Chemical fiber filament and method of manufacturing same, and airbag

Abstract

The present application relates to a kind of chemical fiber industry filaments and its manufacturing method and air bag, the manufacturing method of the chemical fiber industry filaments includes: the polyester chip of preset viscosity is pre-crystallized, then solid-phase polymerization processing is carried out, and polymeric tackifying chip is obtained;Polymeric tackifying chip is placed into screw extruder and is melted, and spinning melt is obtained;Spinning melt is filtered by filter screen in spinning assembly;After filtering, spinning melt is formed by spinneret in preset spinning assembly, to form the chemical fiber long filament continuum that multiple fiber bundles are combined. Spinneret includes: first through hole area and second through hole area with spinneret hole, and partition for separating first through hole area and second through hole area, and, the density of spinneret hole is from sparse to dense from outside to inside, compared with prior art, the present application can further reduce the single filament fineness and hairiness amount of chemical fiber industry filaments, while good mechanical properties are maintained.

Description

Technical Field

[0001] This invention relates to the field of chemical fiber weaving, and more particularly to a chemical fiber industrial filament, its manufacturing method, and an airbag. Background Technology

[0002] Nylon filament and other chemical fiber filaments are commonly used yarns in fabric weaving. Due to their softness and abrasion resistance, they are widely used in various textile products, such as airbag products.

[0003] Currently, automotive airbag fabrics are widely used in airbag products. It is estimated that each car contains approximately 1.2 kg of airbags, accounting for about 6% of the total amount of automotive textiles used. The airbag fabric bag plays a crucial protective role within the airbag. Because airbags must withstand strong forces such as tension, tearing, and bursting impact when inflated and deployed under high-speed airflow, they are highly susceptible to breakage or damage. Therefore, the airbag fabric bags used in airbag manufacturing need to be woven from high-performance chemical fiber filaments to ensure that the fabric bags meet high airbag specifications during tensile, tearing, and bursting strength tests, thus guaranteeing the safe and reliable operation of the airbags.

[0004] In existing technologies, the airbag yarn mainly used in airbag fabric bags is nylon-66 filament. However, due to its high manufacturing cost, some technicians have tried to use polyester filament instead of nylon-66 filament to weave airbag fabric bags in order to reduce costs. However, the flexibility and foldability of airbags made with polyester filament are still difficult to meet the manufacturing requirements of airbag fabric bags. Therefore, its application in airbags is relatively small. If it is necessary to improve the flexibility and foldability of the airbag yarn in the airbags made with polyester filament, it is necessary to further reduce the single filament fineness (dpf) of polyester filament and reduce its fuzziness. However, in actual manufacturing, due to the constraints of spinning preparation processes and spinning equipment, such as the structure of the spinneret, polyester industrial filament products are generally 72f to 144f, while the single filament fineness (dpf) is usually 3.5D to 6.9D. If the number of holes in the spinneret is further increased and the single filament fineness (dpf) is reduced, it is very easy to cause an increase in the amount of fuzz and filament bundle adhesion, making it difficult to meet the requirements of flexibility and foldability. At the same time, physical indicators such as mechanical properties are also difficult to guarantee.

[0005] Therefore, how to provide a chemical fiber industrial filament, its manufacturing method, and an airbag, so as to further reduce the single filament fineness and fuzz content of the chemical fiber industrial filament while maintaining good mechanical properties, making it softer and easier to fold, is the technical problem that this invention urgently needs to solve. Summary of the Invention

[0006] The purpose of this invention is to provide a chemical fiber industrial filament, its manufacturing method, and an airbag, which can maintain good mechanical properties, be softer, and easier to fold while further reducing the single filament fineness and fuzz content of the chemical fiber industrial filament.

[0007] To achieve the above objectives, this invention proposes a method for preparing filaments for the chemical fiber industry, comprising:

[0008] Polyester chips with a preset viscosity are pre-crystallized and then subjected to solid-state polymerization to obtain polymerized and thickened chips.

[0009] The polymerized thickening chips are placed in a screw extruder for melt treatment to obtain a spinning melt;

[0010] The spinning melt is filtered through a filter screen in the spinning assembly;

[0011] The filtered spinning melt is passed through a spinneret in a pre-set spinning assembly to form a continuous chemical fiber filament composed of multiple fiber bundles. The spinneret includes a first through-hole area and a second through-hole area with spinneret holes, and a partition for separating the first through-hole area and the second through-hole area. The density of the spinneret holes changes from sparse to dense from the outside to the inside.

[0012] Further preferably, the first through-hole area and the second through-hole area are symmetrically arranged with the central axis of the partition as the axis of symmetry; at least one of the first through-hole area and the second through-hole area is an irregular fan shape.

[0013] Further, as a preferred embodiment, the spacing between the partition portions is 7.0 mm to 10 mm.

[0014] Further, as a preferred embodiment, the spacing between two adjacent spinnerets is 6.0 mm to 11 mm along the same arrangement direction; wherein, the transverse arrangement spacing of the spinnerets arranged in the transverse direction on the spinneret plate is 3.0 to 5.5 mm; and the longitudinal arrangement spacing of the spinnerets arranged in the longitudinal direction on the spinneret plate is 6 to 9 mm.

[0015] Further preferably, the spinneret orifice includes: a first melt channel, a first gathering channel, a second gathering channel, and a second melt channel connected in sequence with their cross-sectional areas decreasing sequentially; wherein, the ratio of the cross-sectional areas of the two opposite ends of the first gathering channel is greater than the ratio of the cross-sectional areas of the two opposite ends of the second gathering channel; and the ratio of the channel length of the second melt channel to the diameter of the spinneret orifice is 2.0 to 3.5.

[0016] Further, as a preferred embodiment, the cone angle θ1 of the first converging channel is 35~50°, and the cone angle θ2 of the second converging channel is 15~30°.

[0017] Further, as a preferred embodiment, the ratio of the channel length of the spinneret to the diameter of the spinneret is 2.0 to 3.5.

[0018] Further, as a preferred embodiment, the number of spinnerets is 180-500, or the number of spinnerets is 180-300.

[0019] Further, as a preferred embodiment, the number of spinnerets is 200.

[0020] Furthermore, preferably, the density of spinnerets distributed in the longitudinal and transverse directions in the region near the partition is less than the density of spinnerets distributed in the longitudinal and transverse directions in the region away from the partition.

[0021] Further, as a preferred embodiment, in the outermost spinneret region of the first and second through-hole regions, at least some adjacent two spinnerets form an isolation zone, and the distance between these isolation zones is greater than the average distance. Furthermore, the distance between the isolation zones decreases sequentially from the outermost layer to the next Nth layer until it reaches the average distance. Here, N is a natural number.

