WO2005012218A1 - テレフタル酸の製造方法及びテレフタル酸 - Google Patents
テレフタル酸の製造方法及びテレフタル酸 Download PDFInfo
- Publication number
- WO2005012218A1 WO2005012218A1 PCT/JP2004/010576 JP2004010576W WO2005012218A1 WO 2005012218 A1 WO2005012218 A1 WO 2005012218A1 JP 2004010576 W JP2004010576 W JP 2004010576W WO 2005012218 A1 WO2005012218 A1 WO 2005012218A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- terephthalic acid
- crystallization
- crystallization tank
- stirring blade
- blade
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/487—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to chemical modification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C63/00—Compounds having carboxyl groups bound to a carbon atoms of six-membered aromatic rings
- C07C63/14—Monocyclic dicarboxylic acids
- C07C63/15—Monocyclic dicarboxylic acids all carboxyl groups bound to carbon atoms of the six-membered aromatic ring
- C07C63/26—1,4 - Benzenedicarboxylic acid
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
Definitions
- the present invention relates to a method for producing terephthalic acid, and more particularly to a method for producing terephthalic acid, which is suitable as a raw material for producing polyester such as polyethylene terephthalate.
- the present invention also relates to terephthalic acid having a narrow particle size distribution produced using the production method.
- Crude terephthalic acid obtained by oxidation of para-xylene usually contains relatively large amounts of various impurities including 4-carboxybenzaldehyde (abbreviated as “4 CBA”). After purification, it is used as a raw material for polyester.
- 4 CBA 4-carboxybenzaldehyde
- para-xylene In the oxidation reaction of para-xylene, para-xylene is usually reacted with molecular oxygen in an acetic acid solvent at a temperature of 170 to 230 ° C in the presence of a catalyst containing, for example, conoreto, manganese, and bromine. Is adopted.
- the terephthalic acid obtained by this method generally contains 100 to 100 ppm of lipoxybenzaldehyde as an impurity by weight. This terephthalic acid is mixed with water to form a slurry of 10 to 40% by weight.
- this slurry is pressurized to a pressure slightly higher than the reaction pressure by a pressurizing pump and sent to a heating and dissolving step to be converted into an aqueous terephthalic acid solution.
- This terephthalic acid aqueous solution is passed through a column reactor filled with a catalyst containing a platinum group metal.
- Catalysts containing platinum group metals include palladium, ruthenium, rhodium, Smdium, iridium, platinum or the like, or a metal oxide thereof is used. These metals or metal oxides can be used as catalysts as they are, but they are used by being insoluble in an aqueous terephthalic acid solution, for example, supported on a carrier such as activated carbon.
- Purification of terephthalic acid with a platinum group metal catalyst can be performed simply by contacting an aqueous solution of terephthalic acid with the catalyst, but is advantageously performed in the presence of a reducing agent.
- a reducing agent usually, hydrogen is used as a reducing agent, and an aqueous solution of terephthalic acid and hydrogen gas are supplied to the reactor, and the reaction is carried out at a temperature of 220 to 320 ° C, preferably 260 to 300 ° C.
- Hydrogen gas may be supplied at a rate of 0.05 to 1 ON m 3 , preferably 0.1 to 3 Nm 3, based on an aqueous terephthalic acid solution of 100: 8.
- the terephthalic acid that has undergone the purification step is sent to the crystallization step, where terephthalic acid is crystallized by depressurized cooling. Crystallization is usually performed in multiple stages, and finally cooled to a temperature at which most of the terephthalic acid is precipitated, and the formed crystals are dried after solid-liquid separation by centrifugation or the like. Mainly, the average particle size is determined by adjusting the crystallization temperature and average residence time of the first and second crystallization tanks, and usually obtains high purity terephthalic acid of 50 to 150.
- a rotation axis b is provided at a central portion of a crystallization tank a, and a predetermined rotation axis is provided between a lower end thereof and an inner bottom surface of the crystallization tank a.
