CA2505976A1 - Process for the purification of a crude carboxylic acid slurry - Google Patents
Process for the purification of a crude carboxylic acid slurry Download PDFInfo
- Publication number
- CA2505976A1 CA2505976A1 CA002505976A CA2505976A CA2505976A1 CA 2505976 A1 CA2505976 A1 CA 2505976A1 CA 002505976 A CA002505976 A CA 002505976A CA 2505976 A CA2505976 A CA 2505976A CA 2505976 A1 CA2505976 A1 CA 2505976A1
- Authority
- CA
- Canada
- Prior art keywords
- carboxylic acid
- slurry
- product
- zone
- solid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/487—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to chemical modification
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Disclosed is a process to produce a purified carboxylic acid product. The process comprises removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product. The slurry product if further treated in a staged oxidation zone and a crystallization zone to fro m a crystallized product. The crystallized product is further cooled in a cooling zone and subsequently filtered and dried in a filtration and drying zone. The process produces purified carboxylic acid product having good colo r and low impurity levels without the use of purification steps like hydrogenation.
Description
PROCESS FOR THE PURIFICATION OF A CRUDE CARBOXYLIC ACID
SLURRY
FIELD OF~ INVENTION
The present invention relates to a process for the purification of a crude carboxylic acid slurry. More specifically, the present invention relates to a process for the purification of a crude carboxylic acid slurry by utilizing a solid-liquid displacement zone between a primary oxidation zone and a staged oxidation zone.
BACKGROUND OF THE INVENTION:
Terephthalic acid is commercially produced by oxidation of paraxylene in the presence of a catalyst, such as, for example, Co, Mn, Br and a solvent. Terephthalic acid used in the production of polyester fibers, films, and resins must be further treated to remove impurities present due to the oxidation of para-xylene. Typical commercial process produce,a crude terephthalic acid then dissolve the solid crude terephthalic acid in water at high temperatures and pressures, hydrogenate the resultant solution, cool and crystallize the terephthalic acid product out of solution, and separate the solid terephthalic product from the liquid as discussed in U.S. Patent No. 3,584,039 herein incorporated by reference.
SLURRY
FIELD OF~ INVENTION
The present invention relates to a process for the purification of a crude carboxylic acid slurry. More specifically, the present invention relates to a process for the purification of a crude carboxylic acid slurry by utilizing a solid-liquid displacement zone between a primary oxidation zone and a staged oxidation zone.
BACKGROUND OF THE INVENTION:
Terephthalic acid is commercially produced by oxidation of paraxylene in the presence of a catalyst, such as, for example, Co, Mn, Br and a solvent. Terephthalic acid used in the production of polyester fibers, films, and resins must be further treated to remove impurities present due to the oxidation of para-xylene. Typical commercial process produce,a crude terephthalic acid then dissolve the solid crude terephthalic acid in water at high temperatures and pressures, hydrogenate the resultant solution, cool and crystallize the terephthalic acid product out of solution, and separate the solid terephthalic product from the liquid as discussed in U.S. Patent No. 3,584,039 herein incorporated by reference.
A number of processes for producing the purified terephthalic acid solid have been developed and are commercially available. Usually, the purified terephthalic acid solid is produced in a multi-step process wherein a crude terephthalic acid is produced. The crude terephthalic acid does not have sufficient quality for direct use as starting material in commercial polyethylene terephthalate(PET). Instead, the crude terephthalic acid is usually refined to purified terephthalic acid solid.
Liquid phase oxidation of p-xylene produces crude terephthaiic acid.
The crude terephthalic acid is dissolved in water and hydrogenated for the purpose of converting 4-carboxybenzaldehyde to p-toluic acid, which is a more water-soluble derivative, and for the purpose of converting characteristically yellow compounds to colorless derivatives. Significant 4-carboxybenzaldehyde and p-toluic acid in the firial purified terephthalic acid product is particularly detrimental to polymerization processes as they may act as chain terminators during the condensation reaction between terephthalic acid and ethylene glycol in the production of PET. Typical purified terephthalic acid contains on a weight basis less than 250 parts per million (ppm) 4-carboxybenzaldehyde and less than 150 ppm p-toluic acid.
The crude terephthalic acid typically contains on a weight basis from about 800 to 7,000 parts per million (ppm) 4-carboxybenzaldehyde and about 200 to 1,500 ppm p-toluic acid as the main impurities. The crude terephthalic acid also contains lesser amounts, about 20-200 ppm range, of aromatic compounds having the structures derived from benzil, fluorenone, and/or anthraquinone, which are characteristically yellow compounds as impurities resulting from coupling side reactions occurring during oxidation of p-xylene Such a purification process typically comprises adding water to the crude terephthalic acid to form a crude terephthalic acid slurry, which is heated to dissolve the crude terephthalic acid. The crude terephthalic acid solution is then passed to a reactor zone in which the solution is contacted with hydrogen in the presence of a heterogeneous catalyst at temperatures of about 200° to about 375° G. This reduction step converts the various color causing compounds present in the crude terephthalic acid to colorless derivatives. The principal impurity, 4-carboxybenzaldehyde, is converted to p-toluic acid.
Typical crude terephthalic acid contains excessive amounts of both 4-carboxybenzaldehyde and p-toluic acid on aweight basis. Therefore, to achieve less than 250 ppmv~i 4-carboxybenzafdehyde and less than 150 ppmw p-toluic acid in the purified terephthalic acid requires mechanisms for purifying the crude terephthalic acid and removing the contaminants.
!n many processes, colored impurities are hydrogenated to colorless derivatives and leave the process with the terephthalic acid solid product and waste water streams. However, one embodiment of this invention provides an attractive process to produce a purified carboxylic acid slurry by utilizing a solid-liquid displacement zone comprising a solid-liquid separator after oxidation of a crude carboxylic acid slurry product and prior to final filtration and drying without the use of an hydrogenation step.
SUMMARY OF THE INVENTION
In one embodiment of the invention, a process to produce the purified carboxylic acid product is provided without the use of hydrogenation of the terephthalic acid or a process separating impurities from oxidation 19 solvent as disclosed in U.S. patent #3,584,039.
In another embodiment of this invention, a process to produce a slurry product is provided. The process comprises removing impurities .from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product.
In another embodiment of this invention, a process to produce a purified carboxylic acid product is provided. The process comprises:
(a) removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product;
(b) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product;
(c) crystallizing the staged oxidation product in a crystallization zone to forma crystallized product.
Liquid phase oxidation of p-xylene produces crude terephthaiic acid.
The crude terephthalic acid is dissolved in water and hydrogenated for the purpose of converting 4-carboxybenzaldehyde to p-toluic acid, which is a more water-soluble derivative, and for the purpose of converting characteristically yellow compounds to colorless derivatives. Significant 4-carboxybenzaldehyde and p-toluic acid in the firial purified terephthalic acid product is particularly detrimental to polymerization processes as they may act as chain terminators during the condensation reaction between terephthalic acid and ethylene glycol in the production of PET. Typical purified terephthalic acid contains on a weight basis less than 250 parts per million (ppm) 4-carboxybenzaldehyde and less than 150 ppm p-toluic acid.
The crude terephthalic acid typically contains on a weight basis from about 800 to 7,000 parts per million (ppm) 4-carboxybenzaldehyde and about 200 to 1,500 ppm p-toluic acid as the main impurities. The crude terephthalic acid also contains lesser amounts, about 20-200 ppm range, of aromatic compounds having the structures derived from benzil, fluorenone, and/or anthraquinone, which are characteristically yellow compounds as impurities resulting from coupling side reactions occurring during oxidation of p-xylene Such a purification process typically comprises adding water to the crude terephthalic acid to form a crude terephthalic acid slurry, which is heated to dissolve the crude terephthalic acid. The crude terephthalic acid solution is then passed to a reactor zone in which the solution is contacted with hydrogen in the presence of a heterogeneous catalyst at temperatures of about 200° to about 375° G. This reduction step converts the various color causing compounds present in the crude terephthalic acid to colorless derivatives. The principal impurity, 4-carboxybenzaldehyde, is converted to p-toluic acid.
