JPS6042283B2 - Mixed spinning equipment - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an apparatus for mixing and spinning two or more types of multicomponent polymer streams, and the present invention relates to an apparatus for mixing and spinning two or more types of multi-component polymer streams, and allows sea-island fibers having an arbitrary distribution of fineness of the island components to be produced more stably in any mixed state. The present invention relates to a mixed spinning device that can achieve excellent fiber uniformity.

BACKGROUND ART Mixed spinning technology has been well known for the purpose of modifying synthetic fibers.

The most common method for mixed spinning is to mix component polymers in the form of chips, and then spin this using a melt extruder.

This is considered the simplest and most economical method and device and is the most widely used. However, there are limits to the controllable range of the mixed state of incompatible polymers, that is, the sea-island state obtained by this method and apparatus, and the combinations of polymers that can be mixed are also limited. The present invention has been made in view of such conventional mixed spinning technology, and the purpose is to create a mixed spinning method that allows sea-island fibers having islands with arbitrary fineness distribution to be made into sea-island fibers with extremely good uniformity and stability as a whole. It is an object of the present inventor to provide a method and a mixing device which can achieve such a sea-island state extremely efficiently and which has a simple structure. 71909, Japanese Patent Application No. 1983-64735, Japanese Patent Application No. 132251-1983, and especially Japanese Patent Application No. 1987-1 J1.
In contrast to the invention completed in 47661, the seabird structure was diversified by positively distributing the island fineness of the resulting mixed spun fibers.

In other words, the mixed spun fiber obtained by the above-mentioned method and apparatus proposed by the present inventor has the following characteristics: the average number of islands per filament, the island fineness, and By ensuring that the number of islands and island fineness between filaments hardly change in distribution,
The resulting mixed spun fibers had improved uniformity by eliminating unevenness in the mixing ratio among the filaments. The present invention has a diverse sea-island structure and is a mixed spun fiber that is more useful.In order to obtain a sea-island fiber whose island fineness has an arbitrary distribution within the filament, the island fineness within the filament is adjusted. This was completed as a result of extensive research in order to create a device that can accurately and easily control distribution without reducing the fiber uniformity of the resulting mixed spun fibers.

That is, in the mixing spinning device of the present invention, three or more groove-shaped polymer inlets and outlets are bored in parallel to each other on each of the upper and lower surfaces, and the grooves corresponding to the upper and lower surfaces have a large number of grooves communicating with each other. A plate connected by a communicating hole, has a recessed part on the upper surface for receiving the polymer flow from the A plate, and has a large number of polymer inflow holes in the center of the recessed part, and the hole row consisting of these holes is The holes are drilled parallel to the length direction of the grooves in the plate, and the holes have an arbitrary distribution of hole diameters or hole lengths between the holes, and the upper surface receives the polymer flow from the B plate. , a plurality of recesses smaller than the number of holes drilled in the recesses of plate B, and spinnerets each having one discharge hole are provided in the center of the recesses.

Next, the mixing source in the mixing spinning device of the present invention. Explain the principle. In the present invention, mixing of polymer streams means:
Multi-layering made by 1A plate followed by B plate, 2A
Division and flow velocity distribution created by the polymer inflow holes in plate B following plate 3, and spinneret recesses following plate 3B. The result of a series of three operations on the fast-regulated set, A
When the polymer flow that flows into the plate as a single component flow for each of A and B becomes a polymer flow that flows out from the discharge hole of the spinneret, the B component is present in the A component (or the A component is present in the B component). ) This refers to a change to a state in which the water is dispersed as a large number of microcurrents, a so-called sea-island state.

Next, an example of the mixing device of the present invention and its polymer flow, that is, the mixing mechanism will be explained with reference to the drawings.

FIG. 1 is a plan view of plate A according to the present invention as seen from the outlet side, and FIG. 2 is a cross-sectional view of FIG. 1 taken along line A-A''.