[0022] More preferably, in this embodiment, both the first through-hole area and the second through-hole area are semi-circular, and there is a circular transition between the chord side and the side corresponding to the arc length.

[0023] Further, as a preferred embodiment, the step of pre-crystallizing polyester chips of a predetermined viscosity and then performing solid-state polymerization to obtain polymerized chips includes:

[0024] Polyester chips with a preset viscosity are pre-crystallized and heated in reverse with hot air at 160~180℃ for at least 1~5 hours while being stirred to obtain pre-crystallized chips, wherein the preset viscosity is 0.660~0.68dl / g;

[0025] The pre-crystallized slices are placed in a solid-phase polymerization tower and heated with hot nitrogen at 180~220℃ for at least 24~38 hours to obtain the polymerized thickened slices, wherein the viscosity of the polymerized thickened slices is 1.0~1.2dL / g or 1.11~1.25dL / g.

[0026] Further, as a preferred embodiment, the step of placing the polymerized thickening chips into a screw extruder for melt treatment to obtain the spinning melt includes:

[0027] Polyester chips after solid-phase polymerization are fed to a screw extruder for melt treatment to obtain the filament melt; wherein the screw diameter of the screw extruder is 125~150mm, the length-to-diameter ratio of the screw is 24~33, and the melting temperature of the screw extruder is 285~310℃.

[0028] Further, as a preferred embodiment, the filter screen has a pore diameter of 10~20μm; and the heating shroud in the spinning assembly has a temperature of 285~318℃.

[0029] Further, as a preferred embodiment, after the step of passing the filtered spinning melt through a spinneret in a preset spinning assembly to form a continuous chemical fiber filament composed of multiple fiber bundles, the method further includes:

[0030] After the continuous chemical fiber filament is subjected to slow cooling treatment and cooling molding treatment, it enters the spinning channel to obtain the filament body. The slow cooling treatment is a heat insulation cylinder device with a length of 300~600mm; the cooling method is side blowing; the temperature of the side blowing is 18~25℃, and the wind speed is 0.3~0.5m / s.

[0031] After stretching, shaping, and winding the filament body, the chemical fiber industrial filament is obtained, wherein the traction speed of the filament body is 400~600 m / min; the stretch ratio of the filament body is 5.6~6.2; the shaping temperature of the chemical fiber industrial filament is 230℃~250℃; the winding speed of the filament body is 2300~3000 m / min; and the relaxation rate of the chemical fiber industrial filament is 9.0~12.0%.

[0032] Further, as a preferred embodiment, the polyester chips include: bright polyester chips, wherein the bright polyester chips have a viscosity of 0.670 dl / g, a terminal carboxyl group -COOH content of 28 mol / t, and a diethylene glycol content of 0.9%; the chemical fiber industrial filament is polyester; the chemical fiber industrial filament is polyester.

[0033] This application also provides a chemical fiber industrial filament, which is prepared by the above-described method for preparing chemical fiber industrial filaments.

[0034] Furthermore, preferably, the parameters of the chemical fiber industrial filament include any one or a combination of two or more of the following;

[0035] The single filament fineness of the chemical fiber industrial filament is 1.5-2.5D, or the single filament fineness of the chemical fiber industrial filament is 1.5-2D, or the single filament fineness of the chemical fiber industrial filament is 2.0-2.5D.

[0036] The linear density of the aforementioned chemical fiber industrial filament is 333~1110 dtex;

[0037] The tensile strength of the chemical fiber industrial filament is greater than or equal to 7.5 cN / dtex;

[0038] The coefficient of variation of the breaking strength of the aforementioned chemical fiber industrial filament is less than or equal to 4.0%;

[0039] The breaking elongation of the chemical fiber industrial filament is 21±3%;

[0040] The dry heat shrinkage rate of the chemical fiber industrial filament under test conditions of 177°C and no load for 10 minutes was 6.5±2%.

[0041] This application also provides an airbag comprising: a fabric woven from the aforementioned chemical fiber industrial filaments.

[0042] Compared with the prior art, the beneficial effects of the present invention are mainly reflected in the following: In the process of preparing chemical fiber industrial filaments, a spinneret with a special structure is used. The number of holes in the spinneret is increased to more than 180f compared with the conventional number of holes. The spinneret holes of the spinneret are arranged in a partitioned and spaced manner. At the same time, the density of the spinneret holes in each partition is arranged from the outside to the inside, from sparse to dense. This makes the monofilaments ejected from the spinneret finer, while facilitating the blowing of cold air into the inner layer and improving the cooling effect. This can reduce the monofilament fineness (dpf) of chemical fiber industrial filaments, while avoiding the adhesion of the melt used to form a single filament bundle when it is ejected from the spinneret hole under the expansion effect, thereby reducing the amount of fuzz and the breakage rate, and improving its flexibility and foldability.

[0043] Furthermore, when the spacing of the partitions of the spinneret, i.e. the spacing of the non-porous areas, is 7.0mm to 10.0mm, it can achieve a good cooling effect and greatly reduce the amount of fuzz and the probability of adhesion.

[0044] In addition, this application uses a spinneret with a length-to-diameter ratio of 2.0-3.5 for the second melt channel, which further reduces the amount of fuzz in the chemical fiber filaments, the possibility of spinneret adhesion, and the probability of breakage.

[0045] In addition, the physical and mechanical properties of the chemical fiber industrial filaments prepared in this application, such as the filaments, are consistent with the conventional polyester standards used in mass-produced and conventional airbags. Some of the mechanical properties are superior to those of conventional polyester. Furthermore, the airbag fabric prepared using chemical fiber industrial filaments is softer and easier to fold, which can further reduce the volume of the airbag assembly. Attached Figure Description

[0046] Figure 1 This is a schematic diagram of the spinneret structure in one embodiment of the present invention;

[0047] Figure 2 is a schematic diagram of the cooling process in one embodiment of the present invention;

[0048] Figure 3 This is a schematic cross-sectional view of the spinneret in one embodiment of the present invention;

[0049] Figure 4This is a schematic diagram of the guide angle of the spinneret in one embodiment of the present invention;

[0050] Figure 5 This is a schematic diagram of the layout of the spinneret holes in a pair of proportions of the present invention;

[0051] Figure 6 This is a schematic diagram of the winding direction of the layers corresponding to the spinneret holes in a spinneret plate according to an embodiment of the present invention;

[0052] Explanation of reference numerals in the attached drawings: Spacing A of the partition zone, longitudinal spacing B1, transverse spacing B2, spinneret 1, spinneret plate 2, first through-hole area 2a, second through-hole area 2b, partition 3, first melt channel 10, first gathering channel 11, second gathering channel 12, second melt channel 14, cone angle θ1, cone angle θ2, length L1 of the second melt channel, diameter D1 of the spinneret, outermost layer Q1, next-level layer Q2. Detailed Implementation

[0053] The chemical fiber industrial filament of the present invention will now be described in more detail with reference to the schematic diagrams, which illustrate preferred embodiments of the invention. It should be understood that those skilled in the art can modify the invention described herein while still achieving its advantageous effects. Therefore, the following description should be understood as being of general knowledge to those skilled in the art and is not intended to limit the invention.