- a stirring blade c such as an inclined paddle type or a turbine blade is attached, and a baffle plate d is provided on an inner surface of the crystallization tank a.
- the rotating shaft f is suspended from the installed apparatus or the center of the crystallization tank e as shown in Fig.
- a stirring blade g such as an inclined paddle blade is attached to the lower end of the rotating shaft f, and a baffle plate d is provided on the inner surface of the crystallization tank e.
- a device provided with a collision plate h is known.
- the rotation of the stirring blade causes a rotating flow of the terephthalic acid aqueous solution at the tip of the stirring blade, and as a result, a slurry is formed at the center of the crystallization tank at the center of the stirring blade at the lower surface. Stagnation and clogging.
- terephthalic acid is a glycopolymer such as ethylene glycol.
- the mixture is sent to the reaction system in a slurry state after being mixed with the phenols and used for the reaction.
- the particle size distribution and average particle size of terephthalic acid particles greatly affect the handling and transport of terephthalic acid, the mixing property with ethylene glycols, and the uniformity of the reaction.
- a particle size distribution over a wide range from large to small particle size tends to improve the slurry properties with ethylene glycols, and is more suitable for mixing with ethylene glycol.
- the average particle size is usually in the range of 50 to 15.
- terephthalic acid tends to remain as unreacted components during the direct polymerization method, resulting in a longer reaction time. It has been found that there is a need to take this, and there are problems such as an increase in by-products. On the other hand, it has been found that if the proportion of fines below 50 zm increases too much, there is a problem that it takes time to handle and transport the product.
- the present invention is to obtain terephthalic acid efficiently and prevent the required particle size distribution of terephthalic acid particles directly from the crystallization tank by preventing stagnation of the slurry generated at the center of the bottom of the crystallization tank. It is an object of the present invention to provide a method for producing terephthalic acid that can be made separately. The present invention also provides terephthalic acid having a narrow particle size distribution produced using the production method.
- the present invention provides, for example, the following method.
- the shape of the stirring blade is such that the length in the vertical direction is long at the center of the crystallization tank,
- Crystallization consisting of a plurality of crystallization tanks connected in series, having a stirrer with stirring blades close to the inner bottom surface, and providing a baffle plate extending vertically on the inner surface of the crystallization tank.
- Crude terephthalic acid is dissolved in an aqueous medium, purified by contacting with a platinum group metal catalyst at a temperature of 260 to 320, and a plurality of crystals in which terephthalic acid is connected in series from the aqueous solution of terephthalic acid.
- your Keru crystallization temperature in the first crystallization vessel and 240 to 260 ° C the range of stirring power 0. 01 ⁇ 10 kw / m 3 at the stirring blade
- the crystallization temperature in the second crystallization tank is set to 180 to 230 ° C, and the crystallization temperature is set to 20 to 60 lower than the crystallization temperature in the first crystallization tank.
- the method for producing terephthalic acid according to any one of the above (1) to (7).
- the average particle size is 50 to 150 m, and the standard deviation is 30 to 50.
- terephthalic acid is
- a first embodiment of the present invention will be described with reference to FIG. Fig. 1 shows an example in which a motor is installed at the top of the crystallization tank, but it may be installed at the crystallization pot.
- Reference numeral 1 denotes a crystallization tank, and a rotating shaft 2 was provided at the center of the crystallization tank 1 so as to hang down.
- a stirring blade 3 was attached to a lower end of the rotating shaft 2.
- each of the plurality of blades 3a of the stirring blade 3 has a large width in the up-down direction on the root side close to the rotating shaft 2, and the width gradually decreases toward the tip side.
- Each wing body 3 a is formed in a substantially trapezoidal plate shape, and the lower end thereof is attached close to the inner bottom surface of the crystallization tank 1.
