CN1832914A - Method for producing terephthalic acid and terephthalic acid - Google Patents
Method for producing terephthalic acid and terephthalic acid Download PDFInfo
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- CN1832914A CN1832914A CNA2004800223409A CN200480022340A CN1832914A CN 1832914 A CN1832914 A CN 1832914A CN A2004800223409 A CNA2004800223409 A CN A2004800223409A CN 200480022340 A CN200480022340 A CN 200480022340A CN 1832914 A CN1832914 A CN 1832914A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- 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
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- 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
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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
- 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
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- C—CHEMISTRY; METALLURGY
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- C07C51/42—Separation; Purification; Stabilisation; Use of additives
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- 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
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- C—CHEMISTRY; METALLURGY
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- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
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Abstract
A method for producing terephthalic acid wherein an aqueous terephthalic acid solution is purified with a platinum group metal catalyst and then terephthalic acid is crystallized from the resultant aqueous solution, which comprises carrying out the crystallization in an agitating vessel which has, in the bottom portion thereof, an agitating blade being formed in a shape of an approximately trapezoidal plate and being capable of changing a rotating number; and a terephthalic acid product having a narrow particle size distribution. The above method allows the production with good efficiency of terephthalic acid crystals which are excellent in powder characteristics, slurry characteristics and reactivity, and can be controlled with respect to the particle size distribution.
Description
Technical field
The present invention relates to the manufacture method of terephthalic acid, in more detail, relate to the manufacture method of the terephthalic acid that the manufacturing raw material as polyester such as polyethylene terephthalates is fit to.The invention still further relates to the terephthalic acid of the narrow particle size distribution that utilizes this manufacture method manufacturing.
Background technology
By in the resulting crude terephthalic acid of oxidation of p-Xylol, contain morely usually with the various impurity headed by the 4-carboxyl benzaldehyde (abbreviating " 4CBA " as), after it is refining, use as the raw material of polyester.
Process for purification as such crude terephthalic acid, in aqueous solvent, dissolve crude terephthalic acid, under high pressure, high temperature, making it to contact and carry out the purified method with platinum metal catalysts is known (for example the spy opens flat 6-329583 communique), and several process for purification also are known.
As the oxidizing reaction of p-Xylol, adopt in acetic acid solvent, usually in the method that in the presence of the catalyzer that for example contains cobalt, manganese and bromine, under 170～230 ℃ temperature condition p-Xylol and molecularity oxygen is reacted.By the terephthalic acid that this method obtains, containing usually as the benchmark by weight of impurity is the 4-carboxyl benzaldehyde of 1000～10000ppm.This terephthalic acid is mixed with water, form the slurries of 10～40 weight %.Then, these slurries utilize boosting pump to be pressurized to the pressure higher than reaction pressure, deliver to the heating for dissolving operation, become aqueous terephthalic acid solution.
This aqueous terephthalic acid solution is passed through in having filled the tower reactor of the catalyzer that contains the platinum metals.As the catalyzer that contains the platinum metals, use the oxide compound of palladium, ruthenium, rhodium, osmium, iridium, platinum etc. or these metals.Though these metals or metal oxide also can directly be used as catalyzer, being supported in aqueous terephthalic acid solution is to use on the such carrier of insoluble for example activated carbon.
Utilize the refining of terephthalic acid that platinum metal catalysts carries out, aqueous terephthalic acid solution is contacted with catalyzer also can carry out, but is favourable in the presence of reductive agent.Usually use hydrogen as reductive agent, in reactor, supply with aqueous terephthalic acid solution and hydrogen, 220～320 ℃, preferably under 260～300 ℃ temperature condition, contact with catalyzer.With respect to the 1000kg aqueous terephthalic acid solution, as long as hydrogen is with 0.05～10Nm
3, 0.1～3Nm preferably
3Ratio supply with just.
Terephthalic acid through refining step is sent to the partial crystallization operation, presses cooling by putting, and terephthaldehyde's acid crystal is separated out.Partial crystallization carries out with multistage usually, finally is cooled to the temperature that the major part of terephthalic acid is separated out, and the crystallization that is generated is utilizing centrifugation etc. to carry out drying after carrying out solid-liquid separation.Median size mainly decides by partial crystallization temperature, the average retention time of adjusting the 1st partial crystallization groove and the 2nd partial crystallization groove, obtains the high purity terephthalic acid of 50～150 μ m usually.
