U.S. patent application number 11/708244 was filed with the patent office on 2007-11-01 for process for the preparation of polyesters containing 1,4-cyclohexanedimethanol.
Invention is credited to Benjamin Fredrick Barton, Joseph Franklin Knight, Daniel Lee Martin, Damon Bryan Shackelford.
Application Number | 20070255020 11/708244 |
Document ID | / |
Family ID | 37991420 |
Filed Date | 2007-11-01 |
United States Patent
Application |
20070255020 |
Kind Code |
A1 |
Martin; Daniel Lee ; et
al. |
November 1, 2007 |
Process for the preparation of polyesters containing
1,4-cyclohexanedimethanol
Abstract
Disclosed is a process for the preparation of high molecular
weight polyesters by reacting one or more dicarboxylic acids
directly with 1,4-cyclohexanedimethanol and, optionally, one or
more diols. The process uses an overall diol to dicarboxylic acid
molar ratio of about 0.97 to about 1.2 and an incremental addition
of either the diacid or diol components. The process provides a
shorter total reaction time and, thus, lessens the thermal
degradation of polyester which may result in high color and reduced
molecular weight.
Inventors: |
Martin; Daniel Lee;
(Kingsport, TN) ; Knight; Joseph Franklin;
(Kingsport, TN) ; Barton; Benjamin Fredrick;
(Kingsport, TN) ; Shackelford; Damon Bryan;
(Kingsport, TN) |
Correspondence
Address: |
Louis N. Moreno;Eastman Chemical Company
P.O. Box 511
Kingsport
TN
37662-5075
US
|
Family ID: |
37991420 |
Appl. No.: |
11/708244 |
Filed: |
February 20, 2007 |
Related U.S. Patent Documents
|
|
|
|
|
|
Application
Number |
Filing Date |
Patent Number |
|
|
11414466 |
Apr 28, 2006 |
7211634 |
|
|
11708244 |
|
|
|
|
Current U.S.
Class: |
526/65 ; 528/272;
528/302 |
Current CPC
Class: |
C08G 63/199 20130101;
C08G 63/78 20130101 |
Class at
Publication: |
526/65 ; 528/272;
528/302 |
International
Class: |
C08G 63/16 20060101
C08G063/16; C08G 63/02 20060101 C08G063/02; C08G 85/00 20060101
C08G085/00 |
Claims
1. A process for the preparation of a polyester consisting
essentially of heating a mixture of a diol component comprising
about 10 to about 100 mole percent 1,4-cyclohexanedimethanol, based
on the total moles of diol component, and a diacid component
comprising about 5 to about 40 mole percent isophthalic acid, based
on the total moles of diacid component, the mixture having total
diol:diacid component molar ratio of about 1.0 to about 1.15, at a
temperature of about 220 to about 300.degree. C. to produce a
substantially linear, thermoplastic polyester having an inherent
viscosity of at least 0.60 dL/g.
2. The process according to claim 1 wherein the temperature is
about 220 to about 240.degree. C.
3. The process according to claim 1 wherein the diacid component
further comprises about 0 to 20 mole percent of one or more
dicarboxylic acids selected from the group consisting of fumaric,
succinic, adipic, glutaric, azelaic, sebacic, resorcinol diacetic,
diglycolic, 4,4'-oxybis(benzoic), biphenyldicarboxylic,
4,4'-methylenedibenzoic, trans-4,4'-stilbenedicarboxylic, and
sulfoisophthalic acids.
4. The process according to claim 3 wherein the diol component
comprises about 10 to about 99 mole percent of
1,4-cyclohexanedimethanol, 0 to about 90 mole percent of ethylene
glycol, and about 1 to about 25 mole percent of diethylene
glycol.
5. The process according to claim 3 wherein the diol component
comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
ethylene glycol.
6. The process according to claim 1 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.10.
7. The process according to claim 6 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.05.
8. The process according to claim 1 wherein the diacid component is
added in at least 2 stages to a reaction zone.
9. The process according to claim 1 wherein the diacid component is
added continuously to a reaction zone.
10. The process according to claim 3 wherein the diacid component
is added as a mixture in water, an alcohol, or one or more
diols.
11. The process according to claim 3 wherein a reaction zone
comprises at least 2 reactors.
12. The process according to claim 9 wherein the inherent viscosity
of the thermoplastic polyester is at least 0.65 dL/g.
13. The process according to claim 9 wherein the inherent viscosity
of the thermoplastic polyester is at least 0.7 dL/g.
14. A process for the preparation of a polyester, comprising:
adding a diol component and a diacid component to a reaction zone
at a total diol:diacid component molar ratio of about 0.97 to about
1.15 to produce a substantially linear, thermoplastic polyester
having an inherent viscosity of at least 0.5 dL/g, wherein the diol
component is added incrementally to the reaction zone at a
temperature of about 210 to about 250.degree. C. and the molar
ratio of diol:diacid components added to the reaction zone is less
than the total molar ratio until the addition of the diol component
is completed.
15. The process according to claim 14 wherein the temperature is
about 210 to about 240.degree. C.
16. The process according to claim 15 wherein the temperature is
about 220 to about 240.degree. C.
17. The process according to claim 14 wherein the diacid component
comprises at least 80 mole percent, based on the total moles of
diacid component, of one or more dicarboxylic acids selected from
the group consisting of terephthalic acid, naphthalenedicarboxylic
acid, 1,4-cyclohexanedicarboxylic acid, and isophthalic acid; and
the diol component comprises about 10 to 100 mole percent, based on
the total moles of the diol component, 1,4-cyclohexanedimethanol
and 0 to about 90 mole percent of one or more diols selected from
the group consisting of neopentyl glycol, diethylene glycol,
ethylene glycol, 1,2-propanediol, 1,3-propanediol, 1,4-butanediol,
1,5-pentanediol, 1,6-hexanediol, 1,8-octanediol,
2,2,4-trimethyl-1,3-pentanediol, 1,3-cyclohexanedimethanol,
bisphenol A, and polyalkylene glycol.
18. The process according to claim 17 wherein the diacid component
further comprises about 0 to 20 mole percent of one or more
dicarboxylic acids selected from the group consisting of fumaric,
succinic, adipic, glutaric, azelaic, sebacic, resorcinol diacetic,
diglycolic, 4,4'-oxybis(benzoic), biphenyldicarboxylic,
4,4'-methylenedibenzoic, trans-4,4'-stilbenedicarboxylic, and
sulfoisophthalic acids.
19. The process according to claim 18 wherein the diacid component
comprises from about 60 to 100 mole percent terephthalic acid and 0
to about 40 mole percent isophthalic acid and the diol residue
comprises about 100 mole percent 1,4-cyclohexanedimethanol.
20. The process according to claim 19 wherein the diacid component
comprises about 95 mole percent terephthalic acid and about 5 mole
percent isophthalic acid.
21. The process according to claim 19 wherein the diacid component
comprises 100 mole percent terephthalic acid.
22. The process according to claim 18 wherein the diacid component
comprises 80 to 100 mole percent terephthalic acid and the diol
component comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
1,3-cyclohexanedimethanol.
23. The process according to claim 18 wherein the diacid component
comprises 100 mole percent terephthalic acid and the diol component
comprises about 10 to about 40 mole percent
1,4-cyclohexanedimethanol and 60 to about 90 mole percent ethylene
glycol.
24. The process according to claim 18 wherein the diol component
comprises about 10 to about 99 mole percent of
1,4-cyclohexanedimethanol, 0 to about 90 mole percent of ethylene
glycol, and about 1 to about 25 mole percent of diethylene
glycol.
25. The process according to claim 18 wherein the diol component
comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
ethylene glycol.
26. The process according to claim 18 wherein the diacid component
comprises about 90 to 100 mole percent 1,4-cyclohexanedicarboxylic
acid and the diol component comprises 90 to 100 mole percent
1,4-cyclohexanedimethanol.
27. The process according to claim 14 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.10.
28. The process according to claim 27 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.05.
29. The process according to claim 14 wherein the diacid component
is added in at least 2 stages to the reaction zone.
30. The process according to claim 14 wherein the diacid component
is added continuously to the reaction zone.
31. The process according to claim 30 wherein the diacid component
is added as a mixture in water, an alcohol, or one or more
diols.
32. The process according to claim 30 wherein the reaction zone
comprises at least 2 reactors.
33. The process according to claim 30 wherein the inherent
viscosity of the polyester is at least 0.65 dL/g.
34. The process according to claim 30 wherein the inherent
viscosity of the polyester is at least 0.7 dL/g.
35. A process for the preparation of a polyester, comprising: (i)
contacting a portion of a diacid component with a diol component
comprising a diol having a boiling point of at least 230.degree. C.
at 101 kPa, under esterification conditions and at a diol:diacid
component molar ratio greater than 1.2, while recovering a
distillate comprising substantially water, to form an oligomer,
(ii) adding at least one additional portion of the diacid component
to the oligomer to give a total diol:diacid component molar ratio
of 1.2 or less; and (iii) heating the oligomer under polymerization
conditions for a period of 4 hours or less to produce a linear,
thermoplastic polyester having an inherent viscosity of at least
0.65 dL/g.
36. The process according to claim 35 wherein the diacid component
comprises at least 80 mole percent, based on the total moles of
diacid component, of one or more dicarboxylic acids selected from
the group consisting of terephthalic acid, naphthalenedicarboxylic
acid, 1,4-cyclohexanedicarboxylic acid, and isophthalic acid; and
the diol component comprises about 10 to 100 mole percent, based on
the total moles of the diol component, 1,4-cyclohexanedimethanol
and 0 to about 90 mole percent of one or more diols selected from
the group consisting of neopentyl glycol, diethylene glycol,
ethylene glycol, 1,2-propanediol, 1,3-propanediol, 1,4-butanediol,
1,5-pentanediol, 1,6-hexanediol, 1,8-octanediol,
2,2,4-trimethyl-1,3-pentanediol, 1,3-cyclohexanedimethanol,
bisphenol A, and polyalkylene glycol.