1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11 are A
This is a polymer outlet in the form of an annular groove that is concentrically (parallel to each other) drilled in the plate.
″, 5″, 6′, ding, 8′, 9′, 1″, 1″ is 1, 2
, 3, 4, 5, 6, 7, 8, 9, 10, 1 No. 1. In this figure, the groove-shaped outflow port is 11.
The figure shows the case where two holes are drilled.

The annular groove-shaped outlet and inlet are penetrated by a large number of pores 1'', 2'', . . . that connect them. Fig. 3 is a plan view of plate B, and Fig. 4 is a sectional view taken along the line B-B'' in Fig. 3. 12 is a concave portion of plate B, and its shape is shown in Fig. 3. , but is not limited to that shown in FIG.

13, 14, 15, 16... are inlet holes drilled so that the hole rows coincide with the circumferential direction formed by the groove-shaped outlet of the plate A, and 13, 14, 15. , 16 have pore diameters that change in order and are different from each other, and if these are considered as one set, in this example, there are 12 sets of 13, 14, 15, and 16 that have the same structure and the same pore diameter and move. A total of 48 holes have been drilled.

13″, 14″, 15″, 16″ are 13, 14, 15,
16, and the set of 4 is 1
There are two sets, or a total of 48 holes.

The lengths of the pores are all equal in this example. FIG. 5 is a plan view of the spinneret, and FIG. 6 is a C of the spinneret.
It is a sectional view taken along the line -C''.

Reference numeral 17 indicates recesses of the spinneret, and in this example, there are 12 recesses throughout the spinneret at positions corresponding to the outlets of the inlet holes of plate B.
One of the recesses is formed so as to receive four exits of the inlet holes of the B plate, that is, a set of different holes whose diameters are changed in order.

Its shape is not limited to those shown in FIGS. 5 and 6, and other shapes such as cylindrical, conical, etc. can be used. Reference numeral 16 indicates a discharge hole formed in the recessed portion of the spinneret, which communicates with a nozzle orifice 19 .

In these drawings, many parts having the same structure and symmetrical parts are omitted to the extent that it does not impair the explanation. The flow of polymer in this mixing device will be explained in the case of a polymer flow of two components A and b.

The two polymer flows of component a and component b, respectively, metered by a gear pump are 1″, 2″, 3″, 4″, 5″, 6
″, 7″, 8″, 9″, 1″, 1″ enter the polymer inflow hole next to each other 1, 2, 3, 4, 5, 6, 7, 8, 9
, 10, 11 concentric. The a component and the b component are extruded from the annular groove-shaped polymer inflow port drilled into the recess of the B plate and flow side by side with 6 layers of the a component and 5 layers of the b component, that is, a composite flow of the A and bll layers. enter.

At this time, generally the component with a large number of layers, that is, the a component in this example, becomes the sea component. The composite surface of the composite flow is the direction in which the holes bored in the center of the B plate recess are arranged, that is, the circumferential direction of the B plate. This composite flow becomes the A, bll layer, which corresponds to the number of groove-shaped outflow ports in the A plate, and the number of the outflow ports is increased so that each component polymer is passed through every other groove-shaped flow. If the flow is allowed to flow out from the outlet, it is possible to easily and reliably send a composite flow having the same number of layers as the number of groove-shaped outlets to the B plate portion.
The 11-layer polymer flow that entered the B plate recess 12 in Fig. 4 is 1
The polymer is supplied to the polymer inflow holes of the B plate arranged in a circumferential manner, with a total of 48 pore groups having the same structure as the pore groups, consisting of four holes 3, 14, 15, and 16, and 13'', 14″, 1
A pore group consisting of 4 holes of 5″ and 16″ and 12 holes with the same structure.
The polymer flows out from a total of 48 polymer outflow holes in the set of pore groups.

