FIELD
The present disclosure relates to heat resistant polyester. The present disclosure also relates to a
process for the preparation of heat resistant polyester and products thereof.

BACKGROUND
Polyethylene terephthalate (PET) is a thermoplastic polymer extensively used for packaging
applications due to its features such as acceptable process ability and barrier properties,
recyclability and compatibility with food applications. Further, the packaging articles prepared
from PET are light in weight, unbreakable and have aesthetic appeal.
Packaging articles prepared from PET and used for packaging foodstuffs such as fruit juices,
food concentrates, sport drinks, ketchups, sauces and jams need to be hot fillable to achieve
desired shelf-life of the products.
Extensive research is being carried out to improve hot fillability of polyethylene terephthalate by
adding isosorbide monomer. The polyethylene terephthalate modified by isosorbide exhibits
glass transition temperature (Tg) from 82 to 180
o
C based on the quantity of isosorbide used in
the polyethylene terephthalate.
For instance, US6818730 suggests a process for producing isosorbide-containing polyesters.
US20120177854 suggests a process for the preparation of polyester by using terephthalic acid,
cyclohexanedimethanol and isosorbide.

US5959066 suggests a method for the preparation of polyester. In the method, 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, are combined with a condensation catalyst and heated to
prepare the polyester.

US6025061 suggests a method for making a sheet. The method consists of preparing a polyester
and producing a sheet from the polyester. The polyester contains terephthaloyl moieties;
optionally, one or more other aromatic diacid moieties; ethylene glycol moieties; isosorbide 3

moieties; and, optionally, one or more other diol moieties, wherein said polyester has an inherent
viscosity of at least about 0.35 dL/g.

US6063464 suggests a process for producing polyesters. The process contains steps of
combining one or more monomers comprising a diacid moiety; a monomer comprising an
isosorbide moiety; and one or more monomers comprising another diol moiety; with a
condensation catalyst andheating to a polymerization temperature to produce a polyester polymer
having the diacid moieties, the isosorbide moieties and other diol moieties. The polyester obtain
by the process suggested in US6063464 has an inherent viscosity of at least about 0.15 dL/g.

The polyester containers obtained by using polyester obtained by these suggested processes
suffer from several drawbacks due to the hygroscopic nature and high reactivity of isosorbide.
Isosorbide present in the container reacts easily with atmospheric moisture and readily undergoes
oxidative degradation and discoloration. Due to these properties of isosorbide, the polyester
containers are not transparent and do not provide requisite barrier properties and therefore cannot
be used in several applications in food industry.
Further, the polyester containers may not be used for preparing hot fill packaging containers as
they cannot withstand a temperature of 90
o
C and tend to undergo deformation and shrinkage.

Therefore, in light of the foregoing drawbacks, there is a felt need for polyester that is capable of
withstanding high temperature without undergoing any deformation and shrinkage along with
acceptable physical and chemical properties for packaging applications. Further, there is a need
for a process for preparing polyester that is capable of withstanding high temperature without
undergoing any deformation and shrinkage.

OBJECTS:
Some of the objects of the present disclosure which at least one embodiment is adapted to
provide, are described herein below

An object of the present disclosure is to provide heat resistant polyester. 4

Another object of the present disclosure is to provide heat resistant polyester that is capable of
withstanding high temperature.
Still another object of the present disclosure is to provide heat resistant polyester which
possesses enhanced impact strength, tensile strength and elongation properties.
Still another object of the present disclosure is to provide heat resistant polyester having
enhanced barrier properties.

Yet another object of the present disclosure is to provide heat resistant polyester which upon
processing results into transparent and colorless packaging material, a packaging container or a
pre-form.
Yet another object of the present invention is to provide heat resistant polyester having improved
melt flow properties and flow ability to enable manufacturing of thin wall containers by injection
molding process.
Further object of the present disclosure is to provide a process for preparing heat resistant
polyester.
Still further object of the present disclosure is to provide a packaging material, a packaging
container or a pre-form which is capable of withstanding high temperature without undergoing
any deformation and shrinkage.

Other objects and advantages of the present disclosure will be more apparent from the following
description which is not intended to limit the scope of the present disclosure.

SUMMARY:
The present disclosure relates to a process for preparing a polyester having at least one of the
following properties, intrinsic viscosity greater than 0.7 dl/g at 25
o
C; color L* ranges from 72 to
76 %; color b* ranges from -1.5 to -2.5; diethylene content of less than 1.5 %; glass transition
temperature in the range of 81 to 85
o
C; impact strength of 54 to 57 J/M; and tensile strength
from 500 to 600 Kgf/cm2
. The process for preparing the polyester essentially involves the 5

preparation of the isosorbide oligomer and the isosorbide polymer from the isosorbide oligomer.
The isosorbide oligomer or isosorbide polymer is then co-polymerized with the polyester. The
copolymerization isosorbide oligomer or isosorbide polymer may be carried out at any stage of
the preparation of the polyester. The isosorbide oligomer or isosorbide polymer improves the
physical, mechanical and chemical properties of the polyester in which it is co-polymerized.
The polyester obtained in accordance with the process of the present disclosure can be used in
packaging applications such as preparing packaging materials or containers. The material or
container obtained from the polyester of the present disclosure is capable of withstanding a
temperature of 60 to 90
o
C without undergoing any deformation and shrinkage. Further, the
material or container obtained from the polyester of the present disclosure is transparent or has
lower color b* value.

DETAILED DESCRIPTION:
The present disclosure provides polyester that can be used in packaging applications. A
packaging container, a packaging material or a pre-form prepared from the polyester is capable
of withstanding a temperature of 60 to 90
o
C without any deformation and shrinkage. The
polyester of the present disclosure exhibits one or more properties of intrinsic viscosity greater
than 0.7 dl/g at 25
o
C, color L* ranges from 72 to 76 %; color b* ranges from -1.5 to -2.5;
diethylene content of less than 1.5 %; glass transition temperature in the range of 81 to 85
o
C;
impact strength of 54 to 57 J/M; and tensile strength from 500 to 600 Kgf/cm2
. The polyester of
the present disclosure comprises at least one polyester, polymer of isosorbide and aromatic
dicarboxylic acid or ester thereof, and at least one agent.
The polyester present in the polyester product is obtained from the polymerization reaction of at
least one aromatic dicarboxylic acid or ester thereof and alkylene glycol. The aromatic
dicarboxylic acid useful for obtaining the polyester is at least one selected from the group
consisting of terephthalic acid, isophthalic acid, 2,6-napthalene dicarboxylic acid, 3,4'-diphenyl
ether dicarboxylic acid, hexahydrophthalic acid, 2,7-naphthalenedicarboxylic acid, phthalic acid
and 4,4'-methylenebis(benzoic acid), whereas the ester of aromatic dicarboxylic acid that can be
used for obtaining the polyester is at least one selected from the group consisting of dimethyl
terephthalate, dimethyl isophthalate, dimethyl-2,6-naphthalate, dimethyl-3,4'-diphenyl ether 6

dicarboxylate, dimethyl hexahydrophthalate, dimethyl-2,7-naphthalate, dimethyl phthalate and
dimethyl-4,4'-methylenebis(benzoate).
The alkylenediol is selected from the group consisting of from the group consisting of ethylene
glycol, propanediol, butanediol, cyclohexanedimethanol, hexane diol and combinations thereof.

