GB2106797A - Process and apparatus for producing terephthalic acid by liquid phase oxidation of paraxylene - Google Patents
Process and apparatus for producing terephthalic acid by liquid phase oxidation of paraxylene Download PDFInfo
- Publication number
- GB2106797A GB2106797A GB08226863A GB8226863A GB2106797A GB 2106797 A GB2106797 A GB 2106797A GB 08226863 A GB08226863 A GB 08226863A GB 8226863 A GB8226863 A GB 8226863A GB 2106797 A GB2106797 A GB 2106797A
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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
- B01J19/0053—Details of the reactor
- B01J19/0066—Stirrers
-
- 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
-
- 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
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00182—Controlling or regulating processes controlling the level of reactants in the reactor vessel
-
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
Terephthalic acid with good qualities is continuously produced by liquid phase oxidation of paraxylene with a molecular oxygen-containing gas in acetic acid as a solvent in the presence of a catalyst containing cobalt, manganese, and bromine in a low percent acetic acid combustion by supplying 2 to 50 parts by weight of water per 100 parts by weight of the paraxylene into a vertical cylindrical reactor with a vertical stirrer having at least one stirring blade means, at a level in the zone between (1) the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means, and (2) the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor, supplying a feed solution comprising the paraxylene, the acetic acid and the catalyst, and the molecular oxygen-containing gas to the level in the said zone, while maintaining a water concentration of reaction solution at 5 to 20% by weight and a reaction temperature of 195 DEG to 225 DEG C.
Description
SPECIFICATION
Process and apparatus for producing terephthalic acid by liquid phase oxidation of paraxylene
This invention relates to a process and an apparatus for continuously producing terephthalic acid by liquid phase oxidation of paraxylene with a molecular oxygen-containing gas in acetic acid as a solvent in the presence of a catalyst containing cobalt, manganese, and bromine with reduced loss of acetic acid by combustion due to the oxidation of paraxylene.
The process for producing terephthalic acid by liquid phase oxidation of paraxylene with a molecular oxygen-containing gas in acetic acid as a solvent in the presence of a catalyst containing cobalt, manganese and bromine is known as SD process and is commercially widely utilized. However, loss of acetic acid due to its oxidation and decomposition which occurs in the oxidation process of paraxylene is inevitable in the process. Thus, reduction in such loss will not only lower the production cost of terephthalic acid, but will also greatly contribute to resource saving.
From such economical viewpoint, many attempts have been so far made for reducing the solvent loss. For example, Japanese Laid-Open Patent Applications Nos. 133347/74, 32140/75, 127033/76, 1 27034/76, 127035/76, 77023/77, and 51035/80 propose catalyst compositions; Japanese Laid-Open Patent Application
No.91221/76 proposes a process for using a strong acid such as phosphoric acid,etc. as an additive;
Japanese Laid-Open Patent Applications No. 109939/79 and Japanese Patent Publication No. 14098/79 propose structures of reactors and reaction systems;Japanese Laid-Open Patent Application No.90135/79 proposes a process for replacing a reaction mother liquor at a high temperature; and Japanese Patent
Publication No.21014/81 proposes a process relating to the concentration of terephthalic acid in a reaction product slurry. Furthermore, Japanese Laid-Open Patent Applications Nos. 127037/76,3030/77, 77022/77, 79836/78, 52049/79, 7235/79 and Japanese Patent Publication No. 21015/81 propose catalyst concentrations and water concentration for optimizing reaction conditions. Considerable successes have been obtained according to these proposed measures, but no satisfactory effect has been obtained yet on prevention of the acetic acid as a solvent from combustion in most of these proposed measures.
Under these situations, the present inventors have made extensive studies on the effect of water in a reaction solution, which has not been an established theory as yet among the so far well known cases, and have found that the water in the reaction solution has (1) afunction of relaxing an over-reaction in paraxylene oxidation, and (2) a function of suppressing oxidation and decomposion of acetic acid as the solvent, thereby reducing the combustion loss, and that it is effective to supply an appropriate amount of water to an appropriate position in a reactor to effectively perform these two functions.That is, the present inventors have found that the loss of acetic acid as a solvent due to its combustion can be reduced by materializing the findings in the structure or reactor, while keeping the quality of terephthalic acid constant, and have established the present invention.
