CN105413598A - Systems and methods for production of aromatic carboxylic acids - Google Patents
Systems and methods for production of aromatic carboxylic acids Download PDFInfo
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- CN105413598A CN105413598A CN201510525883.2A CN201510525883A CN105413598A CN 105413598 A CN105413598 A CN 105413598A CN 201510525883 A CN201510525883 A CN 201510525883A CN 105413598 A CN105413598 A CN 105413598A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
- C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00004—Scale aspects
- B01J2219/00006—Large-scale industrial plants
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This invention relates to systems and methods to recover heat and scrub the off-gas from oxidation reactors in a process to produce aromatic carboxylic acids, such as terephthalic acid. The invention belongs to the technical field of production of aromatic carboxylic acids. In the prior art, an alternative method needs to be found for simplifying a system to recover heat and scrub the off-gas from oxidation reactors in a process to producethe terephthalic acid, and for reducing capital expenditure of using equipment. The invention comprises systems for production of terephthalic acid, methods for treating terephthalic acid, and so on. As certain systems and components are needed for treating the terephthalic acid, the invention has the advantage of reducing capital expenditure. For example, in comparison with one system, a steam scrub system can be removed, and in comparison with the other system, a steam compression system can be removed. The systems and the methods can be used for production of terephthalic acid.
Description
The application is the applying date is on December 15th, 2010, and application number is 201080056879.1, and denomination of invention is the divisional application of the application for a patent for invention of " system and method producing aromatic carboxylic acids ".
Invention field
The present invention relates to and reclaim heat and the system and method for washing from the waste gas of oxidation reactor in the process of producing aromatic carboxylic acids.
the cross reference of related application
This application claims the rights and interests of the priority of the U.S. Provisional Application 61/286957 that on December 16th, 2009 submits to.
background of invention
Two-stage process can be adopted to prepare the terephthalic acid (TPA) (PTA) of purifying.In the first phase, in oxidation workshop, in solvent (such as acetic acid and water), terephthaldehyde's acid crude (CTA) is prepared in paraxylene air oxidation by adopting homogeneous catalyst.The scope of the temperature of described reaction is about 150-210 DEG C.Described oxidation reaction usually one, carry out in two or three vessel cascade, and multiple parallel reactor can be adopted for each step.Reactor vessel is stirred vessel normally, and wherein said stirring is achieved by the combination of mechanical agitation with the mixing effect of the air be added into.
The second stage of described preparation technology carries out purifying by catalytic hydrogenation in aqueous to CTA.Usually, CTA is dissolved in the water under high pressure (70-90barA) and high temperature (275-290 DEG C), and carries out hydrogenation through catalyst fixed bed on carbon of palladium load.When the solution obtained is by a series of four to six crystallizers, described solution is cooled, here terephthalic acid (TPA) (PTA) crystallization of purifying, and most of impurity and accessory substance (such as paratolunitrile) retain in the solution.Then the slurry (at 140-160 DEG C) obtained is fed to suitable continuous solid-liquid separating equipment, such as sedimentation-type centrifuge, rotational pressure or vacuum filter etc., said PTA and purification mother liquor flow point from, then dry.
Fig. 1 illustrates that a kind of paraxylene that makes reacts the method preparing CTA crude product, wherein adopts the oxidation reactor of two series connection.Primary oxidation reactor comprises paraxylene, acetic acid aqueous solution, catalyst and air, and is about 200 DEG C in reaction temperature, operates described primary oxidation reactor at 16barA.Slurry from described primary oxidation reactor is transferred into secondary oxidation reactor, and here described slurry and air react at about 187 DEG C and 12barA, so that more reactant is converted into CTA.Elementary and the secondary oxidation reactor separative waste gas system of tool separately, to reclaim heat and washing steam.Owing to operating under the elementary temperature and pressure significantly different with each leisure of secondary oxidation reactor, adopt two recuperations of heat and vapor wash system, which increase Capital expenditure.In order to overcome this impact, compressor (not shown) raising can be adopted from the pressure of the waste gas of secondary oxidation heat recovery system, with to single vapor wash system adverse current feeding, thus reduce the assembly repeated, such as described secondary oxidation reactor exhaust vapor wash system.But the method needs the Capital expenditure of this compressor.
Summary of the invention
In the industry, need to develop another kind of method, it can simplify described system with the waste gas reclaiming heat and wash from described oxidation reactor in the process of producing terephthalic acid (TPA), also reduces the Capital expenditure to the equipment adopted simultaneously.