[0054] Example 1

[0055] This embodiment provides a spinneret for preparing polyester filaments, such as... Figure 1 As shown, it includes: a spinneret hole 1 opened on the spinneret plate 2, a first through hole area 2a and a second through hole area 2b having the spinneret hole 1, and a partition part 3 for separating the first through hole area 2a and the second through hole area 2b, etc.

[0056] Among them, the density of the spinneret 1 changes from sparse to dense from the outside to the inside.

[0057] By dividing the spinneret holes 1 on the spinneret plate 2 into zones and by using the distribution of the density of the spinneret holes 1 in each zone from the outside to the inside, it is possible to increase the number of holes in the spinneret plate 2 while avoiding excessive density of the spinneret holes 1. This facilitates the blowing of cold air into the inner layer and improves the cooling effect. In turn, it can reduce the dpf (dilution per filament) of chemical fiber filaments and prevent the melt used to form a single filament bundle from sticking together under the expansion effect when it is ejected from the spinneret holes 1, thereby reducing the amount of fuzz.

[0058] In detail, such as Figure 1 and Figure 5As shown, in the first through-hole region 2a and the second through-hole region 2b, the density of spinnerets 1 distributed in the longitudinal and transverse directions in the region near the partition 3 is less than the density of spinnerets 1 distributed in the longitudinal and transverse directions in the region away from the partition 3.

[0059] In addition, it is worth mentioning that, such as Figure 6 As shown, in the outermost spinneret 1 region of the first through-hole region 2a and the second through-hole region 2b, at least some adjacent spinneret 1 areas form isolation zones, and the spacing between these isolation zones is greater than the average spacing. Furthermore, as... Figure 6 As shown by the dashed line, the spacing between the isolation zones from the outermost layer Q1 to the next level layer Q2 and / or the next Nth level layer decreases sequentially until the average spacing is reached, where N is a natural number greater than 1. This layout ensures that the spinnerets 1 in each through-hole area gradually increase in density from the outside in, effectively preventing excessive density of spinnerets 1 in the outermost layer. This facilitates the inflow of cold air into the inner layer, improving cooling efficiency and preventing the melt from the single filament bundles ejected from the two outermost adjacent spinnerets 1 from sticking together under expansion, thus effectively reducing filament shearing.

[0060] In addition, it is worth mentioning that in this embodiment, the shape of each layer matches or is similar to the shape of each through-hole area, and decreases gradually from the outermost layer inward.

[0061] Specifically, as a preferred embodiment, the first through-hole area 2a and the second through-hole area 2b are symmetrically arranged about the central axis of the partition portion 3. At least one of the first through-hole area 2a and the second through-hole area 2b is an irregular fan shape.

[0062] More preferably, in this embodiment, both the first through-hole area 2a and the second through-hole area 2b are preferably semi-circular, and their chord edge, that is, one side of the non-hole area, and the side corresponding to the arc length are in a rounded transition, so as to avoid the phenomenon that the melt of the single filament bundle formed by the two adjacent spinnerets 1 in the area is prone to sticking together due to uneven cooling in the area where the chord edge and arc length are connected.

[0063] Furthermore, preferably, the spacing of the partition portions 3, for example... Figure 1 The spacing of the non-porous areas shown is 7.0mm~10mm. Furthermore, as shown in Table 1 below, this distance parameter can achieve a good cooling effect, greatly reducing the amount of fuzz and the probability of adhesion.

[0064] Further, as a preferred embodiment, the spacing between two adjacent spinnerets 1 is 6.0mm to 11mm along the same arrangement direction. Specifically, the transverse arrangement spacing B1 of the spinnerets arranged transversely on the spinneret plate 2 is 3.0mm to 5.5mm, and the longitudinal arrangement spacing B2 of the spinnerets arranged longitudinally on the spinneret plate 2 is 6 to 9mm. This is to better prevent the melt of adjacent single filament bundles from sticking together under the expansion effect when it is ejected from the spinneret hole 1, and to reduce the amount of filaments.

[0065] Further, preferably, the spinneret 1 includes: a first melt channel 10, a first gathering channel 11, a second gathering channel 12, and a second melt channel 14, which are connected in sequence and have progressively decreasing cross-sectional areas; wherein the ratio of the cross-sectional areas of the opposite ends of the first gathering channel 11 is greater than the ratio of the cross-sectional areas of the opposite ends of the second gathering channel 12. This layout allows the spinning melt to gradually reduce the channel area it flows through during ejection, which helps alleviate outlet swelling and reduces the risk of unstable spinning caused by changes in the flow rate of adjacent layers of spinning melt due to variations in the number of orifices.

[0066] In detail, the cross-sectional areas of the first melt channel 10 and the second melt channel 14 remain relatively constant, while the cross-sectional areas of the first converging channel 11 and the second converging channel 12 gradually shrink.

[0067] Furthermore, as a preferred embodiment, both the first gathering channel 11 and the second gathering channel 12 are tapered channels, and the tapered angle of the first gathering channel 11 is greater than that of the second gathering channel 12. By superimposing the tapered surfaces, the guide angle can be further reduced, the outlet swelling effect can be alleviated, and the change in the flow rate of the spinning melt between adjacent layers caused by the change in the number of holes can be further alleviated, so as to avoid the formation of unstable spinning.

[0068] Further, as a preferred embodiment, the cone angle θ1 of the first gathering channel 11 is 35~50°, and the cone angle θ2 of the second gathering channel 12 is 15~30°.

[0069] Further, as a preferred embodiment, the cone angle θ1 of the first gathering channel 11 is 45°, and the cone angle θ2 of the second gathering channel 12 is 20°. By setting the cone angles of the first gathering channel 11 and the second gathering channel 12 in coordination, the outlet swelling effect can be better mitigated, and the change in the flow rate of the adjacent two spinning melt layers caused by the change in the number of holes can be mitigated to the greatest extent, so as to better avoid the formation of unstable spinning.

