JPS6042283B2 - Mixed spinning equipment - Google Patents

Description

【発明の詳細な説明】 本発明は２種以上の多成分ポリマー流を混合して紡糸
する装置に関するもので、任意な混合状態とりわけ島成
分の繊度に任意な分布を有する海島繊維を、より安定か
つすぐれた繊維均斉度でえる混合紡糸装置に関するもの
である。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.

混合紡糸技術は合成繊維の改質等を目的とし従来から
よく知られている。BACKGROUND ART Mixed spinning technology has been well known for the purpose of modifying synthetic fibers.

混合紡糸で最も一般的な方法としては、成分ポリマー
をチップ状態で混合し、これを溶融押出機を用いて紡糸
するものである。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.

これは最も簡便かつ経済的な方法および装置と考えられ
、最も広く利用されている。しかし、この方法、装置で
えられる非相溶性ポリマーの混合状態すなわち海島状態
にはコントロール可能な範囲に、また混合可能なポリマ
ーの組合せも制限がある。 本発明はこのような従来の
混合紡糸技術に鑑みてなされたものであり、目的とする
ところは、任意な繊度分布の島を有する海島繊維を海島
全体としては極めて均斉度よく安定にえる混合紡糸方法
およびそのような海島状態を極めて効率よくとる事がで
き、しかも構造が簡単である混合装置を提供せんとする
ものであつて、本発明者が特開昭５０−３６７１７、特
開昭５０−７１９０９、特願昭５０−６４７３５、特願
昭５０−１３２２５１およびとりわけ特願昭５０一Ｊ１
４７６６１に完成した発明に対して、えられる混合紡糸
繊維の島繊度に積極的に分布をもたせる事によつて海鳥
構造の多様化を行なつたものである。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.

つまり、本発明者がすてに提案した前記の方法及び装
置でえられる混合紡糸繊維は、１つの口金から吐出され
たヤーン全体の平均として求めたフィラメント当りの平
均島数、島繊度、さらにはフィラメント相互の島数およ
び島繊度はほとんど分布変動しない様にする事により、
えられる混合紡糸繊維はフィラメント相互で混合比率ム
ラ等の発生が解消されて均斉度の向上がなされた。本発
明は多様性に富んだ海島構造を有し、より利用価値のあ
る混合紡糸繊維であるところの島繊度がフィラメント内
で任意な分布をもつ海島繊維をえるに際し、フィラメン
ト内での島繊度を正確かつ容易に制御して分布させる事
が可能な装置を、えられる混合紡糸繊維の繊維均斉度を
全く低下せしめる事なくえるために鋭意検討を重ねた結
果完成したものである。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.

すなわち、本発明の混合紡糸装置は上面及び下面夫々に
３個以上の溝状ポリマー流入口及び流出口が相互に平行
に穿設されかつ該上面及び下面に対応する溝が溝を連通
する多数の連通孔により連結されるＡ板、上面にＡ板か
らのポリマー流を受け入れる凹部を有し、かつ該凹部の
中心部に多数のポリマー流入孔をもち、しかもそれらの
孔からなる孔列が前記Ａ板の溝の長さ方向と平行になる
ように、さらに当該孔は孔間で孔径又は孔長が任意の分
布をもつて穿設されたＢ板、及び上面にＢ板からのポリ
マー流を受け入れる、Ｂ板凹部に穿設された孔数より少
ない複数の凹部を有し、かつ該凹部の中心部にはそれぞ
れ１個の吐出孔を有する紡糸口金を設けたものである。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.