The embodiments of the present invention briefly introduced comprise system, method etc. for the production of terephthalic acid (TPA).
One of them example system comprises primary oxidation reactor, wherein at the temperature of the pressure of about 12 to 18barA and about 180 to 210 DEG C, operate described primary oxidation reactor, wherein said primary oxidation reactor is communicated with elementary heat recovery system, and wherein said elementary heat recovery system is communicated with vapor wash system; With secondary oxidation reactor, wherein at the pressure than the low 2bar of being less than of the pressure of described primary oxidation reactor and operate described secondary oxidation reactor at the temperature of about 5-15 lower than the temperature of described primary oxidation reactor DEG C, the slurry wherein produced in described primary oxidation reactor is transferred into described secondary oxidation reactor, wherein said secondary oxidation reactor is communicated with secondary heat recovery system, and wherein said secondary heat recovery system is communicated with described vapor wash system.
Wherein, an illustrative methods for the production of terephthalic acid (TPA) comprises: provide primary oxidation reactor, and wherein said primary oxidation reactor is communicated with elementary heat recovery system, and wherein said elementary heat recovery system is communicated with vapor wash system; There is provided secondary oxidation reactor, wherein said secondary oxidation reactor is communicated with secondary heat recovery system, and wherein said secondary heat recovery system is communicated with described vapor wash system; Paraxylene, acetic acid, catalyst and air are incorporated in described primary oxidation reactor; Described primary oxidation reactor is operated to produce the first slurry at the temperature of the pressure of about 12 to 18barA and about 180 to 210 DEG C; Described first slurry produced in described primary oxidation reactor is incorporated in described secondary oxidation reactor; With at the pressure than the low 2bar of being less than of the pressure of described primary oxidation reactor and operate described secondary oxidation reactor, to produce the second slurry at the temperature of about 5-15 lower than the temperature of described primary oxidation reactor DEG C.
accompanying drawing is sketched
Many aspects of the present invention can be understood better with reference to the following drawings.Assembly in the drawing is not necessarily drawn in proportion.
Fig. 1 illustrates the schematic diagram of a part for the technique of producing terephthalic acid (TPA).
Fig. 2 illustrates the schematic diagram of a part for the improving technique producing terephthalic acid (TPA).
detailed Description Of The Invention
Before more detailed description the present invention, will be appreciated that the disclosure of invention is not limited to the specific embodiment described, because these can (certainly can) change.What should also be clear that be the term adopted here is only to describe specific embodiment, and is not intended to limit the present invention, because scope of the present invention will only be limited by the claims of enclosing.
Unless otherwise defined, all technical terms adopted herein have with scientific terminology the identical implication usually understood with the those of ordinary skill in the technical field belonging to the present invention.Although with method described herein and material type like or suitable arbitrary method and material can be used for enforcement and the test of present disclosure, introduce now preferred method and material.
Unless otherwise, the embodiment of present disclosure will adopt the technology belonging to the chemistry, Chemical Engineering, chemical recovery etc. of art technology.These technology are illustrated in the literature fully.
How to implement described method to provide to those of ordinary skill in the art and use disclosed herein and composition required for protection and compound, disclosing following examples.Although guaranteed the accuracy of numerical value (such as amount, temperature etc.) as possible, in requisition for some errors of consideration and deviation.Unless otherwise, number is parts by weight, and temperature is DEG C to represent, and pressure represents with barA.
It must be noted that, as in description and the claims of enclosing apply, unless context is clearly pointed out in addition, described singulative " " and " being somebody's turn to do " comprise a plurality of referent.Therefore, such as mention that " carrier " comprises multiple carrier.In this manual and in claims subsequently, unless there is significantly contrary intention, manyly the term with following implication will be defined by mentioning.
Discuss
The embodiment of present disclosure comprises the system for the production of terephthalic acid (TPA), the method etc. for the treatment of terephthalic acid (TPA).Owing to needing certain system and assembly process terephthalic acid (TPA), and the advantage of the system and method for present disclosure is that they decrease Capital expenditure.Such as, compared with a system, a vapor wash system can be removed, and compared with another system, a steam compression system can be removed.
