Method for preparing aromatic carboxylic acids

Disclosed is a method for preparing an aromatic carboxylic acid comprising oxidizing in the liquid phase an aromatic feed compound containing at least one alkyl or acyl group with a molecular oxygen-containing gas, in a solvent comprising a low molecular weight aliphatic carboxylic acid, and in the presence of a heavy metal oxidation catalyst, thereby forming an oxidation reaction product mixture comprising an aromatic carboxylic acid; subsequently heating the oxidation reaction product mixture at a temperature of at least about 500.degree. F. to form a second product mixture; and recovering from the second product mixture the aromatic carboxylic acid. The method of this invention provides for purer, larger particle size aromatic carboxylic acid product.

FIELD OF THE INVENTION 
This invention relates generally to a method for preparing aromatic 
carboxylic acids. More particularly, this invention relates to an improved 
method for preparing aromatic carboxylic acids by the liquid phase 
oxidation of an alkyl or acyl substituted aromatic feed compound. 
BACKGROUND OF THE INVENTION 
Aromatic carboxylic acids are highly useful organic compounds. Some are 
used as intermediates for the preparation of other organic compounds, and 
some are used as monomers for the preparation of polymeric materials. For 
example, terephthalic acid is used to prepare polyethylene terephthalate, 
a widely used polyester material and the naphthalenecarboxylic acids (i.e. 
the naphthoic acids) are used for preparing photographic chemicals and 
dyestuffs. Additionally, naphthalenedicarboxylic acids can be used to 
prepare a variety of polyester and polyamide compositions. One such 
naphthalenedicarboxylic acid, 2,6-naphthalenedicarboxylic acid, is a 
particularly useful aromatic carboxylic acid because it can be reacted 
with ethylene glycol to prepare poly(ethylene-2,6-naphthalate) (PEN). 
Fibers and films manufactured from PEN display improved strength and 
superior thermal properties relative to other polyester materials such as 
polyethylene terephthalate. High strength fibers made from PEN can be used 
to make tire cord, and films made from PEN are advantageously used to 
manufacture magnetic recording tape and components for electronic 
applications. 
In order to prepare high quality PEN most suitable for the aforementioned 
applications, it is desirable to use purified 2,6-naphthalenedicarboxylic 
acid. Similarly, it is desirable to use purified forms of other aromatic 
carboxylic acids when using these compounds for the hereinabove mentioned 
applications. 
Aromatic carboxylic acids, and particularly 2,6-naphthalenedicarboxylic 
acid, are conveniently prepared by the liquid phase, metal catalyzed 
oxidation of an alkyl or acyl substituted aromatic compound. During this 
oxidation, the alkyl group (for example a methyl, ethyl or isopropyl 
group) or acyl group is oxidized to a carboxylic acid group. Although this 
is an effective oxidation reaction it nevertheless has some drawbacks. For 
example, when a 2-alkyl or 2-acyl substituted naphthalene compound is 
oxidized, the naphthalene ring itself is susceptible to oxidation and 
trimellitic acid is produced. Incomplete oxidation of a methyl group 
produces an aldehyde group instead of a carboxylic acid group. 
Furthermore, when a promoter such as bromine is used during the liquid 
phase oxidation, brominated aromatic carboxylic acids are produced. 
Although all of these impurities are undesirable, trimellitic acid is 
particularly troublesome because it tends to complex tightly to the metal 
oxidation catalysts. Such complexed metal is difficult to remove from the 
aromatic carboxylic acids and, additionally, any process streams 
containing trimellitic acid are not readily returned to the oxidation 
reaction mixture because the trimellitic acid complexes to and 
consequently deactivates the oxidation metal catalysts. Such a recycle 
stream may originate from oxidation reaction mixture mother liquor that is 
separated from the aromatic carboxylic acid after the alkyl or acyl group 
is oxidized. Such recycle stream can also be a wash stream that is formed 
by washing the aromatic carboxylic acid with a suitable solvent. Thus, a 
method that provides for an aromatic carboxylic acid having a reduced 
level of trimellitic acid and/or other impurities, or that reduces the 
level of trimellitic acid in a process stream so that it can be more 
effectively recycled to the oxidation reaction mixture is desirable. The 
present invention provides such a method. 
SUMMARY OF THE INVENTION 
This invention is a method for preparing an aromatic carboxylic acid 
comprising a) oxidizing in the liquid phase an aromatic compound having at 
least one oxidizable alkyl or acyl group with an oxygen containing gas, in 
a solvent comprising a low molecular weight carboxylic acid, in the 
presence of a heavy metal oxidation catalyst, and at a reaction 
temperature of about 250.degree. F. to about 450.degree. F., thereby 
forming an oxidation reaction product mixture comprising an aromatic 
carboxylic acid; subsequently b) heating the oxidation reaction product 
mixture at a temperature of at least about 500.degree. F. thereby forming 
a second product mixture; and c) recovering from the second product 
mixture the aromatic carboxylic acid. 
In the first step in the method of this invention, the aromatic compound 
containing at least one oxidizable alkyl or acyl group is oxidized until 
at least 90% mole percent and preferably until substantially all of the 
oxidizable alkyl and/or acyl groups are oxidized to carboxylic acid groups 
thereby forming an aromatic carboxylic acid. In a subsequent step, the 
resulting product mixture is heat treated at a high temperature of at 
least about 500.degree. F. Surprisingly, it has been discovered that this 
procedure provides for a purer form of aromatic carboxylic acid isolated 
from the oxidation reaction mixture. Additionally, the mixture remaining 
after the desired aromatic carboxylic acid is recovered, commonly referred 
to as the mother liquor, has either a reduced level of impurities and 
byproducts, or contains impurities and byproducts that are less 
detrimental for recycle to the liquid phase oxidation reaction, thereby 
facilitating the recycle of mother liquor to the oxidation reaction 
mixture. It is desirable to recycle mother liquor because it contains 
useful oxidation catalyst metals, and also because it contains oxidation 
intermediates that can be oxidized to the desired aromatic carboxylic 
acid. 
The method of this invention is particularly suitable for the oxidation of 
a dialkyl-, an alkyl-acyl- or diacylnaphthalene compound to the 
corresponding naphthalenedicarboxylic acid. The heavy metal catalyzed, 
liquid phase oxidation of such naphthalene compounds typically requires a 
high level of metal catalysts, and the oxidation reaction produces 
trimellitic acid as a reaction byproduct. The method of this invention, 
however, greatly reduces the level of trimellitic acid in the oxidation 
reaction product mixture thereby allowing for the recycle of a greater 
amount of mother liquor to the oxidation reaction. The recycled mother 
liquor contains--in addition to the valuable oxidation catalyst 
metals--fine particles of the naphthalenedicarboxylic acid, oxidation 
intermediates that can be oxidized to naphthalenedicarboxylic acids, and 
oxidation solvent. Thus, recycle saves these valuable components and also 
eliminates waste disposal problems. Additionally, the 
naphthalenedicarboxylic acid produced by the method of the invention 
contains reduced levels of undesirable impurities and byproducts, and 
2,6-naphthalenedicarboxylic acid produced by the method of this invention 
has a large particle size making filtration and washing of the 
2,6-naphthalenedicarboxylic acid more efficient. Importantly, this 
purification is achieved without first separating the 
naphthalenedicarboxylic acid from the oxidation reaction mixture. Finally, 
the method of this invention provides for greater flexibility in the 
composition of the oxidation reaction mixture and oxidation reaction 
conditions used for oxidizing the alkyl- or acylaromatic compound to the 
corresponding aromatic carboxylic acid. For example, oxidation conditions 
heretofore considered to be undesirable because they result in an 
excessive amount of trimellitic acid can now be used because the method of 
this invention provides for the efficient removal of such trimellitic acid 
before recycling the oxidation reaction mother liquor to the oxidation 
reaction.

DETAILED DESCRIPTION OF THE INVENTION 
The oxidation reaction product mixture used in the method of this invention 
is obtained from the liquid phase, heavy metal catalyzed oxidation of an 
alkyl- or acyl substituted aromatic compound. Such aromatic compounds 
include any acyl- and/or alkyl substituted aromatic compound wherein the 
acyl and/or alkyl group can be oxidized to an aromatic carboxylic acid 
group. For the purposes of this invention, a formyl group can also be 
oxidized and is considered to be equivalent to an acyl group. Particularly 
suitable aromatic feed compounds are those having the structure: 
##STR1## 
wherein n is an integer from 1 to 8, preferably 1 to 4, more preferably n 
is 1 or 2, and wherein R is independently selected from the group 
consisting of alkyl groups having 1 to about 6 carbon atoms, inclusive, 
and an acyl group containing 1 to about 6 carbon atoms, inclusive. 
Preferably, R is methyl, ethyl, isopropyl, acetyl, or formyl. Examples of 
suitable aromatic feed compounds include: o-xylene, m-xylene, p-xylene, 
4,4'-dialkyldiphenylether, 3,4'-dialkyldiphenylether, 
4,4'-dialkylbiphenyl, 3,3',4,4'-tetraalkyldiphenylether, dixylypropane, 
3,3',4,4'-tetraalkyldiphenylsulfone, wherein the alkyl group preferably 
contains 1 to 4 carbon atoms, inclusive, and more preferably wherein the 
alkyl group is methyl. Examples of useful naphthalene-based aromatic feed 
compounds include: 1-methyl- and 2-methylnaphthalene, 1-ethyl-and 
2-ethylnaphthalene, 1-isopropyl- and 2-isopropylnaphthalene; and 
2,6-dialkyl or 2-acyl-6-alkylnaphthalene compounds such as 2,6-dimethyl-, 
2,6-diethyl-, and 2,6-diisopropylnaphthalene; 
2-acetyl-6-methylnaphthalene, 2 -methyl-6-ethylnaphthalene, 
2-methyl-6-isopropylnaphthalene, and the like. Preferred aromatic 
compounds for the method of this invention are p-xylene, m-xylene and 
2,6-dimethylnaphthalene which, when oxidized, are converted to 
terephthalic acid, isophthalic acid and 2,6-naphthalenedicarboxylic acid, 
respectively. 
Sikkenga et al. U.S. Pat. Nos. 5,034,561; 5,030,781 and 4,950,825 disclose 
methods for preparing dimethylnaphthalene. In Hagen et al. U.S. Pat. 
5,026,917, a process for preparing 2-methyl-6-acetylnaphthalene is 
disclosed, and in Hagen et al., U.S. Pat. 4,873,386, a process for 
preparing 2,6-diethylnaphthalene is disclosed. 
