CN119956514A - Polyethylene ultra-thick denier monofilament for rope and preparation method thereof - Google Patents
Polyethylene ultra-thick denier monofilament for rope and preparation method thereof Download PDFInfo
- Publication number
- CN119956514A CN119956514A CN202311465084.1A CN202311465084A CN119956514A CN 119956514 A CN119956514 A CN 119956514A CN 202311465084 A CN202311465084 A CN 202311465084A CN 119956514 A CN119956514 A CN 119956514A
- Authority
- CN
- China
- Prior art keywords
- water tank
- temperature
- ultra
- polyethylene
- monofilament
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Landscapes
- Artificial Filaments (AREA)
Abstract
本发明公开了一种绳索用聚乙烯超粗旦单丝及其制备方法。该单丝细度为400D‑2000D，强度为13cN/dtex以上，断裂伸长率为3‑10％。制备方法包括以下步骤：(1)原料选择:选用重均分子量8万‑50万，分子量分布小于等于4，190℃、2.16KG下熔融指数为0.3‑10.0g/10min的HDPE粉料。此外，HDPE每1000个碳原子含0.1‑5个支链。(2)物料混合，将HDPE与抗氧剂、色母粒等混合均匀。(3)熔融纺丝：依次经过进料机1，单螺杆挤出机2，熔体过滤器3，计量泵4，喷丝板5，第一冷却水箱6，第二冷却水箱7，第一牵引设备8，第一加热设备9，第二牵引设备10，第二加热设备11，第三牵引设备12，最后通过卷绕机13收卷到辊子上，收卷速度200‑800m/min。该制备流程简单，成本低，制备的超粗旦单丝强力高，断裂伸长率低，耐磨性好，适用于制备绳索。
The invention discloses a polyethylene ultra-thick denier monofilament for ropes and a preparation method thereof. The monofilament has a fineness of 400D-2000D, a strength of more than 13cN/dtex, and an elongation at break of 3-10%. The preparation method comprises the following steps: (1) raw material selection: selecting HDPE powder with a weight average molecular weight of 80,000-500,000, a molecular weight distribution of less than or equal to 4, and a melt index of 0.3-10.0 g/10 min at 190° C. and 2.16 kg. In addition, HDPE contains 0.1-5 branches per 1000 carbon atoms. (2) material mixing, mixing HDPE with an antioxidant, a masterbatch, etc. uniformly. (3) Melt spinning: sequentially passing through a feeder 1, a single screw extruder 2, a melt filter 3, a metering pump 4, a spinneret 5, a first cooling water tank 6, a second cooling water tank 7, a first traction device 8, a first heating device 9, a second traction device 10, a second heating device 11, a third traction device 12, and finally being wound onto a roller by a winder 13, with a winding speed of 200-800 m/min. The preparation process is simple, the cost is low, and the prepared ultra-coarse denier monofilament has high strength, low elongation at break, and good wear resistance, and is suitable for preparing ropes.
Description
Technical Field
The invention relates to the field of polyethylene fibers for ropes, in particular to a polyethylene ultra-coarse denier monofilament for medium-high strength ropes and a preparation method thereof.
Background
At present, the fiber for the rope mainly comprises terylene, chinlon, polyethylene filaments, polypropylene filaments and the like, the strength is 5-10cN/dtex, and the fiber for the rope also comprises aramid fibers, ultra-high molecular weight polyethylene fibers and the like, the strength is 22-40cN/dtex, and the domestic market is blank for medium-high strength fibers with the strength of 10-20 cN/dtex.
The ropes prepared by the ultra-high molecular weight polyethylene fiber have high strength and excellent performance, but for partial middle-end civil markets, the special high strength is not needed in the use stage, and the phenomena of high cost and pollution caused by the ultra-high molecular weight polyethylene filament spinning process are unavoidable. The ultra-high molecular weight polyethylene monofilament is thinner, and is easy to break and hook in the use process, so that the ultra-high molecular weight polyethylene rope can be used later only by coating in the preparation process. The common polyethylene heavy denier monofilament sold in the market has the strength below 7cN/dtex and needs to be replaced frequently in use. In the process of preparing the coarse monofilaments, the problems of difficult cooling and low production speed exist, and the winding speed is generally 100-150m/min.