The aromatic dicarboxylic acid used for preparing isosorbide polymer is at least one selected
from the group consisting of terephthalic acid,isophthalic acid and 2,6 naphthalene dicarboxylic
acid. The ester of aromatic dicarboxylic acid used for preparing isosorbide polymer is at least
one selected from the group consisting of dimethyl terephthalate, dimethyl isophthalate and
dimethyl-2, 6-naphthalene dicarboxylate.
Examples of agents useful for the purpose of the present disclosure is at least one selected from
the group consisting of branching agent in an amount of 10 ppm to 2000 ppm, nucleating agent
in an amount of 10 ppm to 2000 ppm and liquid plasticizer in an amount of 0.5 to 2 wt%, at least
one stabilizing agent and at least one anti-oxidizing agent in an amount ranging from 0.1 to 5
%.Other agents useful for the purpose of the present disclosure include at least one end capped
oligomer in an amount from 1 to 20 wt%.
The branching agent useful for the purpose of the present disclosure includes but is not limited to
1,2,4-benzenetricarboxylic acid (trimellitic acid); trimethyl-1,2,4-benzenetricarboxylate; 1,2,4-
benzenetricarboxylic anhydride (trimellitic anhydride); 1,3,5-benzenetricarboxylic acid; 1,2,4, 5-
benzenetetracarboxylic acid (pyromellitic acid); 1,2,4,5-benzenetetracarboxylic dianhydride
(pyromellitic anhydride); 3,3',4,4'-benzophenonetetracarboxylic dianhydride; 1,4,5,8-
naphthalenetetracarboxylic dianhydride; citric acid; tetrahydrofuran-2,3, 4,5-tetracarboxylic acid;
1,3,5-cyclohexanetricarboxylic acid;pentaerythritol, 2-(hydroxymethyl)-1,3-propanediol; 2,2-
bis(hydroxymethyl) propionic acid; sorbitol; glycerol and combinations thereof. Particularly,
branching agents such aspentaerythritol, trimellitic acid, trimellitic anhydride, pyromellitic acid,
pyromellitic anhydride and sorbitol are used.

The nucleating agent improves the crystallinity and increases heat deformation temperature of
the polyester product. The nucleating agent can be organic or inorganic. Examples of inorganic 7

nucleating agent useful for the purpose of the present disclosure include but are not limited to
calcium silicate, nano silica powder, talc, microtalc, aclyn, kaolinite, montmorillonite, synthetic
mica, calcium sulfide, boron nitride, barium sulfate, aluminum oxide, neodymium oxide and a
metal salt of phenyl phosphonate. The inorganic nucleating agent can be modified by an organic
material to improve its dispersibility in the polyester product of the present disclosure.
Examples of organic nucleating agent include but are not limited to carboxylic acid metal salts
such as sodium benzoate, potassium benzoate, lithium benzoate, calcium benzoate, magnesium
benzoate, barium benzoate, lithium terephthalate, sodium terephthalate, potassium terephthalate,
calcium oxalate, sodium laurate, potassium laurate, sodium myristate, potassium myristate,
calcium myristate, sodium octacosanoate, calcium octacosanoate, sodium stearate, potassium
stearate, lithium stearate, calcium stearate, magnesium stearate, barium stearate, sodium
montanate, calcium montanate, sodium toluoylate, sodium salicylate, potassium salicylate, zinc
salicylate, aluminum dibenzoate, potassium dibenzoate, lithium dibenzoate, sodium β-
naphthalate and sodium cyclohexane carboxylate; organic sulfonates such as sodium p-toluene
sulfonate and sodium sulfoisophthalate; carboxylic acid amides such as stearic acid amide,
ethylene bis-lauric acid amide, palmitic acid amide, hydroxystearic acid amide, erucic acid
amide and tris(t-butylamide) trimesate; phosphoric compound metal salts such as benzylidene
sorbitol and derivatives thereof, sodium-2,2'-methylenebis(4,6-di-t-butylphenyl)phosphate, and
2,2-methylbis(4,6-di-t-butylphenyl)sodium.
Examples of liquid plasticizer useful for the purpose of the present disclosure include but are not
limited to N-isopropyl benzene sulfonamide, N-tert-butyl benzene sulfonamide, N-pentyl
benzene sulfonamide, N-hexyl benzene sulfonamide, N-n-octyl benzene sulfonamide, N-methyl-
N-butyl benzene sulfonamide, N-methyl-N-ethyl benzene sulfonamide, N-methyl-N-propyl
benzene sulfonamide, N-ethyl-N-propyl benzene sulfonamide, N-ethyl p-
ethylbenzenesulfonamide, N-ethyl p-(t-butyl)benzene sulfonamide, N-butyl p-butyl benzene
sulfonamide, N-butyl toluene sulfonamide, N-t-octyl toluene sulfonamide, N-ethyl-N-2-
ethylhexyl toluene sulfonamide, N-ethyl-N-t-octyl toluene sulfonamide and tri-octyltrimellitate.
Examples of anti-oxidizing agent include but are not limited to irganox 1010, irganox 1076,
irgafos 126 and irgafos 168. 8

Examples of stabilizing agent include but are not limited to ortho-phosphoric
acid,trimethylphosphate (TMP), triphynylphosphate (TPP) and Triethyl phosphono acetate
(TEPA). Preferably ortho-phosphoric acid is used as stabilizing agent.
Examples of end capped oligomer include but are not limited to oligomers of polyethylene
terephthalate, polybutylene terephthalate, polytrimethylene terephthalate,
polytreimethylenenaphthalate and polybutylenenaphthalate.
The polyester product of the present disclosure additionally may comprise additives which
include but are not limited to pigments; flame retardant additives such as 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; ionomers; liquid crystal polymers; fluoropolymers; olefins including cyclic olefins,
polyamides and ethylene vinyl acetate copolymers.
The present disclosure also provides a process for preparing the polyester. Initially, isosorbide
and at least one anti-oxidizing agent are mixed in water and heated to 60 to 90 ºC, preferably 65
to 75
o
C to obtain an aqueous solution comprising 60 to 95 wt% of isosorbide. Preferably,
isosorbide content in the aqueous solution ranges from 70 to 85 %.