- the blade diameter of the stirring is (0.3 to 0.8) D, preferably (0.4 to 0.6) D
- the shape of the wing is in the center and the length in the up-down direction is (0.3:! ⁇ 3.0) R, preferably (0.3-0.7) R, and more preferably (0.4).
- ⁇ 0.6) R and a plurality of agitating blades whose vertical length at the blade tip is (0-0.5) R, preferably (0.1-0.3) R It is characterized by using.
- the ratio c / R between the clearance C between the lower end of the stirring blade and the inner bottom surface of the crystallization tank and the blade diameter R of the stirring blade is in the range of 0.005 to 0.10, preferably 0.1. 01 to 0.05, more preferably 0.01 to 0.03.
- a plurality of baffle plates 4 extending vertically are fixed to the inner side surface of the crystallization tank 1, and the lower end of the baffle plate 4 is close to the inner bottom surface of the crystallization tank 1.
- a stirrer with a stirring blade close to the inner bottom surface and a baffle plate extending vertically on the inner surface of the crystallization tank are required.
- reference numeral 5 denotes an inflow pipe for an aqueous solution of terephthalic acid connected to the crystallization tank
- the rotating shaft 2 is driven and rotated by the drive of the motor (not shown) to rotate the stirring blade 3 whose lower end is close to the inner bottom surface of the crystallization tank 1
- the terephthalic acid in the crystallization tank 1 is removed.
- the aqueous solution is pressed by the wings 3a of the dog on the root side at the center lower part of the crystallization tank 1 while being pressed by the wings 3a of the dog, and the wings 3a of the upper and lower widths become smaller toward the tip.
- the flow becomes concentrated outward and flows along the inner bottom surface of the crystallization tank 1, and then the aqueous solution flows upward at a high speed along the baffle plate 4 whose lower end is close to the inner bottom surface. After flowing toward the portion, it becomes a downward flow at the center and becomes a circulating flow C.
- stirring power requirement is 0. 01 ⁇ 10 kwZm 3 crystalliser 1, more preferably 0. 1 ⁇ 1.
- 0 kwZm 3 the agitation ⁇ main power is 0.1 5-0 . were carried out in the range of 7 kwZm 3.
- the aqueous solution does not become a slurry at the center of the inner bottom surface of the crystallization tank 1 and stagnates, and becomes an ascending flow at a high speed at a peripheral portion near the inner side surface of the crystallization tank 1. Uniform crystallization does not occur, and crystals having a uniform particle size can be obtained efficiently.
- the rotation speed of the stirring blade 3 can be controlled in a wide range.
- terephthalic acid having a narrow particle size distribution having an average particle size of 50 to 150 zm, preferably 80 to 110 m and a standard deviation of 30 to 50 can be obtained.
- the stirring power is 0.01 to 10 kw / m 3 , preferably 0.1 to 1. O kwZm 3 .
- the standard deviation is calculated by the following equation. That is,
- Average value X (X-Xo) / h,
- the stirring blade 3 is formed by six blades 3a.
- the invention is not limited to this, and may be formed by two or more wing bodies 3a.
- crude terephthalic acid is dissolved in an aqueous medium, and purified by contacting with a platinum group metal catalyst under a temperature condition of 260 to 320 ° C., and terephthalic acid is added in series from the aqueous solution of terephthalic acid.
- the crystallization temperature in the first crystallization tank was set at 240 to 260 ° C for crystallization by cooling stepwise in a plurality of crystallization tanks connected to the crystallization tank, and the stirring power was set by a stirring blade.
- a method for producing terephthalic acid in which stirring is performed in the range of 0 to 10 kw Zm 3 and then the crystallization temperature in the second crystallization tank is set to 180 to 230 ° C.
- the crystallization temperature in the second crystallization tank is lowered by 20 to 60 ° C from the crystallization temperature in the first crystallization tank, and the crystallization temperature in the second crystallization tank is changed. Is preferably set to 180 to 230 ° C.
