Title of Invention

A METHOD FOR MAKING A POLYESTER POLYMER

Abstract

A method for making a polyester polymer comprising: (1) combining in a reactor a monomer comprising a terephthaloyl moiety; optionally, one or more other monomers containing an aromatic diacid moiety; a monomer comprising an ethylene glycol moiety; a monomer comprising an isosorbide moiety; optionally, one or more other monomers comprising a diol moiety; and optionally, a monomer comprising a diethylene glycol moiety, with a condensation catalyst suitable for condensing aromatic diacids and glycols; and

Full Text

FORM-2 THE PATENTS ACT, 1970 COMPLETE SPECIFICATION SECTION 10 TITLE : A METHOD FOR MAKING A POLYESTER POLYMER. APPLICANT (S): E.I.DU PONT DE NEMOURS AND COMPANY, A DELAWARE CORPORATION, OF 1007 MARKET STREET, WILMINGTON, DELAWARE 19898, UNITED STATES OF AMERICA. The following Specification particularly describes the nature of this invention and the manner in which it is to be performed :- POLYESTERS INCLUDING ISOSORBIDE AS A COMONOMER AND METHODS FOR MAKING SAME Field of the Disclosure This disclosure relates to polyesters and methods of making 5 polyesters, and more specifically to polyesters containing an isosorbide j movely,and methods of making them. Background of the Disclosure The diol 1,4:3,6-dianhydro-D-sorbitol, referred to hereinafter as isosorbide, the structure of which is illustrated below, is readily made from 10 renewable resources, such as sugars and starches. For example, isosorbide can be made from D-glucose by hydrogenation followed by acid-catalyzed dehydration. Isosorbide has been incorporated as a monomer into polyesters 15 that also include terephthaloyl moieties. See, for example, R. Storbeck et al. Makrornol.Chem.. Vol. 194, pp. 53-64 (1993); R. Storbeck et a!, Eolyrner, Vol. 34, p. 5003 (1993). However, it is generally believed that secondary alcohols such as isosorbide have poor reactivity and are sensitive to acid-catalyzed reactions. See, for example, D. Braun et al., 20 J. Prakt.Chem , Vol. 334, pp. 298-310 (1992). As a result of the poor reactivity, polyesters made with an isosorbide monomer and esters of xt§rephthalic acid are expected to have a relatively low molecular weight. /Ballauff et al, Polyesters (Derived from Renewable Sources), Polymeric Materials Encyclopedia, Vol. 8, p. 5892 (1996). Copolymers containing isosorbide moieties, ethylene glycol moieties, and terephthaloyl moieties have been reported only rarely. A copolymer containing these three moieties, in which the mole ratio of ethylene glycol to isosorbide was about 90:10, was reported in published German Patent Application No. 1,263,981 (1968). The polymer was used as a minor component (about 10%) of a blend with polypropylene to improve the dyeability of polypropylene fiber. It was made by melt polymerization of dimethyl terephthalate, ethylene glycol, and isosorbide, but the conditions, which were described only in general terms in the publication, would not have given a polymer having a high molecular weight. Copolymers of these same three monomers were described again recently, where it was observed that the glass transition temperature Tg of the copolymer increases with isosorbide monomer content up to about 200°C for the isosorbide terephthalate homopolymer. The polymer samples were made by reacting terephthaloyl dichloride in solution with the diol monomers. This method yielded a copolymer with a molecular weight that is apparently higher than was obtained in the German Patent Application described above but still relatively low when compared against other polyester polymers and copolymers. Further, these polymers were made by solution polymerization and were thus free of diethylene glycol moieties as a product of polymerization. See R. Storbeck, Dissertation, Universitat Karlsruhe (1994); R. Storbeck, et al., J. Appl. Polymer Science. Vol. 59, pp. 1199-1202(1996). U.S. Patent 4,418,174 describes a process for the preparation of polyesters useful as raw materials in the production of aqueous stoving lacquers. The polyesters are prepared with an alcohol and an acid. One of the many preferred alcohols is dianhydrosorbitol. However, the average molecular weight of the polyesters is from 1,000 to 10,000, and no polyester actually containing a dianhydrosorbitol moiety was made. U.S. Patent 5,179,143 describes a process for the preparation of compression molded materials. Also, described therein are hydroxyl containing polyesters. These hydroxyl containing polyesters are listed to include polyhydric alcohols, including 1,4:3,6-dianhydrosorbitol. Again, however, the highest molecular weights reported are relatively low, i.e. 400 to 10,000, and no polyester actually containing the 1,4:3,6-dianhydrosorbitol moiety was made. Published PCT Applications WO 97/14739 and WO 96/25449 describe choiesteric and nematic liquid crystalline polyesters that include sosorbide moieties as monomer units. Such polyesters have relatively ow molecular weights and are not isotropic. Summary of the Disclosure Contrary to the teachings and expectations that have been aublished in the prior art, isotropic, i.e. semi-crystalline and amorphous or lonliquid crystalline, copolyesters containing terephthaloyl moieties, gthylene glycol moieties, isosorbide moieties and, optionally, diethylene glycol moieties are readily synthesized in molecular weights that are suitable for making fabricated products, such as films, beverage bottles, molded products, sheets and fibers on an industrial scale. The process conditions of the present invention, particularly the amounts of monomers used, depend on the polymer composition that is desired. The amount of monomer is desirably chosen so that the final polymeric product contains the desired amounts of the various monomer units, desirably with equimblar amounts of monomer units derived from a diol and a diacid. Because of the volatility of some of the monomers, including isosorbide, and depending on such variables as whether the reactor is sealed (i.e. is under pressure) and the efficiency of the distillation columns used in synthesizing the polymer, some of the monomers are desirably included in excess at the beginning of the polymerization reaction and removed by distillation as the reaction proceeds. This is particularly true of ethylene glycol and isosorbide. In the polymerization process, the monomers are combined, and are heated gradually with mixing with a catalyst or catalyst mixture to a temperature in the range of about 260°C to about 300°C, desirably 280°C to about 285°C. The catalyst may be included initially with the reactants, and/or may be added one or more times to the mixture as it is heated. The catalyst used may be modified as the reaction proceeds. The heating and stirring are continued for a sufficient time and to a sufficient temperature, generally with removal by distillation of excess reactants, to yield a molten polymer having a high enough molecular weight to be suitable for making fabricated products. In a preferred embodiment, the number of terephthaloyl moieties in the polymer is in the range of about 25% to about 50 mole % (mole % of the total polymer). The polymer may also include amounts of one or more other aromatic diacid moieties such as, for example, those derived from isophthalic acid, 2,5-furandicarboxylic acid, 2,5-thiophenedicarboxylic acid, 2,6-naphthalenedicarboxylic acid, 2,7-naphthalenedicarboxylic acid, and 4,4'~bibenzoic acid, at combined levels up to about 25 mole % (mole % of the total polymer). In a preferred embodiment, ethylene