As the existing partial crystallization device that is applicable to that terephthalic acid is made, following such device is arranged: as shown in Figure 4, central part at partial crystallization groove a, make the sagging with gap turning axle b that is provided with that has predetermined distance between the inner bottom surface of the lower end of turning axle b and this partial crystallization groove a, bottom at above-mentioned turning axle b, the agitating wing c of for example tilt oar shape, the turbine type wing etc. is installed, simultaneously, the device of baffle plate d is set at the medial surface of above-mentioned partial crystallization groove a; Perhaps, as shown in Figure 5, central part at partial crystallization groove e, make the sagging with gap turning axle f that is provided with that has predetermined distance between the inner bottom surface of the lower end of turning axle f and this partial crystallization groove e, in the bottom of above-mentioned turning axle f, the agitating wing g of the installation inclination oar shape wing etc., simultaneously, medial surface at above-mentioned partial crystallization groove e is provided with baffle plate d, and the device of crash panel h is set near the front end of above-mentioned agitating wing g again.These devices all are known.
In existing partial crystallization device, by the rotation of agitating wing, produce the rotational flow of aqueous terephthalic acid solution at the leading section of agitating wing, consequently, slurries are stuck in the central part of the partial crystallization groove inner bottom surface of agitating wing central part, and problem such as obstruction is arranged.
On the other hand, in recent years, the so-called direct polymerization method of utilizing terephthalic acid and glycols direct reaction in vogue is made the method for polyester, particularly polyethylene terephthalate.In this direct polymerization method, terephthalic acid mixes with glycolss such as ethylene glycol, delivers to reaction system with slurry condition, for reacting.In the process at this moment, because the size distribution of terephthaldehyde's acid particles or the value difference of median size, to the loading and unloading of terephthalic acid, conveying, cause big influence with the Combination and the reaction uniformity of glycols.
In general, when having the size-grade distribution of broad range, exist the tendency that improves with the slurry characteristics of glycols from big particle diameter to small particle size, aspect the Combination of ethylene glycol, being suitable, as median size, the scope of 50～150 μ m normally.On the contrary, particle diameter surpasses the ratio of the so big particle diameter particle of 250 μ m if too increase, then when the direct polymerization method, terephthalic acid becomes unreacted component easily and is residual, consequently, problems such as generation needs the reaction of propagation time, by product increase, this has been very clearly.On the other hand, be lower than the ratio of the such micro mist of 50 μ m, then have in the loading and unloading of goods or need the problem of time and so on when carrying if too increase.
Therefore, satisfy fully terephthalic acid loading and unloading, conveying, with the manufacturing of the terephthalic acid of the Combination of glycols and reaction uniformity be difficult, because terephthalic acid is different with device, scale, the method for operation of the so-called direct polymerization method equipment that glycols directly reacts, often desired quality is also different.
Summary of the invention
The object of the present invention is to provide a kind of manufacture method of terephthalic acid, this manufacture method is the delay by the slurries that prevent to take place at partial crystallization groove inner bottom surface central part, obtains terephthalic acid effectively and can directly form the size-grade distribution of desired terephthaldehyde's acid particles respectively in the partial crystallization groove.The present invention further provides the terephthalic acid of the narrow particle size distribution that utilizes this manufacture method manufacturing.
The present invention for example provides following method.
(1) a kind of manufacture method of terephthalic acid, when making terephthalic acid carry out partial crystallization, use the partial crystallization device from the terephthalic acid aqueous solution, this partial crystallization device is, when setting makes the stirrer of agitating wing near inner bottom surface, the baffle plate that extends along above-below direction in the medial surface setting of partial crystallization groove.
(2) according to the manufacture method of the terephthalic acid of record in above-mentioned (1), it is characterized in that the shape of above-mentioned agitating wing forms, in the central part side of above-mentioned partial crystallization groove, the length of above-below direction is long, and the length of above-below direction is along with the periphery to this partial crystallization becomes little by little shorten tabular.
According to the manufacture method of the terephthalic acid of record in above-mentioned (1) or (2), it is characterized in that (3) top in this partial crystallization groove is to the opening of the inflow pipe that forms the terephthalic acid aqueous solution that is connected with above-mentioned partial crystallization groove.
(4) according to the manufacture method of the terephthalic acid of each record in above-mentioned (1)～(3), wherein, the ratio c/R of the gap c between the inner bottom surface of the lower end of above-mentioned agitating wing and above-mentioned partial crystallization groove and the wing of above-mentioned agitating wing footpath R is 0.005～0.10 scope.