The diol used for preparing isosorbide solution includes but is not limited to mono ethylene
glycol; 1,3-propanediol; 1,4-butanediol; 1,6-hexanediol; 1,8-octanediol; 1,10-decanediol; 1,12-
dodecanediol; 1,14-tetradecanediol; 1,16-hexadecanediol; dimer diol; 1,4-
cyclohexanedimethanol; di(ethylene glycol); tri(ethylene glycol); poly(ethylene ether) glycols;
poly(butylene ether) glycols; (cis, trans) 1,3-cyclohexanedimethanol; (cis, trans) 1,4
cyclohexanedimethanol; 2-methyl-1,3-propanediol; 2,2-dimethyl-1,3-propanediol; 2-butyl-2-
ethyl-1,3-propanediol; trimethylpentanediol.
In one embodiment where cycloaliphatic diol such as (cis, trans) 1,3-cyclohexanedimethanol and
(cis, trans) 1,4 cyclohexanedimethanol is used it is supplemented with at least one additional
cyclic or branched diol.
The aqueous solution of isosorbide is reacted with at least one aromatic dicarboxylic acid or ester
thereof at 200 to 260
o
C to obtain an esterified product or trans-esterified product. The reaction is 9

catalyzed by catalysts such as the acetate or other alkanoate salts of Co(II) and Sb(III), oxides of
Sb(III) 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 such as n-butylstannoic acid can also be used.
Preferable catalysts for reacting isosorbide with at least one aromatic dicarboxylic acid or ester
thereof include antimony trioxide, germanium dioxide, tetraisopropyltitanate. The esterified or
trans-esterified product is simultaneously converted into oligomerized product. The oligomerized
product can be used for coating normal polyester chips and then processed for solid state
polymerization to increase the viscosity of polyester to get improved Tg and mechanical
properties.
The aromatic dicarboxylic acid reacted with isosorbide is selected from the group consisting of
terephthalic acid; isophthalic acid; 2, 6 naphthalene dicarboxylic acid and combinations thereof.
The ester of the aromatic dicarboxylic acid is selected from the group consisting of dimethyl
terephthalate; dimethyl isophthalate; dimethyl-2, 6-naphthalene dicarboxylate and combinations
thereof. The esterified or trans-esterified product depends on the acid used in the reaction.
Accordingly, esterified or trans-esterified product can be D-Glucitol; 1,4:3,6-dianhydro-, 2,2'-(1,
4-benzenedicarboxylate), 2,2'-(1,3-benzenedicarboxylate), diisosorbide-2, 6-naphthalene
dicarboxylate and combinations thereof.
The oligomerized product is subjected to a polymerization reaction using at least one
polymerization catalyst to obtain an isosorbide polymer having an intrinsic viscosity of 0.5 to
0.69 dl/g at 25
o
C. The polymerization reaction of isosorbide oligomer is carried out at 220 to
300
o
C. The polymerization catalyst used for the polymerization of isosorbide polymer is
selected from the group consisting of antimony trioxide, germanium dioxideand cobalt acetate.
The isosorbide oligomer or isosorbide polymer is co-polymerized with polyester of alkylene aryl
dicarboxylate.The co-polymerization of isosorbide oligomer or isosorbide polymer with the
polyester can be done at any stage. In one embodiment, the isosorbide oligomer or isosorbide
polymer can be co-polymerized with the polyester by adding isosorbide oligomer or isosorbide
polymer before the polymerization reaction of alkylene aryl dicarboxylate. Alternatively or
simultaneously, the isosorbide oligomer or isosorbide polymer can be co-polymerized with the 10

polyester by adding isosorbide oligomer or isosorbide polymer during or after the polymerization
reaction of alkylene aryl dicarboxylate monomer.
Examples of alkylene aryl dicarboxylate include but are not limited to ethylene terephthalate;
ethylene isophthalate; ethylene-2,6-naphthalate; ethylene-3,4'-diphenyl ether dicarboxylate;
ethylene hexahydrophthalate; ethylene-2,7-naphthalate; ethylene phthalate and ethylene-4,4'-
methylenebis(benzoate).
Alkylene aryl dicarboxylate is obtained by esterification reaction of aromatic dicarboxylic acid
such as terephthalic acid, isophthalic acid, 2,6-napthalene dicarboxylic acid, 3,4'-diphenyl ether
dicarboxylic acid, hexahydrophthalic acid, 2,7-naphthalenedicarboxylic acid, phthalic acid and
4,4'-methylenebis(benzoic acid) with at least one diol selected from the group consisting of
ethylene glycol, propanediol, butanediol, cyclohexanedimethanol, hexane diol and combinations
thereof. To the alkylenearyldicarboxylate, at least one stabilizing agent and optionally, at least
one end capped oligomer is added. The alkylene aryl dicarboxylate is then subsequently
polymerized to prepare polyester.
Alternatively, alkylene aryl dicarboxylate is obtained from ester of aromatic dicarboxylic acid
such dimethyl terephthalate, dimethyl isophthalate, dimethyl-2,6-naphthalate, dimethyl-3,4'-
diphenyl ether dicarboxylate, dimethyl hexahydrophthalate, dimethyl-2,7-naphthalate, dimethyl
phthalate and dimethyl-4,4'-methylenebis(benzoate) with alkylene glycol such as ethylene
glycol, propylene glycol, butylene glycol, neopentyl glycol, MPdiol, hexane diol, isosorbide. To
the alkylene aryl dicarboxylate, at least one stabilizing agent and optionally, at least one end
capped oligomer is added. The alkylene aryl dicarboxylate is then subsequently polymerized to
prepare polyester.
In one embodiment, the isosorbide oligomer or isosorbide polymer can be co-polymerized with
the polyester by adding isosorbide oligomer or isosorbide polymer before the esterification or
ester interchange reaction. Alternatively or simultaneously, the isosorbide oligomer or isosorbide
polymer can be co-polymerized with the polyester by adding isosorbide oligomer or isosorbide
polymer during or after the esterification or ester interchange reaction.
The polymerization reaction of alkylene aryl dicarboxylate is carried out by a process known to a
person skilled in the art which includes process steps such as polycondensation and solid state 11