The most preferred aromatic feed compound for oxidation in the method of 
this invention is 2,6-dimethylnaphthalene. 2,6-Naphthalenedicarboxylic 
acid obtained by the oxidation of 2,6-dimethylnaphthalene is a suitable 
monomer for preparing PEN, a high-performance polyester. Furthermore, 
2,6-dimethylnaphthalene is superior to, for example, 2,6-diethyl- or 
2,6-diisopropylnaphthalene feed because it is lower in molecular weight 
and the yield of 2,6-naphthalenedicarboxylic acid per given weight of 
2,6-dialkylnaphthalene feed compound is greater for 
2,6-dimethylnaphthalene than for 2,6-diethyl- or 
2,6-diisopropylnaphthalene. 
Methods for conducting the liquid phase, heavy metal catalyzed oxidation of 
an alkyl- or acyl-substituted aromatic compound to the corresponding 
aromatic carboxylic acid are well known in the art. For example, U.S. 
Pats. 4,950,786; 4,933,491; 3,870,754 and 2,833,816 disclose such 
oxidation methods. In general, suitable heavy metal oxidation catalysts 
include those metals having an atomic number of about 21 to about 82, 
inclusive, preferably a mixture of cobalt and manganese. The preferred 
oxidation solvent is a low molecular weight monocarboxylic acid having 2 
to about 6 carbon atoms, inclusive, preferably it is acetic acid or 
mixtures of acetic acid and water. A reaction temperature of about 
300.degree. F. to about 450.degree. F. is typical, and the reaction 
pressure is such that the reaction mixture is under liquid phase 
conditions. A promoter such as a low molecular weight ketone having 2 to 
about 6 carbon atoms or a low molecular weight aldehyde having 1 to about 
6 carbon atoms can also be used. Bromine promoter compounds known in the 
art such as hydrogen bromide, molecular bromine, sodium bromide and the 
like can also be used. A source of molecular oxygen is also required, and 
typically it is air. 
A particularly suitable method for oxidizing a 2,6-dialkyl or 
2-acyl-6-alkylnaphthalene to 2,6-naphthalenedicarboxylic acid is disclosed 
in U.S. Pat. 4,933,491 to Albertins et al. Suitable solvents for such 
liquid phase oxidation reaction of 2,6-dialkyl or 
2-acyl-6-alkylnaphthalene include benzoic acid, any aliphatic C.sub.2 
-C.sub.6 monocarboxylic acid such as acetic acid, propionic acid, 
n-butyric acid, isobutyric acid, n-valeric acid, trimethylacetic acid, 
caproic acid, and water. Preferably the solvent is a mixture of water and 
acetic acid, which mixture is preferably 1 to 20 weight percent water. The 
source of molecular oxygen employed in such liquid phase oxidation of a 
2,6-dialkyl or 2-acyl-6-alkylnaphthalene can vary in molecular oxygen 
content from that of air to oxygen gas. Because of economy, air is the 
preferred source of molecular oxygen. 
The catalyst employed in such oxidation of a 2,6-dialkyl or 
2-acyl-6-alkylnaphthalene comprises a bromine-containing compound and at 
least one of a cobalt- and manganese-containing compound. Preferably, the 
catalyst comprises cobalt-, manganese-, and bromine-containing components. 
The ratio of cobalt (calculated as elemental cobalt) in the cobalt 
component of the catalyst to 2,6-dialkyl or 2-acyl-6-alkylnaphthalene in 
the liquid phase oxidation is in the range of about 0.1 to about 100 
milligram atoms (mga) per gram mole of 2,6-dialkyl or 
2-acyl-6-alkylnaphthalene. The ratio of manganese (calculated as elemental 
manganese) in the manganese component of the catalyst to cobalt 
(calculated as elemental cobalt) in the cobalt component of the catalyst 
in the liquid phase oxidation is in the range of from about 0.1 to about 
10 mga per mga of cobalt. The ratio of bromine (calculated as elemental 
bromine) in the bromine component of the catalyst-to-total cobalt and 
manganese (calculated as elemental cobalt and elemental manganese) in the 
cobalt and manganese components of the catalyst in the liquid-phase 
oxidation is in the range of from about 0.1 to about 1.5 mga per mga of 
total cobalt and manganese. 
Each of the cobalt and manganese components can be provided in any of its 
known ionic or combined forms that provide soluble forms of cobalt, 
manganese, and bromine in the solvent in the reactor. For example, when 
the solvent is an acetic acid medium, cobalt and/or manganese carbonate, 
acetate tetrahydrate, and/or bromide can be employed. The 0.1:1.0 to 
1.5:1.0 bromine-to-total cobalt and manganese milligram atom ratio is 
provided by a suitable bromine source such as elemental bromine 
(Br.sub.2), or ionic bromide (e.g., HBr, NaBr, KBr, NH.sub.4 Br, etc.), or 
organic bromides which are known to provide bromide ions at the operating 
temperature of the oxidation (e.g., bromobenzenes, benzylbromide, 
tetrabromoethane, ethylenedibromide, etc.). The total bromine in molecular 
bromine and ionic bromide is used to determine satisfaction of the 
elemental bromine-to-total cobalt an manganese milligram atom ratio of 
0.1:1.0 to 1.5:1.0. The bromine is released from the organic bromides at 
the oxidation operating conditions of be readily determined by known 
analytical means. Tetrabromoethane, for example, at operating temperatures 
of 335.degree. F. to 440.degree. F. has been found to yield about 3 
effective gram atoms of bromine per gram mole. 
In operation, the minimum pressure at which the oxidation reactor is 
maintained is that pressure which will maintain a substantial liquid phase 
of the 2,6-dialkyl or 2-acyl-6-alkylnaphthalene and at least 70 weight 
percent of the solvent. The 2,6-dialkyl or 2-acyl-6-alkylnaphthalene and 
solvent not in the liquid phase because of vaporization is removed from 
the oxidation reactor as a vapor-gas mixture, condensed, and then returned 
to the oxidation reactor. When the solvent is an acetic acid-water 
mixture, suitable reaction gauge pressures in the oxidation reactor are in 
the range of from about 0 kg/cm.sup.2 to about 35 kg/cm.sup.2, and 
typically are in the range of from about 10 kg/cm.sup.2 to about 30 
kg/cm.sup.2. The temperature range within the oxidation reactor is 
generally from about 250.degree. F., preferably from about 350.degree. F. 
to about 450.degree. F., preferably to about 420.degree. F. At 
temperatures greater than 450.degree. F., excessive burning of the solvent 
and/or naphthalene compound occurs. The solvent residence time in the 
oxidation reactor is generally from about 20 to about 150 minutes and 
preferably from about 30 to about 120 minutes. 
The oxidation can be performed either in a batch, continuous, or 
semicontinuous mode. In the batch mode, the 2,6-dialkyl or 
2-acyl-6-alkylnaphthalene, solvent and the catalyst components are 
initially introduced batchwise into the reactor, and the temperature and 
pressure of the reactor contents are then raised to the desired levels for 
the commencement of the oxidation reaction. Air is introduced continuously 
into the reactor. After commencement of the oxidation reaction, for 
example, after all of the 2,6-dialkyl or 2-acyl-6-alkylnaphthalene has 
been completely introduced into the reactor, the temperature of the 
reactor contents is raised. In the continuous mode, each of the 
2,6-dialkyl or 2-acyl-6-alkylnaphthalene, air, solvent, and catalyst are 
continuously introduced into the oxidation reactor, and a product stream 
comprising 2,6-naphthalenedicarboxylic acid and catalyst components 
dissolved in the solvent is withdrawn from the reactor. In the 
semicontinuous mode, the solvent and catalyst are initially introduced 
into the reactor and then the 2,6-dialkyl or 2-acyl-6-alkylnaphthalene and 
air are continuously introduced into the reactor. The hereinabove 
described method for oxidizing 2,6-dialkyl or 2 -acyl-6-alkylnaphthalene 
compounds can also be used to oxidize other alkyl and/or acyl substituted 
aromatic compounds such as oxidizing p-xylene to terephthalic acid and 
m-xylene to isophthalic acid. 
For large-scale commercial operation it is preferable to use a continuous 
oxidation process. In such a process using the preferred 
2,6-dimethylnaphthalene as the aromatic feed, the weight ratio of 
monocarboxylic acid solvent to 2,6-dimethylnaphthalene is preferably about 
2:1 to about 12:1, the mga ratio of manganese to cobalt is about 5:1 to 
about 0.3:1, the mga ratio of bromine to the total of cobalt and manganese 
is about 0.3:1 to about 0.8:1, and the total of cobalt and manganese, 
calculated as elemental cobalt and elemental manganese is at least about 
0.40 weight percent based on the weight of the solvent, and the oxidation 
reaction temperature is about 370.degree. F. to about 420.degree. F. 
Acetic acid is the most suitable solvent for such preferred continuous 
oxidation of 2,6-dimethylnaphthalene. 
Depending on the oxidation reaction conditions used, the aromatic feed 
compound selected, the oxidation catalysts, and the levels of catalyst 
selected, the reaction mixture produced in the oxidation reaction 
contains, in addition to the desired aromatic carboxylic acid, a number of 
impurities and reaction by-products. For example, when 
2,6-dimethylnaphthalene is the aromatic feed compound for the oxidation 
reaction and a catalyst comprising cobalt, manganese and bromine 
components is used, the oxidation reaction mixture directly from the 
oxidation reactor, (also called the total reactor effluent or TRE) 
contains the reaction solvent, which is typically a mixture of acetic acid 
and water, the desired 2,6-naphthalenedicarboxylic acid, and impurities 
including trimellitic acid (TMLA), bromo-2,6-naphthalenedicarboxylic acid 
(BR-2,6-NDA), 2-formyl-6-naphthoic acid (2-FNA), 2-naphthoic acid (2-NA), 
a collection of other impurities, and cobalt and manganese catalyst 
components. The acetic acid and water can be removed by evaporation or 
distillation from the oxidation reaction mixture to leave a residue of 
solids. Analysis of these solids provides a useful assessment of all of 
the solid components in the oxidation reaction mixture and consequently an 
assessment of the yield of desired product and reaction by-products. In a 
typical oxidation of 2,6-dimethylnaphthalene, the amount of trimellitic 
acid in the oxidation reaction mixture solids can be as high as 5 wt % of 
the solids and typically about 3-4 wt. %. The amount of 
2-formyl-6-naphthoic acid can be as high as 1 wt % and typically is about 
0.4-0.5 wt %. The amount of bromo-2,6-naphthalenedicarboxylic acids can be 
as high as 3 wt % and is typically about 0.2 to 1 wt %. The total of 
cobalt and manganese in the solid portion of the oxidation reaction 
mixture can be as high as 4 wt %. Although the desired 
2,6-naphthalenedicarboxylic acid is generally insoluble in the oxidation 
reaction mixture, particularly when the oxidation reaction mixture is 
cooled to a temperature below the oxidation reaction temperature, and can 
be easily separated from the oxidation reaction mixture, the 
2,6-naphthalenedicarboxylic acid recovered is also contaminated with 
trimellitic acid, 2-formyl-6-naphthoic acid, 
bromo-2,6-naphthalenedicarboxylic acids, other organic impurities and 
by-products, as well as the cobalt and manganese oxidation metal 
catalysts. Furthermore, even when the 2,6-naphthalenedicarboxylic acid is 
separated from the oxidation reaction mixture at an elevated temperature, 
and even if the separated 2,6-naphthalenedicarboxylic acid is washed with 
fresh solvent at an elevated temperature to remove residual mother liquor, 
the recovered 2,6-naphthalenedicarboxylic acid still contains substantial 
amounts of the aforementioned impurities and by-products which require 
removal from the 2,6-naphthelenedicarboxylic acid. 
