CN111074358A - Method for preparing polyethylene fiber by double-metering conveying method - Google Patents
Method for preparing polyethylene fiber by double-metering conveying method Download PDFInfo
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- CN111074358A CN111074358A CN201911408968.7A CN201911408968A CN111074358A CN 111074358 A CN111074358 A CN 111074358A CN 201911408968 A CN201911408968 A CN 201911408968A CN 111074358 A CN111074358 A CN 111074358A
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/06—Wet spinning methods
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D10/00—Physical treatment of artificial filaments or the like during manufacture, i.e. during a continuous production process before the filaments have been collected
- D01D10/02—Heat treatment
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D10/00—Physical treatment of artificial filaments or the like during manufacture, i.e. during a continuous production process before the filaments have been collected
- D01D10/06—Washing or drying
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/04—Dry spinning methods
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/12—Stretch-spinning methods
- D01D5/14—Stretch-spinning methods with flowing liquid or gaseous stretching media, e.g. solution-blowing
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/02—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds
- D01F6/04—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds from polyolefins
Abstract
Discloses a method for preparing polyethylene fibers by a double-metering conveying method, belonging to the technical field of polyethylene fiber preparation. Which comprises the following steps: selecting ultrahigh molecular weight polyethylene resin with viscosity average molecular weight of more than 400 ten thousand as raw material polyethylene resin; dissolving raw material polyethylene resin in an organic solvent to prepare spinning solution; the spinning solution sequentially passes through a first metering pump, a static mixer, a second metering pump and a spinning assembly of a spinning box body, and is extruded from spinneret orifices to form spinning trickle; cooling and solidifying the spinning trickle to obtain gel tows; removing the organic solvent from the gel tows through a drying hot box to obtain dry-state precursor; and (3) performing multi-stage post-spinning drafting on the dry precursor to obtain the polyethylene fiber. The polyethylene fiber prepared by the method has high breaking strength and initial modulus, and low CV value of breaking strength.
Description
Technical Field
The invention relates to the technical field of polyethylene fiber preparation, in particular to a method for preparing polyethylene fibers by a double-metering conveying method.
Background
At present, ultra-high molecular weight polyethylene (UHMWPE) fibers are mostly prepared from polyethylene having a flexible macromolecular chain by solution spinning, and are also called high-strength high-modulus polyethylene fibers, high-orientation polyethylene fibers, and high-performance polyethylene fibers. The fiber is a fiber material with the highest known strength-to-mass ratio, has various excellent characteristics of high strength, high modulus, light weight (the density is less than 1), high energy absorption, chemical stability, water resistance, light resistance, fatigue resistance, wear resistance, bending resistance, low temperature resistance, easy transmission of electric waves and the like, and is called as three high-performance fibers together with carbon fiber and aramid fiber. The UHMWPE fiber can be used for producing body armor, bulletproof helmets, stab-resistant clothes, motor armor, mooring ropes, net cages for marine fishery, medical materials, clothes, sports equipment and the like. The fiber is mixed with other fibers for use, and has wide prospect in the aspects of being used as impact-resistant and shock-absorbing materials and high-performance light composite materials.
Disclosure of Invention
In view of the above, the present invention provides a method for preparing polyethylene fiber by a dual metering conveying method, and the polyethylene fiber prepared by the method has high breaking strength and initial modulus, and low CV value of breaking strength, so that the method is more practical.
