CN102924266A - Method for preparing phthalic acid by xylol co-oxidation catalyst system - Google Patents
Method for preparing phthalic acid by xylol co-oxidation catalyst system Download PDFInfo
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- CN102924266A CN102924266A CN201210418909XA CN201210418909A CN102924266A CN 102924266 A CN102924266 A CN 102924266A CN 201210418909X A CN201210418909X A CN 201210418909XA CN 201210418909 A CN201210418909 A CN 201210418909A CN 102924266 A CN102924266 A CN 102924266A
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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
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- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The invention relates to a method for preparing phthalic acid by a xylol co-oxidation catalyst system. The method comprises that air or oxygen-rich air as an oxidant undergoes a liquid-phase oxidation reaction at a temperature of 160 to 210 DEG C under the pressure of 0.5 to 2.0MPa in the presence of the traditional Co-Mn-Br catalyst added with a transition metal cocatalyst and/or an imide cocatalyst, and acetic acid as a solvent to produce mixed phthalic acid-containing slurry; and the mixed phthalic acid-containing slurry is subjected to separation refining. Through the transition metal cocatalyst, a reaction rate is improved. Through the imide cocatalyst, a use amount of strongly corrosive bromide ions is reduced. M-phthalic acid and p-phthalic acid can be directly used for copolyester production without separation so that a xylene separation cost is reduced. The method can be used basically without a change of the existing p-xylene oxidation device. The method has a fast oxidation reaction rate, is conducive to improvement of a device production capacity, has a low bromide use amount, reduces equipment corrosion, an equipment investment and an operation cost, and reduces environmental pollution produced by bromides.
Description
Technical field
The present invention relates to field of chemical technology, particularly brightly relate to the method that a kind of catalyst system by the xylol co-oxidation prepares phthalic acid.
Background technology
Phthalic acid is the important source material of producing polyester, and wherein terephthalic acid has the call mainly for the production of polyethylene terephthalate; M-phthalic acid then can be used as the 3rd monomer and terephthalic acid together with the ethylene glycol copolymerization to produce copolyesters; Phthalic acid is mainly for the production of phthalic anhydride.
At present the production method of these three kinds of carboxylic acids mainly is respectively take each self-corresponding high purity xylene isomer as raw material, and acetic acid is solvent, 150 ℃ ~ 220 ℃ of temperature, under pressure 0.5 ~ 2.5MPa, obtains through the oxygen-containing gas liquid-phase oxidation.Three's oxidizing process process is closely similar, and the catalyst system therefor main body is the Co-Mn-Br catalyst system.
Because the boiling point of three kinds of xylene isomers is very approaching, therefore by the xylol high-purity to,, the o-Xylol isomer, usually adopt low temperature crystallization to separate or molecular sieve adsorption is separated, cost is very high.After isolating p-Xylol, the mixture of position and ortho isomer carries out isomerization reaction between inciting somebody to action again, and making it Partial Conversion is p-Xylol, separates again, and iterative cycles like this is to produce to greatest extent p-Xylol.
Although can produce m-phthalic acid with pure m-xylene oxidation, but the main application of m-phthalic acid is to carry out copolymerization with terephthalic acid, the preparation copolyesters if just carry out co-oxidation before separation of Xylene Isomer, then can reduce the running cost of separation of Xylene Isomer.Because the dissolubility difference of the pure mixed phthalic acid that obtains after the oxidation is very large, therefore after can separating phthalic acid, the m-phthalic acid and the terephthalic acid that mix are directly carried out copolymerization, and also further Crystallization Separation obtains respectively the sterling of three kinds of phthalic acid isomer.
CN1962598A provides a kind of method of producing benzene dicarboxylic acid by mixed dimethylbenzene cooxidation, adopts traditional Co-Mn-Br catalyst system, but does not add promotor.Its reaction time is relatively long, and the bromide content in the catalyst system is higher, can be more serious to the corrodibility of equipment.
The CN1314878A proposition is a kind of to separate pure terephthalic acid and the method for m-phthalic acid from xylol co-oxidation product slurry, but does not relate to xylol oxidation catalyst system therefor system and oxidation reaction process.