There have been many studies on the direct melt spinning of ultra-high molecular weight polyethylene by modifying it and using a screw extruder, most of which are blended with low molecular weight polyolefin or lubricant, etc., and the extrusion speed is slow. Meanwhile, the compatibility of the additive materials and the ultra-high molecular weight polyethylene is poor, the phenomenon of broken filaments can occur in actual production, and large-scale production is difficult.
There are also some studies that the fineness of the monofilaments prepared by adding a modifier to High Density Polyethylene (HDPE) and then melt spinning is fine, and the abrasion resistance effect is not particularly ideal in the application to ropes. And excessive modifier is added to influence the spinning continuity, the strength of the finished product and the hand feeling.
Patent CN102154749a discloses a heavy denier ultra-high molecular weight polyethylene fiber yarn, which adopts gel spinning, and has complex flow and high cost.
Patent CN115029810A discloses a high-performance polyethylene heavy denier monofilament for a stormy wave resistant fishery rope net, the diameter of a filament outlet hole is 5-50mm, such a large filament spraying hole means that the quantity of produced monofilaments is small,
The yield is low, and the extruded filaments have too large a diameter to be cooled uniformly.
Therefore, in order to solve the above problems, there is a need to develop a medium-strength polyethylene ultra-coarse denier monofilament which has low cost and simple preparation process and can be used for ropes.
Disclosure of Invention
In view of the defects of the prior art, the invention provides a polyethylene ultra-coarse denier monofilament for a rope and a preparation method thereof, the production process of the monofilament is simple, the cost is low, and compared with a common polyethylene rope, the prepared rope has greatly improved stretching and wear resistance, improves the durability of the rope in use, and is suitable for middle-end civil markets.
The polyethylene monofilament prepared by the invention has fineness of 400D-2000D, strength of more than 13cN/dtex and elongation at break of 3-10%.
The invention aims at realizing the following means:
The invention provides a preparation method of polyethylene ultra-coarse denier monofilament for ropes, which is characterized by comprising the following steps of:
(1) Raw material selection
HDPE powder with the weight average molecular weight of 8 ten thousand to 50 ten thousand and the molecular weight distribution of less than or equal to 4,190 ℃ and the melt index of 0.3 g/10.0 g/10min under 2.16KG is selected, and the polyethylene has good fluidity, is easy to process and does not need to be added with lubricant. In addition, HDPE contains 0.1-5 branches per 1000 carbon atoms, the less branches, the higher the crystallinity of the polyethylene, and the higher the strength of the finished product produced.
(2) Material mixing
Based on the weight of HDPE, 0.1-1% of antioxidant is added, and 0.5-5% of polyethylene color master batch is added according to the color requirement, and the mixture can be obtained for standby after the mixture is directly mixed uniformly by stirring for 5-10min by a high-speed mixer.
(3) Melt spinning
The melt spinning process flow comprises a feeding machine, a single screw extruder, a melt filter, a metering pump, a spinneret plate, a first cooling water tank, a second cooling water tank, a first traction device, a first heating device, a second traction device, a second heating device, a third traction device and a winding machine.
Wherein, the length-diameter ratio of the single screw extruder is 30-35, and the screw diameter is more than 65 mm. The temperature of each zone is set to be 150-230 ℃ in the feeding section of the screw, 220-320 ℃ in the melting section and 220-320 ℃ in the metering section.
Because the extrusion amount of the ultra-coarse denier monofilaments is large, the metering pump is 50cc or 100cc or 150cc, the rotating speed is 10-50r/min, and one-in-one-out is adopted. The temperature of the spinneret plate is 220-320 ℃. The diameter of the spinneret holes is 0.8-3mm, the length-diameter ratio is 6-15, and the gap of the spinneret holes is larger than that of the conventional gap, so that the extruded filaments are prevented from being adhered. The draft ratio of the spray nozzle is 5-50.
