US20110256331A1 - Ultra-high iv polyester for extrusion blow molding and method for its production - Google Patents

Ultra-high iv polyester for extrusion blow molding and method for its production Download PDF

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Publication number
US20110256331A1
US20110256331A1 US12/760,030 US76003010A US2011256331A1 US 20110256331 A1 US20110256331 A1 US 20110256331A1 US 76003010 A US76003010 A US 76003010A US 2011256331 A1 US2011256331 A1 US 2011256331A1
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Prior art keywords
resin
polyester
solid
ultra
starting material
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US12/760,030
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English (en)
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Helen J. Codd
George F. Rollend
Norman W. LISSON
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DAK Americas LLC
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DAK Americas LLC
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Application filed by DAK Americas LLC filed Critical DAK Americas LLC
Priority to US12/760,030 priority Critical patent/US20110256331A1/en
Assigned to DAK AMERICAS LLC reassignment DAK AMERICAS LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: LISSON, NORMAN W., ROLLEND, GEORGE F., CODD, HELEN J.
Priority to ES11717092T priority patent/ES2715610T3/es
Priority to TR2019/03694T priority patent/TR201903694T4/tr
Priority to PCT/US2011/032300 priority patent/WO2011130396A1/en
Priority to CN201180029506.XA priority patent/CN102971358B/zh
Priority to PL11717092T priority patent/PL2558514T3/pl
Priority to KR1020127029609A priority patent/KR101785753B1/ko
Priority to LTEP11717092.8T priority patent/LT2558514T/lt
Priority to CA2795918A priority patent/CA2795918C/en
Priority to MX2012011793A priority patent/MX341188B/es
Priority to BR112012026238A priority patent/BR112012026238B8/pt
Priority to PT11717092T priority patent/PT2558514T/pt
Priority to EP11717092.8A priority patent/EP2558514B1/en
Priority to JP2013505091A priority patent/JP5706516B2/ja
Priority to TW100113046A priority patent/TWI516521B/zh
Priority to ARP110101291A priority patent/AR081078A1/es
Publication of US20110256331A1 publication Critical patent/US20110256331A1/en
Priority to US13/760,784 priority patent/US9399700B2/en
Priority to US15/934,009 priority patent/US10844168B2/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
    • C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
    • C08G63/16—Dicarboxylic acids and dihydroxy compounds
    • C08G63/18—Dicarboxylic acids and dihydroxy compounds the acids or hydroxy compounds containing carbocyclic rings
    • C08G63/181—Acids containing aromatic rings
    • C08G63/183—Terephthalic acids
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/78—Preparation processes
    • C08G63/80—Solid-state polycondensation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
    • C08G63/78—Preparation processes
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J5/00—Manufacture of articles or shaped materials containing macromolecular substances
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T428/00—Stock material or miscellaneous articles
    • Y10T428/13—Hollow or container type article [e.g., tube, vase, etc.]
    • Y10T428/1352—Polymer or resin containing [i.e., natural or synthetic]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T428/00—Stock material or miscellaneous articles
    • Y10T428/13—Hollow or container type article [e.g., tube, vase, etc.]
    • Y10T428/1352—Polymer or resin containing [i.e., natural or synthetic]
    • Y10T428/1397—Single layer [continuous layer]

Definitions

  • the invention relates to an ultra-high intrinsic viscosity (IV) polyester resin useful in extrusion blow molding, and a method for its production.
  • IV intrinsic viscosity
  • Polyester resins including resins such as poly(ethylene terephthalate) (PET), poly(butylene terephthalate) (PBT), poly(ethylene naphthalate) (PEN), poly(trimethylene terephthalate) (PTT), and poly(trimethylene naphthalate) (PTN), are conventionally used as resins in the manufacture of containers such as beverage bottles. Properties such as flexibility, good impact resistance, and transparency, together with good melt processability, permit polyester resins to be widely used for this application.
  • the term resin as it is used herein includes all of the aforementioned materials.
  • the starting feedstocks for polyester resins are petroleum derivatives such as ethylene, which is obtained from petroleum or natural gas, and para-xylene, which is typically obtained from petroleum.
  • Polyester resins are generally made by a combined esterification/polycondensation reaction between monomer units of a diol (e.g., ethylene glycol (EG)) and a dicarboxylic acid (e.g., terephthalic acid (TPA)).
  • a diol e.g., ethylene glycol (EG)
  • a dicarboxylic acid e.g., terephthalic acid (TPA)
  • carboxylic acid and/or dicarboxylic acid include ester derivatives of the carboxylic acid and dicarboxylic acids.
  • Esters of carboxylic acids and dicarboxylic acids may contain one or more C1-C6 alkyl groups (e.g., methyl, ethyl, propyl, iso-propyl, butyl, iso-butyl, tert-butyl, pentyl, hexyl and mixtures thereof) in the ester unit, for example, dimethyl terephthalate (DMT).
  • DMT dimethyl terephthalate
  • polyester may be formed, for example, by first producing a prepolymer of low molecular weight and low intrinsic viscosity (IV) (e.g., a mixture of oligomers), for example, by reacting a diol and a dicarboxylic acid in a melt phase reaction.
  • IV intrinsic viscosity
  • the formation of the oligomers may be carried out by reacting a slurry of diol and dicarboxylic acid monomer units in an esterification reactor.
  • EG may be lost to evaporation during the esterification reaction which may be carried out at high temperatures.
  • the slurry of diol and dicarboxylic acid may contain an excess of EG, for example the diol and dicarboxylic acid may be present in a molar ratio of from about 1.2 to about 2.5 based on the total glycol to total di-acid.
  • Further pre-polycondensation and polycondensation of the oligomers can be carried out to provide a resin mixture having an IV of from 0.50 to 0.65.
  • Such resin mixtures are suitable in various applications such as fibers/filaments, fiber chips, or bottle-resin precursors.
  • Amorphous clear base chips having an IV of from 0.50 to 0.65 may be subjected to solid-state polymerization (SSP) to increase the molecular weight (e.g., to an IV of from 0.72 to 0.76 for water bottle applications, 0.81 to 0.85 for CSD/Beer bottles, etc.).
  • SSP solid-state polymerization
  • the solid-state polymerization (SSP) process unit can result in the resin undergoing crystallization which forms opaque pellets.
  • a continuous polyester melt-phase polycondensation process usually consists of three reaction steps: (i) esterification to form low molecular weight oligomers, (ii) pre-polymerization of the oligomers to form a pre-polymer, and (iii) polycondensation to form a polymer with an intermediate molecular weight or intrinsic viscosity (e.g., a target intrinsic viscosity of from 0.50 to 0.85).
  • an intermediate molecular weight or intrinsic viscosity e.g., a target intrinsic viscosity of from 0.50 to 0.85.
  • the three reaction steps (i), (ii), and (iii) above, can be carried out to achieve the target intrinsic viscosity in from 2 to 6 reactors using existing melt-phase process technology.
  • esterification is conducted in one or two vessels to form a mixture of low molecular weight oligomers with a low degree of polymerization (e.g., about up to 5 to 10 monomer unit pairs reacted).
