# Patent

## Title
Manufacturing method for U-bolts

## Abstract

This is a continuation of application Ser. No. 08/538,695, filed Oct. 3, 1995, now abandoned, which is a continuation-in-part of application Ser. No. 08/435,065, filed May 8, 1995, now abandoned.

## Background
This invention relates to the spinning of synthetic polymeric yarns. In a specific embodiment, the invention relates to spinning poly(trimethylene terephthalate) into yarn suitable for carpets.

Polyesters prepared by condensation polymerization of the reaction product of a diol with a dicarboxylic acid can be spun into yarn suitable for carpet fabric. U.S. Pat. No. 3,998,042 describes a process for preparing poly(ethylene terephthalate) yarn in which the extruded fiber is drawn at high temperature (160.degree. C.) with a steam jet assist, or at a lower temperature (95.degree. C.) with a hot water assist. Poly(ethylene terephthalate) can be spun into bulk continuous filament (BCF) yarn in a two-stage drawing process in which the first stage draw is at a significantly higher draw ratio than the second stage draw. U.S. Pat. No. 4,877,572 describes a process for preparing poly(butylene terephthalate) BCF yarn in which the extruded fiber is drawn in one stage, the feed roller being heated to a temperature 30.degree. C. above or below the Tg of the polymer and the draw roller being at least 100.degree. C. higher than the feed roll. The application of conventional polyester spinning processes to prepare poly(trimethylene terephthalate) BCF results in yarn which is of low quality and poor consistency. It would be desirable to have a process for preparing high-quality BCF carpet yarn from poly(trimethylene terephthalate).

It is therefore an object of the invention to provide a process for preparing high-quality bulk continuous filament yarn from poly(trimethylene terephthalate).

According to the invention, poly(trimethylene terephthalate) is formed into a bulk continuous filament yarn by a process comprising: the range of about 240.degree. to about 280.degree. C. to produce a plurality of spun filaments; to about 2 in a first drawing stage defined by at least one feed roller and at least one first draw roller, each of said at least one feed roller operated at a temperature less than about 100.degree. C. and each of said at least one draw roller heated to a temperature greater than the temperature of said at least one feed roller and within the range of about 50 to about 150.degree. C.; 2.2 times that of the first draw ratio in a second drawing stage defined by said at least one first draw roller and at least one second draw roller, each of said at least one second draw roller heated to a temperature greater than said at least one first draw roller and within the range of about 100 to about 200.degree. C.; and

The process may optionally include texturing the drawn yarn prior to or after winding step (f).

The process of the invention permits the production of poly(trimethylene terephthalate) bulk continuous filament yarn suitable for high-quality carpet.

FIG. 1 is a schematic diagram of one embodiment of the invention yarn preparation process.

FIG. 2 is a schematic diagram of a second embodiment of the invention process.

The fiber-spinning process is designed specifically for poly(trimethylene terephthalate), the product of the condensation polymerization of the reaction product of trimethylene diol (also called "1,3-propane diol") and a terephthalic acid or an ester thereof, such as terephthalic acid and dimethyl terephthalate. The poly(trimethylene terephthalate) may be derived from minor amounts of other monomers such as ethane diol and butane diol as well as minor amounts of other diacids or diesters such as isophthalic acid. Poly(trimethylene terephthalate) having an intrinsic viscosity (i.v.) within the range of about 0.8 to about 1.0 dl/g, preferably about 0.86 to about 0.96 dl/g (as measured in a 50/50 mixture of methylene chloride and trifluoroacetic acid at 30.degree. C.) and a melting point within the range of about 215 to about 230.degree. C. is particularly suitable. The moisture content of the poly(trimethylene terephthalate) should be less than about 0.005% prior to extrusion. Such a moisture level can be achieved by, for example, drying polymer pellets in a dryer at 150-180.degree. C. until the desired dryness has been achieved.