Existing patent is used for transition metal and imide analog compounds the oxidising process of p-Xylol, but does not find these auxiliary agents are used for the report of xylol co-oxidation reaction.
Summary of the invention
The object of the present invention is to provide a kind of catalyst system of xylol co-oxidation to prepare the method for phthalic acid.Namely in traditional Co-Mn-Br catalyst system, introduce transition metal and/or the new catalyst system of imide analog compounds promotor formation.
The adding of promotor can increase reactive behavior, improves speed of reaction, reduces the consumption of former catalyst system bromide, and the reduction of bromine can greatly reduce the corrosion to equipment.
Concrete technical scheme of the present invention is as follows:
A kind of catalyst system by the xylol co-oxidation prepares the method for phthalic acid, it is characterized in that in traditional Co-Mn-Br catalyzer, introducing transition metal co-catalyst and/or acid imide promotor, take air or oxygen-rich air as oxygenant, acetic acid is solvent, 160 ℃ ~ 210 ℃ of temperature, under the condition of pressure 0.5MPa ~ 2.0MPa, obtain containing the slurry that mixes phthalic acid through liquid phase oxidation reaction, then carry out separation and purification.
The mass ratio of described acetic acid and xylol is 3 ~ 6:1, and the mass content of water is 8% ~ 15% in the reaction system; The addition of transition metal ion is 0.001% ~ 0.1% of xylol in the reaction system, water and solvent acetic acid total mass; Preferred 0.003% ~ 0.05%.The consumption of imide analog compounds is 0.005% ~ 0.1% of xylol, water and solvent acetic acid total mass.
Described imide analog compounds is selected from a kind of in the following compounds at least: HP, N-hydroxyl tetrabromo phthalimide, N-hydroxyl tetrachloro-phthalimide, N-hydroxyl divinyl imines, N-hydroxyl-1,8-naphthalimide, N-hydroxyl maleimide, 1,3,5-trihydroxy-tricarbimide, N-acetoxyl group phthalic imidine.
Mixed slurry can adopt traditional separation method, also can adopt the method for CN1962598A to separate, make with extra care: the separable thick product of pure mixed phthalic acid that obtains, obtain again the pure mixed phthalic acid product of polymerization-grade through hydrofining, be directly used in the production copolyester section; Also can obtain respectively terephthalic acid, m-phthalic acid and O-phthalic acid product through the multistage crystallization separating-purifying.
Pure mixed phthalic acid refers to three kinds or any two kinds mixture in terephthalic acid, m-phthalic acid and the phthalic acid.
The transistion metal compound of introducing in the catalyst system of the present invention comprises oxide compound, organic salt or the inorganic salts of Zr, Hf, Ti, Ce metal, the compound of preferred Zr, particularly preferably acetic acid zirconium.
In the described catalyst system, the addition of transition metal ion is 0.001% ~ 0.1% of xylol in the reaction system, water and solvent acetic acid total mass,
Described imide analog compounds is selected from a kind of in the following compounds at least: HP, N-hydroxyl tetrabromo phthalimide, N-hydroxyl tetrachloro-phthalimide, N-hydroxyl divinyl imines, N-hydroxyl-1,8-naphthalimide, N-hydroxyl maleimide, 1,3,5-trihydroxy-tricarbimide, N-acetoxyl group phthalic imidine.
Wherein in traditional Co-Mn-Br catalyzer, the atomic ratio of preferred Co/Mn is that 0.4 ~ 10, Br/ (Co+Mn) atomic ratio is that 0.1 ~ 1.5, Co, Mn, three kinds of ions of Br account for 0.06% ~ 0.2% of xylol in the reaction system, water and solvent acetic acid total mass.
Among the present invention, used oxidation reactor can be batch stirred tank reactor, continuous bubbling tower reactor or semicontinuous stirred-tank reactor.
