JPH04163307A - Mixed melt spinning device - Google Patents

Abstract

PURPOSE:To prevent a mixed component polymer from being attached to a wall face of flow channel by forming a sheath core conjugate flow comprising a mixed component polymer flow as core and a main component polymer flow not containing pigment as sheath. CONSTITUTION:A mixed component polymer flow B is made to flow from an inlet nozzle 34 of a feeder 20 toward approximately the central part of a flow channel section of a main component polymer flow A. A sheath core conjugate flow comprising the mixed component polymer flow as core and the main component polymer flow not containing pigment as sheath is formed and the mixed component polymer will not be attached to a wall part in a flow channel toward a stationary blender.

Description

DETAILED DESCRIPTION OF THE INVENTION <Industrial Application Field> The present invention relates to an apparatus for mixing and spinning molten polymers, and particularly to an apparatus for mixing and spinning two types of polymers by melting them.

<Prior Art> As a mixed melt spinning device that mixes two types of molten polymers at a certain ratio and extrudes the mixture from a plurality of spinnerets to form fibers, a device disclosed in Japanese Patent Publication No. 2-4684 has conventionally been used. be. This will be explained with reference to FIG.

Polymer A (main component polymer) melted in the main extruder 1 passes through the main line 2, is divided into many parts by branch piping 3, and is guided to the feeder 9.

The polymer B (mixed component polymer) melted in the other subexiter 10 is also divided into the same number of branch pipes 3 by the distribution pipe 12, and each is divided into the second metering pump 11.
After being metered at , it is guided to the feeder 9 .

Polymer A and polymer B are combined in this feeder 9, followed by a static kneader 5, a first metering pump 6, and a static kneader 7.
, spinning pack 8, and other mixed spinning lines.

As described above, when mixing two types of polymers to form fibers, it is said to be difficult to mix each polymer uniformly. In other words, if the difference in the mixing ratio of Polymer A and Polymer B is large, the polymer flow tends to be biased in the cross-sectional direction of the polymer pipe after merging, and even when passing through the static kneader, Polymers A and B are uniform. May not be mixed. In order to solve this problem, this device uses polymer A,
The feeder 9 that merges B is designed as follows. The structure of the feeder 9 will be explained with reference to FIG.

An annular supply chamber 9b communicating with the distribution pipe 12 is arranged around the main pipe 9a communicating with the branch pipe 3, and this supply chamber 9
A plurality of (in this example, four) inflow nozzles 9c are provided that penetrate from b to the same cross-sectional position of the main pipe 9a while maintaining angles at equal intervals.

According to this feeder 9, since the polymer B to be mixed with the polymer A is simultaneously fed from different directions by the plurality of inflow nozzles 9c, the area occupied by the polymer B in the cross-sectional direction of the flow path after merging is reduced. When the number of effective divisions by the subsequent static kneader 5 increases significantly and the difference in kneading ratio is extremely large, for example, even when the mixing ratio of polymer A and polymer B is 100:1 or less, the number of elements is relatively small. A very homogeneous mixture can be obtained using a static kneader with a small amount of heat.

<Problems to be Solved by the Invention> As described above, in the conventional device, the inhomogeneity of mixing of two types of polymers is solved by devising the feeder 9. 9, the following new problems arise.

That is, since polymer B merges from the annular supply chamber 9b arranged around the main pipe 9a through which polymer A flows, when looking at the cross section of the flow path after merging, polymer A is in the center and polymer B is in the center. It looks like it flows around the outer periphery. In other words, the main component Polymer A is the core, and the mixed component Polymer B
A core-sheath composite flow is formed with the core and sheath as a sheath, flows through the main pipe 9a, and heads toward the static kneader 5. Generally, polymer B, which is a mixed component, contains pigments for dyeing fibers, etc., and when polymer B circulates as a sheath, it passes through the main pipe in the process up to the static kneader 5. The pigment may adhere to the inner wall of 9a.

Therefore, there is a problem in that a specified amount of pigment is not supplied to the subsequent mixing and spinning line, resulting in color irregularities in the formed fibers.