37. The process according to claim 36 wherein the diacid component
further comprises about 0 to 20 mole percent of one or more
dicarboxylic acids selected from the group consisting of fumaric,
succinic, adipic, glutaric, azelaic, sebacic, resorcinol diacetic,
diglycolic, 4,4'-oxybis(benzoic), biphenyldicarboxylic,
4,4'-methylenedibenzoic, trans-4,4'-stilbenedicarboxylic, and
sulfoisophthalic acids.
38. The process according to claim 37 wherein the diacid component
comprises from about 60 to 100 mole percent terephthalic acid and 0
to about 40 mole percent isophthalic acid and the diol residue
comprises about 100 mole percent 1,4-cyclohexane-dimethanol.
39. The process according to claim 38 wherein the diacid component
comprises about 95 mole percent terephthalic acid and about 5 mole
percent isophthalic acid.
40. The process according to claim 38 wherein the diacid component
comprises 100 mole percent terephthalic acid.
41. The process according to claim 37 wherein the diacid component
comprises 80 to 100 mole percent terephthalic acid and the diol
component comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
1,3-cyclohexanedimethanol.
42. The process according to claim 37 wherein the diacid component
comprises 100 mole percent terephthalic acid and the diol component
comprises about 10 to about 40 mole percent
1,4-cyclohexanedimethanol and 60 to about 90 mole percent ethylene
glycol.
43. The process according to claim 37 wherein the diol component
comprises about 10 to about 99 mole percent of
1,4-cyclohexanedimethanol, 0 to about 90 mole percent of ethylene
glycol, and about 1 to about 25 mole percent of diethylene
glycol.
44. The process according to claim 37 wherein the diol component
comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
ethylene glycol.
45. The process according to claim 37 wherein the diacid component
comprises about 90 to 100 mole percent 1,4-cyclohexanedicarboxylic
acid and the diol component comprises 90 to 100 mole percent
1,4-cyclohexanedimethanol.
46. The process according to claim 35 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.10.
47. The process according to claim 46 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.05.
48. The process according to claim 35 wherein the diacid component
is added in at least 2 stages to the reaction zone.
49. The process according to claim 35 wherein the diacid component
is added continuously to the reaction zone.
50. The process according to claim 37 wherein the diacid component
is added as a mixture in water, an alcohol, or one or more
diols.
51. The process according to claim 37 wherein the reaction zone
comprises at least 2 reactors.
52. The process according to claim 49 wherein the inherent
viscosity of the thermoplastic polyester is at least 0.7 dL/g.
53. A process for the preparation of a polyester, comprising: (i)
contacting a portion of a diacid component comprising about 60 to
100 mole percent, based on the total moles of diacid component, of
terephthalic acid with a diol component comprising about 10 to 100
mole percent, based on the total moles of diol component, of
1,4-cyclohexanedimethanol, under esterification conditions and at a
diol:diacid component molar ratio greater than 1.2, while
recovering a distillate comprising substantially water, to form an
oligomer having a inherent viscosity of less than 0.4 dL/g, (ii)
adding at least one additional portion of the diacid component to
the oligomer to give a total diol:diacid component molar ratio of
1.2 or less; and (iii) heating the oligomer under polymerization
conditions for a period of 4 hours or less to produce a linear,
thermoplastic polyester having an inherent viscosity of at least
0.7 dL/g.
54. The process according to claim 53 further comprising heating
the diol and diacid components at a temperature of about 210 to
about 250.degree. C. at an absolute pressure of about 48 kPa to
about 552 kPa after the addition of the diacid component is
completed.
55. The process according to claim 54 wherein the temperature is
about 210 to about 240.degree. C.
56. The process according to claim 55 wherein the temperature is
about 220 to about 240.degree. C.
57. The process according to claim 54 wherein the diacid component
further comprises about 0 to 20 mole percent of one or more
dicarboxylic acids selected from the group consisting of fumaric,
succinic, adipic, glutaric, azelaic, sebacic, resorcinol diacetic,
diglycolic, 4,4'-oxybis(benzoic), biphenyldicarboxylic,
4,4'-methylenedibenzoic, trans-4,4'-stilbenedicarboxylic, and
sulfoisophthalic acids.
58. The process according to claim 57 wherein the diacid component
comprises from about 60 to 100 mole percent terephthalic acid and 0
to about 40 mole percent isophthalic acid and the diol residue
comprises about 100 mole percent 1,4-cyclohexane-dimethanol.
59. The process according to claim 58 wherein the diacid component
comprises about 95 mole percent terephthalic acid and about 5 mole
percent isophthalic acid.
60. The process according to claim 59 wherein the diacid component
comprises 100 mole percent terephthalic acid.
61. The process according to claim 57 wherein the diacid component
comprises 80 to 100 mole percent terephthalic acid and the diol
component comprises about 50 to about 90 mole percent
1,4-cyclo-hexanedimethanol and about 10 to about 50 mole percent
1,3-cyclohexanedimethanol.
62. The process according to claim 57 wherein the diacid component
comprises 100 mole percent terephthalic acid and the diol component
comprises about 10 to about 40 mole percent
1,4-cyclohexanedimethanol and 60 to about 90 mole percent ethylene
glycol.
63. The process according to claim 57 wherein the diol component
comprises about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
ethylene glycol.
64. The process according to claim 53 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.10.
65. The process according to claim 64 wherein the total diol:diacid
component molar ratio is about 1.0 to about 1.05.
66. The process according to claim 53 wherein the diacid component
is added in at least 2 stages to the reaction zone.
67. The process according to claim 53 wherein the diacid component
is added continuously to the reaction zone.
68. The process according to claim 57 wherein the diacid component
is added as a mixture in water, an alcohol, or one or more
diols.
69. The process according to claim 57 wherein the reaction zone
comprises at least 2 reactors.
Description
CROSS-REFERENCE
[0001] This application is a divisional application of prior
application Ser. No. 11/414/466, filed Apr. 28, 2006.
FIELD OF THE INVENTION
[0002] This invention pertains to a process for the preparation of
thermoplastic polyesters. More particularly, this invention
pertains to a polyester process in which one or more dicarboxylic
acids is reacted directly with a diol component comprising
1,4-cyclohexanedimethanol and, optionally, one or more diols, in a
low overall diol:dicarboxylic acid ratio.
BACKGROUND OF THE INVENTION
[0003] Polyesters containing 1,4-cyclohexanedimethanol (abbreviated
hereinafter as "CHDM") as a diol component are often produced using
a dialkyl esters such as, for example, dimethylterephthalate (DMT),
dimethylisophthalate, and 1,4-dimethylcyclohexane dicarboxylate, as
the source of the diacid component. In a typical process, for
example, a dialkyl ester is reacted with one or more diols in a
transesterification reaction to produce an oligomer. The alkyl
alcohol by-product is removed from the reaction medium, usually by
distillation, to help to push the reaction equilibrium toward
oligomer formation. The transesterification step is conducted at
high temperatures, typically from about 200.degree. C. to about
270.degree. C., and at pressures between about 101 to 515 kPa (0 to
60 psig). The transesterification step is followed by a
polymerization step where excess diol is removed and the oligomer
converted further in a polycondensation reaction to yield a high
molecular weight polyester. This method requires high diol:ester
mole ratios (typically in the range of 1.5 to 6.0) to obtain high
conversion of the alkyl ester groups in the transesterification
step. High diol:ester ratios, however, require removal of excess
diol in order to produce a polyester of sufficiently high molecular
weight for film, sheet, and molded plastic applications. Removal of
excess diol, however, is difficult when high-boiling diols are
used, that is diols having a boiling point greater than about
230.degree. C. such as, for example, CHDM. With high-boiling diols,
it is frequently necessary to conduct the polycondensation step at
high temperatures of about 270.degree. C. to 310.degree. C. and at
pressures of about 53 kPa to about 0.013 kPa for extended periods
of time in order to remove sufficient diol to produce a high
molecular weight polyester.
[0004] Although diester-based polyester processes have been
practiced commercially for many years, dicarboxylic acids are
preferred as starting materials because water is generated as a
by-product instead of an alcohol. Water is easy to remove and is
non-hazardous. In addition, reacting a dicarboxylic acid directly
with a diol eliminates the additional processing steps associated
with the esterification of diacids to the corresponding dialkyl
esters. Unfortunately, using dicarboxylic acids as a starting
material instead of a dialkyl esters in polyester process presents
a number of problems, especially when CHDM and other high boiling
diols are used as a diol component. For example, many dicarboxylic
acids have low solubility in diols which greatly reduces the rate
of the esterification reaction. In particular, TPA has an low
solubility in CHDM. To help overcome this low solubility, excess
diol is often added to the esterifcation step to help drive
conversion of the diol and the dicarboxylic acid to the oligomer.
Any excess diol, however, must be removed during the polymerization
step, often requiring extended process times at elevated
temperatures and low pressures (typically less than 0.7 kPa). In
addition, long reaction times during the polymerization step are
often required to build sufficient molecular weight. Lengthy
process times and elevated temperatures, however, frequently can
lead to the development of color and the thermal degradation of the
polyester. In polyester compositions that are substantially
amorphous, this degradation can lead to a loss of clarity or to the
formation of high color in the polyester product. For polyesters
that exhibit a sufficient degree of crystallinity, the
polycondensation reaction can be terminated at some intermediate
step and the polyester then subjected to solid-state polymerization
to increase molecular weight. Solid state polymerization, however,
is expensive and requires additional equipment. These problems have
created a need for a polyester process that avoids long reaction
times and thermal degradation problems when dicarboxylic acids are
used as starting materials in combination with CHDM.
SUMMARY OF THE INVENTION
[0005] We have discovered that polyesters based on
1,4-cyclohexanedimethanol, abbreviated herein as "CHDM", may be
produced efficiently by the reaction of one or more dicarboxlic
acids directly with CHDM and, optionally, one or more diols in low
diol:dicarboxylic acid molar ratios. Thus, the present invention
provides process for the preparation of a polyester, comprising:
adding a diol component comprising 1,4-cyclohexanedimethanol, and a
diacid component to a reaction zone at a total diol:diacid
component molar ratio of about 0.97 to about 1.2 to produce a
substantially linear, thermoplastic polyester having an inherent
viscosity of at least 0.5 dL/g, wherein the diacid component is
added incrementally to the reaction zone and the diol:diacid
component molar ratio in the reaction zone is greater than the
total ratio until the addition of the diacid component is
completed. Our novel process uses a low total diol:diacid molar
ratio of about 0.97 to about 1.2 and an incremental addition of the
dicarboxylic acid component to a reaction zone in which the molar
ratio of diol:diacid components added to the reaction zone is
greater than the total molar ratio mixture until the addition of
the carboxylic acid is completed. Further, it has been found
unexpectedly that maintaining the reaction zone during the
esterification phase of the process at a temperature of 250.degree.