In order to achieve the purpose, the technical scheme of the method for preparing the polyethylene fiber by the double metering conveying method is as follows:
the method for preparing the polyethylene fiber by the double-metering conveying method comprises the following steps:
selecting ultrahigh molecular weight polyethylene resin with viscosity average molecular weight of more than 400 ten thousand as raw material polyethylene resin;
dissolving the raw material polyethylene resin in an organic solvent to prepare a spinning solution, wherein the mass percentage content of the raw material polyethylene resin in the spinning solution ranges from 4% to 7%, and the organic solvent is one or a mixture of more of decalin, paraffin oil, white oil and xylene; the intrinsic viscosity of the spinning solution ranges from 9dl/g to 29 dl/g;
the spinning solution sequentially passes through a first metering pump, a static mixer, a second metering pump and a spinning assembly of a spinning manifold, and is extruded from a spinneret orifice to form a spinning trickle, wherein the value range of pressure difference between the first metering pump and the second metering pump is 1MPa-10MPa, and the value range of pressure in the spinning assembly is 0.1MPa-4 MPa;
cooling and solidifying the spinning trickle to obtain gel tows;
removing the organic solvent from the gel tows through a drying hot box to obtain dry-state precursor;
and carrying out multi-stage post-spinning drafting on the dry precursor to obtain the polyethylene fiber.
The invention can be further realized by adopting the following technical measures.
Preferably, in the process of cooling and solidifying the spinning fine flow to obtain the gel tow, the cooling method is realized by a liquid coagulating bath, a side blowing method or a circular blowing method, wherein,
the temperature of the liquid coagulating bath is lower than the temperature of the spinning trickle, and the value range is 20-200 ℃;
the value range of the temperature of the cross air blow or the circular air blow which is lower than the temperature of the spinning trickle is 20-200 ℃.
Preferably, the liquid in the coagulating bath is one or a mixture of water, a decalin solution, an ethylene glycol solution and inorganic saline.
Preferably, the temperature of the drying hot box ranges from 60 ℃ to 100 ℃.
As a preference, the first and second liquid crystal compositions are,
the temperature range of the multi-stage post-spinning drafting is 130-160 ℃,
the total stretching ratio of the multi-stage post-spinning drafting is more than or equal to 5 times.
Preferably, a first metering pump, a static mixer, a second metering pump and a spinning assembly are arranged in the spinning box body, wherein a spinning stock solution is extruded from a spinneret plate hole after sequentially passing through the feed inlet, the first metering pump, the static mixer, the second metering pump and the spinning assembly,
a pressure sensor is arranged between the first metering pump and the second metering pump,
the pressure between the first metering pump and the second metering pump measured by the pressure sensor can be acquired by a control terminal,
the first metering pump is controlled by a first metering pump motor,
the second metering pump is controlled by a second metering pump motor,
the first metering pump motor and the second metering pump motor are respectively communicated with the control terminal:
and the control terminal controls the first metering pump motor to reduce the rotating speed or increase the rotating speed, so that the value range of the pressure between the first booster pump motor and the second booster pump motor is controlled to be 1-10 MPa.
Preferably, a gas nozzle is arranged in the drying hot box, and the gas nozzle is selected from a network nozzle, an air knife or an air knife.
Preferably, the gas nozzles are in the form selected from the group consisting of micro-holes and slits, wherein,
the distance between the orifice of the micropore and the solid jelly silk bundle is less than or equal to 5 mm;
the distance between the slit opening of the slit and the solid jelly silk bundle is less than or equal to 5 mm.
Preferably, the solid jelly glue tow is subjected to hot drawing after the organic solvent is removed by a drying hot box provided with a gas nozzle, and the solid jelly glue tow is in direct contact with the orifice of the micropore or the slit opening of the slit in the process of obtaining dry-state precursor filaments.
Preferably, in the process of obtaining dry-state filaments after the solid jelly tow is passed through a drying hot box provided with a gas nozzle to remove the organic solvent and is thermally drawn,
the value range of the gas pressure in the gas nozzle is 0.1MPa-0.8 MPa;
the value range of the gas temperature in the gas nozzle is 80-120 ℃;
the gas in the gas nozzle is selected from nitrogen, steam, carbon dioxide, air or a mixed gas of the nitrogen, the steam, the carbon dioxide and the air.