This problem can be solved by the device mentioned as a conventional example (Japanese Patent Publication No. 2-46
This is not limited to the device described in Publication No. 84), but in a device that merges the mixed component polymers from the outer circumferential direction of the flow path of the main component polymer, even if both polymers meet at one point, it is sufficient to This is a possible problem.

In addition to the above-mentioned problems, the conventional device has another problem.

This is because, after the polymer B is divided by the distribution pipe 12, the discharge amount of each polymer B to be supplied to the supply device 9 is measured by the second metering pump 11.

When spinning ordinary filaments, the amount of polymer A discharged per divided spindle is approximately 5 to 100 [g/min], and when the mixing ratio of polymer B is 5%, the amount of discharged is 0. The amount is extremely small at 25-5 [g/min]. When measuring such a minute amount, it is difficult to obtain sufficient measurement accuracy with a commonly used metering pump of simple structure such as a gear pump. If there is a problem in measurement accuracy and a specified amount of polymer B is not supplied, the spinning state will become unstable and problems such as yarn breakage will occur.

This invention was made in view of the above circumstances, and is a melting method that can prevent the pigment contained in Polymer B from adhering to the flow channel wall surface and stabilize the measurement accuracy of Polymer B. The purpose is to provide a mixed spinning device.

<Means for Solving the Problems> In order to achieve the above object, the present invention has the following configuration.

[I] The first invention involves kneading a main component polymer stream supplied from a main extruder and a mixed component polymer stream supplied from a sub-extruder via a second metering pump in a static kneader. In a melt-mixing spinning device that spins out mixed fibers through a spinning pack after metering the synthetic polymer with a first metering pump, the main component is placed in the middle of a pipe connecting the main extruder and the static kneader. The present invention is characterized in that a feeder is provided with an inflow nozzle that opens toward substantially the center of a cross section of the flow path of the polymer flow, and the inflow nozzle is communicatively connected to the second metering pump.

+Il] The second invention is the melt-mixing yarn-protecting device according to the above [11], in which one main extruder is provided with one feeder and one static kneader, and the first metering pump and the metering pump are provided with one feeder and one static kneader. a synthetic line and a plurality of lines (υ) consisting of a yarn protection pack connected to There is.

<Effect> ” - The effect of the configuration is as follows.

[11 In the first invention, the mixed component polymer flow sent from the supply line flows through the inflow nozzle of the feeder toward the substantially center of the flow path cross section of the main component polymer flow. As a result, a core-sheath composite flow is formed in which the mixed component polymer is the core and the main component polymer is the sheath, and the flow heads toward the static kneader. That is, since the mixed component polymer flows while being coated with the main component polymer over its outer periphery, the mixed component polymer does not adhere to the wall surface of the channel.

[11] The second invention is a branch point of a plurality of synthetic lines;
The feeder and the static kneader are arranged in this order between the extruder (in other words, the feeder and the static kneader are arranged before the main component polymer is branched). The number of supply lines for the mixed component polymer flow connected in communication with Since the total amount of supply from each supply line is measured, not the amount from each individual supply line, the separate unit becomes large and sufficient measurement accuracy is ensured.

<Example> Embodiments of the present invention will be described below with reference to the drawings.

FIG. 1 shows an example of the arrangement of an apparatus for melting and mixing and spinning two types of polymers.

In FIG. 1, reference numeral 1 denotes a main extruder for the main component polymer (hereinafter referred to as polymer A). Head to the 24th. The mixed component polymer (hereinafter referred to as polymer B) melt-extruded by the other sub-extruder 10 is metered by the second metering pump 12 and then reaches the feeder 20 via the sub-pipe 21, where polymer A After merging with , it heads to a static kneader 24 via a merging path 23 . As the main and sub-extruders 1 and 10, for example, a known melt extruder such as a screw 2 can be used. Further, as the static kneader 24, various known static kneaders can be used, but in particular, an element having spiral blades inserted in two passages and an intermediate chamber following this, 90 of the above elements
Arranged at different angles (for example, JP 513618
The one disclosed in Publication No. 2) is effective. The synthetic polymers of polymer A and polymer B kneaded in the static kneader 24 were divided into many parts in the distribution pipe 25, and then the first il quantity pump 6, static kneader 7, spinning pack 8, etc. were arranged in sequence. A plurality of mixed spinning lines 15 (this mixed spinning line 15
corresponds to the synthesis line) and is spun.