  • the oligomers are then pumped to one or two pre-polymerization vessels where higher temperatures and lower pressures aid in removing water and EG.
  • the degree of polymerization then increases to a level of 10 to 40 repeating units.
  • the temperatures are further increased and pressures are further reduced in the final one or two vessels to form a polymer ready to be cut into pellets for example, or to be spun directly into fibers or filaments.
  • Esterification and pre-polymerization vessels may be agitated.
  • Polycondensation vessels e.g., finishers, wiped-film reactors etc.
  • agitators designed to generate very thin films. Temperatures and hold-up times are optimized for each set of vessels to minimize the degradation and other side reactions.
  • Some by-products that may be generated by the polyester melt phase reaction include diethylene glycol (DEG), acetaldehyde, water, cyclic oligomers, carboxyl end groups, vinyl end groups, and anhydride end groups.
  • Both time and temperature are two variables that are preferably controlled during an esterification/polycondensation reaction. With higher reaction temperatures, the total reaction time is significantly reduced and less residence time and/or fewer reactors are needed.
  • polyesters may be prepared using a batch method.
  • a batch method the diol and dicarboxylic acid units are mixed together in a single reactor.
  • more than one reactor e.g., reaction vessel
  • the diol/dicarboxylic acid mixture is heated to cause the monomer units to undergo a condensation reaction.
  • the by-products of the condensation reaction may include water or an alcohol.
  • Certain physical and chemical properties of polymeric materials are negatively affected by long exposure to elevated temperature, especially if the exposure is in an oxygen-containing atmosphere or at temperatures above, for example, 250° C.
  • Conventional methods for preparing polyester resins such as PET may suffer from disadvantages associated with the need to carry out a solid state polymerization (SSP) which subjects the resin to a long heat history and/or may require high capital expenditure.
  • SSP solid state polymerization
  • FIG. 1 A conventional process for producing polyester resins for container applications including melt-phase polycondensation and solid-state polymerization is shown schematically in FIG. 1 wherein the monomer components of a polyester resin such as PET are mixed in a melt-phase esterification/polycondensation reactor. The reaction is carried out to provide a molten resin having an intrinsic viscosity (IV) of from 0.50 to 0.65. The molten product obtained by the melt-phase esterification/polycondensation is then subjected to a polymer filtration.
  • IV intrinsic viscosity
  • the melt-phase esterification/polycondensation is typically carried out in a plurality of reactors. Therefore, the monomers may be added to a first esterification reactor to form a low IV material. As the oligomers pass through the remaining reactors, the IV is subsequently raised as the polycondensation reaction proceeds sequentially through a series of reactors.
  • the material in molten form is subjected to solidification and pelletizing.
  • the molten material may be solidified by passage of strands or filaments of the material formed by pumping the material through, for example, a die with a series of orifices. As the molten polyester resin is passed through an orifice, a continuous strand is formed.
  • the strands By passing the strands through water, the strands are immediately cooled to form a solid. Subsequent cutting of the strands provides pellets or chips which, in a conventional process, are then transferred to a solid-state polymerization stage (i.e., SSP).
  • SSP solid-state polymerization stage
  • the molten polymerized resin may be pumped through a die to form multiple strands.
  • the molten resin exiting from the die is quickly quenched in water to harden the resin.
  • the quick cooling e.g., water quench
  • the molten polyester does not have time to crystallize and is solidified in an amorphous state.
  • Solidified polyester strands, or pellets derived from cut strands are clear, transparent and in an amorphous state.
  • Solid-state polymerization is an important step in some conventional processes used to manufacture high molecular weight polyester resins for bottle, food-tray, and tire-cord applications.
  • the clear amorphous pellets (0.50 to 0.65 IV) produced by conventional melt polycondensation reaction processes may be further polymerized in the solid state at a temperature substantially higher than the resin's glass transition temperature but below the resin's crystalline melting point.
  • the solid state polymerization is carried out in a stream of an inert gas (usually nitrogen under continuous operation) or under a vacuum (usually in a batch rotary vacuum dryer).
  • the functional end groups of the polymer (e.g., PET) chains are sufficiently mobile and react with one another to further increase the molecular weight.
  • the SSP may include several individual reactors and/or processing stations.
  • the SSP may include a pre-crystallization step wherein the chips and/or pellets are transformed from an amorphous phase into a crystalline phase.
  • the use of a crystalline phase polyester resin is important in later steps of the SSP because the use of amorphous polyester chips may result in clumping of the pellets since an amorphous state polyester resin may not be sufficiently resistant to adherence between pellets and/or chips.
  • the SSP process further includes a crystallizer (e.g., crystallization step), a pre-heater, a cooler, and an SSP reactor.
  • IV intrinsic viscosity
  • the production of a polyester resin such as PET may be carried out directly from a melt phase of the monomer units without any final solid-state polymerization.
  • a batch process may be carried out at a sufficient temperature, for a sufficient time and at a sufficient pressure to drive the polycondensation reaction to completion thus avoiding the need for any subsequent finishing (e.g., final reaction).
  • Some manufacturing processes do not include an SSP. Processing a polyester resin directly from a melt phase condensation to obtain pre-forms for stretch blow molding applications is described in U.S. Pat. No. 5,968,429 (incorporated herein by reference in its entirety). The polymerization is carried out without an intermediate solidification of the melt phase and permits the continuous production of molded polyester articles (e.g., pre-forms), from a continuous melt phase reaction of the starting monomers.
  • the chips and/or pellets may be subjected to a final crystallization.
  • a final crystallization may include, for example, proper heating of the chips (pellets, pastilles, granules, round particles, etc.) at appropriate temperatures.
  • the pellets and/or chips are preheated and ready for transfer to the top of a counter-flow SSP reactor (parallel to the pre-heater) via a pneumatic system (e.g., Buhler technology). If a tilted crystallizer is stacked above the SSP reactor, the hot/crystallized chips then enter the SSP reactor by the rotating screw of the crystallizer (e.g., Sinco technology).
  • the SSP reactor can be considered as a moving bed of chips that move under the influence of gravity.
  • the chips have a slow down-flow velocity of from 30 to 60 mm/minute and the nitrogen has a high up-flow velocity of about 18 m/minute.
  • a typical mass-flow ratio of nitrogen to PET is in the range of 0.4 to 0.6.
  • the pellets and/or chips are subjected to elevated temperatures for periods of up to 15 hours. The heating and nitrogen sweeping through the gravity-flow reactor will drive the polycondensation reaction and result in longer chain lengths and, concurrently, a higher IV of the resins.
  • pellets and/or chips of a wide range of IV can be formed, e.g., having an average IV of about 0.80-0.84 dL/g, e.g., for CSD/Beer.
  • the pellets and/or chips have an opaque characteristic due to their crystallinity.
  • the crystalline material is transferred to a product silo for storage and/or packaging.
  • the finished product in a crystalline state and having an IV of about 0.80-84 dL/g, e.g., for CSD/Beer, can be further mixed with other co-barrier resins (powders, granules, pellets, pastilles, etc.) by molders or processors who purchase the polyester resins for manufacturing, for example, bottles and/or containers.
