Title of Invention	"APPARATUS FOR CRYSTALLIZATION OF POLYTRIMETHYLENE TEREPHTHALATE"
Abstract	The present invention discloses a process and apparatus for crystallizing polytrimethylene terephthalate pellets which comprises introducing polytrimethylene terephthalate pellets having an intrinsic viscosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through the pip, thereby causing the pellets to move throught he pipe with the liquid wherein the liquid to pellet weight ratio is greater than 6.67 : 1 and wherein the flow rate of the liquid in the conduit is sufficient to prevent the pellets from settling; adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95°C for a time sufficient to induce a degree of crystallinity of at least 35% in the pellets;; separating the pellets from the liquid; directing the separated pellets to a classifier; removing the pellet fines, dust and undersized by passing the pellets through a screen in the classifier; passing the pellets through a slice plate section in the classifier where air is glowing through to cool the pellet; passing the pellets through a perforated plate in the classifier that retains oversized pellets; and removing the pellets from the classifier

Title of Invention

"APPARATUS FOR CRYSTALLIZATION OF POLYTRIMETHYLENE TEREPHTHALATE"

Abstract

The present invention discloses a process and apparatus for crystallizing polytrimethylene terephthalate pellets which comprises introducing polytrimethylene terephthalate pellets having an intrinsic viscosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through the pip, thereby causing the pellets to move throught he pipe with the liquid wherein the liquid to pellet weight ratio is greater than 6.67 : 1 and wherein the flow rate of the liquid in the conduit is sufficient to prevent the pellets from settling; adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95°C for a time sufficient to induce a degree of crystallinity of at least 35% in the pellets;; separating the pellets from the liquid; directing the separated pellets to a classifier; removing the pellet fines, dust and undersized by passing the pellets through a screen in the classifier; passing the pellets through a slice plate section in the classifier where air is glowing through to cool the pellet; passing the pellets through a perforated plate in the classifier that retains oversized pellets; and removing the pellets from the classifier