Typical crude terephthalic acid contains excessive amounts of both 4-carboxybenzaldehyde and p-toluic acid on aweight basis. Therefore, to achieve less than 250 ppmv~i 4-carboxybenzafdehyde and less than 150 ppmw p-toluic acid in the purified terephthalic acid requires mechanisms for purifying the crude terephthalic acid and removing the contaminants.
!n many processes, colored impurities are hydrogenated to colorless derivatives and leave the process with the terephthalic acid solid product and waste water streams. However, one embodiment of this invention provides an attractive process to produce a purified carboxylic acid slurry by utilizing a solid-liquid displacement zone comprising a solid-liquid separator after oxidation of a crude carboxylic acid slurry product and prior to final filtration and drying without the use of an hydrogenation step.
SUMMARY OF THE INVENTION
In one embodiment of the invention, a process to produce the purified carboxylic acid product is provided without the use of hydrogenation of the terephthalic acid or a process separating impurities from oxidation 19 solvent as disclosed in U.S. patent #3,584,039.
In another embodiment of this invention, a process to produce a slurry product is provided. The process comprises removing impurities .from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product.
In another embodiment of this invention, a process to produce a purified carboxylic acid product is provided. The process comprises:
(a) removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product;
(b) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product;
(c) crystallizing the staged oxidation product in a crystallization zone to forma crystallized product.
In another embodiment of this invention, a process to produce a purified carboxylic acid slurry is provided. The process comprises:
(a) ~ removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein the crude carboxylic acid siurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(b) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product; wherein the oxidizing is conducted at a temperature between about 190°C to about 2~0 °C; and wherein the oxidizing is at a higher temperature in the staged oxidation zone than in the primary oxidation zone;
(c) crystallizing the staged oxidation product in a crystallization zone to form a crystallized product;
(d) cooling the crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (e) filtering and optiorially drying the cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from the cooled carboxylic acid slurry to produce the purified carboxylic acid product.
In yet another embodiment of this invention, a process to produce a purified carboxylic acid product is. provided. The process comprises:
(a) ~ removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein the crude carboxylic acid siurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(b) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product; wherein the oxidizing is conducted at a temperature between about 190°C to about 2~0 °C; and wherein the oxidizing is at a higher temperature in the staged oxidation zone than in the primary oxidation zone;
(c) crystallizing the staged oxidation product in a crystallization zone to form a crystallized product;
(d) cooling the crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (e) filtering and optiorially drying the cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from the cooled carboxylic acid slurry to produce the purified carboxylic acid product.
In yet another embodiment of this invention, a process to produce a purified carboxylic acid product is. provided. The process comprises:
(a) oxidizing an aromatic feed stock in a primary oxidation zone to form a crude carboxylic acid slurry; wherein the crude carboxylic acid slurry comprises terephthalic acid; wherein the oxidizing is conducted at a temperature between about 120°C to about 190 °C;
(b) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein the crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(c) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product; wherein the oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein the oxidizing is at a higher temperature in the staged oxidation zone than in the primary oxidation zone;
(d) crystallizing the staged oxidation product in a crystallization zone to form a crystallized product;
(e) cooling the crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (f) filtering and optionally drying the cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from the cooled carboxylic acid slurry to produce the purified carboxylic acid product.
These objects, and other objects, will become more apparent to others with ordinary skill in the art after reading this disclosure.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic of the inventive process for the oxidative purification of carboxylic acid wherein a solid-liquid displacement zone 40 is utilized between the primary oxidation zone 20 and the staged oxidation zone 80.
DETAILED DESCRIPTION OF THE INVENTION
The present invention provides a process for the purification of a 1 ~ crude carboxylic acid slurry 30. The process comprises the steps of displacing a mother liquor from the crude carboxylic acid slurry in a solid-liquid displacement zone 40 to form a slurry product 70.
Crude terephthalic acid is conventionally made via the liquid phase air oxidation of paraxylene in the presence of a suitable oxidation catalyst.
Suitable catalysts comprises at least one selected from, but are not limited to, cobalt, bromine and manganese compounds, which are soluble in the selected solvent. Suitable solvents include, but are not limited to, aliphatic mono-carboxylic acids, preferably containing 2 to 6 carbon atoms, or _g_ benzoic acid and mixtures thereof and mixtures of these compounds with water. Preferably the solvent is acetic acid mixed with water, in a ratio of about 5:1 to about 25:1, preferably befiveen about 8:1 and about 20:1.
Throughout the specification acetic acid will be referred to. as the solvent.
However, it should be appreciated that other suitable solvents, such as those disclosed previously, may also be utilized. Patents disclosing the production of terephthalic acid such as U.S patent #4,158,738 and #3,996,271 are hereby incorporated by reference.
In an embodiment of this invention, a process to produce slurry product 70 is provided in Figure 1. The process comprises removing impurities from a crude carboxylic acid slurry 30 in.a solid-liquid displacement zone 40 to form a slurry. product 70; wherein the slurry product 70 is formed without a hydrogenation step..' The solid-liquid displacement zone 40, impurities, crude carboxylic acid slurry 30, and slurry product 70 are all described subsequently in this disclosure.
In another embodiment of this invention a process to produce a purified carboxylic acid product 230 is provided in Figure 1. The process comprises:
Step (a) comprises removing impurities from a crude carboxylic acid slurry 30 in an solid-liquid displacement zone 40 to form a slurry. product 70;
A crude carboxylic acid slurry 30 comprises at least one carboxylic acid, catalyst, at least one solvent, and impurities is withdrawn via like 30.
The impurities typically comprise at least one or more of the following compounds: 4-carboxybenzaldehyde(4-CBA), trimellitic acid(TMA), and 2,6-dicarboxyfluorenone(2,6-DCF). The solvent typically comprises acetic acid, but can be any solvent that has been previously mentioned.
The crude carboxylic acid slurry 30 is produced by oxidizing in a primary oxidation zone 20 an aromatic feed stock 10. In one embodiment, the aromatic feedstock comprises paraxylene. The primary oxidation zone 20 comprises at least one oxidation reactor, and the crude carboxylic acid slurry 30 comprises at least one carboxylic acid. The oxidation reactor can be operated at temperatures between about 120°C to about 200°C, preferably about 140°C to about 170°C. Typically the aromatic feed stock 10 is paraxylene and the carboxylic acid is terephthalic acid. In one embodiment of the invention the primary oxidation gone comprises a bubble column.
Therefore, when terephthalic acid is utilized, the crude carboxylic acid slurry 30 would be referred to as crude terephthalic acid slurry and the purified carboxylic acid product 230 would be referred to as a purified terephthalic acid product.
Carboxylic acids include aromatic carboxylic acids produced via controlled oxidation of an organic substrate. Such aromatic carboxylic acids include compounds with at least one carboxylic acid group attached to a carbon atom that is part of an aromatic ring, preferably having at least 6 carbon atoms, even more preferably having only carbon atoms. Suitable examples of such aromatic rings include, but are not limited to, benzene, biphenyl, terphenyl, naphthalene, and other carbon-based fused aromatic rings. Examples of suitable carboxylic acids include, but are not limited to, terephthalic acid, benzoic acid, p-toluic, isophthalic acid, trimellitic acid, naphthalene dicarboxylic acid, and 2,5-diphenyl-terephthalic acid. Each of the embodiments of this invention can be practiced wherein there is a substantial absence of terephthalic acid and isophthalic acid in the crude carboxylic acid slurry. When the term substantial absence is used it means less than 5% by weight.
Crude terephthalic acid slurry is conventionally synthesized via the liquid phase oxidation of paraxylene in the presence of suitable oxidation catalyst. Suitable catalysts include, but are not limited to, cobalt, manganese and bromine compounds, which are soluble in the selected solvent. In one embodiment of the invention the catalyst comprises cobalt, bromine and manganese. The cobalt and manganese combined can be in concentrations of about 150 ppm to about 3200 ppm by weight in the crude carboxylic acid slurry. The bromine can be in concentrations of about 10 ppm to about 5000 ppm by weight in the crude carboxylic acid slurry.