polymerization reactions to obtain polyester co-polymerized with isosorbide polymer. The
polyester manufactured in polymerization reaction is crystallized in any convention crystallizer
and subsequently processed in batch or continuous solid state polymerization (SSP) to get the
desired intrinsic viscosity (IV). The batch SSP may be pursed with nitrogen to expedite the
reaction. In continuous SSP the circulating nitrogen gas is used as a carrier of by- products.
The polymerization reaction is carried out using at least one agent selected from the group
consisting of branching agent, nucleating agent and liquid plasiticizer.
Additives may also be added before or during or after the polymerization reaction to impart
requisite property to the resulting polyester. Such additives include but are not limited to
pigments; flame retardant additives such as 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, ionomers, liquid
crystal polymers, fluoropolymers, olefins including cyclic olefins, polyamides and ethylene vinyl
acetate copolymers.
Examples of agents useful for the purpose of the invention are described herein before.
The polyester is extruded and cut underwater to obtain chips of polyester. The chips are dried,
blow molded at 270 to 290
o
C and cooled to obtain a material, a container or a pre-form having a
hot fillable capacity ranging from 70 to 90
o
C. Particularly, the material, the container or the pre-
form has a hot fillable capacity in the range of 70 to 85
o
C.
The present disclosure also provides a packaging product comprising a polyester product of the
present disclosure. The packaging product can be a pre-form or a packaging material or a
packaging container.
The isosorbide polymer produced in accordance with the present disclosure imparts improved
heat resistance, good color (L* > 55% ,a* of -1.0 & b* of -1.0) and transparency(haze value
below 5 NTU), improved melt flow characteristic to the polyester in which it is added. The
polyester prepared in accordance with the present disclosure can be used to manufacture
containers by normal ISBM, IBM, IM, EBM processes (without heat set blow molding process ) 12

for applications in various beverages, sport drinks , sauces, jams etc. which can be filled at a
temperature of 60 to 90
o
C.
The polyester of the present disclosure is used for making the transparent and opaque flexible
and rigid packaging containers, films, sheets, textile fabric and yarns. The polyester of the
present disclosure is also used for making hot fill and cold fill containers by using at least one
moulding process selected from the group consisting of heat set blow moulding process and cold
set blow moulding process.
The present disclosure is further described in light of the following examples which are set forth
for illustration purpose only and not to be construed for limiting the scope of the disclosure.

Quality Parameter Analytical Methods
A. Intrinsic Viscosity
The intrinsic viscosity or IV is a measure of the molecular mass of the polymer and is measured
by dilute solution viscosimetry. All IVs were measured in a 3:2 mixture of phenol-1,2
dichlorobenzene solution, at 25° C. About 8-10 chips were dissolved to make a solution with a
concentration of about 0.5%. The IV was obtained from the measurement of relative viscosity ηr
for a single polymer concentration by using the Billmeyer equation shown below (see F. W.
Billmeyer, J. of Polymer Sci. 1949 IV, 83), which equation is valid for the range c=0.5-0.65
g/dL.
IV=[η]=0.25(ηr−1+3 lnηr)/c.
B. Color
The color parameters were measured with a HunterLabColorFlex Model No 45/0, serial No. CX
0969. Amorphous chips were used without grinding or crystallisation, in the transparent state.
Generally, the changes measured could also be seen. The color of the transparent amorphous
chips was categorized using the CIE tristimulus L*, a* and b* values. The L* indicates the
brightness of the samples, with a high value signifying high brightness. L*=100 stands for
perfectly white; L*=0 is perfectly black. a* value indicates the green-red contrast (− value 13

indicates greenness; + value indicates redness); the b* value indicates blue-yellow contrast (−
value indicates blue; + indicates yellow).
The measurements of the color of the SSP chips were carried out without grinding. The L*
values after SSP are higher because of whitening caused by spherulitic crystallisation of the
polymer.
C. Haze
Haze of blown bottles was measured on panels of about 3 cm diameter and 0.238 mm thickness,
cut from flat parts of a 1.5 L bottle made from a 32 g perform, using a Haze Gard Plus (BYK
Gardner). Haze is the percentage of transmitted light that after passing through the sample is
scattered by more than 2.5° (ASTM D-1003-97). Values are reported as % haze normalized to
the sample thickness (%/mm, or % haze per mm of sample thickness).
In case of experiments performed on smaller scale, test plates were made by injection moulding
(in a cold mould) and haze was visually evaluated.
D. Diethylene Glycol (DEG) content:
To determine the DEG content, the PET was trans-esterified with methanol in an autoclave at
220° C. During this, the PET is depolymerised and the DEG is liberated as the diol. The liquid
formed was analysed by Gas Chromatography (GC) to determine the DEG content of the
polymer, after suitable calibration.
E. COOH End Groups
The PET was dissolved in a mixture of o-cresol and chloroform, under reflux conditions. After
cooling to room temperature, the COOH end groups were determined using potentiometric
titration with ethanolic KOH solution, under a nitrogen atmosphere. The results are expressed in
mVal of COOH/kg of PET (milli equivalent of COOH per kg of PET).
F. DSC analysis
A Perkin-Elmer DSC-7 was used to monitor thermal properties of all copolymers samples at
heating and cooling rates of 10° C. per minute. A nitrogen purge was utilized to prevent
oxidation degradation. The results are expressed as glass transition temperatures (Tg), 14

crystallization exotherm peak temperatures and heats of crystallization (∆H), as well as peak
endotherm temperatures and heats of fusion for all materials.
The disclosure will now be described with the help of following non-limiting examples.
Example 1: Preparation of Isosorbide polymer
Step 1A: Preparation of isosorbide solution
80 kg of isosorbide and 20 kg of water along with 0.5 kg mixture of Irganox 1010, irganox 1076
and 1 kg of Irgafos-168 were added into additive preparation vessel equipped with agitator,
heating coils and venting lines through a head condenser to obtain a mixture. The mixture was
heated gently at 60
o
C for 20 minutes to obtain 100 kg of an aqueous solution containing 80%
isosorbide.
Step 1B: Preparation of isosorbide oligomer
In a 200 lit. volume reactor, equipped with a stirrer, nitrogen sweep, a vacuum connection, a
device for collecting distillates, and means for heating and stirring, was charged 75 kg of above
prepared aqueous solution of isosorbide, 60.1 kg of isophthalic acid (IPA) and 140 mg of n-
butylstannoic acid. The molar ratio of isosorbide: IPA was 1.16:1. The reactor was purged with
nitrogen and the contents of the reactor were heated with stirring. The temperature was raised to
240
o
C and held there for about 20 minutes to remove water formed as a by-product of the
condensation reaction. After about 30 minutes at 250
o
C, a clear solution was obtained. The clear
solution was heated at 250
o
C for another 1.5 hours until no more water evolves to obtain105kg
of isosorbide oligomer.