Among the present invention, gained pure mixed phthalic acid slurry can obtain the pure mixed phthalic acid product by solid-liquid separation, also can through the multistage crystallization separating-purifying obtain respectively to,, the phthalic acid product at ortho position.After for example phthalic acid can being separated, the m-phthalic acid that obtains mixing and terephthalic acid are directly used in the preparation copolyesters.
Basic fundamental thinking of the present invention is: introduce transition metal and/or acid imide promotor in traditional Action In The Liquid Phase Oxidation of Xylene catalyst system, be used for xylol liquid phase co-oxidation and prepare phthalic acid.Add transition metal co-catalyst to improve speed of reaction, add the consumption that the acid imide promotor has reduced the strong bromide anion of corrodibility.M-phthalic acid can be directly used in co-polyester production without separating with terephthalic acid, thereby reduces dimethylbenzene lock out operation cost.Technology of the present invention can be used on the basis of substantially not changing existing p xylene oxidation device.
Advantage of the present invention is: oxidizing reaction rate is fast, is conducive to improve device capbility; The consumption of bromide is low, reduces equipment corrosion, reduces facility investment and running cost, alleviates bromide to the pollution of environment.
Embodiment:
The below is elaborated to the method that the present invention proposes with embodiment, but and does not limit the present invention in any way.
Embodiment 1
Adopt 2L continuous bubbling tower reactor, the liquid starting material proportioning sees Table 1, liquid feed rate is 17g/min, air feed speed 10L/min, 186 ℃ ~ 188 ℃ of temperature of reaction, pressure 1.1MPa, the residence time is 45min, the total conversion rate of BTX aromatics is 99.6%, and the overall selectivity of pure mixed phthalic acid is 96.5%, and the ratio of terephthalic acid and m-phthalic acid is 2:1, tail gas oxygen concn 3.2%, tail gas CO
2Concentration 1.2%.
Table 1. oxidizing reaction liquid proportioning raw materials
Annotate: PX-p-Xylol in the table, the MX-m-xylene, lower same
Embodiment 2
In catalyzer, do not add the zirconium, other proportioning raw materials is all identical with embodiment 1 with feeding rate, 186 ℃ ~ 188 ℃ of temperature of reaction, pressure 1.1MPa, the residence time is 60min, the total conversion rate of BTX aromatics is 99.5%, and the overall selectivity of pure mixed phthalic acid is 96.0%, and the ratio of terephthalic acid and m-phthalic acid is 2:1, tail gas oxygen concn 3.5%, tail gas CO
2Concentration 1.0%.
Comparative example 1
Except not adding zirconium, N-hydroxyl-1 in the catalyzer, beyond the 8-naphthalimide, other proportioning raw materials and feeding rate are all with embodiment 1,186 ℃ ~ 188 ℃ of temperature of reaction, pressure 1.1MPa, the residence time is 100min, the total conversion rate of BTX aromatics is 98%, the overall selectivity of pure mixed phthalic acid is 88.0%, the ratio of terephthalic acid and m-phthalic acid is 2:1, tail gas oxygen concn 6.2%, tail gas CO
2Concentration 0.87%.
Comparative example 2
Except the Br consumption be 0.09% other proportioning raw materials and feeding rate all with comparative example 1,186 ℃ ~ 188 ℃ of temperature of reaction, pressure 1.1MPa, the residence time is 70min, the total conversion rate of BTX aromatics is 99.3%, and the overall selectivity of pure mixed phthalic acid is 96.2%, and the ratio of terephthalic acid and m-phthalic acid is 2:1, tail gas oxygen concn 3.4%, tail gas CO
2Concentration 1.1%.
Embodiment 3
Adopt the 1L batch stirred tank reactor, the liquid starting material proportioning sees Table 2, in the disposable adding still of 500g liquid starting material, oxygen level is that 23% oxygen-rich air incoming stock speed is 5L/min, 180 ℃ ~ 183 ℃ of temperature of reaction, pressure 0.9MPa, the residence time is 80min, the total conversion rate of BTX aromatics is 97.6%, the overall selectivity of pure mixed phthalic acid is 93.5%, and wherein the ratio of terephthalic acid, m-phthalic acid and phthalic acid is 6.8:2.6:1.