However, we have now discovered that the level of the undesirable 
impurities formed during the liquid phase oxidation of an alkyl- or 
acyl-substituted aromatic feed compound can be substantially reduced by 
heating the oxidation reaction product mixture (i.e., the total reactor 
effluent (TRE)) at an elevated temperature of at least about 500.degree. 
F., preferably at least about 550.degree. F., and most preferably at least 
about 600.degree. F. Although reaction temperatures above about 
600.degree. F., for example, 650.degree. F., are highly effective, it is 
preferable not to operate at a temperature greater than 700.degree. F. 
Importantly, the high temperature step of this invention is subsequent to 
the oxidation step where, preferably, substantially all of the oxidizable 
alkyl or acyl groups on the aromatic ring are oxidized to carboxylic acid 
groups. Additionally, the high temperature step is effective in reducing 
the level of undesirable impurities in the absence of any added molecular 
oxygen, i.e., molecular oxygen added from an external source. 
While the oxidation reaction product mixture is heat treated at the 
aforementioned elevated temperatures of at least about 500.degree. F., it 
is desirable to maintain at least about 50 weight percent and preferably 
substantially all of the solvent in the liquid phase and to avoid the loss 
of solvent. Consequently, it is desirable to employ a pressurized vessel 
to maintain the low molecular weight carboxylic acid oxidation solvent in 
the liquid phase. A suitable pressure for the heat treatment is a pressure 
of about 200 psig to about 3000 psig. The pressure required will 
necessarily be related to the temperature selected and the vapor pressure 
of water and of the low molecular weight carboxylic acid solvent used for 
the oxidation reaction. Additionally, the oxidation reaction mixture can 
be supplemented with additional low molecular weight carboxylic acid, 
water or other solvent prior to heating to a temperature above about 
500.degree. F. Suitable low molecular weight carboxylic acids are those 
containing 1 to about 8 carbon atoms. Preferably, it is an aliphatic, 
monocarboxylic acid, and most preferably it is the same low molecular 
weight carboxylic acid that is used for the oxidation reaction. The amount 
of solvent present during the heat treating step in the method of this 
invention can be an amount that provides for the dissolution of 
substantially all of the aromatic carboxylic acid present. However, 
complete or substantially complete dissolution is not required. For 
example, the heat treating step of this invention is effective when at 
least 10 weight percent, preferably 20 weight percent of the aromatic 
carboxylic acid is in solution. A suitable weight ratio of solvent to 
aromatic carboxylic acid is at least about 2:1, preferably from about 3:1 
to about 10:1. When the aromatic carboxylic acid is 
2,6-naphthalenedicarboxylic acid, the preferred solvent for the high 
temperature heat treatment is acetic acid, optionally containing about 2 
to about 50 weight percent water. 
In the heat treatment step of this invention, the oxidation reaction 
product mixture is heated at a temperature of at least about 500.degree. 
F. for a time period sufficient to reduce the level of undesirable 
impurities and by-products contained therein. The time period during which 
the oxidation reaction mixture is maintained at a temperature of at least 
about 500.degree. F. is suitably at least about 0.1 minute, preferably at 
least about 1 minute and most preferably at least about 10 minutes. After 
this heating at a temperature of at least about 500.degree. F., the levels 
of undesirable impurities in the oxidation reaction product mixture are 
reduced. For example, when the oxidation reaction product mixture contains 
trimellitic acid, the level of trimellitic acid is reduced, when the 
oxidation reaction mixture contains a formyl naphthoic acid, the level of 
the formyl naphthoic acid is reduced, and when the oxidation reaction 
mixture contains one or more bromo naphthalenecarboxylic acids, the level 
of these brominated acids is reduced. The reduced levels of impurities in 
the oxidation reaction mixture after the heat treatment according to the 
method of this invention, for example, provides for a purer form of 
2,6-naphthalenedicarboxylic acid when the 2,6-naphthalenedicarboxylic acid 
is separated from heat-treated the oxidation reaction mother liquor. 
Additionally, the oxidation reaction mixture mother liquor after the heat 
treatment according to the method of this invention contains lower levels 
of trimellitic acid thereby making the mother liquor more suitable for 
recycle to the oxidation reaction since it contains less trimellitic acid 
to complex and deactivate the metal oxidation catalysts. For example, when 
the oxidation reaction mixture is produced by the oxidation of 
2,6-dimethylnaphthalene or other 2,6-dialkylnaphthalene compounds and the 
oxidation reaction mixture contains bromo-2,6-naphthalenedicarboxylic 
acids, 2-formyl-6-naphthoic acid and trimellitic acid, the amount of 
bromo-2,6-naphthalenedicarboxylic acid in the oxidation reaction mixture 
can be reduced by at least about 25 percent and preferably by at least 
about 50 percent, the amount of 2-formyl-6-naphthoic acid can be reduced 
by at least about 15 percent, and preferably by at least about 30 percent, 
and the amount of trimellitic acid can be reduced by at least about 20 
percent and preferably by at least about 50 percent. Preferably, the 
oxidation reaction mixture used in the high temperature treatment step of 
this invention comprises acetic acid, water, cobalt and manganese 
oxidation metals, 2,6-naphthalenedicarboxylic acid, trimellitic acid, 
2-formyl-6-naphthoic acid and bromo-2,6-naphthalenedicarboxylic acids. 
During the heat treating step of the method of this invention, the 
oxidation reaction mixture containing the aromatic carboxylic acid can be 
treated with one or more oxidizing, reducing or other purification agents 
to further improve the purity of the resulting aromatic carboxylic acid 
and to further eliminate undesirable components such as aldehydes and 
brominated aromatic compounds in the oxidation reaction mixture mother 
liquor. For example, the oxidation reaction mixture (either before or 
after the desired aromatic carboxylic acid is removed) when being heated 
at a temperature of at least about 500.degree. F. can be treated with one 
or more oxidizing agents such as manganese dioxide, hypobromous acid, 
hydrogen peroxide or other peroxides, and the like. Alternatively, and 
preferably, it can be treated with a reducing agent such as hydrogen gas. 
Hydrogen gas is the preferred reagent and a suitable hydrogen gas partial 
pressure is about 5 psig to about 500 psig. When hydrogen gas is used it 
is also preferable to use one or more standard hydrogenation catalysts. 
Suitable hydrogenation catalysts include one or more of the Group VIII 
noble metals. A Group VIII noble metal deposited on a support material is 
a preferred hydrogenation catalyst. For example, at least one of platinum, 
palladium, rhodium, rhenium, or ruthenium deposited on a support material 
such as alumina, titania or carbon. Most preferably, the hydrogenation 
catalyst is platinum, ruthenium, or palladium deposited on a carbon 
support. The weight ratio of hydrogenation catalyst to oxidation reaction 
mixture is suitably about 0.001:1 to about 0.5:1, preferably about 0.005:1 
to about 0.05:1, based on the total weight of the catalyst, including the 
support material, if used. When a Group VIII noble metal catalyst is used 
the noble metal is present in the catalyst typically in amount of about 
0.1 wt % to about 5 wt % based on the total weight of the catalyst. A 
preferred catalyst is a platinum, ruthenium or palladium on carbon 
catalyst wherein the metal is present in an amount of about 0.01% to about 
1.0 wt % based on the weight of the catalyst. 
When hydrogen is used in the heat treatment step of this invention along 
with a hydrogenation catalyst, it is desirable to operate at a temperature 
and at a ratio of solvent to aromatic carboxylic acid such that the 
aromatic carboxylic acid is substantially or, preferably, completely in 
solution. Under such conditions, it is possible to pass the oxidation 
reaction mother liquor containing the impure aromatic carboxylic acid 
through a fixed bed of hydrogenation catalyst. However, when using 
hydrogen it is not absolutely necessary to have all the aromatic 
carboxylic acid in solution. For example, the hydrogenation catalyst can 
be contained on one side of screen or filter or other barrier that permits 
the passage of dissolved aromatic carboxylic acid, other dissolved 
components and the hydrogen, but does not permit the passage of 
particulate material such as the insoluble components of the oxidation 
reaction mixture, including the aromatic carboxylic acid not in solution. 
Using this type of arrangement, the hydrogenation reaction can proceed 
without subjecting the hydrogenation catalyst to the insoluble components 
of the oxidation reaction mixture, which components could plug the 
hydrogenation catalyst. However, as mentioned hereinabove, when using 
hydrogen during the high temperature treatment, it is desirable to operate 
under conditions where the aromatic carboxylic acid is substantially 
completely and, preferably, completely in solution. In an integrated 
process such as in a large scale manufacturing plant, the oxidation 
reaction mixture exiting the oxidation reaction zone may not contain 
sufficient low molecular weight carboxylic acid and/or water to dissolve 
the aromatic carboxylic acid at the temperature used for the high 
temperature treatment. It may, therefore, be desirable to add additional 
solvent such as water or a low molecular weight carboxylic acid to the 
reaction mixture to dissolve additional aromatics, and preferably all, of 
the aromatic carboxylic acid. One possible source of such solvent is the 
mixture of low molecular carboxylic acid and water that is obtained from 
the oxidation reaction mixture vapor which would otherwise be condensed 
and at least partially returned to the oxidation reaction mixture. 
However, some or all of this condensate can be added to the high 
temperature reaction mixture to assist in dissolving the aromatic 
carboxylic acid. Example 10 hereinbelow provides data for the solubility 
of 2,6-naphthalenedicarboxylic acid in water and acetic acid. These data 
can be used to estimate the amount of acetic acid, a preferred solvent, 
and/or water, another preferred solvent, required to dissolve 
2,6-naphthalenedicarboxylic acid at a given reaction temperature. 