(5) according to the manufacture method of the terephthalic acid of each record in above-mentioned (1)～(4), it is characterized in that, constitute by placed in-line a plurality of partial crystallization grooves and have make the stirrer of agitating wing near inner bottom surface in, be provided with in the partial crystallization groove of the baffle plate that extends along above-below direction at partial crystallization groove medial surface, make at least 50 weight % of the holocrystalline amount of analysing of terephthalic acid carry out partial crystallization.
According to the manufacture method of the terephthalic acid of each record in above-mentioned (1)～(5), it is characterized in that (6) the stirring power that is produced by the agitating wing of the 1st partial crystallization groove is 0.01～10kw/m
3
(7) according to the manufacture method of the terephthalic acid of record in above-mentioned (2), it is characterized in that, the internal diameter of establishing the 1st partial crystallization groove be D, the wing directly when the R, using the wing footpath R that stirs is that the shape of (0.3～0.8) D and the wing is that length at central part side above-below direction is (0.1～3.0) R and is the many pieces of agitating wings of (0～0.5) R in the length of wing leading section above-below direction.
(8) according to the manufacture method of the terephthalic acid of each record in above-mentioned (1)～(7), it is characterized in that, crude terephthalic acid is dissolved in the aqueous solvent, under 260～320 ℃ temperature condition, contact with platinum metal catalysts and to make with extra care, utilizing placed in-line a plurality of partial crystallization groove to make terephthalic acid interim cooling and when carrying out partial crystallization from this terephthalic acid aqueous solution, making the partial crystallization temperature in the 1st partial crystallization groove is 240～260 ℃, stir with agitating wing, stir power at 0.01～10kw/m
3Scope, then, making the partial crystallization temperature in the 2nd partial crystallization groove is 180～230 ℃, and, make this partial crystallization temperature hang down 20～60 ℃ than the partial crystallization temperature of the 1st partial crystallization groove.
(9) according to the manufacture method of the terephthalic acid of each record in above-mentioned (1)～(8), it is characterized in that,, form the size-grade distribution of terephthaldehyde's acid particles respectively by changing the revolution that stirs power, change agitating wing.
(10) a kind of terephthalic acid is characterized in that, median size is 50～150 μ m, and its standard deviation is 30～50.
(11) a kind of terephthalic acid is characterized in that, it is to utilize the method for each record in above-mentioned (1)～(9) to make, and median size is 50～150 μ m, and its standard deviation is 30～50.
According to Fig. 1 the 1st embodiment of the present invention is described.Fig. 1 is provided with the example of electric motor at partial crystallization groove top, but also can be arranged on the partial crystallization trench bottom.
1 expression partial crystallization groove, the central part in this partial crystallization groove 1 hangs down turning axle 2 is set, and in the bottom of this turning axle 2 agitating wing 3 is installed.
Here, many pieces of this agitating wing 3 each wing body 3a are in the root side near above-mentioned turning axle 2, the width of above-below direction is big, along forming the tabular of roughly platform shape that this width little by little diminishes towards front, each wing body 3a, install near the inner bottom surface ground of above-mentioned partial crystallization groove 1 its lower end.
Promptly, it is characterized in that, the internal diameter of establishing the partial crystallization groove be D, the wing directly when the R, use the wing footpath R that stirs be (0.3～0.8) D, preferably the shape of (0.4～0.6) D and the wing be length at central part side above-below direction be (0.1～3.0) R, preferably (0.3～0.7) R, be more preferably (0.4～0.6) R and be (0～0.5) R, the many pieces of agitating wings of (0.1～0.3) R preferably in the length of wing leading section above-below direction.
The ratio c/R of gap c between the inner bottom surface of the lower end of agitating wing and above-mentioned partial crystallization groove and the wing of above-mentioned agitating wing footpath R is 0.005～0.10 scope, preferably 0.01～0.05, be more preferably 0.01～0.03 scope.
In addition, be fixed with a plurality of baffle plates 4 that extend along the vertical direction at the medial surface of this partial crystallization groove 1, the lower end of this baffle plate 4 is near the inner bottom surface of this partial crystallization groove 1.