The present invention provides a process for continuously producing terephthalic acid by liquid phase oxidation of paraxylene with a molecular oxygen-containing gas in acetic acid as a solvent in the presence of a catalyst containing cobalt, manganese and bromine, which comprises supplying 2 to 50 parts by weight of water per 100 parts by weight of the paraxylene into a vertical cylindrical reactor with a vertical stirrer having at least one stirring blade means at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor, supplying a feed solution comprising the paraxylene, the acetic acid and the catalyst, and the molecular oxygen-containing gas to the level in the said zone, while maintaining a water concentration of reaction solution at 5 to 20% by weight and a reaction temperature at 1950 to 225"C.
The present invention further provides an apparatus for continuous oxidation of paraxylene to terephthalic acid, which comprises a vertical cylindrical reactor provided with a vertical stirrer having at least one stirring blade means, and with a water inlet, a feed solution inlet and a molecular oxygen-containing gas inlet, each inlet being positioned at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor.
The reactor for use in the present invention must have such a structure as a vertical cylindrical reactor provided with a vertical stirrer having at least one stirirng blade means, and with a water inlet, a feed solution inlet and a molecular oxygen-containing gas inlet each inlet being positioned at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor. A preferable structure is that a reaction product outlet is provided in the reaction solution and above the upper end of lowest stirring blade means.The water inlet can be provided independently, as described above, but it can be provided as integrated with the molecular oxygen-containing gas inlet by connecting a water inlet line to a molecular oxygen-containing gas inlet line, or with the feed solution inlet by connecting a water inlet line to a feed solution inlet line just before the reactor.
The water to the reactor may be pure water, or by-product water containing acetic acid or other minor components from the reactor, for example, a condensate comprising acetic acid and water from an effluent gas condenser of the reactor. It is economically advantageous to use the by-product water.
The amount of water to the reactor is desirably 2 to 50 parts by weight per 100 parts by weight of the fed xylene, while the water concentration of the reaction solution is maintained at 5 to 20% by weight by withdrawal of reactor condensate.
Above 50 parts by weight of water, the inhibiting effect of water upon the reaction is considerable. This is economically disadvantageous.
The withdrawal of water from the reaction system is carried out by withdrawing a portion of condensate comprised mainly of water and acetic acid from an effluent gas condenser. Thus, the amount of condensate to be withdrawn is such as to maintain the water concentration of the reaction solution at 5 to 20% by weight according to the amount of water contained in the withdrawn condensate.
The water concentration of the reaction solution must be maintained at 5 to 20% by weight, preferably 10 to 20% by weight. Below 5% by weight, more combustion of acetic acid takes place, whereas above 20% by weight, the oxidation reaction is inhibited, and the quality of the resulting terephthalic acid is deteriorated.
The catalyst is the well known catalyst composition containing cobalt, manganese and bromine. The cobalt component includes, for example, cobalt acetate, cobalt naphthenate, cobalt bromide, etc., the manganese component includes, for example, manganese acetate, manganese naphthenate, manganese bromide, etc., and the bromine component includes, for example, 1,1 ,2,2-tetrabromoethane, hydrogen bromide, cobalt bromide, manganese bromide, etc. The catalyst concentration of reaction solution is 50 to 1,000 ppm by weight of Co, 50 to 1,000 ppm by weight of Mn, and 400 to 2,000 ppm by weight of Br in terms of atom, and can be appropriately selected in view of the quality of terephthalic acid.
The reaction temperatuer is 195"two 225"C, preferably 200 to 220"C. Below 195"C, more catalyst is required, whereas above 225"C, loss of acetic acid due to its oxidation and decomposition cannot be reduced, and this leads to economical disadvantages.
The reaction pressure must be such that the reaction solution can be kept substantially in liquid phase at the reaction temperature.
The molecular oxygen-containing gas to the reactor is usually air from the economical viewpoint, and pure oxygen or pure oxygen diluted with an inert gas to an appropriate degree can be also used.
The oxygen concentration in the effluent gas depends upon the reaction pressure, and usually is in a range of 0.5 to 7% by volume, and can be selected from the said range in view of the desired quality of terephthalic acid.
The present invention will be described in detail below, referring to the drawing showing one embodiment of the present invention.