When hydrogen gas is used in the high temperature process of this 
invention, the removal of 2-formyl-6-naphthoic acid and 
bromo-2,6-naphthalenedicarboxylic acid from an oxidation reaction mixture 
and from the 2,6-naphthalenedicarboxylic acid isolated from the oxidation 
reaction mixture is facilitated. For example, when hydrogen gas and a 
suitable hydrogenation catalyst is used during the heat treatment of the 
oxidation reaction mixture formed by the oxidation of 
2,6-dimethylnaphthalene, the hydrogen assists in the removal of 
2-formyl-6-naphthoic acid, and the hydrogen also assists in the removal of 
bromo-2,6-naphthalenedicarboxylic acid. Significantly, the 
2-formyl-6-naphthoic acid is converted to materials that when recycled to 
the oxidation reaction are converted to 2,6-naphthalenedicarboxylic acid. 
The reaction of bromo-2,6-naphthalenedicarboxylic acid with hydrogen 
produces 2,6-naphthalenedicarboxylic acid. Thus, there is no loss of 
valuable product. Consequently, when hydrogen is used during the high 
temperature treatment, an oxidation reaction mixture containing greater 
amounts of 2-formyl-6-naphthoic acid and bromo-2,6-naphthalenedicarboxylic 
acid can be tolerated. Therefore, the conditions used to oxidize the 
2,6-dialkyl- or 2-alkyl-6-acylnaphthalene compound can be adjusted to 
provide for higher levels of 2-formyl-6-naphthoic acid and/or 
bromo-2,6-naphthalene-dicarboxylic acid. This is advantageous because in 
prior art processes it was necessary to use rather severe oxidation 
conditions to assure the complete oxidation of the 2-formyl-6-naphthoic 
acid to 2,6-naphthalanedicarboxylic acid. However, the severe oxidation 
conditions that provide for low levels of 2-formyl-6-naphthoic acid also 
produces greater amounts of trimellitic acid. Therefore, the method of 
this invention, wherein hydrogen is added during the high temperature 
treatment, provides for the flexibility of selecting oxidation conditions 
that produces aromatic aldehydes and brominated aromatic compounds because 
the treatment with hydrogen facilitates the removal of such compounds from 
the oxidation reaction mixture. 
Following the high temperature treatment step in the method of this 
invention, either with or without the use of hydrogen or other 
purification agent, the mixture is typically cooled to promote the 
crystallization of the desired aromatic carboxylic acid. The degree of 
cooling necessary will depend on such variables as the specific aromatic 
carboxylic acid present, the amount of low molecular weight carboxylic 
acid solvent used, the temperature used for the high temperature 
treatment, and the desired purity of the aromatic carboxylic acid. 
However, in general, the reaction mixture is cooled to a temperature of no 
more than about 450.degree. F., preferably in the range of about 
100.degree. F. to about 400.degree. F., more preferably about 150.degree. 
F. to about 350.degree. F. When the aromatic carboxylic acid is 
2,6-naphthalenedicarboxylic acid, the reaction mixture is preferably 
cooled to a temperature less than about 500.degree. F., more preferably in 
the range of about 200.degree. F. to about 450.degree. F. 
While the reaction mixture can be cooled relatively rapidly by using, for 
example, one or more flash crystallizers, slow cooling is preferred. Slow 
cooling provides for larger particle size product and may provide for 
purer aromatic carboxylic acid. Preferably, the cooling rate is no more 
than about 80.degree. F./minute, more preferably no more than about 
50.degree. F./minute. Most preferably the cooling rate is in the range of 
about 1.degree. F./minute to about 40.degree. F./minute. 
An advantage of the high temperature treatment step in the method of this 
invention is the formation of large particle size aromatic carboxylic 
acid. For example, the 2,6-naphthalenedicarboxylic acid isolated directly 
from the oxidation reaction mixture without a high temperature treatment 
typically has a small mean particle size of about 15-20 microns, as 
measured by a Microtrac.RTM. particle size analyzer, and also contains a 
substantial amount of very fine particles, e.g., about 20-40 wt. % of the 
particles have a particle size less than about 11 microns. The method of 
this invention, however, produces 2,6-naphthalenedicarboxylic acid having 
a mean particle size of at least about 40 microns, more preferably at 
least about 60 microns, and, significantly, only a small percentage of the 
2,6-naphthalenedicarboxylic acid is in the form of very small particle, 
e.g., no more than about 15 wt. % of the 2,6-naphthalenedicarboxylic acid 
having a particle size less than about 11 microns and, more preferably, no 
more than about 10%. 2,6-Naphthalenedicarboxylic acid having a mean 
particle size of 100 microns and greater have been prepared by the method 
of this invention. 
The formation of large particle size aromatic carboxylic acid, and 
particularly 2,6-naphthalenedicarboxylic acid, is desirable because the 
large particle size aromatic carboxylic acid is more easily filtered or 
otherwise separated from the reaction mixture mother liquor, and is also 
more easily washed with solvent to remove the last traces of mother 
liquor. Additionally, the presence of the very fine particles of aromatic 
carboxylic acid causes plugging of filters and other devices used to 
separate the aromatic carboxylic acid from the reaction mother liquor or 
wash solvent. 
After the heat treatment step in the method of this invention, either with 
or without a cooling step, the solid aromatic carboxylic acid, and 
preferably 2,6-naphthalenedicarboxylic acid, is partitioned, i.e., 
separated, from the reaction mother liquor. Any suitable means can be used 
for this partitioning step, such as filtration, centrifugation, settling 
and the like. The mother liquor separated from the aromatic carboxylic 
acid contains valuable oxidation catalyst metals and, as discussed 
hereinabove, is typically recycled at least in part to the oxidation 
reaction mixture. Some or all of the low molecular weight carboxylic acid 
solvent can be removed prior to recycle. The aromatic carboxylic acid 
collected in the apparatus used for partitioning the aromatic carboxylic 
acid from the high temperature reaction mixture is optionally washed with 
a solvent to remove residual mother liquor. This solvent can be water, a 
low molecular weight carboxylic acid having 1 to about 6 carbon atoms, 
preferably acetic acid, mixtures of such low molecular weight carboxylic 
acid with water, or any other suitable solvent such as toluene, xylene, a 
C.sub.9 aromatic, and the like. The weight ratio of wash solvent to 
aromatic carboxylic acid is suitably about 0.2:1 to about 3:1. When the 
aromatic carboxylic acid is 2,6-naphthalenedicarboxylic acid, the 
preferred wash solvent is acetic acid or mixtures of acetic acid and 
water, where the water present is about 5 to about 95 weight percent of 
the mixture, and wherein the weight ratio of acetic acid or mixture of 
acetic acid and water to 2,6-naphthalenedicarboxylic acid is about 0.2:1 
to about 2:1. Furthermore, it is preferable that the wash solvent be at an 
elevated temperature preferably at about 200.degree. F. to about 
450.degree. F. Although one wash step is usually sufficient, additional 
washing steps can be used. 
After the aromatic carboxylic acid is partitioned from the high temperature 
reaction mixture, or after the optional washing step, the aromatic 
carboxylic acid is typically dried to remove the remaining solvent. The 
dried aromatic carboxylic acid is used as is for one or more of the 
heretofore mentioned applications, or it is purified further by one or 
more purification procedures such as the esterification procedure 
described below. For example, when the aromatic carboxylic acid is 
2,6-naphthalenedicarboxylic acid, it can be purified by heating it with a 
solvent comprising a mixture of water and acetic acid at a temperature of 
at least about 500.degree. F. in the presence of hydrogen and a Group VIII 
noble metal hydrogenation catalyst. 
As mentioned hereinabove, the aromatic carboxylic acid recovered from the 
oxidation reaction mixture after the oxidation reaction mixture is heated 
at elevated temperatures according to the method of this invention can be 
purified further by converting the aromatic carboxylic acid to an ester. 
The ester can be purified by methods such as recrystallization, 
distillation, sublimation, etc. The esters are suitably prepared by 
methods well known in the art. For example, the aromatic carboxylic acid 
can be heated at an elevated temperature in the presence of an alcohol, 
and, optionally, in the presence of one or more esterification catalysts. 
Typically, the alcohol selected is a low-molecular weight alcohol having 1 
to about 6 carbon atoms. Methods for preparing the ester of 
2,6-naphthalenedicarboxylic acid are disclosed in U.S. Pat. No. 4,886,901 
to Holzhauer et al., and in U.S. patent applications 07/708,492 and 
07/708,500 filed on May 31, 1991, the specifications of such patent and 
applications are hereby incorporated by reference. 
An advantage of the present invention is that the aromatic carboxylic acid 
prepared according to the method of this invention is more suitable for 
preparing an ester. This is because the aromatic carboxylic acids are 
purer than they would otherwise be and during the preparation and 
purification of the ester, the purer form of aromatic carboxylic acid 
contributes less impurities that need to be removed during the ester 
purification process. For example, a preferred method for preparing the 
dialkylester of 2,6-naphthalenedicarboxylic acid is to react 
2,6-naphthalenedicarboxylic acid with a molar excess of an alcohol, 
preferably methanol, at an elevated temperature. For example, a weight 
ratio of alcohol to 2,6-naphthalenedicarboxylic of about 1:1 to about 
10:1, respectively, at a temperature in the range of about 100.degree. F. 
to about 700.degree. F. An esterification catalyst such as sulfuric acid, 
phosphoric acid, hydrochloric acid or other strong acid, in an amount of 
about 0.1 to about 10 weight percent based on the weight of the 
2,6-naphthalenedicarboxylic acid, or one or more of the metal-based 
catalysts disclosed in British Patent Specification 1,437,897 may be used, 
if desired. Following the esterification reaction, the mixture is cooled 
to crystallize the product ester. The product ester is preferably 
recrystallized in methanol or an aromatic solvent such as toluene, or a 
xylene, and the recrystallized product is optionally fractionally 
distilled at reduced pressure, preferably in a high efficiency 
fractionation column, to form a purified 
dimethyl-2,6-naphthalenedicarboxylate. During the preparation and 
purification of this as with other aromatic carboxylic acid esters, a 
number of process streams containing concentrates of impurities are 
produced. For example, when the ester is crystallized, the mother liquor 
from the esterification reaction contains impurities such as fully or 
partially esterified oxidation impurities. This stream, after removal of 
substantially all of the alcohol, can be recycled to the oxidation 
reaction mixture or, preferably, it can be recycled to the high 
temperature heating step of this invention. Similarly, the mother liquor 
from the recrystallization reaction, after removal of substantially all of 
the methanol or aromatic solvent, can be recycled to the oxidation 
reaction mixture or, preferably, to the high temperature heating step of 
this invention. Also, if a distillation of the ester is performed, the 
distillation bottoms contain a concentration of one or more impurities and 
the distillation bottoms, or a part thereof, can be recycled to the 
oxidation reaction mixture or, preferably, to the high temperature heating 
step of this invention. 
Although it is preferable to perform the heat treatment step of this 
invention prior to separating the aromatic carboxylic acid from the 
oxidation reaction mixture, heat treating the mother liquor after the 
separation is also beneficial. Thus, another embodiment of the method of 
this invention is to first separate the aromatic carboxylic acid from the 
oxidation reaction mixture, and subsequently subject the recovered mother 
liquor to the high temperature treatment as described hereinabove. 