Step 1C: Preparation of 100 mole% polyisosorbideisophthalate master batch.
The above isosorbide oligomer was polymerized in an autoclave by adding 200 ppm of antimony
trioxide as antimony, 50 ppm of cobalt acetate as cobalt at 260
o
C by applying vacuum to obtain
100kg of amorphous polyisosorbideisophthalate.


15

Example 2: Preparation of modified polyethyylene terephthalate through PTA process
In a 250 lit. reactor equipped with a stirrer, condenser, pressurizing and vacuum system 82 kg of
terephthalic acid (PTA) and 36.0 kg of mono ethylene glycol (PTA: MEG mole ratio of 1:1.16)
were made into a paste and fed to the reactor. 4.65kg of polyisosorbideisophthalate, 24 gm
(200ppm as Sb) of antimony trioxide catalyst, 4.32 gm (30 ppm as Ge) GeO2 catalyst, 25 gm (60
ppm as Co) of Cobalt Acetate powder, 12 g (120 ppm) of Pentaerythritol, 6g (60 ppm) of sodium
acetate, 0.25 wt% nButyl benzene sulfonamide (nBBSA) were also added in the reactor to obtain
a mixture. The mixture was heated to 250 °C to obtain a reaction mass comprising ethylene
terephthalate monomer. 18 gm (50 ppm as P) of orthophosphoric acid was added to the reaction
mass containing ethylene terephthalate monomer. The reaction mass containing ethylene
terephthalate monomer was transferred via a 10 micron filter to the polycondensation reactor in
which the polycondensation reaction was conducted at 270- 285 °C with a peak temperature of
288 °C. The polycondensation reaction was monitored based on reactor agitator power
consumption and reaction was terminated to obtain amorphous polyethylene terephthalate having
I.V of about 0.621 dl/g copolymerized with polysisosorbideisophthalate, the amorphous
polyethylene terephthalate was extruded out as strands and cut under water and collected as
amorphous chips. These amorphous chips were dried and pre-crystallized before subjecting to
solid state polymerization (SSP) for increasing the I.V. to 0.838 dl/g.

Example 3: Preparation of polyethyle terephthalate through DMT process
35.4 kg of ethylene glycol (EG) and 95.9 kg of dimethyl terephthalate (DMT), were charged in
the reactor and heated with stirring. 4.65 kg of polyisosorbideisophthalate was charged in the
reactor. Initially, heating rate was controlled to maintain 140 °C in the reactor. After reaching
140 °C, 84.7gm (200 ppm as Mn) of manganese acetate catalyst solution, 25 gm (60 ppm as Co)
of Cobalt Acetate powder, 12 g (120 ppm) of pentaerythritol, and 6g (60 ppm) of sodium acetate
were added to the reactor to initiate the trans-esterification reaction during which methanol was
distilled off through the packed column via the condenser. The temperature of top column was
maintained at 75°C to avoid loss of ethylene glycol. The temperature of the reaction mass was
gradually and slowly increased from 140 °C to 230 °C in 150 min. After the completion of trans-
esterification reaction, 17gm (50 ppm as P) of phosphoric acid was added to the trans-esterified 16

reaction mass as a stabilizer and reaction mass was filtered through 10 micron filter into the
polycondenzation reactor.
The polycondensation reactor was gradually evacuated to a pressure of 0.5 mb and heated to 280
°C. The polycondensation reaction was monitored based on reactor agitator power consumption
and reaction was terminated to obtain amorphous polyethylene terephthalate having I.V of 0.618
dl/g, copolymerized with polysisosorbideisophthalate. The polyethylene terephthalate was
extruded to amorphous chips. Subsequently, the amorphous PET chips were crystallized in batch
solid stat polymerization at temperature of 140°C and upgraded to final I.V of 0.84 dl/g.
Example 4: Preparation of polyethylene terephthalate through post-consumer recycled
(PCR) process
In a 250 lit. reactor equipped with a stirrer, condenser, pressurizing and vacuum system, 39 kg of
terephthalic acid (PTA) and 17 kg of monoethylene glycol (PTA:MEG mole ratio of 1:1.16)
were made into a paste and fed to the esterification reactor. 50 kg of hot wash cleaned
polyethylene terephthalate bottle flakes (post-consumer recycled –PCR) corresponding to 50
wt%; 4.65 kg of polyisosorbideisophthalate, 24 gm (200ppm as Sb) of antimony trioxide
catalyst, 4.32 gm (30 ppm as Ge) GeO2 catalyst, 25 gm (60 ppm as Co) ofCobalt Acetate
powder, 12 g (120 ppm) of pentaerythritol, and 6g (60 ppm) of sodium acetatewere added to the
esterification reactor to obtain a reaction mass. The reaction mass heated to 240-250° C to obtain
a reaction mass containing ethylene terephthalate. 18 gm (50 ppm as P) of orthophosphoric acid
added to the reaction mass containing ethylene terephthalate and transferred via a 10 micron
filter to the poly-condensation reactor. The poly-condensation reaction was conducted at 270 to
285 °C with a peaktemperature of 288 °C to obtain amorphous polyethylene terephthalate having
I.V. of 0.623 dl/g co-polymerized with polyisosorbideisophthalate. The amorphous polyethylene
terephthalate was extruded out as strands and cut under water and collected as amorphous chips.
These amorphous chips were dried and pre-crystallized before subjecting to solid state
polymerization (SSP) for increasing the I.V to 0.836 dl/g.
Table 1: Tabulation of raw materials employed and results obtained in Examples 2, 3 and 4
Raw materials Unit Example 2 Example 3 Example 4
PTA Kg 82 -- 40.9 17

DMT Kg -- 95.9 --
PCR flakes Kg -- -- 50
Isosorbide/IPA
polymer
Kg 4.65 4.65 4.65
EG Kg 36.0 35.4 17
Sb2O3 as Sb ppm 200 200 200
GeO2 as Ge ppm 30 30 30
Manganese acetate ppm -- 200 --
Cobalt acetate as CO ppm 60 60 60
H3PO4 as P ppm 50 50 50
Sodium Acetate ppm 60 60 60
Penta ppm 120 120 120
nBBSA Kg 0.250 -- --
Amorphous samples Analysis report
IV @ 25 ºC Dl/g 0.621 0.618 0.623
-COOH Meg/kg 25 18 22
Color L* % 55 56 54
Color b* - -2 -1.5 -1.2
DEG content % 1.45 1.0 1.58
Glass transition
Temp.(Tg2)
0
C 82.5 82.7 81.9
Melting Point (Tm1)
0
C
245 246 244
Tch2
0
C
168 165 170
SSP samples Analysis report
IV @ 25 ºC Dl/g 0.838 0.84 0.836
-COOH Meg/kg 20 15 19
Color L* % 75 76 76 18