[0070] Further, as a preferred option, such as Figure 3As shown, the ratio of the channel length L1 of the second melt channel 14 to the diameter D1 of the spinneret 1, i.e., the length-to-diameter ratio, is 2.0~3.5. By setting this range of length-to-diameter ratio parameters, the flow of high-viscosity melt can be made more stable, the outlet expansion phenomenon can be reduced, and the adhesion of adjacent single filament bundles of melt when ejected from the spinneret 1 under the expansion effect can be further avoided, as well as the effect of reducing the amount of filaments.

[0071] Further, preferably, the number of spinneret holes 1 is 180-500.

[0072] Example 2

[0073] This embodiment provides a method for preparing filaments for the chemical fiber industry, which includes the following steps:

[0074] Step 1: Processing high-viscosity polyester chips: First, the raw polyester chips are pre-crystallized by heating them in a counter-current manner with hot air at 163°C for 2.5 hours while stirring. Then, the chips are introduced into a solid-phase polymerization tower and heated uniformly with hot nitrogen to a temperature of 205°C for a residence time of 31 hours. This process increases the viscosity of the polyester chips after solid-phase polymerization from 0.670 dl / g to 1.15 dl / g.

[0075] Step 2: The solid-phase polymerized polyester chips are fed to the spinning screw extruder. The spinning screw extruder extrudes the melt, which is distributed to the melt pipes of each spinning box through the melt manifold to form the spinning melt. The screw diameter of the spinning screw extruder is 125mm, the length-to-diameter ratio of the screw is 28, and the melting temperature of the spinning screw is 285~310℃.

[0076] Step 3: The spinning melt enters the spinning assembly via a metering pump and is filtered through a filter screen in the spinning assembly. Then... Figure 2 The melt flow direction shown in C indicates that after melt spinning from the spinneret 2 shown in Example 1, a continuous chemical fiber filament is obtained. The aspect ratio of the spinneret 2, i.e., the ratio of the channel length L1 of the second melt channel 14 to the diameter D1 of the spinneret orifice 1, is 2.0. The number of spinneret orifices 1 is 200. The spacing of the non-perforated areas of the spinneret 2, i.e., the partitions 3, is 9 mm. The transverse spacing B1 between two adjacent spinneret orifices 1 is 4.7 mm. The longitudinal spacing B2 between two adjacent spinneret orifices 1 is 7.97 mm. The filter screen in the spinning assembly has a filter precision of 15 μm. The heating hood temperature of the spinning assembly is 285°C to maintain good heat preservation and slow cooling effects. The first convergence channel 11 and the second convergence channel 12 are tapered channels, and the tapered angle θ1 of the first convergence channel 11 is 45°, and the tapered angle θ2 of the second convergence channel 12 is 20°.

[0077] Step 4: After the continuous chemical fiber filament is slowly cooled using a slow cooling device, it is then... Figure 2 The direction of the side-blowing air shown in D is used to cool the continuous chemical fiber filament to obtain the filament body. The temperature of the side-blowing air is 19℃, the wind speed is 0.5m / s, the humidity is 60%, and the height of the heat insulation cylinder in the slow cooling device is 400mm. This greatly improves the phenomenon of high CV value and many broken filaments caused by uneven cooling of low dpf yarn.

[0078] Step 5: After the cooled filament body is fed into the spinning tunnel, it is stretched, shaped, and wound to obtain the chemical fiber industrial filament. The stretching and winding parameters are as follows: spinning with 6 heads / position, 4 positions / line, and 1 screw / line, the traction speed is 462 m / min, oil is applied to the surface of the filament body, and a two-stage stretching and one-stage shaping and relaxation method is adopted. The total stretch ratio is 5.75, the shaping temperature is 238℃, and the total relaxation rate is 9.6%.

[0079] Relevant process parameters for Example 2:

[0080] Raw materials: Polyester chips with a viscosity of 0.670 dl / g, a terminal carboxyl group -COOH content of 28 mol / t, and a diethylene glycol content of 0.9% are selected. The viscosity after SSP thickening is 1.15 dl / g.

[0081] 1. Temperature of the screw extruder (°C)

[0082] Zone 1 Zone 2 Zone 3 Zone 4 Zone 5 Zone 6 300 310 310 285 285 285

[0084] 2. Spinning temperature

[0085] 297℃

[0086] 3. Heating temperature of the heating cover

[0087] 285℃

[0088] 4. Length of heat insulation cylinder

[0089] 400mm

[0090] 5. Side-blowing cooling parameters

[0091] Wind speed: 0.5 m / s; Humidity: 60%; Wind temperature: 19℃

[0092] 6. Tensile conditions

[0093] Pre-stretch ratio: 1.03

[0094] First-order stretch ratio: 4.0

[0095] Total stretch ratio: 5.75

[0096] Stretch roller speed (m / min) Temperature (°C)

[0097] GR1462 80

[0098] GR2476 110

[0099] GR31848 114

[0100] GR42655 238

[0101] GR52400 /

[0102] Relaxation rate: 9.6%

[0103] 7. Winding speed: 2400m / min

[0104] 8. Networker pressure: 0.45 MPa.

[0105] Example 3

[0106] This embodiment provides a method for preparing filaments for the chemical fiber industry, which includes the following steps:

[0107] Step 1: Processing high-viscosity polyester chips: First, the raw polyester chips are pre-crystallized by heating them in a counter-current manner with hot air at 163°C for 2.5 hours while stirring. Then, the chips are fed into a solid-phase polymerization tower and heated uniformly with hot nitrogen to 218°C for 37 hours. This process increases the viscosity of the polyester chips after solid-phase polymerization from 0.670 dl / g to 1.15 dl / g.

[0108] Step 2, Melting: The solid-phase polymerized polyester chips are fed to the spinning screw extruder. The spinning screw extruder extrudes the melt, which is distributed to the melt pipes of each spinning box through the melt manifold to form the spinning melt. The screw diameter of the spinning screw extruder is 125mm, the length-to-diameter ratio of the screw is 28, and the melting temperature of the spinning screw is 285~310℃.

