Patent Publication Number: US-7902395-B2

Title: Versatile oxidation byproduct purge process

Description:
RELATED APPLICATIONS 
     This application is a divisional of application Ser. No. 11/655,395, entitled “VERSATILE OXIDATION BYPRODUCT PURGE PROCESS”, filed Jan. 19, 2007 which claims the priority benefit of U.S. Provisional Pat. App. Ser. Nos. 60/777,829; 60/777,903; 60/777,905; 60/777,907; 60/777,992; 60/778,117; 60/778,120; 60/778,123; and 60/778,139, all filed Mar. 1, 2006. The foregoing applications are hereby incorporated by reference 
    
    
     BACKGROUND OF THE INVENTION 
     1. Field of the Invention 
     The present invention relates generally to a purge process for use in the production of a carboxylic acid. More specifically, the present invention relates to the use of a purge process for separating and routing various oxidation byproducts formed in a terephthalic acid production process. 
     2. Description of the Prior Art 
     In conventional terephthalic acid (TPA) production processes, para-xylene undergoes oxidation. In such processes, oxidation byproducts are produced along with the formation of TPA. Typically, such oxidation byproducts include the oxidation intermediates and side reaction products formed in the oxidation of para-xylene, as well as any impurities originating from the raw materials. Some of these byproducts are detrimental to the use of TPA in various production processes, such as for the production of polyethylene terephthalate (PET), dimethyl terephthalate (DMT), or cyclohexane dimethanol (CHDM). Accordingly, at least a portion of these detrimental oxidation byproducts are typically removed from the TPA production process in order to yield a commercially usable TPA product. On the other hand, some oxidation byproducts are not detrimental to these production processes. In fact, some oxidation byproducts, such as bi-functional compounds, are actually useful in a PET production process. 
     It is known in the art to employ a purge process to remove oxidation byproducts from TPA production processes, thus rendering the TPA product suitable for use in the various above-mentioned production processes. A purge process typically involves separating a portion of a mother liquor, generated from the separation of liquid from the product stream, to form a purge feed stream. The purge feed stream generally constitutes in the range of from 5 to 40 percent of the total mother liquor, but can be up to 100 percent of the mother liquor. In a typical conventional purge process, the purge feed stream contains acetic acid, catalyst, water, oxidation byproducts, and minor amounts of terephthalic acid. The purge feed stream in conventional processes is usually resolved into a catalyst rich stream and an oxidation byproduct rich stream. The catalyst rich stream is typically recycled to the oxidizer, whereas the oxidation byproduct rich stream is usually routed out of the TPA production process for waste treatment or destruction. In such a conventional process, the oxidation byproduct rich stream contains all of the different types of byproducts generated in the oxidation step. Thus, conventional purge processes expel both detrimental and non-detrimental oxidation byproducts from the TPA production process. 
     Accordingly, there is a need for a purge process that can differentiate detrimental oxidation byproducts from non-detrimental and/or beneficial oxidation byproducts. Such differentiation enables the operator to allow some or all of the non-detrimental and/or beneficial oxidation byproducts to exit the TPA production process along with the TPA product in order to increase product yield and decrease costs associated with waste treatment. 
     SUMMARY OF THE INVENTION 
     One embodiment of the present invention concerns a process for treating a purge feed stream comprising oxidation byproducts and one or more catalyst components, wherein the oxidation byproducts include benzoic acid (BA) and non-BA byproducts. The process of this embodiment comprises: (a) separating at least a portion of the purge feed stream into a non-BA byproduct rich stream and a catalyst and BA rich stream; and (b) separating at least a portion of the catalyst and BA rich stream into a catalyst rich stream and a BA rich stream. 
     Another embodiment of the present invention concerns a process for treating a purge feed stream comprising impurities and one or more catalyst components, wherein the impurities comprise mono-functional impurities and non-mono-functional impurities. The process of this embodiment comprises: (a) separating the purge feed stream into a mono-functional impurity depleted stream and a catalyst and mono-functional impurity rich mother liquor; and (b) separating the catalyst and mono-functional impurity rich mother liquor into a catalyst rich stream and a mono-functional impurity rich stream. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWING FIGURES 
       A preferred embodiment of the present invention is described in detail below with reference to the attached drawing figures, wherein: 
         FIG. 1  is a process flow diagram illustrating a system for the production and purification of carboxylic acid constructed in accordance with the present invention, particularly illustrating a configuration where the crude slurry from the oxidation reactor is subjected to purification, the resulting purified slurry is subjected to product isolation, and a portion of the mother liquor from the product isolation zone is employed as a feed to a purge treatment system; 
         FIG. 2  is a process flow diagram illustrating an overview of a purge treatment system constructed in accordance with a first embodiment of the present invention, particularly illustrating a configuration where the purge feed stream is subjected to non-benzoic acid (non-BA) byproduct removal and the resulting catalyst and benzoic acid (BA) rich mother liquor is subjected to BA removal; 
         FIG. 3  is a process flow diagram illustrating in detail a purge treatment system constructed in accordance with a first configuration of the first embodiment of the present invention, particularly illustrating a configuration where the purge feed stream is subjected to concentration, the resulting concentrated purge stream is subjected to solid/liquid separation, the resulting catalyst and BA rich mother liquor is subjected to concentration, and the resulting concentrated catalyst and BA rich mother liquor is subjected to BA/catalyst separation; 
         FIG. 4  is a process flow diagram illustrating in detail a purge treatment system constructed in accordance with a second configuration of the first embodiment of the present invention, particularly illustrating a configuration where the purge feed stream is subjected to concentration, the resulting concentrated purge stream is subjected to solid/liquid separation, the resulting catalyst and BA rich mother liquor is subjected to catalyst removal, and the resulting BA and solvent rich stream is subjected to BA/solvent separation; 
         FIG. 5  is a process flow diagram illustrating an overview of a purge treatment system constructed in accordance with a second embodiment of the present invention, particularly illustrating a configuration where the purge feed stream is subjected to BA removal and the resulting catalyst and non-BA byproduct rich stream is subjected to non-BA byproduct removal; and 
         FIG. 6  is a process flow diagram illustrating in detail a purge treatment system constructed in accordance with the second embodiment of the present invention, particularly illustrating a configuration where the purge feed stream is subjected to concentration, the resulting concentrated purge stream is subjected to BA separation, the resulting catalyst and non-BA byproduct rich stream is reslurried, and the reslurried catalyst and non-BA byproduct rich stream is subjected to solid/liquid separation. 
     
    
    
     DETAILED DESCRIPTION 
       FIG. 1  illustrates an embodiment of the present invention where carboxylic acid produced in an oxidation reactor and purified in a purification reactor is subjected to product isolation/catalyst removal. A portion of the resulting mother liquor from the product isolation/catalyst removal zone is treated in a purge treatment zone and resolved into a catalyst rich stream, a benzoic acid (BA) rich stream, and a non-BA byproduct rich stream. Various embodiments of the purge zone are described in detail below with reference to  FIGS. 2-6 . 
     In the embodiment illustrated in  FIG. 1 , a predominately fluid-phase feed stream containing an oxidizable compound (e.g., para-xylene), a solvent (e.g., acetic acid and/or water), and a catalyst system (e.g., cobalt, manganese, and/or bromine) can be introduced into oxidation zone  10 . A predominately gas-phase oxidant stream containing molecular oxygen can also be introduced into oxidation zone  10 . The fluid- and gas-phase feed streams form a multi-phase reaction medium in oxidation zone  10 . The oxidizable compound can undergo partial oxidation in a liquid phase of the reaction medium contained in oxidation zone  10 . 
     In one embodiment of the present invention, oxidation zone  10  can comprise an agitated reactor. Agitation of the reaction medium in oxidation zone  10  can be provided by any means known in the art. As used herein, the term “agitation” shall denote work dissipated into the reaction medium causing fluid flow and/or mixing. In one embodiment, oxidation zone  10  can be a mechanically-agitated reactor equipped with means for mechanically agitating the reaction medium. As used herein, the term “mechanical agitation” shall denote agitation of the reaction medium caused by physical movement of a rigid or flexible element(s) against or within the reaction medium. For example, mechanical agitation can be provided by rotation, oscillation, and/or vibration of internal stirrers, paddles, vibrators, or acoustical diaphragms located in the reaction medium. In another embodiment of the present invention, oxidation zone  10  can comprise a bubble column reactor. As used herein, the term “bubble column reactor” shall denote a reactor for facilitating chemical reactions in a multi-phase reaction medium, wherein agitation of the reaction medium is provided primarily by the upward movement of gas bubbles through the reaction medium. As used herein, the terms “majority,” “primarily,” and “predominately” shall mean more than 50 percent. 