The first cooling water tank and the second cooling water tank adopt circulating water cooling, the extruded precursor wire has a thicker diameter, the cooling effect is difficult to achieve by adopting air cooling, and the precursor wire can be cooled uniformly by adopting the circulating water cooling, and the energy can be saved. Meanwhile, two-stage cooling is adopted, so that the crystallization time of polyethylene is increased, and the crystallinity is improved. The length of the first cooling water tank and the second cooling water tank is 1.5-3 m. The temperature of the first cooling water tank is kept at 50-70 ℃ and the temperature of the second cooling water tank is kept at 15-30 ℃ by controlling the water inlet valve and the water outlet valve. The spinneret plate is 1-5cm away from the water surface of the first cooling water tank.
The first heating equipment adopts water bath heating, the length of a water tank is 4-8m, the temperature is controlled to be 90-100 ℃, and the first heating equipment is provided with a temperature controller with the precision of +/-1 ℃. The heat conductivity coefficient of water is high, which is favorable for uniform heating and full drafting of the coarse monofilaments.
The second heating equipment adopts a steam oven for heating, and hot air dries the monofilaments while hot drawing. Because the diameter of the monofilaments is thicker, the length of the oven is longer than that of a conventional oven in order to ensure that the filaments are heated uniformly at a certain traction speed, the length is 8-12m, and the temperature is set to 105-115 ℃.
The speed ratio of the second traction equipment to the first traction equipment is 2-5 times, and the speed ratio of the third traction equipment to the second traction equipment is 3-7 times, so that the cooled precursor is drawn by 8-25 times. The fully drawn monofilament has high strength and small elongation, and is more suitable for preparing ropes.
The winding speed is 200-800m/min, when the winding speed is too high, the yarn can not be sufficiently cooled, and the drafting process is heated unevenly, so that the strength of the final finished product is affected.
The invention has the beneficial effects that:
(1) The strength of the prepared polyethylene monofilament is more than 13cN/dtex, the elongation is 3-10%, and compared with the common polyethylene monofilament, the strength is improved, the elongation is reduced, the spinning winding speed is improved, and the yield is increased. The cost is much lower than that of ultra-high molecular weight polyethylene filaments, and the fiber is widely applicable to civil cable markets.
(2) The fineness of the prepared monofilaments is 400D-2000D, the higher the fineness of the monofilaments is, the better the wear resistance of the prepared rope is, and the prepared rope does not need to be added with a coating for use.
(3) The melt method is adopted to directly carry out extrusion spinning, the process flow is simple, the cost is low, and no pollution is caused.
(4) And the method does not need to add excessive flow additives and other additives, reduces the cost, reduces the yarn breakage phenomenon in the spinning process, and does not excessively influence the strength and the hand feeling of the finished product.
Drawings
FIG. 1 is a drawing of a device for making and using an embodiment of the present invention.
In the figure, a 1-feeder, a 2-single screw extruder, a 3-melt filter, a 4-metering pump, a 5-spinneret plate, a 6-first cooling water tank, a 7-second cooling water tank, an 8-first drawing device, a 9-first heating device, a 10-second drawing device, a 11-second heating device, a 12-third drawing device and a 13-winder.
Detailed Description
The present invention will be described in further detail with reference to examples.
Example 1
HDPE powder with weight average molecular weight of 11 ten thousand and molecular weight distribution of 2.8 and branched chain number of 0.5,190 ℃ and melt index of 1.0g/10min under 2.16KG is selected, and antioxidant with the weight average molecular weight of 0.3% of HDPE raw material is added and mixed uniformly by a high-speed mixer. The mixture was melt extruded by a single screw extruder with a diameter of 65mm and an aspect ratio of 30, the screw feed section temperature was 180 ℃, the melt section temperature was 260 ℃, the metering section temperature was 260 ℃, and the spinneret temperature was 260 ℃.50 cc of metering pump. The diameter of the spinneret hole is 1.0mm, the length-diameter ratio is 10, the nozzle draft ratio is 45, the extruded precursor enters a water tank for cooling, the temperature of the first cooling water tank is 50-55 ℃, the temperature of the second cooling water tank is 20-25 ℃, the temperature of the first heating device is 95 ℃, the temperature of the second heating device is 110 ℃, the speed ratio of the second drawing device to the first drawing device is 3.2 times, the speed ratio of the third drawing device to the second drawing device is 6 times, the cooled precursor is 19.2 times, and the winding speed is 700m/min. The fineness of the prepared monofilaments is 460D, the strength is 14.2cN/dtex, and the elongation at break is 5.3%.