Full Text	PROCESS AND APPARATUS FOR CRYSTALLIZATION OF POLYTRIME-THYLENE TEREPHTHALATE (PTT) FIELD OF THE INVENTION This invention relates to the preparation of 1,3- propanediol based polyesters such as polytrimethylene terephthalate. (hereafter PTT). More particularly this invention relates to a process for achieving a degree of crystallization of PTT which will prevent pellet blocking and agglomeration. In one aspect, the inven-tion relates to a process that can be carried out in a continuous manner, as well as batch. In another aspect, the invention relates to an apparatus for the conti-nuous crystallization of polytrimethylene terephthalate (PTT). BACKGROUND OF THE INVENTION Polytrimethylene terephthalate is a polyester useful in fiber applications in the carpet and textile industries. The manufacture of polytrimethylene terephthalate involves the condensation polymerization of 1,3-propanediol and terephthalic acid to a polymer having an intrinsic viscosity (hereafter referred to as IV) of about 0.4 to 1.0 dl/g. The polymer melt is discharged from the melt reactor and extruded through an extrusion die into strands. The strands are quenched in cold water and cut into pellets for storage or transportation. It has been found that polytrimethylene terephthalate pellets tend to adhere to-gether, or block, during storage or shipping at temperatures above the polymer glass transition temperature Tg (about 45 °C), which temperature can easily be reached during storage in a silo, rail car, or hopper. Agglomeration of the pellets can also occur during drying. BRIEF SUMMARY OF THE INVENTION In accordance with the foregoing, the present invention is a process and appa-ratus for crystallizing pellets of polytrimethylene terephthalate which comprises: a) introducing polytrimethylene terephthalate pellets having an intrinsic vis- cosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through the pipe, thereby causing the pellets to move through the pipe with the liquid; wherein the liquid to pellet weight ratio is greater than 6.67:1 and wherein the flow rate of the liquid in the pipe is sufficient to prevent the pellets from settling. b) adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95 °C for a time sufficient to induce a degree of crystallinity of at least 35% in the pellets; and c) separating the pellets from the liquid. d) directing the separated pellets to a classifier; e) removing the pellet fines, dust, and undersizes by passing the pellets through a screen in the classifier; f) passing the pellets through a slice plate section in the classifier where air is flowing through to cool the pellets; g) passing the pellets through a perforated plate in the classifier that retains oversized pellets; and h) removing the pellets from the classifier. The process is preferably carried out in a continuous liquid pellet suspension apparatus comprising, for example, a hot water crystallization (HWC) pipe, at a sufficient flow rate to retard settling of pellets. The desired pellet properties are generally reached in a residence time in the pipe within the range of 3 seconds to 5 minutes. It is preferred that weight ratio of the liquid to the pellets be from 5:1 to 200:1, most preferably 10:1 to 100:1. In one aspect of the practice of the invention, crystallized pellets are cooled to a temperature below their glass transition temperature during classification to re-move fines and oversized pellets. The combined classifier-cooler includes a screen for removing pellet fines, dust and undersized pellets, a slice plate sec-tion having air flowing through, preferably from underneath, to cool the pellets, and a perforated plate through which pellets of the desired size will pass and which retains oversized pellets. BRIEF DESCRIPTION OF THE FIGURES Figure 1 is a schematic process flow diagram of a hot water crystallization (HWC) unit. Figure 2 is a block diagram of the combined classification and cooling section. DETAILED DESCRIPTION OF THE INVENTION The invention involves the preparation of polytrimethylene terephthalate pellets characterized by an increased crystallinity. The invention process overcomes the problem of polytrimethylene terephthalate pellets adhering together during hot weather storage or transportation, and enables drying of the pellets in a hopper-type dryer prior to melt processing or solid-state polymerization. The process also assists in reducing fines, which can be generated in the manufac-ture and processing of polytrimethylene terephthalate. The resulting partially crystallized polytrimethylene terephthalate pellets can be spun into fibers or made into film or engineering thermoplastics. In general, polytrimethylene terephthalate is prepared by reacting, at elevated temperature, a molar excess of 1,3-propanediol with terephthalic acid in a multi-stage (esterification/polycondensation) process, with removal of by-product wa-ter, for a time effective to produce polytrimethylene terephthalate. The polymeri-zation conditions are selected so as to produce molten polyester having a target intrinsic viscosity of at least 0.4 dl/g, preferably 0.4 to 1.0 dl/g. Polytrimethylene terephthalate may also be produced by the reaction of 1,3-propanediol with di- methyl terephthalate. For example, the polytrimethylene terephthalate (PTT) is discharged from the melt reactor and passed through an extrusion die to form polymer melt strands which are cooled and partially solidified by contact with cold water on a strand guide. The sequence of pelletization/ crystallization is not critical. Pre-pelletizing crystallization involves immersion of polymer melt strands in hot water prior to cutting of the strands, preferably en route from the extruder to the pelletizer. The preferred method, however, for process efficiency and pellet quality, and for practice in conjunction with the present invention, is to conduct crystallization downstream of pelletization. In the present invention we have found a process design for producing PTT pel-lets exhibiting sufficient crystallinity to prevent agglomeration, which process his several advantages not previously available in any similar process. The process is efficient in that a typical drying step prior to crystallization can optionally be omitted, the pellets are crystallized while being transported, and the process can be operated in a continuous manner, as well as the more common batch operation. Furthermore, by controlling the temperature of the liquid, the degree of crystallinity of the pellets can be controlled. It is desirable that they not be too soft or they will agglomerate but if they are too brittle, an unacceptable amount of fines will be produced. In addition, a stirred tank having a physical agitator, such as a blade, is not required, thus greatly reducing damage (abrasion) to the pellets. The process is also economical, as will be apparent to those skilled in the art from the description below of the relatively inexpensive materials em-ployed. The polymer strands are cut to pellets of, for example, 1/8 inch by 1/8 inch (0.3 cm by 0.3 cm). Pelletizing may be accomplished with a strand-cut pelletizer or an underwater pelletizer or by other means. In the preferred embodiment herein a strand-cut pelletizer was employed. Immediately after pelletization, the sur-faces of the pellets are solid while the cores are still partially molten and have a low degree of crystallinity. Since the PTT crystallization of the present invention is executed in a hot water medium, at 50 up to 95 °C, the cold water used in pelletizing is preferably separated from the polymer pellets before the pellets reach the hot water crystallization unit (hereafter referred to as HWC). In the following description, the pellets are dry-cut, but the process could be operated to accommodate wet pellets. The pellets are delivered from the pelletizer to the HWC by way of a wash-down hopper. Referring to Figure 1, in the present invention the pellets 1 are received in the wash-down hopper 2 of a hydraulically driven (preferably water) eductor 4. The eductor is generally funnel shaped and provides its own induction force to pull the pellet s into the top side 3 of the eductor by the creation of a vacuum due to the flow of water through the eductor in the direction of eductor inlet 5 to eductor tip 6. The pellets are then drawn to the tip 6 of the eductor 4 and carried by hydraulic medium, again preferably water, to the inside of the hot water crystallization pipe 7. The pipe can be made of any material that can meet the temperature requirement, including materials, such as, for example, chlorinated polyvinyl-chloride (CPVC). The temperature of the water in the crystallization pipe 7 is adjusted to 50°C to 95°C and the crystallization of PTT is achieved via hot water contact with polymer pellets. The residence time of hot water crystallization is controlled by the pipe length and water flowrate. The water temperature may be controlled by a heater temperature control 18 installed in line 17. The separation of hot water from the pellets is achieved