning phenomenon was completed within 1 cm even if the discharge amount per unit area of the polymer melt increased rapidly.

Example 17

A coarse filamentary fiber aggregate having an average single yarn denier of 31 denier was taken out while being cooled using the same polymer melt as the apparatus used for carrying out Example 15 except the spinneret.

In the present Example, the coagulation length of the filamentary fiber aggregate was short as 0.6 cm despite the extremely high average single yarn denier.

[CV (F)] of the filamentary fiber aggregate having small single yarn denier values such as the cross-sectional area variation coefficient [CV (F)] and the release coefficient (D / d) of the fibers, which is a feature of the present invention even when the average single yarn denier is increased. And (D / d) and the like in the same range.

Example 18

This embodiment manufactures a filamentary fiber focusing body in a relatively large amount. Using a molding apparatus such as that according to FIG. 8 by melt extrusion through supplying a fixed quantity of polyporopylene (melting point 438 ° K, melt index 15) chips continuously every 1070 gr / min from an extruder having an internal diameter of 60 mm, A rectangular molding area of 3000 cm ² having four 150 cm by 5 cm rectangular molding areas arranged in parallel is discharged. The unevenness of the surface of the molding region is as described in Table 1.

The cooling device is composed of two tubular objects having a minute and a nozzle, and simultaneously cools the four forming zones by using a suction pipe to provide a discharged place of cold air. The obtained filamentary fiber bundle has a total denier of about 1.1 million denier, and the main properties of the fiber bundle are as shown in the second table.

Example 19

Polypropylene (melting point 438 °) by an extruder with an internal diameter of 40 mm in FIG. 8, in which two rectangular forming zones of 500 mm × 50 mm are arranged in parallel and attached to a detention which is 500 cm ² forming area area (S _O ). K, Melt Index 20) The chip was melted at a temperature in the range of 200 to 300 ° C, and 136 g of the melt was quantitatively extruded per minute by a gear pump under the conditions described in Table 1. The cooling device is cooled from the cooling device in the vicinity of each melt discharge surface of the spinneret under the conditions of detention shown in Tables 1 to 3 provided in the center between the molding regions made up of tubular objects having injection nozzles and arranged in parallel. The fluid is fed at a wind speed of 7 to 10 m / sec and drawn at a rate of 612 cm / min while cooling to obtain a filamentary fiber concentrator. The main properties of the fiber bundle are shown in Table 2.

Example 20

Using a chip of nylon-6 (melting point 488 DEG K), 170 g of the discharge amount per minute was extruded according to Example 19. The filamentary fiber aggregate was obtained under the conditions shown in Table 1 under the conditions of detention and molding.

In addition, the main performance of the fiber assembly is shown in Table 2.

Example 21

From an internal diameter of 60mm extruder renre polybutylene terephthalate (melting point 505 ° K) detained by quantitative supplying chips in a row by 1,540g per minute by performing the melt-extruded molding having a concave-convex surface is made of a region area 3000cm ² as in Example 18, The molten polymer was discharged from the. The detention conditions are as described in Table 1.

The cooling device is composed of a tubular material having an injection nozzle, and is blown while blowing cold air on the surface of the uneven discharge surface and the vicinity thereof to obtain a filamentary fiber aggregate by solidifying the fibrous trickle.

The obtained fiber concentrator has a cross-sectional coefficient of variation in filament CV (F) of 0.34 at 1 mm intervals, and a filament cross-sectional variation coefficient of CV (A) of 0.5 at intervals of 1 mm, and has a bone shape along the fiber axis direction. It is a fiber condenser of mold release and idenier that hydrates.

In addition, other functions are as shown in Table 2.

[Examples 22 and 23]

The melt polymerization solution was extruded in accordance with Example 19 using a polyethylene (melting point 410 ° K, melt index 20) chip from a mold having a molding area of 500 cm ² . The confinement conditions and the molding conditions of the molding region were obtained in the filamentary fiber concentrator by the method described in the Example 22 column of Table 1.

In addition, the filamentary fiber concentrator was molded similarly to the polyethylene terephthalate (melting point 538 ° K) under the molding conditions described in the Example 23 column of Table 1.

Example 24, 25

According to Example 2, polyethylene terephthalate (melting point 540 ° K) was melted and melted at a temperature range of 230 to 330 ° C. using a plain weave gold mesh having the same molding area, and a 70 g molten polymer was formed into a plain weave gold mesh every minute by a gear pump. It is extruded in a mold (p = 0.443mm, h = 0.138, d = 0.277), and the polymer discharge surface and its vicinity of the metal net are taken out while cooling with an air stream to obtain a filamentary fiber aggregate.

In addition, the nylon 6-(melting point 496 ° K) is similarly extruded and taken out while cooling to obtain a filamentary fiber aggregate.

In addition, the molding conditions of a present Example are described in the 1st table | surface, and the performance of the said fiber assembly is shown in the Example 22 (PET) and Example 23 ( _Ny ) column of the 2nd table, respectively.