Preferably, the cobalt and manganese combined can be in concentrations of about 1050 ppm to about 2700 ppm by weight in the crude carboxylic acid slurry. The bromine can be in concentrations of about 1000 ppm to about 2500 ppm by weight in the crude carboxylic acid slurry.
The crude carboxylic acid slurry in conduit 30 is fed to a solid-liquid displacement zone 40 capable of removing a portion of the liquid contained in the crude carboxylic acid slurry 30 to produce the slurry product in conduit 70. A portion means at least 5~/o by weight of the liquid is removed.
The removal of a portion of the liquid to produce a slurry product in conduit 70 can be accomplished by any means known in the art. Typically, the solid-liquid displacement zone 40 comprises a solid-liquid separator that is selected from the group consisting of a decanter centrifuge, rotary disk centrifuge, belt filter, rotary vacuum filter, and the like. The crude carboxylic acid slurry in conduit 30 is fed to the solid-liquid displacement zone 40 comprising a solid-liquid separator. The solid-liquid separator is operated at temperatures between about 50°C to about 200°C, preferably 140°C to about 170°C. The solid-liquid separator is operated at pressures between about 30 psig to about 200 psig. The solid-liquid separator in the solid-liquid displacement zone 40 'may be operated in continuous or batch mode, although it will be appreciated that for commercial processes, the continuous mode is preferred.
The impurities are displaced from the solid-liquid displacement zone 40 in a mother liquor and withdrawn via line 60. In one embodiment of the invention, additional solvent is~fed to~the solid-liquid displacement zone 40 via line 50 to reslurry the crude carboxylic acid slurry 30 and form a slurry product 70. The mother liquor 60 is withdrawn from solid-liquid displacement zone 40 via line 60 and comprises a solvent, typically acetic acid, catalyst, and bromine compounds. The mother liquor in line 60 may either be sent to a process for separating impurities from oxidation solvent via lines not shown or recycled to the catalyst system via lines not shown.
One technique for impurity removal from the mother liquor 60 commonly used in the chemical processing industry is to draw out or "purge" some portion of the recycle stream. Typically, the purge stream is simply disposed of or, if economically justified, subjected to various treatments to remove undesired impurities while recovering valuable components. Examples of impurity removal processes include U.S. Patent # 4,939,297 and U.S.
Patent 4,356,319, herein incorporated by reference.
Step (b) comprises oxidizing the slurry product 70 in a staged oxidation zone 80 to form a staged oxidation product 110.
In one embodiment of the invention, the slurry product 70 is withdrawn via line 70 to a staged oxidation zone 80 where it is heated to between about 190°C to about 280°C and preferably between about 200°C
to about 250°C and further oxidized with air fed by line 100 to produce a staged oxidation product 110.
The staged oxidation zone 80 comprises at least one staged oxidation reactor vessel. The slurry product 70 is fed to the staged oxidation zone 80. The term "staged"means that the oxidation occurs in both the primary oxidation zone 20 discussed previously as well as in the staged oxidation zone 80. For example, the staged oxidation zone 80 can comprise staged oxidation reactor vessels in series.
When the carboxylic acid is terephthalic acid, the staged oxidation zone 80 comprises an oxidation reactor that is heated to between about 190°C to 'about 280°C, preferably between about 200°C to about 250°C, and most preferably between 205 °C to 225°C and further oxidized with air or a source of molecular oxygen fed by line 100 to produce a staged oxidation product 110. Generally, oxidation in the staged oxidation zone 80 is at a higher temperature than the oxidation in the primary oxidation zone 20 to enhance the impurity removal. The staged oxidation zone 80 can be heated directly with solvent vapor, or steam via conduit 90 or indirectly by any means known in the art. Purification in the staged oxidation zone takes place by a mechanism involving recrystallization or crystal growth and oxidation of impurities.
Additional air or molecular oxygen may be fed via conduit 100 to the staged oxidation zone 80 in an amount necessary to oxidize a substantial portion of the partially oxidized products such as 4-carboxybenzaldehyde (4-CBA) in the crude carboxylic acid slurry 30 or slurry product 70 to the corresponding carboxylic acid.. Generally, at least 70% by weight of the 4-CBA is converted to terephthafic acid in the staged oxidation zone 80.
Preferably, at least 80% by weight of the 4-CBA is converted to terephthalic acid in the staged oxidation zone 80. Significant concentrations of 4-carboxybenzaldehyde and p-toluic acid in the terephthalic acid product are particularly detrimental to polymerization processes as they may act as chain terminators during the condensation reaction between terephthalic acid and ethylene glycol in the production of polyethylene terephthalate(PET). Typical terephthalic acid product contains on a weight basis less than about 250 parts per million (ppm) 4-carboxybenzaldehyde and less than about 150 ppm p-toluic acid Impurities in the crude carboxylic acid slurry 30 or slurry product 70 go into solution as the terephthalic acid particles are dissolved and re-crystallized in staged oxidation zone 80. OfFgas from the staged oxidation zone 80 is withdrawn via line 105 and fed to a recovery system where the solvent is removed from the offgas comprising volatile organic compounds (VOCs). VOCs including methyl bromide may be treated, for example by incineration in a catalytic oxidation unit. The staged oxidation product 110 from the staged oxidation zone 80 is withdrawn via line 110.
Step (c) comprises crystallizing the staged oxidation product 110 in a crystallization zone 120 to form a crystallized product 160. Generally, the crystallization zone 120 comprises at least one crystallizer. Vapor product from the crystallization zone can be condensed in at least one condenser and returned to the crystallization zone. Optionally, the liquid from the condenser or vapor product from the crystallization zone can be recycled, or it can be withdrawn or sent to an energy recovery device. In addition, the crystallizer offgas is removed ,via line 170 and can be routed to a recovery system where the solvent is removed and crystallizer ofFgas comprising VOCs may be~treated, for example by incineration in a catalytic oxidation unit.
When the carboxylic acid is terephthalic acid, the staged oxidation product 110 from the staged oxidation zone 80 is withdrawn via line 110 and fed to~a crystallization zone 120 comprising at least one crystallizer where it is cooled to a temperature between about 110°C to about 190°C to form a crystallized product 160, preferably to a temperature between about 140°C to about 180°C, most preferably about 150°C to about 170°C.
The crystallized product 160 from the crystallization zone 120 is withdrawn via line 160. Typically, the crystallized product 160 is then fed directly to a vessel and cooled to form a cooled purified carboxylic acid slurry 210. When the carboxylic acid is terephthalic acid, the cooled crystallized purified carboxylic acid slurry 210 is cooled in a vessel to typically a temperature of approximately 90° C or less before being introduced into a process for recovering the terephthalic acid as a dry powder or wet cake.
Step (d) comprises cooling the crystallized product in a cooling zone 200 to form a cooled purified carboxylic acid slurry 210.
The crystallized product 160 is withdrawn from the crystallization zone 120 via line 160. The crystallized product 160 is fed to a cooling zone 200 and cooled to less than about 90 °C to form the cooled purified carboxylic acid slurry 210. The cooling of the purified carboxylic acid slurry can be accomplished by any means known in the art, typically the cooling zone 200 comprises a flash tank..
Step (e) comprises filtering and optionally drying the cooled purified carboxylic acid slurry 210 in a filtration and drying zone 220 to remove a portion of the solvent from the cooled purified carboxylic acid slurry 210 to produce the purified carboxylic acid product 230.
The cooled, purified carboxylic acid slurry 210 is withdrawn from cooling zone 200 and fed to a filtration and drying zone 220. A portion of the solvent and remaining catalyst and impurities is separated, and the purred carboxylic acid product is withdrawn via line 230.
The filtration and drying zone 220 comprises a filter suitable for recovering the solid carboxylic acid and a dryer. The filtration can be accomplished by any means known in the art. For~.example, a rotary vacuum filter can be used for the filtration to produce a filtration cake. The filtration cake goes through an initial solvent removal step, is then rinsed with acid wash to remove residual catalyst, and then solvent removed again before being sent to the dryers. The drying of the filter cake can be accomplished by any means known in the art that's capable of evaporating at least 10% of the volatiles remaining in the filter cake to produce the carboxylic acid product. For example, a Single Shaft Porcupine~ Processor dryer can be used.