     The oxidizable compound present in the fluid-phase feed stream introduced into oxidation zone  10  can comprise at least one hydrocarbyl group. Also, the oxidizable compound can comprise an aromatic compound. In one embodiment, the oxidizable compound can comprise an aromatic compound with at least one attached hydrocarbyl group or at least one attached substituted hydrocarbyl group or at least one attached heteroatom or at least one attached carboxylic acid function (—COOH). In another embodiment, the oxidizable compound can comprise an aromatic compound with at least one attached hydrocarbyl group or at least one attached substituted hydrocarbyl group with each attached group comprising from 1 to 5 carbon atoms. In yet another embodiment, the oxidizable compound can be an aromatic compound having exactly two attached group with each attached group comprising exactly one carbon atom and consisting of methyl group and/or substituted methyl group and/or at most one carboxylic acid group. Suitable examples of the oxidizable compound include, but are not limited to, para-xylene, meta-xylene, para-tolualdehyde, meta-tolualdehyde, para-toluic acid, meta-toluic acid, and/or acetaldehyde. In one embodiment of the present invention, the oxidizable compound comprises para-xylene. 
     A “hydrocarbyl group,” as defined herein, is at least one carbon atom that is bonded only to hydrogen atoms and/or to other carbon atoms. A “substituted hydrocarbyl group,” as defined herein, is at least one carbon atom bonded to at least one heteroatom and to at least one hydrogen atom. “Heteroatoms,” as defined herein, are all atoms other than carbon and hydrogen atoms. “Aromatic compounds,” as defined herein, comprise an aromatic ring and can comprise at least 6 carbon atoms and can also comprise only carbon atoms as part of the ring. Suitable examples of such aromatic rings include, but are not limited to, benzene, biphenyl, terphenyl, naphthalene, and other carbon-based fused aromatic rings. 
     The amount of oxidizable compound present in the fluid-phase feed stream introduced into oxidation zone  10  can be in the range of from about 4 to about 20 weight percent, or in the range of from 6 to 15 weight percent. 
     The solvent present in the fluid-phase feed stream introduced into primary oxidation reactor  10  can comprise an acid component and a water component. The solvent can be present in the fluid-phase feed stream at a concentration in the range of from about 60 to about 98 weight percent, in the range of from about 80 to about 96 weight percent, or in the range of from 85 to 94 weight percent. The acid component of the solvent can be an organic low molecular weight monocarboxylic acid having from 1 to 6 carbon atoms, or 2 carbon atoms. In one embodiment, the acid component of the solvent can comprise acetic acid. The acid component can make up at least about 75 weight percent of the solvent, at least about 80 weight percent of the solvent, or in the range of from 85 to 98 weight percent of the solvent, with the balance being water. 
     As mentioned above, the fluid-phase feed stream introduced into oxidation zone  10  can also include a catalyst system. The catalyst system can be a homogeneous, liquid-phase catalyst system capable of promoting at least partial oxidation of the oxidizable compound. Also, the catalyst system can comprise at least one multivalent transition metal. In one embodiment, the catalyst system can comprise cobalt, bromine, and/or manganese. 
     When cobalt is present in the catalyst system, the fluid-phase feed stream can comprise cobalt in an amount such that the concentration of cobalt in the liquid phase of the reaction medium is maintained in the range of from about 300 to about 6,000 parts per million by weight (ppmw), in the range of from about 700 to about 4,200 ppmw, or in the range of from 1,200 to 3,000 ppmw. When bromine is present in the catalyst system, the fluid-phase feed stream can comprise bromine in an amount such that the concentration of bromine in the liquid phase of the reaction medium is maintained in the range of from about 300 to about 5,000 ppmw, in the range of from about 600 to about 4,000 ppmw, or in the range of from 900 to 3,000 ppmw. When manganese is present in the catalyst system, the liquid-phase feed stream can comprise manganese in an amount such that the concentration of manganese in the liquid phase of the reaction medium is maintained in the range of from about 20 to about 1,000 ppmw, in the range of from about 40 to about 500 ppmw, or in the range of from 50 to 200 ppmw. 
     In one embodiment of the present invention, cobalt and bromine can both be present in the catalyst system. The weight ratio of cobalt to bromine (Co:Br) in the catalyst system can be in the range of from about 0.25:1 to about 4:1, in the range of from about 0.5:1 to about 3:1, or in the range of from 0.75:1 to 2:1. In another embodiment, cobalt and manganese can both be present in the catalyst system. The weight ratio of cobalt to manganese (Co:Mn) in the catalyst system can be in the range of from about 0.3:1 to about 40:1, in the range of from about 5:1 to about 30:1, or in the range of from 10:1 to 25:1. 
     During oxidation, the oxidizable compound (e.g., para-xylene) can be continuously introduced into oxidation zone  10  at a rate of at least about 5,000 kilograms per hour, at a rate in the range of from about 10,000 to about 80,000 kilograms per hour, or in the range of from 20,000 to 50,000 kilograms per hour. During oxidation, the ratio of the mass flow rate of the solvent to the mass flow rate of the oxidizable compound entering oxidation zone  10  can be maintained in the range of from about 2:1 to about 50:1, in the range of from about 5:1 to about 40:1, or in the range of from 7.5:1 to 25:1. 
     The predominately gas-phase oxidant stream introduced into oxidation zone  10  can comprise in the range of from about 5 to about 40 mole percent molecular oxygen, in the range of from about 15 to about 30 mole percent molecular oxygen, or in the range of from 18 to 24 mole percent molecular oxygen. The balance of the oxidant stream can be comprised primarily of a gas or gases, such as nitrogen, that are inert to oxidation. In one embodiment, the oxidant stream consists essentially of molecular oxygen and nitrogen. In another embodiment, the oxidant stream can be dry air that comprises about 21 mole percent molecular oxygen and about 78 to about 81 mole percent nitrogen. In an alternative embodiment of the present invention, the oxidant stream can comprise substantially pure oxygen. 
     During liquid-phase oxidation in oxidation zone  10 , the oxidant stream can be introduced into oxidation zone  10  in an amount that provides molecular oxygen somewhat exceeding the stoichiometric oxygen demand. Thus, the ratio of the mass flow rate of the oxidant stream (e.g., air) to the mass flow rate of the oxidizable compound (e.g., para-xylene) entering oxidation zone  10  can be maintained in the range of from about 0.5:1 to about 20:1, in the range of from about 1:1 to about 10:1, or in the range of from 2:1 to 6:1. 
     The liquid-phase oxidation reaction carried out in oxidation zone  10  can be a precipitating reaction that generates solids. In one embodiment, the liquid-phase oxidation carried out in oxidation zone  10  can cause at least about 10 weight percent of the oxidizable compound (e.g., para-xylene) introduced into oxidation zone  10  to form solids (e.g., crude terephthalic acid (CTA) particles) in the reaction medium. In another embodiment, the liquid-phase oxidation carried out in oxidation zone  10  can cause at least about 50 weight percent of the oxidizable compound (e.g., para-xylene) introduced into oxidation zone  10  to form solids (e.g., CTA particles) in the reaction medium. In yet another embodiment, the liquid-phase oxidation carried out in oxidation zone  10  can cause at least about 90 weight percent of the oxidizable compound (e.g., para-xylene) introduced into oxidation zone  10  to form solids (e.g., CTA particles) in the reaction medium. In one embodiment, the solids content of the reaction medium can be maintained in the range of from about 5 to about 40 weight percent, in the range of from about 10 to about 35 weight percent, or in the range of from 15 to 30 weight percent. As used herein, the term “solids content” shall denote the weight percent solids in a multi-phase mixture. 
     During oxidation in oxidation zone  10 , the multi-phase reaction medium can be maintained at an elevated temperature in the range of from about 125 to about 200° C., in the range of from about 150 to about 180° C., or in the range of from 155 to 165° C. The overhead pressure in oxidation zone  10  can be maintained in the range of from about 1 to about 20 bar gauge (barg), in the range of from about 2 to about 12 barg, or in the range of from 4 to 8 barg. 
     In the embodiment of  FIG. 1 , a crude slurry can be withdrawn from an outlet of oxidation zone  10  via line  12 . The solid phase of the crude slurry in line  12  can be formed primarily of solid particles of CTA. The liquid phase of the crude slurry in line  12  can be a liquid mother liquor comprising at least a portion of the solvent, one or more catalyst components, and minor amounts of dissolved terephthalic acid (TPA). The solids content of the crude slurry in line  12  can be the same as the solids content of the reaction medium in oxidation zone  10 , discussed above. 
     In one embodiment of the present invention, the crude slurry in line  12  can comprise impurities. As used herein, the term “impurities” is defined as any substance other than TPA, solvent, catalyst, and water. Such impurities can include oxidation byproducts formed during the at least partial oxidation of the above-mentioned oxidizable compound (e.g., para-xylene) including, but not limited to, benzoic acid (BA), bromo-benzoic acid, bromo-acetic acid, isophthalic acid, trimellitic acid, 2,5,4′-tricarboxybiphenyl, 2,5,4′-tricarboxybenzophenone, para-toluic acid (p-TAc), 4-carboxybenzaldehyde (4-CBA), monocarboxyfluorenones, monocarboxyfluorenes, and/or dicarboxyfluorenones. 