Single Figure is a view of a reactor according to the present invention.
The necessary catalyst and solvent are charged into reactor 1, and pressurized and heated. Then, a molecular oxygen-containing gas is introduced into the reactor 1, through a feed gas inlet line 3 while stirring the mixture in the reactor 1, and at the same time, a feed solution consisting of paraxylene, the solvent and the catalyst is continuously supplied to the reactor 1 through a feed solution inlet line 4to carry out reaction.
The reaction produced is withdrawn through a reaction productwithdrawal line5so asto keep the liquid level 13 constant in the reactor 1.
Water can be supplied to the reactor 1 through an independent water inlet line, but can be also supplied thereto through the feed solution inlet line by connecting a water inlet line to the feed solution inlet line at a position just before the reactor or through the molecular oxygen containing gas inlet line by connecting the water inlet line to the said gas inlet line. In any way it is essential to provide a water inlet at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end 12 of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor.
The gas mixture comprising an oxidation off-gas, solvent vapor and water vapor is withdrawn from the reactor 1 through a gas mixture discharge line 6 and a condenser 7to a receiving tank 8. In the receiving tank 8, the oxidation off-gas is separated from the condensate of the solvent and the water. The oxidation off-gas is discharged through an off-gas discharge line 9, whereas a portion of the condensate is withdrawn from the receiving tank 8 through a condensate discharge line 10 and the remaining portion of the condensate is returned to the reactor 1 through a condensate reflux line 11.
The withdrawal rate of condensate is adjusted so that the water concentration of the reaction solution can be kept to 5 to 20% by weight, preferably 10 to 20% by weight.
According to the present invention, consumption ratio of acetic acid to productterephthalic acid (which will be hereinafter referred to as percent acetic acid combustion) is reduced and the process economy is considerably improved, when the major factors giving an influence on the quality of terephthalic acid, i.e., 4-carboxybenzaldehyde content (which will be hereinafter referred to as 4CBA content) and absorbancy of an alkaline solution at 340 m representing the amount of coloring impurities in terephthalic acid (which will be hereinafter referred to as OD 340) are substantially at equal levels. Thus, the present process has a high commercial significance.
The present invention will be described in detail, referring to Exampies and Comparative Example, where parts are by weight.
Example 1
Into a vertical cylindrical reactor provided with a vertical stirrer, a feed gas inlet line, a feed solution inlet
line, a reaction product withdrawal line, a gas mixture discharge line, a condenser, a condensate reflux line, a condensate discharge line, and off-gas discharge line, as shown in Figure were charged a feed solution consisting of 100 parts of paraxylene, 350 parts of acetic acid (water content: 10% by weight), 0.436 parts of cobalt acetate tetrahydrate, 0.859 parts of manganese acetate tetrahydrate, 0.454 parts of 1,1,2,2tetrabromoethane (that is, 295 ppm of Co, 550 ppm of Mn, and 1,200 ppm of Br per 350 parts of acetic acid)
per hour, as continuously admixed with 12.5 parts of water just before the reactor, through a feed solution
inlet line having an outlet to the reactor at a level near the bottom of the reactor, given in the following Table at the same time, air was introduced into the reactor through a feed gas inlet line having an outlet to the reactor at a level near the bottom of the reactor. Reaction was carried out at the reaction temperature of 210"C, the pressure of 19.5 kg/cm2 gauge, an average residence time of 45 minutes and an off-gas oxygen concentration of 1.5%.
Through the condensate withdrawal line 92.8 prts of condensate comprising water and acetic acid (water content: 43% by weight) was withdrawn per hour to keep the water concentration of the reaction solution at
14% by weight. The amount of water withdrawn as the condensate was 46.0 parts while the amount of water formed in the reactor was 40.5 parts.
The reaction solution was withdrawn from the reactor, led to a crystallizer and cooled. The crystals were separated from the reaction solution by solid-liquid separation, washed with acetic acid, and dried as a sample for evaluating terephthalic acid.
The yield of terephthalic acid thus formed on the basis of paraxylene was 97.3% by mole. Terephthalic acid thus obtained had the following qualitites:
4CBA content: 148 ppm
OD340: 1.02 wherein the 4CBA value is a value obtained by polarographic analysis, and the OD 340 value is an absorbancy of a solution containing 2 g ofterephthalic acid in 25 ml of an aqueous 2N KOH solution at the wavelength of 340 my (with a 5-cm cell).