Example 2
HDPE powder with 20 ten thousand weight average molecular weight and 2.5 molecular weight distribution and 2,190 ℃ branched chain number and melt index of 0.6g/10min under 2.16KG is selected, and antioxidant with 0.3% of HDPE raw material is added and uniformly mixed by a high-speed mixer. The mixture was melt extruded by a single screw extruder with a diameter of 65mm and an aspect ratio of 30, the screw feed section temperature was 180 ℃, the melt section temperature was 280 ℃, the metering section temperature was 280 ℃, and the spinneret temperature was 280 ℃. 50cc of metering pump. The diameter of the spinneret hole is 1.0mm, the length-diameter ratio is 10, the nozzle draft ratio is 45, the extruded precursor enters a water tank for cooling, the temperature of the first cooling water tank is 50-55 ℃, the temperature of the second cooling water tank is 20-25 ℃, the temperature of the first heating device is 95 ℃, the temperature of the second heating device is 110 ℃, the speed ratio of the second drawing device to the first drawing device is 3.5 times, the speed ratio of the third drawing device to the second drawing device is 6 times, the cooled precursor is drafted 21 times, and the winding speed is 600m/min. The fineness of the prepared monofilaments is 460D, the strength is 14.9cN/dtex, and the elongation at break is 5.0%.
Example 3
HDPE powder with weight average molecular weight of 11 ten thousand and molecular weight distribution of 2.8 and branched chain number of 0.5,190 ℃ and melt index of 1.0g/10min under 2.16KG is selected, and antioxidant with the weight average molecular weight of 0.3% of HDPE raw material is added and mixed uniformly by a high-speed mixer. The mixture was melt extruded by means of a single-screw extruder with a diameter of 65mm and an aspect ratio of 30, at a screw feed stage temperature of 180℃and a melt stage temperature of 270℃and a metering stage temperature of 270℃and a spinneret temperature of 270 ℃. 50cc of metering pump. The diameter of the spinneret hole is 1.5mm, the length-diameter ratio is 10, the nozzle draft ratio is 32, the extruded precursor enters a water tank for cooling, the temperature of the first cooling water tank is 50-55 ℃, the temperature of the second cooling water tank is 20-25 ℃, the temperature of the first heating device is 98 ℃, the temperature of the second heating device is 110 ℃, the speed ratio of the second drawing device to the first drawing device is 3.5 times, the speed ratio of the third drawing device to the second drawing device is 6.1 times, the cooled precursor is 21.4 times, and the winding speed is 550m/min. The fineness of the prepared monofilaments is 850D, the strength is 14.0cN/dtex, and the elongation at break is 4.9%.
Example 4
HDPE powder with weight average molecular weight of 11 ten thousand and molecular weight distribution of 2.8 and branched chain number of 0.5,190 ℃ and melt index of 0.9g/10min under 2.16KG is selected, and antioxidant with the weight average molecular weight of 0.3% of HDPE raw material is added and mixed uniformly by a high-speed mixer. The mixture was melt extruded by means of a single-screw extruder with a diameter of 80mm and an aspect ratio of 30, at a screw feed stage temperature of 220 ℃, at a melting stage temperature of 280 ℃ and at a metering stage temperature of 280 ℃. 100cc of metering pump. The spinneret temperature was 280 ℃. The diameter of the spinneret hole is 2.0mm, the length-diameter ratio is 12, the nozzle draft ratio is 25, the extruded precursor enters a water tank for cooling, the temperature of the first cooling water tank is 55-60 ℃, the temperature of the second cooling water tank is 15-20 ℃, the temperature of the first heating device is 100 ℃, the temperature of the second heating device is 115 ℃, the speed ratio of the second drawing device to the first drawing device is 4.2 times, the speed ratio of the third drawing device to the second drawing device is 4.8 times, the cooled precursor is 20.2 times, and the winding speed is 450m/min. The fineness of the prepared monofilaments is 1200D, the strength is 13.8cN/dtex, and the elongation at break is 5.3%.