The polymer flow that has passed through the A plate is multilayered and divided by the B plate, and a continuous flow distribution is provided between the divided polymer streams. Next, the polymer trickle formed after passing through the B plate flows out into the 12 spinneret recesses provided under the B plate through a pore group consisting of 4 pores with different pore diameters. Polymer trickles flow precisely into each. That is, they gather in the spinneret recesses in a highly regulated manner, and are then discharged from the discharge holes drilled one by one in the spinneret recesses. That is, according to the present invention, when the polymer trickle from the B plate is separated on the upper surface of the spinneret, it is highly regulated by the plurality of recesses on the upper surface of the spinneret and guided to one discharge hole. A single polymer trickle never splits and flows into the spinneret's discharge holes. It is considered that the polymer streams are efficiently mixed by passing the two component polymers A and b through the apparatus of the present invention as described above.
How the mixing can be controlled in the mixing device of the present invention will be described below. Regarding the number of islands, A of the number of layers Sl2 of one component (island component) when multi-layered is 1.
The number of divisions made by the B plate following the plate, that is, the total number of pores in the pore groups drilled in the B plate recesses, Ul3. The number of spinneret recesses, that is, the number of nozzle orifices in the spinneret. Letting I be the number of fine currents flowing through the hole, that is, the number of islands in the sea-island state, it is thought that the relationship shown in equation (1) holds between I and S, U, and V.

Next, in the case of the devices shown in Figures 1 to 6, S = 5, U = 4
8, ■ = 12, and the pores of plate B are composed of pore clusters consisting of pores with four different diameters, in which case the sea component is actually made of polyethylene (high pressure method), and the island component is was mixed and spun as polyethylene terephthalate. In this example, the pore lengths of plate B are equal as shown in FIG. As a result, each hole has exactly 12 islands.
, and the island fineness also has an exact distribution of four levels of size (
A mixed spun multifilament with a sea-island structure (one stage consists of five islands) was obtained. In this example, the number of filaments is 1
It is 2. This completely coincided with the calculated value obtained by substituting (1) for S, U, and V. That is, the degree of mixing, that is, the number of islands, and the sea-island condition, that is, the island fineness distribution, of the mixed spun fibers obtained by the apparatus of the Mokura invention are determined by the pore diameters of the pores in one set of pore groups of the S, U, V, and B plates. It can be seen that it can be controlled freely by arbitrarily selecting the ratio. Therefore, it can be seen that this mixing control is possible extremely easily and over a wide range, and that the performance and method of the mixing spinning apparatus of the present invention are excellent. Further, the progress of mixing in the mixing device of the present invention will be shown.
In the A board of 1, each component of Ab is a component = 6 layers of sea component, b
Component = 5 layers of island component, and these are pasted side by side and flow into the concave part of plate B following plate A, and the hole row is located in the center of the concave part of plate B in the circumferential direction of the annular groove of plate A. It is divided into 48 fine streams by 48 polymer inflow holes drilled so that

These 48 fine flows consisting of 6 layers of the a component and 5 layers of the b component pass through the pores at different flow rate ratios depending on the pore diameter ratio of the pores of the B plate, and each flow enters the inflow hole of the B plate. The 12 spinneret recesses leading from the outlet to the bottom of the B plate gather in a highly regulated manner. At this time, immediately after the 48 microflows flow into the pores in the annular groove of the B plate, they are stuck side by side with 6 layers of the a component and 5 layers of the b component, but when they flow out, the phases of the A and b component polymers are combined. When one component is dispersed in the other due to differences in solubility, cohesive force, and flow behavior, a state in which component b is dispersed in component a) begins to change to a sea-island state, and B In the recess at the top of the spinneret following the plate, it forms an almost perfect sea-island structure and merges in a highly regulated manner. In this case, the 48 fine streams flowing out from the outlet of the inflow hole of the B plate are composed of 12 sets of 4 flows with different flow rates, and each fine stream is composed of 5 b components each. 4 flows out from each spinneret outlet because it has a dispersed phase consisting of
Each of the eight microstreams has a dispersed phase consisting of three B components, so in one recess of each spinneret, the microstreams flowing out from the outlet of the inflow hole of the B plate are one set of streams with different flow rates. In other words, the polymer flow flowing into each discharge hole of the spinneret is made up of 5 x 4 = 20 (5 x 4 = 20) dispersed particles, each of which has the same size and has a size distribution of 4 stages. It has an island facies. In order to achieve such mixing, the mixing apparatus of the present invention only needs to incorporate three main plates, plate 1A, plate 2B, and spinneret 3, into the nozzle bag in this order. In the previous explanation, we have shown an example in which the island fineness distribution is controlled by selecting the pore diameter ratio of the pores in the B plate. The pore diameters of the pores are kept the same and the pore length ratio of the pores is selected. For example, by partially cutting out each pore on the bottom side of plate B and changing the pore length of each pore, Also, by giving the pore length ratio between the pores, which will be explained later! As shown in Example 2, the island fineness distribution can be controlled.