  • co-barrier resins pellets, granules, pellets, pastilles, etc.
  • a melt-phase polycondensation process may be used to make clear amorphous pellets (typically, 0.50 to 0.65 IV) as precursors to bottle resins.
  • the amorphous pellets are first pre-crystallized, crystallized, and/or preheated, then subjected to SSP in a gravity flow reactor (e.g., a reactor that is not agitated). After crystallization, the resin pellets become opaque and do not stick together if the temperature of SSP is at least 10° C. below the onset of the melting temperature of the resin pellets.
  • a direct high IV melt process as shown in FIG.
  • a finisher e.g., a wiped- or thin-film evaporator
  • EG major
  • water e.g., water, acetaldehyde, and so on. Immediate removal of EG/water under high temperatures drives the polycondensation reaction equilibrium toward the polymer side.
  • PET or other polyester resins are known to have hygroscopic behavior (e.g., absorb water from the atmosphere), so pellets obtained by cutting water-quenched strands contain significant quantities of water.
  • the pellets may be dried by passing dry air over the pellets or by heating. Heating for an extended period at an elevated temperature may lead to problems because the amorphous polyester (e.g., PET) pellets may have a tendency to stick to one another.
  • PET resins Because of the challenge of achieving high IV with PET based polyesters in a cost effective, time-efficient manner, and due to the increased crystallinity that often results from the thermal history, PET resins have typically been limited to use in injection stretch blow molding to prepare products such as soda bottles or other thin wall containers. Thicker walled products, such as “handleware”, have typically been formed by extrusion blow molding (EBM) with PETG copolymer, PVC, polyethylene, or polypropylene resins, due to the ability to achieve high enough IV and melt strength with the requisite characteristics, at acceptable cost.
  • EBM extrusion blow molding
  • “Handleware” is the term used for thicker walled containers (thickness of container wall being 25-55 mils) typically having handles (with handles typically having thickness of 30-40 mils), such as juice, milk, or laundry detergent bottles, and other such containers. (See FIGS. 8 , 9 , 10 , 11 for details of a typical “handleware” container.)
  • PET resins that could be used to produce “handleware” through EBM, in place of PETG copolymer, PVC, polyethylene or polypropylene, with comparable or better costs and providing clearer and colorless containers (which cannot be readily produced with some other materials).
  • one object of the invention is to provide an ultra-high IV polyester product having low crystallinity and suitable for use in a variety of high melt strength end uses.
  • Another object of the invention is to provide a method of producing such a high IV polyester product.
  • Another object of the invention is to provide a method for producing a handleware container that includes forming a molten parison from solid polyester resin and then forming the handleware container from the molten parison.
  • Another object of the invention is to provide a method of producing such a high IV polyester product using less energy and having a faster production time.
  • Another object of the invention is to provide an ultra-high IV polyester resin that can be used in high melt strength resin applications, including, but not limited to, injection blow molding, extrusion blow molding, pipe extrusion, and profile extrusion.
  • the polyester starting material is a polyethylene terephthalate polymer, optionally containing one or more comonomers in amounts up to 30 mol %, wherein the polyester starting material has been prepared by melt polymerization up to the IV st with no more than 0.05 dL/g of IV lift due to solid-state polymerization, and wherein the polyester starting material is in solid form as a resin particle having been subjected to latent heat crystallization upon formation of the resin particle, and having a variation of IV of no more than 0.05 dL/g across any dimension of the resin particle; and a parison and final article produced therefrom.
  • FIG. 1 shows a schematic of a conventional melt-phase process with subsequent solid-state polymerization (SSP);
  • FIG. 2 shows a schematic of a non-SSP direct high-IV melt process used to make a starting material resin for one embodiment of the present invention
  • FIG. 3 shows a schematic of a typical extrusion blow molding (EBM) process
  • FIG. 4 provides a graphical representation of IV change during SSP processing in preparation of ultra-high IV PET resins of the present invention (diamond, square, and triangle symbols) as compared with conventional resins (circle symbols);
  • FIG. 5 provides a graphical representation of IV change during SSP over longer SSP times of a starting material resin of the present invention to provide the ultra-high IV resin of the present invention
  • FIG. 6 provides further graphical representation comparing the SSP lifting of a conventional PET resin of low starting IV of ⁇ 0.65 (square symbols), conventional PET resin that has been solid-state polymerized to IV of >0.8 (diamond symbols), with melt-produced starting material used to prepare the ultra-high IV PET resin of the present invention (circle and triangle symbols).
  • FIG. 7 provides Top View of typical wall material thickness distribution in a 128 oz. bottle manufactured by an extrusion blow molding process. Bottle weight 150 ⁇ 4 grams. All dimensions in mils.
  • FIG. 8 provides Wide Side View of typical wall material thickness distribution in a 128 oz. bottle manufactured by an extrusion blow molding process. Bottle weight 150 ⁇ 4 grams. All dimensions in mils.
  • FIG. 9 provides Narrow Side View of typical wall material thickness distribution in a 128 oz. bottle manufactured by an extrusion blow molding process. Bottle weight 150 ⁇ 4 grams. All dimensions in mils.
  • FIG. 10 provides Bottom View of typical wall material thickness distribution in a 128 oz. bottle manufactured by an extrusion blow molding process. Bottle weight 150 ⁇ 4 grams. All dimensions in mils.
  • the present invention relates to an ultra-high IV polyester resin suitable for use in high melt strength applications, including, but not limited to, extrusion blow molding (EBM), injection blow molding, and profile extrusion, and its method of production.
  • EBM extrusion blow molding
  • ultra-high IV refers to a polyester resin having an IV of 0.9 or higher, preferably 1.1 or higher, more preferably 1.2 or higher, most preferably 1.3 or higher.
  • Such ultra-high IV resins are also known in the art as high melt strength resins.
  • the ultra-high IV polyester resin is produced by solid-state polymerization (SSP) of a starting resin having an IV of 0.65 to 0.90, preferably 0.70 to 0.85, more preferably 0.72 to 0.80, that is prepared by a melt process meeting one or more conditions selected from the group consisting of (i) without solid state polymerization, (ii) high IV melt polycondensation, (iii) having underwater pelletizing and (iv) having direct latent heat crystallization, such as that described in U.S. Published Application 2007/0128389 and U.S. Published Application 2007/0248778, the entire contents of each of which are hereby incorporated by reference.
  • SSP solid-state polymerization
  • this starting polyester resin is subjected to SSP to raise the IV to a level of 0.9 or higher, preferably 1.1 or higher, more preferably 1.2 or higher, most preferably 1.3 or higher.
  • the starting resin preferably contains a level of isophthalate units (as percent of the total starting di-acid monomer) of 1% or higher, preferably 2% or higher, more preferably 3% or higher, most preferably 4% or higher, in order to reduce the crystallinity and enhance the melting characteristics of the product formed through the SSP process.
  • the present invention ultra-high IV polyester can be processed by any method of processing a resin, e.g., by melting the resin, forming a shaped article from the molten resin, and cooling the shaped article to form a solid shaped article.