     In one embodiment of the present invention, the impurities in the crude slurry in line  12  can be classified according to their functionality in a polyester polymerization process, such as, for example, in the production of polyethylene terephthalate (PET). Some impurities can be mono-functional while others can be non-mono-functional in a process for producing a polyester (e.g., PET). As used herein, an impurity that is “mono-functional” is defined as having only one reactive moiety in a process for producing a polyester (e.g., PET). Typically, such reactive moieties can include carboxyl and/or hydroxyl group. Mono-functional impurities include, but are not limited to, BA, bromo-benzoic acid, bromo-acetic acid, 4-CBA, p-TAc, monocarboxyfluorenones, and/or monocarboxyfluorenes. Non-mono-functional impurities can comprise any impurity having less than or greater than one reactive moiety in a process for producing a polyester (e.g., PET). Non-mono-functional impurities include, but are not limited to, isophthalic acid, trimellitic acid, 2,5,4′-tricarboxybiphenyl, 2,5,4′-tricarboxybenzophenone, and dicarboxyfluorenones. 
     Subsequent to removal from oxidation zone  10 , the crude slurry can optionally be introduced into purification zone  14  via line  12 . In one embodiment, the crude slurry can be treated in purification zone  14  such that the concentration of at least one of the above-mentioned impurities in the crude slurry is reduced, thereby producing a purified slurry. Such reduction in the concentration of impurities in the TPA can be accomplished by oxidative digestion, hydrogenation, and/or dissolution/recrystallization. 
     In one embodiment of the present invention, the crude slurry fed to purification zone  14  can have a 4-CBA content of at least about 100 parts per million based on the weight of the solids in the crude slurry (ppmw cs ), in the range of from about 200 to about 10,000 ppmw cs , or in the range of from 800 to 5,000 ppmw cs . The crude slurry fed to purification zone  14  can have a p-TAc content of at least about 250 ppmw cs , in the range of from about 300 to about 5,000 ppmw cs , or in the range of from 400 to 1,500 ppmw cs . The purified slurry exiting purification zone  14  can have a 4-CBA content of less than about 150 parts per million based on the weight of the solids in the purified slurry (ppmw ps ), less than about 100 ppmw ps , or less than 50 ppmw ps . The purified slurry exiting purification zone  14  can have a p-TAc content of less than about 300 ppmw ps , less than about 200 ppmw ps , or less than 150 ppmw p . In one embodiment, treatment of the crude slurry in purification zone  14  can cause the purified slurry exiting purification zone  14  to have a 4-CBA and/or p-TAc content that is at least about 50 percent less than the 4-CBA and/or p-TAc content of the crude slurry fed to purification zone  14 , at least about 85 percent less, or at least 95 percent less. By way of illustration, if the 4-CBA content of the crude slurry fed to purification zone  14  is 200 ppmw cs  and the 4-CBA content of the purified slurry exiting purification zone  14  is 100 ppmw ps , then the 4-CBA content of the purified slurry is 50 percent less than the 4-CBA content of the crude slurry. 
     In one embodiment of the present invention, the crude slurry can be subjected to purification by oxidative digestion in purification zone  14 . As used herein, the term “oxidative digestion” denotes a process step or step where a feed comprising solid particles is subjected to oxidation under conditions sufficient to permit oxidation of at least a portion of the impurities originally trapped in the solid particles. Purification zone  14  can comprise one or more reactors or zones. In one embodiment, purification zone  14  can comprise one or more mechanically-agitated reactors. A secondary oxidant stream, which can have the same composition as the gas-phase oxidant stream fed to oxidation zone  10 , can be introduced into purification zone  14  to provide the molecular oxygen required for oxidative digestion. Additional oxidation catalyst can be added if necessary. In an alternative embodiment of the present invention, a stream comprising hydrogen can be introduced into purification zone  14  for at least partial hydrogenation of the crude slurry. 
     When oxidative digestion is employed in purification zone  14 , the temperature at which oxidative digestion is carried out can be at least about 10° C. greater than the temperature of oxidation in oxidation zone  10 , in the range of from about 20 to about 80° C. greater, or in the range of from 30 to 50° C. greater. The additional heat required for the operation of purification zone  14  can be provided by supplying a vaporized solvent to purification zone  14  and allowing the vaporized solvent to condense therein. The oxidative digestion temperature in purification zone  14  can be maintained in the range of from about 180 to about 240° C., in the range of from about 190 to about 220° C., or in the range of from 200 to 210° C. The oxidative digestion pressure in purification zone  14  can be maintained in the range of from about 100 to about 350 pounds per square inch gauge (pig), in the range of from about 175 to about 275 pig, or in the range of from 185 to 225 pig. 
     In one embodiment of the present invention, purification zone  14  can include two digestion reactors/zones—an initial digester and a final digester. When purification zone  14  includes an initial digester and a final digester, the final digester can be operated at a lower temperature and pressure than the initial digester. In one embodiment, the operating temperature of the final digester can be at least about 2° C. lower than the operating temperature of the initial digester, or in the range of from about 5 to about 15° C. lower than the operating temperature of the initial digester. In one embodiment, the operating pressure of the final digester can be at least about 5 pig lower than the operating pressure of the initial digester, or in the range of from about 10 to about 50 pig lower than the operating pressure of the initial digester. The operating temperature of the initial digester can be in the range of from about 195 to about 225° C., in the range of from 205 to 215° C., or about 210° C. The operating pressure of the initial digester can be in the range of from about 215 to about 235 pig, or about 225 pig. The operating temperature of the final digester can be in the range of from about 190 to about 220° C., in the range of from 200 to 210° C., or about 205° C. The operating pressure of the final digester can be in the range of from about 190 to 210 pig, or about 200 pig. 
     In one embodiment of the present invention, purification zone  14  can comprise optional first and second solvent swap zones. Optional first and second solvent swap zones can operate to replace at least a portion of the existing solvent in a slurry with a replacement solvent. Equipment suitable for such replacement includes, but is not limited to, a decanter centrifuge followed by a reslurry with replacement solvent, a disc stack centrifuge, an advancing front crystallizer, or multiple decanter centrifuges with optional counter current washing. The replacement oxidation solvent can have substantially the same composition as the solvent introduced into oxidation zone  10 , as described above. 
     In one embodiment, the crude slurry fed to purification zone  14  can be treated in the optional first solvent swap zone prior to purification of the crude slurry by the above-mentioned oxidative digestion. In another embodiment, a purified slurry resulting from oxidative digestion of the crude slurry can be treated in the optional second solvent swap zone. 
     Optionally, at least a portion of the displaced oxidation solvent from the optional first and/or second solvent swap zones can be discharged from purification zone  14  via line  38 . At least a portion of the displaced oxidation solvent in line  38  can be routed to solids removal zone  32  via line  40 , purge treatment zone  100  via line  38   a , and/or oxidation zone  10  via line  38   b.    
     In another embodiment of the present invention, purification zone  14  can comprise an optional crystallization zone and/or an optional cooling zone. A purified slurry resulting from the above-mentioned oxidative digestion of the crude slurry can be treated in the optional crystallization zone to at least partially increase the particle size distribution of the purified slurry. Optional crystallization zone can comprise any equipment known in the art that can operate to increase the particle size distribution of the purified slurry. When an optional cooling zone is employed, the purified slurry can be cooled therein to a temperature in the range of from about 20 to about 195° C. When both a crystallization zone and a cooling zone are employed, the purified slurry can be treated first in the crystallization zone and subsequently in the cooling zone. 
     Referring again to  FIG. 1 , a purified slurry can be withdrawn from an outlet of purification zone  14  via line  16 . The solid phase of the purified slurry can be formed primarily of purified terephthalic acid (PTA) particles, while the liquid phase can be formed of a mother liquor. The solids content of the purified slurry in line  16  can be in the range of from about 1 to about 50 percent by weight, in the range of from about 5 to about 40 weight percent, or in the range of from 20 to 35 weight percent. The purified slurry in line  16  can be introduced into product isolation/catalyst removal zone  18  for at least partial recovery of the solid PTA particles. 
     Optionally, at least a portion of the crude slurry in line  12  can be introduced into product isolation/catalyst removal zone  18  via line  12   a . As mentioned above, the solid phase of the crude slurry can be formed primarily of CTA particles, while the liquid phase can be formed of a mother liquor. The solids content of the crude slurry in line  12   a  can be in the range of from about 1 to about 50 percent by weight, in the range of from about 5 to about 40 weight percent by weight, or in the range of from 20 to 35 percent by weight. The crude slurry in line  12   a  can be introduced into product isolation/catalyst removal zone  18  for recovery of the solid CTA particles. 
     Product isolation/catalyst removal zone  18  can separate the crude slurry and/or the purified slurry into a predominately fluid phase mother liquor and a wet cake. Product isolation/catalyst removal zone  18  can comprise any method of solid/liquid separation known in the art that is capable of generating a wet cake and a mother liquor stream. In addition, it may be desirable for product isolation/catalyst removal zone  18  to have the capability of washing the wet cake. Suitable equipment for use in product isolation/catalyst removal zone  18  includes, but is not limited to, a pressure drum filter, a vacuum drum filter, a vacuum belt filter, multiple solid bowl centrifuges with optional counter current wash, or a perforated centrifuge. 