In a word, by adopting homogeneous catalyst, in acetic acid aqueous solution solvent, terephthaldehyde's acid crude (CTA) is prepared in paraxylene air oxidation.Before being fed into oxidation reactor, the air rubber capsule that oxidation reaction adopts is containing can the molecular oxygen of enrichment or dilution compared with air.CTA slurry from the gained of described oxidation reactor (includes CTA, oxidation catalyst, reaction intermediate and accessory substance, comprise pigment compound) be usually fed into a more than container (by being called as crystallizer), to reduce the pressure and temperature of process flow.CTA solid is separated with oxidation technology mother liquor, and described CTA solid is carried out drying by the described oxidation solvent of optional removal.Then described CTA solid mixes to form CTA purifying feed streams with water, then in the second stage of terephthalic acid (TPA) (PTA) preparation technology of purifying to described CTA purifying.Described CTA purifying process/system can comprise many stages, include but not limited to CTA again pulp stage, slurry heating and CTA dissolution phase, catalytic hydrogenation stage, crystallization stage, filtration stage, solvent recovery stage, drying stage, mother liquor stream processing stage, mother liquor solids treatment stage etc.
Fig. 2 illustrates the embodiment of a part for the system of producing CTA.The detailed description of the invention of present disclosure is the improvement to existing technique.Described system comprises primary oxidation reactor and secondary oxidation reactor.In brief, adopt described primary oxidation reactor and described secondary oxidation reactor to form terephthalic acid (TPA) by oxidation reaction, described oxidation reaction comprises paraxylene, acetic acid, catalyst (such as cobalt and/or manganese compound or other heavy metal, the lanthanide series of such as vanadium, chromium, iron, molybdenum, such as cerium, zirconium, hafnium and/or nickel and oxidation accelerator) and air.The relative weight percents of each component adopted in the liquid phase is the paraxylene of about 10 to 25, the acetic acid aqueous solution of about 74 to 90, the catalyst of about 0.1 to 1, and about 4.5 times of paraxylene mass flow described in the flow-rate ratio of described air (for normal atmospheric, there is not oxygen concentration or dilution).Initial oxidation reaction is there is in described primary oxidation reactor, produce waste gas (being also referred to as " primary exhaust ") and slurry (being also referred to as " elementary slurry "), described pulp bales contains described reactant, reaction intermediate and product, and described slurry is transmitted (such as flow or otherwise move) to described secondary oxidation reactor.Another oxidation reaction is there is, to form slurry (being also referred to as " secondary slurry ") and waste gas (being also referred to as " secondary waste gas ") in described secondary oxidation reactor.Described secondary slurry is processed with the terephthalic acid (TPA) producing purifying further.
Described primary exhaust is transmitted (such as adopt pipe or transmission member flowing or otherwise transmit) to elementary heat recovery system, and described secondary waste gas is transferred into secondary heat recovery system.Described elementary and secondary heat recovery system using the removing of the heat of described waste gas and by with accept the water of fluid or steam as heat and as the condensate flow exchanged heat of liquid to produce steam.The remainder of exhaust gas of each from described elementary heat recovery system and described secondary heat recovery system is transferred into described vapor wash system.Described vapor wash system process remainder of exhaust gas stream, to produce the liquid and steam that can be further processed.
Described primary oxidation reactor can operate under the pressure of about 12 to 18barA, and in one embodiment, operate under the pressure of about 16barA, and the temperature of described primary oxidation reactor can be about 180 to 210 DEG C, and in one embodiment, temperature is about 200 DEG C.The pressure being less than 2bar lower than the pressure of described primary oxidation reactor and pressure more than 1bar lower than the pressure of described primary oxidation reactor, and operate described secondary oxidation reactor at the temperature of at the temperature of about 5-15 lower than the temperature of described primary oxidation reactor DEG C or in one embodiment (when described primary oxidation reactor is about 200 DEG C) about 192 DEG C.
Because the minimizing of the Pressure Drop between described primary oxidation reactor and described secondary oxidation reactor is less than 2bar, the remainder of exhaust gas flowed out from described elementary heat recovery system can combine with the waste gas flowed out from described secondary heat recovery system, to flow to single vapor wash system.But in order to make described embodiment successful implementation, the Pressure Drop running through described elementary heat recovery system also must increase.Increasing the benefit running through the Pressure Drop of described elementary heat recovery system is the heat transfer coefficient enlarging markedly heat exchanger in described elementary heat recovery system.This reduce the size of described heat exchanger, thus decrease the Capital expenditure in described elementary heat recovery system.Because described heat recovery system is normally made up of the expensive corrosion resistant material of such as titanium, therefore the reduction of cost of investment is significant.