次に、本発明の混合紡糸装置における混合の原．理につ
いて説明する。本発明においてポリマー流の混合とは、
１Ａ板とそれに続くＢ板によつてなされる多層化、２Ａ
板に続くＢ板のポリマー流入孔によつてなされる分割と
流速分布付与、３Ｂ板に続く紡糸口金凹部．でなされる
高速に規制された集合、の３個の一連の操作の結果、Ａ
板にＡ，ｂ各々単一の成分の流れとして流入したポリマ
ー流が紡糸口金の吐出孔より流出するポリマー流となつ
たときは、ａ成分中にｂ成分が（またはｂ成分中にａ成
分が）多数・個の微細流として分散した状態いわゆる海
島状態へと変化することをいうものである。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.

次に本発明の混合装置の１例とそのポリマーの流れ、つ
まり混合機構について図面によつて説明する。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.

第１図は本発明にいうＡ板の流出口側から望んだ平面図
であり、第２図は第１図をＡ−Ａ″線で切断したときの
断面図である。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はＡ
板に同心円状（相互に平行な状態）に穿設された円環溝
状をしたポリマー流出口であり、１″，２″，３″，４
″，５″，６′，丁，８′，９′，１『，１「は１，２
，３，４，５，６，７，８，９，１０，１ノ１に対応し
たポリマー流入口であり、この図は溝状の流出口が１１
個穿設されている場合を示している。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.

該円環溝状の流出口と流入口は各々それらを連結する多
数の細孔１″，２″・・・・で貫通されている。第３図
はＢ板の平面図であり第４図は第３図・のＢ−Ｂ″線で
切断したときの断面図である。１２は当該Ｂ板の凹部で
ありその形状は第３図、第４図に限定されるものではな
い。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・・・・・・は孔列が前記Ａ板
の溝状流出口のつくる円周方向と一致するように穿設さ
れた流入孔”であつて１３，１４，１５，１６の４個は
その細孔径が順に変化して相互に異なるもので、これを
１組とみなすとこの例では１３，１４，１５，１６と同
構造、同孔径の細五』動く１２組、合計で４８ホール穿
設されている。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″は１３，１４，１５，
１６に対応した当該流入孔の出口であり、４個の組が１
２組つまり合計で４８ホール穿設されている。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.

細孔の孔長はこの例では全て等しくなつている。第５図
は紡糸口金の平面図であり、第６図は当該紡糸口金のＣ
−Ｃ″線で切断したときの断面図である。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''.

１７は当該紡糸口金の凹部であり、この例ては紡糸口金
全体に１２個がＢ板の流入孔の出口に対応した位置に、
該凹部の１個がＢ板の流入孔の出口４個つまり孔径か順
に変化して相互に異なる１組ずつを受け入れる様に穿設
されている。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.

その形状は第５図、第６図に限定されるものでなく、他
の形たとえば円管状、円錐状等が利用される。１６は当
該紡糸口金凹部に穿設された吐出孔で、これらはノズル
オリフィス１９へ連通している。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 .

なお、これらの図面において多数の同構造の部分や対称
部分は、説明を害しない程度に省略した部分がある。こ
の混合装置中のポリマーの流れをＡ，ｂ２成分のポリマ
ー流の場合について説明する。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.

各々、ギアポンプで計量されたａ成分、ｂ成分の２つの
ポリマー流はＡ板の１″，２″，３″，４″，５″，６
″，７″，８″，９″，１『，１「のポリマー流入ロへ
となり合せで入り１，２，３，４，５，６，７，８，９
，１０，１１の同円心状．に穿設された円環溝をしたポ
リマー流入口より押出されてＢ板凹部へａ成分とｂ成分
がサイドバイサイドに各々ａ成分６層、ｂ成分５層ずつ
、すなわちＡ，ｂｌｌ層の複合流として入る。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.