  • Processing includes any method by which the polyester resin is transformed from a solid form to a flowable and/or plastic form. The transforming may include heating the polyester resin beyond the glass transition temperature then forming a shaped solid article from the heated polyester resin.
  • Processing further includes any method by which a solid polyester resin is heated above its glass transition temperature and/or melt temperature and is subsequently and/or concurrently formed into a shaped article, particularly those processes that require the use of a high melt strength resin, including: injection molding, reaction injection molding (RIM), stretch blow molding, injection blow molding, recycling, extrusion molding (including EBM), compression molding, thermoforming, and such methods for processing polyester resins as described in “PET Packaging Technology,” by David W. Brooks and Geoff Giles (2002), the portions of which describe processing methods for polyester resins and/or PET resins are incorporated herein by reference.
  • Preferred processing includes injection (blow) molding, sheet and film extrusion, profile extrusion, extrusion blow molding (EBM) and compression molding; most preferably EBM.
  • the extrusion blow molding (EBM) process is the most common process for producing plastic bottles, particularly large plastic bottles.
  • the basic extrusion blow molding process is shown in FIG. 3 , and comprises plasticizing or melting of the resin in an extruder ( 10 ), forming the parison by extrusion of the molten resin through a die into a mold ( 15 ), blowing the parison to fit the shape of the bottle mold and cooling ( 20 ), then deflashing of the blown bottle and ejection of the finished product ( 25 ).
  • Variations can include multiple extruders for coextrusion of two or more materials for multilayer bottle structures, parison programmer to shape the parison to match complex blown product shapes and wall thickness, and multiple mold clamp systems to improve output through the use of multiple molds.
  • an extruder melts, mixes, and feeds a homogeneous molten polymer into a die head that forms the molten hollow plastic tube, called a parison, used in blowing hollow containers or other hollow products.
  • the first step is extrusion of a hollow plastic parison which is usually in a downward direction for making bottles.
  • the two halves of the mold close on the parison, capturing it as it is cut off from the extruder by a cold or heated cut-off knife.
  • a blow pin or a needle is inserted and air is blown into the mold, expanding the parison.
  • the blown pin cooled by water assists in forming the thread finish by compressing the thread finish section into the mold (neck calibration), rather than simply blowing it in. This results in a smooth interior in the finish region.
  • the needle blow case the needle is inserted into a part of the molded object that is trimmed off forming the final container shape, and the inside of the finish is formed only by air.
  • the mold is cooled, usually with water, to solidify the plastic. When the container is cool enough to maintain its shape, it is ejected from the mold.
  • the flash is trimmed from the container neck and bottom, as well as from other areas that are pinched off, for instance to form handles or offset necks.
  • the mark left from the removal of the flash serve as an easy means for identification of extrusion blow-molded containers. Usually, this is easiest to see on the bottom of the container. It typically appears as a rough area along the mold parting line, centered in the middle of the bottom and running half or so of the distance to the heel of the bottle. It is also possible, on careful examination, to identify the roughness at the top of the finish, or on other areas where flash was trimmed.
  • the flash after being trimmed, is usually granulated in a closed-loop fashion with the extruder and is immediately fed back into the drying hoppers on the extruder at a controlled rate, mixed with the virgin resin.
  • regrind can be problematic for heat-sensitive resins like PVC, especially if the proportion of the flash is high.
  • ultra-high IV PET there is no practical limit for regrind levels because it is a thermally stable resin.
  • the process of extruding a parison can be continuous or intermittent.
  • intermittent extrusion the melt from the continuously rotating extruder may be fed into an accumulator, from which it is periodically ejected, or a reciprocating extruder like those used for injection molding may be used.
  • Continuous extrusion is preferred for most packaging applications. It provides higher productivity and reduces thermal degradation, since the melt is not held up. Intermittent extrusion is commonly used for the production of very large blown containers, where a large parison must be produced in a very short time, and in the production of gasoline tanks for automobiles.
  • Extrusion In the extrusion process, molten plastic is pushed through a die with a cross section that shapes the plastic. The plastic is then drawn through a cooling apparatus, cut into sections or rolled up. Extrusion can only produce parts that have a continuous cross section. Some common parts that are extruded are pipe, vinyl siding, weed trimmer line, sheet, and film. Extrusion is a continuous process and can produce parts of any length.
  • Profile Extrusion is used to prepare solid parts with cross-sectional shapes other than round rods or flat sheets are called profiles.
  • Pipe and tubing is produced by extruding a circular, hollow cross section.
  • solution intrinsic viscosity (IV) of polyester (e.g., PET) resins is conventionally known.
  • Solution IV can be measured at 0.50% concentration of the resin in a 60/40 (wt. %/wt. %) phenol/1,1,2,2-tetrachloroethane solution by means of a glass capillary viscometer.
  • Conditions for measuring solution IV are described in ASTM D 4603-03 (approved on Mar. 10, 2003 and published in April 2003, incorporated herein by reference in its entirety).
  • the solution IV of the co-barrier resins described herein can also be measured with the same method used to determine solution IV for polyester resins.
  • the glass transition temperature of the polyester resin used as a starting material (hereafter “starting material resin”) in the invention is not restricted and may be defined or influenced by the degree of polymerization and/or co-monomer content of the polyester resin (e.g., the number of polymerized monomer units making up the polymer chain) and/or the molecular weight distribution of a mixture of different polymers of different polymerization degree (polydispersity) and/or the identity and quantity of the monomer or co-monomer units of the polyester resin.
  • a polyester resin having a narrower molecular weight distribution is used because it may show less degradation and a more stable IV upon processing than a polyester resin having a broad molecular weight distribution.
  • the glass transition temperature (Tg) of the starting material resin is preferably from 75 to 90° C., more preferably from 80 to 85° C. and most preferably about 82° C.
  • the Tg of resin compositions containing additives may have glass transition temperatures higher or lower than those mentioned above by as much as 5° C.
  • the polyester starting material of the invention may include, but are not limited to, polyester synthesized from aliphatic, aromatic or cyclic (aliphatic or aromatic) dicarboxylic acids, or an aliphatic, aromatic or cyclic (aliphatic or aromatic) ester, with an aromatic, aliphatic or cyclic (aliphatic or aromatic) diol; or an esters prepared from two or more aliphatic, aromatic or cyclic (aliphatic or aromatic) esters.
  • polyesters include, but are not limited to, polyethylene terephthalate, polyethylene naphthalate, polyethylene isophthalate, polypropylene terephthalate, polybutylene terephthalate, poly(1,4-cyclohexylene dimethylene terephthalate) and polyethylene-2,6-naphthalene dicarboxylate, and mixtures thereof. Copolymers, blends and mixtures thereof are also included.
  • Preferred embodiments of the present invention use polyethylene terephthalate polymers having copolymerized therewith from 0 to 5 wt % of isophthalic acid (or the dialkyl isophthalate counterpart, depending on whether the polyester is produced from a terephthalic acid or dimethyl (or dialkyl) terephthalate based process) and from 1 to 3 wt % of diethylene glycol.