Usually, described elementary and secondary oxidation reactor can be built into or adopt described corrosion resistant material as liner by the corrosion resistant material of such as titanium separately.Because described oxidation reaction is implemented at the pressure raised, each oxidation reactor can be built into the high pressure that can stand described oxidation reaction and adopt.In addition, stir the content of described oxidation reactor, make described oxidation reaction optimization, also make described solid reaction product remain in suspension.Agitator comprises the configuration of specific fluid chemical field, and described oxidation reactor can be equipped with one or more mechanical agitator.Terephthaldehyde's acid crude (solid reaction product produced by described oxidation reaction) leaves this two oxidation reactors with the form of such as oxidation reaction slurry along output line, and described oxidation reaction slurry comprises the mixture of terephthalic acid (TPA) crude product, water, acetic acid, catalyst metals, oxidation reaction intermediate and byproduct of reaction.
Described elementary heat recovery system comprises at least one condenser, wherein each condenser condenses part waste gas produce (raise) steam.In one embodiment, described primary exhaust is transferred into gas line, and described primary exhaust is transferred to a series of condenser by described gas line.In one embodiment, first condenser produces the steam (such as at about 145 DEG C and 4.5barA) of the first pressure, described second condenser produces the steam (such as at about 130 DEG C and 3barA) of the second pressure, and the 3rd condenser produces the steam (such as at about 100 DEG C and 1barA) of the 3rd pressure.Other embodiment can comprise the condenser greater or less than three, operates under the temperature and pressure that described condenser can adapt in the quantity with condenser.
Described secondary heat recovery system can comprise at least one heat exchanger, described heat exchanger by Heat transmission to heat-transfer fluid.In one embodiment, described heat exchanger serves as condenser, and the condensation described waste gas of a part also produces steam.Described steam can be applied in other place in the process, and can also produce power.In one embodiment, the initial heat exchanger serving as condenser can produce the steam of about 130 DEG C and about 3barA.
Described vapor wash system operates under about 40-50 DEG C and about 9-15barA, it optionally comprises the condensate from described elementary and secondary heat recovery system one or both of is carried out to degassed system, reclaims the system of volatile organic matter (such as methyl acetate, paraxylene etc.), and is preserved for the liquid of the washing in described vapor wash system and discharges the system of residual gas.The assembly of described washing system is well known in the art.Described wash liquid can comprise acetic acid and water, and their combination.Described vapor wash system comprises at least one scrubbing section.
Usually, comprise for the production of an embodiment of the method for CTA that use is described comprises the elementary and system for the treatment of terephthalic acid (TPA) that is secondary oxidation reactor herein.Such as the reactant of paraxylene, acetic acid, catalyst and air is introduced in described primary oxidation reactor.Described primary oxidation reactor can be operated, to produce elementary slurry at the temperature (or at other temperature described in the invention or pressure) of the pressure of about 12 to 18barA and about 180 to 210 DEG C.Then described elementary slurry is introduced in described secondary oxidation reactor.Described secondary oxidation reactor is operated, to produce secondary slurry at the pressure than the low 2bar of being less than of the pressure of described primary oxidation reactor and the temperature (or at other temperature described in the invention or pressure) at about 5-15 lower than the temperature of described primary oxidation reactor DEG C.
As mentioned above, during described oxidation reaction, primary exhaust is produced from described primary oxidation reactor.Described primary exhaust flow to described elementary heat recovery system, to produce treated primary exhaust.Described treated primary exhaust flow to described vapor wash system, here washs described treated primary exhaust.Described elementary heat recovery system and described vapor wash system and described operating condition describe above.
As mentioned above, during described oxidation reaction, secondary waste gas is produced from described secondary oxidation reactor.Described secondary waste gas streams is described secondary heat recovery system extremely, to produce treated secondary waste gas.Described treated secondary waste gas streams, to described vapor wash system, here washs described treated secondary waste gas.Described secondary heat recovery system and described vapor wash system and described operating condition describe above.
Described elementary heat recovery system carries out heat exchange by adopting one or more heat exchanger, removes the heat of described primary exhaust.When described waste gas flows through each heat exchanger, the temperature of described waste gas reduces, and the elementary condensate formed as the liquid phase be separated, described elementary condensate comprises volatile organic matter and aqueous components, such as acetic acid, paraxylene, reaction intermediate and water.Collect described elementary concentrate liquid, and described oxidation reactor can be recycled to, carry out purifying to remove accessory substance and water, or be sent back to other place of described preparation technology as required.