このとき一般に層数の多い成分すなわちこの例ではａ成
分が，海成分となる。該複合流の複合面はＢ板凹部の中
心部に穿設された孔の配列方向すなわちＢ板の円周方向
となる。この複合流はＡ，ｂｌｌ層となるが、Ａ板の溝
状の流出口の数に対応するものであつて、当該流出口の
数を増加せしめ各成分ポリマーを１つおきの溝状の流出
口より流出せしめれば、容易に溝状の流出口の数と同数
層の複合流を極めて確実にＢ板部へ送ることができる。
第４図のＢ板凹部１２へ入つた１１層のポリマー流は１
３，１４，１５，１６の４ホールからなる，細孔群と同
構造の１２組の細孔群合計４８個の円周状に配列された
Ｂ板のポリマー流入孔へ供給され、１３″，１４″，１
５″，１６″の４ホールからなる細孔群と同構造の１２
組の細孔群合計４８個のポリマー流出孔より流出する。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.

Ａ板を通過したポリマー流はＢ板により多層化と分割お
よび分割されたポリマー細流間に流連分布の付与が行な
われる。次にＢ板を通過して形成されたポリマー細流は
Ｂ板の下に設けられた１２個の紡糸口金凹部へ４個の異
なる細孔径の細孔からなる細孔群より流出した４個ずつ
のポリマー細流が各々へ正確に流入する。すなわち紡糸
口金凹部において高度に規制されて集合し、つづいて当
該紡糸口金凹部に１個ずつ穿設された吐出孔から吐出さ
れる。すなわち、本発明によればＢ板からのポリマー細
流を紡糸口金の上面で分流するに際し、紡糸口金上面の
複数の凹部により高度に規制して１個の吐出孔へ導くか
ら、Ｂ板よりの１つのポリマー細流が決して紡糸口金の
複数の吐出孔に分れて流れ込むことがない。以上のよう
にＡ，ｂ２成分ポリマーが本発明装置を通過することに
よつてポリマー流が効率よく混合されると考えられる。
本発明の混合装置における混合の制御がいかにすれば可
能となるかについて次に記す。島数については１の多層
化したときの一方の成分（島成分）の層の数Ｓｌ２のＡ
板に続くＢ板によつてなされる分割の数すなわちＢ板凹
部に穿設された細孔群の合計の細孔数Ｕｌ３紡糸口金凹
部の数すなわち口金のノズルオリフィス数■とすると紡
糸口金の細孔を流れる微細流の数つまり海島状態中の島
数をＩとすると、ＩとＳ，Ｕ，Ｖの間には（１）式の様
な関係が成立すると考えられる。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.

次に図１〜図６で示す装置の場合つまりＳ＝５，Ｕ＝４
８，■＝１２であつて、Ｂ板の細孔は４個の異なる孔径
の細孔からなる細孔群丘組からなつている場合において
実際に海成分をポリエチレン（高圧法）とし、島成分を
ポリエチレンテレフタレートとして混合及び紡糸を行な
つた。この例でＢ板の細孔長は第４図に示すように等し
くなつている。その結果、各ホールの島数が正確に１２
個であり、島繊度も又正確に大小４段階の分布をもつ（
１段階は島数５本からなる）海島構造の混合紡糸マルチ
フィラメントがえられた。この例でフィラメント数は１
２である。これはＳ，Ｕ，Ｖを（１）に代人して求めら
れた計算値に全く一致していた。すなわち、杢発明の装
置によつてえられる混合紡糸繊維の混合の程度すなわち
島数、海島状態つまり島繊度分布はＳ，Ｕ，Ｖ及びＢ板
の１組の細孔群中の細孔の孔径比を任意に選択する事に
よつて自在に制御てきる事がわかる。したがつて、この
混合制御は極めて容易かつ広い範囲で可能であり、本発
明混合紡糸装置の性能及び方法の優れている事がわかる
。さらに本発明の混合装置の混合の進行について示す。
１のＡ板でＡｂ各々の成分゜はａ成分＝海成分６層、ｂ
成分＝島成分５層とな・つて、これがサイドバイサイド
にはり合わせられてＡ板に続くＢ板凹部へ流入し、Ｂ板
凹部の中心部にその孔列がＡ板の円環状溝の円周方向と
なるように穿設された４８個のポリマー流入孔で４８個
の微細な流れに分割される。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