  • Dicarboxylic acids include, but are not limited to, aromatic dicarboxylic acids, such as terephthalic acid, isophthalic acid, phthalic acid and 2,6-naphthalenedicarboxylic acid; aliphatic dicarboxylic acids, such as adipic acid, azelaic acid, sebacic acid and decanedicarboxylic acid; and alicyclic dicarboxylic acids, such as cyclohexanedicarboxylic acid.
  • aromatic dicarboxylic acids such as terephthalic acid, isophthalic acid, phthalic acid and 2,6-naphthalenedicarboxylic acid
  • aliphatic dicarboxylic acids such as adipic acid, azelaic acid, sebacic acid and decanedicarboxylic acid
  • alicyclic dicarboxylic acids such as cyclohexanedicarboxylic acid.
  • Diols include, but are not limited to, aliphatic diols such as 1,4-butanediol, 1,3-propanediol, 1,6-hexanediol, monoethylene glycol, diethylene glycol, triethylene glycol and polyethylene glycol; alicyclic diols, such as 1,4-cyclohexanedimethanol; and aromatic diols such as bisphenol A. These diacids and diols may be used alone or in combination of two or more.
  • polyester components include, but are not limited to, phthalic anhydride, trimellitic acid, pyromellitic acid, dimeric acid and 5-sodiumsulfoisophthalic acid.
  • Suitable catalysts can be any catalyst for polymerizing polyesters, including, but not limited to, catalysts based on antimony, titanium, germanium, zinc or combinations thereof.
  • the starting material resin is in the form of a solid particle and has a substantially uniform IV distribution across all dimensions of the particles.
  • Conventional resins in the form of solid particles made with conventional solid-state polymerization may have a substantial intrinsic viscosity gradient when in the form of a chip or pellet.
  • a chip or pellet having an IV gradient may have an IV that varies across the dimension of the pellet and/or chip.
  • a particular pellet of polyester resin may have an IV of 0.9 when measured at the exterior of a pellet or chip and an IV that is different from the IV measured at the interior of the pellet and/or chip (e.g., there may be an IV gradient of as much as 0.20 to 0.30 IV dL/g across the dimension of the chip and/or pellet).
  • Such an IV gradient normally does not affect the overall or average IV of the polyester resin when measured in the bulk. However it may introduce variability into the IV determination of small samples of the polyester resin if there is an insufficient amount of polyester resin in the sample and thus the sample does not provide a representative cross-section of materials present in the polyester pellets and/or chips.
  • the existence of the IV gradient in a conventional solid form resin may be due to solid-state polymerization during which the resin particles are heated in the solid form and ethylene glycol may be formed and released (e.g., as the resin undergoes further condensation and chain lengthening). If the ethylene glycol is slow to diffuse out of the resin its presence may slow the chain lengthening reaction.
  • the starting material resin used in the process of the present invention has not been previously subjected to conventional (external heating) crystallization and/or solid-state polymerization and preferably has minimal (no more than 0.05 dl/g) IV gradient within the resin particle or substantially less intrinsic viscosity variation (e.g., gradient) across the resin particle.
  • the IV of the starting resin of the present invention may, in one aspect of the invention, vary by no more than 0.05, preferably no more than 0.03 across any dimension of the resin particle.
  • An additional advantage of the present invention ultra-high IV polyester is that the resin preferably does not contain any phthalate plasticizer.
  • Di (2-ethylhexyl) phthalate, or DEHP is the most commonly used of a group of related chemicals called phthalates or phthalic acid esters.
  • the greatest use of DEHP is as a plasticizer for polyvinylchloride (PVC) and other polymers including rubber, cellulose and styrene.
  • PET in general, and the present invention ultra-high IV polyester specifically usually does not contain DEHP or any other plasticizer, and does not require such plasticizers for effective use of the polyester.
  • a further advantage of the present invention ultra-high IV polyester is that the resulting molded products (such as gallon size detergent bottles) qualify as standard bottle grade PET and can be readily recycled in the same recycle stream as PET beverage bottles bearing the recycling symbol and identifier “1” or “PETE”.
  • the starting material resin of 0.65 to 0.90 IV has been crystallized directly from the melt by the method of underwater pelletization and latent heat crystallization.
  • the ultra-high IV polyester resin of the invention is prepared by conventional SSP processing of the starting material resin. The present inventors have found that when the melt-polymerized and latent heat crystallized starting material resin has an IV in the range of 0.65 to 0.90, the IV lift found during SSP processing is surprisingly higher that the IV lift observed during SSP processing of conventional lower IV resins (IV range of 0.50 to 0.65).
  • the present invention provide a faster SSP IV lift rate, but the rate appeared to stay nearly constant throughout the SSP processing of the resin, up to a stopping IV of 1.2 to 1.3. This gave an SSP time that was significantly shorter than that required to reach such an IV level using conventional resins.
  • the enhanced SSP lift rate is due to a combination of factors including (i) lower and more uniform degree of crystallization of the starting material, (ii) more uniform molecular weight distribution and therefore more uniform distribution of reactive end groups in the starting material, and/or (iii) enhanced diffusivity of condensation reaction by-products as a result of a more open crystalline structure produced by latent heat crystallization to a low level of crystallinity.
  • the processing of the invention includes heating the ultra-high IV polyester resin above its melting temperature. Further preferably, the polyester resin is heated to the point where it is a free-flowing liquid. In a further preferable embodiment of the invention, the polyester resin is subjected to high shear stress while heating. High shear stress conditions are those conditions which may be observed or created in processes such as conventional injection molding and/or extrusion which result in melting and mixing of the polyester resin during processing.
  • blow molding also known as blow forming
  • blow forming is a manufacturing process by which hollow plastic parts are formed. It is a process used to produce hollow objects from thermoplastic.
  • extrusion blow molding injection blow molding
  • stretch blow molding there are three main types of blow molding: extrusion blow molding, injection blow molding, and stretch blow molding.
  • the blow molding process begins with melting down the plastic and forming it into a parison or preform.
  • the parison is a tube-like piece of plastic with a hole in one end in which compressed air can pass through.
  • the basic process has two fundamental phases. First, a preform (or parison) of hot plastic resin, often in a somewhat tubular shape, is created. Second, a pressurized gas, usually air, is used to expand the hot preform and press it against a mold cavity. The pressure is held until the plastic cools. This action identifies another common feature of blow molded articles. Part dimensional detail is better controlled on the outside than on the inside, where material wall thickness can alter the internal shape. Once the plastic has cooled and hardened the mold opens up and the part is ejected.
  • a pressurized gas usually air
  • EBM extrusion blow molding
  • Types of equipment for continuous EBM may be categorized as follows: rotary wheel blow molding systems and shuttle machinery.
  • Examples of parts made by the EBM process include dairy containers, shampoo bottles, hoses/pipes, and hollow industrial parts such as drums.
  • Intermittent extrusion blow molding may be also called shot extrusion. Parison shot extrusion is accomplished by means of a reciprocating screw almost identical to those used in injection molding machines.