     In one embodiment of the present invention, a wash stream can be introduced into product isolation/catalyst removal zone  18  to wash at least a portion of the wet cake generated in product isolation/catalyst removal zone  18 , thereby producing a washed wet cake. In one embodiment, the wash stream can comprise acetic acid and/or water. Optionally, after washing the wet cake, the used wash liquor can be withdrawn from product isolation/catalyst removal zone  18 , and at least a portion of the wash liquor can be routed, either directly or indirectly, to oxidation zone  10 . 
     The above-mentioned wet cake generated in product isolation/catalyst removal zone  18  can be discharged via line  20 . In one embodiment of the present invention, the wet cake generated in product isolation/catalyst removal zone  18  can primarily comprise solid particles of TPA. The solid TPA particles can comprise CTA and/or PTA particles. The wet cake can comprise in the range of from about 5 to about 30 weight percent liquid, in the range of from about 10 to about 25 weight percent liquid, or in the range of from 12 to 23 weight percent liquid. Additionally, the TPA product wet cake in line  20  can comprise oxidation byproducts, as discussed above. In one embodiment, the TPA product in line  20  can comprise a cumulative concentration of mono-functional oxidation byproducts of less than about 1,000 ppmw, less than about 750 ppmw, or less than 500 ppmw. 
     In one embodiment of the present invention, the wet cake in line  20  can be introduced into drying zone  22  via line  20  to thereby produce a dry TPA particulate product comprising solid TPA particles. Drying zone  22  can comprise any drying device known in the art that can produce a dried TPA particulate product comprising less than about 5 weight percent liquid, less than about 3 weight percent liquid, or less than 1 weight percent liquid. Dried TPA particulate product can be discharged from drying zone  22  via line  24 . 
     In another embodiment, the wet cake in line  20  can be introduced into solvent swap zone  26  to produce a wet TPA particulate product comprising solid TPA particles. Solvent swap zone  26  can operate to replace at least a portion of the liquid in the wet cake with a replacement solvent. Equipment suitable for such replacement includes, but is not limited to, a decanter centrifuge followed by a reslurry with replacement solvent, a disc stack centrifuge, an advancing front crystallizer, or multiple decanter centrifuges with counter current washing. Wet TPA particulate product can be discharged from solvent swap zone  26  via line  28 . The wet TPA particulate product can comprise in the range of from about 5 to about 30 weight percent liquid, in the range of from about 10 to about 25 weight percent liquid, or in the range of from 12 to 23 weight percent liquid. 
     Referring still to  FIG. 1 , the above-mentioned mother liquor can be discharged from product isolation/catalyst removal zone  18  via line  30 . In one embodiment of the present invention, at least a portion of the mother liquor can optionally be introduced into solids removal zone  32 . Solids removal zone  32  can comprise any equipment known in the art that is operable to remove a sufficient amount of solids from the mother liquor to produce a solids-depleted mother liquor comprising less than about 5 weight percent solids, less than about 2 weight percent solids, or less than 1 weight percent solids. Suitable equipment that may be employed in solids removal zone  32  includes a pressure filter, such as, for example, a filter press, a candle filter, a pressure leaf filter, and/or a cartridge filter. In one embodiment, solids removal zone  32  can be operated at a temperature in the range of from about 20 to about 195° C. and a pressure in the range of from about 750 to about 3750 torr during solids removal. The solids-depleted mother liquor can be discharged from solids removal zone  32  via line  34 . In one embodiment of the present invention, at least a portion of the solids removed from the mother liquor in solids removal zone  32  can be discharged via line  36  and can be routed to product isolation/catalyst removal zone  18  via line  36   a  and/or to line  20  via line  36   b.    
     As mentioned above, at least a portion of the displaced oxidation solvent from purification zone  14  can also optionally be treated in solids removal zone  32 . Such displaced oxidation solvent can be withdrawn from purification zone  14  via line  38  and introduced into solids removal zone  32  via line  40 . When displaced oxidation solvent from oxidation zone  14  is treated in solids removal zone  32 , the resulting solids-depleted displaced oxidation solvent can be combined with the solids-depleted mother liquor and can be discharged via line  34 . 
     In one embodiment of the present invention, at least a portion of the optionally solids-depleted mother liquor in line  34  can be withdrawn from line  34  via line  42  to form a purge feed stream. The amount of mother liquor withdrawn by line  42  to form the purge feed stream can be in the range of from about 1 to about 55 percent of the total weight of the mother liquor, in the range of from about 5 to about 45 percent by weight, or in the range of from 10 to 35 percent by weight. Optionally, at least a portion of the displaced oxidation solvent discharged from purification zone  14  in line  38  can be combined with the purge feed stream via line  38   a . In another embodiment, at least a portion of the remaining mother liquor in line  34  can be routed, either directly or indirectly, to oxidation zone  10  via line  44 . Optionally, at least a portion of the wash liquor discharged from product isolation/catalyst removal zone  18  can be combined with at least a portion of the mother liquor in line  44  prior to introduction into oxidation zone  10 . 
     In one embodiment of the present invention, the mother liquor in line  34 , and consequently the purge feed stream in line  42 , can comprise solvent, one or more catalyst components, oxidation byproducts, and TPA. The solvent in the mother liquor in line  34  and the purge feed stream in line  42  can comprise a monocarboxylic acid. In one embodiment, the solvent can comprise water and/or acetic acid. The mother liquor in line  34  and the purge feed stream in line  42  can comprise solvent in an amount of at least about 85 weight percent, at least about 95 weight percent, or at least 99 weight percent. 
     The catalyst components in the mother liquor in line  34  and the purge feed stream in line  42  can comprise the catalyst components as described above with reference to the catalyst system introduced into oxidation zone  10 . In one embodiment, the catalyst components can comprise cobalt, manganese, and/or bromine. The mother liquor in line  34  and the purge feed stream in line  42  can have a cumulative concentration of all of the catalyst components in the range of from about 500 to about 20,000 ppmw, in the range of from about 1,000 to about 15,000 ppmw, or in the range of from 1,500 to 10,000 ppmw. 
     The oxidation byproducts in the mother liquor in line  34  and the purge feed stream in line  42  can comprise one or more of the oxidation byproducts discussed above. In one embodiment, the oxidation byproducts in the mother liquor in line  34  and the purge feed stream in line  42  can comprise both BA and non-BA byproducts. As used herein, the term “non-BA byproducts” is defined as any oxidation byproduct that is not benzoic acid. Non-BA byproducts include, but are not limited to, isophthalic acid (IPA), phthalic acid (PA), trimellitic acid, 2,5,4′-tricarboxybiphenyl, 2,5,4′-tricarboxybenzophenone, p-TAc, 4-CBA, naphthalene dicarboxylic acid, monocarboxyfluorenones, monocarboxyfluorenes, and/or dicarboxyfluorenones. In one embodiment, the mother liquor in line  34  and the purge feed stream in line  42  can comprise BA in an amount in the range of from about 500 to about 150,000 ppmw based on the weight of the purge feed stream, in the range of from about 1,000 to about 100,000 ppmw, or in the range of from 2,000 to 50,000 ppmw. Additionally, the mother liquor in line  34  and the purge feed stream in line  42  can have a cumulative concentration of non-BA byproducts in the range of from about 500 to about 50,000 ppmw, in the range of from about 1,000 to about 20,000 ppmw, or in the range of from 2,000 to 10,000 ppmw. 
     In one embodiment of the present invention, the mother liquor in line  34  and the purge feed stream in line  42  can comprise solids in an amount of less than about 5 weight percent, less than about 2 weight percent, or less than 1 weight percent. Additionally, the purge feed stream can have a temperature of less than about 240° C., in the range of from about 20 to about 200° C., or in the range of from 50 to 100° C. 
     Referring still to  FIG. 1 , the purge feed stream can be introduced into a purge treatment zone  100  via line  42 . As will be discussed in greater detail below, the purge treatment zone  100  can separate the purge feed stream into a catalyst rich stream, a BA rich stream (i.e., a mono-functional impurity rich stream), and a non-BA byproduct rich stream (i.e., a mono-functional impurity depleted stream). The BA rich stream can be discharged from purge treatment zone  100  via line  48 , the catalyst rich stream can be discharged from purge treatment zone  100  via line  50 , and the non-BA byproduct rich stream can be discharged from purge treatment zone  100  via line  52 . 
     The BA rich stream in line  48  can have a relatively higher concentration of BA on a weight basis compared to the BA concentration of the purge feed stream in line  42 . In one embodiment of the present invention, the BA rich stream in line  48  can have a concentration of BA that is at least about 1.5 times the concentration of BA in the purge feed stream on a weight basis, at least about 5 times the concentration of BA in the purge feed stream on a weight basis, or at least 10 times the concentration of BA in the purge feed stream on a weight basis. In one embodiment, BA can be the primary oxidation byproduct in the BA rich stream. Depending of the temperature and pressure of the BA rich stream upon exiting purge treatment zone  100 , the BA rich stream in line  48  can predominately comprise solids or fluid. Thus, in one embodiment, the BA rich stream in line  48  can comprise at least about 50 weight percent fluid, at least about 70 weight percent fluid, or at least 90 weight percent fluid. In an alternate embodiment, the BA rich stream in line  48  can comprise at least about 50 weight percent solids, at least about 70 weight percent solids, or at least 90 weight percent solids. 