in a centrifugal dryer 8 which has a vent 9 and is connected to the classifier 10. The pellets may be cooled in the dryer 8 or they may be cooled in the classifier 10 as described below or they may be cooled by other means. The flow of water through the HWC moves the pellets along. Water flows from the storage tank 16 through line 19 to water pump 20 and then through optional filter 21 to the inlet 5 of eductor 4. The water is circulated from dryer 8 via line 11 to a water surge tank 12 and recycled for reuse through line 13 back to the hot water storage tank 16, preferably after filtering at 15 to remove pellet dust and fines from the water stream. A water pump 14 in line 13 helps to move the water. Crystallization is achieved in the flowing hot water stream inside the crystalliza-tion pipe which can be any elongated pipe and is located between the pelletizer and the pellet dryer. The pipe may have a diameter suitable in proportion to the rest of the equipment. The diameter may suitably be in the range of 2 (5.1) inches to 10 (25.4) inches (centimeters) or more, but is preferably in the range of 4 (10.2) to 6 (15.2) inches (centimeters). A very broad range of compositions is suitable for construction of the hot water crystallization pipe. It is only necessary that the material meet the temperature and pressure requirements of the desired operation. Examples of suitable mate-rials include, but are not limited to CPVC, stainless steel, brass, and copper. CPVC may be employed with good results without the use of insulation. A liquid pellet suspension or slurry exemplified by the present invention is pre-ferred because it offers uniform residence time and uniform heating of the pel-lets in order to produce pellets of uniform crystallization and opacity. The hot water suspension or slurry of pellets is moved through the pipe at a rate which results in the desired hot water contact time. The water flow rate should be high enough to prevent PTT pellets from settling. The pipe should be long enough to offer the required residence time. A suitable residence time is in the range of 3 seconds to 5 minutes, preferably 30 seconds to 3 minutes, more preferably 1.5 to 2 minutes. It can take longer at temperatures at the lower end of the range. An additional advantage of this invention is that the pellets are moving by turbu-lent flow rather than by agitation, as in stirred tank process designs, and incur less damage due to abrasion. The flow system should have sufficient flexibility to control and adjust the flow rate in the crystallization pipe and also to adjust the water to pellet ratio if de- sired. The water to pellet weight ratio is preferably from 5:1 to 200:1, most pre-ferably 10:1 to 100:1. The residence time required to heat up PTT pellets from ambient temperature to the target temperature in a turbulent hot water stream can be calculated using the following: (FORMULA REMOVED) where 9 is the time required to achieve temp T across the pellet, T, is the initial surface temperature of the PTT pellet, Tfi is the ambient fluid temperature, T is the uniform pellet temperature at instant time 8, c is the average heat capacity of PTT pellets (between 20 °C and 80 °C, c = 0.131 BTU/LB • ° F [0.548 kJ/kg • ○K]), w is the volume of one PTT pellet = 5.918 x 10-7 ft3 [0.168 x 10-7 m3] (for a 1/8 inch [0.3 cm] by 1/8 inch [0.3 cm] pellet), A is the surface area of one PTT pellet = 0.001363 ft2 [0.0001266 m2] (again for a 1/8 inch [0.3 cm] by 1/8 inch [0.3 cm] pellet), h is the uniform value of the surface heat conductance, i.e. the heat transfer coefficient between water and PTT pellets. The surface conduc-tance h can be calculated from Equation 2: (FORMULA REMOVED) where (FORMULA REMOVED) where dp is the diameter of PTT pellets = 1/8 inch (0.3 cm), hF is the thermal conductivity of fluid (water) = 0.3795 BTU/ -hr • ft • ° F (0.6568 W/m • °K)at 70 °C, NRe is Reynolds number, vR is relative velocity between polymer pellets and water in feet/sec, ΗF is the viscosity of fluid, NPr is Prantl number, CP,F is the heat capacity of fluid. It was assumed in these calculations that there is negligible internal resistance inside the pellet for heat transfer and that the pellet is of an elongated spherical shape. To ensure that the pellets are sufficiently crystallized to prevent blocking, it is desirable to crystallize the pellets to the extent that the product does not exhibit a conspicuous cold crystallization peak on its DSC thermogram. The imparted degree of crystallization is related to the starting polymer density and IV, the temperature of the water, and the length of time the polymer is immersed. The following chart provides general guidance on immersion times required to achieve 35% or greater crystallinity (for non-delustered polytrimethylene tereph-thalate) over the temperature range of 60 to 100°C. (Table Removed) For commercial operation, the desirability of faster crystallization must be ba-lanced against the cost of maintaining higher water temperatures. The upper temperature is also limited by the tendency of polytrimethylene terephthalate to undergo hydrolytic degradation (detected as a decrease in intrinsic viscosity) at temperatures above 95○C. Preferably, the water temperature is within the range of 65 °c to 85°C and the polymer is immersed for no longer than 3 minutes, pre-ferably for a time within the range of 30 seconds to 3 minutes, with delustered polymer generally requiring longer immersion than non-delustered polymer. Polytrimethylene terephthalate pellets treated by the invention process general-ly have an opaque appearance and generally exhibit the following physical properties: Density of at least 1.33 g/cm Crystallinity of at least 35% Tg of at least 55 °c, preferably at least 60 °C Apparent crystallite size of at least 10 nm As used herein, crystallinity refers to an increase in the crystalline fraction and a decrease in the amorphous fraction of the polymer. In general, crystallinity greater than 35%, preferably within the range of 36 to 45%, is desired. The cal-culation of crystallinity herein is based on the relationship of volume fractional crystallinity (Xc) of a sample to the density (Ds) of the sample: (FORMULA REMOVED) where Ds is the density of the sample, Da is the density of amorphous polytrime-thylene terephthalate (= 1.295 g/cm3) and Dc is the density of polytrimethylene terephthalate crystal (= 1.387 g/cm ). The weight fractional crystallinity equals (Dc/Ds)*Xc. After the selected residence time in the hot water crystallization pipe, the pel-let/water slurry may be discharged into a pellet dryer. The temperature of the PTT pellets after HWC may be 70 to 80°C. To reduce the tendency of the PTT pellets to block during storage, the PTT pellets may be cooled below their glass transition temperature. The pellets may be cooled to a temperature below 60 °C either by cold water quench en route to the dryer or, if the dryer environment is sufficiently cool, in the dryer itself. The glass transition temperature of PTT pel-lets with crystallinity of about 36 weight percent is around 50 °C. Therefore the PTT pellets should be cooled below 50°C or agglomeration can occur again. The pellet dryer can include a mechanism for water removal by centrifugal force. The pellets may be cooled in the dryer or elsewhere. After the dewatering and drying operation is completed, the pellets are passed to a classifier. The object of the classifier is to remove fines and oversized pellets. Pellet fines, dust, and undersizes are removed first by passing pellets through a screen. Pel lets are then passed through a perforated plate where the oversized pellets are retained on the plate and are removed whereas the pellets of the desired size pass through the plate. In preferred embodiment of the present invention the steps of classifying and cooling the crystallized PTT pellets to below 50 °C are accomplished with one piece of classification equipment. A cooling section is inserted between two pel-let classification sections. A block diagram of an apparatus for cooling the pel-lets while classifying is shown in Figure 2. This apparatus is incorporated into the classifier 10 shown in Figure 1. After the drying operation, the PTT pellets are introduced to a classifier, 10. Pellet fines, dust, and undersizes are removed first by passing the pellets through a screen, 22. The screen 22 is typically, but not limited to, 8-mesh 0.025-inch diameter wire screen made of stainless steel. Pellets are then passed through a slice plate section 23 where air is flowing through from underneath to pass through the slice plate to cool the pellets. The air can be at any temperature, as long as the air temperature is below the pellet temperature. The air can be incorporated in a number of ways. One effective method was to use air from a centrifugal blower with an air temperature of, for example, about 25 to 30°C. Cooling air could also be generated by suction from the classifier. The pellets are then moved to a perforated plate 24, where the oversized pellets are retained on