The method for preparing the polyethylene fiber by the double-metering conveying method sequentially selects the ultrahigh molecular weight polyethylene resin with the viscosity-average molecular weight of more than 400 ten thousand as the raw material polyethylene resin; dissolving raw material polyethylene resin in an organic solvent to prepare a spinning stock solution, wherein the mass percentage content of the raw material polyethylene resin in the spinning stock solution is 4-7%, and the organic solvent is one or a mixture of more of decalin, paraffin oil, white oil and xylene; the value range of the intrinsic viscosity of the spinning solution is 9dl/g-29 dl/g; the spinning solution sequentially passes through a first metering pump, a static mixer, a second metering pump and a spinning assembly of a spinning manifold, and is extruded from a spinneret orifice to form a spinning trickle, wherein the value range of pressure difference between the first metering pump and the second metering pump is 1MPa-10MPa, and the value range of pressure in the spinning assembly is 0.1MPa-4 MPa; cooling and solidifying the spinning trickle to obtain gel tows; removing the organic solvent from the gel tows through a drying hot box to obtain dry-state precursor; and (3) performing multi-stage post-spinning drafting on the dry precursor to obtain the polyethylene fiber. The breaking strength of the polyethylene fiber is not less than 40CN/dtex, the initial modulus is not less than 1600cN/dtex, and the breaking strength CV value is less than 2%. It has the advantages of fine denier, high strength and uniformity.
Detailed Description
The invention provides a method for preparing polyethylene fibers by a double metering conveying method, aiming at solving the problems in the prior art, the polyethylene fibers are high in breaking strength and initial modulus and low in breaking strength CV value, so that the method is more practical.
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following detailed description is given to the method for preparing polyethylene fiber by dual metering transportation according to the present invention, and the specific implementation manner, structure, characteristics and effects thereof are described in detail. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the features, structures, or characteristics of one or more embodiments may be combined in any suitable manner.
The term "and/or" herein is merely an association describing an associated object, meaning that three relationships may exist, e.g., a and/or B, with the specific understanding that: both a and B may be included, a may be present alone, or B may be present alone, and any of the three cases can be provided.
Example one
The method for preparing the polyethylene fiber by the double-metering conveying method provided by the embodiment of the invention comprises the following steps: selecting ultra-high molecular weight polyethylene with the viscosity-average molecular weight of 400 ten thousand, preparing a decalin solution with the mass percent of the ultra-high molecular weight polyethylene of 7 percent to ensure that the intrinsic viscosity of the decalin solution of the ultra-high molecular weight polyethylene is 18dl/g, conveying the decalin solution of the ultra-high molecular weight polyethylene into a spinning manifold, sequentially passing through a first metering pump, a static mixer, a second metering pump and a spinning assembly of the spinning manifold, and extruding from a spinneret orifice to form a spinning trickle, wherein the pressure between the first metering pump and the second metering pump is 4.0MPa, and the pressure of the assembly is 1.0 MPa. The spinning stream is cooled and solidified in a water bath to obtain gel tows, the gel tows are subjected to a drying hot box at 90 ℃ to remove organic solvent to obtain dry-state precursor fibers, the dry-state precursor fibers are subjected to two-stage drafting to obtain the ultra-high molecular weight polyethylene fibers, wherein the drafting temperature of the first stage of drafting is 130 ℃, and the drafting temperature of the second stage of drafting is 150 ℃. The breaking strength of the ultra-high molecular weight polyethylene fiber is 40cN/dtex, the initial modulus is 1644cN/dtex, and the CV value of the breaking strength is 1.5%.
Wherein the content of the first and second substances,
first, the purpose or benefit of dual metering: firstly, the material is extruded from the spinneret orifice, and need to guarantee that enough material can enter into the spinneret orifice through the measurement, accurate feed promptly, and the second measuring pump is the effect of measurement, lets the material accurate entering spinneret orifice, guarantees evenly to eat the material. The first metering pump is used for supersaturated feeding, and continuous materials are guaranteed to enter the second metering pump in a standby mode. The first metering pump performs signal chain reaction between the motor frequency converter and the pressure sensor.