The high temperature heat treatment step of this invention can be conducted 
in the batch mode as well as a continuous mode of operation. 
DETAILED DESCRIPTION OF THE FIGURE 
FIG. 1 is a schematic of the preferred method of operating this invention 
using 2,6-dimethylnaphthalene as the feed for the oxidation reaction. The 
liquid phase, catalytic oxidation of 2,6-dimethylnaphthalene occurs in 
reactor section 1. Feed lines 2-5 are used to feed, respectively, 
2,6-dimethylnaphthalene, acetic acid oxidation solvent, catalyst (i.e., 
bromine, cobalt and manganese components) and air, to the oxidation 
reactor. The total oxidation reactor effluent (i.e., impure 
2,6-naphthalenedicarboxylic acid, water, and the acetic acid reaction 
solvent containing dissolved catalyst components and reaction by-products 
and impurities) is fed to the high temperature treatment reactor 20 
through line 15. In the high temperature treatment reactor, the total 
oxidation reactor effluent is heated to an elevated temperature of at 
least about 500.degree. F. to reduce the levels of impurities and 
byproducts in the mother liquor, to improve the purity of the 
2,6-naphthalenedicarboxylic acid and to increase the particle size of the 
2,6-naphthalenedicarboxylic acid. This reactor can be for example, a 
stirred tank reactor or a compartmentalized reactor. Optionally, hydrogen 
gas can be added to the high temperature reactor through line 25 and a 
suitable hydrogenation catalyst can be added to the high temperature 
reactor 20. The product mixture from the high temperature reactor is 
cooled in crystallizer 35. Cooling is suitably accomplished by a pressure 
reduction allowing the mixture to cool by the evaporation of solvent as 
the pressure is reduced. If a more gradual cooling is desired, a series of 
crystallizers can be used in order to reduce the temperature in a stepwise 
manner. Alternatively, a scraped-wall tubular heat exchanger can be used 
to gradually cool the mixture. Gradual cooling promotes the formation of 
large crystals of 2,6-naphthalenedicarboxylic acid. After crystallization, 
the crystallized 2,6-naphthalenedicarboxylic acid and the mother liquor 
are transferred through line 40 to a solid-liquid separation device 45. 
The solid liquid separation device is suitably a rotary filter, centrifuge 
or settling vessel. The collected 2,6-naphthalenedicarboxylic acid is 
optionally washed with, for example, acetic acid or a mixture of acetic 
acid and water. The wash liquid, optionally at an elevated temperature, is 
added to the solid-liquid separation device through line 50. Solid, wet 
2,6-naphthalenedicarboxylic acid is sent through line 55 to dryer 60 where 
any residual solvent is evaporated. The product 
2,6-naphthalenedicarboxylic acid exits dryer through line 65. The liquid 
separated from the reaction mixture in the solid-liquid separating device, 
as well as the used wash solvent, is sent to a mother liquor recovery unit 
75 through line 70. A portion of the mother liquor, optionally having at 
least some of the water removed, is recycled to the oxidation reactor 
through line 80. The remaining portion, for example, 5 to 50 percent of 
the total mother liquor, is sent to the solvent recovery unit 95 through 
line 90. The solvent recovery unit is typically a multi-step distillation 
apparatus for removing water from the acetic acid solvent. The recovered 
acetic acid is optionally recycled to the oxidation reactor 1, bottoms 
from the solvent recovery are purged through line 98. During the oxidation 
reaction, an overhead condenser 110 condenses and cools the acetic 
acid/water mixture vapor produced by the exothermic oxidation reaction and 
supplied to the condenser through line 115. The cool condensate is, in 
part, returned to the reactor through line 120 to control the temperature 
of the oxidation reaction. A portion of the condensate, which is enriched 
in water relative to the oxidation solvent mixture is also sent to the 
high temperature treatment reactor 20 through line 130. The proportion of 
condensate returned to the reactor compared to that sent to the high 
temperature reactor depends on the level of solvent desired in the high 
temperature reactor. The ability to add the oxidation reaction condensate 
to the high temperature reactor provides for the ability to provide for 
lower levels of water in the oxidation reactor. Lower water levels in the 
oxidation of 2,6-dimethylnaphthalene to 2,6-naphthalenedicarboxylic acid 
provides for reduced levels of oxidation impurities and by-products. 
The present invention will be more clearly understood from the following 
examples. It being understood, however, that these examples are presented 
only to illustrate some embodiments of the invention and are not intended 
to limit the scope thereof. 
EXAMPLES 
The following is the general oxidation procedure that was used to oxidize 
2,6-dimethylnaphthalene to 2,6-naphthalenedicarboxylic acid for Examples 1 
and 2. 
The oxidation apparatus consisted of a one-liter titanium reactor equipped 
with an overhead, water-cooled titanium condenser, a thermowell, an inlet 
line for air, a heated feed line, and a pressure regulator. Acetic acid 
was used as the oxidation solvent and cobalt (II) acetate tetrahydrate and 
manganese (II) acetate tetrahydrate were used as the oxidation catalysts. 
Aqueous hydrobromic acid was the source of bromine for the oxidation 
reaction. The condenser provided for cooling by returning to the reactor 
condensed solvent that vaporized by the heat generated in the oxidation 
reaction. During the oxidation reaction, both air and the 
2,6-dimethylnaphthalene feedstock were fed to the oxidation reactor so 
that there was a slight excess of air and to provide up to 6% oxygen in 
the vent gas. At the end of the oxidation reaction, the feedstock and air 
flow into the reactor were stopped and the reactor contents, i.e., the 
total reactor effluent, were transferred to a product receiver through a 
transfer line. The total reactor effluent was allowed to cool in the 
product receiver to below the boiling point of acetic acid at ambient 
pressure. 
Particle size was measured using a Microtrac II.TM. Standard Range Analyzer 
manufactured by Leeds and Northrup Co., St. Petersburg, Fla. Methanol (or 
water) was used as circulating liquid for suspending the 
2,6-naphthalenedicarboxylic acid particles. This method is a based on 
laser light scattering, and provides both a mean (average) and median 
value for the particles measured. The weight percent of the 
2,6-naphthalenedicarboxylic acid having a particle size of less than 11 
microns can also be determined by this particle size analysis. Organic 
components were analyzed by liquid chromatography. Metals and bromine were 
measured by X-ray fluorescence spectroscopy. 
In the following Examples and Tables, 2,6-naphthalenedicarboxylic acid is 
2,6-NDA, trimellitic acid is TMLA, 2-formyl-6-naphthoic acid is 2-FNA, 
2-naphthoic acid is 2-NA, and bromo-2,6-naphthalenedicarboxylic acid is 
Br-2,6-NDA. 
Values in the Tables and Examples referred to as "Normalized 2,6-NDA", were 
obtained by dividing the actual percent 2,6-NDA obtained directly from the 
liquid chromatographic analysis by the "Total" value reported and 
multiplying by 100. Because of the magnitude of signal for the 2,6-NDA 
component, the actual value obtained is a less accurate measurement of 
concentration. The value was, therefore, normalized as described above. 
Values of 0.00 in the Tables indicate that the component was not detected 
by the analysis method used. 
EXAMPLE 1 
Table I reports the data for five oxidation reactions each using the same 
weight ratio of oxidation solvent to 2,6-dimethylnaphthalene feedstock. 
For Runs 1 and 3, oxidation conditions were selected to minimize the 
amount of 2-formyl-6-naphthoic acid in the product. This would be 
desirable in a conventional process because 2-FNA is difficult to remove 
and it is an undesirable component in 2,6-NDA used for preparing PEN and 
other polyesters. However, as demonstrated by the data in Table 1, the 
conditions that minimize 2-FNA also cause the formation of trimellitic 
acid and increased burning of the acetic acid solvent as evidenced by the 
high amount of carbon oxides. For Runs 2, 4 and 5, conditions were 
selected so that the amount of TMLA and/or carbon oxides were reduced to 
produce, generally, a higher yield of 2,6-NDA but also a higher yield of 
the undesirable 2-FNA. 
However, as discussed hereinabove and demonstrated in subsequent Examples, 
the high temperature heating method of this invention can be used to 
reduce the level of 2-FNA in the oxidation reaction mixture. Additionally, 
when hydrogen is employed in this heating step, the 2-FNA is presumably 
converted to an intermediate that, when recycled to the oxidation reaction 
mixture, is oxidized to 2,6-naphthalenedicarboxylic acid. 
EXAMPLE 2 
Table 2, Runs 1-3, reports data for the oxidation of 
2,6-dimethylnaphthalene to 2,6-naphthalenedicarboxylic acid using 
reactions conducted at decreasing weight ratios of solvent to 
2,6-dimethylnaphthalene feedstock. Low ratios of solvent to feedstock are 
desirable because more 2,6-NDA can be prepared per given size oxidation 
reactor, and these data demonstrate that low ratios of 
solvent-to-feedstock can successfully be used. Furthermore, the amount of 
reaction byproduct such as bromo-2,6-naphthalenedicarboxylic acid caused 
by the lower ratio of solvent to 2,6-dimethylnaphthalene feedstock can be 
reduced, and in some cases its presence can be eliminated using the method 
of this invention. Therefore, the method of this invention allows for the 
use of lower amounts of solvent in the oxidation reaction mixture. 
Table 2, Runs 4-6, demonstrate that the use of higher levels of bromine in 
the oxidation reaction can cause a desirable decrease in the amount of 
acetic acid burning as identified by the carbon oxide production. However, 
the increase in bromine in the oxidation reaction mixture increases the 
amount of bromo-2,6-naphthalenedicarboxylic acids produced. However, as 
described hereinabove and as demonstrated subsequently, the method of this 
invention can be used to decrease the level of Br-2,6-NDA in the oxidation 
reaction product mixture. Also, when hydrogen is used, the 
bromo-2,6-naphthalenedicarboxylic acid is converted to 
2,6-naphthalenedicarboxylic acid. 
The following Examples 3-4 demonstrate the high temperature treatment of 
this invention. These Examples were conducted using crude 
2,6-naphthalenedicarboxylic acid made in a continuous, liquid phase 
oxidation process using acetic acid as a solvent and catalyzed by cobalt, 
manganese and bromine. This 2,6-naphthalenedicarboxylic acid contains most 
of the impurities and by-products expected to be found in an actual 
oxidation reaction effluent, but in somewhat lower concentrations. 