     The catalyst rich stream in line  50  can have a relatively higher cumulative concentration of all of the catalyst components on a weight basis compared to the cumulative concentration of all of the catalyst components in the purge feed stream in line  42 . In one embodiment of the present invention, the catalyst rich stream in line  50  can have a cumulative concentration of all of the catalyst components that is at least about 1.5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, at least about 5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, or at least 10 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis. Depending of the temperature and pressure of the catalyst rich stream upon exiting purge treatment zone  100 , the catalyst rich stream in line  50  can predominately comprise solids or fluid. Thus, in one embodiment, the catalyst rich stream in line  50  can comprise at least about 50 weight percent fluid, at least about 70 weight percent fluid, or at least 90 weight percent fluid. In an alternate embodiment, the catalyst rich stream in line  50  can comprise at least about 50 weight percent solids, at least about 70 weight percent solids, or at least 90 weight percent solids. 
     The non-BA byproduct rich stream in line  52  can have a relatively higher cumulative concentration of non-BA byproducts on a weight basis compared to the cumulative concentration of non-BA byproducts in the purge feed stream in line  42 . In one embodiment of the present invention, the non-BA byproduct rich stream in line  52  can have a cumulative concentration of non-BA byproducts that is at least about 1.5 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis, at least about 5 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis, or at least 10 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis. In one embodiment, non-BA byproducts can cumulatively be the primary oxidation byproducts in the non-BA byproduct rich stream. The non-BA byproduct rich stream in line  52  can be in the form of a wet cake, comprising in the range of from about 5 to about 30 weight percent liquid, in the range of from 10 to about 25 weight percent liquid, or in the range of from 12 to 23 weight percent liquid. 
     In one embodiment of the present invention, at least a portion of the BA rich stream, the catalyst rich stream, and the non-BA byproduct rich stream can be routed to different locations. Such locations include, but are not limited to, various points in a TPA production process, an IPA production process, a phthalic acid (PA) production process, a BA production process, a naphthalene-dicarboxylic acid (NDA) production process, a dimethylterephthalate (DMT) production process, a dimethylnaphthalate (DMN) production process, a cyclohexane dimethanol (CHDM) production process, a dimethylcyclohexanedicarboxylate (DMCD) production process, a cyclohexanedicarboxylic acid (CHDA) production process, a polyethylene terephthalate (PET) production process, a production process for any isomers of NDA, DMT, DMN, CHDM, DMCD, CHDA, a copolyester production process, a polymer production process employing one or more of TPA, IPA, PA, BA, NDA, DMT, DMN, CHDM, DMCD, CHDA, or any isomers thereof as one component and/or as a monomer, and/or outside the TPA, IPA, PA, BA, NDA, DMT, DMN, CHDM, DMCD, CHDA, PET, or polymer production processes. 
     In one embodiment, the amount of BA that exits the TPA production process with the TPA product and/or is combined with the TPA product downstream of the TPA production process can be sufficient to result in a TPA product comprising BA in an amount of less than about 1000 ppmw, less than about 500 ppmw, or less than 250 ppmw. In another embodiment, the rate at which BA exits the TPA production process with the TPA product and/or is combined with the TPA product downstream of the TPA production process can be less than about 50 percent, less than about 10 percent, less than about 1 percent, or less than 0.1 percent of the make-rate of BA in the TPA production process. As used herein with reference to BA, when no purification step (e.g., purification zone  14 ) is employed in the TPA production process, the term “make-rate” is defined as the difference between the mass per unit time of BA entering the oxidation step (e.g., oxidation zone  10 ) and the mass per unit time of BA exiting the oxidation step. When a purification step is employed in the TPA production process, the term “make-rate” when referring to BA is defined as the difference between the mass per unit time of BA entering the oxidation step (e.g., oxidation zone  10 ) and the mass per unit time of BA exiting the purification step (e.g., purification zone  14 ). By way of illustration, for a TPA production process that employs a purification step, if BA enters the oxidation step of the TPA production process at a rate of 50 kilograms per hour (kg/hr), and BA exits the purification step at a rate of 150 kg/hr, then the make-rate of BA in the TPA production process is 100 kg/hr. 
     In another embodiment, at least a portion of the BA rich stream can exit the process depicted in  FIG. 1  and be routed to a purification and recovery process, a subsequent chemical process, and/or a waste treatment or disposal process. Such waste treatment or disposal processes include, but are not limited to, sale, burial, incineration, neutralization, anaerobic and/or aerobic digestion, treatment in a waste oxidizer, and/or treatment in a waste reactor. In one embodiment of the present invention, at least a portion of the BA rich stream can be routed to a waste treatment process where at least about 50 weight percent, at least about 60 weight percent, or at least 70 weight percent of the BA present in the BA rich stream is treated. 
     As mentioned above, the catalyst rich stream in line  50  can be routed to various points in a TPA production process. In one embodiment of the present invention, at least a portion of the catalyst rich stream in line  50  can be routed, either directly or indirectly, to oxidation zone  10 , where at least about 50 weight percent, at least about 60 weight percent, or at least 70 weight percent of the catalyst components of the catalyst rich stream are introduced into oxidization zone  10 . In one embodiment, prior to routing, a liquid can optionally be added to the catalyst rich stream in line  50  to produce a reslurried catalyst rich stream. The reslurried catalyst rich stream can comprise at least about 35 weight percent liquid, at least about 50 weight percent liquid, or at least 65 weight percent liquid. The liquid added to the catalyst rich stream can be, for example, acetic acid and/or water. 
     Referring still to  FIG. 1 , as noted above, the non-BA byproduct rich stream in line  52  can be routed to various points in the depicted TPA production process. Such routing includes, but is not limited to, returning at least a portion of the non-BA byproduct rich stream, either directly or indirectly, to oxidation zone  10  and/or purification zone  14 . In one embodiment, at least a portion of the non-BA byproduct rich stream can be routed such that at least a portion of the non-BA byproducts in said non-BA byproduct rich stream exit the TPA production process with the dry TPA product discharged from line  24  and/or with the wet TPA product discharged from line  28 . For example, at least a portion of the non-BA byproduct rich stream can be introduced into the purified slurry in line  16  and/or into the product slurry/cake in line  20  and allowed to exit the TPA production process with the TPA product. In another embodiment, at least a portion of the non-BA byproducts in the non-BA byproduct rich stream can be combined with the TPA product downstream of the TPA production process. In one embodiment, at least about 5 weight percent, at least about 25 weight percent, at least about 50 weight percent, or at least 75 weight percent of the non-BA byproducts in the non-BA byproduct rich stream can be allowed to exit the TPA production process with the TPA product and/or can be combined with the TPA product downstream of the TPA production process. 
     In one embodiment, the cumulative rate at which the non-BA byproducts exit the TPA production process with the TPA product and/or are combined with the TPA product downstream of the TPA production process can be at least about 5 percent, at least about 10 percent, at least about 20 percent, or at least 50 percent of the make-rate of the non-BA byproducts in the TPA production process. As used herein with reference to non-BA byproducts, when no purification step (e.g., purification zone  14 ) is employed in the TPA production process, the term “make-rate” is defined as the difference between the mass per unit time of non-BA byproducts entering the oxidation step (e.g., oxidation zone  10 ) and the mass per unit time of non-BA byproducts exiting the oxidation step. When a purification step is employed in the TPA production process, the term “make-rate” when referring to non-BA byproducts is defined as the difference between the mass per unit time of non-BA byproducts entering the oxidation step (e.g., oxidation zone  10 ) and the mass per unit time of non-BA byproducts exiting the purification step (e.g., purification zone  14 ). By way of illustration, for a TPA production process that employs a purification step, if non-BA byproducts enter the oxidation step of the TPA production process at a rate of 50 kg/hr, and non-BA byproducts exit the purification step at a rate of 150 kg/hr, then the make-rate of non-BA byproducts in the TPA production process is 100 kg/hr. 
     In another embodiment, the non-BA byproduct rich stream can exit the process depicted in  FIG. 1  and can be routed to a purification and recovery process, a process utilizing non-BA byproducts for making non-BA byproduct derivatives, and/or a waste treatment or disposal process. Such waste treatment or disposal processes include, but are not limited to, sale, burial, incineration, neutralization, anaerobic and/or aerobic digestion, treatment in a waste oxidizer, and/or treatment in a waste reactor. 
     As mentioned above, the non-BA byproduct rich stream in line  52  can be in the form of a wet cake. In one embodiment of the present invention, prior to routing the non-BA byproduct rich stream, at least a portion the non-BA byproduct rich stream may optionally be dried in drying zone  54 . Drying zone  54  can comprise any drying device known in the art that can produce a dried non-BA byproduct rich stream comprising less than about 5 weight percent liquid, less than about 3 weight percent liquid, or less than 1 weight percent liquid. The optionally dried non-BA byproduct rich stream can be discharged from drying zone  54  via line  56 . 