C. or less, such as, for example, at a temperature of about 210 to
about 250.degree. C., produces an oligomer which exhibits higher
polymerization rates than an oligomer produced at higher
esterification temperatures. A higher polymerization rate provides
a shorter reaction time to obtain a polyester of high molecular
weight. The polyesters from the process of the invention have
excellent clarity and may be used in packaging applications,
textiles, sheeting, and film.
[0006] Although the process of the invention may be used to prepare
any polyester, it is particularly useful for polyesters containing
the residues of high boiling diols, such as CHDM, where removal of
excess diol is difficult because of the high temperatures required
to distill the diol from the reaction mixture. The term
"high-boiling diol", as used herein, means a diol that exhibits a
boiling point above 230.degree. C. at atmospheric pressure
(approximately 101 kPa). Thus, our process can be used
advantageously for the preparation of a variety of polyesters and
copolyesters containing 1,4-cyclohexanedimethanol. For example, the
diacid component may comprise at least 80 mole percent, based on
the total moles of diacid component, of one or more dicarboxylic
acids selected from the group consisting of terephthalic acid,
naphthalenedicarboxylic acid, 1,4-cyclohexane-dicarboxylic acid,
and isophthalic acid. The diol component may comprise about 10 to
100 mole percent, based on the total moles of the diol component,
1,4-cyclohexanedimethanol. In addition to CHDM, the diol component
may comprise from 0 to about 90 mole percent of one or more diols
selected from neopentyl glycol, diethylene glycol, ethylene glycol,
1,2-propanediol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol,
1,6-hexanediol, 1,8-octanediol, 2,2,4-trimethyl-1,3-pentanediol,
1,3-cyclohexanedimethanol, bisphenol A, and polyalkylene glycol.
The polyesters prepared by the process of the instant invention are
thermoplastic polyesters having an inherent viscosity (abbreviated
herein as "IV") of at least 0.5 dL/g. Other examples of IV's that
may be exhibited by the polyester are at least 0.6 dL/g, at least
0.65 dL/g, and at least 0.7 dL/g.
[0007] Alternatively, our process may be carried out by adding the
diol component incrementally to the reaction zone. Thus, another
embodiment of the present invention is a process for the
preparation of a polyester, comprising: adding at least one diol
and at least one dicarboxylic acid to a reaction zone under
polymerization conditions at a total diol:dicarboxylic acid molar
ratio of about 0.97 to about 1.2 to produce a substantially linear,
thermoplastic polyester having an inherent viscosity of at least
0.5 dL/g, wherein the diol is added incrementally to the reaction
zone at a reaction zone temperature of about 210 to about
250.degree. C. and the molar ratio of diol:dicarboxylic acid added
to the reaction zone is less than the total molar ratio until the
addition of the diol is completed. This embodiment of the invention
may be used, for example, when the physical properties of the
diacid or diol component are such that it is preferable for ease of
operation to add the diol incrementally to the reaction zone.
[0008] The process of our invention may be carried out as a batch,
semicontinuous, or continuous process and may employ 2 or more
reactors. Without being bound by theory, it is believed that during
the addition of the diacid component, the primary reaction
mechanism for increasing molecular weight in the polymerization
stage is esterification rather than polycondensation. The water
produced from the esterification reaction, from a mass transfer
consideration, is easier to remove than excess diol. In addition,
because the reaction kinetics for esterification are, in general,
faster than the reaction kinetics for transesterification of the
associated alkyl ester, the overall rate of the polymerization
process is increased.
DETAILED DESCRIPTION
[0009] The present invention provides a process for the preparation
of high molecular weight thermoplastic polyesters containing
1,4-cyclohexanedimethanol. In a general embodiment, our invention
provides a process for the preparation of a polyester, comprising:
adding a diol component comprising 1,4-cyclohexanedimethanol, and a
diacid component to a reaction zone at a total diol:diacid
component molar ratio of about 0.97 to about 1.2 to produce a
substantially linear, thermoplastic polyester having an inherent
viscosity of at least 0.5 dL/g, wherein the diacid component is
added incrementally to the reaction zone and the diol:diacid
component molar ratio in the reaction zone is greater than the
total molar ratio until the addition of the diacid component is
completed. Our process provides an increased rate of reaction in
comparison to traditional methods where higher diol ratios and
higher temperatures are used and is useful for polyesters
containing CHDM and other high-boiling diols where removal of
excess diol from the reaction milieu is difficult.
[0010] Unless indicated to the contrary, the numerical parameters
set forth in the following specification and attached claims are
approximations that may vary depending upon the desired properties
sought to be obtained by the present invention. At the very least,
each numerical parameter should be construed in light of the number
of reported significant digits and by applying ordinary rounding
techniques. Further, the ranges stated in this disclosure and the
claims are intended to include the entire range specifically and
not just the endpoint(s). For example, a range stated to be 0 to 10
is intended to disclose all whole numbers between 0 and 10 such as,
for example 1, 2, 3, 4, etc., all fractional numbers between 0 and
10, for example 1.5, 2.3, 4.57, 6.1113, etc., and the endpoints 0
and 10. Also, a range associated with chemical substituent groups
such as, for example, "C1 to C5 hydrocarbons", is intended to
specifically include and disclose C1 and C5 hydrocarbons as well as
C2, C3, and C4 hydrocarbons.
[0011] Notwithstanding that the numerical ranges and parameters
setting forth the broad scope of the invention are approximations,
the numerical values set forth in the specific examples are
reported as precisely as possible. Any numerical value, however,
inherently contains certain errors necessarily resulting from the
standard deviation found in its respective testing
measurements.
[0012] As used in the specification and the appended claims, the
singular forms "a," "an" and "the" include their plural referents
unless the context clearly dictates otherwise. For example,
reference a "polyester," or a "dicarboxylic acid," is intended to
include the processing or making of a plurality of polymers, or
dicarboxylic acids. For example, references to a composition
containing or including "an" ingredient or "a" polyester is
intended to include other ingredients or other polyesters,
respectively, in addition to the one named. By "comprising" or
"containing" or "including" we mean that at least the named
compound, element, particle, or method step, etc., is present in
the composition or article or method, but do not exclude the
presence of other compounds, catalysts, materials, particles,
method steps, etc, even if the other such compounds, material,
particles, method steps, etc., have the same function as what is
named, unless expressly excluded in the claims.
[0013] Also, it is to be understood that the mention of one or more
process steps does not preclude the presence of additional process
steps before or after the combined recited steps or intervening
process steps between those steps expressly identified. Moreover,
the lettering of process steps or ingredients is a convenient means
for identifying discrete activities or ingredients and the recited
lettering can be arranged in any sequence, unless otherwise
indicated.
[0014] The process of the present invention is for the preparation
of thermoplastic polyesters comprising dicarboxylic acid monomer
residues, diol monomer residues, and repeating units. Thus, the
term "monomer residue", as used herein, means a residue of a
dicarboxylic acid, a diol, or a hydroxycarboxylic acid. A
"repeating unit", as used herein, means an organic structure having
2 monomer residues bonded through a carbonyloxy group. The
polyesters of the present invention contain substantially equal
molar proportions of acid residues (100 mole %) and diol residues
(100 mole %) which react in substantially equal proportions such
that the total moles of repeating units is equal to 100 mole %. The
mole percentages provided in the present disclosure, therefore, may
be based on the total moles of acid residues, the total moles of
diol residues, or the total moles of repeating units. For example,
a polyester containing 30 mole % of a monomer, which may be a
dicarboxylic acid, a diol, or hydroxycarboxylic acid, based on the
total repeating units, means that the polyester contains 30 mole %
monomer out of a total of 100 mole % repeating units. Thus, there
are 30 moles of monomer residues among every 100 moles of repeating
units. Similarly, a polyester containing 30 mole % of a
dicarboxylic acid monomer, based on the total acid residues, means
the polyester contains 30 mole % dicarboxylic acid monomer out of a
total of 100 mole % acid residues. Thus, in this latter case, there
are 30 moles of dicarboxylic acid monomer residues among every 100
moles of acid residues.
[0015] The term "polyester", as used herein, encompasses both
"homo-polyesters" and "copolyesters" and means a synthetic polymer
prepared by the polycondensation of a diacid component, comprising
one or more difunctional carboxylic acids, with a diol component,
comprising one or more, difunctional hydroxyl compounds. Typically
the difunctional carboxylic acid is a dicarboxylic acid and the
difunctional hydroxyl compound is a dihydric alcohol such as, for
example glycols and diols. Alternatively, the difunctional
carboxylic acid may be a hydroxy carboxylic acid such as, for
example, p-hydroxybenzoic acid, and the difunctional hydroxyl
compound may be a aromatic nucleus bearing 2 hydroxy substituents
such as, for example, hydroquinone. The term "thermoplastic
polyester", as used herein, is intended to have its plain meaning
as would be understood by persons having ordinary skill in the art,
that is, a polyester that softens when exposed to heat and returns
to its original condition when cooled to room temperature. By the
term "substantially linear", as used in the specification and the
claims, it is meant that the polyester contains 2 mole percent or
less, based on the total moles of diol or diacid residues, of the
residues of a branching agent. The term "residue", as used herein,
means any organic structure incorporated into the polymer through a
polycondensation reaction involving the corresponding monomer.
Although the dicarboxylic acid residue may be derived from a
dicarboxylic acid monomer or its associated acid halides, esters,
salts, anhydrides, or mixtures thereof, the diacid component of
present invention is understood to comprise dicarboxylic acids
instead of the corresponding derivatives of dicarboxylic acids such
as, for example, the associated acid halides, esters, half-esters,
salts, half-salts, anhydrides, mixed anhydrides, or mixtures
thereof. For example, in one embodiment of the invention the diacid
component consists essentially of one or more dicarboxylic acids.