the plate and are removed, wherein the pellets of the desired size pass through the plate. This perforated plate 24 used to re-move oversizes is typically, but not limited to, 16 gauge stainless steel perfo-rated with 7/32 inch round holes. Those skilled in the art will see variations that can be made within the scope of the invention. In calculating the residence time required to cool PTT pellets from, for example, 80°C to 40°C, it is assumed again that there is negligible internal resistance inside the pellet for heat transfer and the pellet is of an elongated spherical shape. Assuming a 1/8 inch by 1/8 inch PTT pellet (here regarded as a 1/8 inch sphere) being cooled from some initial uniform temperature state Tj in a flowing air stream of temperature Tf, the heat conduction equation for the pellet leads to the following: (FORMULA REMOVED) where 6 is the time required to achieve temperature T across the pellet, T, is the initial surface temperature of the PTT pellet, Tf is the ambient fluid (air) temperature, T is the uniform pellet temperature at instant time 8, c is the average heat capacity of PTT pellets (between 40°C and 80 °C, c = 0.2998 BTU/LB • °F [1.255 kJ/kg. • °K]), w is the specific weight of one PTT pellet, V is the volume of one PTT pellet, A is the surface area of one PTT pellet = 0.001363 ft2 (0.0001266 m ), h is the uniform value of the surface heat conductance, i.e. the heat transfer coefficient between air and PTT pellets. The surface conductance h can be calculated from: (FORMULA REMOVED) where dp is the diameter of PTT pellets = 1/8 inch (0.3 cm), hF is the thermal conductivity of fluid (air) = 0.015 BTU/ hr • ft • °F (0.026 W/m • °K) at 27 °C, NRe is Reynolds number, VR is relative velocity between polymer pellets and air, ΗF is the viscosity of air, Npr is Prantl number, CP,F is the heat capacity of air. To calculate the surface area of the cooling slice plate required to contact the pellets and the required flowrate, it was assumed: 1. The surface area in contact with pellets must be large enough to allow one single layer of pellets on the slice plate during cooling process. 2. The single pellet can be considered of cylindrical shape (1/8 inch [0.3 cm] in length and 1/8 inch [0.3 cm] in diameter). One single PTT pellet volume is 5.918 x 10-7ft3 (0.168 x 10-7m3), and PTT pellet density is 80.7 lb/ft3 (1293 kg/m3 ). with a 2 second residence time and 520 Ib/hr (236 kg/hr) throughput, the number of pellets on the cooling slice plate 23 of Figure 2 at any given moment is 6048 (where each pellet has a surface area of 1.085 x 10-4ft2 [0.1 x 10-4m ]). This leads to a figure for the surface area of the slice plate of 0.656 ft (0.06 m ). Considering only a certain percentage of the slice plate area is the open area allowing air to pass through, then a 1.5 ft2 (0.14 m2 ) slot screen area may be employed with good results. The air flow rate should be high enough to permit the air to pass through the gaps between pellets and have pellets fluidized with the support of the slice plate. The gap between any adjacent slice plate should be large enough to al-low airflow through, while the gap should be small enough to not allow pellets to drop through. In practice the width of the slice plate may be suitably around 4 millimeters. It is preferred to not completely fluidize the pellets. Although the process of the present invention is preferably carried out conti-nuously, it could be operated as a batch process. The process is preferably car-ried out continuously for efficiency. Integration of crystallization into a conti-nuous polymerization process may involve coordination with upstream and downstream processing, careful control of pellet residence time in the crystalliz-er for uniform crystallization of the pellets, recycling of water for reuse, along with additional means for filtration, temperature control, etc. In batch mode the pellet delivery to the eductor is carried out as discreet loads while the HWC loop recirculates constantly. In either continuous or batch crystallization, the polytrimethylene terephthalate pellets will be immersed in hot water at temperatures within the range of 50 to 95°C, preferably 65 to 95 °C, most preferably 65 to 85 °C, for a time sufficient to achieve the desired crystallinity. This allows the latent heat to be used for auto crystallization. Directly after pelletization, the pellets have a latent energy which is high enough to initiate crystallization at 50 to 95 °C. As used herein, crystal-linity indicates the degree of crystallization. In general, crystallinity greater than 35%, preferably within the range of 36 to 45%, measured as described above, is desired. The following examples will serve to further illustrate the invention disclosed herein. The examples are intended only as a means of illustration and should not be construed as limiting the scope of the invention in any way. Those skilled in the art will recognize many variations that may be made without departing from the spirit of the disclosed invention. Example 1 A trial of the hot water crystallization (HWC) process and apparatus was con-ducted. The water temperature, water flow rate, pellet residence time in the wa-ter stream, and water pressure at the eductor for four trials are shown in Table 1. The pellet content in water was a little less than 2 %wt -a water:pellet weight ratio of a little more than 50:1. In four separate experiments dry-cut pellets were fed into the HWC eductor with a flow rate of between 35 to 40 gpm (132.5 to 151.4 liters per minute). The water temperature, crystallinity before and after HWC, and the cooling effect with classification are shown in Table 2. The pellet crystallinities after HWC were all higher than 35% when the HWC water temperature was near or greater than 70 °C. The glass transition temperatures of those hot water crystallized pellets were all above 55 °C and thus there were no agglomeration problems under all typical storage conditions and transport processes. Use of hot water temperatures below 60 °C would require longer residence time, i.e., longer HWC pipe. In the last three runs, the pellets were cooled in the combined classification- cooling process as described above. In these three runs the pellet temperatures were measured by inserting a thermocouple into the pellet pile. The cooling sec-tion successfully cooled the pellets to a temperature below 50 ○C. The glass transition temperatures of these hot water crystallized pellets were all above the temperatures of the pellets and thus agglomeration problems did not occur when storing these pellets. (Table Removed) Claims 1. A process for crystallizing polytrimethylene terephthalate pellets which comprises: a) introducing polytrimethylene terephthalate pellets having an intrinsic viscosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through the pipe, thereby causing the pellets to move through the pipe with the liquid; wherein the liquid to pellet weight ratio is greater than 6.67:1 and wherein the flow rate of the liquid in the conduit is sufficient to prevent the pellets from settling; b) adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95 °C for a time sufficient to induce a degree of crystallinity of at least 35 % in the pellets; c) separating the pellets from the liquid; d) directing the separated pellets to a classifier; e) removing the pellet fines, dust, and undersizes by passing the pellets through a screen in the classifier; f) passing the pellets through a slice plate section in the classifier where air is flowing through to cool the pellets; g) passing the pellets through a perforated plate in the classifier that retains oversized pellets; and h) removing the pellets from the classifier. 2. The process of claim 1 wherein the weight ratio of the liquid to the pellets is from 10:1 to 100:1. 3. The process of claim 1 or 2 wherein the polytrimethylene terephthalate pellets are maintained in contact with the liquid for a time within the range of 3 seconds to 5 minutes. 4. The process of claims 1 to 3 wherein the pellets are contacted with the liquid for a sufficient time to produce polytrimethylene terephthalate pellets hav- ing a glass transition of at least 55 °C. 5. The process of claims 1 to 4 in which the polytrimethylene terephthalate pellets have a differential scanning calorimeter thermogram characterized by the absence of a cold crystallization peak. 6. An apparatus for crystallizing polytrimethylene terephthalate pellets which comprises: a) means for introducing polymer pellets into a pipe containing a liquid; b) means for moving the liquid through the pipe; c) means for controlling the temperature of the liquid; d) means for separating the pellets from the liquid; e) combined classifier/cooling means for removing pellet fines and dust and oversized pellets which comprises: i) a screen for removing pellet fines, dust, and undersizes; ii) a slice plate section in which air flows through to cool the pellets; iii) a perforated bottom plate that retains oversized pellets; and f) means for recycling the liquid.