     In another embodiment, prior to routing the non-BA byproduct rich stream, a liquid may be added to at least a portion of the non-BA byproduct rich stream in reslurry zone  58  to produce a reslurried non-BA byproduct rich stream. The reslurried non-BA byproduct rich stream can be discharged from reslurry zone  58  via line  60 . The reslurried non-BA byproduct rich stream can comprise at least about 35 weight percent liquid, at least about 50 weight percent liquid, or at least 65 weight percent liquid. The liquid added to the non-BA byproduct rich stream in reslurry zone  58  can comprise acetic acid and/or water. 
       FIG. 2  illustrates an overview of one embodiment of purge treatment zone  100 , briefly discussed above with reference to  FIG. 1 . In the embodiment of  FIG. 2 , purge treatment zone  100  comprises a non-BA byproduct removal zone  102  and a BA removal zone  104 . The purge feed stream in line  42  can initially be introduced into non-BA byproduct removal zone  102 . As will be discussed in greater detail below, non-BA byproduct removal zone  102  can separate the purge feed stream into the above-mentioned non-BA byproduct rich stream and a catalyst and BA rich mother liquor (i.e., a catalyst and mono-functional impurity rich mother liquor). The non-BA byproduct rich stream can be discharged from non-BA byproduct removal zone  102  via line  52 , and the catalyst and BA rich mother liquor can be discharged via line  106 . 
     In one embodiment of the present invention, the catalyst and BA rich mother liquor in line  106  can comprise one or more catalyst components, BA, and solvent. The catalyst and BA rich mother liquor can comprise solids in an amount of less than about 5 weight percent, less than about 3 weight percent, or less than 1 weight percent. The solvent in the catalyst and BA rich mother liquor can comprise acetic acid and/or water. The catalyst components in the catalyst and BA rich mother liquor can comprise cobalt, manganese, and/or bromine, as discussed above in relation to the catalyst system introduced into oxidation zone  10  of  FIG. 1 . 
     The catalyst and BA rich mother liquor in line  106  can have a relatively higher concentration of BA and catalyst components on a weight basis compared to the concentration of BA and catalyst components in the purge feed stream in line  42 . In one embodiment, the catalyst and BA rich mother liquor in line  106  can have a cumulative concentration of all of the catalyst components that is at least about 1.5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, at least about 5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, or at least 10 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis. Furthermore, the catalyst and BA rich mother liquor in line  106  can have a concentration of BA that is at least about 1.5 times the concentration of BA in the purge feed stream on a weight basis, at least about 5 times the concentration of BA in the purge feed stream on a weight basis, or at least 10 times the concentration of BA in the purge feed stream on a weight basis. 
     In the embodiment of  FIG. 2 , the catalyst and BA rich mother liquor can be introduced into BA removal zone  104  via line  106 . As will be discussed in greater detail below, BA removal zone  104  can separate the catalyst and BA rich mother liquor into the above-mentioned BA rich stream and the above-mentioned catalyst rich stream. The BA rich stream can be discharged from BA removal zone  104  via line  48  and the catalyst rich stream can be discharged via line  50 . 
       FIG. 3  illustrates in detail one configuration of non-BA byproduct removal zone  102  and BA removal zone  104 . In the embodiment of  FIG. 3 , non-BA byproduct removal zone  102  comprises concentration section  202  and solid/liquid separation section  208 . In this embodiment, the purge feed stream can initially be introduced into concentration section  202  via line  42 . Concentration section  202  can operate to remove at least a portion of the volatile compounds contained in the purge feed stream. In one embodiment, the volatile compounds comprise at least a portion of the solvent in the purge feed stream. The solvent can comprise water and/or acetic acid. Concentration section  202  can remove at least about 30, at least about 45, or at least 60 weight percent of the volatile compounds in the purge feed stream. Volatile compounds can be discharged from concentration section  202  via line  204 . In one embodiment of the present invention, at least a portion of the volatiles in line  204  can be routed, either directly or indirectly, to oxidation zone  10  depicted in  FIG. 1 . 
     Any equipment known in the industry capable of removing at least a portion of the volatile compounds from the purge feed stream may be employed in concentration section  202 . Examples of suitable equipment include, but are not limited to, one or more evaporators. In one embodiment, concentration section  202  can comprise at least two evaporators. When two evaporators are employed, each one individually can be operated under vacuum at reduced temperature, or can be operated at elevated temperature and pressure. In one embodiment, each evaporator can be operated at a temperature in the range of from about 40 to about 180° C. and a pressure in the range of from about 50 to about 4500 torr during concentration. Suitable equipment for use in concentration section  202  includes, but is not limited to, a simple agitated tank, a flash evaporator, an advancing front crystallizer, a thin film evaporator, a scraped thin film evaporator, and/or a falling film evaporator. 
     In the embodiment of  FIG. 3 , a concentrated purge feed stream can be discharged from concentration section  202  via line  206 . The solids content of the concentrated purge feed stream in line  206  can be at least about 1.5 times, at least about 5 times, or at least 10 times the solids content of the unconcentrated purge feed stream in line  42 , where solids content is measured on a weight basis. The concentrated purge feed stream can comprise solids in an amount in the range of from about 5 to about 70 weight percent, or in the range of from 10 to 40 weight percent. Also, the concentrated purge feed stream can comprise one or more catalyst components, BA and non-BA oxidation byproducts, TPA particles, and solvent, each as discussed above. 
     The concentrated purge feed stream can be introduced into solid/liquid separation section  208  via line  206 . Solid/liquid separation section  208  can separate the concentrated purge feed stream into a predominately fluid phase catalyst and BA rich mother liquor and a wet cake. In the embodiment of  FIG. 3 , solid/liquid separation section  208  comprises mother liquor removal section  208   a  and wash section  208   b . Mother liquor removal section  208   a  can operate to separate the concentrated purge feed stream into the above-mentioned catalyst and BA rich mother liquor and an initial wet cake. The catalyst and BA rich mother liquor can be discharged from mother liquor removal section  208   a  via line  106 . The initial wet cake can be introduced into wash section  208   b . At least a portion of the initial wet cake can then be washed with the wash feed introduced into wash section  208   b  via line  210  to produce a washed wet cake. The wash feed in line  210  can comprise water and/or acetic acid. Furthermore, the wash feed can have a temperature in the range of from about the freezing point of the wash feed to about the boiling point of the wash feed, in the range of from about 20 to about 110° C., or in the range of from 40 to 90° C. The wash feed can operate to remove at least a portion of catalyst components from the wet cake. After washing the wet cake, the resulting wash liquor can be discharged from wash section  208   b  via line  212 , and the washed wet cake can be discharged via line  52 . In one embodiment, the above-mentioned non-BA byproduct rich stream comprises at least a portion of the washed wet cake. 
     Solid/liquid separation section  208  can comprise any solid/liquid separation device known in the art. Suitable equipment for use in solid/liquid separation section  208  includes, but is not limited to, a pressure drum filter, a vacuum drum filter, a vacuum belt filter, multiple solid bowl centrifuges with counter current wash, or a perforated centrifuge. In one embodiment, solid/liquid separation section  208  can be operated at a temperature in the range of from about 20 to about 170° C. and a pressure in the range of from about 375 to about 4500 torr during separation. 
     As mentioned above, the wash liquor can be discharged from solid/liquid separation section  208  via line  212 . In one embodiment, at least a portion of the wash liquor in line  212  can be routed, either directly or indirectly, to oxidation zone  10  as depicted in  FIG. 1 . Optionally, at least a portion of the wash liquor in line  212  can be concentrated prior to introduction in oxidation zone  10 . The optional concentrator can be any device known in the art capable of concentrating the wash liquor stream, such as, for example, membrane separation or evaporation. In another embodiment, at least a portion of the wash liquor in line  212  can be routed to a waste treatment facility. 
     Referring still to  FIG. 3 , BA removal zone  104  comprises concentration section  214  and BA/catalyst separation section  220 . In one embodiment, the catalyst and BA rich mother liquor in line  106  can initially be introduced into concentration section  214 . Concentration section  214  can operate to remove at least a portion of the volatile compounds contained in the catalyst and BA rich mother liquor. In one embodiment, the volatile compounds comprise at least a portion of the solvent in the catalyst and BA rich mother liquor. The solvent can comprise water and/or acetic acid. Concentration section  214  can remove at least about 50, at least about 70, or at least 90 weight percent of the solvent in the catalyst and BA rich mother liquor. Evaporated compounds can be discharged from concentration section  214  via line  216 . 
     Any equipment known in the industry capable of removing at least a portion of the volatile compounds from the catalyst and BA rich mother liquor can be employed in concentration section  214 . Examples of suitable equipment include, but are not limited to, a simple agitated tank, a flash evaporator, an advancing front crystallizer, a thin film evaporator, a scraped thin film evaporator, or a falling film evaporator. In one embodiment, concentration section  214  can be operated at a pressure in the range of from about 50 to about 800 torr during concentration. Additionally, concentration section  214  can be operated at a temperature of at least about 120° C., or at least 130° C. during concentration. 