[0109] Step 3: The spinning melt enters the spinning assembly via a metering pump and is filtered through a filter screen in the spinning assembly. It is then ejected from the spinneret 2 shown in Example 1 for melt spinning, resulting in a continuous chemical fiber filament. The aspect ratio of the spinneret 2 (i.e., the ratio of the channel length L1 of the second melt channel 14 to the diameter D1 of the spinneret orifice 1) is 2.0. The number of spinneret orifices 1 is 200. The spacing between the non-perforated sections of the spinneret 2 is 9 mm. The transverse spacing B1 between two adjacent spinneret orifices 1 is 4.7 mm. The longitudinal spacing B2 between two adjacent spinneret orifices 1 is 7.97 mm. The filter screen in the spinning assembly has a filter precision of 15 μm. The heating hood temperature of the spinning assembly is 285℃ to maintain good heat preservation and slow cooling effects. The first convergence channel 11 and the second convergence channel 12 are tapered channels, and the tapered angle θ1 of the first convergence channel 11 is 45°, and the tapered angle θ2 of the second convergence channel 12 is 20°.

[0110] Step 4: After the continuous chemical fiber filament is slowly cooled using a slow cooling device, it is then... Figure 2 The direction of the side-blowing air shown in D is used to cool the continuous chemical fiber filament to obtain the filament body; wherein, the temperature of the side-blowing air is 19℃, the wind speed is 0.5m / s, the humidity is 60%, and the slow cooling treatment is a heat insulation cylinder device with a length of 400mm.

[0111] Step 5: After stretching, shaping, and winding the filament body, the chemical fiber industrial filament is obtained. The stretching and winding parameters are: spinning with 6 heads / position, 4 positions / thread, and 1 screw / thread, the traction speed is 463 meters / minute, oil is applied to the surface of the filament body, and a two-stage stretching and one-stage shaping and relaxation method is adopted. The total stretch ratio is 5.75, the shaping temperature is 235℃, and the total relaxation rate is 9.8%.

[0112] Example 3 Relevant Process Parameters

[0113] Raw materials: Polyester chips with a viscosity of 0.670 dl / g, a terminal carboxyl group -COOH content of 28 mol / t, and a diethylene glycol content of 0.9% are selected. The viscosity after SSP thickening is 1.15 dl / g.

[0114] 1. Temperature of the screw extruder (°C)

[0115] Zone 1 Zone 2 Zone 3 Zone 4 Zone 5 Zone 6 300 310 310 285 285 285

[0117] 2. Spinning temperature

[0118] 297℃

[0119] 3. Heating temperature of the heating cover

[0120] 285℃

[0121] 4. Length of heat insulation cylinder

[0122] 400mm

[0123] 5. Side-blowing cooling parameters

[0124] Wind speed: 0.5 m / s; Humidity: 60%; Wind temperature: 19℃

[0125] 6. Tensile conditions

[0126] Pre-stretch ratio: 1.03

[0127] First-order stretch ratio: 4.0

[0128] Total stretch ratio: 5.75

[0129] Stretch roller speed (m / min) Temperature (°C)

[0130] GR1 463 80

[0131] GR2 477 110

[0132] GR3 1852 114

[0133] GR4 2660 235

[0134] GR5 2400 /

[0135] Relaxation rate: 9.8%

[0136] 7. Winding speed: 2400m / min

[0137] 8. Networker pressure: 0.47 MPa.

[0138] Example 4

[0139] This embodiment four provides a method for preparing chemical fiber industrial filaments. This embodiment four is largely the same as embodiment two, except that the non-porous zone spacing of the spinneret 2 in this embodiment is 7 mm.

[0140] Example 5

[0141] This fifth embodiment provides a method for preparing chemical fiber industrial filaments. This fifth embodiment is largely the same as the second embodiment, except that the spacing between the non-porous areas of the spinneret 2 in this embodiment is 10 mm.

[0142] Example 6

[0143] This sixth embodiment provides a method for preparing chemical fiber industrial filaments. This sixth embodiment is largely the same as the second embodiment, except that the aspect ratio of the spinneret 2 in this embodiment, that is, the ratio of the channel length L1 of the second melt channel 14 to the diameter D1 of the spinneret hole 1, is 3.0.

[0144] Example 7

[0145] This embodiment seven provides a chemical fiber industrial filament, which is prepared by the chemical fiber industrial filament preparation method provided in any of the above embodiments.

[0146] Example 8

[0147] This embodiment eight provides an airbag, comprising: a fabric made of chemical fiber industrial filaments as described in embodiment seven above.

[0148] Comparative Example 1

[0149] This comparative example provides a method for preparing filaments for the chemical fiber industry, which includes the following steps:

[0150] Step 1: Processing high-viscosity polyester chips: First, the raw polyester chips are pre-crystallized. While the chips are being stirred, they are counter-currently heated with hot air at 165°C for 3 hours to pre-crystallize them. Then, they are introduced into a solid-phase polymerization tower and uniformly heated with hot nitrogen to 210°C. The residence time is 26 hours, which increases the viscosity of the polyester chips after solid-phase polymerization from 0.655 dl / g to 1.05 dl / g.

[0151] Step 2: The polyester chips after solid-phase polymerization are fed to the spinning screw extruder. The spinning screw extruder extrudes the melt, which is distributed to the melt pipes of each spinning box through the melt manifold to form the spinning melt. The screw diameter of the spinning screw extruder is 130mm, the length-to-diameter ratio of the screw is 28, and the melting temperature of the spinning screw is 293~320℃.

[0152] Step 3: The spinning melt enters the spinning assembly via a metering pump and is filtered through a filter screen within the spinning assembly. It then exits through the spinneret holes (which have no partitions and whose spinneret holes are evenly distributed within the through-hole area) for melt spinning, resulting in a continuous chemical fiber filament. The spinneret has an aspect ratio of 2.0. There are 96 spinneret holes evenly distributed on the spinneret. The filter screen in the spinning assembly has a filter resolution of 25 μm. The spacing between adjacent spinneret holes is 9 mm.

[0153] Step 4: After the chemical fiber filament continuous body is slowly cooled by the slow cooling device, it is then cooled by side blowing to obtain the filament body; wherein, the height of the heat insulation cylinder in the slow cooling device is 150mm, the cooling air is in the form of side blowing, the side blowing temperature is 18℃, the wind speed is 0.6m / s, and the humidity is 60%.

[0154] Step 5: After the cooled filament body is fed into the spinning tunnel, it is stretched, set, and wound to obtain the ordinary polyester filament. The stretching and winding parameters are as follows: spinning with 6 heads / position, 4 positions / line, and 1 screw / line, the traction speed is 500 m / min, the winding speed is 3000 m / min, a two-stage stretching and one-stage setting and relaxation method is adopted, the total stretch ratio is 5.71, the setting temperature is 242℃, and the total relaxation rate is 10.5%.