  • intermittent blow molding there are two main types of processes: straight intermittent is similar to injection molding whereby the screw turns, then stops and pushes the melt out.
  • the accumulator method an accumulator gathers melted plastic and when the previous mold has cooled and enough plastic has accumulated, a rod pushes the melted plastic and forms the parison. In this case the screw may turn continuously or intermittently.
  • the processing may be carried out on a polyester resin that is dried or undried.
  • a dried polyester resin is a crystallized resin that has been heated in its solid state to a temperature above the glass transition temperature in a dehumidifying environment.
  • a dried polyester resin contains less than 1,000 ppm, preferably less than 500 ppm, more preferably less than 50 ppm, especially preferably less than 25 ppm of water based upon the weight of the water relative to the total weight of the resin. Drying may also be accomplished by exposing the polyester resin to a dehumidified atmosphere to thereby remove water adsorbed or absorbed by the polyester resin.
  • Undried polyester resin may be a polyester resin that contains water or a resin that is free of water.
  • a resin that is free of water may be one that is obtained by solidifying a polyester resin liquid obtained directly from a polyester polymerization process in an atmosphere that is substantially free of water (e.g., substantially free of water includes atmospheres that have 99%, preferably 99.5%, more preferably 99.9% by volume free of water vapor).
  • an undried polyester resin may be one that has not undergone heating in the solid state.
  • An undried polyester resin may be one that is obtained in the solid form from a polyester polymerization process then stored in an atmosphere that is not inert and/or not dried (e.g., dehumidified). Water vapor present in the atmosphere may absorb onto the surface of the polyester resin and/or may absorb into the matrix of the polyester resin. An amount of water of as much as 5% by weight based upon the weight of the water relative to the total weight of the resin may be present.
  • the polyester resin used in the method of the invention is an undried water-free resin or a dried resin.
  • the solid form ultra high IV polyester resin is dried before processing by the EBM process of the present invention.
  • the drying may be carried out in a conventional drier by passing dehumidified air over chips and/or pellets of the solid form polyester resin.
  • the polyester resin is dried in a dehumidified environment for 2 to 10 hours, more preferably 4 to 8 hours and most preferably about 6 hours.
  • the dehumidified gas passing over the polyester pellets and/or chips has a dew point of less than ⁇ 10° C., preferably less than ⁇ 20° C., more preferably less than ⁇ 40° C., even more preferably less than ⁇ 50° C., most preferably less than ⁇ 60° C.
  • the dehumidified gas passing over the polyester pellets has a temperature in the range 220 to 400° F., preferably 260 to 360° F., more preferably 300 to 320° F.
  • polyester resin starting materials made without solid-state polymerization include those resins described in U.S. Published Application 2007/0128389 and U.S. Published Application 2007/0248778, each of which has been incorporated by reference in its entirety above.
  • the starting material resin used in the method of the invention is a resin that is prepared without solid-state polymerization.
  • a resin prepared without solid-state polymerization may include a resin that is made to its final intrinsic viscosity (e.g., that viscosity which is measured on the pellets or the commercially transported form) with less than 0.03 dL/g solid-state polymerization (e.g., heating of the resin in the solid-state at a temperature and for a period of time sufficient for increasing the IV by 0.03 dL/g or more).
  • the resin of the invention is made without solid-state polymerization and has an IV achieved substantially by polymerizing the monomer units in the melt phase.
  • the solid form resin thus obtained is not subsequently heated to a temperature at which a further or finishing polymerization may be achieved.
  • the starting material resin used in the method of the invention may have a minor degree of polymerization that is at least partially achieved by heating the resin in the solid form after it is made by melt polymerization and isolated in the solid phase.
  • a resin used in the method of the invention may have an IV of 0.70 and may be derived from a resin having an IV of 0.65 achieved by carrying out polymerization without conventional solid-state polymerization.
  • subsequent handling or heating of resin in the solid form either through a solid-state heating or through other means such as drying at elevated temperature may increase the intrinsic viscosity by an amount of, for example, 0.03 dL/g.
  • the resin, having a final IV of 0.70 is produced by first forming a resin having an IV of 0.67 without conventional solid-state polymerization then increasing the IV of the resin by a minor amount (e.g., 0.03 dL/g) to thus prepare a resin having a final IV of 0.70.
  • a minor amount e.g. 0.03 dL/g
  • the IV of the resin used in the process of the invention is increased by no more than 0.05, preferably 0.04, more preferably, 0.03 after the resin is initially isolated from melt polymerization.
  • the term without solid state polymerization includes resins that are made by melt polymerization to a first IV then further polymerized in the solid-state to a second IV that is less than 0.03 dL/g higher than the first N.
  • the IV of the polyester resin that may be used in the method of the invention may fall within a wide range.
  • the IV of the starting polyester resin may be from 0.6 to 1.0 dL/g, preferably from 0.65 to 0.9, more preferably from 0.7 to 0.85, even more preferably from 0.72 to 0.80, especially preferably about 0.76.
  • the solid-state polymerization process to which the starting material resin is subsequently subjected to achieve the final product of the invention may include multiple steps such as preheating, solid-state-polymerization, and cooling and may use multiple types of commercially utilized, batch, semi-continuous, or continuous SSP reactors.
  • SSP reactors may be agitated or unagitated examples of which may include a vacuum oven, a rotary vacuum dryer, a co- or counter-flow gas-purged horizontal rotary reactor, and a co- or counter-flow gas-purged down-flow vertical reactor.
  • the conventional steps of pre-crystallization and crystallization are not required since the starting material resin has already been crystallized shortly after pelletization by a direct latent heat crystallization method.
  • the temperature profile of the SSP process may more rapidly achieve the desired reaction temperature as compared with a conventional SSP process.
  • the steady-state temperature of the SSP process should be in the range of 190 to 230° C., preferably 200 to 225° C., more preferably 210 to 220° C. and most preferably about 215° C. depending on the level of co-monomer in the starting material resin.
  • the polyester resin starting material is in the form of a solid (e.g., a solid-form polyester resin).
  • the initial solid-form polyester resin may be in the form of chips or pellets.
  • the solid-form polyester resin may contain an amount of regrind or recycled polyester of from 0 to 50% by weight based upon the total weight of the polyester resin, preferably the recycled or regrind material is present in an amount of no more than 25% by weight, more preferably no more than 10% by weight, even more preferably no more than 5% by weight, in a most preferred embodiment the solid-form polyester resin is a virgin resin containing no regrind or recycled polyester material and is in the form of distinct solid particles (e.g., pellets and/or chips).
  • these articles are ground, chipped or otherwise reduced into smaller parts (e.g., particles) for the purpose of preparing the resin for reuse.
  • the particulate form material thereby obtained is commonly known as “regrind” or “post-industrial recycle” (PIR).
  • the regrind may be introduced into the virgin resin stream.
  • the amount of regrind that may be present in the resin used to manufacture articles such as preforms for blow molding bottles and/or containers may vary over a wide range depending on availability of the resin, the end purpose of the formed article, and other various factors. Regrind may constitute from 0 to 100% of the resin used to form a processed (e.g., injection molded) article such as a preform that may be used to blow mold a container.