     In the embodiment of  FIG. 3 , a concentrated catalyst and BA rich mother liquor (i.e., a mono-functional impurity rich slurry) can be discharged from concentration section  214  via line  218 . The concentrated catalyst and BA rich mother liquor can comprise one or more catalyst components, BA, and solvent. The concentration of all the catalyst components and BA of the concentrated catalyst and BA rich mother liquor can be at least about 1.5 times, at least about 5 times, or at least 10 times the concentration of all the catalyst components and BA of the unconcentrated catalyst and BA rich mother liquor in line  106 . 
     The concentrated catalyst and BA rich mother liquor can be introduced into BA/catalyst separation section (i.e., mono-functional impurity removal section)  220  via line  218 . BA/catalyst separation section  220  operates to separate the concentrated catalyst and BA rich mother liquor into the above-mentioned catalyst rich stream and the above-mentioned BA rich stream. In one embodiment, separation of the concentrated catalyst and BA rich mother liquor can be accomplished by evaporating and removing at least a portion of the BA in the concentrated catalyst and BA rich mother liquor. Any dryer known in the art that can evaporate and remove at least about 50 weight percent, at least about 70 weight percent, or at least 90 weight percent of the BA in the concentrated catalyst and BA rich mother liquor can be used. A suitable example of a commercially available dryer that can be employed in BA/catalyst separation section  220  includes, but is not limited to, a LIST dryer. In one embodiment, BA/catalyst separation section  220  can be operated at a temperature in the range of from about 170 to about 250° C. and a pressure in the range of from about 50 to about 760 torr during separation. The catalyst rich stream can be discharged from BA/catalyst separation section  220  via line  50 , and the BA rich stream can be discharged via line  48 . 
       FIG. 4  illustrates in detail a second configuration of non-BA byproduct removal zone  102  and BA removal zone  104 . Non-BA byproduct removal zone  102  comprises concentration section  302  and solid/liquid separation section  308 . In the embodiment of  FIG. 4 , concentration section  302  and solid/liquid separation section  308  are operated in substantially the same manner as discussed above with reference to concentration section  202  and solid/liquid separation section  208  of  FIG. 3 . Additionally, the composition and treatment of the volatiles in line  304 , the concentrated purge feed stream in line  306 , the wash feed in line  310 , and the wash liquor in line  312  are substantially the same as discussed above with reference to the volatiles in line  204 , the concentrated purge feed stream in line  206 , the wash feed in line  210 , and the wash liquor in line  212  of  FIG. 3 . The above-mentioned non-BA byproduct rich stream can be discharged from solid/liquid separation section  308  via line  52 , and the above-mentioned catalyst and BA rich mother liquor can be discharged via line  106 . 
     In the embodiment of  FIG. 4 , BA removal zone  104  comprises catalyst removal section  314  and BA/solvent separation section  318 . In one embodiment, the catalyst and BA rich mother liquor in line  106  can initially be introduced into catalyst removal section  314 . Catalyst removal section  314  can operate to remove at least a portion of the BA and solvent in the catalyst and BA rich mother liquor, generating the above-mentioned catalyst rich stream and a BA and solvent rich stream (i.e., a mono-functional impurity and solvent rich stream). Removal of BA and solvent in catalyst removal section  314  can be accomplished by evaporating and removing at least a portion of the BA and solvent from the catalyst and BA rich mother liquor. In one embodiment, at least about 50 weight percent, at least about 70 weight percent, or at least 90 weight percent of the BA and solvent in the catalyst and BA rich mother liquor can be removed in catalyst removal section  314 . Any dryer known in the art that can evaporate and remove at least a portion of the BA and solvent in the catalyst and BA rich mother liquor can be used. A suitable example of a commercially available dryer that can be employed in catalyst removal section  314  includes, but is not limited to, a LIST dryer. In one embodiment, catalyst removal  314  can be operated at a temperature in the range of from about 170 to about 250° C. and a pressure in the range of from about 50 to about 760 torr during catalyst removal. 
     As mentioned above, catalyst removal zone  314  generates the catalyst rich stream and a BA and solvent rich stream. The catalyst rich stream can be discharged from catalyst removal zone  314  via line  50 . The BA and solvent rich stream can be discharged from catalyst removal section  314  via line  316 . In one embodiment, the BA and solvent rich stream can be a predominately fluid phase stream and can comprise at least two portions having different volatilities (i.e., a lower volatility portion and a higher volatility portion). The lower volatility portion can comprise BA and the higher volatility portion can comprise solvent. The solvent can comprise acetic acid and/or water. 
     In the embodiment of  FIG. 4 , the BA and solvent rich stream can be introduced into BA/solvent separation section (i.e., mono-functional impurity/solvent separation section)  318  via line  316 . BA/solvent separation section  318  can separate the BA and solvent rich stream into the above-mentioned BA rich stream and a solvent rich stream. The separation of the BA and solvent rich stream can be accomplished by fluid/fluid separation. Any fluid/fluid separation device known in the art capable of separating two fluid phases may be used in BA/solvent separation section  318 . Such devices include, but are not limited to, a dryer, an evaporator, a partial condenser, and/or distillation devices. In one embodiment, BA/solvent separation section  318  can be operated at a temperature in the range of from about 170 to about 250° C. and a pressure in the range of from about 50 to about 760 torr during separation. 
     The BA rich stream can be discharged from BA/solvent separation section  318  via line  48 . The solvent rich stream can be discharged from BA/solvent separation section  314  via line  320 . In one embodiment, the solvent rich stream can comprise a higher concentration of solvent than the BA and solvent rich stream in line  316 . The solvent rich stream can have a concentration of solvent that is at least about 1.5 times the concentration of solvent in the BA and solvent rich stream on a weight basis, at least about 5 times the concentration of solvent in the solvent and BA rich stream on a weight basis, or at least 10 times the concentration of solvent in the solvent and BA rich stream on a weight basis. In one embodiment, at least a portion of the solvent rich stream in line  320  can be routed, either directly or indirectly, to oxidation zone  10  depicted in  FIG. 1 . 
       FIG. 5  illustrates an overview of another embodiment of purge treatment zone  100 , briefly discussed above with reference to  FIG. 1 . In the embodiment of  FIG. 5 , purge treatment zone  100  comprises BA removal zone  400  and non-BA byproduct removal zone  402 . The purge feed stream in line  42  can initially be introduced into BA removal zone  400 . As will be discussed in greater detail below, BA removal zone  400  can separate the purge feed stream into the above-mentioned BA rich stream and a catalyst and non-BA byproduct rich stream (i.e., a catalyst and non-mono-functional impurity rich stream). The BA rich stream can be discharged from BA removal zone  400  via line  48 , and the catalyst and non-BA byproduct rich stream can be discharged via line  404 . 
     In one embodiment of the present invention, the catalyst and non-BA byproduct rich stream can comprise one or more catalyst components, non-BA byproducts, and solvent. Depending of the temperature and pressure of the catalyst and non-BA byproduct rich stream upon exiting BA removal zone  400 , the catalyst and non-BA byproduct rich stream in line  404  can predominately comprise solids or fluid. Thus, in one embodiment, the catalyst and non-BA byproduct rich stream in line  404  can comprise at least about 50 weight percent fluid, at least about 70 weight percent fluid, or at least 90 weight percent fluid. In an alternate embodiment, the catalyst and non-BA byproduct rich stream in line  404  can comprise at least about 50 weight percent solids, at least about 70 weight percent solids, or at least 90 weight percent solids. The solvent in the catalyst and non-BA byproduct rich stream can comprise acetic acid and/or water. The catalyst components in the catalyst and non-BA byproduct rich stream can comprise cobalt, manganese, and/or bromine, as discussed above in relation to the catalyst system introduced into oxidation zone  10  of  FIG. 1 . 
     The catalyst and non-BA byproduct rich stream in line  404  can have a relatively higher concentration of catalyst components and non-BA byproducts on a weight basis compared to the concentration of catalyst components and non-BA byproducts in the purge feed stream in line  42 . In one embodiment, the catalyst and non-BA byproduct rich stream in line  404  can have a cumulative concentration of all of the catalyst components that is at least about 1.5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, at least about 5 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis, or at least 10 times the cumulative concentration of all of the catalyst components in the purge feed stream on a weight basis. Furthermore, the catalyst and non-BA byproduct rich stream in line  404  can have a cumulative concentration of non-BA byproducts that is at least about 1.5 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis, at least about 5 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis, or at least 10 times the cumulative concentration of non-BA byproducts in the purge feed stream on a weight basis. 
     In the embodiment of  FIG. 5 , the catalyst and non-BA byproduct rich stream can be introduced into non-BA byproduct removal zone  402  via line  404 . As will be discussed in greater detail below, non-BA byproduct removal zone  402  can separate the catalyst and non-BA byproduct rich stream into the above-mentioned non-BA byproduct rich stream and the above-mentioned catalyst rich stream. The non-BA byproduct rich stream can be discharged from non-BA byproduct removal zone  402  via line  52  and the catalyst rich stream can be discharged via line  50 . 