glycol monomer units are present in amounts of about 5 mole % to about 49.75 mole %. The polymer may also contain diethylene glycol moieties. Depending on the method of manufacture, the amount of diethylene glycol moieties is in the range of about 0.0 mole % to about 25 mole %. In a preferred embodiment, isosorbide is present in the polymer in amounts in the range of about 0.25 mole % to about 40 mole %. One or lore other diol monomer units may also be included in amounts up to a otal of about 45 mole %. Of course, all of the percentages are dependent on the particular pplication desired. Desirably, however, equimolar amounts of diacid lonomer units and diol monomer units are present in the polymer. This balance is desirable to achieve a high molecular weight. The polyester has an inherent viscosity, which is an indicator of nolecular weight, of at least about 0.35 dL/g, as measured on a 1% /veight/volume) solution of the polymer in o-chlorophenol at a temperature f 25°C. This inherent viscosity is sufficient for some applications, such as ome optical articles and coatings. For other applications, such as ompact discs, an inherent viscosity of at least about 0.4 dL/g is preferred, ligher inherent viscosities, such as at least about 0.5 dL/g are needed for lany other applications (e.g., bottles, films, sheet, molding resin). Further rocessing of the polyester may achieve inherent viscosities that are even igher. Detailed Description of the Preferred Embodiments of the Disclosure The isotropic polyester polymer, described in detail below, may be lade by the melt condensation of a combination of monomers containing n ethylene glycol moiety, an isosorbide moiety and terephthaloyl moiety, imall amounts of other monomers may be added during the olymerization or may be produced as by-products during the reaction. In a preferred embodiment, ethylene glycol monomer units are resent in amounts of about 5 mole % to about 49.75 mole %, preferably 0 mole % to about 49.5 mole %, more preferably about 25 mole % to bout 48 mole %, and even more preferably about 25 mole % to about 40 lole %. The polymer may also contain diethylene glycol monomer units. Spending on the method of manufacture, the amount of diethylene glycol lonomer units is in the range of about 0.0 mole % to about 25 mole %, preferably 0.25 mole % to about 10 mole %, and more preferably 0.25 mole % to about 5 mole %. Diethylene glycol may be produced as a by¬product of the polymerization process, and may also be added to help accurately regulate the amount of diethylene glycol monomer units that are in the polymer- In a preferred embodiment, isosorbide moieties are present in the polymer in amounts in the range of about 0.25 mole % to about 40 mole %, preferably about 0.25 mole % to about 30 mole % and more preferably about 0.5 mole % to 20 mole %. Depending on the application, isosorbide may be present in any desirable range such as 1 mole % to 3 mole %, 1 mole % to 6 mole %, 1 mole % to 8 mole % and 1 mole % to 20 mole %. One or more other dioi monomer units may optionally be included in amounts up to a total of about 45 mole %, preferably less than 20 mole %, and even more preferably less than 15 mole %, even more preferably less than 10 mole % and even more preferably less than 2 mole %, Examples of these optional other diol units include aliphatic alkylene glycols having from 3-12 carbon atoms and having the empirical formula HO-CnH2n-OH, where n is an integer from 3-12, including branched diols such as 2,2-dimethyl-1,3-propanediol; cis ortrans-1,4-cyclohexanedi-methanol and mixtures of the cis and trans isomers; triethylene glycol; 2,2-bis[4-(2-hydroxyethoxy)phenyl] propane; 1,1-bis[4-(2-hydroxyethoxy)-phenyl]cyclohexane; 9,9-bis[4-(2-hydroxyethoxy)phenyl]fluorene; 1,4:3,6-dianhydromannitol; 1,4:3,6-dianhydroiditol; and 1,4-anhydroerythritol. In a preferred embodiment, the number of terephthaloyl moieties in the polymer is in the range of about 25 mole % to about 50 mole %, more preferably about 40 mole % to about 50 mole %, even more preferably about 45 mole % to about 50 mole % (mole % of the total polymer). The polymer may also include amount of one or more other arornatic biacid moieties such as, for example, those derived from isophthalic acid, 2,5- furandicarboxylic acid, 2,5-thiophenedicarboxylic acid, 2,6-naphthalenedi-carboxylic acid, 2,7-naphthalenedicarboxylic acid, and 4,4'-bibenzoic acid, at combined levels up to about 25 mole %, preferably up to 10 mole %, more preferably up to about 5 mole % (mole % of the total polymer). Of course, all of the percentages are dependent on the particular application desired. Desirably, however, equimolar amounts of diacid monomer units and diol monomer units are present in the polymer. This balance is desirable to achieve a high molecular weight. The polyester has an inherent viscosity, which is an indicator of molecular weight, of at least about 0.35 dL/g, as measured on a 1% (weight/volume) solution of the polymer in o-chlorophenol at a temperature of 25°C. This inherent viscosity is sufficient for some applications, such as some optical articles and coatings. For other applications, such as compact discs, an inherent viscosity of about 0.4 dL/g is preferred. Higher inherent viscosities are needed for many other applications (e.g., bottles, films, sheet, molding resin). The conditions can be adjusted to obtain desired inherent viscosities up to at least about 0.5 and desirably higher than 0.65 dL/g. Further processing of the polyester may achieve inherent viscosities of 0.7, 0.8, 0.9,1.0, 1.5, 2.0 dL/g and even higher. The molecular weight is normally not measured directly. Instead, the inherent viscosity of the polymer in solution or the melt viscosity is used as an indicator of molecular weight. For the present polymers, the inherent viscosity is measured by the method described previously, with a molecular weight corresponding to an inherent viscosity of about 0.35 or more being sufficient for some uses. Higher molecular weights, corresponding to inherent viscosities of about 0.45 or more, may be required for other applications. Generally, the inherent viscosity/molecular weight relationship can be fitted to the linear equation: log (IV) = 0.5856 x log (Mw) - 2.9672. he inherent viscosities are a better indicator of molecular weight for omparisons of samples and are used as the indicator of molecular weight herein. Some of the polyesters of the invention can be made by any of several methods. The product compositions vary somewhat depending on the method used, particularly in the amount of diethylene glycol moieties that are present in the polymer. These methods include the reaction of the diol monomers with the acid chlorides of terephthalic acid and any other acids that may be present. The reaction of terephthaloyl dichloride with isosorbide and ethylene glycol is readily carried out by combining the monomers in a solvent (e.g., toluene) in the presence of a base, such as pyridine, which neutralizes HCI as it is produced. This procedure is described in R. Storbeck et al., J. Appl. Polymer Science, vol. 59, pp. 1199 -1202 (1996). Other well-known variations using terephthaloyl dichloride may also be used (e.g., interfacial polymerization), or the monomers may simply be stirred together while heating. When the polymer is made using the acid chlorides, the ratio of monomer units in the product polymer is about the same as the ratio of reacting monomers. Therefore, the ratio of monomers charged to the reactor is about the same as the desired ratio in the