  • thermoforming may include regrind in an amount of from about 40 to 100%
  • EBM may include about 20 to 60% regrind
  • custom containers may include regrind from about 0 to 20%
  • CSD/Beer containers include regrind from about 0 to 30%, where % is % by weight based on the amount of regrind and the total weight of the resin.
  • Amounts of regrind that vary from the above amounts may be present including any range or sub-range of the ranges above including any increment of 1, 2, 3, 5, and 10%.
  • the extruded shaped article formed from the ultra-high IV polyester resin is a molten parison used to make handleware.
  • the parison contains the polyester resin but in other embodiments the parison may include additives or may be a mixture of the polyester with one or more other resins.
  • the parison is fabricated from the polyester resin by melt extrusion.
  • the parison may be of any size including the range of from 50 or less grams to 200 or more grams for each parison.
  • the extrusion of the polyester resin to form the EBM parison may be carried out under different conditions.
  • extrusion is carried out with an EBM apparatus that is capable of completely melting the polyester resin and having sufficient injection pressure to rapidly extrude the molten resin through a shaped die into the desired parison shape.
  • the extruder portion of such a molding apparatus may contain a plurality of heating zones. The temperature of each heating zone is independently controlled. The number of heating zones is not limited, preferably, the number of heating zones is 4 or more, more preferably 5 or more, more preferably 6 or more, more preferably 7 or more, more preferably 8 or more, even more preferably 9 or more, most preferably 10 or more.
  • Each heating zone is capable of heating the polyester resin to a temperature above the melting temperature of the polyester resin.
  • the temperature of any zone may vary from, for example, 400 to 600° F., preferably from 450 to 550° F., more preferably from 475 to 525° F., most preferably about 500° F. Any of the aforementioned temperatures may be varied by any increment of, for example, 2, 4, 6, 8 or 10° F., or any multiple thereof.
  • the screw speed of an EBM apparatus used to carry out the molding may be varied as needed to adjust cycle time and other factors of the extrusion process.
  • the screw speed may be from 5 to 100 rpm, preferably from 10 to 80 rpm, more preferably from 20 to 60 rpm, more preferably from 30 to 50 rpm, more preferably about 40 rpm.
  • the screw speed may be varied in any increment of 1, 2, 4, 6, 8 and 10 rpm within any of the aforementioned ranges, or any multiple thereof.
  • the head pressure of the extrusion process may be varied and may range from 0 to 1800 psig, preferably from 300 to 1500 psi, more preferably from 800 to 1200 psi.
  • the cycle time is preferably less than 30 seconds, more preferably less than 20 seconds, and most preferably less than 10 seconds.
  • the cycle time is the total time from clamp open to clamp open.
  • the cycle time is usually defined by the following functions; mold close, blow air injection, hot-knife cut, mold shuttle, part cooling, mold open, part ejection, mold return, mold close. Simultaneously and within the same amount of time, resin is being melted into a liquefied state, the resin is undergoing conditioning (e.g.
  • One method includes feeding the resin into an extruder for melting and mixing within a heated extruder with a revolving screw that compresses and conditions the polymer as it changes phase from a solid to a liquid, the liquefied resin is then continuously extruded into a hollow parison which is subsequently captured into a mold. Since these actions may dependently coincide, a correlation can be drawn between the time of the cycle, and the time that the polymer is in the liquid phase. This correlation may differ from bottle parison to bottle parison and from mold to mold and from machine to machine.
  • the hoop stretch ratio of the EBM container may be, for example, from 3 to 7 times, preferably from 3.5 to 6.5 times, more preferably from 4 to 6 times, most preferably from about 4.5 to about 5.5 times, even more preferably about 5 times.
  • the bottle parison may be blown into a straight wall mold or into shaped and/textured molds and of all sizes may be used without restriction.
  • One handleware bottle form is a two-liter or larger laundry detergent bottle.
  • Another form is a one-gallon juice bottle.
  • the container formed from the polyester parison is preferably free of haze.
  • the temperature of the extruded parison may be adjusted so that haze is not observed in the EBM article. A parison temperature that is too low during EBM may result in unacceptable material distribution whereas a parison temperature that is too high may result in haze or unacceptable material distribution.
  • the polyester resin starting material obtained without solid-state polymerization is made by processing directly from a finisher (e.g., a wiped- or thin-film evaporator), through a die and subsequently pelletizing with water cooling and latent heat crystallization.
  • a finisher e.g., a wiped- or thin-film evaporator
  • the starting material resin is extruded in the form of strands that may be cut at temperatures higher than the glass transition temperature of the resin.
  • the strands are cut at temperatures that are 50, 100, 150, or 200° C. or more above the glass transition temperature of the resin concurrently or after the strands have passed through a water bath.
  • the chips are preferably separated from the water as quickly as possible.
  • the temperature at the exterior of the pellets may be lower than the temperature inside the pellets.
  • the chips and/or pellets may continue to crystallize via their inside residual heat (e.g., latent heat crystallization).
  • the polymer (e.g., resin) used in the invention may be latent heat crystallized or alternatively may be conventionally crystallized.
  • a chip vibrator or a fluidized bed may be used to prevent the chips from sticking together during heating and/or crystallization.
  • One way to reduce the tendency of chips to stick together is by imparting more rapid or more robust crystallinity to the chips and/or pellets formed during cooling and/or cutting. This may especially be the case if the resin contains more than one type of polymer.
  • Suitable comonomers for this purpose include, but are not limited to, isophthalic acid (IPA, or esters thereof), di-ethylene glycol (DEG), cyclohexane di-methanol (CHDM). These co-monomers are used individually in amounts of 1% or higher, preferably 2% or higher, more preferably 3% or higher, most preferably 4% or higher or collectively in amounts of 4% or higher, preferably 5% or higher, and more preferably 6% or higher.
  • IPA isophthalic acid
  • DEG di-ethylene glycol
  • CHDM cyclohexane di-methanol
  • the molten polyester composition is partially cooled to solidify the composition.
  • the temperature to which the polyester compositions are partially cooled is between the glass transition temperature (Tg) and the melting point of the polyester resins.
  • the polymer composition is then maintained at a temperature of 170 ⁇ 50° C., preferably ⁇ 40° C., and more preferably ⁇ 30° C., especially preferably ⁇ 20° C., for PET crystallization by separating the hot chips from the water as quickly as possible. Separation of the solidified polyester composition from, for example, a water bath, may be facilitated with a centrifugal drier, a vibrating plate and/or a vibrating screener, such as those available from Rieter, BKG and Gala Industries.
  • the residual heat of the chips can be used for in-situ (latent heat) crystallization without a conventional crystallizer.
  • this aspect of the invention is carried out on a polyester resin.
  • the polyester starting material resin may be made by a melt-phase reaction carried out in a plurality of reactors connected in series, in parallel, or in both series and parallel.
  • the reaction of the dicarboxylic acid and diol monomers may be carried out in the absence of any solvent (e.g., a diluent component that does not form a substantial portion of the reacted polymer units in the resin composition).