The mixing device of the present invention is based on the principles previously proposed by the present inventors in Japanese Patent Application Laid-Open No. 50-36717 and Japanese Patent Application Laid-open No. 50-71909.
No., Patent Application No. 1983-64735, Patent Application No. 1983-1476
No. 61, etc. 3, in that the chemical and physical properties of the polymer components to be mixed at any stage are fully considered and utilized, but the present invention The number of structural plates used for this purpose is 3 including the spinneret.
The previously proposed method has made it possible to achieve simplification and miniaturization compared to the 5 to 6 constituent plates in the case of 4 devices, and in addition, the island fineness of the resulting mixed spun fibers has been reduced. This made it possible to accurately and easily control the distribution within the filament, thereby expanding the scope of mixed spinning technology.

Furthermore, it is thought that it is possible to obtain sea-island fibers with a controlled island fineness distribution as obtained by the present invention using the multi-core core-to-sheath spinning apparatus proposed in Japanese Patent Publication No. 44-183.
In that case, the part through which the core component polymer flows is made up of a large number of thin tubes, and the spinneret part with such thin tubes requires not only engineering but also maintenance and maintenance compared to a normal spinneret. This is considered extremely labor-intensive and is a big difference from the fact that the equipment parts of the present invention can be handled in exactly the same way as a conventional spinneret.

A proposal aimed at this improvement was published in JP-A-49-19111.
This is a method in which the thin tubes used in the 1911 Japanese Patent Publication Trowel are all replaced with pores made in the plate.
It is clear that a branch channel or narrow channel for the sheath component surrounding the pore is required for each pore, which increases the size of the device, and the space is not used efficiently. However, with the device of the present invention, the number of islands can be easily and accurately controlled by arbitrarily changing S, V, and U, and the island fineness can be distributed by simply changing the pore diameter and length of the pores in the B plate. can be given,
Furthermore, the number of main constituent plates is three, making it extremely compact.

This is because the present invention attempts to achieve the desired mixing state by fully utilizing the chemical and physical properties of the polymers to be mixed when they are melted, and the apparatus has been simplified as described above. , maintenance, and maintenance can be handled in the same way as ordinary melt spinnerets, and there are no special considerations or difficulties. Furthermore, one way to bring about changes in the sea-island structure of mixed spun fibers has been thought to be to create a distribution of island fineness.
In that case, there were no concrete proposals on how to achieve this in a sufficiently controlled manner.