EXAMPLE 3 
Table III, Runs 1-6, were conducted in a 50 ml high pressure reactor fitted 
with an internal thermocouple and charged with the indicated solvents and 
crude 2,6-NDA having the composition listed in Table III. A wire mesh 
basket containing the catalyst as 0.5% Pd/carbon granules was inserted 
into the reactor. The catalyst had been previously heated in the solvent 
for 72 hours at 530.degree. F. to "age" it and impart more stability to 
the catalyst. Finally, the reactor was purged with hydrogen to remove the 
oxygen and pressurized with the indicated amount of hydrogen and sealed. 
The reactor was placed in a shaker device which agitated the reactor 
contents by shaking at 360 cycles/minute. While shaking, the reactor was 
partially immersed into a sand bath to attain the desired temperature as 
measured by the internal thermocouple. The shaking and reaction 
temperature was maintained for 30 minutes as indicated in Table III. After 
the reaction period, the reactor was withdrawn from the sand bath, cooled 
to room temperature, weighed to determine reactor integrity, and the 
entire reactor contents transferred to a dish for drying in a vacuum oven 
at 175.degree.-195.degree. F. The dry total product was mixed well for 
uniformity of sampling and analyzed. 
Runs 1-3 in Table III were conducted with 85% acetic acid and 15% water 
using various hydrogen pressures. This solvent ratio is similar to that 
expected in the oxidation reactor effluent. In all cases, 100% of the 
Br-2,6-NDA was converted, 62-72% of the TMLA, and 61-71% of the 2-FNA. The 
amount of 2-NA formed by decarboxylation of 2,6-NDA ranged from 0.0 to 
0.06 weight percent. The amount of dicarboxytetralin increased with 
increasing hydrogen pressure and ranged from 0.02 to 0.14%. Thus, high 
conversion of impurities was obtained along with low formation of 
by-products. The net increase in the normalized % 2,6-NDA indicates that 
some of the impurities (like Br-2,6-NDA) are being converted to 2,6-NDA. 
In Runs 4-6, a 50/50 mixture of acetic acid/water was used. The conversion 
of Br-2,6-NDA was 100% just as with the 85% acetic acid. The conversion of 
TMLA and 2-FNA was somewhat higher than with the 85% acetic acid. However, 
the amount of 2-NA and tetralin formed was greater than with the 85% 
acetic acid. 
EXAMPLE 4 
This run was made in a large, stirred, high-pressure reactor which was 
charged with the crude 2,6-NDA feedstock, 90% acetic acid/water, hydrogen 
and hydrogenation catalyst. Following the reaction period, the run was 
cooled to 300.degree. F. and filtered via a screen in the bottom of the 
reactor. The reactor containing the cake was then washed at 300.degree. F. 
with an additional 400 g of 90% acetic acid/water and the mother liquor 
removed by filtration was added to the first mother liquor. The results 
are reported in Table IV. 
The mother liquor and cake were both dried in a vacuum oven at 
175.degree.-195.degree. F., mixed for uniformity and analyzed by liquid 
chromatography for organic composition and by x-ray fluorescence 
spectroscopy for metals. The cake samples were analyzed by a Microtrak.TM. 
particle analyzer for particle size. The weights and compositions of the 
filtrate and cake were used to calculate the total product composition 
which is reported in Table IV as the "Combined Products." 
The cake composition indicates that a high purity 2,6-NDA product can be 
obtained by using the hydrogen/Pd/carbon treatment followed by 
conventional solid/liquid separation techniques. The "Combined Products" 
data indicates that there was an actual conversion of the TMLA, 
Br-2,6-NDA, and 2-FNA to other products allowing their removal from the 
cake. The composition of the filtrate indicates that the bulk of the 
metals and bromine are concentrated there for recycle to the oxidation 
reactor. In addition, the TMLA concentration in this stream is low due to 
conversion to TA and IA (included in "Others"). The particle size of the 
purified cake is much larger than that of the 2,6-NDA feedstock and 
contains fewer fines indicating that the purification process will make 
solid recovery easier. 
EXAMPLE 5 
To prove that the treatment of Br-2,6-NDA with hydrogen and Pd/carbon will 
result in the formation of 2,6-NDA, a run conducted with a feedstock 
comprised of high purity 2,6-NDA spiked with 4.3% Br-2,6-NDA (about 2-10 
times higher than normally obtained). After treatment for 10 minutes at 
600.degree. F., the total reaction mixture was dried and the dried product 
contained only 0.02% Br-2,6-NDA and the normalized 2,6-NDA content 
increased by 4.8% indicating a good balance between Br-2,6NDA loss and 
2,6-NDA appearance. No other major new components were detected in the 
product. This example supports the stated advantage of this invention as a 
method to sncrease 2,6-NDA yield while allowing greater flexibility in the 
oxidation step. The results are reported in Table V. 
EXAMPLE 6 
For this example, a total oxidation reactor effluent (TRE) obtained from a 
continuous oxidation reaction was used after cooling but without any 
separation, concentration, or dilution of the total oxidation reactor 
effluent. This TRE contained acetic acid/water as solvent and a solids 
content of about 25 wt. %. A sample of this TRE was dried in a vacuum oven 
and the solids had the composition indicated in Table VI. The TRE was 
charged to a 300 ml autoclave along with 0.5% Pd/carbon catalyst in a 
stainless steel basket. The autoclave was purged of oxygen with helium 
then pressurized to 300 psig with hydrogen. With stirring, the autoclave 
was heated rapidly to the indicated temperature and held at that 
temperature for the indicated time. At the end of the reaction period, the 
heating was stopped and the autoclave was allowed to cool to 400.degree. 
F. for about 30 minutes, then cooled rapidly to room temperature. The 
entire reactor contents were removed, the solvent evaporated in a vacuum 
oven at 185.degree. F., and the mixed solids analyzed by liquid 
chromatography. 
Run 1 at 600.degree. F. illustrates that high conversions of TMLA, 
Br-2,6-NDA and 2-FNA can be obtained in a short reaction time of 10 
minutes at 600.degree. F. using a fresh hydrogenation catalyst. This is 
true in spite of the high concentration of solids (25%) which might have 
prevented complete dissolution of all solids at one time. The crystallized 
product has a large mean particle size with few fines. Less than 20% of 
the bromine was lost as HBr although 90% of the Br-2,6-NDA was converted. 
No 2-NA formation by decarboxylation was detected. 
Run 2 was conducted at a lower temperature with a used catalyst and a 
longer reaction time. The results are similar to those in Run 1 with high 
TMLA and Br-2,6-NDA conversion but somewhat lower levels of 2-FNA 
conversion. There was lower bromine loss at the lower temperature. 
Operation at the lower temperature reduces reactor pressure and corrosion 
rates. However, complete dissolution of the solids was probably not 
obtained. For use in a fixed bed reactor, complete dissolution may be 
necessary to prevent plugging of the catalyst bed. 
In the following Examples 7-9, the same reactor was used as in Example 3, 
and the total reactor effluent (TRE) used in all of these Examples was 
obtained from the continuous oxidation of 2,6-dimethylnaphthalene to 
2,6-naphthalenedicarboxylic acid in acetic acid/water solvent catalyzed by 
cobalt, manganese and bromine. 
EXAMPLE 7 
Table VII provides the results from heating the TRE at a temperature 
ranging from 575.degree.-650.degree. F. for either 10 or 30 minutes, as 
indicated for Runs 1-6. Hydrogen was not used. The total reactor product 
was dried to remove the solvent and analyzed. The results indicate that 
trimellitic acid (TMLA) is largely converted to terephthalic acid (TA) and 
isophthalic acid (IA). In addition, the Br-2,6-NDA is converted and a 
large percentage of the 2-FNA is converted by the high temperature 
treatment. 
EXAMPLE 8 
Table VIII reports data for a series of high temperature treatment 
procedures without hydrogen wherein a hot filtration was used and the 
product filter cake was washed at 200.degree. F. with a mixture of 85% 
acetic acid and 15% water. These data demonstrate, that under a variety of 
conditions, the 2,6-naphthalenedicarboxylic acid produced by the method of 
this invention is greatly reduced in metals, TMLA, bromine and several of 
the organic impurities. Significantly, the particle size of the 
2,6-naphthalenedicarboxylic acid produced was considerably larger than the 
particle size of the 2,6-naphthalenedicarboxylic acid in the TRE starting 
material. 
EXAMPLE 9 
Table IX reports data for the results for the high temperature treatment 
according to the method of this invention wherein after the high 
temperature treatment the product 2,6-naphthalenedicarboxylic acid was 
filtered hot from the reactor, but no washing procedure was used. These 
data also demonstrate that the high temperature treatment facilitates 
removal of TMLA, Br-2,6-NDA and 2-FNA from the final product. 
Significantly, the "dry filtrate" which contains the bulk of the oxidation 
reaction catalyst metals contains low levels of TMLA which means that this 
material can be recycled to the oxidation reaction without adding 
undesirable TMLA. 
EXAMPLE 10 
Solubility data for 2,6-naphthalenedicarboxylic acid in distilled water and 
in acetic acid are provided below. 
______________________________________ 
Solubility 
Temperature (grams 2,6-NDA/100 g solvent) 
(.degree.C./.degree.F.) 
Water Acetic Acid Acetic Acid/Water* 
______________________________________ 
160/320 0.041 0.16 0.18 
200/392 0.22 0.44 0.59 
240/464 1.19 1.2 2.0 
280/536 6.07 3.1 4.5 
320/608 33.2 -- 10.8 
______________________________________ 
*85 wt. % acetic acid 
TABLE I 
______________________________________ 
Run # 
1 2 3 4 5 
______________________________________ 
Reaction Conditions 
Temperature (.degree.F.) 
415 385 410 410 410 
Co:Mn:Br Atom Ratio 
2:1:3.3 1:3:2 3:1:2 1:3:2 1:3:2 
Co (wt %).sup.a 
0.15 0.15 0.15 0.15 0.15 
Residence Time, 
44 112 71 44 110 
minutes 
Water (wt %).sup.a 
5 4 5 25 5 
Solvent/2,6-DMN 
6 6 6 6 6 
(wt).sup.b 
Reactor Yields 
(mole %) 
2,6-NDA 88 92 85 86 90 
TMLA 4.6 2.4 4.5 5.5 3.8 
Carbon Oxides 
8 6 11 2.6 9.1 
2-FNA 0.09 0.41 &lt;0.1 0.30 0.30 
______________________________________ 
.sup.a) Weight percent based on total solvent weight. 
.sup.b) Weight ratio of total solvent to 2,6dimethylnaphthalene feed. 
TABLE II 
______________________________________ 
Run # 
1 2 3 4 5 6 
______________________________________ 
Reaction 
Conditions 
Temperature 
390 390 400 400 410 400 
(.degree.F.) 