Full Text

PROCESS AND APPARATUS FOR CRYSTALLIZATION OF POLYTRIME-THYLENE TEREPHTHALATE (PTT)
FIELD OF THE INVENTION
This invention relates to the preparation of 1,3- propanediol based polyesters such as polytrimethylene terephthalate. (hereafter PTT). More particularly this invention relates to a process for achieving a degree of crystallization of PTT which will prevent pellet blocking and agglomeration. In one aspect, the inven-tion relates to a process that can be carried out in a continuous manner, as well as batch. In another aspect, the invention relates to an apparatus for the conti-nuous crystallization of polytrimethylene terephthalate (PTT).
BACKGROUND OF THE INVENTION
Polytrimethylene terephthalate is a polyester useful in fiber applications in the carpet and textile industries. The manufacture of polytrimethylene terephthalate involves the condensation polymerization of 1,3-propanediol and terephthalic acid to a polymer having an intrinsic viscosity (hereafter referred to as IV) of about 0.4 to 1.0 dl/g. The polymer melt is discharged from the melt reactor and extruded through an extrusion die into strands. The strands are quenched in cold water and cut into pellets for storage or transportation.
It has been found that polytrimethylene terephthalate pellets tend to adhere to-gether, or block, during storage or shipping at temperatures above the polymer glass transition temperature Tg (about 45 °C), which temperature can easily be reached during storage in a silo, rail car, or hopper. Agglomeration of the pellets can also occur during drying.
BRIEF SUMMARY OF THE INVENTION
In accordance with the foregoing, the present invention is a process and appa-ratus for crystallizing pellets of polytrimethylene terephthalate which comprises:
a) introducing polytrimethylene terephthalate pellets having an intrinsic vis-
cosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through
the pipe, thereby causing the pellets to move through the pipe with the liquid;
wherein the liquid to pellet weight ratio is greater than 6.67:1 and wherein the
flow rate of the liquid in the pipe is sufficient to prevent the pellets from settling.
b) adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95 °C for a time sufficient to induce a degree of crystallinity of at least 35% in the pellets; and
c) separating the pellets from the liquid.
d) directing the separated pellets to a classifier;
e) removing the pellet fines, dust, and undersizes by passing the pellets through a screen in the classifier;
f) passing the pellets through a slice plate section in the classifier where air is flowing through to cool the pellets;
g) passing the pellets through a perforated plate in the classifier that retains oversized pellets; and
h) removing the pellets from the classifier.
The process is preferably carried out in a continuous liquid pellet suspension apparatus comprising, for example, a hot water crystallization (HWC) pipe, at a sufficient flow rate to retard settling of pellets. The desired pellet properties are generally reached in a residence time in the pipe within the range of 3 seconds to 5 minutes. It is preferred that weight ratio of the liquid to the pellets be from 5:1 to 200:1, most preferably 10:1 to 100:1.
In one aspect of the practice of the invention, crystallized pellets are cooled to a temperature below their glass transition temperature during classification to re-move fines and oversized pellets. The combined classifier-cooler includes a screen for removing pellet fines, dust and undersized pellets, a slice plate sec-tion having air flowing through, preferably from underneath, to cool the pellets, and a perforated plate through which pellets of the desired size will pass and which retains oversized pellets.
BRIEF DESCRIPTION OF THE FIGURES
Figure 1 is a schematic process flow diagram of a hot water crystallization
(HWC) unit.
Figure 2 is a block diagram of the combined classification and cooling section.
DETAILED DESCRIPTION OF THE INVENTION
The invention involves the preparation of polytrimethylene terephthalate pellets characterized by an increased crystallinity. The invention process overcomes the problem of polytrimethylene terephthalate pellets adhering together during hot weather storage or transportation, and enables drying of the pellets in a hopper-type dryer prior to melt processing or solid-state polymerization. The process also assists in reducing fines, which can be generated in the manufac-ture and processing of polytrimethylene terephthalate. The resulting partially crystallized polytrimethylene terephthalate pellets can be spun into fibers or made into film or engineering thermoplastics.
In general, polytrimethylene terephthalate is prepared by reacting, at elevated temperature, a molar excess of 1,3-propanediol with terephthalic acid in a multi-stage (esterification/polycondensation) process, with removal of by-product wa-ter, for a time effective to produce polytrimethylene terephthalate. The polymeri-zation conditions are selected so as to produce molten polyester having a target intrinsic viscosity of at least 0.4 dl/g, preferably 0.4 to 1.0 dl/g. Polytrimethylene terephthalate may also be produced by the reaction of 1,3-propanediol with di-
methyl terephthalate.
For example, the polytrimethylene terephthalate (PTT) is discharged from the melt reactor and passed through an extrusion die to form polymer melt strands which are cooled and partially solidified by contact with cold water on a strand guide. The sequence of pelletization/ crystallization is not critical. Pre-pelletizing crystallization involves immersion of polymer melt strands in hot water prior to cutting of the strands, preferably en route from the extruder to the pelletizer. The preferred method, however, for process efficiency and pellet quality, and for practice in conjunction with the present invention, is to conduct crystallization downstream of pelletization.
In the present invention we have found a process design for producing PTT pel-lets exhibiting sufficient crystallinity to prevent agglomeration, which process his several advantages not previously available in any similar process. The process is efficient in that a typical drying step prior to crystallization can optionally be omitted, the pellets are crystallized while being transported, and the process can be operated in a continuous manner, as well as the more common batch operation. Furthermore, by controlling the temperature of the liquid, the degree of crystallinity of the pellets can be controlled. It is desirable that they not be too soft or they will agglomerate but if they are too brittle, an unacceptable amount of fines will be produced. In addition, a stirred tank having a physical agitator, such as a blade, is not required, thus greatly reducing damage (abrasion) to the pellets. The process is also economical, as will be apparent to those skilled in the art from the description below of the relatively inexpensive materials em-ployed.
The polymer strands are cut to pellets of, for example, 1/8 inch by 1/8 inch (0.3 cm by 0.3 cm). Pelletizing may be accomplished with a strand-cut pelletizer or an underwater pelletizer or by other means. In the preferred embodiment herein a strand-cut pelletizer was employed. Immediately after pelletization, the sur-faces of the pellets are solid while the cores are still partially molten and have a low degree of crystallinity.
Since the PTT crystallization of the present invention is executed in a hot water medium, at 50 up to 95 °C, the cold water used in pelletizing is preferably separated from the polymer pellets before the pellets reach the hot water crystallization unit (hereafter referred to as HWC). In the following description, the pellets are dry-cut, but the process could be operated to accommodate wet pellets.
The pellets are delivered from the pelletizer to the HWC by way of a wash-down hopper. Referring to Figure 1, in the present invention the pellets 1 are received in the wash-down hopper 2 of a hydraulically driven (preferably water) eductor 4. The eductor is generally funnel shaped and provides its own induction force to pull the pellet s into the top side 3 of the eductor by the creation of a vacuum due to the flow of water through the eductor in the direction of eductor inlet 5 to eductor tip 6.