In mixed spinning, creating a distribution in island fineness means making the sea-island structure non-uniform, which often results in a decrease in fiber uniformity and may not result in a fiber that is of practical use, or may not be stable. This is probably because it has been thought that it is impossible to spin such yarn. In fact, similar results were obtained in many cases in the studies conducted by the present inventors, but from such studies, the present inventors conducted an operation to give a distribution to the island fineness as in the present invention. This is done by dividing the bonded polymer flow through the fine holes of plate B and giving a flow distribution, and the resulting fine polymer flow with a flow rate distribution is highly regulated and collected in each nozzle recess, and then spun out from the nozzle discharge hole. Therefore, for the first time, it has become possible to achieve stable mixing and to spin mixed spun fibers with an island fineness distribution with good fiber uniformity without causing any fluctuations in the discharge amount from each spinneret and the mixing component ratio. be. This is because even if plate B causes a flow rate distribution, the entire flow of the two component bonded polymers will have a flow rate distribution, and there will be no change in the component polymers that make up the bonded polymer, so the mixing ratio will be This is probably because it is completely stable. The combination of polymers used for spinning in the mixed spinning device of the present invention may include any known combination of spinnable polymers.
It is a species or a combination of two or more kinds of polymers.

Typical examples of polymers include polyolefins such as polyethylene and polypropylene, atactic or isotactic polystyrene, alkyl- and halogen-substituted polystyrenes, polyamides such as 6-nylon and 6,6-nylon, polyesters such as polyethylene terephthalate, and polymethyl methacrylate. Polymethacrylic acid ester, polyvinyl acetal acetalized with various aldehydes, polyvinyl alcohol,
Various low molecular substances for polyvinyl halides such as polyvinyl chloride, polyvinylidene halides such as polyacrylonitrile, polyvinylidene chloride, copolymers of various condensed or polymerized low molecular substances, or various high molecular substances. These include grafted polymers.

In the mixed spun fiber obtained by the mixed spinning apparatus of the present invention, the island component phase (hereinafter referred to as "island phase") has an average distribution of 0.05 to 3 deniers.

Therefore, by dissolving or extracting the sea component phase (hereinafter referred to as "sea phase"), extremely fine fibers that are completely impossible to be produced by normal spinning (including mixed spinning) can be obtained.
In other words, a mixed fiber aggregate is obtained in which fibers with a fineness on the order of 1/0 denier are mixed with fibers with a fineness on the order of 0.1 to 3 deniers. Such a fiber aggregate is very useful as a material for napped type artificial leather.

In other words, by arbitrarily changing the composition of the mixed fibers, that is, the fineness and mixing ratio, different types of products can be produced, for example,
The material fibers can be optimally used for deerskin-like artificial leather, suede-like artificial leather, velor-like artificial leather, buckskin-like artificial leather, etc. Even if an attempt was made to obtain the above-mentioned artificial leather by blending raw cotton of ordinary mixed spun fibers with different constituent island finenesses instead of such mixed fibers, the appearance and wind Especially in the state of piloerection,
The condition of the surface fluff was completely poor.
The reason for this is thought to be that in the mixed cotton type, there is a limit to the mixing of fine fibers with different finenesses, and it is impossible to achieve a uniform state of mixing fine fibers like mixed fibers. Furthermore, the mixed fibers obtained by the apparatus and method of the present invention have very good fiber uniformity even in the presence of sea-island structures, which is considered impossible with conventional mixed spun fibers, that is, fibers with a sea-island structure. It is fully possible to handle it as a filament fiber for textiles. EXAMPLES Next, the present invention will be described in more detail with reference to examples, but the present invention is not limited to these examples. In addition, the intrinsic viscosity [η] (d'
/g) is measured using a mixed solvent of phenolnitetrachloroethane (1:1) at 30°C.

Also, the relative viscosity of nylon 6 is 1/100 of that of nylon 6.
(g/r!Ll) dissolved in 96% H2SO4 at a concentration of 30
Measured at °C.

What is the melt index of polyethylene? JIS-K67
6O.

・Example 1 Polyethylene terephthalate with an intrinsic viscosity of 0.68 and high-pressure low-density polyethylene with a melt index of 20 were melt-extruded using separate extruders, weighed with a gear pump, and then extruded at a liquid delivery ratio of 60 Wtj% polyethylene terephthalate and 40 Wt% polyethylene. Introduce and mix into the invention mixing device.