The purified carboxylic acid product 230 has a b* less than about 4.5. Preferably, the b* color of the purified carboxylic acid product 230 is less than about 3.5. Most preferably, the b* color in purified carboxylic acid product 230 is less than about 3. The b* color is one of the three-color attributes measured on a spectroscopic reflectance-based instrument. The color can be measured by any device known in the art. A Hunter Ultrascan XE instrurrient in reflectance mode is typically the measuring device.
Positive readings signify the degree of yellow (or absorbance of blue), while negative readings signify the degree~of blue (or absorbance of yellow).
It should be appreciated that the process zones previously described can be utilized in any other logical order to produce the purified carboxylic acid product. It should also be appreciated that when the process zones are reordered that the process conditions may change.
In another embodiment of this invention each embodiment can optionally include an additional step comprising decolorizing the carboxylic acid or an esterified carboxylic acid via hydrogenation.
The decolorizing of the purified carboxylic acid slurry or an esterified carboxylic acid can be accomplished by any means known in the art and is not limited to hydrogenation: However, for example in one embodiment of the invention, the decolorizing can be accomplished by reacting a carboxylic acid that has undergone esterification treatment , for example with ethylene glycol, with molecular hydrogen in the presence of a hydrogenation catalyst in a reactor zone to produce a decolorized carboxylic acid solution or a decolorized ester product. For the reactor zone, there are no special limitations in the form or construction thereof, subject to an arrangement that allows supply of hydrogen to effect intimate contact of the carboxylic acid or ester product with the catalyst in the reactor zone. Typically, the hydrogenation catalyst is usually a single Group Vlll metal or combination of Group Vlll metals. Preferably, the catalyst is ~~selected from a group consisting of palladium, ruthenium, rhodium and combination thereof. The reactor zone comprises a hydrogenation reactor that operates at a temperature and pressure sufficient to hydrogenate a portion of the characteristically yellow compounds to colorless derivatives EXAMPLES
This invention can be further illustrated by the following example of preferred embodiments thereof, although it will be understood that these examples are included merely for purposes of illustration and are not intended to limit the scope of the invention unless otherwise specifically indicated.
Example Paraxylene was oxidized at 160°C utilizing a Co, Mn, Br catalyst system to produce a crude terephthalic acid slurry having 30-35% solids.
The crude terephthalic acid slurry was crystallized and purified using the process shown in Figure 1. with the omission of a hydrogenation step and the crystallized product from the crystallization zone 120 was transferred directly to flash tank. The product was removed after filtration and drying and analyzed for 4-carboxybenzaldehyde(4-CBA), trimellitic acid(TMA), and 2,6-dicarboxyfluorenone(2,6-DCF), percent transmittance and b*. The b* is one of the three-color attributes measured on a spectroscopic reflectance-based instrument. A Hunter Ultrascan XE instru.ment is. typically the measuring device. Positive readings signify the degree of yellow (or absorbance of blue), while negative readings signify the degree of blue (or absorbance of yellow).
The concentrations of 4-CBA, TMA, 2,6-DCF in the terephthalic acid were analyzed via liquid chromatography. To determine the percent transmittance, a 10% solution of terephthalic acid product in 2M KOH was measured using a UV visible spectrometer at 340nm. The b* of the terephthalic acid was measured using a reflectance color method at 340nm.
The results are shown in Table 1.
Ex. # 4-CBA TMA~ 2,6-DCF %T b*
(ppm) (ppm) (ppm) 1 103 51 10 89 4.1 The amount of 4-CBA present in the purified terephthalic acid product produced by the process of the present invention decreased significantly from typical levels found in the crude carboxylic acid slurry.
The typical levels weren't measured during this trial but these levels were known to those skilled in the art to be about what has been previously disclosed wherein the crude carboxylic acid slurry comprising terephthalic acid, typically contains on a weight basis from about 800 to 7,000 parts per million (ppm) 4-carboxybenzaldehyde. The % transmittance of the purified terephthalic acid product has a direct influence on the color of the polyethylene terephthalate (PET) produced. Desirable PTA (purified terephthalic acid) is white (which is referred to as having low color). Higher transmittance indicates less color in the PTA. The degree of improvement in all the measured categories is particularly surprising given the simplicity of the centrifugation in the solid-liquid separation zone and that no hydrogenation step was performed. In the past, comparable purity levels have been achieved typically by utilization of a hydrogenation plant which includes numerous steps and pieces of equipment, and significant capital investment.
The invention has been described in detail with particular reference to preferred embodiments thereof, but it will be understood 'that variations and modifications can be effected within the spirit and scope of the invention
(b) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein the crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(c) oxidizing the slurry product in a staged oxidation zone to form a staged oxidation product; wherein the oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein the oxidizing is at a higher temperature in the staged oxidation zone than in the primary oxidation zone;
(d) crystallizing the staged oxidation product in a crystallization zone to form a crystallized product;
(e) cooling the crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (f) filtering and optionally drying the cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from the cooled carboxylic acid slurry to produce the purified carboxylic acid product.
These objects, and other objects, will become more apparent to others with ordinary skill in the art after reading this disclosure.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic of the inventive process for the oxidative purification of carboxylic acid wherein a solid-liquid displacement zone 40 is utilized between the primary oxidation zone 20 and the staged oxidation zone 80.
DETAILED DESCRIPTION OF THE INVENTION
The present invention provides a process for the purification of a 1 ~ crude carboxylic acid slurry 30. The process comprises the steps of displacing a mother liquor from the crude carboxylic acid slurry in a solid-liquid displacement zone 40 to form a slurry product 70.
Crude terephthalic acid is conventionally made via the liquid phase air oxidation of paraxylene in the presence of a suitable oxidation catalyst.
Suitable catalysts comprises at least one selected from, but are not limited to, cobalt, bromine and manganese compounds, which are soluble in the selected solvent. Suitable solvents include, but are not limited to, aliphatic mono-carboxylic acids, preferably containing 2 to 6 carbon atoms, or _g_ benzoic acid and mixtures thereof and mixtures of these compounds with water. Preferably the solvent is acetic acid mixed with water, in a ratio of about 5:1 to about 25:1, preferably befiveen about 8:1 and about 20:1.
Throughout the specification acetic acid will be referred to. as the solvent.
However, it should be appreciated that other suitable solvents, such as those disclosed previously, may also be utilized. Patents disclosing the production of terephthalic acid such as U.S patent #4,158,738 and #3,996,271 are hereby incorporated by reference.
In an embodiment of this invention, a process to produce slurry product 70 is provided in Figure 1. The process comprises removing impurities from a crude carboxylic acid slurry 30 in.a solid-liquid displacement zone 40 to form a slurry. product 70; wherein the slurry product 70 is formed without a hydrogenation step..' The solid-liquid displacement zone 40, impurities, crude carboxylic acid slurry 30, and slurry product 70 are all described subsequently in this disclosure.
In another embodiment of this invention a process to produce a purified carboxylic acid product 230 is provided in Figure 1. The process comprises:
Step (a) comprises removing impurities from a crude carboxylic acid slurry 30 in an solid-liquid displacement zone 40 to form a slurry. product 70;
A crude carboxylic acid slurry 30 comprises at least one carboxylic acid, catalyst, at least one solvent, and impurities is withdrawn via like 30.
The impurities typically comprise at least one or more of the following compounds: 4-carboxybenzaldehyde(4-CBA), trimellitic acid(TMA), and 2,6-dicarboxyfluorenone(2,6-DCF). The solvent typically comprises acetic acid, but can be any solvent that has been previously mentioned.
The crude carboxylic acid slurry 30 is produced by oxidizing in a primary oxidation zone 20 an aromatic feed stock 10. In one embodiment, the aromatic feedstock comprises paraxylene. The primary oxidation zone 20 comprises at least one oxidation reactor, and the crude carboxylic acid slurry 30 comprises at least one carboxylic acid. The oxidation reactor can be operated at temperatures between about 120°C to about 200°C, preferably about 140°C to about 170°C. Typically the aromatic feed stock 10 is paraxylene and the carboxylic acid is terephthalic acid. In one embodiment of the invention the primary oxidation gone comprises a bubble column.