In another embodiment, the diacid component consists of one or more
dicarboxylic acids.
[0016] The process of the instant invention comprises adding a diol
component comprising 1,4-cyclohexanedimethanol, and a diacid
component to a reaction zone at a total diol:diacid component molar
ratio of about 0.97 to about 1.2. The diacid component, for
example, may comprise at least 80 mole percent, based on the total
moles of diacid component, of one or more dicarboxylic acids
selected from terephthalic acid, naphthalenedicarboxylic acid,
1,4-cyclohexanedicarboxylic acid, and isophthalic acid. Any of the
various isomers of naphthalenedicarboxylic acid or mixtures of
isomers may be used, but the 1,4-, 1,5-, 2,6-, and 2,7-isomers are
preferred. Also, 1,4-cyclohexanedicarboxylic acid may be present at
the pure cis or trans isomer or as a mixture of cis and trans
isomers. In addition to the dicarboxylic acids listed above, the
diacid component may further comprise about 0 to 20 mole percent of
one or more modifying dicarboxylic acids. Examples of modifying
dicarboxylic acids include, but are not limited to, fumaric,
succinic, adipic, glutaric, azelaic, sebacic, resorcinol diacetic,
diglycolic, 4,4'-oxybis(benzoic), biphenyldicarboxylic,
4,4'-methylenedibenzoic, trans-4,4'-stilbenedicarboxylic, and
sulfoisophthalic acids.
[0017] The diol component may comprise about 10 to 100 mole
percent, based on the total moles of the diol component, of
1,4-cyclohexanedimethanol (referred to as "CHDM"0 hereinafter). The
CHDM may be used as a pure cis or trans isomer or as a mixture of
cis and trans isomers. In addition to CHDM, the diol component may
comprise from 0 to about 90 mole percent of one or more diols
selected from neopentyl glycol, diethylene glycol, ethylene glycol,
1,2-propanediol, 1,3-propanediol, 1,4-butanediol, 1,5-pentanediol,
1,6-hexanediol, 1,8-octanediol, 2,2,4-trimethyl-1,3-pentanediol,
1,3-cyclohexanedimethanol, bisphenol A, and polyalkylene
glycol.
[0018] For example, the diacid component may comprise from about 60
to 100 mole percent terephthalic acid and 0 to about 40 mole
percent isophthalic acid and the diol residue may comprise about
100 mole percent 1,4-cyclohexanedimethanol. In another example, the
diacid component may comprise about 95 mole percent terephthalic
acid and about 5 mole percent isophthalic acid. In yet another
example, the diacid component may comprise 100 mole percent
terephthalic acid. The diol component may comprise other diols in
addition to CHDM. For example, the diacid component may comprise 80
to 100 mole percent terephthalic acid and the diol component may
comprise about 50 to about 90 mole percent
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent
1,3-cyclohexanedimethanol. Additional examples of diacid and diol
components include, but are not limited to, (i) a diacid component
comprising 100 mole percent terephthalic acid, and a diol component
comprising about 10 to about 40 mole percent
1,4-cyclohexanedimethanol and 60 to about 90 mole percent ethylene
glycol; (ii) a diol component comprising about 10 to about 99 mole
percent of of 1,4-cyclohexanedimethanol, 0 to about 90 mole percent
of ethylene glycol, and about 1 to about 25 mole percent of
diethylene glycol; (iii) a diol component comprising about 50 to
about 90 mole percent 1,4-cyclohexanedimethanol and about 10 to
about 50 mole percent ethylene glycol; (iv) a diacid component
comprising about 90 to 100 mole percent
1,4-cyclohexane-dicarboxylic acid and a diol component comprising
about 90 to 100 mole percent 1,4-cyclohexanedimethanol; and (v) a
diacid component comprising about 65 mole percent terephthalic acid
and about 35 mole percent isophthalic acid.
[0019] The process of the invention may be carried out by
continuous, semi-continuous, and batch modes of operation and may
utilize a reaction zone comprising a variety of reactor types.
Examples of suitable reactor types include, but are not limited to,
stirred tank, continuous stirred tank, slurry, tubular, wiped-film,
falling film, or extrusion reactors. The reaction zone, for
example, may comprise 2 or more reactors which, typically, are
arranged in a series configuration. The term "continuous" as used
herein means a process wherein reactants are introduced and
products withdrawn simultaneously in an uninterrupted manner. By
"continuous" it is meant that the process is substantially or
completely continuous in operation and is to be contrasted with a
"batch" process. "Continuous" is not meant in any way to prohibit
normal interruptions in the continuity of the process due to, for
example, start-up, reactor maintenance, or scheduled shut down
periods. The term "batch" process as used herein means a process
wherein all or a portion of the reactants are added to the reactor
and then processed according to a predetermined course of reaction
during which additional reactants may be fed to but no polymer is
removed from the reactor. The term "semicontinuous" means a process
where some of the reactants are charged at the beginning of the
process and the remaining reactants are fed continuously as the
reaction progresses. Alternatively, a semicontinuous process may
also include a process similar to a batch process in which all or a
portion of the reactants are added at the beginning of the process
except that one or more of the products are removed continuously as
the reaction progresses. Typically, on a commercial scale, the
process is operated advantageously as a continuous process for
economic reasons and to reduce color formation and thermal
degradation of the polymer as the polyester may deteriorate in
appearance if allowed to reside in a reactor at an elevated
temperature for too long a duration.
[0020] The diacid and diol components are added to the reaction
zone such that the molar ratio of diol:diacid components is
initially greater than the total diol:diacid component molar ratio.
The total diol:diacid component molar ratio, which is the total
moles of diol component added to the reaction zone divided by the
total moles of acid component added to the reaction zone, typically
is about 0.97 to about 1.2. Other, non-limiting examples of total
diol:diacid component molar ratio ranges are about 1.0 to about
1.15, about 1.0 to about 1.10; about 1.0 to about 1.05, and about
1.0 to about 1.03. Specific examples of total diol:diacid component
molar ratios which may be used in the process of the invention are
0.97, 0.98, 1.0, 1.03, 1.05, 1.07, 1.1, 1.12, and 1.15. Persons of
skill in the art will understand, however, that the total molar
ratio of diol component to diacid component is generally determined
by the design of the reactor in which the process occurs and the
nature of the diacid and diol components. The remaining diacid
component then can be added incrementally to the reaction zone to
bring the molar ratio of diol and diacid added to the reaction zone
down to the total ratio. The term "incrementally", as used herein,
is intended to have its plain meaning of adding the diacid
component or diol component to the reaction zone in one or more
increments or portions to increase the amount of the diol or diacid
component in the reaction zone. The increments do not have to be
equal in size. For example, one increment may contain 90% of the
total amount of diacid component and a second increment may contain
the remaining 10%. The increments may be added stepwise in discrete
portions, continuously, or in a combination thereof. Therefore, the
term "incrementally", as used in the description and claims, is
intended to include both continuous and stepwise additions of the
diol and/or diacid components. Thus, "incrementally" means that,
over the duration of the entire process, the diol or diacid
components can be added to the reaction zone continuously, stepwise
in 2 or more stages or discrete steps, or in a combination of
continuous and stepwise addition. Thus, in one embodiment of the
invention, the diacid component is added to the reaction zone in 2
or more stages. In another embodiment, the diacid component is
added to the reaction zone continuously. For example, for a
polyester prepared from the reaction of a diol component and a
diacid component at a total diol:diacid molar ratio of 1.1, the
diol component and a first increment or portion of the diacid
component may be added to the reaction zone, typically at a
temperature of about 200 to about 250.degree. C., to give intial
diol:diacid molar ratio of 1.2 or greater. A second increment
containing the remaining the diacid component then can be added
either continuously or in one or more discrete steps, also at a
temperature of about 200 to about 250.degree. C., such that at the
end of the addition the diol:diacid molar ratio is 1.1. In another
example, in a batch reaction involving terephthalic acid (TPA),
isophthalic acid (IPA), and 1,4-cyclohexanedimethanol (CHDM) at a
total diol:diacid molar ratio of 1.03, initially only IPA and a
portion of the CHDM is charged to the reactor at a CHDM:IPA molar
ratio of 1.5. The IPA and CHDM, which may be fed to the reactor in
one increment, more than one increment, or continuously, are
reacted for a period of time whereupon the remaining TPA and CHDM
is fed to the reactor in a second increment such that at the end of
the addition, the molar ratio of the total amount of diol and
diacid component added to the reactor is 1.03. The remaining TPA
and CHDM may be fed to the reactor in one or more increments,
continuously, or in a combination thereof. In another embodiment,
the process may be carried out in a series of batch or continuous
reactors, wherein a portion of one or more of TPA, IPA, and CHDM
may be added to the first reactor and the remaining portion added
to a subsequent reactor downstream in the process. The diacid and
diol components may be added separately or as a slurry mixture,
provided that the slurry components have no deleterious effect upon
the process or can be removed easily. For example, the diacid
component may be added as a mixture in water; an alcohol such as
methanol, propanol, butanol, and isopropanol; a hydrocarbon such as
toluene and xylene; or in one or more diols.
[0021] Typically, the polyester process of the invention will
comprise 2 stages: an esterification stage and a polymerization
stage, which are carried out at different temperatures and
pressures. In the esterification stage, the diol and diacid
components are esterified to form a low molecular weight polyester
or oligomer and water as a byproduct. The majority of the water
by-product is removed from the reaction zone during the
esterifcation stage. The term "oligomer", as used herein, is
understood to mean a low molecular weight polyester having an IV of
0.4 dL/g or less. In the process of the invention, the addition of
diol and diacid components typically is completed during the
esterification stage. Esterification generally occurs rapidly as
the diol and diacid components are added to the reaction zone.