As shown in Figure 1, the mixing device has a plate A with 11 concentric annular groove polymer outlet holes, and as shown in Figure 3, a plate with 48 polymer outlet holes in the center of the recess. The four pores are composed of 12 groups of pores, and the pore diameter ratio of the four pores in one group of pores is 1:
1.19:1.38:1.56 and all hole lengths are equal, and spinneret recess 1 having the structure as shown in Fig. 6.
A spinneret with 12 No. 7 holes installed in the above order was used. Of course, the pore groups of one set of B plates are arranged to correspond to one spinneret recess. Polyethylene terephthalate, which is an island component, is introduced into plate A through five annular grooves, i.e., 2″, 4″, and 4″ in Fig. 1.
6'', 8'', 1'', polyethylene as a sea component was made into four annular grooves 1'', 3'', 5'', 7'', 9'', 1''.

Therefore, in this example, S (i.e., the number of layers of island components in plate A) = 5, and U (number of pores drilled in the concave portion of plate B) = 4.
&V (number of base orifices)=12. For spinning, the spindle temperature was 280°C, the number of spindle holes = 12, and the discharge amount = 41.
．． The winding speed was set at 5 g/min and a winding speed of 750 rr1/min. The cooling air was applied to the spun yarn with a cross current at a wind speed of 0.2 to 0.7 m/Sec between 2 and 30 cm below the spinneret. The obtained mixed spun yarn was stretched 4 times with a roller plate type drawing machine, and
/12fi1 drawn yarn was obtained.

The resulting mixed spun fiber has an island phase composed of polyethylene terephthalate in all the holes of the spindle, in each of the 12 holes in this example, 2 C@, that is, 2 C@ per filament. Microscopic observation of the cross-section of the fibers revealed that the 2C@ island phase had a distribution of 4 levels, with each 5 pieces having equal fineness. Furthermore, the fineness of the island phase, which is distributed in four stages, was determined from microscopic observation of the fiber cross section.
0.083dr, 0.194dr, 0.334dr, 0
．． Five island facies of 639c1r were distributed in each area. From this result, the change in the fineness of the island phase is approximately 4.5 times the pore diameter of the B plate.
I found that it changed in proportion to the hotness. This shows that the flow rate distribution of the polymer flow in plate B is the same as the fineness distribution of the island phase of the mixed spun fibers, and furthermore, the flow rate distribution is free from pressure loss due to friction in a general laminar flow of fluid. It can be seen that the flow rate of the Hagen-Boiseuille equation, which is a theoretical equation, is given accurately, almost in agreement with the relationship proportional to the fourth power of the diameter of the hole j.

The actual spinning was repeated in continuous operation for 10 to 14 days. During this period, there was no yarn breakage due to dropped screws, and the spinning condition was good. In addition, the mixed state of the mixed spun fibers was completely stable during spinning. The mixed state, ie, the sea-island state, was extremely stable with no change observed in the number of islands, island shape, and island fineness distribution from the start of spinning to the end of spinning.
The uniformity of the drawn yarn obtained was determined by a normal test using a Worcester evenness tester.
%=about 0.5 to 0.8%, which was good. Example 2 The same polymer used in Example 1 was introduced into the mixing device of the present invention at the same feed ratio and mixed.

The mixing device was the same as that used in Example 1, and the four pores in one set of pores on plate B had a pore length ratio of 1:2.1:3.8:6.
．． 0 and the pore diameters were all the same, but the same ones were used. The spinning conditions and stretching conditions were exactly the same as in Example 1.

In order to investigate the sea-island structure of the obtained blended spun fibers, microscopic observation of the cross section of the fibers was carried out.

In this case as well, 1) island phases made of polyethylene terephthalate were present in the filament in a fineness distribution of 4 stages with 5 pieces per 2α gourd stage. The fineness of one island phase at each stage is 0.107 dr, 0.194 dr, and 0.37 dr, respectively.
8 dr and 0.571 dr, and this distribution is the ratio of the pore length of the B plate. This shows that the flow rate distribution of the polymer flow in the B plate results in the fineness distribution of the island phase of the mixed spun fibers, which is based on the Hagen-Boiseuille theoretical formula that accounts for pressure loss due to friction in general laminar flow of fluids. It can be seen that the flow rate in the equation is given accurately, almost in agreement with the relationship in which it is proportional to the hole length.