[0155] Comparative Example 1: Relevant Process Parameters

[0156] Raw materials: High-viscosity polyester chips with a viscosity of 0.670 dl / g, a terminal carboxyl group -COOH content of 15 mol / t, and a diethylene glycol content of 1.2% were selected to form polymerized and thickened chips. The viscosity after SSP thickening was 1.05 dl / B.

[0157] 1. Temperature of the screw extruder (°C)

[0158] Zone 1 Zone 2 Zone 3 Zone 4 Zone 5 Zone 6 300 300 298 295 295 295

[0160] 2. Spinning temperature

[0161] 300℃

[0162] 3. Heating temperature of the heating cover

[0163] 330℃

[0164] 4. Length of heat insulation cylinder

[0165] 150mm

[0166] 5. Side-blowing cooling parameters

[0167] Wind speed: 0.6 m / s; Humidity: 60%; Wind temperature: 19℃

[0168] 6. Tensile conditions

[0169] Pre-stretch ratio: 1.03

[0170] First-order stretch ratio: 3.4

[0171] Total stretch ratio: 5.71

[0172] Stretch roller speed (m / min) Temperature (°C)

[0173] GR1 509 90

[0174] GR2 524 123 / 125

[0175] GR3 1731 110

[0176] GR4 2905 242

[0177] GR5 2600 140

[0178] Relaxation rate: 10.5%

[0179] 7. Winding speed: 2600m / min

[0180] 8. Network pressure: 0.4 MPa

[0181] Comparative Example 2

[0182] This embodiment provides a method for preparing filaments for the chemical fiber industry, which includes the following steps:

[0183] Step 1: Processing high-viscosity polyester chips: First, the raw polyester chips are pre-crystallized. While the chips are being stirred, they are counter-currently heated with hot air at 165°C for 3 hours to pre-crystallize them. Then, they are introduced into a solid-phase polymerization tower and uniformly heated with hot nitrogen to 210°C. The residence time is 26 hours, which increases the viscosity of the polyester chips after solid-phase polymerization from 0.655 dl / g to 1.05 dl / g.

[0184] Step 2: The polyester chips after solid-phase polymerization are fed to the spinning screw extruder. The spinning screw extruder extrudes the melt, which is distributed to the melt pipes of each spinning box through the melt manifold to form the spinning melt. The screw diameter of the spinning screw extruder is 130mm, the length-to-diameter ratio of the screw is 28, and the melting temperature of the spinning screw is 293~320℃.

[0185] Step 3: The spinning melt enters the spinning assembly via a metering pump and is filtered through a filter screen within the spinning assembly. It then exits through the spinneret holes (which have no partitions and whose spinneret holes are evenly distributed within the through-hole area) for melt spinning, resulting in a continuous chemical fiber filament. The spinneret has an aspect ratio of 2.0. There are 96 spinneret holes evenly distributed on the spinneret. The filter screen in the spinning assembly has a filter resolution of 25 μm to improve the uniformity of the nascent fibers. The heating element of the spinning assembly is set to a temperature of 330℃ to maintain good heat retention.

[0186] Step 4: After the continuous chemical fiber filament is slowly cooled by the slow cooling device, it is then cooled by side blowing to obtain the filament body. The height of the heat insulation cylinder in the slow cooling device is 190mm, the cooling air is side blowing, the side blowing temperature is 18℃, the wind speed is 0.6m / s, and the humidity is 60%.

[0187] Step 5: After the cooled filament body is fed into the spinning tunnel, it is stretched, set, and wound to obtain ordinary polyester filament. The stretching and winding parameters are as follows: spinning with 6 heads / position, 4 positions / line, and 1 screw / line, the traction speed is 500 m / min, the winding speed is 2600 m / min, a two-stage stretching and one-stage setting and relaxation method is adopted, the total stretch ratio is 5.71, the setting temperature is 242℃, and the total relaxation rate is 10.5%.

[0188] Comparative Example 2: Relevant Process Parameters

[0189] Raw materials: High-viscosity polyester chips with a viscosity of 0.670 dl / g, a terminal carboxyl group -COOH content of 15 mol / t, and a diethylene glycol content of 1.2% were selected to form polymerized and thickened chips. The viscosity after SSP thickening was 1.05 dl / B.

[0190] 1. Temperature of the screw extruder (°C)

[0191] Zone 1 Zone 2 Zone 3 Zone 4 Zone 5 Zone 6 300 300 298 293 293 293

[0193] 2. Spinning temperature

[0194] 300℃

[0195] 3. Heating temperature of the heating cover

[0196] 330℃

[0197] 4. Length of heat insulation cylinder

[0198] 190mm

[0199] 5. Side-blowing cooling parameters

[0200] Wind speed: 0.6 m / s; Humidity: 60%; Wind temperature: 19℃

[0201] 6. Tensile conditions

[0202] Pre-stretch ratio: 1.03

[0203] First-order stretch ratio: 3.4

[0204] Total stretch ratio: 5.68

[0205] Stretch roller speed (m / min) Temperature (°C)

[0206] GR1509 90

[0207] GR2524 123 / 125

[0208] GR31731 110

[0209] GR42905 242

[0210] GR52600 140

[0211] Relaxation rate: 10.5%

[0212] 7. Winding speed: 2600m / min

[0213] 8. Network pressure: 0.4 MPa

[0214] Comparative Example 3

[0215] This embodiment provides a nylon filament, wherein the nylon filament is nylon 66.

[0216] Comparative Example 4

[0217] This comparative example provides a method for preparing filaments for the chemical fiber industry, which is largely the same as Comparative Example 1. The difference is that the winding speed in the comparative example is 2400 m / min, and in the process of processing high-viscosity polyester chips, the raw polyester chips are first pre-crystallized. The chips are heated counter-currently with hot air at 163°C for 2.5 hours while being stirred to allow pre-crystallization. Then, the chips are introduced into a solid-phase polymerization tower, where hot nitrogen is used to uniformly raise the temperature to 205°C, and the residence time is 31 hours, so that the viscosity of the polyester chips after solid-phase polymerization increases from 0.670 dl / g to 1.15 dl / g.

[0218] Comparative Example 5

[0219] This comparative example provides a method for preparing chemical fiber industrial filaments. This comparative example is largely the same as the above-mentioned Example 2, except that after oiling the surface of the filament body in this comparative example, the viscosity of the oil-containing filament body is 0.914 dl / g.

[0220] Comparative Example 6

[0221] This comparative example provides a method for preparing chemical fiber industrial filaments. This comparative example is largely the same as the above-mentioned Example 2, except that in this comparative example, after oiling the surface of the filament body, the viscosity of the oil-containing filament body is 0.937 dl / g.

