Process for preparing poly(trimethylene terephthalate) carpet yarn

Abstract

Poly(trimethylene terephthalate) is formed into a bulk continuous filament yarn by a process comprising: Poly(trimethylene terephthalate)-based carpet having the bulk and resiliency of nylon as well as the stain resistance and low static generation of polyester is disclosed.

Description

BACKGROUND OF THE INVENTION

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° C.) with a steam jet assist, or at a lower temperature (95° 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° C. above or below the Tg of the polymer and the draw roller being at least 100° 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).

SUMMARY OF THE INVENTION

According to the invention, poly(trimethylene terephthalate) is formed into a bulk continuous filament yarn by a process comprising:

(a) melt-spinning poly(trimethylene terephthalate) at a temperature within the range of about 240° to about 280° C. to produce a plurality of spun filaments;

(b) cooling the spun filaments;

(c) converging the spun filaments into a yarn;

(d) drawing the yarn at a first draw ratio within the range of about 1.01 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° 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° C.;

(e) subsequently drawing the yarn at a second draw ratio of at least about 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° C.; and

(f) winding the drawn yarn.

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.

BRIEF DESCRIPTION OF THE FIGURES

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.

DETAILED DESCRIPTION OF THE INVENTION

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° C.) and a melting point within the range of about 215 to about 230° 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° 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° C., preferably about 250 to about 270° 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° C., preferably within the range of about 40 to about 85° C. Roller 7 can be an unheated roll, in which case its temperature of operation will be somewhat elevated (30-45° 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° C., preferably about 90 to about 140° 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° 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° C. The texturing air jet temperature is generally within the range of about 150 to about 210° 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° C. The temperature of draw roll 29 is within the range of about 50 to about 150° C. The temperature of draw roll 30 is within the range of about 100 to about 200° 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.

EXAMPLE 1

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
Polymer IV (dl/g):
Extruder Temp. Profile:	Units	0.84, 0.88	0.69, 0.76
Zone 1	° C.	230	225
Zone 2	° C.	250	235
Zone 3	° C.	250	235
Zone 4	° C.	250	235
Melt Temp.	° 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.: ° 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

Fiber Drawing Conditions
Polymer IV (dl/g)	0.88	0.84	0.76	0.69
Roll Temp.: ° 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

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.

EXAMPLE 2

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	° C.	230
	Zone 2	° C.	260
	Zone 3	° C.	260
	Zone 4	° C.	260
	Melt Temp.	° 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	° C./m/min	80/235	80/235	100/235	100/235	100/235	100/235	100/235
Roll 3 Temp./Speed	° C./m/min	90/317	100/286	100/817	100/817	100/817	100/993	100/945
Roll 4 Temp./Speed	° C./m/min	155/1123	100/1021	155/1047	140/1103	140/1145	130/1044	140/996
Roll 5 Temp./Speed	° 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
Yam 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.

EXAMPLE 3

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, ° 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, ° C. 180
Feed Roll Speed, m/min.     980
Air Jet Temperature, ° 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 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° 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 1 was measured after 30 seconds. The 50 g weight was removed, a 10 lb weight was attached, and the length L 2 was measured after 30 seconds. Percent bulk was calculated as (L 0 -L 1 )/L 0 ×100% and shrinkage was calculated as (L 0 -L 2 )/L 0 ×100%. Results are shown in Table 2.

	TABLE 2
	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.

EXAMPLE 4

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	° C.	240
	Zone 2	° C.	255
	Zone 3	° C.	255
	Zone 4	° C.	255
	Melt Temperature	° C.	260
	Pack Pressure	psi	1830

Extrusion Conditions
	Extruder Temperature	Units
	Zone 1	° C.	240
	Zone 2	° C.	255
	Zone 3	° C.	255
	Zone 4	° C.	255
	Melt Temperature	° C.	260
	Pack Pressure	psi	1830

Extrusion Conditions
	Extruder Temperature	Units
	Zone 1	° C.	240
	Zone 2	° C.	255
	Zone 3	° C.	255
	Zone 4	° C.	255
	Melt Temperature	° C.	260
	Pack Pressure	psi	1830

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 3.

TABLE 3
			Accelerated
		Heat	Floor	% Loss
		Setting	Traffic	in Pile
Run	Twist/Inch	Conditions	Rating	Thickness
12 (Poly(trimethylene	4.5 × 4.5	270° F.	3.75	2.4
terephthalate)		Autoclave
13 (Poly(trimethylene	4.5 × 4.5	180° C.	3.5	7.1
terephthalate)		Seussen
14 (Poly(trimethylene	5.0 × 5.0	270° F.	3.75	1.7
terephthalate)		Autoclave
15 nylon 66	4.0 × 4.0	270° F.	3.0	6.4
		Autoclave
16 nylon 66	4.0 × 4.0	190° C.	3.5	4.5
		Seussen

The heat-set yarns were tufted into 24 oz. cut-pile Saxony carpets in ⅛″ gauge, {fraction (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.

EXAMPLE 5

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(trimethylene terephthalate) BCF yarns having different bulk levels. Extrusion, drawing, texturing and winding conditions were as follows.

Extrusion Conditions
	Extruder Temperature Profiles	Units
	Zone 1	° C.	240
	Zone 2	° C.	260
	Zone 3	° C.	260
	Zone 4	° C.	265
	Melt Temperature	° C.	265
	Pump Pressure	psi	3650

Extrusion Conditions
	Extruder Temperature Profiles	Units
	Zone 1	° C.	240
	Zone 2	° C.	260
	Zone 3	° C.	260
	Zone 4	° C.	265
	Melt Temperature	° C.	265
	Pump Pressure	psi	3650

The yarns were twisted, heat set and tufted into carpets for performance evaluation. Results are shown in Table 4.