When using placed in-line a plurality of partial crystallization groove to make terephthalic acid, use have make the stirrer of agitating wing near inner bottom surface in, the partial crystallization groove of the baffle plate that extends along the vertical direction in the medial surface setting of partial crystallization groove, preferably make at least 50 weight % of the holocrystalline amount of analysing of terephthalic acid, carry out partial crystallization more than being preferably 70 weight %.
In Fig. 1, the inflow pipe of terephthaldehyde's aqueous acid that 5 expressions are connected with above-mentioned partial crystallization groove 1, the outlet pipe of this aqueous solution that 6 expressions are connected with this partial crystallization groove 1.
Like this, if driving turning axle 2 by the driving of electric motor (not shown) is rotated, thereby make agitating wing 3 rotations of lower end near the inner bottom surface of partial crystallization groove 1, the terephthaldehyde's aqueous acid in this partial crystallization groove 1 then, quadrate part under the central authorities of this partial crystallization groove 1, because of each big wing body 3a of width about the root side is extruded, simultaneously, because of form inner bottom surface flowing along this little each wing body 3a of width about leading section to the outer direction of concentrating along partial crystallization groove 1, then, baffle plate 4 near above-mentioned inner bottom surface becomes fireballing upwelling to the aqueous solution along the lower end, then, after the central part of partial crystallization groove 1 flows, stream below this central part forms and become cycling stream C.
At this, as operating condition, preferably 0.01～10kw/m of power is wanted in the stirring of partial crystallization groove 1
2, be more preferably 0.1～1.0kw/m
2, wanting power in this stirring is 0.15～0.7kw/m
2Scope implement.
Therefore, the aqueous solution becomes slurries and does not stagnate at the central part of the inner bottom surface of above-mentioned partial crystallization groove 1, simultaneously, near the periphery the medial surface of this partial crystallization groove 1 becomes fireballing upwelling and uneven partial crystallizationization does not take place, and efficient obtains the crystallization of uniform grading well.
And, as previously mentioned, because there is not stagnation as slurries, so, even make agitating wing 3 low speed rotation, also can't see the stagnation of slurries, like this, can control the revolution of this agitating wing 3 in scope widely, therefore, the control of dead time or grading effect can be accomplished, crystallization can be made artificially with various different distributions uniform size distribution or particle diameter.
For example, can access have median size at 50～150 μ m, preferably be the terephthalic acid of 30～50 narrow like this size-grade distribution at scope, its standard deviation of 80～110 μ m.For example in this case, stirring power is 0.01～10kw/m
2, 0.1～1.0kw/m preferably
2
Standard deviation is obtained according to following formula.That is,
When establishing mean value is that X, standard deviation are that s, typical value are X
0, interval width is that h, the number of degrees are that f, data number are N, u=(X-X
0During)/h,
Mean value is: X=X
0+ ∑ (u * f)/N * h
Standard deviation is: s=h * (1/ (N-1) * { ∑ (u
2* f)-(∑ uf)
2/ N})
Moreover, in this embodiment, represented to form the example of agitating wing 3, but be not limited thereto with 6 pieces of wing body 3a, also can form by many pieces of wing body 3a more than 2 pieces.
In addition, the manufacture method of preferred following such terephthalic acid, that is: crude terephthalic acid is dissolved in the aqueous solvent, under 260～320 ℃ temperature condition, contact with platinum metal catalysts and to make with extra care, when carrying out partial crystallization, making the partial crystallization temperature in the 1st partial crystallization groove is 240～260 ℃ utilize placed in-line a plurality of partial crystallization groove that terephthalic acid is cooled off from this terephthalic acid aqueous solution interimly, stir with agitating wing, stir power at 0.01～10kw/m
3Scope, then, making the partial crystallization temperature in the 2nd partial crystallization groove is 180～230 ℃.
In this case, by change stirring power, make partial crystallization temperature in the 2nd partial crystallization groove than low 20～60 ℃ of the partial crystallization temperature in the 1st partial crystallization groove, preferably making the partial crystallization temperature in the 2nd partial crystallization groove is 180～230 ℃.
Fig. 2 represents the 2nd embodiment of the present invention, in this embodiment, make the leading section of the inflow pipe 5 in the partial crystallization groove 1 of above-mentioned the 1st embodiment in this partial crystallization groove 1, form crookedly upward, and the opening 5a that makes this inflow pipe 5 becomes towards the top, simultaneously, also make the leading section of outlet pipe 6 in this partial crystallization groove 1, form crookedly upward, and the opening 6a of this outlet pipe 6 is become towards the top.