In addition, the symbols 27 and 28 in the figure indicate Ex1 to Ruder1. IO
29 is a screw motor for extruding the melted polymer A and polymer B into the main pipe 2 and the sub pipe 21; 29 is a pressure gauge that measures the pressure on the polymer extruded into the main pipe 2;
0 is a control circuit that controls the screw rotation motor 27 so that the extrusion pressure to the polymer becomes a specified pressure based on the measurement data measured by the pressure gauge 29, and 31 is its electric signal path.

The feeder 20 is a component that represents the characteristics of the present invention, and is a component that represents the characteristics of the present invention.
Polymer A flowing down through the auxiliary pipe 21 and Polymer B flowing through the sub pipe 21 are merged, and Polymer B is used as the core, and Polymer A
This forms a core-sheath composite flow with the sheath as the sheath. Since a plurality of embodiments are possible for such a supply device 20, examples thereof will be described below with reference to FIGS. 2 to 4.

(a) The first embodiment is a feeder 2 shown in FIG.
0, the perspective view is shown in the same figure (a), and the longitudinal cross-sectional view is shown in (b).

A supply chamber 33 is integrally connected to the polymer A outlet of the main pipe 32 communicating with the main pipe 2 . The supply chamber 33 has a hollow disk shape, and has an outer circumferential portion (with some thickness remaining and a depressed central portion) having a width approximately equal to the pipe diameter of the main pipe 32. There is an inlet passage 36 with a thickness of d between the two.

A communication pipe 35 that communicates with the confluence channel 23 (see FIG. 1) is connected to the center of the bottom surface of the inflow channel 36.
An inflow nozzle 34 in the form of a thin tube is communicated with the center of the upper surface of the inflow path 36 corresponding to the center of the inflow channel 36 . This inflow nozzle 34
is connected to a secondary pipe 21 through which polymer B flows.

According to this feeder 20, the polymer A that has flowed down from the main pipe 2 to the main pipe line 32 circulates around the outer circumference of the supply chamber 33, passes through the inflow passage 36, and flows from the outer circumference of the communication pipe 35 into the communication pipe. It flows into 35. That is, the thickness f of the outer peripheral part
Compared to this, the thickness d of the inflow channel 36 is set to be considerably thinner (it is thinner due to the depression), so the polymer A circulates in the outer periphery where the flow resistance is small, and then enters the inflow channel 36 where the flow resistance is large. Head towards. On the other hand, the polymer B flowing through the sub pipe 21 is transferred from the inflow nozzle 34 to the inflow path 3 of the supply chamber 33.
6 from a direction perpendicular to the center of the connecting pipe 35.
flowing down the center of Therefore, the composite flow flowing from the communication pipe 35 through the confluence channel 23 becomes a core-sheath composite flow in which polymer B is the core and polymer A is the sheath, and the polymer B remains stationary with its outer periphery covered by the polymer A. Kneader 2
Head to 4.

(b) The second embodiment is a feeder 2 shown in FIG.
0, the same figure (a) shows a perspective view, and (b) shows its longitudinal cross-sectional view.

It is equipped with a disc-shaped chamber 37 that integrally connects the main pipe line 32 in the center, and a plurality of chambers (preferably 2 to 6, four in the drawing) are installed along the circumferential direction of the chamber 37. A pipe 38 (an example of which is shown) is connected in a hanging state. The other ends of these tubes 38 communicate with the outer periphery of the supply chamber 33. This supply chamber 33 is similar to the one described in (a), and has an inflow passage 36 sunken in the center, and on the upper and lower surfaces of the inflow passage 36, an inflow nozzle 34 and a communication pipe 35 are provided as in (a). are connected.