- FIG. 2 shows a second embodiment of the present invention.
- the tip of the inflow pipe 5 in the crystallization tank 1 of the first embodiment is placed inside the crystallization tank 1.
- the inflow pipe 5 is bent upward and the opening 5 a of the inflow pipe 5 is formed upward, and the outflow pipe 6 also has a tip bent upward in the crystallization tank 1 to form an opening of the outflow pipe 6. 6a was formed upward.
- the aqueous solution of terephthalic acid flows upward from the opening 5a of the inlet pipe 5 into the solution flowing upward around the crystallization tank 1, and the vapor does not directly entangle with the blades. Since the discharge efficiency of the aqueous solution in the stirring blade 3 does not decrease and the opening 6a of the outflow pipe 6 is also directed upward, the aqueous solution rising in the peripheral portion of the crystallization tank 1 stays without directly flowing in and out. The time can be lengthened, and the crystals crystallized in the aqueous solution reaching above the opening 6 flow down, flow into the opening 6a, and are discharged from the discharge pipe 6. Thus, uniform crystals having a predetermined particle size or more can be obtained.
- FIG. 3 shows a third embodiment of the present invention.
- the distal end of the inflow pipe 5 in the first embodiment is bent upward in the crystallization tank 1.
- the opening 5a of the inflow pipe 5 is formed upward, the inverted conical flow dispersion member 5b is provided above the opening 5a, and the tip of the outflow pipe 6 is bent downward. Then, the end face of the tip was closed, and an opening 6 b was formed in a direction facing the inner face of the crystallization tank 1 on the side face of the tip.
- the aqueous solution of terephthalic acid flows upward through the opening 5a of the inflow pipe 5 and then reverses. It is dispersed by the cone-shaped flow dispersing element 5b and flows into the aqueous solution in the crystallization tank 1 in a dispersed manner, thereby preventing the entanglement of the vapor with the blades and the efficiency of discharging the aqueous solution by the stirring blades 3. As a result, it is possible to obtain an initial dispersing action utilizing the inflowing energy.
- the opening 6 b of the outflow pipe 6 is located at a position where the crystallized particles are classified into those that rise with the aqueous solution and those that do not rise in the periphery of the inner bottom surface of the crystallization tank 1. Negative pressure suction of crystal particles having a diameter or more is ensured at the opening 6b.
- FIG. 1 is a sectional view of a first embodiment of the present invention.
- FIG. 2 is a cross-sectional view of a main part according to the second embodiment of the present invention.
- FIG. 3 is a sectional view of a main part according to the third embodiment of the present invention.
- FIG. 4 is a cross-sectional view of one example of a conventional manufacturing apparatus.
- FIG. 5 is a cross-sectional view of another example of the conventional manufacturing apparatus.
- FIG. 6 is a graph showing the relationship between the stirring power and the particle size distribution of terephthalic acid in the crystallization tanks of the production apparatus of the present invention and the conventional production apparatus. Explanation of symbols
- a water slurry of high-purity terephthalic acid having a particle size distribution of 74 to 149 im was prepared, and the slurry was pressurized in a dissolution tank and completely dissolved at 220 ° C. Then, crystallization was performed using three series connected crystallization tanks of the same capacity.
- the stirring blade diameter R is 0.5 D
- the blade shape is the central part and the vertical length is A stirring blade having 0.5 R and six blades having a vertical length of 0.15 R at the tip of the blade was used.
- the ratio c / R between the clearance c between the lower end of the stirring blade and the inner bottom surface of the crystallization tank and the blade diameter R of the stirring blade was 0.02.
- the rotation speed can be changed to 0.2 and.
- Crystallization was performed at 7 kw / m 3 .
- a stirrer with four bladed inclined paddle blades was used as the second crystallization tank.
- the stirring blade was used at a constant stirring power of 0.7 kw / m 3 .