The amount of CO x (CO2 + CO) in the oxidation off-gas was measured to calculate the percent acetic acid combustion. In the present example, the percent acetic acid combustion was 6.7% (which represents % by weight of oxidized and decomposed acetic acid on the basis of the weight of resulting terephthalic acid). The results are shown in the following Table.
Example 2
Reaction was carried out in the same reactor in the same mannner as in Example 1, except that 12.5 parts of water was supplied to the reactor together with the air through the feed gas inlet line in place of the feed solution inlet line.
The resulting terephthalic acid had the following qualities:
4CBA: 1,430 ppm
OD 340: 0.97
Terephthalic acid yield: 97.3% by mole
Example 2 was characterized in that no more clogging phenomenon was observed at the feed gas outlet to the reactor by supplying water through the feed gas inlet line, and the reactor could be smoothly operated.
The results are shown in the following Table.
Comparative Example 1
Reaction was carried out in the same reactor in the same manner as in Example 1 except that 12.5 parts of water was supplied to the reactor through an independent water inlet line having an outlet to the reactor at the liquid surface level in the reactor in place of the feed solution inlet line of Example 1.
In the present example, 40.8 parts of water was formed per hour, whereas 46.3 parts of the water was withdrawn as a condensate to keep the water concentration of the reaction solution 14% by weight. The yield of terephthalic acid was 97.2% by mole, and the percent acetic acid combustion was 7.0% by weight.
The resulting terephthalic acid had the following qualities:
4CBA: 1,450 ppm
OD 340: 1.04
The results are shown in the following Table.
Comparative Example 2
Reaction was carried out in the same reactor in the same manner as in Example 1 except that no water was supplied to the reactor through the feed solution inlet line in Example 1. In the present example, 41.2 parts of water was formed per hour, whereas 36.9 parts of water was withdrawn from the reactor by withdrawing 79.9 parts of condensate per hour through the condensatewithdrawal line.
The yield of terephthalic acid was 97.2% by mole, and the percent acetic acid combustion was 7.4% by weight.
The resulting terephthalic acid had the following qualities.
4CBA: 1,400ppm OD 340: 1.03
The results are shown in the following Table.
Example 3
Reaction was carried out in the same reactor as in Example 1 at the reaction temperature of 215"C, the pressure of 21 kg/cm2 gauge, the off-gas oxygen concentration of 2% and the average residence time of 45 minutes by continuously supplying the same feed solution mixture consisting of 100 parts of paraxylene, 350 parts of acetic acid (water content: 10% by weight), and catalyst (295 ppm of Co, 550 ppm of Mn, and 1,200 ppm of Br per 350 parts of acetic acid), as continuously admixed with 22.5 parts of water just before the reactor, to the reactor through the feed solution inlet line. In the present example, 57.7 parts of water was withdrawn per hour as the condensate to keep the water concentration of the reaction solution at 13.8% by weight. The amount of water formed by the reaction was 42.2 parts per hour.
The results are shown in the following Table.
Comparative Example 3
Reaction was carried out in the same reactor in the same manner as in Example 3, except that no water was supplied to the reactor through the feed solution inlet line of Example 3.
The results are shown in the following Table.
Example 4
Reaction was carried out in the same reactor as in Example 1 at the reaction temperature of212'C, the pressure of 21 kg/cm2 gauge, the residence time of 45 minutes, and the off-gas oxygen concentration of 2% by continuously supplying the same feed solution mixture of paraxylene, acetic acid and catalyst as in
Example 1, as continuously admixed with 12.5 parts of water just before the reactor, to the reactor through the feed solution inlet line. The amount of water formed by the reaction was 43.5 parts per hour, whereas 57.5 parts of water was withdrawn as the condensate to keep the water concentration of the reaction solution at 11.4% by weight.
The results are shown in the following Table.
Comparative Example 4
Reaction was carried out in the same manner as in Example 4, except that no water was supplied to the reactor through the feed solution inlet line of Example 4. The amount of water formed by the reaction was 44.0 parts per hour, whereas 52.0 parts of water was withdrawn per hour as the condensate to keep the water concentration of the reaction solution at 9.0% by weight.