According to this feeder 20, polymer A flowing down from the main pipe 32 is diffused within the chamber 37, divided by the individual pipes 38, flows into the supply chamber 33 from the outer periphery of the supply chamber 33, and enters the communication pipe 35. The water flows down the outer circumference of the water and heads toward the confluence channel 23. On the other hand, the polymer B flowing from the sub pipe 21 flows from the inflow nozzle 34 in a direction perpendicular to the center of the inflow path 36 of the supply chamber 33, and flows down the center of the communication pipe 35. Therefore, a core-sheath composite flow is formed in which the polymer B is the core and the polymer A is the sheath, and flows from the communication pipe 35 through the confluence path 23 to the static kneader 24.

In this way, since the flow of polymer A is dispersed and flows into the communication pipe 35 from the outer peripheral part of the supply chamber 33, the thickness of the inflow path 36 is There is no need to set d very thin.

(c) The third embodiment is the feeder 2 shown in FIG.
0, the same figure (a) shows a perspective view, and (b) shows its longitudinal cross-sectional view.

A hollow disc-shaped chamber 39 is integrally connected to the main pipe line 32, and a communication pipe 35 is connected to the center of the bottom surface of the chamber 39 (lower side in the drawing). The inflow nozzle 34 enters the chamber 3 from the center of the upper surface of the chamber 39.
9, and this inflow nozzle 34 is inserted into the communication pipe 3.
It is inserted halfway through 5.

The wall thickness of the inflow nozzle 34 is set to be thicker than those described in (a) and (b), and the gap between the outer circumferential surface of the inflow nozzle 34 and the inner circumferential surface of the communication pipe 35 is minute. I have to.

According to this supply device 20, from the main pipe line 32 to the chamber 3
The polymer A that has flowed down into the chamber 39 is diffused throughout the entire area inside the chamber 39, flows down through the gap between the inflow nozzle 34 and the communication pipe 35, and heads toward the confluence channel 23. In other words, the flow resistance in this gap is considerably larger than the flow resistance during diffusion within the chamber 39. Therefore, the flow of polymer A that has flowed into the chamber 39 is regulated by this gap, and after being diffused throughout the entire area inside the chamber 39, it flows down from the gap to the communication pipe 35 and circulates around the outer periphery of the communication pipe 35. It becomes a covering flow. On the other hand, the polymer B flowing through the sub pipe 21 passes through the inflow nozzle 34 and joins the flow from the center of the communication pipe 35 to the polymer. In this way, a core-sheath composite flow is formed in which Polymer B is the core and Polymer 8 is the sheath.

In order to more effectively restrict the flow to the polymer, the following modifications can be made.

In other words, instead of making the gap between the inflow nozzle 34 and the communication pipe 35 minute, it is possible to create a connection as shown in FIG.
An annular portion 4 in which a plurality of holes 40 are formed in the tube axis direction of the m tube 35
1 may be provided in a part of the gap portion. In other words, since this hole 40 serves as a flow outlet for the polymer A, the flow resistance to the communication pipe 35 can be increased compared to the flow resistance Q when it diffuses inside the chamber 39, and the flow resistance to the polymer A can be increased. Flow regulation can be performed more effectively.

Such a feeder 20 is connected to a plurality of mixed spinning lines 15.
As shown in FIG. 1, when the auxiliary pipe 21 through which the polymer I3 flows is arranged in front of the branching point of the plurality of mixed spinning lines 15, only one auxiliary pipe 21 is used. be able to. Therefore, the second 4-volume pump 12 that measures the discharge amount of the polymer B does not need to measure minute amounts of individual polymer B divided according to the number of mixing spinning lines 15 as in the conventional method. In other words,
The total amount of polymer B to be divided is 91,
The metering unit of the second metering pump 12 becomes large.

The above-mentioned first and second metering pumps 6 and 12 used in the present invention are known ones, such as gear pumps,
A plunger pump, diaphragm pump, etc. can be used.

An experimental example in which spinning was actually performed using the above-described mixed melt spinning apparatus will be described below.