Secondly, in the ultra-high molecular weight polyethylene solution spinning system, the pressure of the spinning solution in the assembly must be stable, and if the pressure fluctuates or fluctuates greatly, the spraying amount of the spinning solution fluctuates, which causes the transverse or longitudinal unevenness of the fiber tows, the solution generates broken filaments and broken filaments, or causes the unevenness of the fibers to be high. In order to ensure constant pressure, constant quantity and stability of material conveying, the rotating speed of the first metering pump and the signal of the first pressure sensor are controlled in a linkage mode. According to the process requirement, constant pressure is set between the first metering pump and the second metering pump, when the pressure of the system is increased or decreased, the pressure signal detected by the first pressure sensor is transmitted to a motor control system of the first metering pump as a current or voltage signal, and the motor correspondingly decreases or increases the rotating speed to achieve the purpose of stabilizing the pressure, namely stabilizing the material conveying. In the embodiment, the rotating speed of the second metering pump is unchanged, and the second metering pump has the function of accurately metering materials to enter the spinneret plate holes to form uniform spinning trickle and ensure uniform fibers. However, in order to ensure that the second metering pump has material, the space between the first metering pump and the second metering pump must be filled with the material, and the pressure between the first metering pump and the second metering pump ranges from 1MPa to 10 MPa. In this case, the first metering pump serves to ensure that a pressure exists between the first metering pump and the second metering pump. And the pressure sensors arranged among the first metering pump, the first metering pump motor, the first metering pump and the second metering pump are subjected to interlocking control. The method specifically comprises the following steps: when the pressure between the first metering pump and the second metering pump is lower (particularly lower than 1MPa), the second metering pump is not full, so that the metering materials are less and inaccurate; when the pressure between the first and second metering pumps is high (in particular higher than 10MPa), two situations arise: in the first case: the higher pressure can actively push the second metering pump to operate, so that the metering is larger and inaccurate; in the second case: at higher pressures, material may seep out of the pump gap and cause metering inaccuracies. Therefore, when the pressure range between the first metering pump and the second metering pump is 1MPa-10MPa, the accuracy of material metering can be ensured. For example, when the pressure between the first metering pump and the second metering pump is 3MPa, the frequency converter can adjust the rotating speed of the first motor around the material flow of 3MPa, so as to achieve the purpose of pressure stabilization. The project adopts a double-metering spinning box body, and aims to ensure stable pressurization and stable discharge and obtain good fiber uniformity.
And thirdly, in order to convey and mix the materials in the spinning box body, and the materials are heated uniformly, a static mixer is arranged between the first metering pump and the second metering pump in the spinning box body.
Fourthly, in order to ensure that the spinning beam discharge port and the spinning assembly have good sealing performance and no material leakage, a sealing gasket is arranged between the spinning beam discharge port and the spinning assembly. In this embodiment, the gasket is a metal gasket, preferably an aluminum or copper gasket.
Fifthly, a gas nozzle is arranged in the drying hot box and is selected from a network nozzle, an air knife or an air knife. Solitary dry heat box work efficiency is not high, and this application technical scheme is through installing gas nozzle in dry heat box, and the jelly silk bundle that contains the solvent passes through the nozzle gas outlet, and high-speed wind directly sweeps the solvent and spreads to dry heat box in. The solvent diffused into the drying hot box circularly enters an external solvent recovery system along with wind in a gaseous state or a small liquid droplet mode, and the system wind can be recycled. Has the characteristics of high efficiency, energy conservation, consumption reduction and the like.
Sixthly, the form of the gas nozzle is selected from micropores or slits, wherein the distance between the orifice of each micropore and the solid jelly glue tow is less than or equal to 5 mm; the distance between the slit opening of the slit and the solid jelly silk bundle is less than or equal to 5 mm. The adoption of the nozzle in the form of the micropore or the slit is beneficial to generating high-efficiency air to sweep the tows, the solvent removal effect is extremely obvious, the distance between the tows and the orifice or the slit cannot be large, a certain distance needs to be met, otherwise, high-speed air cannot be effectively utilized, or the air utilization rate is low. The test structure shows that the distance between the air port and the tows is not more than 5mm, and the effect is good. The air outlet has better effect of directly contacting with the tows.