       FIG. 6  illustrates in detail one configuration of BA removal zone  400  and non-BA byproduct removal zone  402 . In the embodiment of  FIG. 6 , BA removal zone  400  comprises concentration section  502  and BA separation section  508 . In this embodiment, the purge feed stream in line  42  can initially be introduced into concentration section  502 . Concentration section  502  can operate to remove at least a portion of the volatile compounds contained in the purge feed stream. Concentration section  502  is operated in substantially the same manner as discussed above with reference to concentration section  202  of  FIG. 3 . Volatiles can be discharged from concentration section  502  via line  504 . The composition and treatment of the volatiles in line  504  is substantially the same as discussed above with reference to the volatiles in line  204  of  FIG. 3 . A concentrated purge feed stream can be discharged from concentration section  502  via line  506 . The composition of the concentrated purge feed stream in line  506  is substantially the same as discussed above with reference to the concentrated purge feed stream in line  206  of  FIG. 3 . 
     Referring still to  FIG. 6 , the concentrated purge feed stream in line  506  can be introduced into BA separation section (i.e., mono-functional impurity removal section)  508 . BA separation section  508  can operate to separate the concentrated purge feed stream into the above-mentioned BA rich stream and the above-mentioned catalyst and non-BA byproduct rich stream. In one embodiment, BA separation can be achieved by evaporating and removing at least a portion of the BA from the concentrated purge feed stream. The evaporation can be achieved by heating the concentrated purge feed stream in BA separation section  508  to at least about 123° C. at atmospheric pressure. In another embodiment, BA separation section  508  can be operated at a pressure in the range of from about 50 to about 760 torr during evaporation. Additionally, BA separation section  508  can be operated at a temperature in the range of from about 123 to about 250° C. during evaporation. At least about 40 weight percent, at least about 70 weight percent, or at least 90 weight percent of the BA contained in the concentrated purge feed stream can be removed in BA separation section  508 . Equipment suitable for use in BA separation section  508  includes, but is not limited to, a LIST dryer, a pot distillation device, a partial condenser, or a thin film evaporator. The BA rich stream can be discharged from BA separation section  508  via line  48 , and the catalyst and non-BA byproduct rich stream can be discharged via line  404 . 
     In the embodiment of  FIG. 6 , non-BA byproduct removal zone  402  comprises reslurry section  510  and solid/liquid separation section  516 . In one embodiment, the catalyst and non-BA byproduct rich stream in line  404  can initially be introduced into reslurry section  510 . Reslurry section  510  can be operated to add a liquid to the catalyst and non-BA byproduct rich stream, thereby generating a reslurried catalyst and non-BA byproduct rich stream. The liquid added to the catalyst and non-BA byproduct rich stream in reslurry section  510  can be introduced into reslurry section  510  via line  512 . In one embodiment, the liquid in line  512  can be a solvent, which can comprise acetic acid and/or water. Equipment suitable for use in reslurry section  510  can include any equipment known in the art that can accomplish mixing a liquid stream and a solid stream to generate a slurry. Optionally, reslurry section  510  can comprise a step of crystallization in order to increase particle size distribution. 
     The reslurried catalyst and non-BA byproduct rich stream can be discharged from reslurry section  510  via line  514 . In one embodiment, the reslurried catalyst and non-BA byproduct rich stream can comprise one or more catalyst components, non-BA byproducts, and/or solvent. The solvent can comprise acetic acid and/or water. The catalyst components can comprise cobalt, manganese, and/or bromine, as discussed above in relation to the catalyst system introduced into oxidation zone  10  of  FIG. 1 . The reslurried catalyst and non-BA byproduct rich stream can comprise solids in an amount in the range of from about 0 to about 65 weight percent, or in the range of from 10 to 40 weight percent. 
     The reslurried catalyst and non-BA byproduct rich stream can be introduced into solid/liquid separation section  516  via line  514 . Solid/liquid separation section  514  can separate the reslurried catalyst and non-BA byproduct rich stream into a predominately fluid phase mother liquor (e.g., the above-mentioned catalyst rich stream) and a wet cake. In the embodiment of  FIG. 6 , solid/liquid separation section  516  comprises mother liquor removal section  516   a  and wash section  516   b . Mother liquor removal section  516   a  can operate to separate the reslurried catalyst and non-BA byproduct rich stream into the above-mentioned catalyst rich stream and an initial wet cake. The catalyst rich stream can be discharged from mother liquor removal section  516   a  via line  50 . The initial wet cake can be introduced into wash section  516   b . At least a portion of the initial wet cake can then be washed with the wash feed introduced into wash section  516   b  via line  518  to produce a washed wet cake. The wash feed in line  518  can comprise water and/or acetic acid. The wash feed can operate to remove at least a portion of catalyst components from the wet cake. After washing the wet cake, the resulting wash liquor can be discharged from wash section  516   b  via line  520 , and the washed wet cake can be discharged via line  52 . In one embodiment, the above-mentioned non-BA byproduct rich stream can comprise at least a portion of the washed wet cake. 
     Solid/liquid separation section  516  can comprise any solid/liquid separation device known in the art. Suitable equipment that can be used in solid/liquid separation section  516  includes, but is not limited to, a pressure drum filter, a vacuum drum filter, a vacuum belt filter, multiple solid bowl centrifuges with counter current wash, or a perforated centrifuge. In one embodiment, solid/liquid separation section  516  can be operated at a temperature in the range of from about 20 to about 170° C. and a pressure in the range of from about 375 to about 4500 torr during separation. 
     As mentioned above, the wash liquor can be discharged from solid/liquid separation section  516  via line  520 . In one embodiment, at least a portion of the wash liquor in line  520  can be routed, either directly or indirectly, to oxidation zone  10 , as depicted in  FIG. 1 . Optionally, the wash liquor in line  520  can be concentrated prior to introduction in oxidation zone  10 . The optional concentrator can be any device known in the art capable of concentrating the wash liquor stream, such as, for example, membrane separation or evaporation. In another embodiment, at least a portion of the wash liquor in line  520  can be routed to a waste treatment facility. 
     It will be understood by one skilled in the art that each of the above-described embodiments, as well as any sub-parts of those embodiments, may be operated in a continuous or a non-continuous manner. Non-continuous operations include, but are not limited to, batch-wise operations, cyclical operations, and/or intermittent operations. 
     In some of the embodiments above, temperature ranges are provided for a specified operation. For each of the above embodiments where a temperature range is provided, the temperature is defined as the average temperature of the substance in the given zone or section. By way of illustration, as discussed above with reference to  FIG. 1 , a portion of the mother liquor in line  30  can optionally be treated in solids removal zone  32 , where solids removal zone  32  can be operated at a temperature in the range of from about 20 to about 195° C. This means that the average temperature of the mother liquor while in solids removal zone  32  can be in the range of from about 20 to about 195° C. 
     Numerical Ranges 
     The present description uses numerical ranges to quantify certain parameters relating to the invention. It should be understood that when numerical ranges are provided, such ranges are to be construed as providing literal support for claim limitations that only recite the lower value of the range as well as claims limitation that only recite the upper value of the range. For example, a disclosed numerical range of 10 to 100 provides literal support for a claim reciting “greater than 10” (with no upper bounds) and a claim reciting “less than 100” (with no lower bounds). 
     Definitions 
     As used herein, the terms “comprising,” “comprises,” and “comprise” are open-ended transition terms used to transition from a subject recited before the term to one or more elements recited after the term, where the element or elements listed after the transition term are not necessarily the only elements that make up the subject. 
     As used herein, the terms “including,” “includes,” and “include” have the same open-ended meaning as “comprising,” “comprises,” and “comprise.” 
     As used herein, the terms “having,” “has,” and “have” have the same open-ended meaning as “comprising,” “comprises,” and “comprise.” 
     As used herein, the terms “containing,” “contains,” and “contain” have the same open-ended meaning as “comprising,” “comprises,” and “comprise.” 
     As used herein, the terms “a,” “an,” “the,” and “said” mean one or more. 
     As used herein, the term “and/or,” when used in a list of two or more items, means that any one of the listed items can be employed by itself or any combination of two or more of the listed items can be employed. For example, if a composition is described as containing components A, B, and/or C, the composition can contain A alone; B alone; C alone; A and B in combination; A and C in combination; B and C in combination; or A, B, and C in combination. 
     Claims Not Limited to Disclosed Embodiments 
     The forms of the invention described above are to be used as illustration only, and should not be used in a limiting sense to interpret the scope of the present invention. Obvious modifications to the exemplary embodiments, set forth above, could be readily made by those skilled in the art without departing from the spirit of the present invention. 
     The inventors hereby state their intent to rely on the Doctrine of Equivalents to determine and assess the reasonably fair scope of the present invention as pertains to any apparatus not materially departing from but outside the literal scope of the invention as set forth in the following claims.