product. A stoichiometric equivalent of the diol and diacid is desirably used to obtain a high molecular weight polymer. The polymers can also be made by a melt polymerization process, in which the acid component is either terephthalic acid or dimethyl terephthlate, and also may include the free acid or dimethyl ester of any other aromatic diacids that may be desired in the polyester polymer composition. The diacids or dimethyl esters are heated with the diols (ethylene glycol, isosorbide, optional diols) in the presence of a catalyst to a high enough temperature that the monomers combine to form esters and diesters, then oligomers, and finally polymers. The polymeric product at the end of the polymerization process is a molten polymer. The diol monomers (e.g., ethylene glycol and isosorbide) are volatile and distill from the reactor as the polymerization proceeds. The melt process conditions of the present invention, particularly the amounts of monomers used, depend on the polymer composition that is desired. The amount of diol and diacid or dimethyl ester thereof are desirably chosen so that the final polymeric product contains the desired amounts of the various monomer units, desirably with equimolar amounts of monomer units derived from the diols and the diacids. Because of the volatility of some of the monomers, including isosorbide, and depending on such variables as whether the reactor is sealed (i.e. is under pressure) and the efficiency of the distillation columns used in synthesizing the polymer, some of the monomers may need to be included in excess at the beginning of the polymerization reaction and removed by distillation as the reaction proceeds. This is particularly true of ethylene glycol and isosorbide. The exact amount of monomers to be charged to a particular reactor is readily determined by a skilled practitioner, but often will be in the ranges below. Excesses of ethylene glycol and isosorbide are desirably charged, and the excess ethylene glycol and isosorbide are removed by distillation or other means of evaporation as the polymerization reaction proceeds. Terephthalic acid or dimethyl terephthalate is desirably included in an amount of about 50% to about 100 mole %, more preferably 80 mole% to about 100 mole % of the diacid monomers that are charged, with the remainder being the optional diacid monomers. Isosorbide is desirably charged in an amount of about 0.25 mole % to about 150 mole % or more compared with the total amount of diacid monomers. The use of diethyiene glycol monomer is optional, and is often made in situ. If diethyiene glycoi is added, it is charged in an amount up to about 20 mole % of the total amount of diacid monomers. Ethylene glycol is charged in an amount in the range of about 5 mole % to about 300 mole %, desirably 20 mole % to about 300 mole % of the diacid monomers, and the optional other diols are charged in an amount up to about 100 mole % of the diacid monomers. The ranges given for the monomers are very wide because of the wide variation in monomer loss during polymerization, depending on the efficiency of distillation columns and other kinds of recovery and recycle systems, and are only an approximation. Exact amounts of monomers that are charged to a specific reactor to achieve a specific composition are readily determined by a skilled practitioner. In the melt polymerization process of the invention, the monomers are combined, and are heated gradually with mixing with a catalyst or catalyst mixture to a temperature in the range of about 260°C to about 300°C, desirably 280°C to about 285°C. The exact conditions and the catalysts depend on whether the diacids are polymerized as true acids or as dimethyl esters. The catalyst may be included initially with the reactants, and/or may be added one or more times to the mixture as it is heated. The catalyst used may be modified as the reaction proceeds. The heating and stirring are continued for a sufficient time and to a sufficient temperature, generally with removal by distillation of excess reactants, to yield a molten polymer having a high enough molecular weight to be suitable for making fabricated products. Catalysts that may be used include salts of Li, Ca, Mg, Mn, Zn, Pb, Sb, Sn, Ge, and Ti, such as acetate salts and oxides, including glycol adducts, and Ti alkoxides. These are generally known in the art, and the specific catalyst or combination or sequence of catalysts used may be readily selected by a skilled practitioner. The preferred catalyst and preferred conditions differ depending on whether the diacid monomer is polymerized as the free diacid or as a dimethyl ester. Germanium and antimony containing catalysts are the most preferred. The monomer composition of the polymer is chosen for specific uses and for specific sets of properties. For uses where a partially crystalline polymer is desired, as for example food and beverage containers, such as hot fill or cold fill bottles, fibers, and films, the polymer will generally have a monomer composition in the range of about 0.1% to about 10%, preferably about 0.25% to about 5% on a molar basis of isosorbide moieties, about 49.9 to about 33 % on a molar basis of ethylene glycol moieties, about 0.0 to 5.0%, preferably 0.25 % to about 5 % on a molar basis of diethyiene glycol moieties, and not more than about 2 % on a molar basis of other diol moieties, such as 1,4-cyclohexanedi-methanol. For the bottle resins, the diacid comprises terephthaloyl moieties at a level of about 35 % to about 50 % on a molar basis, and optional other aromatic diacid moieties at levels of up to about 15 % on a molar basis, where the optional aromatic diacid moieties may be derived from 2,6-naphthalenedicarboxylic acid, isophthalic acid, 4,4'-dibenzoic acid, and mixtures thereof. For applications where it is desirable to have an amorphous polymer, such as would be used to make transparent optical articles, the amount of isosorbide moiety is in the range of about 2 % to about 30 % on a molar basis, the ethylene glycol moieties are present in an amount of about 10 % to about 48 % on a molar basis, optional other diols such as 1,4-cyclohexanedimethanol moieties are present in an amount up to about 45 % on a molar basis, diethyiene glycol moieties are present in an amount of about 0.0% to about 5%, preferably 0.25 % to about 5 % on a molar basis, terephthaloyl moieties are present at a level of about 25 % to about 50 %, and other optional diacid moieties, such as 2,6-naphthalenedicarboxylic acid, isophthalic acid, 4,4'-dibenzoic acid, and mixtures thereof, are present in amounts up to a total of about 25 %, on a molar basis. Some of these compositions (i.e. those having isosorbide at levels of less than about 12 %) are semi-crystalline if they are cooled slowly from the melt or if they are annealed above their glass transition temperatures, but are amorphous if they are cooled rapidly from the melt. In general, the compositions that can be semi-crystalline are slower to crystallize than poly(ethylene terephthalate) compositions, so that it is easier to make transparent articles that remain transparent using crystallizable copolymers even though they may be exposed to conditions under which they can crystallize. The melt polymerization process of the present invention is desirably carried out using either dimethyl esters (e.g., dimethyl terephthalate) as reactants or using the free diacid as a reactant. Each process has its own preferred catalysts and preferred conditions. These are described generally below. These are analogous to