One embodiment of the invention process can be described by reference to FIG. 1. Molten poly(trimethylene terephthalate) which has been extruded through a spinneret into a plurality of continuous filaments 1 at a temperature within the range of about 240 to about 280.degree. C., preferably about 250 to about 270.degree. C., and then cooled rapidly, preferably by contact with cold air, is converged into a multifilament yarn and the yarn is passed in contact with a spin finish applicator, shown here as kiss roll 2. Yarn 3 is passed around denier control rolls 4 and 5 and then to a first drawing stage defined by feed roll 7 and draw roll 9. Between rolls 7 and 9, yarn 8 is drawn at a relatively low draw ratio, within the range of about 1.01 to about 2, preferably about 1.01 to about 1.35. Roller 7 is maintained at a temperature less than about 100.degree. C., preferably within the range of about 40 to about 85.degree. C. Roller 7 can be an unheated roll, in which case its temperature of operation will be somewhat elevated (30-45.degree. C.) due to friction and the temperature of the spun fiber. Roller 9 is maintained at a temperature within the range of about 50 to about 150.degree. C., preferably about 90 to about 140.degree. C.

Drawing speeds of greater than 1000 m/min. are possible with the invention process, with drawing speeds greater than 1800 m/min. desirable because of the high tenacity of the resulting yarn.

Drawn yarn 10 is passed to a second drawing stage, defined by draw rolls 9 and 11. The second-stage draw is carried out at a relatively high draw ratio with respect to the first-stage draw ratio, generally at least about 2.2 times that of the first stage draw ratio, preferably at a draw ratio within the range of about 2.2 to about 3.4 times that of the first stage. Roller 11 is maintained at a temperature within the range of about 100 to about 200.degree. C. In general, the three rollers will be sequentially higher in temperature. The selected temperature will depend upon other process variables, such as whether the BCF is made with separate drawing and texturing steps or in a continuous draw/texturing process, the effective heat transfer of the rolls used, residence time on the roll, and whether there is a second heated roll upstream of the texturing jet. Drawn fiber 12 is passed in contact with optional relax roller 13 for stabilization of the drawn yarn. Stabilized yarn 14 is passed to optional winder 15 or is sent directly to the texturing process.

The drawn yarn is bulked by suitable means such as a hot air texturing jet. The preferred feed roll temperature for texturing is within the range of about 150 to about 220.degree. C. The texturing air jet temperature is generally within the range of about 150 to about 210.degree. C., and the texturing jet pressure is generally within the range of about 50 to about 120 psi to provide a high-bulk BCF yarn. Wet or superheated steam can be substituted for hot air as the bulking medium.

FIG. 2 shows a second embodiment of the two-stage drawing process showing texturing steps downstream of the drawing zone. Molten poly(trimethylene terephthalate) is extruded through spinneret 21 into a plurality of continuous filaments 22 and is then quenched by, for example, contact with cold air. The filaments are converged into yarn 24 to which spin finish is applied at 23. Yarn 27 is advanced to the two-stage draw zone via rolls 25 and 26, which may be heated or non-heated.

In the first draw stage, yarn 31 is drawn between feed roll 28 and draw roll 29 at a draw ratio within the range of about 1.01 and about 2. Drawn yarn 32 is then subjected to a second draw at a draw ratio at least about 2.2 times the first draw ratio, preferably a draw ratio within the range of about 2.2 to about 3.4 times that of the first draw. The temperature of roll 28 is less than about 100.degree. C. The temperature of draw roll 29 is within the range of about 50 to about 150.degree. C. The temperature of draw roll 30 is within the range of about 100 to about 200.degree. C. Drawn yarn 33 is advanced to heated rolls 34 and 35 to preheat the yarn for texturing. Yarn 36 is passed through texturing air jet 37 for bulk enhancement and then to jet screen cooling drum 38. Textured yarn 39 is passed through tension control 40, 41 and 42 and then via idler 43 to optional entangler 44 for yarn entanglement if desired for better processing downstream. Entangled yarn 45 is then advanced via idler 46 to an optional spin finish applicator 47 and is then wound onto winder 48. The yarn can then be processed by twisting, texturing and heat-setting as desired and tufted into carpet as is known in the art of synthetic carpet manufacture.