このａ成分６層、ｂ成ノ分５層ずつからなる４８個の微
細な流れはＢ板の細孔の孔径比に応じた異なる流量比で
細孔を通過して、それぞれＢ板の流入孔出口からＢ板の
下に続く１２個の紡糸口金凹部て高度に規制されて集合
する。このとき４８個の微細流はＢ板円環溝中の細孔に
流入した直後はａ成分６層、ｂ成分５層ずつのサイドバ
イサイドにはり合わされているが、流出時にはＡ，ｂ成
分ポリマーの相溶性、凝集力、流動挙動の差によつて一
方の成分中に他方の成分が分散した状態にの場合、ａ成
分中にｂ成分が分散した状態）、すなわち海島状態へと
変化を始め、Ｂ板につづく紡糸口金上部の凹部でほぼ完
全な海島構造となつて高度に規制されて合流する。この
場合、Ｂ板の流入孔の出口から流出する４８個の微細流
は４個の流量の異なる流れの組が１２個から構成されて
おり、さらに１個の微細流は各々５個のｂ成分からなる
分散相をもつているので各紡糸口金出口から流出する４
８個の微細流は各々３個のｂ成分からなる分散相をもつ
ているので各紡糸口金の１つの凹部にはＢ板の流入孔の
出口から流出する微細流は流量の異なる流れの１組つま
り４個が正確に流入するのて紡糸口金の各吐出孔に流れ
るポリマー流は５個ずつが同じ大きさで４段階の大きさ
の分布をもつ５×４＝２０（個）の分散相つまり島相を
有することとなる。この様な混合を実現するのに本発明
混合装置は１Ａ板、２Ｂ板、３紡糸口金の主要なプレー
ト３枚をこの順序でノズルバックへ組込むだけでよいの
である。尚これまての説明では、島繊度分布を制御する
のに、Ｂ板での細孔の孔径比を選択することによ，つて
行なう例で示したが、Ｂ板での細孔群中の細孔の孔径は
等しくしておき、細孔の孔長比を選択する、即ち、例え
ば、Ｂ板下面側を各細孔ごとに部分的に切除して各細孔
の孔長を違え、それにより細孔間て孔長比を与えること
によつても、後述！する実施例２にも示すように、島繊
度分布が制御できるものである。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.

本発明の混合装置は原理的には本発明者らが先に提案し
た特開昭５０−３６７１７号、特開昭５０−７１９０９
号、特願昭５０−６４７３５号、特願昭５０−１４７６
６１号等３と任意の段階まて混合しようとするポリマー
成分の化学的物理的性質を十分に考慮し、それを利用し
ている点では全く同一てあるが、本発明は上述の如く混
合のために用いる構造プレート数が紡糸口金を含めて３
枚とこれまて提案してきた方法、４装置の場合の構成プ
レート数５〜６枚に比べて簡素化、小型化の実現を可能
にしたのに、加えてえられる混合紡糸繊維の島繊度をフ
ィラメント内で正確かつ容易に制御して分布させる事を
可能にしたもので、その結果として混合紡糸技術範囲の
拡大がなされた。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.

さらに特公昭４４−１８３的号等で提案されている多芯
々鞘紡糸装置で本発明でえられるような制御された島繊
度分布をもつ海島繊維をえる事も可能と考えられるが、
その場合には芯成分ポリマーを流す部分は多数の細管か
ら構成されており、この様な細管を有する口金部分は工
作するのはもちろん保守、整備する事も通常の紡糸口金
のそれに比フして極めて多く労力を必要とするものと考
えられ、本発明の装置部品が通常の紡糸口金と全く同様
な取扱いのできるのとは大きな違いである。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.