Actually, spinning was carried out in the same manner as in Example 1, but the spinning condition, the stability of the mixing state, and the uniformity of the obtained mixed spun fibers were as good as in Example 1. Example 3 Nylon 6 with relative viscosity 2.7 and melt index 2
0 high-pressure low-density polyethylene was melt-extruded separately, weighed with a gear pump so that 6% nylon and 6% polyethylene were mixed, introduced into the same inventive mixing device as used in Example 1, and mixed. I did this.

The spinning was carried out under the same conditions as in Example 1 except that the spindle temperature was 250 to 260°C. Stretching was also carried out under the same conditions as in Example 1. The obtained mixed spun fiber has an island phase of nylon 6 in all the holes of the base, in each of the 12 holes in this example, 20 fI1, that is, an island phase per filament.

The nod pieces were distributed in 4 stages with equal fineness of 5 islands. The fineness of the island phase distributed in four stages is 0.08 dr.
, 0.19dr, 0.33dr, and 0.65dr, and the relationship between the island fineness distribution and the pore diameter distribution of the B plate pores was the same as in Example 1. .

The actual spinning and drawing conditions were as good as in Example 1 where the island phase was polyethylene terephthalate.

The uniformity of the obtained fibers was good without any change, and the mixed fine-grained fibers consisting of island phases of nylon 6 from which polyethylene had been extracted and removed became nylon 6 filaments with sufficient commercial value. Example 4 Plate A as shown in Fig. 1 has 11 concentric annular polymer outflow ports, and a plate as shown in Fig. 3 has a 3C41 polymer outflow hole in the center of the recess. The pores are made up of a set of pore groups, and the pore diameter ratio of the three pores in one pore group is 1:1.3:1.6.
The experiment was carried out using the mixing apparatus of the present invention in which a spinneret having 12 spinneret recesses 17 having the structure as shown in FIG. Mixed spinning and drawing was carried out using the same polymer, spinning conditions, and drawing conditions as in Example 1.

Of course, the pore groups of one set of B plates are arranged to correspond to one spinneret recess.

The mixed spun fiber obtained in this example had an island phase consisting of polyethylene terephthalate in any of the 12 holes.
Each filament had b number of cavities, and each of the five islands had an equal fineness and had a three-stage distribution. Furthermore, the fineness of the island phase distributed in three stages is 0.
1 dr, 0.32 dr, 0.83 (1r island facies is 5 each
It was distributed by books. In this case as well, the relationship between the fineness distribution of the island phase and the pore size distribution of the B plate pores is almost the same as in Example 1, and the fineness distribution of the island phase is approximately 4.5 mm larger than the pore size of the B plate pores.
It was proportional to the fifth power.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a plan view of an example of the A plate according to the present invention, and FIG. 2 is a cross-sectional view taken along line AA'' in FIG. 1.

Claims (1)

[Claims] 1. In a mixing spinning device for obtaining sea-island fibers having an arbitrary distribution of fineness of island components, (1) three or more groove-shaped polymer inlets and outlets are bored in parallel to each other on each of the upper and lower surfaces, and A plate in which grooves corresponding to the upper and lower surfaces are connected by a large number of communication holes that communicate the grooves; polymer inflow holes, and the holes have an arbitrary distribution of hole diameter or hole length among the holes so that the hole array consisting of these holes is parallel to the length direction of the groove of the A plate. and (3) have a plurality of recesses on the upper surface smaller than the number of holes drilled in the recesses of the B board, each of which receives the polymer flow from the B board, and one recess in the center of each of the recesses. 1. A mixing spinning device comprising a spinneret having several discharge holes.