Like this, terephthaldehyde's aqueous acid, flowing into upward the mobile solution upward from the periphery of opening 5a in partial crystallization groove 1 of inflow pipe 5, steam does not directly twist on the wing, therefore, the discharge efficient of the aqueous solution on the agitating wing 3 can not reduce, and, the opening 6a of outlet pipe 6 is also towards the top, therefore, the periphery in partial crystallization groove 1, the aqueous solution of rising does not flow directly into discharge, can make the residence time elongated, simultaneously, in the aqueous solution above arrival opening 6, the crystallization that partial crystallization has taken place is to dirty, flow into this opening 6a, discharge from vent pipe 6.So, just obtain above homogeneously crystallized of regulation particle diameter.
Fig. 3 represents the 3rd embodiment of the present invention, in this embodiment, make the leading section of the inflow pipe 5 in above-mentioned the 1st embodiment in this partial crystallization groove 1, form crookedly upward, the opening 5a of this inflow pipe 5 is become towards the top, simultaneously, the flow dispersion body 5b of inverted cone-shaped is set above this opening 5a, and, make the leading section of outlet pipe 6 form crookedly downwards, seal the end face of this leading section, meanwhile, in the side of this leading section, relative to ground formation opening 6b with the medial surface of above-mentioned partial crystallization groove 1.
Like this, terephthaldehyde's aqueous acid, after flowing out upward from the opening 5a of inflow pipe 5, the flow dispersion body 5b of rounded taper disperses, in the dispersion and the aqueous solution of inflow in partial crystallization groove 1, therefore, prevent the coiling of steam guide vane, raising simultaneously, can access the initial stage dissemination of utilizing the energy that flows into by the discharge efficient of the aqueous solution of agitating wing 3 generations.And the periphery that the opening 6b of outlet pipe 6 is located at the inner bottom surface of partial crystallization groove 1 carries out the classification position that the particle of crystallization rises and do not rise with the aqueous solution, therefore, and the crystalline particle more than the vacuum suction regulation particle diameter reliably in above-mentioned opening 6b.
Description of drawings
Fig. 1 is the sectional view of the 1st embodiment of the present invention.
Fig. 2 is the sectional view of the 2nd embodiment of the present invention.
Fig. 3 is the sectional view of the 3rd embodiment of the present invention.
Fig. 4 is the sectional view of an example of existing manufacturing installation.
Fig. 5 is another routine sectional view of existing manufacturing installation.
Fig. 6 is the graph of relation of the size-grade distribution of interior stirring power of the partial crystallization groove of expression manufacturing installation of the present invention and existing manufacturing installation and terephthalic acid.
Nomenclature: 1 partial crystallization groove, 2 turning axles, 3 agitating wings, 3a wing body, 4 plate washers, 5 inflow pipes, 5a opening, 5b flow dispersion body, 6 outlet pipes, 6a, 6b opening, a steel basin, b turning axle, c agitating wing, d plate washer, e partial crystallization groove, f turning axle, g agitating wing, h crash panel, i inflow pipe, j outlet pipe.
Embodiment
Below, according to embodiment the present invention is described, but the present invention is not subjected to the restriction of embodiment.
Embodiment
Embodiment 1
The inventor is to above-mentioned the former's the existing manufacturing installation and the manufacturing installation of the 3rd embodiment of the present invention, the experiment when specifically describing continuous operation.
Adjusting size distribution is the high purity terephthalic acid's of 74～149 μ m aqueous slurry, from dissolving tank with this slurries pressurization, in 220 ℃ of consoluet aqueous terephthalic acid solution, use 3 placed in-line partial crystallization grooves of same capability to carry out partial crystallization.
In this case, when the internal diameter of establishing the 1st partial crystallization groove be D, the wing directly when the R, used by the wing footpath R that stirs as the shape of the 0.5D and the wing be in the length of central part side above-below direction as 0.5R and wing leading section at the length of above-below direction 6 pieces of agitating wings that the wing constitutes as 0.15R.Gap c between the inner bottom surface of the lower end of agitating wing and partial crystallization groove and the ratio c/R of the wing of agitating wing footpath R are 0.02.In addition, can change and stir power at revolution is 0.2 and 0.7kw/m
3Condition under carry out partial crystallization.On the other hand, as the 2nd partial crystallization groove, use the agitating wing of the inclination agitating wing with 4 pieces of wings, the stirring dynamic fixation is 0.7kw/m
3
The temperature of the 1st partial crystallization groove and the 2nd partial crystallization groove, about separately 70 weight %, the 1st partial crystallization groove temperature that about 99 weight % separate out of the amount of separating out are that 160 ℃, the 2nd partial crystallization groove temperature are 120 ℃ entirely to manage into terephthalic acid, the 3rd partial crystallization groove is carried out temperature treatment, and making it is 100 ℃.