Described secondary heat recovery system carries out heat exchange by adopting one or more heat exchanger, removes the heat of described secondary waste gas.When described waste gas flows through each heat exchanger, the temperature of described waste gas reduces, and the B-grade condensation thing formed as the liquid phase be separated, described B-grade condensation thing comprises volatile organic matter and aqueous components, such as acetic acid, paraxylene, reaction intermediate and water.Collect described secondary concentration thing liquid, and described oxidation reactor can be recycled to, carry out purifying to remove accessory substance and water, or be sent back to other place of described preparation technology as required.
For traditional reaction system, such as system as shown in Figure 1, described treated primary exhaust washs in steam washer, and described through washing, treated waste gas streams to energy-recuperation system advantageously to reclaim merit, such as adopt turbine to reduce the pressure of described gas.But treated secondary waste gas streams to independent steam washer, and is disposed in air subsequently.As shown in Figure 2, the advantage of the embodiment of present disclosure be utilize described through washing, treated secondary waste gas and described through washing, treated primary exhaust with the embodiment of the improvement recovered energy.In addition, only need a vapor wash system to wash described elementary and secondary waste gas streams, cause cost of investment to reduce.
It should be pointed out that all various assemblies that Fig. 2 may adopt not included in each system, method or technique.Such as, one or more hydraulic pump can be adopted, flow through described system or technique to cause described stream with one or more flow velocitys with under one or more pressure.
Embodiment
In Table 1, the calculating of the even load (equivalentduty) that the total surface area giving described elementary heat recovery heat exchanger significantly reduces is compared, this demonstrate need for the manufacture of described heat exchanger costliness, the surprising minimizing of the quantity of corrosion resistant material.
The comparison of table 1 process equipment project
| Embodiment 1 | Comparing embodiment | |
| Elementary heat recovery heat exchanger area (m 2） | 6913 | 9106 |
| The pressure drop (bar) of heat exchanger | 0.93 | 0.41 |
| Steam washer | 1 | 2 |
| Steam washer floss hole | Lead to energy regenerating | Lead to energy regenerating and air |
Be to be noted that ratio, concentration, quantity and other numeric data can range format represent in this article.Be understood that, for convenience for purpose of brevity, adopt this range format, therefore described range format should be explained with flexi mode, not only to comprise the numerical value of the boundary being explicitly described as described scope, also comprise and be included in all single numerical value in described scope or subrange, as clearly describing each numerical value and subrange.Illustratively, the concentration range of " about 0.1% to about 5% " should be interpreted as the concentration not only comprising the described about 0.1wt% clearly described to about 5wt%, also be included in the single concentration (such as 1%, 2%, 3% and 4%) in described indicating range and described subrange (such as, 0.5%, 1.1%, 2.2%, 3.3% and 4.4%).Term " about " can comprise the numerical value be modified ± 1%, ± 2%, ± 3%, ± 4%, ± 5%, ± 8% or ± 10%.In addition, term " about ' x ' is to ' y ' " comprises " about ' x ' to about ' y ' ".
Multiple change and modification can be carried out to above-mentioned embodiment.Protected by the claims of enclosing in the scope that all these are modified and change is intended to be included into present disclosure.
Claims (7)
1. a system, it comprises:
Primary oxidation reactor, wherein at the temperature of the pressure of about 12 to 18barA and about 180 to 210 DEG C, operate described primary oxidation reactor, wherein said primary oxidation reactor is communicated with elementary heat recovery system, and wherein said elementary heat recovery system is communicated with vapor wash system; With
Secondary oxidation reactor, wherein at the pressure than the low 2bar of being less than of the pressure of described primary oxidation reactor and operate described secondary oxidation reactor at the temperature of about 5-15 lower than the temperature of described primary oxidation reactor DEG C, the slurry wherein produced in described primary oxidation reactor is transferred into described secondary oxidation reactor, wherein said secondary oxidation reactor is communicated with secondary heat recovery system, and wherein said secondary heat recovery system is communicated with described vapor wash system.
2. the system as claimed in claim 1, wherein said elementary heat recovery system comprises at least one condensation described waste gas of a part and produces the condenser of steam.
3. system as claimed in claim 1 or 2, wherein said secondary heat recovery system comprises at least one heat exchanger, and heat is sent to heat-transfer fluid by described heat exchanger.
4. the system according to any one of claim 1,2 or 3, wherein said vapor wash system comprises at least one and optionally carries out degassed system to from the condensate in described elementary and secondary heat recovery system one or both of, reclaim the system of volatile organic matter, be preserved for the system of the liquid of the washing in described vapor wash system, and for discharging the system of residual gas.