And seventhly, removing the organic solvent from the solid jelly glue tows through a drying hot box provided with a gas nozzle, and performing hot drawing to obtain dry-state precursor filaments, wherein the solid jelly glue tows are in direct contact with the orifices of the micropores or the slit openings of the slits. In this case, it can be ensured that the solid jelly tow can be purged more sufficiently.
Eighthly, removing the organic solvent from the solid jelly tow through a drying hot box provided with a gas nozzle, and performing hot drawing to obtain dry raw filaments, wherein the value range of gas pressure in the gas nozzle is 0.1-0.8 MPa; the value range of the gas temperature in the gas nozzle is 20-120 ℃; the gas in the gas nozzle is selected from nitrogen, steam, carbon dioxide, air or any mixture gas thereof. The gas pressure in the gas nozzle needs to have a certain value range, the too low pressure and the too low speed cannot be achieved, the solvent on the surface of the tows is difficult to blow, and the drying effect is poor; when the gas pressure is too high, the damage to the silk bundles is large, the jelly silk without strength is beaten, the eaten vermicelli is compared, and the broken vermicelli is blown by high-pressure wind. The test shows that the value range of the gas pressure is 0.1MPa-0.8 MPa. The gas temperature in the gas nozzle has great influence on sweeping the gel silk, and the higher the temperature is, is more favorable to the desorption of organic solvent, but, the temperature is high, and the solvent further dissolves destruction to the gel silk, needs the comprehensive consideration: blowing effect, broken filaments or broken ends, cost and the like, and the temperature of 20-120 ℃ is relatively proper.
And ninthly, arranging the static mixed gas at any position of the first metering pump and the spinning component, controlling the flow and pressure of the material after the material passes through the first metering pump, ensuring that the material cannot flow back through the internal resistance of the static mixer, and mainly ensuring that the material is fully mixed in the static mixer to form uniform spinning solution, wherein the static mixed gas is arranged at any position in front of a spinneret plate.
In addition, in this embodiment, the connection between the spinning assembly and the spinning beam is implemented by a gooseneck threaded connection or a bolt fastening connection. Under the condition, the spinning assembly is detachably connected with the spinning manifold, so that the spinning assembly can be replaced conveniently once the spinning assembly is damaged, the depreciation period of the spinning manifold can be prolonged, and the use cost of the spinning manifold can be reduced. The discharge port of the spinning manifold is recessed in the spinning manifold. Under the condition, in the process of moving the spinning manifold, because the discharge port of the spinning manifold is recessed in the spinning manifold, the possibility of abrasion or scratch damage of the discharge port of the spinning manifold can be reduced, and the service life of the spinning manifold is prolonged.
Examples 1-14 operating parameters and results parameters
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. Therefore, it is intended that the appended claims be interpreted as including preferred embodiments and all such alterations and modifications as fall within the scope of the invention.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. A method for preparing polyethylene fiber by a double metering conveying method is characterized by comprising the following steps:
selecting ultrahigh molecular weight polyethylene resin with viscosity average molecular weight of more than 400 ten thousand as raw material polyethylene resin;
dissolving the raw material polyethylene resin in an organic solvent to prepare a spinning solution, wherein the mass percentage content of the raw material polyethylene resin in the spinning solution ranges from 4% to 7%, and the organic solvent is one or a mixture of more of decalin, paraffin oil, white oil and xylene; the intrinsic viscosity of the spinning solution ranges from 9dl/g to 29 dl/g;
the spinning solution sequentially passes through a first metering pump, a static mixer, a second metering pump and a spinning assembly of a spinning manifold, and is extruded from a spinneret orifice to form a spinning trickle, wherein the value range of pressure difference between the first metering pump and the second metering pump is 1MPa-10MPa, and the value range of pressure in the spinning assembly is 0.1MPa-4 MPa;
cooling and solidifying the spinning trickle to obtain gel tows;
removing the organic solvent from the gel tows through a drying hot box to obtain dry-state precursor;
and carrying out multi-stage post-spinning drafting on the dry precursor to obtain the polyethylene fiber.