EXAMPLE 26,27

140 g of polyethylene molten polymer per minute was formed from the molding apparatus of FIG. 8 in which two rectangular bodies having a size of 500 mm x 50 mm were arranged in parallel using the porous carbon body by the same sintering as the spinneret described in Example 5. Melting point 410 ° K, melt index 20) is discharged.

Cooling of the uneven ejection surface of the forming region is carried out 7 to 15 m / sec toward each of the ejection surfaces and its vicinity by a cooling device having a gas ejection nozzle located just below the middle of the two-port ejection opening. Is blown and produced to obtain a filamentary fiber aggregate.

Furthermore, it extruded similarly to the said polyethylene using the nylon-6 (melting point 488 degreeK) chip | tip. In the case of polyethylene and nylon-6, the molding conditions of the filamentary fiber bundle are shown in Table 1, and the main performances are shown in Table 2 in Examples 26 (PE) and 27 (N _y ), respectively. .

Example 28

Extrusion of the molten polymer in the same manner as in Example 26 using a spinneret shown in Table 1 using a mixture chip of 70 wt% nylon-6 (melting point 496 ° K) and 30 wt% polypropylene (melting point 440 ° K) After cooling, the filamentous fiber bundle was molded.

The obtained fiber concentrator was a concentrator of about 120,000 denier, and the fiber concentrator was a bundle of heterofibers and an denier of each single fiber, and its form was a scanning electron micrograph photographed at a 45 ° angle of the fiber axis. 18a (about 1000 times) and 18b (about 3000 times) were the same, and a plurality of continuous bone patterns along the fiber axis of the fiber surface can be clearly recognized.

In addition, the filament cross-sectional area variation coefficient CV (F) of the fiber concentrator according to the description method in the main text is 0.36 at 1 mm intervals, the release coefficient in the filament (D / d) F is 1.67, and the cross-sectional area variation coefficient CV (A) in the filament Is 6.9.

In addition, the other main properties of the fiber assembly is shown in Table 2.

Example 29

Spinneret shown in Table 1 using a mixed chip of 60% by weight of polybutylene terephthalate (melting point 505 ° K, intrinsic viscosity [η] = 1.2) and 40% by weight of polyethylene (melting point 410 ° K, delta index = 20) In the same manner as in Example 26, the filamentary fiber concentrator was obtained by cooling the uneven ejection surface of the forming region while cooling the same as in Example 26. The main properties of the obtained filamentary fiber aggregates are as shown in Table 2, and even after stretching, the fiber aggregates of mold release and edenier were confirmed.

Example 30

Using the same spinneret as in Example 19, a mixed chip of 60% by weight of polypropylene (melting point 438 ° K) and 40% by weight of nylon-6 (melting point 488 ° K) as a thermoplastic polymer was vent type having an inner diameter of 40 mm in FIG. Continuous supply to the extruder while melted in the temperature range of 200 to 300 ℃ extruded by using a gas supply device (Fig. 8-4) in the band portion (Fig. 8-3) of the extruder gas pressure 60kg / mixed in cm ² and sufficiently kneaded with a screw, mixed with nitrogen gas at a gas pressure of 60 kg / cm ² using a gear pump (Fig. 8-4) and kneaded sufficiently with a screw, followed by a gear pump (Fig. 8-5). 150 g of the expandable molten polymer was extruded every minute to form a filamentary fiber bundle in the same manner as in Example 19.

In the case of using two or more kinds of polymers as in the present embodiment, the melting point and the melt viscosity are practical in manufacturing even when the gas is kneaded, even if the average mixing ratio of each polymer is approximately the melting point and melting point of the mixing system. There is no obstacle. That is, in the Example, melting | fusing point and melt viscosity were shown by the value calculated | required according to the following formula.

Melting Point (T _m ) = (438 × 0.6) + (488 × 0.4) ≒ 461 ° K

Melt viscosity (η) = (1,100 × 0.6) + (7,000 × 0.4) 3,500poise

As for the obtained filamentary fiber aggregate, the whole denier (ΣD _e ) was 200,000 denier, and the average of the distance between the junction points of the said fiber was about 2 m.

The filamentary fiber aggregate constituting the filamentary fiber aggregate is obtained as a filamentary fiber aggregate having cross-sections of so-called mold releases and deniers having different shapes and sizes, as is apparent from the scanning electron micrograph of FIG.

Example 31

In addition to the spinneret, the polypropylene chip was melt-extruded and cooled by using the same molding apparatus as the apparatus used for carrying out Example 2 to obtain a filamentary fiber aggregate.

As the spinneret, as shown in Table 1, using a twill mesh of p = 0.212 mm, h = 0.160 mm, and d = 0.158 mm (also referred to as Nippon Filcon long cremp wire mesh, or semi-twilled weave wire mesh). Withdrawal while cooling under spinning conditions yields a filamentary fiber aggregate having a total diameter of 108,000 deniers and an average single yarn denier of 17.1 deniers.