Color b* - -1.5 -2.0 -2.0
DEG content % 1.48 1.1 1.7
Glass transition
Temp.(Tg2)
0
C 82.7 82.8 82.0
Melting Point (Tm1)
0
C
245 246 244
Tch2
0
C
170 171 175
Impact strength J/M 54.5 55 57
Tensile Strength Kgf/cm2 560 555 565
Elongation % 200 168 165

Example 5A-5C: Preparation of modified polyethylene terephthalate by adding end capped
Low IV polyester
Modified co-polyester of examples 5A, 5B and 5C were prepared in the same manner as in
Example 2, 3 and 4, respectively by using the raw materials mentioned in the below table 2
which differs only in the use of PBN/PTN end capped oligomers which were added at the end of
esterification reaction.
Table 2: Raw materials used and the results obtained for examples 5A, 5B and 5C
Raw materials Unit Example 5A Example 5B Example 5C
PTA Kg 86.5 -- 33
DMT Kg -- 89 --
PCR flakes Kg -- -- 50
EG Kg 37.5 36 14.5
Isosorbide/IPA
polymer Kg
2.8
2.8 2.8 19

Sb2O3 as Sb Ppm 120 120 120
GeO2 as Ge Ppm 20 20 20
Manganese Acetate Ppm -- 200 ppm --
Cobalt acetate as CO Ppm 60 60 60
H3PO4 as P Ppm 50 50 50
Sodium Acetate Ppm 100 100 100
Pentaerythritol Ppm 200 200 200
n-BBSA Kg 0.25 0.25 0.25
Ba2SO4 Ppm 100 100 100
Sodium benzoate Ppm 100 100 100
PET end capped
polymer
Kg -- 5.0 10
Amorphous samples Analysis report
IV @ 25 ºC Dl/g 0.611 0.618 0.620
-COOH Meg/kg
28 23
20
Color L* % 56 55 54
Color b* - -2.5 -2.5 -1.8
DEG content % 1.35 1.0 1.4
Glass transition
Temp.(Tg2)
0
C
81.5 81.8
81.2
Melting Point (Tm1)
0
C
252 253 251
Tch2
0
C
138 135 133
SSP samples Analysis report 20

IV @ 25 °C
Dl/g
0.74 0.73
0.74
-COOH Meg/kg 22 18 16
Color L* % 76 75 75
Color b* - -2.0 -1.5 -2.0
DEG content % 1.42 1.0 1.8
Glass transition
Temp.(Tg2)
0
C
82.0 81.8
81.5
Melting Point (Tm1)
0
C
251 252 251
Tch2
0
C
143 142 140
Impact Strength J/M 56 55 55
Tensile Strength kgf/Cm2 580 570 572
Elongation % 80 100 70

Example 6A-6C: Preparation of polyethylene terephthalate
Modified co-polyester of Examples 6A, 6B and 6C were prepared in the same manner as in
Examples 2, 3 and 4 with the exception that the kind of raw material is changed as shown in
below table 3.
Table 3: Raw materials used and the results obtained for examples 6A, 6B and 6C
Raw materials Unit Example 6A Example 6B Example 6C
PTA Kg 81.6 -- 38.5
DMT Kg -- 95.3 --
PCR flakes Kg 50
EG Kg 35.36 35 17
Isosorbide/IPA
polymer Kg
5.6
5.6 5.6
Sb2O3 as Sb ppm
200 200
200
GeO2 as Ge ppm 40 40 40
Manganese Acetate ppm -- 200 --
Cobalt acetate as
CO ppm
60 60
60
H3PO4 as P ppm 50 50 50 21

Sodium Acetate ppm 60 60 60
Penta ppm 300 300 300
n-BBSA kg -- 0.250 0.250
Amorphous samples Analysis report
IV @ 25 ºC Dl/g 0.610 0.615 0.613
-COOH Meg/kg 25 28 26
Color L* % 54 55 54
Color b* - -1.0 -1.8 -1.5
DEG content % 1.4 0.8 1.1
Glass transition
Temp.(Tg2)
0
C
84.0 84.5
83.9
Melting Point
(Tm1)
0
C 248 248
247
Tch2
0
C
160 162 165
SSP samples Analysis repor7
IV @ 25 ºC Dl/g 0.84 0.835 0.84
-COOH Meg/kg 18 21 20
Color L* % 74 75 73
Color b* - -2.5 -2.1 -1.7
DEG content % 1.41 0.92 1.15
Glass transition
Temp.(Tg2)
0
C
84.1 84.4
83.9
Melting Point
(Tm1)
0
C 247 247
247
Tch2
0
C
165 168 165
Impact Strength J/M 55.5 56.8 56
Tensile Strength kgf/Cm2 585 580 590
Elongation % 220 190 180

Example 7: Manufacture of Preforms / Bottles by 2 Stage ISBM
Using co-polyester chips from examples 5 and 6 preforms were manufactured 38 g*130 mm long
on 4 caring injection molding machine of 130 tonnage. Prior to that the resin was dried at 170°C
for 5 hours. The molding temperature was 280-285°C. The performs were conditioned for 24
hours before starting blowing into bottles on blowing machine with single caring.
The performs were heated to 112°C.
The blowing cycles time was 4.13 sec.
Preblow pressure was 8 bar. 22

Blow pressure was 30 bar.
The bottles thus produced could be filled at 82±2°C without any deformation.
Example 8: Manufacture of thin walled containers by IM
The resin from example 5 was used on IM machine to manufacture containers. Prior to that the
chips were dried at 160°C for 7 hours. The mold was cooled with chilled water of 6°C. The melt
flow was satisfactory. The containers of 350µ wall thickness were manufactured. The containers
were of good color & transparency and could be filled at 82°C temperature.
Example 9: Manufacture of 20 liter container by 2 Stage ISBM
The co-polyester from example 2 was used to manufacture 20 liter water container. The chips
were dried at 170°C temperature for 6 hours. On a single caring injection molding machine the
perform were made. The extruder temperatures were in the range 275-285°C.
The preforms were subsequently blow at 30 bar pressure after heating at 120°C on single caring
blowing machines. The 20 liter containers manufactured could be washed at 72 °C.
The embodiments herein and the various features and advantageous details thereof are explained
with reference to the non-limiting embodiments in the description. Descriptions of well-known
components and processing techniques are omitted so as to not unnecessarily obscure the
embodiments herein. The examples used herein are intended merely to facilitate an
understanding of ways in which the embodiments herein may be practiced and to further enable
those of skill in the art to practice the embodiments herein. Accordingly, the examples should not
be construed as limiting the scope of the embodiments herein.
The foregoing description of the specific embodiments will so fully reveal the general nature of
the embodiments herein that others can, by applying current knowledge, readily modify and/or
adapt for various applications such specific embodiments without departing from the generic
concept, and, therefore, such adaptations and modifications should and are intended to be
comprehended within the meaning and range of equivalents of the disclosed embodiments. It is
to be understood that the phraseology or terminology employed herein is for the purpose of
description and not of limitation. Therefore, while the embodiments herein have been described 23