Poly(trimethylene terephthalate) yarn prepared by the invention process has high bulk (generally within the range of about 20 to about 45%, preferably within the range of about 26 to about 35%), resilience and elastic recovery, and is useful in the manufacture of carpet, including cut-pile, loop-pile and combination-type carpets, mats and rugs. Poly(trimethylene terephthalate) carpet has been found to exhibit good resiliency, stain resistance and dyability with disperse dyes at atmospheric boil with optional carrier.

Effect of Intrinsic Viscosity on Poly(trimethylene terephthalate) Fiber Drawing

Four poly(trimethylene terephthalate) polymers having intrinsic viscosities of 0.69, 0.76, 0.84 and 0.88 dl/g, respectively, were each spun into 70 filaments with trilobal cross-sections using a spinning machine having a take-up and drawing configuration as shown in FIG. 1. Roll 1 (see detail below) was a double denier control roll; roll 2 ran at a slightly higher speed to maintain a tension and act as a feed roll for drawing. First stage drawing took place between rolls 2 and 3, and second-stage drawing took place between rolls 3 and 4. The drawn yarn contacted relax roll 5 prior to wind-up. The spin finish was a 15% Lurol PF 4358-15 solution from G. A. Goulston Company applied with a kiss roll.

Fiber extrusion and drawing conditions for each polymer were as follows: Extrusion Conditions Units ______________________________________ Polymer IV (dl/g):     0.84, 0.88 0.69, 0.76 Extruder Temp. Profile: Zone 1        .degree. C. 230        225 Zone 2        .degree. C. 250        235 Zone 3        .degree. C. 250        235 Zone 4        .degree. C. 250        235 Melt Temp.    .degree. C. 255        240 Extrusion Pack Pressure psi      1820-2820  500-1300 Denier Control Roll Speed m/min.   225        220 ______________________________________ Fiber Drawing Conditions ______________________________________ Polymer IV (dl/g) 0.88   0.84     0.76 0.69 Roll Temp.: .degree. C. Roll 2          80     80       80   80 Roll 3          95     95       95   95 Roll 4          155    155      155  155 Roll 5          RT     RT       RT   RT Roll Speeds: m/min. Roll 2          230    230      230  230 Roll 3          310    310      404  404 Roll 4          1020   1165     1089 1089 Roll 5          1035   1102     1075 1075 First Stage Draw Ratio 1.35   1.35     1.76 1.76 Second Stage Draw Ratio 3.29   3.29     2.70 2.70 ______________________________________ ______________________________________ I.V.   Yarn Count   Tenacity % Run     (dl/g) (den.)       (g/den.) Elongation ______________________________________ 1       0.69   1182         1.51   70.7 2       0.76   1146         1.59   79.7 3       0.84   1167         2.03   89.0 4       0.88   1198         2.24   67.5 ______________________________________

Poly(trimethylene terephthalate) of intrinsic viscosities 0.69 and 0.76 (Runs 1 and 2) gave yarn of inferior tensile properties compared with the yarn of Runs 3 and 4. These polymers were re-spun at a lower extruder temperature profile. Although they could be spun and drawn, the fibers had high die swell. When the fiber cross-sections were examined with an optical microscope, the 0.69 i.v. fibers swelled to a point that they were no longer trilobal in shape and resembled delta cross-sections. They also had relatively low tenacity.