2. The method for preparing polyethylene fiber according to the dual metering conveying method of claim 1, wherein the cooling method is selected from a liquid coagulating bath, a side blowing method or a circular blowing method in the process of obtaining the jelly glue filament bundle by cooling and solidifying the spinning fine flow, wherein,
the temperature of the liquid coagulating bath is lower than the temperature of the spinning trickle, and the value range is 20-200 ℃;
the value range of the temperature of the cross air blow or the circular air blow which is lower than the temperature of the spinning trickle is 20-200 ℃.
3. The method for preparing polyethylene fiber according to the dual metering conveying method of claim 2, wherein the liquid in the coagulating bath is one or more selected from water, decalin solution, ethylene glycol solution and inorganic salt water.
4. The method for preparing polyethylene fibers according to the dual metering conveying method of claim 1, wherein the temperature of the drying hot box is in a range of 60 ℃ to 100 ℃.
5. The dual metered delivery process for making polyethylene fibers of claim 1,
the temperature range of the multi-stage post-spinning drafting is 130-160 ℃,
the total stretching ratio of the multi-stage post-spinning drafting is more than or equal to 5 times.
6. The method for preparing polyethylene fiber according to the dual metering conveying method of claim 1, wherein a first metering pump, a static mixer, a second metering pump and a spinning pack are provided in the spinning housing, wherein a spinning dope is extruded from a spinneret hole after passing through the feed port, the first metering pump, the static mixer, the second metering pump and the spinning pack in this order,
a pressure sensor is arranged between the first metering pump and the second metering pump,
the pressure between the first metering pump and the second metering pump measured by the pressure sensor can be acquired by a control terminal,
the first metering pump is controlled by a first metering pump motor,
the second metering pump is controlled by a second metering pump motor,
the first metering pump motor and the second metering pump motor are respectively communicated with the control terminal:
and the control terminal controls the first metering pump motor to reduce the rotating speed or increase the rotating speed, so that the value range of the pressure between the first booster pump motor and the second booster pump motor is controlled to be 1-10 MPa.
7. The method of manufacturing polyethylene fibers according to the dual metering conveying method of claim 1, wherein a gas nozzle is disposed in the drying hot box, and the gas nozzle is selected from a network nozzle, an air knife or an air knife.
8. The dual metering delivery process for making polyethylene fibers according to claim 7, wherein the gas nozzles are in a form selected from the group consisting of micro-holes and slits, wherein,
the distance between the orifice of the micropore and the solid jelly silk bundle is less than or equal to 5 mm;
the distance between the slit opening of the slit and the solid jelly silk bundle is less than or equal to 5 mm.
9. The method for preparing polyethylene fiber according to the dual metering conveying method of claim 8, wherein the solid jelly glue tow is directly contacted with the opening of the micropore or the slit opening of the slit in the process of obtaining dry raw filament after the solid jelly glue tow is passed through a drying hot box provided with a gas nozzle to remove the organic solvent and is thermally drawn.
10. The method of manufacturing polyethylene fiber according to the dual metering transportation of claim 7, wherein in the process of obtaining dry raw filament after the solid jelly tow is passed through a dry hot box equipped with a gas nozzle to remove the organic solvent and is thermally drawn,
the value range of the gas pressure in the gas nozzle is 0.1MPa-0.8 MPa;
the value range of the gas temperature in the gas nozzle is 60-120 ℃;
the gas in the gas nozzle is selected from nitrogen, steam, carbon dioxide, air or a mixed gas of the nitrogen, the steam, the carbon dioxide and the air.
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| CN114481343A (en) * | 2020-10-23 | 2022-05-13 | 中国石油化工股份有限公司 | Fiber spinning method and polyethylene spinning fiber |
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