the well known processes for making poly(ethylene terephthalate). The usefulness of these methods in obtaining high molecular weight polymer is surprising in view of the disclosures by others who have worked with isosorbide polyesters and in view of the generally held expectations that secondary diols have low reactivities and esters of secondary alcohols have reduced thermal stability. These two processes are somewhat different and are described below. Dimethyl Terephthalate Process in this process, which is carried out in two steps, terephthalic acid and the optional diacid monomers, if present, are used as their dimethyl ester derivatives. In minor amounts, e.g., 1-2 wt %, free diacids may also be added. The diols (e.g., ethylene glycol and isosorbide) are mixed with the dimethyl ester of the aromatic diacid (e.g., dimethyl terephthalate) in the presence of an ester interchange catalyst, which causes exchange of s the ethylene glycol for the methyl group of the dimethyl esters through a transesterification reaction. This results in the formation of methanol, which distills out of the reaction flask, and bis (2-hydroxyethyl-terephthalate). Because of the stoichiometry of this reaction, somewhat more than two moles of ethylene glycol are desirably added as reactants for the ester interchange reaction. Catalysts that bring about ester interchange include salts (usually acetates) of the following metals: Li, Ca, Mg, Mn, Zn, Pb, and combinations thereof, Ti(OR)4, where R is an alky! group having 2-12 carbon atoms, and PbO. The catalyst components are generally included in an amount of about 10 ppm to about 100 ppm. Preferred catalysts for ester interchange include Mn(OAc)2, Co(OAc)2, and Zn(OAc)2, where OAc is the abbreviation for acetate, and combinations thereof. The polycondensation catalyst in the second stage of the reaction, preferably Sb(lll) oxide, may be added now or at the start of the polycondensation stage. A catalyst that has been used with particularly good success is based on salts of Mn(ll) and Co(ll), at levels of about 50 to about 100 ppm, each. These were used in the form of Mn(ll) acetate tetrahydrate and Co(ll) acetate tetrahydrate, although other salts of the same metals may also be used. Ester interchange is desirably brought about by heating and stirring the mixture of reactants under an inert atmosphere (e.g., nitrogen) at atmospheric pressure from room temperature to a temperature high enough to induce the ester interchange (about 150°C). Methanol is formed as a by-product and distills out of the reactor. The reaction is gradually heated to about 250°C until methanol evolution stops. The end of methanol evolution can be recognized by a drop in the overhead temperature of the reaction vessel. A small amount of an additive having a boiling point of 170 - 240°C may be added to the ester interchange to aid in the heat transfer within the reaction medium and to help retain volatile components in the vessel that may sublime into the packed column. The additive must be inert and not react with alcohols or dimethyl terephthalate at temperatures below 300°C. Preferably, the additive has a boiling point greater than 170°C, more preferably within the range of 170°C to 240°C, and is used in an amount between about 0.05 and 10 wt %, more preferably between about 0.25 and 1 wt % of reaction mixture. A preferred additive is tetrahydronaphthalene. Other examples include diphenyl ether, diphenyl-sulfone and benzophenone. Other such solvents are described in U.S. Patent 4,294,956, the contents of which are hereby incorporated by reference. The second stage of the reaction is commenced by adding a polycondensation catalyst and a sequestering agent for the transesterification catalyst. Polyphosphoric acid is an example of a sequestering agent and is normally added in an amount of about 10 to about 100 ppm of phosphorous per gm of dimethyl terephthalate. An example of a polycondensation catalyst is antimony (III) oxide, which may be used at a level of 100 to about 400 ppm. The polycondensation reaction is typically carried out at a temperature from about 250°C to 285°C. During this time, ethylene glycol distills out of the reaction due to condensation of the bis(2-hydroxyethy!) terephthalate to form polymer and by-product ethylene glycol, which is collected as a distillate. The polycondensation reaction described above is preferably carried out under vacuum, which can be applied while the reactor is being heated to the temperature of the polycondensation reaction after polyphosphoric acid and Sb(lll) oxide have been added. Alternatively, vacuum can be applied after the polycondensation reaction temperature reaches 280°C - 285oC. In either case, the reaction is accelerated by the application of vacuum. Heating under vacuum is continued until the molten polymer reaches the desired molecuiar weight, usually recognized by an increase in the melt viscosity to a pre-determined level. This is observed as an increase in the torque needed for the stirring motor to maintain stirring. An inherent viscosity of at least 0.5 dL/g, and generally up to about 0.65 dL/g or greater can be achieved by this melt polymerization process without further efforts at raising molecular weight. For certain composition ranges, the molecular weight can be increased further by solid state polymerization, described below. Terephthalic Acid Process The terephthalic acid process is similar to the dimethyl terephthalate process except that the initial esterification reaction that leads to bis(2-hydroxyethylterephthalate) and other low molecular weight esters is carried out at a slightly elevated pressure (autogenous pressure, about 25 to 50 psig). Instead of a two-fold excess of diols, a smaller excess (about 10% to about 60%) of diols (ethylene glycol, isosorbide and other diols, if any) is used. The intermediate esterification product is a mixture of oligomers, since not enough dioi is present to generate a diester of terephthalic acid. The catalysts are also different. No added catalyst is necessary in the esterification reaction. . A polycondensation catalyst (e.g., Sb(lll) or Ti(IV) salts) is still desirable to achieve a high molecular weight polymer. The catalyst that is needed to achieve a high molecular weight can be added after the esterification reaction, or it can be conveniently charged with the reactants at the beginning of the reaction. Catalysts that are useful for making a high molecular weight polymer directly from terephthalic acid and the diols include the acetate or other alkanoate salts of Co(ll) and Sb(lll), oxides of Sb(lll) and Ge(IV), and Ti(OR)4 (where R is an alkyl group having 2 to 12 carbon atoms). Glycol solubilized oxides of these metal salts may also be used. The use of these and other catalysts in the preparation of polyesters is well known in the art. The reaction may be carried out in discrete steps, but this is not necessary. In practice on a large scale, it may be carried out in steps as the reactants and intermediate products are pumped from reactor to reactor at increasing temperatures. In a batch process, the reactants and catalyst may be charged to a reactor at room temperature and then gradually heated to about 285°C as polymer forms. The pressure is vented in the range of about 200°C to about 250°C, and a vacuum is then desirably applied. Esterification to form bis(2-hydroxyethylterephtha!ate) esters and oligomers takes place at elevated temperatures (between room temperature and about 220°C to 265°C under autogenous pressure), and polymer is made at