この改良をねらつた提案が特開昭４９−１９１１１号、
特開昭４９−１９１１鏝でなされているところの・細管
をすべてプレートに穿つた細孔に代えたものであるが、
細孔をとりかこむ鞘成分のための分流路、細流路が各細
孔毎に必要となつて装置は大型化してしまい、スペース
の利用の効率がよくないのは明らかである。しかし、本
発明の装置では、Ｓ，Ｖ，Ｕを任意にかえる事で容易に
かつ正確に島数のコントロールができ又Ｂ板の細孔の孔
径と孔長を任意させるだけで島繊度に分布が付与でき、
しかも主要な構成プレート枚数は３枚で極めてコンパク
トである。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.

これは本発明は実際に混合に供するポリマーの溶融時の
化学的、物理的性質を十分に利用して目的とする混合状
態を実現しようとしたのて装置は上述の如く簡単化でき
たもので、保守、整備は通常の溶融紡糸口金と同様な取
扱いができ、特別な配慮や困難は全くない。さらに従来
から混合紡糸繊維の海島構造に変化をもたらす事の１つ
として島繊度に分布をもたせる事が考えられていたが、
その場合十分に制御された状態で実現する方法の具体的
提案はなかつた。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.

それは混合紡糸において島繊度に分布をたらす事は海島
構造を不均一にする事を意味し、これは多くの場合繊維
均斉度の低下を生じせしめ実用性のある繊維とはならな
いとか安定にその様な紡糸をする事は不可能であるとさ
れてきたからであろう。事実、本発明者の検討において
も、多くの場合に同様な結果となつたが、その様な検討
の中から本発明者らは、本発明のように島繊度に分布を
与えるための操作をＢ板の細孔ての接合ポリマー流の分
割および流量分布付与で行ない、えられる流量分布のあ
る微細ポリマー流を各口金凹部へ高度に規制して集合し
てこれを口金吐出孔より紡出するならば各口金からの吐
出量と混合成分比率に全く変動を生じる事なく、安定な
混合の実現と繊維均斉度の良好な島繊度に分布を有する
混合紡糸繊維の紡糸が初めて可能となつたのである。こ
れはＢ板て流量分布を生じせしめても２成分の接合ポリ
マー流全体が流量分布をもつのであつて接合ポリマーを
構成する各成分ポリマー相互には何らの変化も与える事
がないので混合比率が全く安定しているためと考えられ
る。本発明の混合紡糸装置において紡糸に供されるポリ
マーの組合わせとしては、公知なあらゆる紡糸可能な２
種または２種以上のポリマーからなる組合わせである。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.

ポリマーの代表例としてはポリエチレンおよびポリプロ
ピレンの如きポリオレフィン、アタクチツクまたはアイ
ソタクチックなポリスチレン、アルキルそしてハロゲン
置換のポリスチレン、６ナイロンおよび６，６ナイロン
の如きポリアミド、ポリエチレンテレフタレートの如き
ポリエステル、ポリメチルメタクリレートの如きポリメ
タアクリル酸エステル、各種アルデヒドにてアセタール
化したポリビニルアセタール、ポリビニルアルコール、
ポリ塩化ビニルの如きポリハロゲン化ビニル、ポリアク
リロニトリル、ポリ塩化ビニリデンの如きポリハロゲン
化ビニリデン、あるいは各種の縮合系又は重合系低分子
物質の共重合物又は各種高分子物質に対し、各種低分子
物質をグラフトしたグラフトポリマーなどである。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.

本発明の混合紡糸装置でえられた混合紡糸繊維は、島成
分の相（以下島相とする）が平均０．０５〜３デニール
の間で分布をもつものである。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.

したがつて、海成分の相（以下海相とする）を溶解又は
抽出除去することによつて通常の紡糸（混合紡糸を含む
）てはえる事が全く不可能と思われる極めて微細な１０
０分の１デニールのオーダー繊度の繊維から微細な繊度
つまり０．１〜３デニール程度までの繊維が混合された
、言いかえると混繊された繊維集合体がえられる。この
ような繊維集合体は立毛タイプの人工皮革用素材として
非常に有用なものである。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.