Comparative example 1
HDPE granules with weight average molecular weight of 10 ten thousand and molecular weight distribution of 4.5 and containing branched chain number 5,190 ℃ and melt index of 1.0g/10min under 2.16KG per 1000 carbon atoms are selected, and antioxidant with the weight of 0.3% of HDPE raw material is added and uniformly mixed by a high-speed mixer. The mixture was melt extruded by a single screw extruder with a diameter of 65mm and an aspect ratio of 30, the screw feed section temperature was 180 ℃, the melt section temperature was 260 ℃, the metering section temperature was 260 ℃, and the spinneret temperature was 260 ℃. 50cc of metering pump. The diameter of the spinneret hole is 1.0mm, the length-diameter ratio is 10, the nozzle draft ratio is 45, the extruded precursor enters a water tank for cooling, the temperature of a first cooling water tank is 50-55 ℃, the temperature of a second cooling water tank is 20-25 ℃, the temperature of a first heating device is 95 ℃, the temperature of a second heating device is 110 ℃, the speed ratio of the second drawing device to the first drawing device is 3 times, the speed ratio of the third drawing device to the second drawing device is 4.2 times, the cooled precursor is 12.6 times, and the winding speed is 550m/min. The fineness of the prepared monofilaments is 450D, the strength is 7.5cN/dtex, and the elongation at break is 6.3%.
Comparative example 2
HDPE granules with weight average molecular weight of 10 ten thousand and molecular weight distribution of 4.5 and containing branched chain number 5,190 ℃ and melt index of 1.0g/10min under 2.16KG per 1000 carbon atoms are selected, and antioxidant with the weight of 0.3% of HDPE raw material is added and uniformly mixed by a high-speed mixer. The mixture was melt extruded by a single screw extruder with a diameter of 65mm and an aspect ratio of 30, the screw feed section temperature was 180 ℃, the melt section temperature was 260 ℃, the metering section temperature was 260 ℃, and the spinneret temperature was 260 ℃. 50cc of metering pump. The diameter of the spinneret hole is 0.6mm, the length-diameter ratio is 10, the nozzle draft ratio is 45, the extruded precursor enters a water tank for cooling, the temperature of a first cooling water tank is 50-55 ℃, the temperature of a second cooling water tank is 20-25 ℃, the temperature of a first heating device is 95 ℃, the temperature of a second heating device is 110 ℃, the speed ratio of the second drawing device to the first drawing device is 3 times, the speed ratio of the third drawing device to the second drawing device is 4 times, the cooled precursor is 12 times, and the winding speed is 600m/min. The fineness of the prepared monofilaments is 50D, the strength is 7.8cN/dtex, and the elongation at break is 5.2%.
Comparative example 3
HDPE granules with weight average molecular weight of 10 ten thousand and molecular weight distribution of 4.5 and containing branched chain number 5,190 ℃ and melt index of 1.0g/10min under 2.16KG per 1000 carbon atoms are selected, and antioxidant with the weight of 0.3% of HDPE raw material is added and uniformly mixed by a high-speed mixer. The mixture was melt extruded by a single screw extruder with a diameter of 65mm and an aspect ratio of 30, the screw feed section temperature was 180 ℃, the melt section temperature was 260 ℃, the metering section temperature was 260 ℃, and the spinneret temperature was 260 ℃. 50cc of metering pump. The diameter of the spinneret hole is 0.8mm, the length-diameter ratio is 10, the nozzle draft ratio is 45, and the extruded precursor is cooled by only one water tank, and the temperature of the water tank is 20-25 ℃. Then the material passes through a first traction device and a second traction device, the speed ratio of the second traction device to the first traction device is 8.5, a steam oven is adopted for heating in the middle, the temperature is 100 ℃, the length of the oven is 4m, and the winding speed is 130m/min. The fineness of the prepared monofilaments is 200D, the strength is 6.5cN/dtex, and the elongation at break is 9.8%.