5., for the production of a method for terephthalic acid (TPA), it comprises:
There is provided primary oxidation reactor, wherein said primary oxidation reactor is communicated with elementary heat recovery system, and wherein said elementary heat recovery system is communicated with vapor wash system;
There is provided secondary oxidation reactor, wherein said secondary oxidation reactor is communicated with secondary heat recovery system, and wherein said secondary heat recovery system is communicated with described vapor wash system;
Paraxylene, acetic acid, catalyst and air are incorporated in described primary oxidation reactor;
Described primary oxidation reactor is operated to produce the first slurry at the temperature of the pressure of about 12 to 18barA and about 180 to 210 DEG C;
Described first slurry produced in described primary oxidation reactor is incorporated in described secondary oxidation reactor; With
At the pressure than the low 2bar of being less than of the pressure of described primary oxidation reactor and operate described secondary oxidation reactor, to produce the second slurry at the temperature of about 5-15 lower than the temperature of described primary oxidation reactor DEG C.
6. method as claimed in claim 5, it comprises further:
Primary exhaust is produced from described primary oxidation reactor;
Described primary exhaust is made to flow to described elementary heat recovery system, to produce treated primary exhaust; With
Described treated primary exhaust is made to flow to described vapor wash system.
7. the method according to any one of claim 5 or 6, it comprises further:
Secondary waste gas is produced from described secondary oxidation reactor;
Described secondary waste gas is made to flow to described secondary heat recovery system, to produce treated secondary waste gas; With
Described treated secondary waste gas is made to flow to described vapor wash system.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US28695709P | 2009-12-16 | 2009-12-16 | |
| US61/286957 | 2009-12-16 | ||
| CN201080056879.1A CN102652122B (en) | 2009-12-16 | 2010-12-15 | Produce the system and method for aromatic carboxylic acid |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201080056879.1A Division CN102652122B (en) | 2009-12-16 | 2010-12-15 | Produce the system and method for aromatic carboxylic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105413598A true CN105413598A (en) | 2016-03-23 |
| CN105413598B CN105413598B (en) | 2019-04-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510525883.2A Active CN105413598B (en) | 2009-12-16 | 2010-12-15 | The system and method for producing aromatic carboxylic acids |
| CN201080056879.1A Active CN102652122B (en) | 2009-12-16 | 2010-12-15 | Produce the system and method for aromatic carboxylic acid |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN201080056879.1A Active CN102652122B (en) | 2009-12-16 | 2010-12-15 | Produce the system and method for aromatic carboxylic acid |
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| CN (2) | CN105413598B (en) |
| WO (1) | WO2011084472A2 (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1395554A (en) * | 2000-01-21 | 2003-02-05 | Bp北美公司 | Process for production of high purity aromatic carboxylic acid by oxidation in benzoic acid and water solvent |
| WO2008105085A1 (en) * | 2007-02-28 | 2008-09-04 | Hitachi Plant Technologies, Ltd. | Method of oxidation reaction flue gas treatment and energy recovery |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5612007A (en) * | 1994-10-14 | 1997-03-18 | Amoco Corporation | Apparatus for preparing aromatic carboxylic acids with efficient energy recovery |
| US6500969B1 (en) * | 2000-12-08 | 2002-12-31 | Hydrocarbon Technologies, Inc. | Integrated hydrogen peroxide production and organic chemical oxidation |
| EP1349825B1 (en) * | 2001-01-10 | 2005-10-19 | E.I. Du Pont De Nemours And Company | Improved process for producing carboxylic acids |
-
2010
- 2010-12-15 CN CN201510525883.2A patent/CN105413598B/en active Active
- 2010-12-15 CN CN201080056879.1A patent/CN102652122B/en active Active
- 2010-12-15 WO PCT/US2010/060488 patent/WO2011084472A2/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1395554A (en) * | 2000-01-21 | 2003-02-05 | Bp北美公司 | Process for production of high purity aromatic carboxylic acid by oxidation in benzoic acid and water solvent |
| WO2008105085A1 (en) * | 2007-02-28 | 2008-09-04 | Hitachi Plant Technologies, Ltd. | Method of oxidation reaction flue gas treatment and energy recovery |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2011084472A3 (en) | 2011-10-20 |
| CN102652122A (en) | 2012-08-29 |
| CN102652122B (en) | 2015-09-09 |
| CN105413598B (en) | 2019-04-09 |
| WO2011084472A2 (en) | 2011-07-14 |
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