すなわち、混繊の構成つまり繊度及び混合比率を任意に
変化せしめる事により、異なるタイプの製品たとえば、
鹿皮調人工皮革、スウエード調人工皮革、ベロア調人工
皮革、バックスキン調人工皮革等それぞれに最適となる
素材繊維とする事ができる。このような混繊された混合
繊維の代りとして構成島繊度が異なる通常の混合紡糸繊
維の原綿を混綿する事によつて上述の様な人工皮革をえ
ようと試みても、いずれも外観、風合とくに立毛状態、
表面毛羽の状態が全く粗悪なものにしかならなかつた。
その原因として混綿タイプでは繊度の異なる微細繊維の
混りに限界があつて混繊された混合繊維の様に均一な微
細繊維の混合状態の実現が不可能なためであると考えら
れる。また本発明の装置、方法でえられる混合繊維は海
島共存する状態においても繊維均斉度が非常に良好であ
ることから、従来の混合紡糸繊維つまり海島構造をもつ
た繊維においては不可能とされていた織物用フィラメン
ト繊維として取扱いが十分に可能である。次に本発明を
実施例を示してより具体的に説明するが、本発明はこれ
ら記載例に限定されるものではない。なお、本発明にい
うポリエチレンテレフタレートの極限粘度〔η〕（ｄ′
／ｇ）とは３０゜Ｃのフエノールニテトラクロルエタン
（１：１）の混合溶媒で測定したものである。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.

また、６ナイロンの相対粘度は６ナイロンを１／１００
（ｇ／ｒ！Ｌｌ）の濃度９６％Ｈ２ＳＯ４に溶解し３０
゜Ｃで測定したものである。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.

ポリエチレンのメルトインデックスとはＪＩＳ一Ｋ６７
６Ｏにしたがつて測定したものてある。What is the melt index of polyethylene? JIS-K67
6O.

・実施例１固有粘度０．６８のポリエチレンテレフタレ
ートとメルトインデックス２０の高圧法低密度ポリエチ
レンを別々の押出機により溶融押出し、ギアポンプで計
量してポリエチレンテレフタレート６０Ｗｔｊ％、ポリ
エチレン４０Ｗｔ％の送液比で本発明混合装置に導入し
混合する。・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.

混合装置は第１図のようにＡ板が１１個の同心円をなし
た円環状溝ポリマー流出口をもつものと、第３図のよう
なり板でその凹部の中心部に４８個のポリマー流出孔を
穿設したフもので当該４陥の細孔は１２組の細孔群から
なつていて１組の細孔群中の４個の細孔の孔径比は１：
１．１９：１．３８：１．５６となつていて、孔長は全
て等しいものと、第６図のような構造の紡糸口金凹部１
７を１２個穿設した紡糸口金とを上記の様な順に設置し
たものを用いた。もちろん１組のＢ板の細孔群は１つの
紡糸口金凹部に対応するように配置させてある。Ａ板へ
のポリマーの導入は島成分であるポリエチレンテレフタ
レートが５個の円環状溝すなわち第１図の２″，４″，
６″，８″，１『に、海成分であるポリエチレンが４個
の円環状溝１″，３″，５″，７″，９″，１「になさ
れた。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''.

したがつて、本実施例てはＳ（すなわちＡ板での島成分
の層数）＝５、Ｕ（Ｂ板凹部に穿設された細孔数）＝４
＆Ｖ（口金オリフィス数）＝１２である。紡糸は口金温
度は２８０℃とし、口金ホール数＝１２、吐出量＝４１
．５ｇ／Ｍｉｎ、捲取速度７５０ｒｒ１／Ｍｉｎに設定
して行なつた。冷却風は口金下２〜３０ｃｍの間を風速
０．２〜０．７ｍ／Ｓｅｃで紡出糸条にクロスカレント
でふきつける様にした。えられた混合紡糸原糸はローラ
ープレート方式の延伸機で４倍に延伸し、１５０（１ｒ
／１２ｆｉ１の延伸糸をえた。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.