Comparative example 4
HDPE granules with weight average molecular weight of 10 ten thousand and molecular weight distribution of 4.5 and containing branched chain number 5,190 ℃ and melt index of 1.0g/10min under 2.16KG per 1000 carbon atoms are selected, and antioxidant with the weight of 0.3% of HDPE raw material is added and uniformly mixed by a high-speed mixer. The mixture was melt extruded by means of a single-screw extruder with a diameter of 80mm and an aspect ratio of 30, at a screw feed stage temperature of 180℃and a melting stage temperature of 260℃and a metering stage temperature of 260℃and a spinneret temperature of 260 ℃.100 cc of metering pump. The diameter of the spinneret hole is 2.0mm, the length-diameter ratio is 12, the nozzle draft ratio is 25, and the extruded precursor is cooled by only one water tank, and the temperature of the water tank is 20-25 ℃. Then the first traction equipment and the second traction equipment are passed through, the speed ratio of the second traction equipment to the first traction equipment is 8.5, the middle is heated by adopting an oven, the temperature is 100 ℃, the length of the oven is 4m, and the winding speed is 50m/min. The fineness of the prepared monofilaments is 1200D, the strength is 5.3cN/dtex, and the elongation at break is 11.2%.
Test case
Three 6mm gauge cords were prepared using the same process parameters using the monofilaments prepared in example 1, example 4, comparative example 1, comparative example 2, and comparative example 4, respectively, and the corresponding cords were numbered 1, 2, 3, 4, and 5, respectively, and then subjected to strength and abrasion resistance tests. The strength test was carried out with reference to the standard GB/T8834-2016 determination of the physical and mechanical properties of fiber ropes. Abrasion resistance test is carried out by referring to a test of a measuring drum friction method of abrasion resistance of a standard FZ/T60049-2022 fiber rope, the experimental tension is set to 10KG, the running speed is 30r/min, and the revolution is 12000 revolutions. The abrasion resistance test result is expressed by the rope strength retention, and the rope strength retention is calculated as follows:
strength retention = (strength after 12000 revolutions of rope/strength before abrasion test) ×100%
The higher the results, the better the rope wear resistance, and the test results are shown in table 1.
Test results of Strength and abrasion resistance of ropes prepared in Table 1
| Numbering device | Monofilament strength | Fineness of monofilament | Rope strength | Strong retention rate of rope |
| 1 | 14.2cN/dtex | 460D | 13.7KN | 50% |
| 2 | 13.8cN/dtex | 1200 D | 13.1KN | 66% |
| 3 | 7.5cN/dtex | 450D | 7.3KN | 49% |
| 4 | 7.8cN/dtex | 50D | 7.5KN | 41% |
| 5 | 5.3cN/dtex | 1200D | 5.2KN | 60% |
As can be seen from Table 1, the rope made of the polyethylene monofilament prepared by the invention has greatly improved strength and wear resistance compared with the common polyethylene rope.
Claims (9)
1. A polyethylene ultra-thick denier monofilament for a rope is characterized in that the fineness of the monofilament is 400D-2000D, the strength is more than 13cN/dtex, and the elongation is 3-10%.
2. The preparation method of the polyethylene ultra-coarse denier monofilament for the rope is characterized by comprising the following steps of:
(1) Raw material selection
HDPE powder with weight average molecular weight of 8 ten thousand to 50 ten thousand and molecular weight distribution of less than or equal to 4,190 ℃ and melt index of 0.3 g/10.0 g/10min under 2.16KG is selected. In addition, HDPE contains 0.1-5 branches per 1000 carbon atoms.
(2) Material mixing
Based on the weight of HDPE, 0.1-1% of antioxidant is added, and 0.5-5% of polyethylene color master batch is added according to the color requirement, and the mixture can be obtained for standby after the mixture is directly mixed uniformly by stirring for 5-10min by a high-speed mixer.