in terms of preferred embodiments, those skilled in the art will recognize that the embodiments
herein can be practiced with modification within the spirit and scope of the embodiments as
described herein.
The use of the expression “at least” or “at least one” suggests the use of one or more elements or
ingredients or quantities, as the use may be in the embodiment of the disclosure to achieve one or
more of the desired objects or results.
Any discussion of documents, acts, materials, devices, articles and the like that has been included
in this specification is solely for the purpose of providing a context for the disclosure. It is not to
be taken as an admission that any or all of these matters form a part of the prior art base or were
common general knowledge in the field relevant to the disclosure as it existed anywhere before
the priority date of this application.
While considerable emphasis has been placed herein on the particular features of this disclosure,
it will be appreciated that various modifications can be made, and that many changes can be
made in the preferred embodiments without departing from the principles of the disclosure.
These and other modifications in the nature of the disclosure or the preferred embodiments will
be apparent to those skilled in the art from the disclosure herein, whereby it is to be distinctly
understood that the foregoing descriptive matter is to be interpreted merely as illustrative of the
disclosure and not as a limitation.
24

We Claim:
1. A process for preparing a polyester having at least one of the following properties, intrinsic
viscosity greater than 0.7 dl/g at 25
o
C; color L* ranges from 72 to 76 %; color b* ranges
from -1.5 to -2.5; diethylene content of less than 1.5 %; glass transition temperature in the
range of 81 to 85
o
C; impact strength of 54 to 57 J/M; and tensile strength from 500 to 600
Kgf/cm2
, said process comprising the following steps:

a. dissolving isosorbide and at least one anti-oxidizing agent in water and
optionally, at least one diol to obtain an aqueous solution;

b. reacting said aqueous solution of isosorbide with at least one aromatic
dicarboxylic acid or ester thereof to obtain oligomerized product via
esterification or ester interchange;

c. polymerizing said isosorbide oligomer using at least one polymerization
catalyst to obtain an isosorbide polymer; and

d. co-polymerizing said isosorbide polymer with the polyester by adding said
oligomerized product or said isosorbide polymer in at least one stage selected
from the group consisting of before, during and after the polymerization
reaction of at least one alkylene aryl dicarboxylate monomer, to obtain the
polyester.

2. The process as claimed in claim 1, wherein the method step of dissolving is carried out at a
temperature ranging from 30 to 90
o
C; said anti-oxidizing agent is selected from the group
consisting of irganox 1010, irganox 1076, irgafos 168; said diol is at least one compound
selected from the group consisting of mono ethylene glycol, 1,3-propanediol, 1,4-butanediol,
1,6-hexanediol, 1,8-octanediol, 1,10-decanediol, 1,12-dodecanediol, 1,14-tetradecanediol,
1,16-hexadecanediol, dimer diol, 1,4-cyclohexanedimethanol, di(ethylene glycol),
tri(ethylene glycol), poly(ethylene ether) glycols, poly(butylene ether) glycols, (cis, trans)
1,3-cyclohexanedimethanol, (cis, trans) 1,4 cyclohexanedimethanol, 2-methyl-1,3-25

propanediol, 2,2-dimethyl-1,3-propanediol, 2-butyl-2-ethyl-1,3-propanediol,
trimethylpentanediol; and the concentration of isosorbide in the aqueous solution ranges from
60 to 95 wt %.

3. The process as claimed in claim 1, wherein the method step of reacting is carried out at a
temperature ranging from 200 to 260
o
C in the presence of catalyst selected from the group
consisting of acetate or alkanoate salts of Co(II) and Sb(III), oxides of Sb(III),Ge(IV),
Ti(OR)4 (where R is an alkyl group having 2 to 12 carbon atoms), n-butylstannoic
acid,antimony trioxide, germanium dioxide, tetraisopropyltitanate; said aromatic dicarboxylic
acid is at least one compound selected from the group consisting of terephthalic
acid,isophthalic acid, 2, 6 naphthalene dicarboxylic acid; said ester thereof in step (b) is at
least one compound selected from the group consisting of dimethyl terephthalate, dimethyl
isophthalate and dimethyl-2, 6-naphthalene dicarboxylate; and said esterified or trans-
esterified product is at least one compound selected from the group consisting of D-Glucitol,
1,4:3,6-dianhydro-, 2,2'-(1,4-benzenedicarboxylate), 2,2'-(1,3-benzenedicarboxylate) and
diisosorbide-2, 6-naphthalene dicarboxylate.

4. The process as claimed in claim 1, wherein the method step (c) is carried out at a temperature
ranging from 220 to 300
o
C; andsaid polymerization catalyst is at least one compound
selected from the group consisting of antimony trioxide, germanium dioxide, cobalt acetate.

5. The process as claimed in claim 1, wherein said isosorbide polymer exhibits an intrinsic
viscosity of 0.50 to 0.69 dl/g at 25
o
C.

6. The process as claimed in claim 1, wherein the alkylene aryl dicarboxylate monomer is at
least one selected from the group consisting of ethylene terephthalate, ethylene isophthalate,
ethylene-2,6-naphthalate, ethylene-3,4'-diphenyl ether dicarboxylate, ethylene
hexahydrophthalate,ethylene-2,7-naphthalate, ethylene phthalate and ethylene-4,4'-
methylenebis(benzoate); said alkylene aryl dicarboxylate monomer is obtained by
esterification reaction of at least one aromatic dicarboxylic acid selected from the group
consisting of terephthalic acid, isophthalic acid, 2,6-napthalene dicarboxylic acid, 3,4'-26

diphenyl ether dicarboxylic acid, hexahydrophthalic acid, 2,7-naphthalenedicarboxylic acid,
phthalic acid and 4,4'-methylenebis(benzoic acid) with ethylene glycol or trans-esterification
reaction of at least one ester selected from the group consisting of dimethyl terephthalate,
dimethyl isophthalate, dimethyl-2,6-naphthalate, dimethyl-3,4'-diphenyl ether dicarboxylate,
dimethyl hexahydrophthalate, dimethyl-2,7-naphthalate, dimethyl phthalate and dimethyl-
4,4'-methylenebis(benzoate)with a diol selected from the group consisting of ethylene glycol,
propanediol, butanediol, cyclohexanedimethanol, hexane diol and combinations
thereof,followed by addition of at least one stabilizing agentselected from the group
consisting of ortho-phosphoric acid,trimethylphosphate (TMP), triphynylphosphate (TPP),
Triethyl phosphono acetate (TEPA), , and optionally, at least one end capped oligomer
selected from the group consisting of polyethylene terephthalate, polybutylene terephthalate,
polytrimethylene terephthalate, polytreimethylenenaphthalate and polybutylenenaphthalate.