Table 2. oxidizing reaction liquid proportioning raw materials
Annotate: be the OX-o-Xylol in the table
Comparative example 3
Still adopt the 1L batch stirred tank reactor, the liquid starting material proportioning is not except adding Zr, not adding 1,3, outside the 5-trihydroxy-tricarbimide promotor, other proportioning raw materials and reaction conditions are with embodiment 3, reaction result is that the total conversion rate of xylol is 85.3%, and the overall selectivity of pure mixed phthalic acid is 82.4%, to,, the ratio of three kinds of isomer of phthalic acid is 6.8:2.6:1.
Enforcement 4 ~ 9 and comparative example 4 ~ 6 all adopt 2L continuous bubbling tower reactor, and liquid feed rate is 17g/min, air feed speed 10L/min, and concrete data are listed in the table 3.
Reaction result under table 3. different condition
Claims (10)
1. the catalyst system by the xylol co-oxidation prepares the method for phthalic acid, it is characterized in that in traditional Co-Mn-Br catalyzer, introducing transition metal co-catalyst and/or acid imide promotor, take air or oxygen-rich air as oxygenant, acetic acid is solvent, 160 ℃ ~ 210 ℃ of temperature, under the condition of pressure 0.5MPa ~ 2.0MPa, obtain containing the slurry that mixes phthalic acid through liquid phase oxidation reaction, then carry out separation and purification.
2. the method for claim 1 is characterized in that the mass ratio of acetic acid and xylol is 3 ~ 6:1, and the mass content of water is 8% ~ 15% in the reaction system; The addition of transition metal ion is 0.001% ~ 0.1% of xylol in the reaction system, water and solvent acetic acid total mass; The consumption of imide analog compounds is 0.005% ~ 0.1% of xylol, water and solvent acetic acid total mass.
3. the method for claim 1 is characterized in that the transistion metal compound of introducing in the described catalyst system comprises oxide compound, organic salt or the inorganic salt of Zr, Hf, Ti, Ce metal.
4. the method for claim 1 is characterized in that transistion metal compound is the compound of Zr.
5. the method for claim 1 is characterized in that transistion metal compound is the acetic acid zirconium.
6. method as claimed in claim 2, the addition that it is characterized in that transition metal ion is 0.003% ~ 0.05%.
7. the method for claim 1, it is characterized in that described imide analog compounds is selected from a kind of in the following compounds at least: HP, N-hydroxyl tetrabromo phthalimide, N-hydroxyl tetrachloro-phthalimide, N-hydroxyl divinyl imines, N-hydroxyl-1,8-naphthalimide, N-hydroxyl maleimide, 1,3,5-trihydroxy-tricarbimide, N-acetoxyl group phthalic imidine.
8. the method for claim 1 is characterized in that described xylol refers to three kinds or any two kinds mixture in p-Xylol, m-xylene and the o-Xylol.
9. the method for claim 1, the atomic ratio that it is characterized in that described Co/Mn is 0.4 ~ 10, Br/ (Co+Mn) atomic ratio is that 0.1 ~ 1.5, Co, Mn, three kinds of ions of Br account for 0.06% ~ 0.2% of xylol in the reaction system, water and solvent acetic acid total mass.