えられた混合紡糸繊維はポリエチレンテレフタレートか
らなる島相を口金全ホール、この例では１２ホールの各
ホールにおいていずれも２咋すなわち１フィラメント当
り２Ｃ＠有している。そして、２Ｃ＠の島相は５個ずつ
が等しい繊度で４段階の分布をもつていることが繊維断
面の顕微鏡観察で認められた。さらに４段階に分布する
島相の繊度を繊維断面の顕微鏡観察から求めたところ、
０．０８３ｄｒ，０．１９４ｄｒ，０．３３４ｄｒ，０
．６３９ｃ１ｒの島相が各々５本ずつ分布していた。こ
の結果から島相の繊度の変化はＢ板の細孔径のほぼ４．
辣に比例して変化している事が分つた。これはＢ板にお
けるポリマー流の流量分布の付与がえられる混合紡糸繊
維の島相の繊度分布となる事を示しており、しかも流量
分布は一般的な流体の層流における摩擦による圧損等を
あられす理論式であるハーゲン・ボアズイユの式の流量
が孔ｊ径の４乗に比例する関係とほぼ一致して、正確に
与えられている事が分る。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.

実際の紡糸は１０〜１４日間の連続運転を繰返して行な
つた。その期間中ビス落ちによる断糸は全くなく紡糸調
子は良好であつた。また、混合紡糸繊維の混合状態は紡
糸中全クく安定であつた。混合状態すなわち海島状態は
、島数、島形状島繊度分布は、紡糸開始から紡糸の終る
まで全く変化が認められず極めて安定なものであつた。
またえられた延伸糸の均斉度は、ウースターのイーブン
ネステスターを用いたノーマルテストで求めたところＵ
％＝０．５〜０．８％程度であり良好であつた。実施例
２ 実施例１において用いたと同一のポリマーを同一の送液
比で本発明混合装置に導入し混合する。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.

混合装置は実施例１で用いたものと、Ｂ板の１組の細孔
群中の４個の細孔は孔長の比が１：２．１：３．８：６
．０となつていて孔径は全て等しくなつていフる以外全
く同一のものを用いた。紡糸条件および延伸条件は実施
例１と全く同一条件として行なつた。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.

えられた混合紡糸繊維の海島構造を調べるため繊維断面
の顕微鏡観察を行なつた。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.

この場合も１）フィラメント内にはポリエチレンテレフ
タレートからなる島相が２α瓢１段階５個ずつて４段階
の繊度分布て存在していた。各段階の１個の島相繊度は
、それぞれ０．１０７ｄｒ，０．１９４ｄｒ，０．３７
８ｄｒ，０．５７１ｄｒとなつていて、この分布はＢ板
の細孔長・の比になつている。Ｂ板におけるポリマー流
の流量分布付与がやはり混合紡糸繊維の島相の繊度分布
となる事を示していて、一般的な流体の層流における摩
擦による圧損等をあられす理論式であるハーゲン・ボア
ズイユの式の流量が孔長に比例する関係とほぼ一致して
、正確に与えられている事が分かる。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.

実際紡糸は実施例１と同様に行なつたが、紡糸調子、混
合状態の安定性さらにえられた混合紡糸繊維の均斉度は
実施例１の場合と差違なく良好なものであつた。実施例
３相対粘度２．７の６ナイロンとメルトインデックス２
０の高圧法低密度ポリエチレンを別々に溶融押出し、ギ
アポンプで６ナイロン印憇％、ポリエチレン旬憇％とな
るように計量して実施例１で用いたと全く同一の本発明
混合装置に導入し、混合を行なつた。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.