Generally, the water by-product is removed from the reaction zone
continuously by distillation as the reaction occurs. The
esterification conditions may vary with the number and type of
diacid and diol components added and the stage of reaction at which
each component is added. For example, for copolyesters prepared
from TPA, IPA, and CHDM, the esterification can be conducted at
temperatures between 190.degree. C. and 280.degree. C. at a
absolute pressure of about 48 kPa to about 552 kPa. The diacid
component typically is added during the esterification step of the
process. The preferred temperature range in this case is from about
210.degree. C. to about 250.degree. C. Unexpectedly, it has been
found that maintaining the reaction zone during the esterification
phase of the process at a temperature of 250.degree. C. or less can
produce an oligomer which exhibits higher polymerization rates, as
measured by the rate of increase in IV in the polymerization step
of the process, than an oligomer produced at higher esterification
temperatures. For example, the esterification stage can be carried
out by heating the diol and diacid components at temperature of
about 210 to about 250.degree. C. at an absolute pressure of about
48 kPa to about 552 kPa after the addition of the diacid or diol
component is completed while removing a water by-product. In
another example, the diacid and diol components can be heated at a
temperature of about 210.degree. C. to about 240.degree. C. In yet
another example, the the diacid and diol components can be heated
at a temperature of about 220 to about 240.degree. C. As noted
above, the reaction pressure during esterification step may be from
about 48 kPa absolute (7 psia) to about 552 kPa absolute (80 psia).
Actual pressures used will depend upon the esterification
temperature used and the type and amount of diol and dicarboxylic
acid. The time for the esterification step will depend upon
temperature, pressure, the nature and amount of diol and diacid
components added to the esterification stage and when each
component is added. For example, the esterification times for the
production of copolyesters from TPA, IPA, and CHDM can vary between
30 minutes and 180 minutes. Typically, the duration of the
esterification step is from about 60 minutes to about 120
minutes.
[0022] The esterification step of our inventive process produces a
low molecular weight polyester or oligomer that may be reacted
further in a second, polymerization stage under vacuum at higher
temperatures until a polymer having the desired degree of
polymerization, as determined by inherent viscosity, is obtained.
For the process of the invention, the polyester from the
polymerization stage will have an IV of at least 0.5 dL/g. The
conditions of polymerization stage may vary with the number and
type of acid and diol components added and the diol-to-diacid mole
ratio used. For example, the polymerization may be conducted at
temperatures between 260.degree. C. and 310.degree. C. Additional
temperature ranges for the polymerization step include from about
260.degree. C. to about 290.degree. C. and about 260.degree. C. to
about 280.degree. C. The reaction pressure during polymerization
may be from about 53 kPa absolute (400 mm Hg) to about 0.013 kPa
absolute (0.1 mm Hg). Stirring or appropriate conditions may be
used in both the esterification and polymerization steps to ensure
adequate heat transfer and surface renewal of the reaction mixture.
During the polymerization stage, additional water from continued
esterification of the oligomer may be removed by distillation along
with small amounts of diol.
[0023] The reactions of both steps may be catalyzed by appropriate
catalysts such as, for example, various compounds of titanium, tin,
antimony, germanium, and mixtures thereof. Examples of typical
catalysts include, but are not limited to, alkoxy titanium
compounds, alkali metal hydroxides and alcoholates, salts of
organic carboxylic acids, alkyl tin compounds, metal oxides, and
the like. Typically, the polymerization catalyst is present in the
range of 1 to 500 ppm. Compounds of titanium are the preferred
catalysts. Typically, the titanium catalyst is added to the
reaction zone to give a titanium concentration based on the final
polymer weight of about 5 to about 150 ppm. Preferably, the amount
of titanium is about 10 to about 90 ppm Ti, and more preferably
about 20 to about 80 ppm. Suitable titanium compounds include
acetyltriisopropyltitanate, tetraisopropyltitanate, and
tetraisobutyltitanate. When titanium is the catalyst and ethylene
glycol is used as a comonomer with CHDM in the process, a
phosphorus compound inhibitor may optionally be used.
[0024] Persons of ordinary skill in the art will understand that in
the polymerization stage of a polyester process, two reaction
mechanisms may operate to complete the polymerization process and
increase the molecular weight of the oligomer: (1) polycondensation
whereby excess diol added in the esterification process is removed
and (2) esterification whereby free acid groups continue to react
with free hydroxyl groups from the diol components releasing water
as a byproduct. Depending on the number and type of groups
available for reaction, one or both of these mechanisms may operate
to the final molecular weight obtained and the rate of
polymerization. Without being bound by theory, it is believed that
the primary mechanism for polymerization in the process of the
present invention is esterification. Because esterification is the
primary polymer-forming reaction, the process of the invention can
exhibt an increased polymerization rate and produce a high
molecular weight polyester using low diol-to-diacid ratios and
lower polymerization temperatures.
[0025] Because our polyester process can exhibit increased reaction
rates, it is often desirable that the residence time of the
reaction zone at elevated temperatures is minimized to reduce the
amount of thermal degradation and color formation by the polyester
product. Thermal degradation of a polyester is frequency
characterized by a loss of molecular weight (as determined by IV)
and the development of color. In one embodiment, for example, the
reaction zone may have a residence time of 5 hours or less at a
temperature of 260.degree. C. or greater. Further examples of
residence times for the reaction zone of the invention at a
temperature of 260.degree. C. or greater are 4 hours or less, 3
hours or less, and 2 hours or less.
[0026] The polyesters prepared by the process of this invention
also may contain other conventional additives and ingredients which
do not deleteriously affect their end use. For example, additives
such as fillers, surface friction modifiers, light and heat
stabilizers, extrusion aids, antistatic agents, colorants, dyes,
pigments, fluorescent brighteners, antimicrobials,
anticounterfeiting markers, hydrophobic and hydrophilic enhancers,
viscosity modifiers, slip agents, tougheners, adhesion promoters,
and the like may be used. Colorants, sometimes referred to as
toners, may be added to impart a desired neutral hue and/or
brightness to the polyester. When colored polyesters are desired,
pigments or colorants may be included in the polyester reaction
mixture during the reaction of the diol and the diacid components
or they may be melt blended with the polyester after completion of
the process. A preferred method of including colorants is to use a
colorant having thermally stable organic colored compounds with
reactive groups such that the colorant is copolymerized and
incorporated into the polyester to improve its hue. For example,
colorants such as dyes possessing reactive hydroxyl and/or carboxyl
groups, including, but not limited to, blue and red substituted
anthraquinones, may be copolymerized into the polymer chain. When
dyes are employed as colorants, they may be added to the polyester
reaction process after the direct esterification reaction.
[0027] Small amounts, typically less than 2 mole %, of branching
agents may be used if desired. Conventional branching agents
include polyfunctional acids, anhydrides, alcohols and mixtures
thereof. Examples of suitable branching agents include, but are not
limited to, trimellitic anhydride, pyromellitic dianhydride,
glycerol, trimethylolpropane and pentaerythritol. Small amounts of
a branching agent are useful in increasing the melt strength and
melt viscosity of the polymers.
[0028] The thermoplastic polyesters prepared by the process of the
invention typically have an inherent viscosity, abbreviated herein
as "IV", of at least 0.5 dL/g, preferably about 0.55 to 1.3 dL/g.
For example, the thermoplastic polyesters may have an IV of at
least 0.6 dL/g, at least 0.65 dL/g, or at least 0.7 dL/g, as
measured in a 60/40 parts by weight solution of
phenol/tetrachloroethane solvent at 25.degree. C. and at a
concentration of about 0.5 g of polyester in 100 mL of solvent. In
another example the thermoplastic polyester has an IV about 0.7 to
about 0.9 dL/g. The copolyesters of the present invention typically
have less than 200 milliequivalents of carboxylic acid end groups
per kilogram of polymer (meq/kg) in the final polymer, more
preferably less than 150 meq/kg, and most preferably less than 100
meq/kg as measured by titrating 1-2 grams of copolyester in 35 ml
of o-cresol with a potassium hydroxide/ethanol solution.
[0029] Another embodiment of present invention is a process for the
preparation of a polyester, comprising: adding a diol component
comprising about 10 to about 100 mole percent
1,4-cyclohexanedimethanol, based on the total moles of diol
component, and a diacid component comprising about 60 to about 100
mole percent terephthalic acid, based on the total moles of diacid
component, to a reaction zone and at a total diol:diacid component
molar ratio of about 0.97 to about 1.15 to produce a substantially
linear, thermoplastic polyester having an inherent viscosity of at
least 0.60 dL/g, wherein the diacid component is added
incrementally to the reaction zone at a reaction zone temperature
of about 220 to about 250.degree. C. and the molar ratio of
diol:diacid component added to the reaction zone is greater than
the total molar ratio until the addition of the diacid component is
completed. The diol and diacid components and process conditions
are as described hereinabove. For example, in one embodiment, the
thermoplastic polyester may have an IV of at least 0.7. Other
examples of the total diol:diacid component molar ratio include
about 1.0 to about 1.10 and about 1.0 to about 1.05.
[0030] The thermoplastic polyester, for example, may comprise about
60 to 100 mole percent, based on the total moles of dicarboxylic
acid residues, of the residues of terephthalic acid, about 0 to
about 40 mole percent of the residues isophthalic acid, and may
comprise about 100 mole percent, based on the total moles of diol
residues, of the residues of 1,4-cyclohexanedimethanol. In another
example, the thermoplastic polyester may comprise about 95 mole
percent of the residues of terephthalic acid and about 5 mole
percent of the residues of isophthalic acid. In yet another
example, the thermoplastic polyester comprises 100 mole percent of
the residues of terephthalic acid. The thermoplastic polyester may
contain the residues of other diols in addition to CHDM. For
example, the thermoplastic polyester may comprise 80 to 100 mole
percent of the residues of terephthalic acid, about 50 to about 90
mole percent of the residues of 1,4-cyclohexanedimethanol, and
about 10 to about 50 mole percent 1,3-cyclohexanedimethanol.
Additional examples of thermoplastic polyester compositions
include, but are not limited to, (i) diacid residues comprising
about 100 mole percent of the residues of terephthalic acid and a
diol residues comprising about 10 to about 40 mole percent of the
residues of 1,4-cyclohexanedimethanol and about 60 to about 90 mole
percent of the residues of ethylene glycol; (ii) diol residues
comprising about 10 to about 99 mole percent of the residues of
1,4-cyclohexanedimethanol, 0 to about 90 mole percent of the
residues of ethylene glycol, and about 1 to about 25 mole percent
of the residues of diethylene glycol; (iii) diol residues
comprising about 50 to about 90 mole percent of the residues of
1,4-cyclohexanedimethanol and about 10 to about 50 mole percent of
the residues of ethylene glycol; and (iv) diacid residues
comprising about 65 mole percent of the residues of terephthalic
acid and about 35 mole percent of the residues of isophthalic
acid.