temperatures in the range of about 275°C to about 285°C under a high vacuum (less than 10 Torr, preferably less than 1 Torr). The vacuum is needed to remove residual ethylene glycol, isosorbide and water vapor from the reaction to raise the molecular weight. A polymer having an inherent viscosity of at least 0.5 dL/g, and generally up to about 0.65 dL/g can be achieved by the direct polymerization process, without subsequent solid state polymerization. The progress of the polymerization can be followed by the melt viscosity, which is easily observed by the torque that is required to maintain stirring of the molten polymer. Solid State Polymerization Polymers can be made by the melt condensation process described above having an inherent viscosity of at least about 0.5 dL/g, and often as high as about 0.65 dL/g or greater without further treatment, measured by the method described above. This corresponds to a molecular weight that is suitable for many applications (e.g., molded products). Polymers with lower inherent viscosities can also be made, if desired, as for compact discs. Other applications, such as bottles, may require a still higher molecular weight. Compositions of ethylene glycol, isosorbide , and terephthalic acid having isosorbide in an amount of about 0.25% to about 10% on a mole basis may have their molecular weight increased further by solid state polymerization. The product made by melt polymerization, after extruding, cooling, and pelletizing, is essentially non¬crystalline. The material can be made semi-crystalline by heating it to a temperature in the range of about 115°C to about 140°C for an extended period of time (about 2 to about 12 hours). This induces crystallization so that the product can then be heated to a much higher temperature to raise the molecular weight. The process works best for low levels of isosorbide (about 0.25 mole % to about 3 mole %), because the polyester crystallizes more easily with low levels of isosorbide. The polymer may also be crystallized prior to solid state polymerization by treatment with a relatively poor solvent for polyesters which induces crystallization. Such solvents reduce the glass transition temperature (Tg) allowing for crystallization. Solvent induced crystallization is known for polyesters and is described in U.S. Patent Nos. 5,164,478 and 3,684,766, which are incorporated herein by reference. The crystallized polymer is subjected to solid state polymerization by placing the pelletized or pulverized polymer into a stream of an inert gas, usually nitrogen, or under a vacuum of 1 Torr, at an elevated temperature, above about 140°C but below the melting temperature of the polymer for a period of about two to 16 hours. Solid state polymerization is generally carried out at a temperature in the range of about 190° to about 210°C for a period of about two to about 16 hours. Good results are obtained by heating the polymer to about 195° to about 198°C for about 10 hours. This solid state polymerization may raise the inherent viscosity to about 0.8 dL/g or higher. It should, of course, be apparent to those skilled in the art that othe additives may be included in the present compositions. These additives include plasticizers; pigments; flame retardant additives, particularly, decabromodiphenyl ether and triarylphosphates, such as triphenylphosphate; reinforcing agents, such as glass fibers; thermal stabilizers; ultraviolet light stabilizers processing aids, impact modifiers, flow enhancing additives, nucleating agents to increase crystallinity, and the like. Other possible additives include polymeric additives including ionomers, liquid crystal polymers, fluoropolymers, olefins including cyclic olefins, polyamides, ethylene vinyl acetate copolymers and the like. This invention is further illustrated by the following non-limiting examples. Examples The polymer molecular weights are estimated based on inherent viscosity (I.V.), which is measured for a 1% solution (wt./volume) of polymer in o-chlorophenol at a temperature of 25°C. The levels of catalyse components are expressed as ppm, based on a comparison of the weight of the metal with the weight of either the dimethyl terephthalate or terephthalic acid, depending on which monomer is used. Example 1 The following polymerization reactants are added to a 4-liter polymerization flask fitted with a jacketed Vigreux column with air cooling, a mechanical stirrer, and a water-cooled condenser: dimethyl terephthalate (780.133g), isosorbide (70.531 g), and ethylene glycol (531.211g). The reactants are present in a mole ratio of 1: 0.12: 2.13, respectively. The catalyst is also charged and consists of Mn(ll) acetate tetrahydrate (0.296g), Co(ll) acetate tetrahydrate (0.214g), and Sb(lll) oxide (0.350g). This corresponds to 85 ppm manganese (weight of metal as a fraction of the weight of dimethyl terephthalate), 65 ppm cobalt, and 375 ppm antimony. The flask is purged with a stream of nitrogen while the temperature is raised to 150°C over a period of one hour, using a fluidized sand bath as a heating medium. At this time, the nitrogen purge is stopped and the evolution of methanol commences. Methanol is continuously collected as the reaction is further heated to 250°C over the course of approximately 2 hours. By noting when the temperature drops at the top of the Vigreux column it is possible to determine the end of methanol evolution, indicating the finish of the first step of the reaction, which is the transesterification of the diols and dimethyl terephthalate. At this point, 82 ppm of phosphorous is added in the form of a polyphosphoric acid solution in ethylene glycol. In this case, 1.854g of the solution, which has a concentration of 10.91g P per 100g of polyphosphoric acid solution is used. Heating is continued. The reaction is heated to 285°C over a period of about 2 hours. Vacuum is then applied. Alternatively vacuum can be applied gradually after the polyphosphoric acid solution is added, which allows the heating to 285°C to proceed faster, and thus requires a shorter time (about 12 hours). During this time, ethylene glycol distills off, and a low molecular weight polymer forms. Once the reaction reaches 285°C, it is placed under vacuum if it has not already been placed under vacuum. It is preferred to achieve a vacuum of less than 1 Torr. The molten polymer is heated under vacuum at 285oC for about 2 hours, until the polymer achieves sufficient melt viscosity, as determined by an increase in torque of the stirrer. When sufficient viscosity is achieved, the polymerization is stopped, and the flask is removed from the sand bath. The molten polymer is extruded and pelletized, or the cooled polymer is removed from the flask and ground. The chopped, ground or pelletized polymer is laid out on an aluminum pan in an oven. Under a nitrogen stream, the polymer is heated to 115oC over a period of 4 hours and then held at that temperature for another 6 hours. This allows the polymer flake to partially crystallize. After this treatment, the polymer is placed in a stream of nitrogen and heated, again over a period of 4 hours, to 190°-195°C and held at this elevated temperature for another 12 hours. This effects a solid-state polymerization and allows the molecular weight to be significantly increased, as judged by the inherent viscosity (I.V.) of the polymer solution in ortho-chlorophenol. The solution I.V. of the material increases from about 0.5 dL/g to about 0.7 dL/g during the solid state polymerization. The monomer unit composition of the polymer, determined by