The pellets are then drawn to the tip 6 of the eductor 4 and carried by hydraulic medium, again preferably water, to the inside of the hot water crystallization pipe 7. The pipe can be made of any material that can meet the temperature requirement, including materials, such as, for example, chlorinated polyvinyl-chloride (CPVC). The temperature of the water in the crystallization pipe 7 is adjusted to 50°C to 95°C and the crystallization of PTT is achieved via hot water contact with polymer pellets. The residence time of hot water crystallization is controlled by the pipe length and water flowrate. The water temperature may be controlled by a heater temperature control 18 installed in line 17.
The separation of hot water from the pellets is achieved in a centrifugal dryer 8 which has a vent 9 and is connected to the classifier 10. The pellets may be cooled in the dryer 8 or they may be cooled in the classifier 10 as described below or they may be cooled by other means.
The flow of water through the HWC moves the pellets along. Water flows from the storage tank 16 through line 19 to water pump 20 and then through optional filter 21 to the inlet 5 of eductor 4. The water is circulated from dryer 8 via line
11 to a water surge tank 12 and recycled for reuse through line 13 back to the hot water storage tank 16, preferably after filtering at 15 to remove pellet dust and fines from the water stream. A water pump 14 in line 13 helps to move the water.
Crystallization is achieved in the flowing hot water stream inside the crystalliza-tion pipe which can be any elongated pipe and is located between the pelletizer and the pellet dryer. The pipe may have a diameter suitable in proportion to the rest of the equipment. The diameter may suitably be in the range of 2 (5.1) inches to 10 (25.4) inches (centimeters) or more, but is preferably in the range of 4 (10.2) to 6 (15.2) inches (centimeters).
A very broad range of compositions is suitable for construction of the hot water crystallization pipe. It is only necessary that the material meet the temperature and pressure requirements of the desired operation. Examples of suitable mate-rials include, but are not limited to CPVC, stainless steel, brass, and copper. CPVC may be employed with good results without the use of insulation.
A liquid pellet suspension or slurry exemplified by the present invention is pre-ferred because it offers uniform residence time and uniform heating of the pel-lets in order to produce pellets of uniform crystallization and opacity. The hot water suspension or slurry of pellets is moved through the pipe at a rate which results in the desired hot water contact time. The water flow rate should be high enough to prevent PTT pellets from settling. The pipe should be long enough to offer the required residence time. A suitable residence time is in the range of 3 seconds to 5 minutes, preferably 30 seconds to 3 minutes, more preferably 1.5 to 2 minutes. It can take longer at temperatures at the lower end of the range. An additional advantage of this invention is that the pellets are moving by turbu-lent flow rather than by agitation, as in stirred tank process designs, and incur less damage due to abrasion.
The flow system should have sufficient flexibility to control and adjust the flow rate in the crystallization pipe and also to adjust the water to pellet ratio if de-
sired. The water to pellet weight ratio is preferably from 5:1 to 200:1, most pre-ferably 10:1 to 100:1.
The residence time required to heat up PTT pellets from ambient temperature to the target temperature in a turbulent hot water stream can be calculated using the following:
(FORMULA REMOVED)
where 9 is the time required to achieve temp T across the pellet, T, is the initial surface temperature of the PTT pellet, Tfi is the ambient fluid temperature, T is the uniform pellet temperature at instant time 8, c is the average heat capacity of PTT pellets (between 20 °C and 80 °C, c = 0.131 BTU/LB • ° F [0.548 kJ/kg •
○K]), w is the volume of one PTT pellet = 5.918 x 10-7 ft3 [0.168 x 10-7 m3] (for a 1/8 inch [0.3 cm] by 1/8 inch [0.3 cm] pellet), A is the surface area of one PTT
pellet = 0.001363 ft2 [0.0001266 m2] (again for a 1/8 inch [0.3 cm] by 1/8 inch [0.3 cm] pellet), h is the uniform value of the surface heat conductance, i.e. the heat transfer coefficient between water and PTT pellets. The surface conduc-tance h can be calculated from Equation 2:
(FORMULA REMOVED)
where
(FORMULA REMOVED)
where dp is the diameter of PTT pellets = 1/8 inch (0.3 cm), hF is the thermal
conductivity of fluid (water) = 0.3795 BTU/ -hr • ft • ° F (0.6568 W/m • °K)at 70 °C, NRe is Reynolds number, vR is relative velocity between polymer pellets and water in feet/sec, ΗF is the viscosity of fluid, NPr is Prantl number, CP,F is the heat capacity of fluid.
It was assumed in these calculations that there is negligible internal resistance inside the pellet for heat transfer and that the pellet is of an elongated spherical shape.
To ensure that the pellets are sufficiently crystallized to prevent blocking, it is desirable to crystallize the pellets to the extent that the product does not exhibit a conspicuous cold crystallization peak on its DSC thermogram. The imparted degree of crystallization is related to the starting polymer density and IV, the temperature of the water, and the length of time the polymer is immersed. The following chart provides general guidance on immersion times required to achieve 35% or greater crystallinity (for non-delustered polytrimethylene tereph-thalate) over the temperature range of 60 to 100°C.
(Table Removed)
For commercial operation, the desirability of faster crystallization must be ba-lanced against the cost of maintaining higher water temperatures. The upper temperature is also limited by the tendency of polytrimethylene terephthalate to undergo hydrolytic degradation (detected as a decrease in intrinsic viscosity) at temperatures above 95○C. Preferably, the water temperature is within the range of 65 °c to 85°C and the polymer is immersed for no longer than 3 minutes, pre-ferably for a time within the range of 30 seconds to 3 minutes, with delustered
polymer generally requiring longer immersion than non-delustered polymer.
Polytrimethylene terephthalate pellets treated by the invention process general-ly have an opaque appearance and generally exhibit the following physical properties:
Density of at least 1.33 g/cm Crystallinity of at least 35% Tg of at least 55 °c, preferably at least 60 °C Apparent crystallite size of at least 10 nm
As used herein, crystallinity refers to an increase in the crystalline fraction and a decrease in the amorphous fraction of the polymer. In general, crystallinity greater than 35%, preferably within the range of 36 to 45%, is desired. The cal-culation of crystallinity herein is based on the relationship of volume fractional crystallinity (Xc) of a sample to the density (Ds) of the sample:
(FORMULA REMOVED)
where Ds is the density of the sample, Da is the density of amorphous polytrime-thylene terephthalate (= 1.295 g/cm3) and Dc is the density of polytrimethylene
terephthalate crystal (= 1.387 g/cm ). The weight fractional crystallinity equals (Dc/Ds)*Xc.
After the selected residence time in the hot water crystallization pipe, the pel-let/water slurry may be discharged into a pellet dryer. The temperature of the PTT pellets after HWC may be 70 to 80°C. To reduce the tendency of the PTT pellets to block during storage, the PTT pellets may be cooled below their glass transition temperature. The pellets may be cooled to a temperature below 60 °C either by cold water quench en route to the dryer or, if the dryer environment is sufficiently cool, in the dryer itself. The glass transition temperature of PTT pel-lets with crystallinity of about 36 weight percent is around 50 °C. Therefore the PTT pellets should be cooled below 50°C or agglomeration can occur again.