Co:Mn:Br 1:3:2 1:3:2 1:3:2 1:3:2 1:3:2 1:3:3 
Atom Ratio 
Co (wt %).sup.a 
0.10 0.125 0.125 0.125 0.125 0.125 
Residence 
50 64 57 59 57 56 
Time, minutes 
Water 5 5 5 10 10 10 
(wt %).sup.a 
Solvent/ 6 5 4 4 4 4 
2,6-DMN 
(wt %).sup.b 
Reactor 
Yields 
(mole %) 
2,6-NDA 91 91 91 89 89 86 
TMLA 4.2 4.1 3.4 4.0 4.1 3.8 
Carbon 3.0 2.7 3.8 3.1 3.1 2.1 
Oxides 
2-FNA 0.52 0.58 0.42 0.55 0.37 0.53 
Br-2,6-NDA 
0.12 0.14 0.23 0.47 0.43 0.92 
______________________________________ 
.sup.a) Weight percent based on total solvent weight. 
.sup.b) Weight ratio of total solvent to 2,6dimethylnaphthalene feed. 
TABLE III 
__________________________________________________________________________ 
2,6-NDA 
Run # 
Feed.sup.a 
1 2 3 4 5 6 
__________________________________________________________________________ 
Reactor Charge 
2,6-NDA (g) 4.00 4.01 4.00 4.00 4.00 4.00 
Solvent Used (wt. % Acetic 
85/15 85/15 85/15 50/50 50/50 50/50 
Acid/wt. % Water) 
Solvent Wt. (g) 20.0 20.0 20.0 20.0 20.0 20.0 
Catalyst Used.sup.b 0.5 0.5 0.5 0.5 0.5 0.5 
wt. % Pd/C 
wt. % Pd/C 
wt. % Pd/C 
wt. % Pd/C 
wt. % Pd/C 
wt. % Pd/C 
Catalyst Wt. (g) 0.43 0.43 0.43 0.42 0.42 0.42 
Catalyst Previous Uses 
2 0 1 2 0 1 
Conditions 
Temperature (.degree.F.) 
600 600 600 600 600 600 
Time from 100.degree. F. to Reaction 
2:05 2:10 2:30 1:50 1:50 2:00 
Temp. (min.) 
Reaction Time (min.) 30 30 30 30 30 30 
Shaking Speed (cpm) 360 360 360 360 360 360 
Hydrogen Pressure at 70.degree. F. 
15 30 100 15 30 100 
(psig) 
Product Weight (g).sup.c 
24.20 24.29 24.26 23.96 24.17 24.19 
Wt. % Reactor Loss (g) 
3.20 2.84 2.96 4.16 3.32 3.24 
Dry Down Weight (g) 3.98 3.94 3.95 4.00 3.99 3.93 
Product Analysis (Wt. %) 
2,6-NDA 90.06 
91.98 88.01 89.21 92.64 89.24 89.45 
2,7-NDA 0.01 0.00 0.01 0.01 0.00 0.01 0.01 
TMLA 2.19 0.60 0.70 0.82 0.15 0.33 0.60 
C.sub.8 Acids 0.02 1.15 0.98 0.79 1.35 1.31 1.16 
Br-2,6-NDA 0.59 0.00 0.00 0.00 0.00 0.00 0.00 
2-FNA 0.30 0.10 0.08 0.12 0.08 0.04 0.08 
2,6-Methyl-NA.sup.d 
0.01 0.06 0.07 0.07 0.06 0.07 0.08 
2-NA 0.00 0.00 0.06 0.06 0.00 0.10 0.10 
Dicarboxytetralin 
0.00 0.02 0.05 0.14 0.05 0.16 0.36 
Others 0.39 0.42 0.25 0.31 0.35 0.17 0.21 
Total 93.55 
94.32 90.23 91.52 94.68 91.43 92.05 
Normalized % 2,6-NDA 
96.3 97.5 97.5 97.5 97.8 97.6 97.2 
Weight % Conversion 
TMLA 72.5 67.9 62.4 93.0 84.9 72.5 
Br-2,6-NDA 100.0 100.0 100.0 100.0 100.0 100.0 
2-FNA 67.5 71.5 61.0 71.9 86.5 72.4 
__________________________________________________________________________ 
.sup.a Contained (Wt. %): Cobalt (0.125), manganese (0.75), bromine 
(0.373). Particle size of 20.9 (mean) and 24% less than 11 microns. 
.sup.b 0.5 Weight percent palladium on carbon support 
.sup.c Weight of total reactor effluent 
.sup.d 2Methyl-6-naphthoic acid 
TABLE IV 
______________________________________ 
Run # 
______________________________________ 
Reactor Charge 
2,6-NDA.sup.a (g) 200 
Solvent Used (wt. %. Acetic acid/wt. %. water) 
(90/10) 
Solvent Wt. (g) 1005 
Catalyst Used 0.5% 
Pd/Carbon 
Catalyst Wt. (g) 4.5 
Catalyst Prior Uses 0 
Conditions 
Temperature (.degree.F.) 595 
Pressure (psig) 970 
Residence Time (min) 120 
Hydrogen Pressure at Room Temp. (psig) 
50 
______________________________________ 
Combined 
Cake Filtrate Products 
______________________________________ 
Wt. % of Total 88.8 11.20 
Product Analysis (Wt. %) 
2,6-NDA 94.54 22.49 86.47 
2,7-NDA 0.00 0.16 0.02 
TMLA 0.00 0.27 0.03 
Br-2,6-NDA 0.03 0.03 0.03 
2-FNA 0.01 0.19 0.03 
2-NA 0.00 1.74 0.20 
Others 0.37 25.75 3.21 
Total 94.95 50.63 89.98 
Normalized %, 2,6-NDA 
99.57 44.42 96.10 
Metal Analysis (Wt. %) 
Cobalt 0.01 0.80 0.10 
Manganese 0.08 5.50 0.69 
Bromine 0.03 2.82 0.34 
Wt. % Conversions 
TMLA 98.6 
Br-2,6-NDA 95.2 
2-FNA 88.5 
% Loss of Bromine 8.1 
Particle Size 
Mean (microns) 179 
% &lt;11 microns 0.3 
______________________________________ 
.sup.a Same 2,6NDA as reported in Table III. Mean particle size of 20.9 
microns and 24 wt. percent of particles less than 11 microns. 
TABLE V 
______________________________________ 
2,6-NDA Feed.sup.a 
Example 
______________________________________ 
Reactor Charge 
2,6-NDA.sup.a (g) 5.0 
Solvent Used (wt. % Acetic Acid/ 
0/100 
wt. % Water 
Solvent Weight (g) 25.0 
Catalyst Used 
Catalyst Weight (g) 0.49 
Catalyst Previous Uses 6 
Conditions 
Temperature (.degree.F.) 600 
Pressure (psig) 1600 
Residence Time (min.) 10 
Hydrogen Pressure at Room 50 
Temperature (psig) 
Dry Product Analysis (wt %) 
2,6-NDA 89.83 91.93 
2,7-NDA 0.00 0.00 
TMLA 0.00 0.00 
Br-2,6-NDA 4.30 0.02 
2-FNA 0.00 0.00 
2-NA 0.00 0.13 
Others.sup.b 1.95 1.49 
Total 93.08 93.57 
Normalized %, 2,6-NDA 
93.49 98.25 
Metals Analysis (wt %) 
Cobalt 0 
Manganese 0 
Wt. Conversion 
Br-2,6-NDA 99.5 
______________________________________ 
.sup.a Used pure 2,6NDA obtained by hydrolyzing highly pure 
dimethyl2,6-naphthalenedicarboxylate. 
.sup.b Impurities are monomethyl and dimethyl2,6-naphthalenedicarboxylate 
TABLE VI 
______________________________________ 
2,6-NDA 
Run # 
Feed.sup.a 
1 2 
______________________________________ 
Reactor Charge 
2,6-NDA (g) 31.1 32.1 
Solvent Used (wt. % Acetic 
85/15 85/15 
Acid/wt. % Water) 
Solvent Wt. (g) 88.8 91.6 
Catalyst Used 0.5% Pd/C 0.5%/Pd/C 
Catalyst Weight (g) 1.96 1.60 
Catalyst Previous Uses 0 4 
Conditions 
Temperature (.degree.F.) 600 570 
Pressure (psig) 1070 840 
Residence Time (min.) 10 30 
Hydrogen Pressure at Room 
300 300 
Temperature (psig) 
Dry Product Analysis 
(wt %) 
2,6-NDA 83.76 79.35 79.01 
2,7-NDA 0.00 0.01 0.01 
TMLA 2.26 0.12 0.61 
Br-2,6-NDA 1.84 0.19 0.24 
2-FNA 0.42 0.09 0.15 
2-NA 0.25 0.06 0.35 
Others 2.39 2.93 3.14 
Total 90.92 82.75 83.51 
Normalized %, 2,6-NDA 
92.12 95.90 94.62 
Metals Analysis (wt %) 
Cobalt 0.68 0.57 0.67 
Manganese 1.86 1.62 1.88 
Bromine 1.84 1.51 1.76 
Wt. % Conversions 
TMLA 94.6 73.1 
Br-2,6-NDA 90.0 86.9 
2-FNA 78.4 63.8 
% Loss of Bromine 17.9 4.3 
Particle Size 
Mean (microns) 263 -- 
% &lt;11 (microns) 0.4 -- 
______________________________________ 
TABLE VII 
__________________________________________________________________________ 
Starting Oxidation 
Run # 
Reaction Mixture.sup.a 
1 2 3 4 5 6 
__________________________________________________________________________ 
Conditions 
Temperature (.degree.F.) 575 600 650 575 600 650 
Residence Time (minutes) 10 10 10 30 30 30 
Shaking Speed (rpm) 360 360 360 360 360 360 
Analysis of Product 
Weight of Product (g) 20.14 
20.13 
20.09 
20.04 
20.23 
20.06 
Weight Loss (gain) % (0.70) 
(0.65) 
(0.45) 
(0.20) 
(1.15) 
(0.30) 
Dry Down Weight (g) 5.16 
5.13 
5.15 
5.19 
5.19 
5.19 
Mass Recovery (%) 99.7 
99.1 
99.5 
100.3 
100.2 
100.3 
Analysis of Dry Product (wt %) 
TMLA.sup.b 2.45 1.27 
0.21 
0.00 
0.37 
0.00 
0.00 
TA.sup.c 0.13 0.49 
0.71 
0.84 
0.71 
0.78 
0.83 
IA.sup.d 0.00 0.39 
0.67 
0.94 
0.72 
0.82 
0.83 
2,6-NDA 87.40 86.99 
88.51 
87.12 
84.63 
87.19 
86.90 
2,7-NDA 0.00 0.00 
0.01 
0.01 
0.01 
0.01 
0.01 
Br-2,6-NDA 1.74 0.50 
0.20 
0.09 
0.15 
0.13 
0.06 
2-FNA 0.38 0.29 
0.19 
0.09 
0.24 
0.09 
0.17 
2-NA 0.12 0.22 
0.26 
0.57 
0.22 
0.50 
0.63 
Others 2.51 1.74 
1.99 
3.65 
1.65 
2.67 
3.48 
Total 94.74 91.88 
92.75 
93.30 
88.70 
92.17 
92.91 
Metals & Bromine Analysis (wt %) 
Bromine 1.75 1.59 
1.46 
1.55 
1.47 
1.51 
1.55 
Cobalt 0.66 0.62 
0.57 
0.62 
0.57 
0.61 
0.61 
Manganese 1.81 1.70 
1.57 
1.73 
1.62 
1.70 
1.70 
% Conversion (wt) 
TMLA 48.3 
91.3 
100.0 
84.9 
100.0 
100.0 
Br-2,6-NDA 71.4 
88.7 
94.6 
91.7 
92.8 
96.4 
2-FNA 24.0 
51.6 
77.6 
36.7 
77.1 
56.8 
__________________________________________________________________________ 
.sup.a The oxidation reaction mixture used for these runs was obtained 
from the continuousmode, liquid phase oxidation of 2,6dimethylnaphthalene 
The charge of oxidation reaction mixture for each run weighed 20 grams an 
had the following analyses: 5.17 g of crude 2,6NDA, 25.9 wt % solids, 
14.83 of liquid components and the liquid phase was 85 wt. % acetic acid 
and 15 wt. % water. 