Two-Stage Drawing of PTT Fibers

0.88 i.v. poly(trimethylene terephthalate) was extruded into 72 filaments having trilobal cross-section using a fiber-spinning machine having take-up and drawing configurations as in Example 1. Spin finish was applied as in Example 1. Extrusion and drawing conditions were as follows. Extrusion Conditions Extruder Temperature Profile: Units ______________________________________ Zone 1              .degree. C. 230 Zone 2              .degree. C. 260 Zone 3              .degree. C. 260 Zone 4              .degree. C. 260 Melt Temp.          .degree. C. 265 Denier Control Roll Speed m/min.  230 ______________________________________ Fiber Drawing Conditions Runs Units 5    6    7    8    9    10   11 __________________________________________________________________________ Roll 2 Temp./Speed .degree. C./m/min 80/235 80/235 100/235 100/235 100/235 100/235 100/235 Roll 3 Temp./Speed .degree. C./m/min 90/317 100/286 100/817 100/817 100/817 100/993 100/945 Roll 4 Temp./Speed .degree. C./m/min 155/1123 100/1021 155/1047 140/1103 140/1145 130/1044 140/996 Roll 5 Temp./Speed .degree. C./m/min RT/1096 RT/1011 RT/1029 RT/1082 RT/1134 RT/1019 RT/981 1st Stage Draw Ratio 1.35 1.22 3.48 3.48 3.48 4.23 4.02 2nd Stage Draw Ratio 3.55 3.57 1.28 1.35 1.40 1.05 1.05 Total Draw Ratio 4.79 4.36 4.45 4.70 4.87 4.44 4.22 Yarn Count, den. den.  1225 1281 1275 1185      1210 1288 Tenacity, g/den. g/den. 1.95 1.95 1.61 1.32      1.85 1.11 Elongation %     55   75   70   76        78   86 __________________________________________________________________________

It was observed during spinning and drawing that, when the first-stage draw ratio (between rolls 2 and 3) was less than about 1.5, as in Runs 5 and 6, there were fewer broken filaments and the tenacities of the filaments were generally higher than when first-stage draw was higher than about 1.5. When the first-stage draw was increased to greater than 3 (Runs 7, 8, 9, 10, and 11), it was observed that the fibers had a white streaky appearance, the threadlines were loopy, and there were frequent filament wraps on the draw rolls. The process was frequently interrupted with fiber breaks.

Spinning, Drawing and Texturing Poly(trimethylene terephthalate) BCF to High Bulk.

The extrusion conditions in this experiment were the same as in Example 2. The fibers were spun, drawn and wound as in Example 1. They were then textured by heating the fibers on a feed roll and exposing the fibers to a hot air jet. The textured fibers were collected as a continuous plug on a jet-screen cooling drum. Partial vacuum was applied to the drum to pull the ambient air to cool the yarns and keep them on the drum until they were wound. The yarns were air entangled between the drum and the winder. The feed roll and texturizer air jet temperatures were kept constant, and the air jet pressure was varied from 50 to 100 psi to prepare poly(trimethylene terephthalate) BCF of various bulk levels.

Drawing and texturing conditions were as follows. Drawing Conditions Rolls       Temperature, .degree. C. Speed, m/min. ______________________________________ Roll 1      RT          225 Roll 2      80          230 Roll 3      95          264 Roll 4      90          1058 Roll 5      110         1042 ______________________________________ Texturing Conditions ______________________________________ Feed Roll Temperature, .degree. C. 180 Feed Roll Speed, m/min. 980 Air Jet Temperature, .degree. C. 180 Interlacing Pressure, psi 10 ______________________________________

Yarn bulk and shrinkage were measured by taking 18 wraps of the textured yarn in a denier creel and tying it into a skein. The initial length L.sub.0 of the skein was 22.1 inches in English unit creel. A 1 g weight was attached to the skein and it was hung in a hot-air oven at 130.degree. C. for 5 minutes. The skein was removed and allowed to cool for 3 minutes. A 50 g weight was then attached and the length L.sub.1 was measured after 30 seconds. The 50 g weight was removed, a 10 Lb weight was attached, and the length L.sub.2 was measured after 30 seconds. Percent bulk was calculated as (L.sub.0 -L.sub.1)/L.sub.0 .times.100% and shrinkage was calculated as (L.sub.0 -L.sub.2)/L.sub.0 .times.100%. Results are shown in Table ______________________________________ Package No. Yarn Count, den. % Bulk  % Shrinkage ______________________________________ T50       1437          32.6    3.6 T60       1406          35.7    2.7 T70       1455          39.4    3.2 T80       1500          38.0    3.6 T90       1525          37.6    4.1 T100      1507          38.0    3.6 ______________________________________

The experiment showed that poly(trimethylene terephthalate) BCF can be textured to high bulk with a hot air texturizer.