The pellet dryer can include a mechanism for water removal by centrifugal force. The pellets may be cooled in the dryer or elsewhere. After the dewatering and drying operation is completed, the pellets are passed to a classifier. The object of the classifier is to remove fines and oversized pellets. Pellet fines, dust, and undersizes are removed first by passing pellets through a screen. Pel lets are then passed through a perforated plate where the oversized pellets are retained on the plate and are removed whereas the pellets of the desired size pass through the plate.
In preferred embodiment of the present invention the steps of classifying and cooling the crystallized PTT pellets to below 50 °C are accomplished with one piece of classification equipment. A cooling section is inserted between two pel-let classification sections. A block diagram of an apparatus for cooling the pel-lets while classifying is shown in Figure 2. This apparatus is incorporated into the classifier 10 shown in Figure 1. After the drying operation, the PTT pellets are introduced to a classifier, 10. Pellet fines, dust, and undersizes are removed first by passing the pellets through a screen, 22. The screen 22 is typically, but not limited to, 8-mesh 0.025-inch diameter wire screen made of stainless steel. Pellets are then passed through a slice plate section 23 where air is flowing through from underneath to pass through the slice plate to cool the pellets. The air can be at any temperature, as long as the air temperature is below the pellet temperature. The air can be incorporated in a number of ways. One effective method was to use air from a centrifugal blower with an air temperature of, for example, about 25 to 30°C. Cooling air could also be generated by suction from the classifier. The pellets are then moved to a perforated plate 24, where the oversized pellets are retained on the plate and are removed, wherein the pellets of the desired size pass through the plate. This perforated plate 24 used to re-move oversizes is typically, but not limited to, 16 gauge stainless steel perfo-rated with 7/32 inch round holes. Those skilled in the art will see variations that can be made within the scope of the invention.
In calculating the residence time required to cool PTT pellets from, for example, 80°C to 40°C, it is assumed again that there is negligible internal resistance
inside the pellet for heat transfer and the pellet is of an elongated spherical shape. Assuming a 1/8 inch by 1/8 inch PTT pellet (here regarded as a 1/8 inch sphere) being cooled from some initial uniform temperature state Tj in a flowing air stream of temperature Tf, the heat conduction equation for the pellet leads to the following:
(FORMULA REMOVED)
where 6 is the time required to achieve temperature T across the pellet, T, is the initial surface temperature of the PTT pellet, Tf is the ambient fluid (air) temperature, T is the uniform pellet temperature at instant time 8, c is the average heat capacity of PTT pellets (between 40°C and 80 °C, c = 0.2998 BTU/LB • °F [1.255 kJ/kg. • °K]), w is the specific weight of one PTT pellet, V is the volume of one PTT pellet, A is the surface area of one PTT pellet = 0.001363 ft2
(0.0001266 m ), h is the uniform value of the surface heat conductance, i.e. the heat transfer coefficient between air and PTT pellets. The surface conductance h can be calculated from:
(FORMULA REMOVED)
where dp is the diameter of PTT pellets = 1/8 inch (0.3 cm), hF is the thermal conductivity of fluid (air) = 0.015 BTU/ hr • ft • °F (0.026 W/m • °K) at 27 °C, NRe is Reynolds number, VR is relative velocity between polymer pellets and air, ΗF is the viscosity of air, Npr is Prantl number, CP,F is the heat capacity of air.
To calculate the surface area of the cooling slice plate required to contact the
pellets and the required flowrate, it was assumed:
1. The surface area in contact with pellets must be large enough to allow one single layer of pellets on the slice plate during cooling process.
2. The single pellet can be considered of cylindrical shape (1/8 inch [0.3 cm] in length and 1/8 inch [0.3 cm] in diameter).
One single PTT pellet volume is 5.918 x 10-7ft3 (0.168 x 10-7m3), and PTT pellet
density is 80.7 lb/ft3 (1293 kg/m3 ). with a 2 second residence time and 520 Ib/hr (236 kg/hr) throughput, the number of pellets on the cooling slice plate 23 of Figure 2 at any given moment is 6048 (where each pellet has a surface area of
1.085 x 10-4ft2 [0.1 x 10-4m ]). This leads to a figure for the surface area of the
slice plate of 0.656 ft (0.06 m ). Considering only a certain percentage of the slice plate area is the open area allowing air to pass through, then a 1.5 ft2 (0.14
m2 ) slot screen area may be employed with good results.
The air flow rate should be high enough to permit the air to pass through the gaps between pellets and have pellets fluidized with the support of the slice plate. The gap between any adjacent slice plate should be large enough to al-low airflow through, while the gap should be small enough to not allow pellets to drop through. In practice the width of the slice plate may be suitably around 4 millimeters. It is preferred to not completely fluidize the pellets.
Although the process of the present invention is preferably carried out conti-nuously, it could be operated as a batch process. The process is preferably car-ried out continuously for efficiency. Integration of crystallization into a conti-nuous polymerization process may involve coordination with upstream and downstream processing, careful control of pellet residence time in the crystalliz-er for uniform crystallization of the pellets, recycling of water for reuse, along with additional means for filtration, temperature control, etc. In batch mode the pellet delivery to the eductor is carried out as discreet loads while the HWC loop recirculates constantly.
In either continuous or batch crystallization, the polytrimethylene terephthalate pellets will be immersed in hot water at temperatures within the range of 50 to 95°C, preferably 65 to 95 °C, most preferably 65 to 85 °C, for a time sufficient to achieve the desired crystallinity. This allows the latent heat to be used for auto crystallization. Directly after pelletization, the pellets have a latent energy which is high enough to initiate crystallization at 50 to 95 °C. As used herein, crystal-linity indicates the degree of crystallization. In general, crystallinity greater than 35%, preferably within the range of 36 to 45%, measured as described above, is desired.
The following examples will serve to further illustrate the invention disclosed herein. The examples are intended only as a means of illustration and should not be construed as limiting the scope of the invention in any way. Those skilled in the art will recognize many variations that may be made without departing from the spirit of the disclosed invention.
Example 1
A trial of the hot water crystallization (HWC) process and apparatus was con-ducted. The water temperature, water flow rate, pellet residence time in the wa-ter stream, and water pressure at the eductor for four trials are shown in Table 1. The pellet content in water was a little less than 2 %wt -a water:pellet weight ratio of a little more than 50:1. In four separate experiments dry-cut pellets were fed into the HWC eductor with a flow rate of between 35 to 40 gpm (132.5 to 151.4 liters per minute). The water temperature, crystallinity before and after HWC, and the cooling effect with classification are shown in Table 2. The pellet crystallinities after HWC were all higher than 35% when the HWC water temperature was near or greater than 70 °C. The glass transition temperatures of those hot water crystallized pellets were all above 55 °C and thus there were no agglomeration problems under all typical storage conditions and transport processes. Use of hot water temperatures below 60 °C would require longer residence time, i.e., longer HWC pipe.
In the last three runs, the pellets were cooled in the combined classification-
cooling process as described above. In these three runs the pellet temperatures were measured by inserting a thermocouple into the pellet pile. The cooling sec-tion successfully cooled the pellets to a temperature below 50 ○C. The glass transition temperatures of these hot water crystallized pellets were all above the temperatures of the pellets and thus agglomeration problems did not occur when storing these pellets.