[0031] If the diacid component contains isophthalic acid, we have
found that a high molecular weight polyester also may be prepared
without the incremental addition of the diacid component simply by
heating a mixture the diacid component and diol component together
in the reaction zone. Hence, another embodiment of the invention is
a process for the preparation of a polyester consisting essentially
of heating a mixture of a diol component comprising about 10 to
about 100 mole percent 1,4-cyclohexanedimethanol, based on the
total moles of diol component, and a diacid component comprising
about 5 to about 40 mole percent isophthalic acid, based on the
total moles of diacid component, the mixture having total
diol:diacid component molar ratio of about 1.0 to about 1.15, at a
temperature of about 220 to about 300.degree. C. to produce a
substantially linear, thermoplastic polyester having an inherent
viscosity of at least 0.60 dL/g. Other diacid components as
described hereinabove may be present in addition to IPA. For
example, the diacid component can comprise about 60 to about 95
mole percent TPA in addition to IPA. The neat diol and diacid
components may be mixed together in a diol:diacid molar ratio of
about 1 to about 1.15 and heated in a reaction zone to form a high
molecular weight polymer. No solvents or diluents such as methanol
or water are necessary. It is advantageous to heat to the diol and
diacid components in the presence of one or more catalysts
well-known to persons of ordinary skill in the art and described
hereinabove. The phrase "consisting essentially of" when used in
the context of this embodiment of the invention is intended to
encompass a process in which a mixture comprising a diacid
component comprising about 5 to about 40 mole percent isophthalic
acid is heated in the presence of a diol component comprising about
10 to about 100 mole percent CHDM and is understood to exclude any
elements that would substantially alter the essential and novel
properties of the process to which the phrase refers. For example,
the process may include other additives such as, for example,
catalysts, flame retardants, antioxidants, colorants, etc. which do
not substantially alter the esterification and polymerization
aspects of the process. By contrast, the addition of a solvent or
diluent such as, for example, an alcohol, hydrocarbon, or water (in
excess of that produced as a byproduct of the esterification
reaction) would be expected to alter the essential properties of
the process and would be excluded from the invention.
[0032] As an alternative, our process also may be carried out by
adding the diol component incrementally to the reaction zone. Thus,
in another embodiment, the present invention provides a process for
the preparation of a polyester, comprising: adding a diol component
and a diacid component to a reaction zone at a total diol:diacid
component molar ratio of about 0.97 to about 1.15 to produce a
substantially linear, thermoplastic polyester having an inherent
viscosity of at least 0.5 dL/g, wherein the diol component is added
incrementally to the reaction zone at a temperature of about 210 to
about 250.degree. C. and the molar ratio of diol:diacid components
added to the reaction zone is less than the total molar ratio until
the addition of the diol component is completed. The various
embodiments of the diol and diacid components, process conditions,
catalysts, mole ratios, and the like, are as described hereinabove.
This embodiment, however, differs from aspects of the invention
described above in that the diacid and diol components are added to
the reaction zone such that the molar ratio of diol:diacid
components is initially less than the total diol:diacid component
molar ratio. The total diol:diacid component molar ratio, typically
is about 0.97 to about 1.15. Other, non-limiting examples of total
diol:diacid component molar ratio ranges are about 1.0 to about
1.10, about 1.0 to about 1.05, and about 1. Specific examples of
total diol:diacid component molar ratios which may be used in the
process of the invention are 0.97, 0.98, 1.0, 1.03, 1.05, 1.07,
1.1, 1.12, and 1.15. The total molar ratio of diol component to
diacid component, however, is generally determined by the design of
the reactor in which the process occurs and the nature of the
diacid and diol components. The diol component then can be added
incrementally to the reaction zone to bring the molar ratio of diol
and diacid components added to the reaction zone up to the total
molar ratio.
[0033] The instant invention also provides a process for the
preparation of a polyester, comprising: [0034] (i) contacting a
portion of a diacid component with a diol component comprising a
diol having a boiling point of at least 230.degree. C. at 101 kPa,
under esterification conditions and at a diol:diacid component
molar ratio greater than 1.2, while recovering a distillate
comprising substantially water, to form an oligomer, [0035] (ii)
adding at least one additional portion of the diacid component to
the oligomer to give a total diol:diacid component molar ratio of
1.2 or less, and [0036] (iii) heating the oligomer under
polymerization conditions for a period of 4 hours or less to
produce a linear, thermoplastic polyester having an inherent
viscosity of at least 0.65 dL/g.
[0037] The various embodiments of the diol and diacid components,
process conditions, catalysts, mole ratios, and the like, are as
described hereinabove. The process comprises contacting a portion
of the diacd component with a diol component comprising at least
one high boiling diol under esterification conditions of
temperature and pressure such that the diol:diacid component molar
ratio is greater than 1.2. During the esterification, a distillate
comprising substantially water is recovered from the esterification
reaction by distillation. By the term "substantially", it is meant
that the amount of diol present in the total amount of distillate
collected is 10 weight percent or less. The remaining portion of
the diacid component is added to the reaction zone to give a total
molar ratio of diol:diacid components of 1.2 or less. Preferably
the total diol:diacid component molar ratio is from 0.97 to 1.2,
more preferably from 1 to 1.10, and even more preferably 1.05. As
describe previously, the diacid component may be added continuously
or in 2 or more discrete steps.
[0038] During steps (i) and (ii) of the process, esterification of
the diacarboxylic acid(s) with the diol(s) is the primary
polyester-forming reaction, which releases water as a by-product.
Typically, the esterification and addition of the dicarboxylic acid
may be conducted at temperatures between 190.degree. C. and
280.degree. C. The preferred temperature range in this case is from
about 210.degree. C. to 250.degree. C. As described previously,
operating the esterification stage outside of this temperature
range generally will produce an oligomer which exhibits lower rates
of polymerization, as measured by the rate of increase in IV in the
polymerization step of the process. Other representative
temperature ranges for the esterification part of the reaction are
about 210.degree. C. to about 240.degree. C. and about 220 to about
240.degree. C.
[0039] The reaction pressure during the esterification stage may be
from about 48 kPa absolute (7 psia) to about 552 kPa absolute (80
psia). Actual pressures used will depend upon the esterification
temperature used and the diol type and amount. The time for
esterification step will depend upon temperature, pressure, the
nature and amount of diol and acid components added to the
esterification stage and when each component is added. For example,
the esterification times for the production of copolyesters from
TPA, IPA, and CHDM can vary between 30 minutes and 180 minutes.
Typically the duration of the esterification step is from about 60
minutes to about 120 minutes.
[0040] After the addition of the diacid component is completed, a
low molecular weight polyester or oligomer is produced that may be
reacted further in a second, polymerization stage under vacuum at
higher temperatures until a polymer having the desired degree of
polymerization, as determined by inherent viscosity, is obtained.
The thermoplastic polyester from the polymerization stage typically
will have an IV of at least 0.65 dL/g but a range of IV of from 0.5
dL/g to about 1.2 dL/g can be produced. Representative examples of
IV's for the thermoplastic polyester are about 0.65 dL/g, about
0.70 dL/g, about 0.75 dL/g, and about 0.8 dL/g. The conditions of
the polymerization stage may vary with the number and type of acid
and diol components added and the diol-to-diacid mole ratio used
but, typically, is conducted at temperatures between 260.degree. C.
and 310.degree. C. Additional temperatures ranges for the
polymerization step include from about 260.degree. C. to about
290.degree. C. and about 260.degree. C. to about 280.degree. C. The
reaction pressure during polymerization may be from about 53 kPa
absolute (400 mm Hg) to about 0.013 kPa absolute (0.1 mm Hg).
Stirring or appropriate conditions may be used in both the
esterification and polymerization steps to ensure adequate heat
transfer and surface renewal of the reaction mixture. During the
polymerization stage, additional water from continued
esterification of the oligomer may be removed by distillation along
with small amounts of diol. In yet another embodiment, our
invention provides a process for the preparation of a polyester,
comprising: [0041] (i) contacting a portion of a diacid component
comprising about 60 to 100 mole percent, based on the total moles
of diacid component, of terephthalic acid with a diol component
comprising about 10 to 100 mole percent, based on the total moles
of diol component, of 1,4-cyclohexanedimethanol, under
esterification conditions and at a diol:diacid component molar
ratio greater than 1.2, while recovering a distillate comprising
substantially water, to form an oligomer having a inherent
viscosity of less than 0.4 dL/g, [0042] (ii) adding at least one
additional portion of the diacid component to the oligomer to give
a total diol:diacid component molar ratio of 1.2 or less; and
[0043] (iii) heating the oligomer under polymerization conditions
for a period of 4 hours or less to produce a linear, thermoplastic
polyester having an inherent viscosity of at least 0.7 dL/g.
[0044] The various embodiments of the diol and diacid components,
process conditions, catalysts, mole ratios, and the like, are as
described hereinabove. The process comprises contacting a portion
of the diacd component comprising about 60 to 100 mole percent
terephthalic acid with a diol component comprising about 10 to 100
mole percent CHDM under esterification conditions of temperature
and pressure such that the diol:diacid component molar ratio is
greater than 1.2. Preferably the total diol:diacid component molar
ratio is from 0.97 to 1.2, more preferably from 1 to 1.10, and even
more preferably 1.05. As describe previously, the diacid component
may be added continuously or in 2 or more discrete steps.
[0045] Typically, the esterification is conducted at temperatures
of about 190.degree. C. and about 280.degree. C. The addition of
the diacid component is carried out during the esterification
stage. The preferred temperature range in for esterification is
from about 210.degree. C. to 250.degree. C. Other representative
temperature ranges for the esterification part of the reaction are
about 210.degree. C. to about 240.degree. C. and about 220 to about
240.degree. C. The reaction pressure during the esterification
stage may be from about 48 kPa absolute (7 psia) to about 552 kPa
absolute (80 psia). Actual pressures used will depend upon the
esterification temperature used and the diol type and amount.