Carpet Resiliency Comparison

Poly(trimethylene terephthalate) BCF yarns were made in two separate steps: (1) spinning and drawing set-up as in Example 1 and (2) texturing. Extrusion, drawing and texturing conditions for the poly(trimethylene terephthalate) yarns were as follows. Extrusion Conditions Extruder Temperature Units ______________________________________ Zone 1             .degree. C. 240 Zone 2             .degree. C. 255 Zone 3             .degree. C. 255 Zone 4             .degree. C. 255 Melt Temperature   .degree. C. 260 Pack Pressure      psi    1830 ______________________________________ Units ______________________________________ Drawing Conditions Roll 1 Temp.    .degree. C./m/min. RT/223 Roll 2 Temp.    .degree. C./m/min. 80/230 Roll 3 Temp.    .degree. C./m/min. 95/288 Roll 4 Temp.    .degree. C./m/min. 150/1088 Roll 5 Temp.    .degree. C./m/min. RT/1000 Texturing Conditions Feed Roll Temp. .degree. C. 180 Feed Roll Speed m/min.    980 Air Jet Temp.   .degree. C. 180 Air Jet Pressure psi       90 Interlacing Pressure psi       10 ______________________________________

The yarn produced was 1150 denier with 2.55 g/den tenacity and 63% elongation. The textured yarn was twisted, heat set as indicated, and tufted into carpets. Performances of the poly(trimethylene terephthalate) carpets were compared with a commercial 1100 denier nylon 66 yarn. Results are shown in Table ______________________________________ Accelerated % Loss Heat     Floor   in Pile Twist/   Setting  Traffic Thick- Run         Inch     Conditions Rating  ness ______________________________________ 12 (Poly(trimethylene 4.5 .times. 4.5 270.degree. F. 3.75    2.4 terephthalate)       Autoclave 13 (Poly(trimethylene 4.5 .times. 4.5 180.degree. C. 3.5     7.1 terephthalate)       Seussen 14 (Poly(trimethylene 5.0 .times. 5.0 270.degree. F. 3.75    1.7 terephthalate)       Autoclave 15 nylon 66 4.0 .times. 4.0 270.degree. F. 3.0     6.4 Autoclave 16 nylon 66 4.0 .times. 4.0 190.degree. C. 3.5     4.5 Seussen ______________________________________

The heat-set yarns were tufted into 24 oz. cut-pile Saxony carpets in 1/8" gauge, 9/16" pile height, and dyed with disperse blue 56 (without a carrier) at atmospheric boil into medium blue color carpets. Visual inspection of the finished carpets disclosed that the poly(trimethylene terephthalate) carpets (Runs 12, 13 and 14) had high bulk and excellent coverage which were equal to or better than the nylon controls (Runs 15 and 16). Carpet resiliency was tested in accelerated floor trafficking with 20,000 footsteps. The appearance retention was rated 1 (severe change in appearance), 2 (significant change), 3 (moderate change), 4 (slight change) and 5 (no change). As can be seen in Table 3, the poly(trimethylene terephthalate) carpets were equal to or better than the nylon 66 controls in the accelerated walk tests and in percent thickness loss.

One-Step Processing of Poly(trimethylene terephthalate) BCF Yarn from Spinning to Texturing

Poly(trimethylene terephthalate) (i.v. 0.90) was extruded into 72 trilobal cross-section filaments. The filaments were processed on a line as shown in FIG. 2 having two cold rolls, three draw rolls and double yarn feed rolls prior to texturing. The yarns were textured with hot air, cooled in a rotating jet screen drum and wound up with a winder. Lurol NF 3278 CS (G. A. Goulston Co.) was used as the spin finish. Texturing conditions were varied to make poly(trintethylene terephthalate) BCF yarns having different bulk levels. Extrusion, drawing, texturing and winding conditions were as follows. Extrusion Conditions Extruder Temperature Profiles Units ______________________________________ Zone 1               .degree. C. 240 Zone 2               .degree. C. 260 Zone 3               .degree. C. 260 Zone 4               .degree. C. 265 Melt Temperature     .degree. C. 265 Pump Pressure        psi    3650 ______________________________________ Drawing Conditions Temperature .degree. C. Speed, m/min. ______________________________________ Cold Roll 1  RT          211 Cold Roll 2  RT          264 Draw Roll 1  50          290 Draw Roll 2  90          330 Draw Roll 3  110         1100 ______________________________________