[0222] Process parameters for the above embodiments:

[0223] Equipment: SSP chip continuous solid-state polymerization equipment; spinning equipment; FDY industrial filament spinning equipment. The testing standards for the mechanical properties of the chemical fiber industrial filaments in each embodiment and the filaments provided in each comparative example are GB / T16604.

[0224] Table 1: Mechanical properties of chemical fiber filaments prepared by spinnerets with different parameters under the same process:

[0225]

[0226] Table 2: Mechanical properties of chemical fiber filaments prepared in Examples 2 to 4:

[0227]

[0228] Table 3: Mechanical properties of the chemical fiber industrial filaments prepared in Examples 2 to 6 and the polyester filaments provided in Comparative Examples 1 to 3:

[0229]

[0230] Table 4: Comparison of data for chemical fiber industrial filaments provided in Example 2 and Comparative Example 4 under the same process parameters:

[0231]

[0232] Table 5: Comparison of data for chemical fiber industrial filaments provided in Example 2 with those in Comparative Examples 5 and 6 under the same process parameters:

[0233]

[0234] As shown in Tables 1 to 5 above, the chemical fiber filaments prepared in the above embodiments, due to the use of a specially constructed spinneret, have a spinneret with more than 180f holes, or 180~240f holes, especially more than 192 holes. By partitioning the spinneret holes into different areas, and by utilizing the distribution of the spinneret hole density from the outside to the inside within each partition, excessively dense spinneret hole arrangement can be avoided (especially in the area near the partition where there are no holes). This increases the number of spinneret holes while facilitating the cooling effect during the process of the spinning melt forming the filament body through the spinneret holes. The cooling effect is improved by allowing cold air to be blown into the inner layer of the filament body forming each single filament bundle, thereby reducing the single filament fineness of the chemical fiber filaments and avoiding the need for excessively dense spinneret holes to form single filament bundles. When the filament melt is ejected from the spinneret, it adheres under the effect of expansion, which reduces the amount of filaments and the breakage rate, while maintaining good mechanical properties. For example, when the hole spacing is 9-10 mm, its breaking strength can reach 7.5 cN / dtex, and some can reach more than 7.9 cN / dtex. The dry heat shrinkage rate reaches more than 6%, the coefficient of variation of breaking strength is controlled within 4.0%, and the amount of filaments is controlled within 16 PPM. This can greatly reduce the phenomena of breakage and excessive filaments, thereby improving the impact resistance and air tightness of the fabric woven from the chemical fiber industrial filament. Furthermore, the chemical fiber industrial filament prepared by the above embodiment can also improve the softness and foldability of the woven fabric, so that the airbags made from the fabric, such as automotive airbags, are softer and have good foldability.

[0235] Furthermore, comparing the experimental data provided in Examples 2 to 5 and Comparative Examples 1 and 2, it can be seen that setting the filter screen precision to within 20 μm, such as 15 μm, is beneficial to improving the filtration precision, increasing the spinning pressure, and making the fine flow of melt flow out more smoothly, so as to facilitate continuous spinning and improve the uniformity of spun fibers.

[0236] Furthermore, while controlling the slow cooling time of the spinning melt using the aforementioned heat-insulating cylinder, setting the heating hood temperature to 280-320℃, such as 285℃, serves two purposes: firstly, it protects the spinneret temperature and reduces the impact of the airflow below on the spinneret and the unsolidified spinning melt; secondly, it delays cooling, allowing the filament body used to form low dpf (1.5 dtex~2.5 dtex) chemical fiber filaments to complete spinning and stretching before the melt solidifies. This facilitates the formation of extended macromolecular chains, uniform orientation of each part, and variable length, improving the breaking elongation of individual fiber bundles. When the heating hood temperature is below 280℃ or above 320℃, the strength of the low dpf chemical fiber filaments prepared through the above steps cannot meet the design requirements, and the filaments cannot meet the requirements of softness and foldability for airbag products.

[0237] Comparing the experimental data provided in Example 2 and Comparative Example 4 in Table 4, it can be seen that the chemical fiber filaments prepared using a spinneret with a viscosity of 1.15 dl / g and a common structure (e.g., 96 spinneret holes), i.e., a spinneret without a non-porous zone and with uniformly distributed spinneret holes, even with existing processes, have a breaking strength that is difficult to reach above 7.2 cN / dtex, and a dry heat shrinkage rate that is also difficult to reach above 6%. These results fail to meet the physical-mechanical performance indicators of the chemical fiber filaments provided in Examples 2 and 3. Furthermore, the chemical fiber filaments provided in Examples 2 and 3 can achieve a breaking strength of above 7.5 cN / dtex and a dry heat shrinkage rate of above 6% even with a further reduction in dpf (e.g., 200 spinneret holes), thus better meeting the physical-mechanical performance requirements for airbag design.

[0238] As can be seen from the experimental data in Table 4 above, the combination of process parameters and specially designed spinneret structure involved in Examples 2 to 8 can achieve good physical and mechanical properties in the prepared chemical fiber industrial filaments. It also achieves good mechanical properties while reducing filament quantity and breakage rate at low dpf (e.g., less than 3 dtex), such as a tensile strength of 7.6 cN / dtex or higher, with some reaching 7.8 cN / dtex or higher, and dry heat shrinkage rate of 6.2% or higher, with some even reaching 6.3% or higher. Furthermore, the physical and mechanical properties and filament quantity of the prepared chemical fiber industrial filaments are consistent with the standards of conventional polyester used in mass-produced airbags, and some indicators even surpass the mechanical properties of conventional polyester, as shown in Table 3. The mechanical properties are comparable to or comparable to those of Nylon 66, thus providing a good alternative to Nylon 66 and reducing costs.

[0239] Comparative analysis of the experimental data provided in Comparative Examples 5 and 6 and Example 2 in Table 5 shows that by adjusting the screw temperature, for example, reducing the temperature of the last three zones of the screw extruder (i.e., the temperature of the last three zones is lower than that of the first three zones, and the temperature difference reaches more than 10 degrees Celsius, or even more than 15 degrees Celsius), it is possible to increase the viscosity of the oil-containing filament under low dpf conditions, such as when the spinneret has more than 180 holes and the single filament fineness is less than 2.5 dtex. This allows the viscosity of the oil-containing filament of the aforementioned chemical fiber industrial filament to be controlled at greater than or equal to 0.950 dl / g, thereby better preventing single filament breakage during subsequent stretching, winding, and setting processes. Consequently, it also helps to avoid an increase in fuzz in subsequent weaving processes, achieving low fuzz content in the product and improving its various mechanical properties.