Therefore, when terephthalic acid is utilized, the crude carboxylic acid slurry 30 would be referred to as crude terephthalic acid slurry and the purified carboxylic acid product 230 would be referred to as a purified terephthalic acid product.
Carboxylic acids include aromatic carboxylic acids produced via controlled oxidation of an organic substrate. Such aromatic carboxylic acids include compounds with at least one carboxylic acid group attached to a carbon atom that is part of an aromatic ring, preferably having at least 6 carbon atoms, even more preferably having only carbon atoms. Suitable examples of such aromatic rings include, but are not limited to, benzene, biphenyl, terphenyl, naphthalene, and other carbon-based fused aromatic rings. Examples of suitable carboxylic acids include, but are not limited to, terephthalic acid, benzoic acid, p-toluic, isophthalic acid, trimellitic acid, naphthalene dicarboxylic acid, and 2,5-diphenyl-terephthalic acid. Each of the embodiments of this invention can be practiced wherein there is a substantial absence of terephthalic acid and isophthalic acid in the crude carboxylic acid slurry. When the term substantial absence is used it means less than 5% by weight.
Crude terephthalic acid slurry is conventionally synthesized via the liquid phase oxidation of paraxylene in the presence of suitable oxidation catalyst. Suitable catalysts include, but are not limited to, cobalt, manganese and bromine compounds, which are soluble in the selected solvent. In one embodiment of the invention the catalyst comprises cobalt, bromine and manganese. The cobalt and manganese combined can be in concentrations of about 150 ppm to about 3200 ppm by weight in the crude carboxylic acid slurry. The bromine can be in concentrations of about 10 ppm to about 5000 ppm by weight in the crude carboxylic acid slurry.
Preferably, the cobalt and manganese combined can be in concentrations of about 1050 ppm to about 2700 ppm by weight in the crude carboxylic acid slurry. The bromine can be in concentrations of about 1000 ppm to about 2500 ppm by weight in the crude carboxylic acid slurry.
The crude carboxylic acid slurry in conduit 30 is fed to a solid-liquid displacement zone 40 capable of removing a portion of the liquid contained in the crude carboxylic acid slurry 30 to produce the slurry product in conduit 70. A portion means at least 5~/o by weight of the liquid is removed.
The removal of a portion of the liquid to produce a slurry product in conduit 70 can be accomplished by any means known in the art. Typically, the solid-liquid displacement zone 40 comprises a solid-liquid separator that is selected from the group consisting of a decanter centrifuge, rotary disk centrifuge, belt filter, rotary vacuum filter, and the like. The crude carboxylic acid slurry in conduit 30 is fed to the solid-liquid displacement zone 40 comprising a solid-liquid separator. The solid-liquid separator is operated at temperatures between about 50°C to about 200°C, preferably 140°C to about 170°C. The solid-liquid separator is operated at pressures between about 30 psig to about 200 psig. The solid-liquid separator in the solid-liquid displacement zone 40 'may be operated in continuous or batch mode, although it will be appreciated that for commercial processes, the continuous mode is preferred.
The impurities are displaced from the solid-liquid displacement zone 40 in a mother liquor and withdrawn via line 60. In one embodiment of the invention, additional solvent is~fed to~the solid-liquid displacement zone 40 via line 50 to reslurry the crude carboxylic acid slurry 30 and form a slurry product 70. The mother liquor 60 is withdrawn from solid-liquid displacement zone 40 via line 60 and comprises a solvent, typically acetic acid, catalyst, and bromine compounds. The mother liquor in line 60 may either be sent to a process for separating impurities from oxidation solvent via lines not shown or recycled to the catalyst system via lines not shown.
One technique for impurity removal from the mother liquor 60 commonly used in the chemical processing industry is to draw out or "purge" some portion of the recycle stream. Typically, the purge stream is simply disposed of or, if economically justified, subjected to various treatments to remove undesired impurities while recovering valuable components. Examples of impurity removal processes include U.S. Patent # 4,939,297 and U.S.
Patent 4,356,319, herein incorporated by reference.
Step (b) comprises oxidizing the slurry product 70 in a staged oxidation zone 80 to form a staged oxidation product 110.
In one embodiment of the invention, the slurry product 70 is withdrawn via line 70 to a staged oxidation zone 80 where it is heated to between about 190°C to about 280°C and preferably between about 200°C
to about 250°C and further oxidized with air fed by line 100 to produce a staged oxidation product 110.
The staged oxidation zone 80 comprises at least one staged oxidation reactor vessel. The slurry product 70 is fed to the staged oxidation zone 80. The term "staged"means that the oxidation occurs in both the primary oxidation zone 20 discussed previously as well as in the staged oxidation zone 80. For example, the staged oxidation zone 80 can comprise staged oxidation reactor vessels in series.
When the carboxylic acid is terephthalic acid, the staged oxidation zone 80 comprises an oxidation reactor that is heated to between about 190°C to 'about 280°C, preferably between about 200°C to about 250°C, and most preferably between 205 °C to 225°C and further oxidized with air or a source of molecular oxygen fed by line 100 to produce a staged oxidation product 110. Generally, oxidation in the staged oxidation zone 80 is at a higher temperature than the oxidation in the primary oxidation zone 20 to enhance the impurity removal. The staged oxidation zone 80 can be heated directly with solvent vapor, or steam via conduit 90 or indirectly by any means known in the art. Purification in the staged oxidation zone takes place by a mechanism involving recrystallization or crystal growth and oxidation of impurities.
Additional air or molecular oxygen may be fed via conduit 100 to the staged oxidation zone 80 in an amount necessary to oxidize a substantial portion of the partially oxidized products such as 4-carboxybenzaldehyde (4-CBA) in the crude carboxylic acid slurry 30 or slurry product 70 to the corresponding carboxylic acid.. Generally, at least 70% by weight of the 4-CBA is converted to terephthafic acid in the staged oxidation zone 80.
Preferably, at least 80% by weight of the 4-CBA is converted to terephthalic acid in the staged oxidation zone 80. Significant concentrations of 4-carboxybenzaldehyde and p-toluic acid in the terephthalic acid product are particularly detrimental to polymerization processes as they may act as chain terminators during the condensation reaction between terephthalic acid and ethylene glycol in the production of polyethylene terephthalate(PET). Typical terephthalic acid product contains on a weight basis less than about 250 parts per million (ppm) 4-carboxybenzaldehyde and less than about 150 ppm p-toluic acid Impurities in the crude carboxylic acid slurry 30 or slurry product 70 go into solution as the terephthalic acid particles are dissolved and re-crystallized in staged oxidation zone 80. OfFgas from the staged oxidation zone 80 is withdrawn via line 105 and fed to a recovery system where the solvent is removed from the offgas comprising volatile organic compounds (VOCs). VOCs including methyl bromide may be treated, for example by incineration in a catalytic oxidation unit. The staged oxidation product 110 from the staged oxidation zone 80 is withdrawn via line 110.
Step (c) comprises crystallizing the staged oxidation product 110 in a crystallization zone 120 to form a crystallized product 160. Generally, the crystallization zone 120 comprises at least one crystallizer. Vapor product from the crystallization zone can be condensed in at least one condenser and returned to the crystallization zone. Optionally, the liquid from the condenser or vapor product from the crystallization zone can be recycled, or it can be withdrawn or sent to an energy recovery device. In addition, the crystallizer offgas is removed ,via line 170 and can be routed to a recovery system where the solvent is removed and crystallizer ofFgas comprising VOCs may be~treated, for example by incineration in a catalytic oxidation unit.
When the carboxylic acid is terephthalic acid, the staged oxidation product 110 from the staged oxidation zone 80 is withdrawn via line 110 and fed to~a crystallization zone 120 comprising at least one crystallizer where it is cooled to a temperature between about 110°C to about 190°C to form a crystallized product 160, preferably to a temperature between about 140°C to about 180°C, most preferably about 150°C to about 170°C.
The crystallized product 160 from the crystallization zone 120 is withdrawn via line 160. Typically, the crystallized product 160 is then fed directly to a vessel and cooled to form a cooled purified carboxylic acid slurry 210. When the carboxylic acid is terephthalic acid, the cooled crystallized purified carboxylic acid slurry 210 is cooled in a vessel to typically a temperature of approximately 90° C or less before being introduced into a process for recovering the terephthalic acid as a dry powder or wet cake.