The yarns were twisted, heat set and tufted into carpets for performance evaluation. Results are shown in Table 4. __________________________________________________________________________ Sample Feed Roll Texturizing Texturizing Jet Yarn Count,     Accelerated Walk Number Temp, .degree. C. Jet Temp., .degree. C. Press., psi den.  % Bulk % Shrinkage Test Rating __________________________________________________________________________ 1    150   180     70    1490  19.2 1.58  3.25 2    150   180    110    1420  26  1.59  3.5 3    150   200    110    1546  30.5 1.59  3.0 4    180   180     70    1429  24.6 2.04  3.0 5    180   180    110    1496  29.8 1.81  3.5 6    180   200     70    1475  26.5 1.36  2.75 7    180   200    110    1554  32.8 0.86  3.0 8    150   190     90    1482  26  2.31  3.25 9    180   190     90    1430  29  1.58  3.5 10   165   190     90    1553  29  2.26  3.75 Nylon 6                                  3.5 Nylon 66                                 3.5 __________________________________________________________________________

Effects of Draw Ratio and Roll Temperature on Yarn Properties

Poly(trimethylene terephthalate) (0.90 i.v.) was spun into 72 filaments with trilobal cross-sections using a machine as described in Example 5. Extrusion conditions were as follows. Extrusion Conditions Extruder Temperature Profiles Units ______________________________________ Zone 1               .degree. C. 240 Zone 2               .degree. C. 260 Zone 3               .degree. C. 260 Zone 4               .degree. C. 260 Melt Temperature     .degree. C. 260 ______________________________________

The poly(trimethylene terephthalate) BCF yarns and commercial nylon 6 and 66 yarns were tufted into 32 oz. 5/32 gauge cut-pile Saxony carpets having 20/32" pile height. They were walk-tested with 20,000 footsteps accelerated floor trafficking for resiliency and appearance retention comparisons. Roll conditions and results are shown in Table 5.

Use of Low First-Stage Draw Ratio

Poly(trimethylene terephthalate) (0.9 i.v.) was spun into 69 filaments with trilobal cross-sections using a drawing and texturing configuration similar to that shown in FIG. 1, with the yarn passing via unheated haul-off Roll 1, first-stage draw between Roll 1 and draw Roll 2, and second-stage draw between Roll 2 and dual Roll 3. The drawn yarns were then textured, relaxed and wound up. Extrusion conditions were as follows. __________________________________________________________________________ Sample:       1   2   3   4   5   nylon 6 nylon 66 __________________________________________________________________________ Roll 1 Temp. .degree. C. 50  50  50  50  50 Roll 2 Temp. .degree. C. 90  90  90  90  90 Roll 3 Temp. .degree. C. 110 110 110 150 150 Roll 1 Speed m/min. 290 290 290 290 290 Roll 2 Speed m/min. 330 330 330 330 330 Roll 3 Speed m/min. 1000 1100 1150 1100 1000 Draw Ratio    3.45 3.79 3.97 3.97 3.45 Feed Roll Temp. .degree. C. 165 165 165 165 165 Feed Roll speed m/min. 1000 1100 1150 1100 1000 Texturing Jet Temp. .degree. C. 190 190 190 190 190 Texturing Jet Pressure psi 90  90  90  90  90 Interlacing Pressure psi 30  30  30  30  30 Bulk      %   26.1 31.6 31.9 35.8 33 Shrinkage %   1.75 2.04 2.13 2.26 1.92 Walk Test Rating 4.0 3.5 3.5 3.5 3..5 3.5 3.5 __________________________________________________________________________ Extrusion Conditions Extruder Temp. Profiles Trial 1 Trial 2 ______________________________________ Zone 1             230.degree. C. 230 Zone 2             260     245 Zone 3             260     255 Zone 4             260     255 ______________________________________