紡糸は口金温度を２５０〜２６０℃とする以外は実施例
１と同じ条件で行なつた。延伸も実施例１と同一条件で
行なつた。えられた混合紡糸繊維は６ナイロンからなる
島相を口金全ホール、この例では１２ホールの各ホール
において２０ｆＩ１すなわち１フィラメント当り頷個有
している。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.

そして頷個は島相が５ずつ等しい繊度で４段階に分布し
ていた。４段階に分布する島相の繊度は、０．０８ｄｒ
，０．１９ｄｒ，０．３３ｄｒ，０．６５ｄｒの島相か
各々５本すつ分布していて、島繊度分布とＢ板細孔の孔
径の分布との関係は実施例１と同様になつた。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. .

実際の紡糸延伸の状態を実施例１の島相がポリエチレン
テレフタレートの場合と全く変ることなく良好なもので
あつた。The actual spinning and drawing conditions were as good as in Example 1 where the island phase was polyethylene terephthalate.

えられた繊維の均斉度も何ら変化なく良好でポリエチレ
ンを抽出除去した６ナイロンの島相からなる混繊された
微細繊度繊維は十分に商品価値のある６ナイロンフィラ
メントとなつた。実施例４ 第１図のようなＡ板が１１個の同心円をなした円環状ポ
リマー流出口をもつものと、第３図のようなり板でその
凹部の中心部に３Ｃ４１のポリマー流出孔を穿設したも
ので当該あ個の細孔は帛組の細孔群からなつていて１組
の細孔群中の３個の細孔の孔径比は１：１．３：１．６
となつていて孔長は全て等しいものと、第６図のような
構造の紡糸口金凹部１７を１２個穿設した紡糸口金とを
上記の様な順に設置した本発明混合装置を用いて、実施
例１と全く同一のポリマー、紡糸条件、延伸条件で混合
紡糸延伸を実施した。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.

もちろん、１組のＢ板の細孔群は１つの紡糸口金凹部に
対応するように配置させる。Of course, the pore groups of one set of B plates are arranged to correspond to one spinneret recess.

この例でえられた混合紡糸繊維はポリエチレンテレフタ
レートからなる島相を１２ホールのいずれにおいても、
１陥すなわち１フィラメント当りｂ個有していて、そし
て托個の島相が５個ずつが等しい繊度で３段階の分布を
もつていた。さらに３段階に分布する島相の繊度は０．
１ｄｒ，０．３２ｄｒ，０．８３（１ｒの島相が各々５
本ずつ分布していた。この場合も島相の繊度分布とＢ板
細孔の孔径の分布との関係は実施例１の場合とほとんど
相違なく、島相の繊度分布はＢ板細孔の孔径のほぼ４．
５乗に比例していた。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.

図面の簡単な説明第１図は本発明にいうＡ板の１例の平
面図であり、第２図は第１図のＡ−Ａ″線での断面図で
ある。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)

【特許請求の範囲】[Claims] １ 島成分の繊度に任意の分布を有する海島繊維を得る
混合紡糸装置において、（１）上面及び下面それぞれに
３個以上の溝状ポリマー流入口及び流出口が相互に平行
に穿設され、かつ該上面及び下面に対応する溝が溝を連
通する多数の連通孔により連結されるＡ板、（２）上面
にＡ板からのポリマー流を受け入れる凹部を有し、かつ
該凹部の中心部に多数のポリマー流入孔をもち、しかも
それらの孔からなる孔列が前記Ａ板の溝の長さ方向と平
行になるように、さらに当該孔は孔間で孔径又は孔長が
任意の分布をもつて穿設されたＢ板、及び（３）上面に
Ｂ板からのポリマー流を受け入れる、Ｂ板凹部に穿設さ
れた孔数より少ない複数の凹部を有しかつ該凹部の中心
部にはそれぞれ１個の吐出孔を有する紡糸口金からなる
ことを特徴とする混合紡糸装置。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.