Polyethylene terephthalate was melted as Polymer A, and a master chip of polyethylene terephthalate containing a pigment and a dispersant was melted as Polymer B. The respective polymer streams were mixed at a ratio of 19:1. When they were merged and spun using the apparatus of the present invention, a stable spinning state was obtained with no yarn breakage, and a uniform spun-dyed yarn without color spots was obtained. As the feeder 20, the one shown in -1- (a) was used, and as the static kneader 24, a known fluid mixer (disclosed in Japanese Patent Publication No. 36182/1982) was used.

<Effects of the Invention> As is clear from the explanation below, the mixed melt spinning apparatus of the present invention has the following effects.

(1) In the first invention, since the feeder forms a core-sheath composite flow in which the mixed component polymer flow is the core and the main component polymer flow is the sheath, the mixed component polymer is covered with the main component polymer. As a result, the mixed component polymer does not get stuck on the inner wall of the flow path toward the static kneader. Therefore, the pigment contained in this mixed component polymer is fed in a defined amount to the subsequent synthesis line, so that fibers without color mottle can be spun.

(2) In the second invention, the above-mentioned feeder and static kneader are provided before the branch point of the synthesis line of the mixing melt-spinning apparatus equipped with a plurality of synthesis lines, so that the above-mentioned feeder and static kneader are communicatively connected to the feeder. The number of feed lines for the mixed component polymer stream is also singular. Therefore, the mixed component polymer metered by the second metering pump is not the amount of the individual feed lines divided according to the number of synthesis lines as in the conventional method, but the total amount of the feed amounts of the individual feed lines. Since it is measured as 4
The quantity unit υ" becomes larger, and even a metering pump with a simple structure such as a gear pump can ensure sufficient metering accuracy, and the spinning state can be stabilized.

(3) First. In both of the second inventions, since the supply line for the mixed component polymer stream can always be configured as a single unit, the adhesion of the mixed component polymer to the flow channel wall surface in the supply line is less likely to occur, compared to an apparatus equipped with a plurality of supply lines. It is also possible to suppress as much as possible, and the equipment can be simplified, so it is possible to reduce equipment costs.

[Brief explanation of drawings]

FIGS. 1 to 4 relate to a first embodiment of the present invention.
The figure shows an example of the arrangement of each part of the device, FIG. 2(a) is a perspective view of the feeder, FIG. 3(a) is a longitudinal sectional view thereof, and FIG. 3(a) is a perspective view of another feeder (b) is its vertical cross-sectional view, the fourth
Figure (a) is also a perspective view of another supply device, (b) is a longitudinal cross-sectional view thereof, and (C) is a cross-sectional view of the annular portion. 5 and 6 relate to a conventional device, FIG. 5 is a diagram showing an example of the arrangement of each component of the conventional device, and FIG. 6 is a perspective view of a conventional feeder. ■...Main extruder 2...Main pipe 6...First metering pump death/
・Spinning pack 10... Sub-extruder 12...
・Second metering pump 15...Mixing spinning line (synthesis line) 20...Supplier 24...Static kneader 34...Inflow nozzle Applicant Azuma Shi Co., Ltd. Company agent Patent attorney Sugitani study flow

Claims (2)

[Claims] (1) The main component polymer stream supplied from the main extruder and the mixed component polymer stream supplied from the sub-extruder via the second metering pump are kneaded in a static kneader, and the kneaded synthetic polymer is In a melt-mixing spinning device that spins mixed fibers through a spinning pack after metering with a metering pump No. 1, a flow path cross section of the main component polymer flow is installed in the middle of a pipe connecting the main extruder and the static kneader. 1. A melt-mixing spinning apparatus comprising: a feeder having an inflow nozzle that opens toward a substantially central portion of the melt-mixing spinning apparatus; and the inflow nozzle is communicatively connected to the second metering pump. (2) One main extruder is provided with one feeder and one stationary kneader, and a plurality of lines are provided including a synthesis line consisting of a first metering pump and a yarn protection pack connected to the metering pump, and 2. The melt-mixing yarn-protecting device according to claim 1, wherein one stationary kneader and the first metering pump of each of the synthesis lines are connected to each other through a distribution pipe.