TABLE 4
Sample	Feed Roll	Texturizing	Texturizing Jet	Yarn Count,			Accelerated Walk
Number	Temp, ° C.	Jet Temp., ° 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

EXAMPLE 6

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	° C.	240
	Zone 2	° C.	260
	Zone 3	° C.	260
	Zone 4	° C.	260
	Melt Temperature	° 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.

EXAMPLE 7

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.

TABLE 5
Sample:	1	2	3	4	5	nylon 6	nylon 66
Roll 1 Temp.	° C.	50	50	50	50	50
Roll 2 Temp.	° C.	90	90	90	90	90
Roll 3 Temp.	° 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.	° C.	165	165	165	165	165
Feed Roll Speed	m/min.	1000	1100	1150	1100	1000
Texturing Jet Temp.	° 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° 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.

	TABLE 6
		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 (° C.):
	Roll 1	Unheated	Unheated
	Roll 2	49	65
	Roll 3	135	165
	Relax Dual Roll 4	Unheated	Unheated
	Texturizing Conditions:
	Air Jet Temperature (° C.)	163	190
	Air Jet Pressure (psi)	80	95
	Interlacer Pressure (psi)	20	30
	Yam Properties:
	Yam Count (denier)	1450	1328
	Tenacity (g/den)	1.3	1.98
	Elongation (%)	44	50.4

Claims

1. A carpet comprising bulk continuous filament (BCF) yarn of poly(trimethylene terephthalate) having a bulk greater than about 24 percent prepared by a two-stage draw process, wherein said two-stage draw process comprises:(a) melt-spinning poly(trimethylene terephthalate) at a temperature within the range of about 250 to about 280° C. to produce a plurality of spun filaments; (b) cooling the spun filaments; (c) converging the spun filaments into a yarn; (d) drawing the yarn at a first draw ratio within the range of about 1.01 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 being operated at a temperature less than about 100° C. and each of said at least one draw roller being 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° C.; (e) subsequently drawing the yarn at a second draw ratio of at least about 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 being heated to a temperature greater than said at least one first draw roller and within the range of about 100 to about 200° C.; and (f) winding the drawn yarn.

2. The carpet defined by claim 1 in which the process for forming the BCF yarn further comprises texturing the drawn yarn and cooling the textured filaments.

3. The carpet defined by 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.

4. The carpet defined by claim 2 in which the yarn is fed to texturing via a feed roll maintained at a temperature within the range about 135 to about 220° C.

5. The carpet defined by claim 1 in which the yarn is fed to texturing via a feed roll maintained at a temperature within the range of about 150 to about 210° C.

6. The carpet defined by claim 1 in which each of said at least one feed rollers in the process of making said BCF yarn is maintained at a temperature within the range of from about 40 to about 85° C.

7. The carpet defined by claim 1 in which the first draw ratio in the process for making said BCF yarn is within the range of about 1.01 to about 1.35.

8. The carpet defined by claim 1 in which the second draw ratio in the process of making said BCF yarn is within the range of about 2.2 to about 3.4 times the first draw ratio.

9. The carpet defined by claim 1 in which said poly(trimethylene terephthalate) has an intrinsic viscosity within the range of about 0.80 to about 1.0 dl/g.

10. The carpet defined by 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.

11. The carpet defined by 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.

12. The carpet defined by 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.

13. The carpet defined by claim 1 wherein said carpet is a cut-pile carpet.

14. The carpet defined by claim 1 wherein said carpet is a loop-pile carpet.

15. The carpet defined by claim 1 wherein said carpet is a combination-type carpet.

16. The carpet defined by claim 1 wherein said BCF yarn has a bulk within the range of about 24 to about 45 percent.

17. The carpet defined by claim 1 wherein said BCF yarn has a bulk within the range of about 24 to about 40 percent.

18. The carpet defined by claim 1 wherein said BCF yarn has a bulk within the range of about 26 to about 35 percent.

19. The carpet defined by claim 1 in which each of said at least one feed rollers in the process of making said BCF yarn is unheated.

20. The carpet defined by claim 19 in which the first draw ratio in the process for making BCF yarn is within the range of about 1.01 to about 1.35.

21. A mat comprising bulk continuous filament (BCF) yarn of poly(trimethylene terephthalate) having a bulk greater than about 24 percent prepared by a two-stage draw process, wherein said two-stage draw process comprises:(a) melt-spinning poly(trimethylene terephthalate) at a temperature within the range of about 250 to about 280° C. to produce a plurality of spun filaments; (b) cooling the spun filaments; (c) converging the spun filaments into a yarn; (d) drawing the yarn at a first draw ratio within the range of about 1.01 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 being operated at a temperature less than about 100° C. and each of said at least one draw roller being 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° C.; (e) subsequently drawing the yarn at a second draw ratio of at least about 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 being heated to a temperature greater than said at least one first draw roller and within the range of about 100 to about 200° C.; and (f) winding the drawn yarn.

22. A rug comprising bulk continuous filament (BCF) yarn of poly(trimethylene terephthalate) having a bulk greater than about 24 percent prepared by a two-stage draw process, wherein said two-stage draw process comprises:(a) melt-spinning poly(trimethylene terephthalate) at a temperature within the range of about 250 to about 280° C. to produce a plurality of spun filaments; (b) cooling the spun filaments; (c) converging the spun filaments into a yarn; (d) drawing the yarn at a first draw ratio within the range of about 1.01 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 being operated at a temperature less than about 100° C. and each of said at least one draw roller being 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° C.; (e) subsequently drawing the yarn at a second draw ratio of at least about 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 being heated to a temperature greater than said at least one first draw roller and within the range of about 100 to about 200° C.; and (f) winding the drawn yarn.