The results are shown in the following Table.
Example 5
Reaction was carried out in the same reactor in the same manner as in Example 4, except that 12.5 parts of water was supplied to the reactor through an independent water supply line having an outlet to the reactor 0.45 D higher than the bottom of the reactor in place of the feed solution line of Example 4.
The results are shown in the following Table.
Ex. 1 Ex. 2
1. Reactor inner diameter 300 mm 300 mm
2. Number of stirring 2 2
blade means
3. Level of upper end of 100 mm 100 mm
lowest stirring blade
means
4. Water inlet level 45 mm 35 mm
(ratio to D) *1) (0.15 D) (0.12 D)
5. Manner of water supply Through feed Through feed
solution gas inlet
inlet line line
1. Reaction temp. ( C) 210 210
2. Water concentration of 14.0 14.0
reaction solution
(% by weight)
3. Amount of water withdrawn 46.0 46.0
(parts by weight) *2)
4. Amountofwaterformed 40.5 40.5
(parts by weight)
5.Terephthalic acid yield 97.3 97.3
(% by mole)
6. 4CBA (ppm) *3) 1480 1430 OD340(-) 1.02 0.97
Percent acetic acid
Combustion 6.7 6.6
(% by weight) *4)
Notes:
*1) Inner diameter of the reactor
*2) Amount of water in withdrawn condensate per 100 parts by weight of fed paraxylene
*3) Absorbancy of a solution containing 29 of terephthalic acid in 25 ml of 2N KOH solution at wavelength
of 340 my with a 5-cm cell
*4) % by weight on the basis of product terephthalic acid
Comp. Ex. 1 Comp. Ex. 2 Ex. 3 Comp. Ex. 3 300 mm 300 mm 300 mm 300mm 2 2 2 2 100 mm 100 mm 100mm 100 mm 750 mm none 45mm none (2.5D) (0.15 D)
Through water none Through feed none inlet line solution
inlet line
210 210 215 215
14.0 13.1 13.8 14.0
46.3 36.9 57.7 36.1
40.8 41.2 42.2 43.1
97.2 97.2 97.4 97.4 1450 1400 980 900
1.04 1.03 0.95 1.00
7.0 7.4 8.5 9.5
Ex. 4 Comp. Ex 4 Ex. 5 300 mm 300 mm 300 mm 2 2 2 100 mm 100 mm 100 mm 45mm none 120 mm (0.15 D) (0.4D)
Through feed none Through water inlet line inlet line 215 215 215
11.4 9.0 11.4
57.5 52.0 57.5
43.5 44.0 43.6
97.6 97.5 97.6 750 700 740
0.85 0.87 0.85
10.0 10.6 10.1
Claims (11)
1. A process for continuously producing terephthalic acid by liquid phase oxidation of paraxylene with a molecular oxygen-containing gas in acetic acid as a solvent in the presence of a catalyst containing cobalt, manganese and bromine, which comprises supplying 2 to 50 parts by weight of water per 100 parts by weight of the paraxylene into a vertical cylindrical reactor with a vertical stirrer having at least one stirring blade means at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor, supplying a feed solution comprising the paraxylene, the acetic acid and the catalyst, and the molecular oxygen-containing gas to the level in the said zone, while maintaining a water concentration of reaction solution at 5 to 20% by weight and a reaction temperature at 195 to 225"C.
2. The process according to Claim 1, wherein the water is pure water or by-prouduct water from the reactor.
3. The process according to either of Claims 1 and 2, wherein the molecular oxygen-containing gas is air or pure oxygen or pure oxygen diluted with an inert gas.
4. The process according to any one of Claims 1 to 3, wherein an oxygen-concentration of an effluent gas from the reactor is 0.5 - 7% by volume.
5. An apparatus for continuous oxidation of paraxylene to terephthaiic acid, which comprises a vertical cylindrical reactor provided with a vertical stirrer having at least one stirring blade means, and with a water inlet, a feed solution inlet and a molecular oxygen-containing gas inlet, each inlet being positioned at a level in the zone between the level by 0.5 times the inner diameter of the reactor higher than the level of upper end of lowest stirring blade means and the level by 0.03 times the inner diameter of the reactor higher than the bottom of the reactor.