[0046] After the addition of the diacid component is completed, a
low molecular weight polyester or oligomer having an IV of less
than 0.4 dL/g is produced that may be reacted further in a second,
polymerization stage under vacuum at higher temperatures until a
polymer having the desired degree of polymerization, as determined
by inherent viscosity, is obtained. The thermoplastic polyester
from the polymerization stage typically will have an IV of at least
0.70 dL/g but ranges of 0.5 to about 1.2 dL/g can be produced.
Representative examples of IV's for the thermoplastic polyester are
about 0.70 dL/g, about 0.75 dL/g, and about 0.8 dL/g. The
conditions of the polymerization stage may vary with the number and
type of acid and diol components added and the diol-to-diacid mole
ratio used but, typically, is conducted at temperatures between
260.degree. C. and 310.degree. C. Additional temperatures ranges
for the polymerization step include from about 260.degree. C. to
about 290.degree. C. and about 260.degree. C. to about 280.degree.
C. The reaction pressure during polymerization may be from about 53
kPa absolute (400 mm Hg) to about 0.013 kPa absolute (0.1 mm
Hg).
EXAMPLES
[0047] The invention is further illustrated by the following
examples. The catalyst concentration in the final copolyesters of
the present invention was determined by x-ray fluorescence.
Inherent viscosities (IV) were measured in a 60/40 parts by weight
solution of phenol/tetrachloroethane solvent at 25.degree. C. and
at a concentration of about 0.5 g of polyester in 100 mL of
solvent. Example 1: Production of poly(1,4-cyclohexylenedimethylene
isophthalate) oligomer (PCI-oligomer): A slurry consisting of
approximately 34.2% by weight isophthalic acid (IPA), 59.3% by
weight 1,4-cyclohexanedimethanol (CHDM), and 6.6% by weight water
was fed continuously to a 2.2 liter stirred reactor at a rate of
about 42.2 grams per minute. The reactor was maintained at a
temperature of 240.degree. C. and atmospheric pressure with an
agitator speed of 450 rpm. The PCI-oligomer product was
continuously fed to a catch pot and then to a sample pan where the
PCI-oligomer was allowed to cool to room temperature. The
PCI-oligomer was characterized by proton NMR analysis to have the
following properties: 1.973 moles CHDM component to 1 mole IPA
component, 0.336 moles IPA per mole of PCI-oligomer segments with
an average segment molecular weight in the PCI-oligomer of 141.13
grams/mole.
[0048] Examples 2-10: A copolyester of terephthalic acid was
produced by charging 35.0 grams of terephthalic acid (TPA), 50.0
grams of the PCI-oligomer produced in Example 1, 18.0 grams of
1,4-cyclohexanedimethanol, and approximately 50-70 parts per
million (ppm) titanium catalyst (as acetyltriisopropyltitanate)
based on final polymer weight to a 0.5 liter reaction vessel at
room temperature. Total diol-to-diacid feed mole ratio in this case
was 1.091:1. The reactor vessel was equipped with a mechanical
agitator, a side arm for condensate removal, a nitrogen inlet port,
and a heat source (generally an oil or metal bath). The reaction
vessel was then immersed in the heat source and brought rapidly up
to the starting temperature indicated in Table 1. Esterification
and polymerization were carried out using the reaction profile
shown in Table 1. For Example 2, the resulting polymer had an IV of
0.778 dl/g, an acid content of 38 meq/kg, and a titanium content of
48 ppm.
TABLE-US-00001 TABLE 1 Stir Start End Start End Stir Speed Speed
Time Temp. Temp Press. Press. Start End Stage (min) (.degree. C.)
(.degree. C.) (kPa) (kPa) (RPM) (RPM) 1 0.1 230 230 101 101 0 0 2 1
230 230 101 101 0 150 3 30 230 230 101 101 150 150 4 5 230 240 101
53 150 150 5 10 240 250 53 13 150 150 6 10 250 260 13 0.07 150 100
7 30 260 270 0.07 0.07 100 100 8 180 270 270 0.07 0.07 100 100 9 1
270 270 0.07 13 100 0
[0049] Several additional reactions were performed in a similar
manner as described in Example 2 but the reaction was terminated at
shorter polymerization times of 0, 40, 60, 74, and 140 minutes
after the end of stage 5 listed in Table 1. Replicates of reactions
terminated at 140 and 220 minutes were also performed. In this
example the end of stage 5 is defined as the beginning of the
polymerization phase of the reaction process. The results of these
reactions are summarized in the Table 2. As shown by the data in
Table 2, a copolyester with an IV greater than 0.5 dL/g was
obtained for all polymerization times above 40 minutes and greater
than 0.7 dL/g for polymerization times above 60 minutes.
TABLE-US-00002 TABLE 2 Diol to CHDM Acid diacid Ti by TPA PCI
Oligomer Added Polym. time IV Content mole XRF Example Added (g)
Added (g) (g) (minutes) (dL/g) (meq/kg) ratio (ppm) 3 35.64 50.58
18.20 0 0.086 408 1.086 64 4 35.65 50.56 18.21 40 0.573 117 1.086
58 5 35.50 50.00 18.06 60 0.761 81 1.092 58 6 35.02 50.02 18.10 74
0.817 42 1.093 69 7 35.27 50.00 18.03 140 0.759 50 1.086 66 8 35.62
50.02 18.02 140 0.744 71 1.079 62 9 35.00 50.00 18.20 220 0.767 58
1.095 67 10 35.00 50.00 18.00 220 0.778 38 1.091 48
[0050] Examples 11-16: A copolyester of terephthalic acid was
produced in a similar manner as described in Example 2, but using
higher temperatures in both the esterification and polymerization
steps. In this example, 35.05 grams of terephthalic acid, 50.0
grams of the PCI-oligomer produced in Example 1, 18.02 grams of
1,4-cyclohexanedimethanol, and approximately 50-70 parts per
million titanium catalyst (acetyltriisopropyltitanate) based on
final polymer weight were charged to a 0.5 liter reaction vessel at
room temperature. The TPA and CHDM were charged to the reactor
together as a molten slurry. Total diol-to-diacid feed mole ratio
in this case was 1.090:1.000. Esterification and polymerization
were carried out using the reaction profile shown in Table 3. For
Example 11, the resulting polymer had an IV of 0.640 dl/g, an acid
content of 28 meq/kg, and a titanium content of 66 ppm.
TABLE-US-00003 TABLE 3 Start End Start End Stir Speed Stir Speed
Time Temp. Temp Press. Press. Start End Stage (min) (.degree. C.)
(.degree. C.) (kPa) (kPa) (RPM) (RPM) 1 0.1 255 255 101 101 0 0 2 1
255 255 101 101 0 150 3 37 255 255 101 101 150 150 4 12 255 270 101
101 150 150 5 8 270 285 101 101 150 150 6 5 285 285 101 0.07 150
100 7 15 285 285 0.07 0.07 100 100 8 180 285 285 0.07 0.07 100 100
9 1 285 285 0.07 13 100 0
Additional reactions were performed in a similar manner as
described above but the reaction was terminated at shorter
polymerization times of 0, 30, 70, and 140 minutes after the end of
stage 5 listed in Table 3. In this example the end of stage 5 is
defined as the beginning of the polymerization phase of the
reaction process. The results of these reactions are summarized in
the Table 4. As shown by the data in Table 4, a copolyester with an
IV greater than 0.5 dL/g was obtained for all polymerization times
above 70 minutes, but no reaction yielded a copolyester with an IV
of 0.7 dL/g or greater.
TABLE-US-00004 TABLE 4 TPA CHDM Diol to Added PCI Oligomer Added
Polym. time IV Acid Content diacid mole Ti Example (g) Added (g)
(g) (minutes) (dL/g) (meq/kg) ratio (ppm) 12 35.03 50.06 18.89 0
0.147 278 1.109 68 13 35.28 50.18 18.85 30 0.343 68 1.104 64 14
35.03 50.00 18.84 70 0.538 14 1.108 68 15 35.36 50.04 18.81 140
0.655 11 1.101 64 16 35.05 50.00 18.02 200 0.640 28 1.090 66
[0051] Table 5 shows the time evolution profiles for IV and acid
content for Examples 2 and 11. It is clear that the process of
Example 2 was more successful than the process of Example 11 at
producing a high IV copolyester, even though the starting IV for
polymerization is higher for the Example 11 process. Without being
bound by theory, these results can be attributed to differences in
acid end groups available for reaction between the two processes.
In Example 11, the acid end groups are quickly depleted at low IV.
In this case, further polymerization is no longer driven by
esterification due to a lack of acid ends and therefore must be
driven by polycondensation of the diol ends. By contrast, in the
Example 2 process, there is a sufficient concentration of acid end
groups throughout the polymerization process such that
esterification is the primary reaction driving polymerization and
the reaction proceeds more rapidly. The behavior is also evident in
Table 5, which shows IV as a function of acid content for Examples
2 and 11.
TABLE-US-00005 TABLE 5 Time under vacuum Acid number IV Example
(min) (meq/kg) (dL/g) Example 2 0 408 0.086 Example 2 40 117 0.573
Example 2 60 81 0.761 Example 2 74 42 0.817 Example 2 140 50 0.759
Example 2 140 71 0.744 Example 2 220 58 0.767 Example 2 220 38
0.778 Example 11 0 278 0.147 Example 11 30 68 0.343 Example 11 70
14 0.538 Example 11 140 11 0.655 Example 11 200 28 0.640
[0052] Example 17: A copolyester of terephthalic acid was produced
in a similar manner as described in Example 2, but using a
different temperature profile and a tin catalyst (a hydrated
monobutyltin oxide available as Fastcat.RTM. 4100). In this
example, 35.10 grams of terephthalic acid, 50.07 grams of the
PCI-oligomer produced in Example 1, 18.04 grams of
1,4-cyclohexanedimethanol, and 354 parts per million tin catalyst
based on final polymer weight were charged to a 0.5 liter reaction
vessel at room temperature. The TPA and CHDM were charged to the
reactor together as a slurry. As in Example 2, the reactor was
immersed in the heat source and the temperature brought rapidly up
to the starting value indicated in 6. Total diol-to-diacid mole
ratio in this case was 1.090:1.000. Esterification and
polymerization were carried out using the reaction profile shown in
Table 6. The resulting polymer had an IV of 0.776 dl/g and an acid
content of 92 meq/kg after approximately 110 minutes under a vacuum
of 0.5 torr.