proton NMR, is about 3% isosorbide, 46% ethylene glycol, 1% diethylene glycol, and 50% terephthalic acid, all expressed as a mole % of the polymer. It is noteworthy that the amount of isosorbide in the polymer is approximately half of the amount that was charged, when compared with the amount of terephthalic acid. Unreacted isosorbide was found in the distillates, especially in the ethylene glycol. The amount of isosorbide in the polymer by this process thus is very dependent on the efficiency of the distillation or other separation methods that are used in the process. A skilled practitioner can readily establish specific process details according to the characteristics of the reactor, distillation columns, and the like. Example 2 The following monomers are added to a 5-gallon reactor: terephthalic acid, 8,638.9g; isosorbide, 911.9g; and ethylene glycol, 3,808.5g. The reactants are present in a mole ratio of 1: 0.12: 1.18, respectively. Catalyst components are also added at this time, as follows: Co(ll) acetate tetrahydrate, 1.825g; and Sb(lll) oxide; 3.103g. The catalyst amounts correspond to 50 ppm cobalt and 275 ppm antimony, expressed as the weight of metal compared with the weight of terephthalic acid. The polymerization reactor is equipped with a fractional distillation column and a stirrer. The reactor is purged with nitrogen and then closed under 50 psig of nitrogen pressure. The temperature is raised to 265°C over a period of about five hours while the reactants are stirred. The pressure increases to 70 psig during this time, as esterification takes place. At the end of this time period, the pressure is vented back to 50 psig. Water and ethylene glycol distill from the reactor. The temperature is maintained at 265°C. Within an hour, the contents of the reactor are a clear, viscous melt. The excess pressure in the reactor is then vented. A solution of ethylene glycol and polyphosphoric acid (3.45 weight % phosphorous) is pumped into the reactor. This corresponds to about 50 ppm phosphorous (weight of phosphorous compared with the weight of terephthalic acid). The reactor is then placed under vacuum, while the reactor is heated to the polymerization temperature of 285°C. The distillation of water and excess diol continue. An ultimate vacuum of 1 Torr is reached within an hour. Polymerization and distillation continue for an additional 2-3 hours, at which time the torque of the stirrer reaches a pre-determined level. The polymerization is stopped, and the molten polymer is extruded from the reactor, cooled, and chopped. This polymer is nearly identical to the polymer made in Example 1 before solid state polymerization. It has an inherent viscosity of about 0.5 dL/g. The monomer composition of the polymer, determined by proton NMR, is as follows: terephthalic acid, 50%; isosorbide, 3%; ethylene glycol, 46%; and diethylene glycol, 1%. Us inherent viscosity is increased further from about 0.5 dL/g to about 0.7 dL/g, using the same solid state polymerization procedure as was used in Example 1. Example 3 Purified terephthalic acid (7.48 kg), isosorbide (3.55 kg), and ethylene glycol (1.70 kg) are placed in a stainless steel stirred reactor preheated to 70°C under nitrogen purge at atmospheric pressure. The reactor is equipped with a packed distillation column. The monomer composition corresponds to a mole ratio of terephthalic acid: ethylene glycol: isosorbide of 1:0.61:0.54. The reactor was heated to 285°C within three hours and the reaction mixture was kept under a positive pressure of 50-60 psi. During this time, a distillate of mostly water is collected from the packed column. After the melt temperature reaches at least 275°C and the terephthalic acid is essentially consumed, as determined by a clearing of the reaction mixture, pressure is released and germanium (IV) oxide catalyst (3.77 g) is added as a solution in ethylene glycol (0.100N Ge02 ethylene glycol. The reaction mixture is stirred for an additional 20 minutes. The pressure in the reactor is reduced to 1-2 mm of mercury for a period of 1 hour and an additional distillation fraction is collected. Afterwards, the reaction product, a viscous resin is extruded into a water bath, cut into pellets and dried in an oven. The resin has a glass transition temperature of 116°C and an inherent viscosity of 0.43 dL/g (measured at 25°C in a 1% (w/v) orthochlorophenol solution). The monomer composition of the polymer is measured by NMR as 49.5 % terephthalate, 30.3 % ethylene glycol residue, 2.0 % diethylene glycol residue, and 18.2 % isosorbide residue, expressed as a mole % of the polymer. Example 4 Dimethyl terephthalate (10.68 kg), isosorbide (5.79 kg), ethylene glycol (4.88 kg), manganese (II) acetate (4.76 g) are placed in a stainless steel stirred reactor under nitrogen purge at atmospheric pressure. The reactor is equipped with a packed distillation column. The monomer composition corresponds to a mole ratio of dimethyl terephthalate: ethylene glycol: isosorbide of 1:1.43:0.72. The reactor is heated to 230°C within three hours, to 240 over the next hour and to 265 over the next hour. During this time a distillate that is mostly methanol is collected from the packed column. After the temperature reaches 284 °C, polyphosphoric acid is added to the reactor. The amornt of polyphosphoric acid is equivalent to 402 mg of phosphorous. Germanium (IV) oxide catalyst, (4.66 g) is added as a solution in ethylene glycol (0.100N Ge02 in ethylene glycol). The pressure inside the reactor is now reduced to 1 mm of mercury over a period of two hours. The reaction mixture is kept under vacuum for three more hours, and an additional distillation fraction is collected while the temperature increases to 285°C. Afterwards, the reaction product, a viscous resin is extruded into a water bath, cut into pellets and dried in an oven. The resin has a glass transition temperature of 106°C and an inherent viscosity of 0.43 dL/g (measured at 25°C in a 1% (w/v) ortho-chlorophenol solution). The monomer composition of the polymer is measured by NMR as 50.1 % terephthalate, 33.5 % ethylene glycol residue, 2.6 % diethylene glycol residue, and 12.9 % isosorbide residue, expressed as a mole % of the polymer. Example 5 The following monomers and additives are added to a five gallon reactor, constructed of 316 stainless steel, that is equipped with a reflux column, packed with stainless 316 Pall rings, and a water cooled condenser: Dimethyl terephthalate, 11.65 Kg; isosorbide, 4.384 Kg; ethylene glycol, 3.724 Kg; manganese(ll)acetate, 7.02 g; antimony oxide, 4.18 g; and 1,2,3,4-tetrahydronaphthalene, 125 ml. A nitrogen purge is placed on the reactor and the contents are heated to 250°C within 180 minutes, then to 275°C during the next 60 minutes. During heat up, a distillate is collected that consists mostly of methanol. When the reaction mixture reaches 270°C, polyphosphoric acid is added in an amount equivalent to 25.4 mg of phosphorous. After reaching 275°C, the pressure inside the reactor is reduced to 1-2 mm of mercury over a period of 240 minutes. The reaction mixture is kept at this pressure for 240 minutes and an additional distillate fraction is collected while the temperature is raised to 285°C. When the melt viscosity reached a predetermined level, measured by the torque required to maintain a constant agitator speed of 50 rpm, the reactor is filled with nitrogen to a pressure of 60 psi and the polymer is extruded through a 0.125 inch diameter die into a water trough. The polymer strand is chopped into pellets and dried in an oven