6. The apparatus according to Claim 5, wherein a reaction product outlet is provided in the reaction solution and above the upper end of lowest stirring blade means.
7. The apparatus according to either of Claims 5 and 6, wherein the water inlet and the molecular oxygen-containing gas inlet are integrated into one inlet.
8. The apparatus according to any one of Claims 5 to 7, wherein the water inlet and the feed solution are integrated into one inlet.
9. A process for continuously producing terephthalic acid substantially as hereinbefore described with particular reference to the examples.
10. An apparatus for continuous oxidation of paraxylene to terephthalic acid substantially as hereinbefore described with particular reference to the drawings.
11. Terephthalic acid when produced by a process according to any one of Claims 1 to 4 or 9 or in an apparatus according to any one of Claims 5 to 8 or 10.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56151149A JPS5852243A (en) | 1981-09-24 | 1981-09-24 | Preparation of terephthalic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2106797A true GB2106797A (en) | 1983-04-20 |
| GB2106797B GB2106797B (en) | 1985-08-21 |
Family
ID=15512431
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08226863A Expired GB2106797B (en) | 1981-09-24 | 1982-09-21 | Process and apparatus for producing terephthalic acid by liquid phase oxidation of paraxylene |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPS5852243A (en) |
| GB (1) | GB2106797B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0261892A2 (en) * | 1986-09-26 | 1988-03-30 | Mitsui Petrochemical Industries, Ltd. | The production of aromatic carboxylic acids |
| WO2009128608A3 (en) * | 2008-04-16 | 2010-11-11 | Sam Nam Petrochemical Co., Ltd. | Oxidation reactor for manufacturing of crude terephthalic acid |
| WO2020102639A1 (en) * | 2018-11-16 | 2020-05-22 | Bp Corporation North America Inc. | Process for manufacturing aromatic carboxylic acids |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02269535A (en) * | 1989-04-11 | 1990-11-02 | Fsk Corp | Working method for work |
| US5371283A (en) * | 1993-12-22 | 1994-12-06 | Praxair Technology, Inc. | Terephthalic acid production |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5328901B2 (en) * | 1973-07-28 | 1978-08-17 | ||
| JPS5365841A (en) * | 1976-11-26 | 1978-06-12 | Asahi Chem Ind Co Ltd | Preparation of terephthalic acid |
| JPS5384933A (en) * | 1976-12-30 | 1978-07-26 | Mitsubishi Chem Ind Ltd | Preparation of terephthalic acid |
| JPS53100339A (en) * | 1977-02-14 | 1978-09-01 | Sanwa Seiki Mfg Co Ltd | Shearing type shaft coupling |
| JPS5452049A (en) * | 1977-09-30 | 1979-04-24 | Toray Ind Inc | Preparation of high quality terephthalic acid |
-
1981
- 1981-09-24 JP JP56151149A patent/JPS5852243A/en active Granted
-
1982
- 1982-09-21 GB GB08226863A patent/GB2106797B/en not_active Expired
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0261892A2 (en) * | 1986-09-26 | 1988-03-30 | Mitsui Petrochemical Industries, Ltd. | The production of aromatic carboxylic acids |
| EP0261892A3 (en) * | 1986-09-26 | 1989-03-15 | Mitsui Petrochemical Industries, Ltd. | The production of aromatic carboxylic acids |
| WO2009128608A3 (en) * | 2008-04-16 | 2010-11-11 | Sam Nam Petrochemical Co., Ltd. | Oxidation reactor for manufacturing of crude terephthalic acid |
| CN101990531A (en) * | 2008-04-16 | 2011-03-23 | 三南石油化学公司 | Oxidation reactor for manufacturing of crude terephthalic acid |
| TWI405752B (en) * | 2008-04-16 | 2013-08-21 | Sam Nam Petrochemical Co Ltd | Oxidation reactor for manufacturing of curde terephthalic acid |
| WO2020102639A1 (en) * | 2018-11-16 | 2020-05-22 | Bp Corporation North America Inc. | Process for manufacturing aromatic carboxylic acids |
Also Published As
| Publication number | Publication date |
|---|---|
| GB2106797B (en) | 1985-08-21 |
| JPS6246533B2 (en) | 1987-10-02 |
| JPS5852243A (en) | 1983-03-28 |
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