.sup.b Values are +/- 0.40. 
.sup.c Terephthalic Acid 
.sup.d Isophthalic Acid 
TABLE VIII 
__________________________________________________________________________ 
Starting Oxid. 
Run # 
Mixture.sup.a 
1 2 3 4 5 6 7 8 9 10 
__________________________________________________________________________ 
Reaction Conditions 
Diluent.sup.b none none 
none 
none 
none 
none 
A A A W A 
Wt % Solids Present 26 26 26 26 17 17 17 17 10 
Temperature (.degree.F.) 570 
570 
600 
600 
600 
600 
625 
600 
600 
Pressure (psig) 800 
800 
1000 
1000 
1000 
1000 
1000 
1300 
1000 
Time (minutes) 15 60 15 60 15 60 15 15 15 
After Hot Filtration at 200.degree. F. 
none 
Wt % Solids Lost to Filtrate 
8.3 
10.7 
10.4 
12.3 
11.7 
11.5 
14.3 
12.9 
13.1 
14.1 
Wt % Liquid on Filter Cake 
40 23 23 27 25 10 28 13 25 35 
Analysis of Dry Product.sup.c (wt %) 
TMLA.sup.d 2.43 0.60 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
TA 0.13 0.01 
0.19 
0.21 
0.18 
0.18 
0.07 
0.09 
0.09 
0.03 
0.04 
IA 0.00 0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
2,6-NDA 87.27 94.91 
97.62 
97.40 
96.31 
94.21 
97.10 
96.12 
95.07 
98.08 
96.96 
2,7-NDA 0.00 0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
0.00 
Br-2,6-NDA 1.75 1.20 
0.31 
0.27 
0.30 
0.21 
0.34 
0.19 
0.19 
0.00 
0.10 
2-FNA 0.39 0.25 
0.10 
0.07 
0.09 
0.05 
0.14 
0.06 
0.08 
0.13 
0.08 
2NA 0.13 0.00 
0.03 
0.04 
0.04 
0.10 
0.00 
0.00 
0.02 
0.00 
0.00 
Other Impurities 2.38 0.60 
0.71 
0.56 
0.50 
0.54 
0.77 
0.65 
0.61 
0.70 
0.58 
Total 94.98 97.56 
98.95 
98.56 
97.42 
95.28 
98.42 
97.10 
96.06 
98.93 
97.76 
Normalized 2,6-NDA (wt. %) 
92.37 97.28 
98.66 
98.83 
98.86 
98.88 
98.66 
98.99 
98.97 
99.14 
99.18 
Metals & Bromine Analysis (wt %) 
Cobalt 0.68 0.02 
0.00 
0.00 
0.00 
0.02 
0.01 
0.01 
0.01 
0.01 
0.01 
Manganese 1.83 0.26 
0.02 
0.02 
0.01 
0.05 
0.02 
0.03 
0.04 
0.02 
0.02 
Bromine 1.69 0.49 
0.14 
0.17 
0.16 
0.15 
0.20 
0.13 
0.17 
0.07 
0.11 
TMLA 75 100 
100 
100 
100 
100 
100 
100 
100 
100 
Br-2,6-NDA 32 83 84 83 88 81 89 89 100 
94 
2-FNA 36 76 81 76 87 65 85 79 68 79 
Other Impurities 75 70 76 79 77 68 73 74 71 76 
Cobalt 97 &gt;99 
&gt;99 
&gt;99 
98 99 99 98 99 99 
Manganese 86 99 99 99 97 99 98 98 99 99 
Bromine 71 91 90 91 91 88 92 90 96 94 
Particle Size After Hot Filtration 
Mean (microns) 61 22 212 
140 
179 
159 
200 
262 
142 
217 
143 
% Fine &lt;11 microns 
18 20 10 12 12 9 6 8 11 0 4 
__________________________________________________________________________ 
.sup.a Oxidation reaction mixture used for these runs was obtained from a 
continuous oxidation of 2,6dimethylnaphthalene. The mixture contained 26 
wt. % solids in an 85 wt. % acetic acid/15 wt. % water mixture. 
.sup.b W = Water, A = 85 wt. % acetic acid/15 wt. % water. 
.sup.c After hot filtration, solid filter cake was washed with an 85 wt. 
acetic acid/15% wt. water mixture at 200.degree. F. The amount of wash 
solvent was twice the weight of the filter cake. 
.sup.d Values are +/-0.10. 
TABLE IX 
__________________________________________________________________________ 
Starting Mixture.sup.a 
Run # 
(Feedstock) 
1.sup.b 2.sup.b 3.sup.b 4.sup.b 
__________________________________________________________________________ 
Reaction Conditions.sup.a none.sup.d 
Temperature (.degree.F.) 600 600 625 
Residence Time (minutes) 15 15 15 
Cooling Rate (.degree.F./minute to 550.degree. F.) 
6.3 2.5 7.9 
Weight Percent 
Solvent in Wet Cake 34.3 10 16 13 
Product in Filtrate 8.2 11.5 12.0 12.9 
Mass Balance 99.4 99.0 97.4 100.3 
Total Solvent on Cake 10.2 2.5 4 3.3 
Solids in Feed to Filter 17.6 20.2 19.3 19.5 
__________________________________________________________________________ 
Analysis of Dry Feedstock 
Starting Mixture.sup.a 
1 2 3 4 
Solids, Filter Cake, and Filtrate 
(Feedstock) 
Cake 
Filtrate 
Cake 
Filtrate 
Cake 
Filtrate 
Cake 
Filtrate 
__________________________________________________________________________ 
Metals and Bromine (wt %) 
Br 1.84 0.64 
12.10 
0.34 
9.20 0.32 
9.90 0.22 
9.3 
Co 0.68 0.10 
6.00 0.08 
3.75 0.06 
4.10 0.05 
3.88 
Mn 1.86 0.60 
14.00 
0.21 
11.30 
0.17 
12.10 
0.12 
11.4 
Organic Compounds (wt %) 
TMLA.sup.e 2.26 1.24 
9.65 0.00 
0.68 0.00 
0.36 0.00 
0.03 
TA 0.00 0.03 
1.58 0.18 
6.75 0.15 
7.18 0.16 
6.08 
IA 0.00 0.00 
0.00 0.00 
7.24 0.00 
7.29 0.00 
6.97 
2,6-NDA 83.76 87.34 
2.06 94.89 
4.80 98.23 
4.02 86.75 
3.64 
Br-2,6-NDA 1.84 1.17 
4.79 0.35 
0.01 0.27 
0.00 0.16 
0.03 
2-FNA 0.42 0.20 
1.05 0.15 
0.78 0.15 
0.31 0.11 
0.49 
2-NA 0.25 0.00 
1.72 0.00 
2.64 0.00 
2.69 0.00 
3.20 
Others 2.39 0.80 
22.71 
0.91 
14.61 
0.96 
16.81 
1.05 
15.78 
Total 90.92 90.78 
43.56 
96.48 
37.50 
99.77 
38.66 
88.23 
36.19 
Normalized 2,6-NDA (wt %) 
92.12 96.21 
4.73 98.35 
12.81 
98.46 
10.38 
98.32 
10.05 
__________________________________________________________________________ 
Run # 
Starting Mixture 
1 2 3 4 
__________________________________________________________________________ 
Particle Size of Cake Sample 
Mean (microns) 24.sup.f 200.sup.g 
166.sup.g 
142.sup.g 
(% &lt;11 microns) 20.sup.f 6.2.sup.g 
13.7.sup.g 
11.3.sup.g 
Filter Cake Analysis 
(wt % Removal of Impurities 
Relative to Feedstock 
Br 65.2 81.5 82.8 87.9 
Co 85.3 88.8 90.7 93.4 
Mn 67.7 88.8 90.7 93.4 
TMLA 45.2 100.0 100.0 100.0 
2,6-NDA 0.2 0.6 0.5 0.5 
Br-2,6-NDA 36.4 81.2 85.3 91.3 
FNA 52.5 63.8 63.8 73.9 
2-NA 100.0 100.0 100.0 100.0 
Others 66.4 61.8 59.7 56.0 
Total Product Accountability 
(Cake and Filtrate) % Converted 
(or Lost) From Feedstock 
TMLA 14.8 96.5 98.1 99.8 
Br-2,6-NDA 20.3 83.3 87.1 92.2 
2-FNA 35.8 46.5 59.1 62.1 
Br 14.1 26.1 20.3 24.2 
Mn 8.7 20.2 13.8 15.2 
Co 14.1 26.7 19.5 20.6 
__________________________________________________________________________ 
.sup.a See footnote a) Table VIII 
.sup.b Sample Filtered hot at 200.degree. F. Filter cake was not washed t 
simulate operating with a "solid bowl" centrifuge. 
.sup.c Starting mixture for Runs 1-4 was diluted to a 5:1 weight ratio of 
liquid to solids. A mixture of 85% acetic acid and 15% water (wt) was use 
for the dilution. 
.sup.d No heating at elevated temperature only hot filtration of diluted 
oxidation reaction mixture. 
.sup.e Values are +/- 0.10. 
.sup.f Centrifuged solids from untreated starting mixture. 
.sup.g Cake sample. 
Only certain embodiments of the invention have been set forth and 
alternative embodiments and various modifications will be apparent from 
the above description to those skilled in the art. These and other 
alternatives are considered equivalents and within the spirit and scope of 
the present invention.