Step (d) comprises cooling the crystallized product in a cooling zone 200 to form a cooled purified carboxylic acid slurry 210.
The crystallized product 160 is withdrawn from the crystallization zone 120 via line 160. The crystallized product 160 is fed to a cooling zone 200 and cooled to less than about 90 °C to form the cooled purified carboxylic acid slurry 210. The cooling of the purified carboxylic acid slurry can be accomplished by any means known in the art, typically the cooling zone 200 comprises a flash tank..
Step (e) comprises filtering and optionally drying the cooled purified carboxylic acid slurry 210 in a filtration and drying zone 220 to remove a portion of the solvent from the cooled purified carboxylic acid slurry 210 to produce the purified carboxylic acid product 230.
The cooled, purified carboxylic acid slurry 210 is withdrawn from cooling zone 200 and fed to a filtration and drying zone 220. A portion of the solvent and remaining catalyst and impurities is separated, and the purred carboxylic acid product is withdrawn via line 230.
The filtration and drying zone 220 comprises a filter suitable for recovering the solid carboxylic acid and a dryer. The filtration can be accomplished by any means known in the art. For~.example, a rotary vacuum filter can be used for the filtration to produce a filtration cake. The filtration cake goes through an initial solvent removal step, is then rinsed with acid wash to remove residual catalyst, and then solvent removed again before being sent to the dryers. The drying of the filter cake can be accomplished by any means known in the art that's capable of evaporating at least 10% of the volatiles remaining in the filter cake to produce the carboxylic acid product. For example, a Single Shaft Porcupine~ Processor dryer can be used.
The purified carboxylic acid product 230 has a b* less than about 4.5. Preferably, the b* color of the purified carboxylic acid product 230 is less than about 3.5. Most preferably, the b* color in purified carboxylic acid product 230 is less than about 3. The b* color is one of the three-color attributes measured on a spectroscopic reflectance-based instrument. The color can be measured by any device known in the art. A Hunter Ultrascan XE instrurrient in reflectance mode is typically the measuring device.
Positive readings signify the degree of yellow (or absorbance of blue), while negative readings signify the degree~of blue (or absorbance of yellow).
It should be appreciated that the process zones previously described can be utilized in any other logical order to produce the purified carboxylic acid product. It should also be appreciated that when the process zones are reordered that the process conditions may change.
In another embodiment of this invention each embodiment can optionally include an additional step comprising decolorizing the carboxylic acid or an esterified carboxylic acid via hydrogenation.
The decolorizing of the purified carboxylic acid slurry or an esterified carboxylic acid can be accomplished by any means known in the art and is not limited to hydrogenation: However, for example in one embodiment of the invention, the decolorizing can be accomplished by reacting a carboxylic acid that has undergone esterification treatment , for example with ethylene glycol, with molecular hydrogen in the presence of a hydrogenation catalyst in a reactor zone to produce a decolorized carboxylic acid solution or a decolorized ester product. For the reactor zone, there are no special limitations in the form or construction thereof, subject to an arrangement that allows supply of hydrogen to effect intimate contact of the carboxylic acid or ester product with the catalyst in the reactor zone. Typically, the hydrogenation catalyst is usually a single Group Vlll metal or combination of Group Vlll metals. Preferably, the catalyst is ~~selected from a group consisting of palladium, ruthenium, rhodium and combination thereof. The reactor zone comprises a hydrogenation reactor that operates at a temperature and pressure sufficient to hydrogenate a portion of the characteristically yellow compounds to colorless derivatives EXAMPLES
This invention can be further illustrated by the following example of preferred embodiments thereof, although it will be understood that these examples are included merely for purposes of illustration and are not intended to limit the scope of the invention unless otherwise specifically indicated.
Example Paraxylene was oxidized at 160°C utilizing a Co, Mn, Br catalyst system to produce a crude terephthalic acid slurry having 30-35% solids.
The crude terephthalic acid slurry was crystallized and purified using the process shown in Figure 1. with the omission of a hydrogenation step and the crystallized product from the crystallization zone 120 was transferred directly to flash tank. The product was removed after filtration and drying and analyzed for 4-carboxybenzaldehyde(4-CBA), trimellitic acid(TMA), and 2,6-dicarboxyfluorenone(2,6-DCF), percent transmittance and b*. The b* is one of the three-color attributes measured on a spectroscopic reflectance-based instrument. A Hunter Ultrascan XE instru.ment is. typically the measuring device. Positive readings signify the degree of yellow (or absorbance of blue), while negative readings signify the degree of blue (or absorbance of yellow).
The concentrations of 4-CBA, TMA, 2,6-DCF in the terephthalic acid were analyzed via liquid chromatography. To determine the percent transmittance, a 10% solution of terephthalic acid product in 2M KOH was measured using a UV visible spectrometer at 340nm. The b* of the terephthalic acid was measured using a reflectance color method at 340nm.
The results are shown in Table 1.
Ex. # 4-CBA TMA~ 2,6-DCF %T b*
(ppm) (ppm) (ppm) 1 103 51 10 89 4.1 The amount of 4-CBA present in the purified terephthalic acid product produced by the process of the present invention decreased significantly from typical levels found in the crude carboxylic acid slurry.
The typical levels weren't measured during this trial but these levels were known to those skilled in the art to be about what has been previously disclosed wherein the crude carboxylic acid slurry comprising terephthalic acid, typically contains on a weight basis from about 800 to 7,000 parts per million (ppm) 4-carboxybenzaldehyde. The % transmittance of the purified terephthalic acid product has a direct influence on the color of the polyethylene terephthalate (PET) produced. Desirable PTA (purified terephthalic acid) is white (which is referred to as having low color). Higher transmittance indicates less color in the PTA. The degree of improvement in all the measured categories is particularly surprising given the simplicity of the centrifugation in the solid-liquid separation zone and that no hydrogenation step was performed. In the past, comparable purity levels have been achieved typically by utilization of a hydrogenation plant which includes numerous steps and pieces of equipment, and significant capital investment.
The invention has been described in detail with particular reference to preferred embodiments thereof, but it will be understood 'that variations and modifications can be effected within the spirit and scope of the invention
Claims (31)
1. A process to produce a slurry product, said process comprising removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form said slurry product.
2. The process according to claim 1 wherein said solid-liquid displacement zone comprises a solid-liquid separator that is operated at a temperature between about 50°C to about 200°C.
3. The process according to claim 1 wherein said solid-liquid displacement zone comprises a solid-liquid separator that is operated at a temperature between about 140°C to about 170°C.
4. The process according to claim 2 wherein said solid-liquid displacement zone comprises a solid-liquid separator that is operated at a pressure between about 30 psig to about 200 psig.
5. The process according to claim 1 wherein said solid-liquid displacement zone comprises a decanter centrifuge.
6. The process according to claim 1 wherein said solid-liquid displacement zone comprises a solid-liquid separator selected from the group consisting of a belt filter, a rotary vacuum filter and a rotary disk pack centrifuge.
7. The process according to claim 1 wherein said solid-liquid displacement zone is operated at a pressure of less than about 100 psia.
8. The process according to claim 1 wherein said solid-liquid displacement zone is operated in continuous mode.
9. The process according to claim 1 wherein said slurry product is formed without hydrogenation.
10. A process to produce a purified carboxylic acid product said process comprising:
(a) removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product;
(b) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product;
(c) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product.
(a) removing impurities from a crude carboxylic acid slurry in a solid-liquid displacement zone to form a slurry product;
(b) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product;
(c) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product.
11. The process according to claim 10 further comprising cooling said crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry:
12. The process according to claim 11 further comprising filtering and optionally drying said cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from said cooled carboxylic acid slurry to produce said purified carboxylic acid product.
13. The process according to claim 10, 11 or 12 wherein said solid-liquid displacement zone comprises a solid-liquid separator that is operated at a temperature between about 50°C to about 200°C.
14. The process according to claim 10, 11, or 12 wherein said crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 110°C to about 200°C from the primary oxidation zone.