The speed and temperature of the rolls, texturing conditions and yarn tensile properties are shown in Table 6. In Trial 1, the relax roll was a single roll with a follower, and in Trial 2, the relax roll was a dual roll. The spin finish was Goulston Lurol 3919 applied as a 25-30% emulsion. The first stage draw was about 1.13 (Trial 1) and 1.015 (trial 2) and second-stage draws were about 2.5 and 3.2. Although heat was not added to Roll 1 in these trials, the heat of operation would be expected to be above room temperature. As can be seen from Table 6, the yarn had excellent tenacity and elongation at speeds greater than 2000 m/min. ______________________________________ Trial 1 Trial 2 ______________________________________ Roll speeds (m/min.): Roll 1             430      754 Roll 2             486      765 Dual Roll 3        1226     2500 Relax Roll         1176 Relax Dual Roll 4           2010 Winder             1156     1995 Roll Temperatures (.degree. C.): Roll 1             Unheated Unheated Roll 2             49       65 Roll 3             135      165 Relax Dual Roll 4  Unheated Unheated Texturizing Conditions: Air Jet Temperature (.degree. C.) 163      190 Air Jet Pressure (psi) 80       95 Interlacer Pressure (psi) 20       30 Yarn Properties: Yarn Count (denier) 1450     1328 Tenacity (g/den)   1.3      1.98 Elongation (%)     44       50.4 ______________________________________

## Claims

1. A process for preparing bulk continuous fiber yarn from poly(trimethylene terephthalate) comprising: the range of about 250 to about 280.degree. C. to produce a plurality of spun filaments; to about 2 in a first drawing stage defined by at least one feed roller and at least one first draw roller, each of said at least one feed roller operated at a temperature less than about 100.degree. C. and each of said at least one draw roller heated to a temperature greater than the temperature of said at least one feed roller and within the range of about 50 to about 150.degree. C.; 2.2 times that of the first draw ratio in a second drawing stage defined by said at least one first draw roller and at least one second draw roller, each of said at least one second draw roller heated to a temperature greater than said at least one first draw roller and within the range of about 100 to about 200.degree. C.; and

2. The process of claim 1 which further comprises texturing the drawn yarn and cooling the textured filaments.

3. The process of claim 1 in which each of said at least one feed rollers is maintained at a temperature within the range of about 40 to about 85.degree. C.

4. The process of claim 1 in which the first draw ratio is within the range of about 1.01 to about 1.35.

5. The process of claim 1 in which the second draw ratio is within the range of about 2.2 to about 3.4 times the first draw ratio.

6. The process of claim 1 in which the poly(trimethylene terephthalate) has an intrinsic viscosity within the range of about 0.80 to about 1.0 dl/g.

7. The process of claim 1 in which the poly(trimethylene terephthalate) has an intrinsic viscosity within the range of about 0.88 to about 0.96 dl/g.

8. The process of claim 1 in which the poly(trimethylene terephthalate) is the product of condensation polymerization of the reaction product of 1,3-propane diol and at least one of terephthalic acid and dimethyl terephthalate.

9. The process of claim 1 in which the poly(trimethylene terephthalate) is the product of condensation polymerization of the reaction product of (a) a mixture of 1,3-propane diol and a second alkane diol and (b) a mixture of terephthalic acid and isophthalic acid.

10. The process of claim 2 in which texturing is carried out with an air jet at a pressure within the range of about 50 to about 120 psi.

11. The process of claim 2 in which the product yarn bulk is within the range of about 15 to about 45 percent.

12. The process of claim 2 in which the yarn is fed to texturing via a feed roll maintained at a temperature within the range of about 150 to about 200.degree. C.

13. The process of claim 2 in which the texturing step is carried out at a temperature within the range of about 150 to about 210.degree. C.