7. The process as claimed in claim 1, comprising a step of adding said oligomerized product or
isosorbide polymer in at least one stage selected from the group consisting of before, during
and after esterification or ester interchange reaction.

8. The process as claimed in claim 1, wherein the polymerization reaction of alkylene aryl
dicarboxylate monomer is carried out using at least one agent selected from the group
consisting of branching agent, nucleating agent, liquid plasticizer and additive.

9. The process as claimed in claim 8, wherein the branching agent is at least one compound
selected from the group consisting of pentaerythritol,trimellitic acid, trimellitic anhydride,
pyromellitic acid, pyromellitic anhydride and sorbitol.

10. The process as claimed in claim 8, wherein the nucleating is at least one compound selected
from the group consisting of calcium silicate, nano silica powder, talc, microtalc, aclyn,
kaolinite, montmorillonite, synthetic mica, calcium sulfide, boron nitride, barium sulfate,
aluminum oxide, neodymium oxide, a metal salt of phenyl phosphonate, sodium benzoate,
potassium benzoate, lithium benzoate, calcium benzoate, magnesium benzoate, barium
benzoate, lithium terephthalate, sodium terephthalate, potassium terephthalate, calcium 27

oxalate, sodium laurate, potassium laurate, sodium myristate, potassium myristate, calcium
myristate, sodium octacosanoate, calcium octacosanoate, sodium stearate, potassium stearate,
lithium stearate, calcium stearate, magnesium stearate, barium stearate, sodium montanate,
calcium montanate, sodium toluoylate, sodium salicylate, potassium salicylate, zinc
salicylate, aluminum dibenzoate, potassium dibenzoate, lithium dibenzoate, sodium β-
naphthalate, sodium cyclohexane carboxylate, organic sulfonates, carboxylic acid amides,
phosphoric compound metal salts ofbenzylidene sorbitol and derivatives thereof, sodium-
2,2'-methylenebis(4,6-di-t-butylphenyl)phosphate and 2,2-methylbis(4,6-di-t-
butylphenyl)sodium.

11. The process as claimed in claim 8, wherein the liquid plasticizer is at least one compound
selected from the group consisting of N-isopropyl benzene sulfonamide, N-tert-butyl benzene
sulfonamide, N-pentyl benzene sulfonamide, N-hexyl benzene sulfonamide, N-n-octyl
benzene sulfonamide, N-methyl-N-butyl benzene sulfonamide, N-methyl-N-ethyl benzene
sulfonamide, N-methyl-N-propyl benzene sulfonamide, N-ethyl-N-propyl benzene
sulfonamide, N-ethyl p-ethylbenzene sulfonamide, N-ethyl p-(t-butyl)benzene sulfonamide,
N-butyl p-butyl benzenesulfonamide, N-butyl toluene sulfonamide, N-t-octyl toluene
sulfonamide, N-ethyl-N-2-ethylhexyl toluene sulfonamide, N-ethyl-N-t-octyl toluene
sulfonamide and tri-octyltrimellitate.

12. The process as claimed in claim 8, wherein the additive is at least one selected from the
group consisting of pigments, flame retardant additives, reinforcing agents, thermal
stabilizers, ultraviolet light stabilizers, processing aids, impact modifiers, flow enhancing
additives, ionomers, liquid crystal polymers, fluoropolymers, olefins including cyclic olefins,
polyamides and ethylene vinyl acetate copolymers.

13. The process as claimed in claim 1, wherein the polymerization reaction of at least one
alkylene aryl dicarboxylate comprises polycondensation reaction and solid state
polymerization reaction; and the polyester is further processed by extruding the polyester and
cutting underwater to obtain chips of polyester, drying the chips of polyester to obtain dried
chips; and blow molding at 270 to 290
o
C and cooling the mold to obtain a pre-form, a 28

material or a container, wherein said pre-form, said material or said container is fillable at a
temperature ranging from 70 to 90ºC, preferably 70 to 85ºC.

14. A polyester product obtained by the process as claimed in claim 1; said polyester product
comprising:
a. at least one polyester obtained from at least one aromatic dicarboxylic acid or ester
thereof and ethylene glycol;

b. polymer of isosorbide and at least one aromatic dicarboxylic acid or ester thereof in
an amount of 1 to 20 wt%; and

c. at least one agent selected from the group consisting of liquid plasticizer in an amount
of 0.5 to 2 wt%; at least one nucleating agent in an amount of 10 ppm to 2000 ppm; at
least one branching agent in an amount of 10 ppm to2000 ppm; at least one anti-
oxidizing agent in an amount ranging from 0.1 to 5 wt%; at least one stabilizing
agent; at least one additive and optionally, at least one end capped oligomer in an
amount of 1 to 20 wt%,
wherein, said polyester product is characterized by at least one of the following
properties:
• intrinsic viscosity greater than 0.7 dl/g at 25
o
C;
• color L* ranges from 72 to 76 %;
• color b* ranges from -1.5 to -2.5;
• diethylene content of less than 1.5 %;
• glass transition temperature in the range of 81 to 85
o
C;
• impact strength of 54 to 57 J/M; and
• tensile strength from 500 to 600 Kgf/cm2
.

15. A polyester product in a packaging material, a packaging container or a pre-form; said
polyester product characterized by at least one of the following properties, intrinsic viscosity
greater than 0.7 dl/g at 25
o
C; color L* ranges from 72 to 76 %; color b* ranges from -1.5 to -
2.5; diethylene content of less than 1.5 %; glass transition temperature in the range of 81 to 29

85
o
C; impact strength of 54 to 57 J/M; and tensile strength from 500 to 600 Kgf/cm2
,
wherein, said packaging material, said packaging container or said pre-form exhibits a hot-
fill capacity of 70 to 90
o
C, preferably 70 to 85
o
C.

16. The polyester as claimed in claim 14, used for making the transparent and opaque flexible
and rigid packaging containers, films, sheets, textile fabric and yarns.

17. The polyester as claimed in claim 14, used for making hot fill and cold fill containers by
using at least one moulding process selected from the group consisting of heat set blow
moulding process and cold set blow moulding process.