(3) Melt spinning
The melt spinning process flow comprises a feeder 1, a single screw extruder 2, a melt filter 3, a metering pump 4, a spinneret 5, a first cooling water tank 6, a second cooling water tank 7, a first traction device 8, a first heating device 9, a second traction device 10, a second heating device 11, a third traction device 12 and a winding machine 13.
3. The method for preparing polyethylene ultra-coarse denier monofilament for rope according to claim 2, wherein the single screw extruder in step 3 has an aspect ratio of 30-35 and a screw diameter of 65mm or more. The temperature of each area of the screw is set to be 150-230 ℃ in the feeding section, 220-320 ℃ in the melting section and 220-320 ℃ in the metering section.
4. The method for preparing polyethylene ultra-coarse denier monofilament for rope according to claim 2, wherein in the step 3, the metering pump is 50cc or 100cc or 150cc, and the rotation speed is 10-50r/min, and one-in-one-out is adopted. The temperature of the spinneret plate is 220-320 ℃, the diameter of the spinneret hole is 0.8-3mm, and the length-diameter ratio is 6-15. The draft ratio of the spray nozzle is 5-50.
5. The method for preparing ultra-coarse denier polyethylene monofilaments for ropes according to claim 2, wherein in the step 3, the cooling adopts a two-stage cooling mode, and the circulating water is controlled to enable the temperature of a first cooling water tank to be 50-70 ℃, the length of the water tank to be 1.5-3m, the temperature of a second cooling water tank to be 15-30 ℃ and the length of the water tank to be 1.5-3m. The spinneret plate is 1-5cm away from the water surface of the first cooling water tank.
6. The method for preparing polyethylene ultra-coarse denier monofilament for rope according to claim 2, wherein in step 3, the first heating device adopts water bath heating, the length of the water tank is 4-8m, the temperature controller is provided, the precision is +/-1 ℃, and the temperature is controlled to be 90-100 ℃.
7. The method for preparing polyethylene ultra-coarse denier monofilament for rope according to claim 2, wherein in the step 3, the second heating device is a steam oven with the oven length of 8-12m and the temperature of 105-115 ℃.
8. The method for preparing ultra-coarse denier polyethylene filaments for ropes according to claim 2, wherein in the step 3, the speed ratio of the second drawing device to the first drawing device is 2-5 times, the speed ratio of the third drawing device to the second drawing device is 3-7 times, and the cooled filaments are drawn 8-25 times.
9. The method for preparing polyethylene ultra-coarse denier monofilament for rope according to claim 2, wherein the winding speed of the winding machine is 200-800m/min in the step 3.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311465084.1A CN119956514A (en) | 2023-11-07 | 2023-11-07 | Polyethylene ultra-thick denier monofilament for rope and preparation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311465084.1A CN119956514A (en) | 2023-11-07 | 2023-11-07 | Polyethylene ultra-thick denier monofilament for rope and preparation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN119956514A true CN119956514A (en) | 2025-05-09 |
Family
ID=95590481
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311465084.1A Withdrawn CN119956514A (en) | 2023-11-07 | 2023-11-07 | Polyethylene ultra-thick denier monofilament for rope and preparation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN119956514A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539033A (en) * | 2001-08-08 | 2004-10-20 | �����֯��ʽ���� | High Tensile Polyethylene Fiber |
| CN1646739A (en) * | 2002-04-09 | 2005-07-27 | 东洋纺织株式会社 | Polyethylene fiber and process for producing the same |
| CN105308227A (en) * | 2013-07-23 | 2016-02-03 | 宇部爱科喜模株式会社 | Method for producing drawn conjugated fiber, and drawn conjugated fiber |
| CN109306541A (en) * | 2018-09-14 | 2019-02-05 | 上海化工研究院有限公司 | A kind of preparation method of high strength and high modulus polyethylene fiber |
| CN109914001A (en) * | 2019-03-28 | 2019-06-21 | 浙江千禧龙纤特种纤维股份有限公司 | A kind of manufacturing method of high tenacity high-tenacity polyethylene fibre |