FIG. 22 shows an optical micrograph of a cross section of an arbitrary portion of the filamentary fiber aggregate obtained in this example. As is apparent from this cross-sectional photograph, each fiber cross section has a substantially deformed square shape, and many of these cross sections have a beard shape. In addition, changing the withdrawal speed of the filamentary fiber bundle in a wide range, the size of the beard shape and the frequency of beard formation shown in FIG. 22 greatly change.

In addition, the fiber form and fiber performance of the filamentary fiber aggregate obtained in this example are as shown in the second table.

Comparative Example 1

狀)의 필름상의 토출물을 얻는데 그쳤다. 이와 관련하여, 구금의 성형영역의 요철성은 p=0.02, h=0.007, d=0.01인 스테인레스제 평직금망을 사용하였다.As a result of testing melt extrusion of polypropylene with an ejection surface made of a plain weave gold network having a very fine concavo-convex structure in accordance with Example 2, the melt formed a sea as if covering the entire gold network, while rapidly cooling the ejection surface and its vicinity. Even when trying to take out, since the unevenness | corrugation of a discharge surface is minute, a nonpolymer form (island) was not formed and it was difficult to convert the said melt into fibrous trickle. The discharged molten liquid has a continuous close contact (

Only to obtain the film-like discharge of (iii). In this connection, the unevenness of the forming region of the mold was used a stainless steel plain weave mesh network with p = 0.02, h = 0.007, d = 0.01.

Comparative Example 2

In accordance with Example 2, a rough, large (with uneven structure) plain weave mesh having unevenness of p = 4.08, h = 0.462, and d = 1.308 on the surface of the mold forming region by superimposing a stainless plain weave gold mesh inside the die. Polypropylene and nylon-6 were extruded from the mold to attempt fiberization, but coarse continuous yarn, so-called fibrous material, was not obtained. In addition, excessive quenching of the discharge surface to suppress mutual fusion results in melt fracture, and other narrow liquids extruded from a narrow gap through concave portions (valleys) existing between the convex portions (mountains) of the discharge surface. A lot of cutting occurred without coming and going, and it became a plastic rod shape, and continuous fiberization was difficult. Table 1-4 lists data only for polypropylene as a representative example.

Comparative Example 3

Extrusion of polypropylene, nylon-6, polyethylene phthalate, etc. was carried out by using a spinneret extruded in accordance with Example 1, and a plurality of orifices with a hole diameter of 0.5 mm in a stainless plate having a thickness of 5 mm were laid at a pitch interval of 1 mm. None of them could fuse with each other due to the Barus effect or the bending phenomenon to obtain a fibrous material for the purpose of the present invention. In addition, when excessively quenching the discharge surface and suppressing mutual fusion, a melt fracture phenomenon occurs in a plurality of orifices, the filamentous water is cut, and it becomes a so-called rod-like discharge, which makes it difficult to continuously stabilize the fiber. In Table 1, only the case of polypropylene is represented as data as a representative value.

[Comparative Example 4]

The molten polypropylene was extruded under the same confinement conditions of Example 3, and fiberization was attempted without any quenching at all. The molten liquid discharged from the mold forming region forms an ocean as if covering the entire mold forming region, and even when the melt falls from the sea to a mass and changes the polymer temperature in a wide range, it is difficult to attain fibrosis at all.

[Comparative Example 5]

100 parts by weight of polypropylene and 1 part by weight of talc were melted by a bend-type extruder, and foamed from a 140 mm diameter round slitting die having a slitting interval of 0.025 mm while being supplied with inert gas (nitrogen gas) from the bend part. The polymer was extruded. The expandable polymer discharged from the slit die is taken out immediately while being cooled by the cooling wind in the vicinity of the discharge port to obtain a network fiber sheet having a total denier ΣD _e of 6000 denier.

The obtained fibrous sheet was stretched about two times in the transverse direction perpendicular to the drawing direction, and measured and averaged in the range of about 10 × 10 cm ² between the junction points between the fibrous fibers to about 6 mm.

At this time, due to the network structure in which the distance between the junction points between the fibers is too short, the cross-sectional variation coefficient in the filament with respect to the fiber length direction CV (F) 1mm interval varies from 0.65 to 1.58 in some cases by the method described in the text. The filament cross-sectional area coefficient of variation CV (A) also varied from 0.78 to 1.65. This is because the junction point is Y-shaped and the distance between the junction points is very short, compared with the average distance between the junction points of each fiber of the present case at least 30 cm, CV (F) less than 1.0, and CV (A) less than 1.5. The reticulated fibrous sheet has a very dense junction, and the fibrosis of the present case is completely different.

TABLE 1

TABLE 2

Claims (1)

In manufacturing a filamentary fiber bundle by extruding a melt solution of a thermoplastic synthetic polymer from a plurality of narrowly spaced spinnerets, iron portions are provided discontinuously between narrow gaps adjacent to the solution discharge side of the spinneret. And extruding the molten liquid from the spinneret so that the molten liquid is extruded from the narrow gap formed between the recesses existing between the convex portions and the molten liquid. The method for producing a filamentous fiber connector, characterized in that the melt is extruded through the narrow gap while supplying and cooling to convert to solidify a plurality of separated fibrous trickle.

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