at 100°C for 10 hours. The polymer is found to have a glass transition of 117°C when measured at a heating rate of 10°C per minute. The inherent viscosity, measured in o-chlorophenol at 25°C, is 0.41 dL/g. The polymer composition, determined by proton NMR spectrometry, is 50.6% terephthalic acid moieties, 17.6% isosorbide moieties, 29.9 % ethylene glycol moieties and 1.9 % diethylene glycol moieties. Example 6 The following polymerization reactants are added to a 50 gal. maximum capacity, Hastalloy B polymerization reactor fitted with a 6" radius, Hastalloy B, water cooled reflux column packed with stainless steel rings, a stainless steel helix agitator stirrer, a water-cooled condenser and by-pass: dimethyl terephthalate (78.02kg), isosorbide (15.42kg), and ethylene glycol (49.90kg), which corresponds to a mole ratio of 1: 0.26: 2.00. The catalyst is also charged and consists of Mn(ll) acetate tetrahydrate (29.57g), Co(ll) acetate tetrahydrate (21.43g), and Sb(lll) oxide (35.02g). This corresponds to 85 ppm manganese (weight of metal as a fraction of the weight of dimethyl terephthalate), 90 ppm cobalt, and 375 ppm antimony. The stirred reactor (50rpm) is purged with a stream of nitrogen while the temperature is raised to 250°C over a period of four hours. The reactor is jacketted and uses a temperature controlled, hot oil loop system as a heating medium. Methanol is continuously collected as the reaction is heated above approximately 150°C. By noting when the temperature drops at the top of the packed reflux column it is possible to determine the end of methanol evolution, indicating the finish of the first step of the reaction, which is the transesterification of the diols and dimethyl terephthalate. At this point, 77 ppm of phosphorous is added in the form of a polyphosporic acid solution in ethylene glycol. In this case, 153ml of the solution, which has a concentration of 10.91g P per 100g of polyphosphoric acid solution is used. Also at this time, the nitrogen purge is stopped. Heating is continued. The reaction is heated to 285°C over a period of about 2 hours. Vacuum is then gradually applied using a multi-vane vacuum pump with 20 horse-power blower. The attainment of full vacuum, preferrably less than 1 Torr, takes approximately 1 hour. During this time, ethylene glycol distills off, and a low molecular weight polymer forms. The molten polymer is heated under vacuum at 285DC for about 2 hours, until the polymer achieves sufficient melt viscosity, as determined by an increase in torque of the stirrer. When sufficient viscosity is achieved, the polymerization is stopped, and the reactor is emptied through a heated die at the bottom. The molten polymer emerges as a strand that when cooled through immersion in a cold water trough can be chopped into pellets. The polymer pellets are dried overnight in a rotating drum heated to 120°C. The cooled polymer is removed from the flask and ground. The solution inherent viscosity (I.V.) of the material is 0.64 dL/g. The monomer unit composition of the polymer, determined by proton NMR, is about 6% isosorbide, 42% ethylene gyicol, 2% diethyiene glycol, and 50% terephthalic acid, all expressed as a mole % of the polymer. It is noteworthy that the amount of isosorbide in the polymer is approximately half of the amount that is charged, when compared with the amount of terephthalic acid. Unreacted isosorbide is found in the distillates, especially in the ethylene glycol. The amount of isosorbide in the polymer by this process thus is very dependent on the efficiency of the distillation or other separation methods that are used in the process. A skilled pra^itioner can readily establish specific process details according to the characteristics of the reactor, distillation columns, and the like. Example 7 The second example is prepared in a way similar to Example 6 except that a smaller reactor (5 gal. maximum capacity) is used. The reagent equivalent ratios are also changed in order to prepare a polymer with a greater content of isosorbide. Thus, dimethyl terephthalate (10,680g), isosorbide (5F787g), and ethylene glycol (4,881g), which corresponds to a mole ratio of 1:0.72:1.43 are charged to the reactor in a similar fashion as before along with the catalyst consisting of Mn(ll) acetate tetrahydrate (4.76g), and Ge(IV) oxide (4.66g). This corresponds to 100 ppm manganese (weight of metal as a fraction of the weight of dimethyl terephthalate) and 300 ppm germanium. The germanium oxide is added in the form of a solution in ethylene glycol (0.100 N GeC>2 in ethylene glycol). A solution of polyphosphoric acid in ethylene glycol is added in a similar way as before, in this case 9.6ml, which has a concentration of 3.45g P per 100ml of polyphosphoric acid solution, is used. The polymerization proceeded in a similar fashion as before, however, the resultant finished resin did not achieve the same inherent viscosity within the given time. In this case a solution I.V. of 0.42dL/g is observed. It was also observed that the monomer unit composition of the polymer, determined by proton NMR, is about 13% isosorbide, 34% ethylene gylcol, 3% diethylene glycol, and 50% terephthalic acid, all expressed as a mole % of the polymer. The extent of isosorbide incorporation is somewhat lower in this case than previously observed but reflects the efficiency of the differing reactors rather than the polymer made. Example 8 The third example is prepared in a way similar to the first except that a larger reactor (100gal) equipped with a stainless steel anchor type stirrer is used. The monomers charged are such that an isosorbide content in the finished polymer would be 1 mole %, assuming that some of the input isosorbide would be distilled off during polymerization. As such, dimethyl terephthalate (197 kg),isosorbide (5.12 kg), and ethylene glycol ( 135 kg) along with the catalysts: Mn(ll) acetate tetrahydrate (72.1 g), Co(ll) acetate tetrahydrate (54.1 g) and Sb(lll) oxide (88.5 g) are used. This corresponds to 82 ppm manganese, 65 ppm Co, and 375 ppm Sb calculated using the same basis as in Example 1. The transesterification process is carried in an analogous way as for example 1. A polyphosphoric acid solution in ethylene glycol is added such that 80 ppm of P is used to sequester the transition metals after the transesterification step and before the polycondensation as outlined in Example 1. The polycondensation is also similar to the previous example. Polymer is extruded and pelletized to give clear, colorless resin. The pelletized polymer is loaded into a tumble dryer and under a stream of nitrogen is heated to 115°C over a period of 4 hours and then held at that temperature for another 6 hours. This allows the polymer to partially crystallize. After this treatment, a vacuum is applied to the tumble dryer ulitmately achieving a vacuum less than 1mm of Hg. The heating is continued and reaches a maximum of 213°C. It is then held at this elevated temperature for a total of approximately 15 hours. This effects a solid-state polymerization and allows the molecular weight to be significantly increased, as judged by the inherent viscosity (I.V.) of the polymer solution in ortho-chlorophenol. The solution I.V. of the material increases from about 0.5 dL/g to about 0.7 dL/g during the solid state polymerization. Example 9 This polymer is prepared in a similar way to that for Example 8 except that the amounts of diols were changed in order to result in a resin with a somewhat increased isosorbide content. Thus, the only alterations are in the amount of