(Table Removed)

Claims
1. A process for crystallizing polytrimethylene terephthalate pellets which comprises:
a) introducing polytrimethylene terephthalate pellets having an intrinsic viscosity of at least 0.4 dl/g into a pipe containing a liquid which is moving through the pipe, thereby causing the pellets to move through the pipe with the liquid; wherein the liquid to pellet weight ratio is greater than 6.67:1 and wherein the flow rate of the liquid in the conduit is sufficient to prevent the pellets from settling;
b) adjusting the temperature of the pellets and the liquid to a temperature of 50 to 95 °C for a time sufficient to induce a degree of crystallinity of at least 35 % in the pellets;
c) separating the pellets from the liquid;
d) directing the separated pellets to a classifier;
e) removing the pellet fines, dust, and undersizes by passing the pellets through a screen in the classifier;
f) passing the pellets through a slice plate section in the classifier where air is flowing through to cool the pellets;
g) passing the pellets through a perforated plate in the classifier that retains
oversized pellets; and
h) removing the pellets from the classifier.

2. The process of claim 1 wherein the weight ratio of the liquid to the pellets
is from 10:1 to 100:1.
3. The process of claim 1 or 2 wherein the polytrimethylene terephthalate
pellets are maintained in contact with the liquid for a time within the range of 3
seconds to 5 minutes.
4. The process of claims 1 to 3 wherein the pellets are contacted with the
liquid for a sufficient time to produce polytrimethylene terephthalate pellets hav-
ing a glass transition of at least 55 °C.
5. The process of claims 1 to 4 in which the polytrimethylene terephthalate
pellets have a differential scanning calorimeter thermogram characterized by
the absence of a cold crystallization peak.
6. An apparatus for crystallizing polytrimethylene terephthalate pellets which
comprises:
a) means for introducing polymer pellets into a pipe containing a liquid;
b) means for moving the liquid through the pipe;
c) means for controlling the temperature of the liquid;
d) means for separating the pellets from the liquid;
e) combined classifier/cooling means for removing pellet fines and dust and
oversized pellets which comprises:
i) a screen for removing pellet fines, dust, and undersizes;
ii) a slice plate section in which air flows through to cool the pellets;
iii) a perforated bottom plate that retains oversized pellets; and

f) means for recycling the liquid.

Documents:

http://ipindiaonline.gov.in/patentsearch/GrantedSearch/viewdoc.aspx?id=cwrli1gE00kfPg4YhJo5hg==&loc=+mN2fYxnTC4l0fUd8W4CAA==

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Patent Number

269660

Indian Patent Application Number

1511/DELNP/2011

PG Journal Number

45/2015

Publication Date

06-Nov-2015

Grant Date

30-Oct-2015

Date of Filing

01-Mar-2011

Name of Patentee

LURGI ZIMMER GMBH

Applicant Address

Lurgialli 5, 60295, Frankfurt am Main

Inventors:

#	Inventor's Name	Inventor's Address
1	ALLEN KEVIN DALE	37225 SOUTH LAKESHORE AVENUE, PRAIRIEVILLE, LA 70769 U.S.A.
2	DE LELLIS, THOMAS, LOUIS	20734 CASTLEBEND DRIVE, KATY, TX 77450 U.S.A.
3	DEISS, STEFAN	RHEINSTRASSE 7, 55296 HARXHEIM, GERMANY.
4	DENTON, EDWARD, JAMES	2923 JANE LONG LEAGUE, RICHMOND, TX 77469 U.S.A
5	LEE, JAMES, GAO	19203 ALLVIEW LANE, HOUSTON, TX 77094 U.S.A.
6	MACKENSEN, KLAUS	ZEHNMORGENSTRASSE 25A, 60433 FRANKFURT AM MAIN GERMANY.

PCT International Classification Number

C08G 63/00

PCT International Application Number

PCT/EP02/13562

PCT International Filing date

2002-11-29

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	60/334,353	2001-11-30	U.S.A.