- the temperatures of the first and second crystallization tanks were set at 160 ° C and 160 ° C, respectively, so that about 70% by weight and about 99% by weight of the total terephthalic acid were deposited, respectively.
- the temperature of the crystallization tank was controlled to 120 ° C, and the temperature of the third crystallization tank was controlled to 100 ° C.
- FIG. 6 The result of a physical property test on terephthalic acid particles is shown.
- the difference between the embodiment and the comparative example is that in the comparative example, an inclined paddle blade having a blade diameter of 0.5D was used, and all other operating conditions were the same as in the example.
- the particle size was measured by a laser diffraction / scattering particle size distribution analyzer.
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Abstract
Description
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Priority Applications (1)
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JP2005512486A JPWO2005012218A1 (ja) | 2003-08-05 | 2004-07-16 | テレフタル酸の製造方法及びテレフタル酸 |
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JP2003205951 | 2003-08-05 | ||
JP2003-205951 | 2003-08-05 |
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WO2005012218A1 true WO2005012218A1 (ja) | 2005-02-10 |
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PCT/JP2004/010576 WO2005012218A1 (ja) | 2003-08-05 | 2004-07-16 | テレフタル酸の製造方法及びテレフタル酸 |
Country Status (5)
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JP (1) | JPWO2005012218A1 (ja) |
KR (1) | KR100807762B1 (ja) |
CN (1) | CN100393688C (ja) |
TW (1) | TWI322803B (ja) |
WO (1) | WO2005012218A1 (ja) |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001030939A (ja) * | 1999-07-15 | 2001-02-06 | Honda Motor Co Ltd | 転回機構を備えた四輪車両 |
JP2005053799A (ja) * | 2003-08-05 | 2005-03-03 | Satake Chemical Equipment Mfg Ltd | テレフタル酸の晶析装置 |
WO2007088981A1 (ja) * | 2006-02-03 | 2007-08-09 | Mitsubishi Rayon Co., Ltd. | カルボン酸の製造方法 |
WO2009038045A1 (ja) * | 2007-09-19 | 2009-03-26 | Mitsui Chemicals, Inc. | 芳香族カルボン酸の製造方法 |
WO2009040886A1 (ja) * | 2007-09-25 | 2009-04-02 | Shi Mechanical & Equipment Inc. | 撹拌装置 |
JP2014173058A (ja) * | 2013-03-12 | 2014-09-22 | Unitika Ltd | 半芳香族ポリアミド粉粒体およびその製造方法 |
JP2014524928A (ja) * | 2011-07-26 | 2014-09-25 | ディーエスエム アイピー アセッツ ビー.ブイ. | ジアミン/ジカルボン酸塩の製造方法 |
WO2017014264A1 (ja) * | 2015-07-22 | 2017-01-26 | 三菱瓦斯化学株式会社 | 高純度テレフタル酸の製造方法 |
JP2018047408A (ja) * | 2016-09-20 | 2018-03-29 | 住友金属鉱山株式会社 | 化学反応装置、および、化学反応装置を用いた粒子の製造方法 |
Families Citing this family (2)
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CZ305172B6 (cs) * | 2014-03-28 | 2015-05-27 | Bochemie A.S. | Diskontinuální krystalizační jednotka pro výrobu kulovitých krystalů |
TWI708761B (zh) | 2019-09-26 | 2020-11-01 | 遠東新世紀股份有限公司 | 製造對苯二甲酸的方法 |
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- 2004-07-16 WO PCT/JP2004/010576 patent/WO2005012218A1/ja active Application Filing
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KR20060041237A (ko) | 2006-05-11 |
TWI322803B (en) | 2010-04-01 |
CN1832914A (zh) | 2006-09-13 |
JPWO2005012218A1 (ja) | 2006-09-14 |
KR100807762B1 (ko) | 2008-02-28 |
TW200517371A (en) | 2005-06-01 |
CN100393688C (zh) | 2008-06-11 |
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