10. method according to claim 1 is characterized in that oxidation reactor is batch stirred tank reactor, continuous bubbling tower reactor or semicontinuous stirred-tank reactor.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104107722A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Catalyst used for allyl acetate synthesis |
| CN105152906A (en) * | 2015-09-29 | 2015-12-16 | 衢州群颖化学科技有限公司 | Method for co-producing 3,5-dimethylbenzoic acid and trimesic acid |
| CN105348067A (en) * | 2015-09-29 | 2016-02-24 | 衢州群颖化学科技有限公司 | Co-production method for methyl benzoic acid and phthalic acid |
| CN107175128A (en) * | 2016-03-11 | 2017-09-19 | 中国石油化工股份有限公司 | Liquid phase oxidation prepares the catalyst of aromatic multi-carboxy acid |
| CN108299182A (en) * | 2018-02-02 | 2018-07-20 | 中国石油化工股份有限公司 | A kind of method that meta-xylene and paraxylene mixed oxidization prepare phthalic acid |
| CN109876849A (en) * | 2017-12-06 | 2019-06-14 | 中国科学院大连化学物理研究所 | A kind of naphthalene liquid phase oxidation preparation 1,4- naphthoquinones catalyst and its preparation method and application |
| CN114249675A (en) * | 2020-09-22 | 2022-03-29 | 北京颖泰嘉和生物科技股份有限公司 | Preparation method of 2-nitro-4-methylsulfonylbenzoic acid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5412339A (en) * | 1977-06-27 | 1979-01-30 | Toyobo Co Ltd | Preparation of aromatic dicarboxylic acids |
| CN1865214A (en) * | 2006-06-20 | 2006-11-22 | 扬子石油化工股份有限公司 | Method for producing aromatic carboxylic acid using nitrogen oxide as catalytic additive |
| CN1958552A (en) * | 2006-08-18 | 2007-05-09 | 中国石油化工股份有限公司 | Method for producing aromatic carboxylic acid |
-
2012
- 2012-10-26 CN CN201210418909XA patent/CN102924266A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5412339A (en) * | 1977-06-27 | 1979-01-30 | Toyobo Co Ltd | Preparation of aromatic dicarboxylic acids |
| CN1865214A (en) * | 2006-06-20 | 2006-11-22 | 扬子石油化工股份有限公司 | Method for producing aromatic carboxylic acid using nitrogen oxide as catalytic additive |
| CN1958552A (en) * | 2006-08-18 | 2007-05-09 | 中国石油化工股份有限公司 | Method for producing aromatic carboxylic acid |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104107722A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Catalyst used for allyl acetate synthesis |
| CN104107722B (en) * | 2013-04-16 | 2016-05-18 | 中国石油化工股份有限公司 | For the synthetic catalyst of allyl acetate |
| CN105152906A (en) * | 2015-09-29 | 2015-12-16 | 衢州群颖化学科技有限公司 | Method for co-producing 3,5-dimethylbenzoic acid and trimesic acid |
| CN105348067A (en) * | 2015-09-29 | 2016-02-24 | 衢州群颖化学科技有限公司 | Co-production method for methyl benzoic acid and phthalic acid |
| CN105152906B (en) * | 2015-09-29 | 2017-07-28 | 江西科苑生物药业有限公司 | A kind of method of the mesitylenic acid of coproduction 3,5 and trimesic acid |
| CN107175128A (en) * | 2016-03-11 | 2017-09-19 | 中国石油化工股份有限公司 | Liquid phase oxidation prepares the catalyst of aromatic multi-carboxy acid |
| CN107175128B (en) * | 2016-03-11 | 2020-04-17 | 中国石油化工股份有限公司 | Catalyst for preparing aromatic polycarboxylic acid by liquid phase oxidation |
| CN109876849A (en) * | 2017-12-06 | 2019-06-14 | 中国科学院大连化学物理研究所 | A kind of naphthalene liquid phase oxidation preparation 1,4- naphthoquinones catalyst and its preparation method and application |
| CN109876849B (en) * | 2017-12-06 | 2020-08-11 | 中国科学院大连化学物理研究所 | 1, 4-naphthoquinone catalyst prepared by liquid-phase oxidation of naphthalene and preparation method and application thereof |
| CN108299182A (en) * | 2018-02-02 | 2018-07-20 | 中国石油化工股份有限公司 | A kind of method that meta-xylene and paraxylene mixed oxidization prepare phthalic acid |
| CN114249675A (en) * | 2020-09-22 | 2022-03-29 | 北京颖泰嘉和生物科技股份有限公司 | Preparation method of 2-nitro-4-methylsulfonylbenzoic acid |
| CN114249675B (en) * | 2020-09-22 | 2023-11-21 | 北京颖泰嘉和生物科技股份有限公司 | Preparation method of 2-nitro-4-methylsulfonyl benzoic acid |
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Application publication date: 20130213 |