[0240] The above are merely preferred embodiments of the present invention and do not constitute any limitation on the present invention. Any equivalent substitutions or modifications made by those skilled in the art to the technical solutions and content disclosed in the present invention without departing from the scope of the present invention shall be deemed to have remained within the protection scope of the present invention.

Claims

1. A process for the production of a filament for the textile industry, characterized in that, The application relates to a method for preparing a chemical fiber industrial filament. The polyester chip with preset viscosity is pre-crystallized, and then solid-phase polymerization treatment is conducted to obtain a polymerized tackifying chip; The step of pre-crystallizing the polyester chip with preset viscosity and then conducting solid-phase polymerization treatment to obtain a polymerized tackifying chip comprises the following steps: pre-crystallizing the polyester chip with preset viscosity, and using hot air with a temperature of 160-180 DEG C to reversely heat the polyester chip for at least 1-5 hours in a stirring state to obtain a pre-crystallized chip, wherein the preset viscosity is 0.660-0.68 dl / g; and placing the pre-crystallized chip in a solid-phase polymerization tower, and heating the pre-crystallized chip by hot nitrogen gas at a temperature of 180-220 DEG C for at least 24-38 hours to obtain the polymerized tackifying chip, wherein the viscosity of the polymerized tackifying chip is 1.0-1.2 dL / g; The polymerized tackifying chip is placed into a screw extruder for melting treatment to obtain a spinning melt; The spinning melt is filtered through a filter screen in a spinning assembly; The filtered spinning melt is formed into a chemical fiber filament continuum composed of a plurality of fiber bundles through a spinneret in a preset spinning assembly, wherein the spinneret comprises a first through-hole area and a second through-hole area with spinneret holes and a partition part for separating the first through-hole area and the second through-hole area, and the density of the spinneret holes gradually increases from outside to inside. The spinneret hole comprises a first melt channel, a first converging channel, a second converging channel and a second melt channel which are sequentially connected and have cross-sectional areas of the channels sequentially decreasing; the cross-sectional area ratio of the first converging channel at the opposite ends is greater than that of the second converging channel; the ratio of the channel length of the second melt channel to the diameter of the spinneret hole is 2.0-3.5; the taper angle of the first converging channel is 35-50 DEG, and the taper angle of the second converging channel is 15-30 DEG. The parameters of the chemical fiber industrial filament include any one or a combination of two or more of the following parameters. The filament fineness of the chemical fiber industrial filament is 1.5-2.5D. The linear density of the chemical fiber industrial filament is 333-1110 dtex. The breaking strength of the chemical fiber industrial filament is greater than or equal to 7.5 cN / dtex. The coefficient of variation of the breaking strength of the chemical fiber industrial filament is less than or equal to 4.0%. The breaking elongation of the chemical fiber industrial filament is 18-24%. The dry heat shrinkage rate of the chemical fiber industrial filament under the test condition of 177 DEG C and no load for 10 minutes is 6.5+ / -2%.

2. The method of claim 1, wherein the method further comprises the step of: The first through-hole area and the second through-hole area are symmetrically arranged with the central axis of the partition part as the axis of symmetry; and at least one of the first through-hole area and the second through-hole area is an irregular sector.

3. The method of claim 1, wherein the method further comprises the step of: The density of the spinneret holes distributed along the longitudinal and transverse directions in the area close to the partition part is less than that of the spinneret holes distributed along the longitudinal and transverse directions in the area away from the partition part. ​ 4. The method of claim 1, wherein the method further comprises the step of: The spacing of the partition part is 7.0 mm-10 mm.

5. The method of claim 1, wherein the step of forming the continuous filament comprises the step of: extruding the continuous filament from the die. The interval between two adjacent spinnerets is 6.0mm-11mm in the same arrangement direction; wherein the transverse arrangement interval of the spinnerets arranged in the transverse direction on the spinneret is 3.0-5.5mm; and the longitudinal arrangement interval of the spinnerets arranged in the longitudinal direction on the spinneret is 6-9mm.

6. The method of claim 1, wherein the step of forming the continuous filament comprises the step of: extruding the continuous filament from the die. The number of the spinnerets is 180-500.

7. The method of claim 6, wherein the step of forming the continuous filament is performed by a melt spinning process. The number of the spinnerets is 180-300.

8. The method of claim 6, wherein the step of forming the continuous filament is performed by a melt spinning process. The number of the spinnerets is 200.

9. The method of claim 1, wherein the method further comprises the step of: The step of placing the polymerized and tackified chip into the screw extruder for melting treatment to obtain the spinning melt comprises: ​ The polyester chip after solid-phase polymerization is transported to the screw extruder for melting treatment to obtain the spinning melt; wherein the screw diameter of the screw extruder is 125-150mm, the screw length-diameter ratio is 24-33, and the melting temperature of the screw extruder is 285-310℃.

10. The method of claim 1, wherein the method further comprises the step of: The filter hole diameter of the filter screen is 10-20μm; and the temperature of the heating cover in the spinning assembly is 280-318℃. ​ 11. The method of claim 1, wherein the method further comprises the step of: The step of forming the chemical fiber filament continuum composed of a plurality of fiber bundles through the spinneret in the preset spinning assembly after the filtered spinning melt is still comprises: ​ After the slow cooling treatment and the cooling forming treatment of the chemical fiber filament continuum, the filament body is obtained in the spinning duct, wherein the slow cooling treatment is a heat insulation cylinder device with a length of 300-600mm; the cooling form is lateral air blowing; the temperature of the lateral air blowing is 18-25℃, and the wind speed is 0.3-0.5m / s; After the stretching setting and the winding treatment of the filament body, the chemical fiber industrial filament is obtained, wherein the drawing speed of the filament body is 400-600m / min; the stretching ratio of the filament body is 5.6-6.2; the setting temperature of the chemical fiber industrial filament is 230-250℃; the winding speed of the filament body is 2300-3000m / min; and the relaxation rate of the chemical fiber industrial filament is 9.0-12.0%.

12. The method of claim 4, wherein the method further comprises the step of: The polyester chip comprises a bright polyester chip, wherein the viscosity of the bright polyester chip is 0.670dl / g, the carboxyl end group-COOH content is 28mol / t, and the diethylene glycol content is 0.9%; and the chemical fiber industrial filament is polyester. ​ 13. A man-made industrial filament, characterized by, The chemical fiber industrial filament is prepared by the preparation method of any one of claims 1-12.

14. An airbag, characterized by Comprise: The fabric woven by the chemical fiber industrial filament of claim 13.

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