TABLE-US-00006 TABLE 6 Start End Start End Stir Speed Stir Speed
Time Temp. Temp Press. Press. Start End Stage (min) (.degree. C.)
(.degree. C.) (kPa) (kPa) (RPM) (RPM) 1 0.1 220 220 101 101 0 0 2 1
220 220 101 101 0 150 3 30 220 220 101 101 150 150 4 5 220 230 101
53 150 150 5 10 230 245 53 13 150 150 6 10 245 260 13 0.07 150 100
7 30 260 270 0.07 0.07 100 100 8 27 270 270 0.07 0.07 100 100 9 0.1
270 280 0.07 0.07 100 100 10 53 280 280 0.07 0.07 100 100 11 1 280
280 0.07 13 100 0
[0053] Examples 18-23: Several additional reactions were performed
in a similar manner as described in Example 2 to explore the effect
of changing several process variables on the ability to produce a
high IV polymer. These results are summarized in Table 7. Examples
18 and 19 demonstrate the use of lower diol-to-diacid mole ratios
and different isophthalic acid compositions. Example 20
demonstrates the use of a lower titanium catalyst level and a
higher polymerization temperature of 285.degree. C. Examples 21-23
demonstrate the use of slightly higher diol-to-diacid mole ratios.
As shown in Table 7, all runs in this example were capable of
producing a copolyester with an IV of at least 0.7 dl/g with a
final acid content of 108 meq/kg or less.
TABLE-US-00007 TABLE 7 TPA PCI Acid Diol to Ti by Added Oligomer
CHDM Polymerization IV Content diacid mole XRF Ex. (g) Added (g)
Added (g) time (minutes) (dL/g) (meq/kg) ratio (ppm) 18 52.68 27.24
39.38 210 0.701 108 1.050 70 19 46.96 41.66 29.60 65 0.765 101
1.050 62 20 35.11 50.01 18.04 95 0.768 68 1.090 38 21 37.06 50.08
20.31 130 0.772 51 1.115 85 22 36.03 50.00 20.89 130 0.747 47 1.130
54 23 36.09 50.00 20.22 130 0.875 21 1.115 72
[0054] Examples 24-29: Several additional reactions were performed
in a similar manner as described in Example 11 but with a
diol-to-diacid ratio from 1.005:1 to 1.060:1. These results are
summarized in Table 8. The data in Table 8 show that a copolyester
with an IV of at least 0.7 dl/g and a final acid content of less
than 100 meq/kg can be produced using the reaction profile in
Example 11 by using a diol-to-diacid mole ratio near 1.0:1.
TABLE-US-00008 TABLE 8 TPA PCI Acid Diol to Ti by Added Oligomer
CHDM Polym. time IV Content diacid mole XRF Example (g) Added (g)
Added (g) (minutes) (dL/g) (meq/kg) ratio (ppm) 24 41.28 56.11
20.38 120 0.659 39 1.060 59 25 41.28 56.09 19.81 120 0.660 13 1.049
60 26 41.27 56.16 19.30 120 0.652 16 1.041 60 27 41.30 56.09 18.17
120 0.688 14 1.019 72 28 41.25 56.08 17.62 120 0.700 17 1.010 59 29
41.25 56.08 17.34 120 0.702 20 1.005 67
[0055] Example 30: A copolyester of terephthalic acid was produced
by first reacting IPA and CHDM in the presence of a titanium
catalyst followed by the addition of TPA to the reaction mixture.
Initially, 24.21 grams of the IPA, 63.55 grams of CHDM, and
approximately 50 to 70 parts per million titanium catalyst
(acetyltriisopropyltitanate) based on final polymer weight were
charged to a 0.5 liter reaction vessel at room temperature. The
reactor vessel was equipped with a mechanical agitator, a side arm
for condensate removal, a feed port, a nitrogen inlet port, and a
heat source. The reaction vessel was immersed in the heat source
and rapidly brought up to the starting temperature indicated in
Table 9. Esterification and polymerization were carried out using
the reaction profile shown in Table 9. After the reaction had
proceeded 30 minutes into stage 3, 45.52 grams of TPA was added to
the reaction mixture over approximately 5 minutes. Total
diol-to-diacid feed mole ratio in this case was 1.05:1. The
resulting polymer had an IV of 0.710 dl/g, an acid content of 96
meq/kg, and a titanium content of 50 ppm.
TABLE-US-00009 TABLE 9 Start End Start End Stir Speed Stir Speed
Time Temp. Temp Press. Press. Start End Stage (min) (.degree. C.)
(.degree. C.) (kPa) (kPa) (RPM) (RPM) 1 0.1 220 220 101 101 0 0 2 1
220 220 101 101 0 150 3 60 220 220 101 101 150 150 4 5 220 230 101
101 150 150 5 60 230 230 101 101 150 150 6 5 230 240 101 53 150 150
7 10 240 250 53 13 150 150 8 10 250 260 13 10 150 100 9 30 260 270
10 0.07 100 100 10 95 270 270 0.07 0.07 100 100 11 1 270 270 0.07
13 100 0
[0056] Example 31: A copolyester of terephthalic acid was produced
by charging 45.52 grams of terephthalic acid, 24.21 grams of the
isophthalic acid, 60.5 grams of 1,4-cyclohexanedimethanol, and
approximately 50-70 parts per million titanium catalyst
(acetyltriisopropyltitanate) based on final polymer weight to a 0.5
liter reaction vessel. Total diol-to-diacid mole ratio in this case
was 1.0:1. The reactor vessel was equipped with a mechanical
agitator, a side arm for condensate removal, a nitrogen inlet port,
and a heat source. Esterification and polymerization were carried
out using the same reaction profile used in Example 2 (Table 1)
except the reaction time in stage 8 was reduced to 50 minutes. The
resulting polymer had an IV of 0.715 dL/g, an acid content of 143
meq/kg, and a titanium content of 59 ppm. A repeat of this run
resulted in a polymer with an IV of 0.678 dL/g, an acid content of
121 meq/kg, and a titanium content of 63 ppm.
[0057] Examples 32-35: Several reactions were performed in a
similar manner as described in Example 31 using a range of
diol-to-diacid ratios from 1.01:1 to 1.20:1. The reaction profile
was the same as shown in Table 8 but with a starting temperature of
210.degree. C. in stages 1-4. These results are summarized in Table
10. In these examples, the polymerization time is defined as the
time of reaction following the end of stage 8 shown in Table 9. As
shown in Table 10, all examples were capable of producing a
copolyester with an IV of at least 0.5 dL/g with a final acid
content of 100 meq/kg or less. However, from Examples 32 and 33, it
is clear that using lower diol-to-diacid ratios in this case
produces copolyesters with a higher IV in a shorter time than
Examples 34 and 35 which use higher diol-to-diacid ratios.
TABLE-US-00010 TABLE 10 TPA Acid Diol to Ti by Added IPA Added CHDM
Polym. time IV Content diacid mole XRF Example (g) (g) Added (g)
(minutes) (dL/g) (meq/kg) ratio (ppm) 32 45.52 24.21 61.13 110
0.688 99 1.010 53 33 45.52 24.21 63.55 110 0.692 89 1.050 53 34
45.52 24.21 69.60 210 0.550 30 1.150 50 35 45.52 24.21 72.63 210
0.543 38 1.200 47
[0058] Example 36: A polyester of terephthalic acid was produced by
adding TPA to CHDM in stages in the presence of a titanium
catalyst. Initially, 57.85 grams of CHDM, and approximately 50 to
70 parts per million titanium catalyst (acetyltriisopropyltitanate
in butanol) based on final polymer weight were charged to a 0.5
liter reaction vessel. The reactor vessel was equipped with a
mechanical agitator, a side arm for condensate removal, a feed
port, a nitrogen inlet port, and a heat source. Esterification and
polymerization were carried out using the reaction profile shown in
Table 11. Once the reactor came up to a reaction temperature of
260.degree. C. in stage 2, 4 distinct charges of 7.93 grams of
terephthalic acid were added to the mixture every 10 minutes
through stage 3. A final charge of 31.73 grams of terephthalic acid
was added 5 minutes after the start of stage 5. Total
diol-to-diacid feed mole ratio in this case was 1.05:1. The
resulting polymer had an IV of 0.807 dL/g, an acid content of 45
meq/kg, and a titanium content of 65 ppm.
TABLE-US-00011 TABLE 11 Start End Start End Stir Speed Stir Speed
Time Temp. Temp Press. Press. Start End Stage (min) (.degree. C.)
(.degree. C.) (kPa) (kPa) (RPM) (RPM) 1 0.1 260 220 101 101 0 0 2
15 260 220 101 101 0 150 3 50 260 220 101 101 150 150 4 30 260 275
101 101 150 150 5 10 275 280 101 101 150 150 6 5 280 285 101 53 150
150 7 5 285 290 53 13 150 100 8 5 290 295 13 0.07 100 100 9 5 295
300 0.07 0.07 100 100 10 10 300 300 0.07 0.07 100 100
[0059] Example 37: A polyester of terephthalic acid was produced in
a similar manner as in Example 36 but without staged addition of
TPA. In this example, 63.46 grams of TPA, 57.85 grams of CHDM, and
approximately 50 to 70 parts per million titanium catalyst
(acetyltriisopropyltitanate) based on final polymer weight were
charged to a 0.5 liter reaction vessel. The reactor vessel was
equipped with a mechanical agitator, a side arm for condensate
removal, a nitrogen inlet port, and a heat source. Esterification
and polymerization were carried out using the reaction profile
shown in Table 11 except stage 10 was extended to 180 minutes to
allow additional time for polymerization. Total diol-to-diacid feed
mole ratio in this case was 1.05:1. The resulting polymer had an IV
of 0.437 dL/g, an acid content of 91 meq/kg, and a titanium content
of 48 ppm.
* * * * *