15. The process according to claim 12 wherein said solid-liquid displacement zone comprises a solid-liquid separator selected from the group consisting of a belt filter, a rotary vacuum filter and a rotary disk pack centrifuge.
16. The process according to claim 12 wherein said purified slurry is formed without hydrogenation.
17. The process according to claim 15 wherein said purified slurry product has a b* of less than about 4.5.
18. The process according to claim 14 wherein said catalyst comprises cobalt, manganese and bromine compounds.
19. The process according to claim 18 wherein the cobalt and manganese combined is present in concentrations of about 150 ppm to about 3200 ppm by weight in the crude carboxylic acid slurry and the bromine can be in concentrations of about 10 ppm to about 5000 ppm by weight in the crude carboxylic acid slurry.
20. A process to produce a purified carboxylic acid product comprising:
(a) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein said crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(b) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product; wherein said oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein said oxidizing is at a higher temperature in said staged oxidation zone than in said primary oxidation zone;
(c) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product;
(d) cooling said crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (e) filtering and optionally drying said cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from said cooled carboxylic acid slurry to produce said purified carboxylic acid product.
(a) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein said crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(b) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product; wherein said oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein said oxidizing is at a higher temperature in said staged oxidation zone than in said primary oxidation zone;
(c) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product;
(d) cooling said crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (e) filtering and optionally drying said cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from said cooled carboxylic acid slurry to produce said purified carboxylic acid product.
21. A process to produce a purified carboxylic acid product comprising: .
(a) oxidizing an aromatic feed stock in a primary oxidation zone to form a crude carboxylic acid slurry; wherein said crude carboxylic acid slurry comprises terephthalic acid; wherein said oxidizing is conducted at a temperature between about 120°C to about 200 °C;
(b) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein said crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(c) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product; wherein said oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein said oxidizing is at a higher temperature in said staged oxidation zone than in said primary oxidation zone;
(d) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product;
(e) cooling said crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (f) filtering and optionally drying said cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from said cooled carboxylic acid slurry to produce said purified carboxylic acid product.
(a) oxidizing an aromatic feed stock in a primary oxidation zone to form a crude carboxylic acid slurry; wherein said crude carboxylic acid slurry comprises terephthalic acid; wherein said oxidizing is conducted at a temperature between about 120°C to about 200 °C;
(b) removing in a solid-liquid displacement zone impurities from a crude carboxylic acid slurry to form a slurry product; wherein said crude carboxylic acid slurry comprises terephthalic acid, catalyst, acetic acid, and impurities that is withdrawn at a temperature between about 140°C and about 170°C from the oxidation of paraxylene in a primary oxidation zone;
(c) oxidizing said slurry product in a staged oxidation zone to form a staged oxidation product; wherein said oxidizing is conducted at a temperature between about 190°C to about 280 °C; and wherein said oxidizing is at a higher temperature in said staged oxidation zone than in said primary oxidation zone;
(d) crystallizing said staged oxidation product in a crystallization zone to form a crystallized product;
(e) cooling said crystallized product in a cooling zone to form a cooled purified carboxylic acid slurry; and (f) filtering and optionally drying said cooled purified carboxylic slurry in a filtration and drying zone to remove a portion of the solvent from said cooled carboxylic acid slurry to produce said purified carboxylic acid product.
22. The process according to claim 20 or 21 further comprising decolorizing in a reactor zone said purified carboxylic acid slurry or a carboxylic acid that has been esterified.
23. The process according to claim 22 wherein said decolorizing is accomplished by reacting said crude carboxylic acid solution with hydrogen in the presence of a hydrogenation catalyst in a reactor zone to produce a decolorized carboxylic acid solution.
24. The process according to claim 20 or 21 wherein said solid-liquid displacement zone comprises a solid-liquid separator that is operated at a temperature between about 50 °C to about 200 °C.
25. The process according to claim 20 or 21 wherein said purified slurry product has a b* of less than about 4.5.
26. The process according to claim 21 wherein said catalyst comprises cobalt, manganese and bromine compounds.
27. The process according to claim 26 wherein the cobalt and manganese combined is present in concentrations of about 1050 ppm to about 2700 ppm by weight in the crude carboxylic acid slurry and the bromine can be in concentrations of about 1000 ppm to about 2500 ppm by weight in the crude carboxylic acid slurry.
28. The process according to claim 1, 10, 19, 20 or 21 wherein said crude carboxylic acid slurry comprises terephthalic acid.
29. A slurry product produced by the process in claim 21.
30. A staged oxidation product produced by the process of claim 21.
31. A crystallized product produced by the process of claim 21.
Applications Claiming Priority (11)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US31529502A | 2002-12-09 | 2002-12-09 | |
| US31529402A | 2002-12-09 | 2002-12-09 | |
| US10/315,294 | 2002-12-09 | ||
| US10/315,295 | 2002-12-09 | ||
| US10/645,734 US7161027B2 (en) | 2002-12-09 | 2003-08-21 | Process for the oxidative purification of terephthalic acid |
| US10/645,737 | 2003-08-21 | ||
| US10/645,734 | 2003-08-21 | ||
| US10/645,737 US7074954B2 (en) | 2002-12-09 | 2003-08-21 | Process for the oxidative purification of terephthalic acid |
| US10/667,744 | 2003-09-22 | ||
| US10/667,744 US7132566B2 (en) | 2003-09-22 | 2003-09-22 | Process for the purification of a crude carboxylic acid slurry |
| PCT/US2003/038305 WO2004052820A1 (en) | 2002-12-09 | 2003-12-03 | Process for the purification of a crude carboxylic acid slurry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2505976A1 true CA2505976A1 (en) | 2004-06-24 |
Family
ID=42777809
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002505976A Abandoned CA2505976A1 (en) | 2002-12-09 | 2003-12-03 | Process for the purification of a crude carboxylic acid slurry |
Country Status (9)
| Country | Link |
|---|---|
| JP (1) | JP2006509044A (en) |
| KR (1) | KR101004211B1 (en) |
| AR (1) | AR042321A1 (en) |
| CA (1) | CA2505976A1 (en) |
| MX (1) | MXPA05006046A (en) |
| MY (1) | MY140391A (en) |
| PL (1) | PL208869B1 (en) |
| TW (1) | TW200510292A (en) |
| WO (1) | WO2004052820A1 (en) |
Families Citing this family (47)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2005121568A (en) | 2002-12-09 | 2006-01-20 | Истман Кемикал Компани (US) | METHOD FOR OXIDATIVE CLEANING OF TERPHTHALIC ACID |
| US7546747B2 (en) | 2004-01-15 | 2009-06-16 | Eastman Chemical Company | Process for production of a dried carboxylic acid cake suitable for use in polyester production |
| US20050283022A1 (en) * | 2004-06-18 | 2005-12-22 | Sheppard Ronald B | Filtrate preparation process for terephthalic acid filtrate treatment |
| US7692037B2 (en) | 2004-09-02 | 2010-04-06 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7399882B2 (en) * | 2004-09-02 | 2008-07-15 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7390921B2 (en) * | 2004-09-02 | 2008-06-24 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| CN101518726B (en) * | 2004-09-02 | 2012-12-12 | 奇派特石化有限公司 | Bubble column reactor mainly used for reactions of liquid-phase flow and vapor-phase flow |