  • the monomer units are reacted to form a material having an intrinsic viscosity that may preferably range in one embodiment of the invention from 0.2 to 0.5 IV prior to the final finisher.
  • the molten material thus formed in the melt-phase reactor is then pumped or transferred to a finishing reactor.
  • the finishing reactor may be a reactor such as a wiped- or thin-film reactor which provides substantial contact between surface areas of the reactor and results in high mixing of the molten reacted melt-phase product.
  • the finishing process may be carried out in one or more reactors connected in series, parallel, or both in series and parallel.
  • one or more falling film or pipe reactors may be included.
  • the resin product obtained from the last finishing reactor may have an intrinsic viscosity of from 0.65 to 0.9, preferably from 0.7 to 0.85, more preferably from 0.72 to 0.80, and especially preferably about 0.76.
  • the molten resin product obtained from the finishing reactor is then preferably subjected to a polymer filtration in the molten form.
  • Polymer filtration may be carried out in one or more steps.
  • the polymerization of the monomer units is preferably carried out to provide a target intrinsic viscosity of from 0.65 to 0.9, more preferably from 0.7 to 0.85, even more preferably from 0.72 to 0.80, especially preferably about 0.76.
  • the polymeric compositions of the invention contain one or more additives such as fillers.
  • Fillers may include materials such as clays, nanomaterials and/or other polymeric materials, e.g., nylon.
  • the polyester compositions of the invention preferably contain a PET resin that contains copolymerized IPA monomer units.
  • the invention encompasses at least a low-IPA and a high-IPA PET resin.
  • a low-IPA composition (i) which contains a PET resin having an amount of IPA monomer units of up to 6% by mol.
  • the low-IPA PET resin contains 4-5 mol % of IPA monomer units.
  • the low-IPA PET resin contains from 2-4 mol % of polymerized IPA monomer units based upon the total number of moles dicarboxylic acid monomer units.
  • the PET resin containing a low amount of IPA monomer units is referred to as the low-IPA PET resin.
  • Another PET resin is a high-IPA PET resin, for example (ii) high-IPA PET resin wherein IPA monomer units are present in an amount of from 6-30 mol %, preferably from 8-25%, and more preferably from 10-20% by mol based on the total number of moles of dicarboxylic acids in the PET polymer. Other ranges include 10-28%, 12-30%, and all ranges and sub-ranges appearing between and any of 14%, 16%, 18%, 20%, 22%, 24%, and 26% and/or the above stated ranges.
  • the polyester compositions of the invention may include a PET matrix resin such as the low-IPA resin or the high-IPA resin described above together with one or more additives such as an inorganic filler or a co-barrier resin.
  • a composition comprising the low-IPA resin contains from 2-8% by weight of a co-barrier resin, where % by weight is based on the total weight of the composition. More preferably, the co-barrier resin is present in the low-IPA PET matrix resin in an amount of from 2-6% by weight, and even more preferably the co-barrier resin is present in an amount of from 4-5% by weight.
  • the starting material resin of the invention contains the high-IPA resin as a matrix and a co-barrier resin.
  • the co-barrier resin is preferably present in the matrix of the high-IPA PET resin in an amount of up to 5% by weight, preferably less than 3% by weight, more preferably up to 1% by weight, where percent by weight is based on the total weight of the composition.

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  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
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  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
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  • Blow-Moulding Or Thermoforming Of Plastics Or The Like (AREA)
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US12/760,030 2010-04-14 2010-04-14 Ultra-high iv polyester for extrusion blow molding and method for its production Abandoned US20110256331A1 (en)

Priority Applications (18)

Application Number Priority Date Filing Date Title
US12/760,030 US20110256331A1 (en) 2010-04-14 2010-04-14 Ultra-high iv polyester for extrusion blow molding and method for its production
EP11717092.8A EP2558514B1 (en) 2010-04-14 2011-04-13 Ultra-high iv polyester for extrusion blow molding and method for its production
JP2013505091A JP5706516B2 (ja) 2010-04-14 2011-04-13 押出ブロー成形のための超高ｉｖポリエステル及びその製造方法
LTEP11717092.8T LT2558514T (lt) 2010-04-14 2011-04-13 Aukšto klampumo iv poliesteris, skirtas ekstruzinio pūtimo formavimui, ir jo gavimo būdas
BR112012026238A BR112012026238B8 (pt) 2010-04-14 2011-04-13 método para produzir uma resina de poliéster de viscosidade intrínseca ultraelevada, resina de poliéster de viscosidade intrínseca ultraelevada, artigo moldado, e, parison
PCT/US2011/032300 WO2011130396A1 (en) 2010-04-14 2011-04-13 Ultra-high iv polyester for extrusion blow molding and method for its production
CN201180029506.XA CN102971358B (zh) 2010-04-14 2011-04-13 用于挤出吹塑的超高iv聚酯及其生产方法
PL11717092T PL2558514T3 (pl) 2010-04-14 2011-04-13 Poliester o bardzo wysokiej lepkości istotnej do wytłaczania z rozdmuchiwaniem i metoda jego produkcji
KR1020127029609A KR101785753B1 (ko) 2010-04-14 2011-04-13 압출 취입 성형용 초고 ｉｖ 폴리에스터 및 그의 제조 방법
ES11717092T ES2715610T3 (es) 2010-04-14 2011-04-13 Poliéster ultraalto IV para el moldeo de soplado por extrusión y procedimiento para su producción
CA2795918A CA2795918C (en) 2010-04-14 2011-04-13 Ultra-high iv polyester for extrusion blow molding and method for its production
MX2012011793A MX341188B (es) 2010-04-14 2011-04-13 Poliéster con ultra-elevada i.v. para moldeo por extrusión-soplado y método para su producción.
TR2019/03694T TR201903694T4 (tr) 2010-04-14 2011-04-13 Ekstrüzyonlu şişirme kalıplamaya yönelik ultra yüksek IV polyester ve üretim yöntemi.
PT11717092T PT2558514T (pt) 2010-04-14 2011-04-13 Poliéster de iv ultra-elevada para extrusão de molde de sopro e método para a sua produção
ARP110101291A AR081078A1 (es) 2010-04-14 2011-04-14 Poliester de vi ultra -elevada para moldeo por soplado y extrusion y metodo para su produccion
TW100113046A TWI516521B (zh) 2010-04-14 2011-04-14 用於擠壓吹塑成型之超高固有黏度聚酯及其製備方法
US13/760,784 US9399700B2 (en) 2010-04-14 2013-02-06 Ultra-high IV polyester for extrusion blow molding and method for its production
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US20180037358A1 (en) * 2011-08-25 2018-02-08 Plastipak Packaging, Inc. Extruded pet parison, container, and method
WO2015157754A1 (en) 2014-04-11 2015-10-15 Dak Americas Llc Ebm epet container drop-impact enhancement
EP3320016A4 (en) * 2014-04-11 2019-11-27 Dak Americas LLC EBM EPET TANK WITH FALL IMPACT IMPROVEMENT
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MX2012011793A (es) 2013-02-26
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