isosorbide charged, 17.8kg, and the amount of Mn(ll) acetate tetrahydrate catalyst used, 79.2 g corresponding to 90ppm Mn(ll) calculated on the same basis as in the above example. The transesterification and polycondensation are repeated as has been just described. Also, the finished polymer is pelletized, crystallized, and solid-state polymerized in an identical fashion to the previous example. This results in a polymer with approximately 3 mole % isosorbide content. Example 10 This example describes a blend of isosorbide containing polymers with nucleating agents and glass fiber. The purpose of nucleating agents is to increase crystallinity and thereby improve the thermal resistance (heat deflection temperature) of the blends. The polymer of Examples 6, 7, and 9 are blended together with the nucleating agent sodium bicarbonate (Aldrich) and glass fiber type OCF 183 (PPG, Pittsburgh, PA) using the Leistritz brand extruder (Model MC 1866/GL, Leistritz AG). Then, the blends are injection molded into test parts using the Arburg molding machine as described in Example 5. The molded parts (Examples 10a-c) are heat treated in an oven at 130°C for 30 minutes. The compositions and results are summarized below. Table ASTM test method Composition(weight %) Example 10a Example 10b Example 10c Example 10d Example 10e PEIT-3 70 0 0 70 0 PEIT-6 0 70 0 0 70 PEIT-13 0 0 70 0 0 OCF-183 29.6 29.6 29.6 30 30 sodium bicarbonate 0.4 0.4 0.4 0 0 D638 tensile modulus(Mpsi) 1.19 1.26 1.26 1.28 na D638 tensile elong @ bk(%) 1.94 1.85 1.29 2.55 na D638 tensile stress@bk(Ksi) 15.6 16.9 12.8 16.6 na D256 Notched Izod (ft-lb)@20°C 0.82 1.19 2.17 1.33 1.93 D3763 Multiaxial impact load(lb) @ max.load (208C) 296 305 287 236 265 D3763 Multiaxial impact load(lb) @ max.load (-20°C) 314 302 294 na na D3763 Multiaxial impact load(lb) @ max.load (-40°C) 315 321 287 na na D648 HDT(°C) @264 psi 136 147 106 81 r_ 88 It is to be understood that the above described embodiments are illustrative only and that modification throughout may occur to one skilled in the art. Accordingly, this invention is not to be regarded as limited to the embodiments disclosed herein. WE CLAIM: A method for making a polyester polymer comprising: (1) combining in a reactor a monomer comprising a terephthaloyl moiety; optionally, one or more other monomers containing an aromatic diacid moiety; a monomer comprising an ethylene glycol moiety; a monomer comprising an isosorbide moiety; optionally, one or more other monomers comprising a diol moiety; and optionally, a monomer comprising a diethylene glycol moiety, with a condensation catalyst suitable for condensing aromatic diacids and glycols; and (2) heating said monomers and said catalyst to a temperature sufficient to polymerize said monomers into a polyester polymer having at least terephthaloyl moieties, ethylene glycol moieties and isosorbide moieties; wherein said heating is continued for a sufficient time to yield an isotropic polyester having an inherent viscosity of at least about 0,35 dL/g when measured as a 1 % (weight/volume) solution of said polyester in o-chlorophenol at a temperature of 25oC, wherein an additional in added optionally half retain volatil comprimints The method as claimed claim 1, wherein said process optionally includes stirring of said monomers during said heating and the concurrent removal of by-products by distillation and/or evaporation. The method as claimed in claim 1, wherein said monomer comprising a terephthaloyl moiety is terephthalic acid. The method as claimed in claim 3, wherein water and unreacted monomer are removed while said monomers polymerize. The method as claimed in claim 1, wherein said monomer comprising a terephthaloyl moiety is dimethyl terephthalate. The method as claimed in claim 5, wherein methanol and unreacted monomer are removed while said monomers polymerize. The method as claimed in claim wherein said additive is tetrahydronapthalene. The method as claimed in claim 1, wherein said one or more optional other diols are selected from the group consisting of aliphatic alkylene glycols and branched aliphatic glycols having from 3-12 carbon atoms and having the empirical formula HO-CnH2n-OH, where n is an integer from 3-12; cis and trans-1,4-cyclohexanedimethanol and mixtures thereof; triethylene glycol; 2,2-bis[4-(2-hydroxyethoxy)phenyl]propane; 1,1 -bis[4-(2-hydroxyethoxy) phenyl]cyclohexane; 9,9-bis[4-(2-hydroxy-ethoxy)phenyl]fluorene; l,4:3,6-dianhydromannitol; l,4:3,6-dianhydroiditol; and 1,4-anhydroerythritol. The method as claimed in claim 1, wherein said one or more optional other aromatic diacids are selected from the group consisting of isophthalic acid, 2,5-furandicarboxylic acid, 2,5-thiophenedicarboxylic acid, 2,6-naphthalenedicarboxylic acid, 2,7-naphthalenedicarboxylic acid, and 4,4'-bibenzoic acid. The method as claimed in claim 1, wherein said monomers are included in amounts such that said terephthaloyl moieties are present in an amount of about 40 mole % to about 50 mole % of said polyester, one or more optional other aromatic diacid moieties are present in an amount up to about 10 mole % of said polyester, said ethylene glycol moieties are present in an amount of about 10 mole % to about 49.5 mole % of said polyester, diethylene glycol moieties are present in an amount of about 0.25 mole % to about 10 mole % of said polyester, said isosorbide moieties are present in an amount of about 0.25 mole % to about 40 mole % of said polyester, and said one or more other diol moieties are present in an amount up to about 15 mole % of said polyester. The method as claimed in claim 11, wherein said monomers are included in amounts such that said terephthaloyl moieties are present in an amount of about 45 mole % to about 50 mole % of said polyester, one or more optional other aromatic diacid moieties are present in an amount up to about 5 mole % of said polyester, said ethylene glycol moieties are present in an amount of about 10 mole % to about 49.5 mole % of said polyester, diethylene glycol moieties are present in an amount of about 0.25 mole % to about 5 mole % of said polyester, said isosorbide moieties are present in an amount of about 0.25 mole % to about 30 mole % of said polyester, and other diol moieties are present in an amount up to about 10 mole % of said polyester. The method as claimed in claim 1, optionally comprising increasing the molecular weight of said polyester by solid state polymerization. The method as claimed in claim 12 , wherein said solid state polymerization comprises: (a) crystallizing said polyester by heating said polyester to a temperature in the range of about 115°C to about 140°C or treating said polyester with a solvent which reduces the glass transition temperature of the polyester allowing for crystallization; and (b) heating said polyester under vacuum or in a stream of inert gas at an elevated temperature above about 140°C but below the melting temperature of said copolyester to yield a copolyester having an increased inherent viscosity. The method as claimed in claim 13, wherein said heating step (b) is carried out at a temperature of about 195° to about 198°C for about 10 hours. The method as claimed in claim 12,wherein said inherent viscosity is increased to at least about 0.8 dL/g. The method as claimed in claim 12, wherein said polyester comprises from about 0.25 mole % to about 10 mole % isosorbide moieties. Dated this 3rd day of October, 2000. [DR. RAMESH KUMAR MEHTA] OF REMFRY & SAGAR ATTORNEY FOR THE APPLICANTS

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