| CA2576341A1 (en) * | 2004-09-02 | 2006-03-23 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7361784B2 (en) * | 2004-09-02 | 2008-04-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7572936B2 (en) * | 2004-09-02 | 2009-08-11 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7572932B2 (en) * | 2004-09-02 | 2009-08-11 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US20060047153A1 (en) * | 2004-09-02 | 2006-03-02 | Wonders Alan G | Optimized liquid-phase oxidation |
| MX2007002283A (en) * | 2004-09-02 | 2007-04-23 | Eastman Chem Co | Optimized liquid-phase oxidation. |
| PT1786753E (en) * | 2004-09-02 | 2015-12-01 | Grupo Petrotemex Sa De Cv | Optimized liquid-phase oxidation |
| US7586000B2 (en) * | 2004-09-02 | 2009-09-08 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7910769B2 (en) | 2004-09-02 | 2011-03-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7495125B2 (en) * | 2004-09-02 | 2009-02-24 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| CN101023046B (en) * | 2004-09-02 | 2019-01-18 | 奇派特石化有限公司 | The liquid phase oxidation of optimization |
| US7371894B2 (en) * | 2004-09-02 | 2008-05-13 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| MX359077B (en) * | 2004-09-02 | 2018-09-13 | Grupo Petrotemex Sa De Cv | Optimized production of aromatic dicarboxylic acids. |
| US7504535B2 (en) * | 2004-09-02 | 2009-03-17 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7683210B2 (en) | 2004-09-02 | 2010-03-23 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| WO2006028817A2 (en) * | 2004-09-02 | 2006-03-16 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7741515B2 (en) * | 2004-09-02 | 2010-06-22 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7692036B2 (en) | 2004-11-29 | 2010-04-06 | Eastman Chemical Company | Optimized liquid-phase oxidation |
| US7615663B2 (en) | 2004-09-02 | 2009-11-10 | Eastman Chemical Company | Optimized production of aromatic dicarboxylic acids |
| DE102004047076A1 (en) | 2004-09-28 | 2006-04-06 | Zimmer Ag | Process for the preparation of polyesters |
| US7557243B2 (en) | 2005-05-19 | 2009-07-07 | Eastman Chemical Company | Enriched terephthalic acid composition |
| US7741516B2 (en) | 2005-05-19 | 2010-06-22 | Eastman Chemical Company | Process to enrich a carboxylic acid composition |
| US20060264664A1 (en) * | 2005-05-19 | 2006-11-23 | Parker Kenny R | Esterification of an exchange solvent enriched composition |
| US7880031B2 (en) | 2005-05-19 | 2011-02-01 | Eastman Chemical Company | Process to produce an enrichment feed |
| US7432395B2 (en) | 2005-05-19 | 2008-10-07 | Eastman Chemical Company | Enriched carboxylic acid composition |
| US7897809B2 (en) | 2005-05-19 | 2011-03-01 | Eastman Chemical Company | Process to produce an enrichment feed |
| US7834208B2 (en) | 2005-05-19 | 2010-11-16 | Eastman Chemical Company | Process to produce a post catalyst removal composition |
| US7919652B2 (en) | 2005-05-19 | 2011-04-05 | Eastman Chemical Company | Process to produce an enriched composition through the use of a catalyst removal zone and an enrichment zone |
| US7884231B2 (en) | 2005-05-19 | 2011-02-08 | Eastman Chemical Company | Process to produce an enriched composition |
| US20070179312A1 (en) * | 2006-02-02 | 2007-08-02 | O'meadhra Ruairi Seosamh | Process for the purification of a crude carboxylic axid slurry |
| US7816556B2 (en) | 2006-03-01 | 2010-10-19 | Eastman Chemical Company | Polycarboxylic acid production system employing enhanced multistage oxidative digestion |
| US7326807B2 (en) | 2006-03-01 | 2008-02-05 | Eastman Chemical Company | Polycarboxylic acid production system with enhanced heating for oxidative digestion |
| US7326808B2 (en) | 2006-03-01 | 2008-02-05 | Eastman Chemical Company | Polycarboxylic acid production system employing cooled mother liquor from oxidative digestion as feed to impurity purge system |
| US7888529B2 (en) | 2006-03-01 | 2011-02-15 | Eastman Chemical Company | Process to produce a post catalyst removal composition |
| US7393973B2 (en) | 2006-03-01 | 2008-07-01 | Eastman Chemical Company | Polycarboxylic acid production system with enhanced residence time distribution for oxidative digestion |
| US7772424B2 (en) | 2006-03-01 | 2010-08-10 | Eastman Chemical Company | Polycarboxylic acid production system employing enhanced evaporative concentration downstream of oxidative digestion |
| US20070208194A1 (en) | 2006-03-01 | 2007-09-06 | Woodruff Thomas E | Oxidation system with sidedraw secondary reactor |
| US7420082B2 (en) | 2006-03-01 | 2008-09-02 | Eastman Chemical Company | Polycarboxylic acid production system employing hot liquor removal downstream of oxidative digestion |
| KR100713253B1 (en) | 2006-04-25 | 2007-05-02 | 삼성석유화학(주) | Solid and liquid separator in producing terephthalic acid and separating method using the same |
| KR102070065B1 (en) | 2018-03-14 | 2020-03-02 | 엘지전자 주식회사 | Cyclone type dust collector and Cleaner having the same |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3170768A (en) * | 1959-04-22 | 1965-02-23 | Standard Oil Co | System for continuous preparation of terephthalic acid |
| GB2072162B (en) * | 1980-03-21 | 1984-03-21 | Labofina Sa | Process for the production and the recovery of terephthalic acid |
| GB9302333D0 (en) * | 1993-02-05 | 1993-03-24 | Ici Plc | Filtration process |
| KR970000136B1 (en) * | 1993-09-28 | 1997-01-04 | 브이.피. 유리예프 | Process for producing highly purified benzenedicarboxylic acid isomers |
| RU2005121568A (en) * | 2002-12-09 | 2006-01-20 | Истман Кемикал Компани (US) | METHOD FOR OXIDATIVE CLEANING OF TERPHTHALIC ACID |
-
2003
- 2003-12-03 PL PL375595A patent/PL208869B1/en not_active IP Right Cessation
- 2003-12-03 KR KR1020057010451A patent/KR101004211B1/en not_active IP Right Cessation
- 2003-12-03 JP JP2005508451A patent/JP2006509044A/en active Pending
- 2003-12-03 MX MXPA05006046A patent/MXPA05006046A/en active IP Right Grant
- 2003-12-03 CA CA002505976A patent/CA2505976A1/en not_active Abandoned
- 2003-12-03 WO PCT/US2003/038305 patent/WO2004052820A1/en active Application Filing
- 2003-12-04 TW TW092134212A patent/TW200510292A/en unknown
- 2003-12-05 AR ARP030104500A patent/AR042321A1/en unknown
- 2003-12-06 MY MYPI20034682A patent/MY140391A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| PL208869B1 (en) | 2011-06-30 |
| PL375595A1 (en) | 2005-12-12 |
| MY140391A (en) | 2009-12-31 |
| WO2004052820A8 (en) | 2004-09-30 |
| KR20050085478A (en) | 2005-08-29 |
| WO2004052820A1 (en) | 2004-06-24 |
| AR042321A1 (en) | 2005-06-15 |
| TW200510292A (en) | 2005-03-16 |
| MXPA05006046A (en) | 2005-08-18 |
| JP2006509044A (en) | 2006-03-16 |
| KR101004211B1 (en) | 2010-12-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7132566B2 (en) | Process for the purification of a crude carboxylic acid slurry | |
| US7074954B2 (en) | Process for the oxidative purification of terephthalic acid | |
| US7161027B2 (en) | Process for the oxidative purification of terephthalic acid | |
| KR101004211B1 (en) | Process for the purification of crude carboxylic acid slurry | |
| US7358392B2 (en) | Process for the oxidative purification of terephthalic acid | |
| US20070179312A1 (en) | Process for the purification of a crude carboxylic axid slurry | |
| US7601795B2 (en) | Process for production of a carboxylic acid/diol mixture suitable for use in polyester production | |
| EP1704137B1 (en) | Process for production of a dried terephthalic acid cake suitable for use in polyester production | |
| US20050228164A1 (en) | Process for production of a carboxylic acid/diol mixture suitable for use in polyester production | |
| EP1551788B1 (en) | Process for production of a carboxylic acid/diol mixture suitable for use in polyester production | |
| KR101034964B1 (en) | Process for the oxidative purification of terephthalic acid | |
| RU2341512C2 (en) | Method of purification of raw carboxylic acid suspension | |
| EP1569887A1 (en) | Process for the purification of a crude carboxylic acid slurry | |
| CA2616024A1 (en) | Process for removal of benzoic acid from an oxidizer purge stream | |
| MXPA06007994A (en) | Process for production of a carboxylic acid/diol mixture suitable for use in polyester production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Discontinued |