| CN110820058A (en) * | 2019-11-05 | 2020-02-21 | 上海化工研究院有限公司 | Preparation method of civil high-performance polyethylene fiber |
| TW202124803A (en) * | 2019-12-27 | 2021-07-01 | 南韓商可隆工業股份有限公司 | Skin cooling fabric, polyethylene yarn therefor, and method for manufacturing polyethylene yarn |
-
2023
- 2023-11-07 CN CN202311465084.1A patent/CN119956514A/en not_active Withdrawn
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539033A (en) * | 2001-08-08 | 2004-10-20 | �����֯��ʽ���� | High Tensile Polyethylene Fiber |
| CN1646739A (en) * | 2002-04-09 | 2005-07-27 | 东洋纺织株式会社 | Polyethylene fiber and process for producing the same |
| CN105308227A (en) * | 2013-07-23 | 2016-02-03 | 宇部爱科喜模株式会社 | Method for producing drawn conjugated fiber, and drawn conjugated fiber |
| CN109306541A (en) * | 2018-09-14 | 2019-02-05 | 上海化工研究院有限公司 | A kind of preparation method of high strength and high modulus polyethylene fiber |
| CN109914001A (en) * | 2019-03-28 | 2019-06-21 | 浙江千禧龙纤特种纤维股份有限公司 | A kind of manufacturing method of high tenacity high-tenacity polyethylene fibre |
| CN110820058A (en) * | 2019-11-05 | 2020-02-21 | 上海化工研究院有限公司 | Preparation method of civil high-performance polyethylene fiber |
| TW202124803A (en) * | 2019-12-27 | 2021-07-01 | 南韓商可隆工業股份有限公司 | Skin cooling fabric, polyethylene yarn therefor, and method for manufacturing polyethylene yarn |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101724265B (en) | Denier/superfine denier nylon master granule, preoriented yarn (POY) and draw textured yarn (DTY) stretch yarn and preparation method thereof | |
| CN104805519B (en) | Production method of polyamide-6 profiled fiber | |
| CN102839432B (en) | Preparation method of ultra-high-speed spinning polyester pre-oriented yarn | |
| CN104153077B (en) | A kind of production technology of wear-resisting type PA6 bulk yarn | |
| CN101851795B (en) | Method for processing high-performance modified polyethylene monofilaments for manufacturing fishing net | |
| CN104514037B (en) | A kind of production method of high-strength fine denier light terylene short fine dimension | |
| CN108642584B (en) | Spinning and drawing combination machine for split-fiber female yarns | |
| CN106319652A (en) | Preparation method of chinlon 6 fine denier stretch yarns | |
| CN102677238A (en) | Production process of environment-friendly heather grey effect composite textured filament for knitting | |
| CN102677239A (en) | Environment-friendly heather grey effect composite deformation filament yarn production process | |
| CN111411407A (en) | Production process of regenerated super-dull elastic composite yarn | |
| CN102418169B (en) | Sea-island fibre and preparation method thereof | |
| CN106319654B (en) | 6 elastic filament of cationic dye capable of dyeing polyamide fibre and its production technology | |
| CN103866405B (en) | A kind of high density holes profiled filaments and preparation method thereof | |
| CN104480555A (en) | Production process of high-elasticity-feature terylene pre-oriented fibers | |
| CN103696034B (en) | The production method of a kind of full-dull thin dawn or super fine denier nylon 6FDY long filament | |
| CN207537607U (en) | A kind of color spins fine-denier polyamide fiber silk production equipment | |
| CN103484967B (en) | A kind of copolyesters melt ultrahigh speed directly spins controlled how different contraction composite fiber and preparation method thereof | |
| CN1113115C (en) | Method for producing polyester-based mixed fiber yarn | |
| CN103225117A (en) | Spinning method for polyester cationic composite yarns | |
| CN113550036A (en) | Bulked yarn and preparation method thereof | |
| CN102517679B (en) | The fine denier polyamide fiber 6 pre-oriented yarn of a kind of porous, preparation method and equipment thereof | |
| CN101037846B (en) | Preparation process of polypropylene wear-resistant fiber rope | |
| CN117248294A (en) | A kind of manufacturing method of snow yarn fiber | |
| CN105821550A (en) | Production technology of color yarn air covered yarns |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20250509 |