Result about the physical property test of terephthaldehyde's acid particles is shown.In Fig. 6, the difference of embodiment and comparative example is, using wing footpath in comparative example is the inclination agitating wing of 0.5D, and other operating condition is fully identical with embodiment.Moreover the mensuration of particle diameter uses laser diffraction and scattering formula particle size distribution device to carry out.
Stirring power is 0.2kw/m
3The time median size be 190.7 μ m, standard deviation is 61.1.In addition, obtain stirring power and reach 0.7kw/m
3The time median size be that 134 μ m, standard deviation are 46.9 and the terephthalic acid of narrow particle size distribution.
Utilizability on the industry
Like this, according to the present invention, but efficient obtains the crystallization of terephthalic acid (TPA) well, and has also the effect that can control the particle diameter of crystallization.
Claims (11)
1. the manufacture method of a terephthalic acid, when making terephthalic acid from the terephthalic acid aqueous solution, carry out partial crystallization, use the partial crystallization device, this partial crystallization device is, when setting makes the stirrer of agitating wing near inner bottom surface, the baffle plate that extends along above-below direction in the medial surface setting of partial crystallization groove.
2. the manufacture method of terephthalic acid according to claim 1, it is characterized in that: the shape of described agitating wing forms, in the central part side of described partial crystallization groove, the length of above-below direction is long, and the length of above-below direction is along with the periphery to this partial crystallization groove becomes little by little shorten tabular.
3. the manufacture method of terephthalic acid according to claim 1 and 2 is characterized in that: the top in this partial crystallization groove is to the opening of the inflow pipe that forms the terephthalic acid aqueous solution that is connected with described partial crystallization groove.
4. according to the manufacture method of each described terephthalic acid in the claim 1～3, it is characterized in that: the ratio c/R of the gap c between the inner bottom surface of the lower end of described agitating wing and described partial crystallization groove and the wing of described agitating wing footpath R is 0.005～0.10 scope.
5. according to the manufacture method of each described terephthalic acid in the claim 1～4, it is characterized in that: constitute by placed in-line a plurality of partial crystallization grooves and have make the stirrer of agitating wing near inner bottom surface in, be provided with in the partial crystallization groove of the baffle plate that extends along above-below direction at partial crystallization groove medial surface, make at least 50 weight % of the holocrystalline amount of analysing of terephthalic acid carry out partial crystallization.
6. according to the manufacture method of each described terephthalic acid in the claim 1～5, it is characterized in that: the stirring power that is produced by the agitating wing of the 1st partial crystallization groove is 0.01～10kw/m
3
7. the manufacture method of terephthalic acid according to claim 2, it is characterized in that: when the internal diameter of establishing the 1st partial crystallization groove be D, the wing directly when the R, using the wing footpath R that stirs is that the shape of (0.3～0.8) D and the wing is that length at central part side above-below direction is (0.1～3.0) R and is the many pieces of agitating wings of (0～0.5) R in the length of wing leading section above-below direction.
8. according to the manufacture method of each described terephthalic acid in the claim 1～7, it is characterized in that: crude terephthalic acid is dissolved in the aqueous solvent, under 260～320 ℃ temperature condition, contact with platinum metal catalysts and to make with extra care, utilizing placed in-line a plurality of partial crystallization groove to make terephthalic acid interim cooling and when carrying out partial crystallization from this terephthalic acid aqueous solution, making the partial crystallization temperature in the 1st partial crystallization groove is 240～260 ℃, stir with agitating wing, stir power at 0.01～10kw/m
3Scope, then, making the partial crystallization temperature in the 2nd partial crystallization groove is 180～230 ℃, and, make this partial crystallization temperature hang down 20～60 ℃ than the partial crystallization temperature of the 1st partial crystallization groove.
9. according to the manufacture method of each described terephthalic acid in the claim 1～8, it is characterized in that:, form the size-grade distribution of terephthaldehyde's acid particles respectively by changing the revolution that stirs power, change agitating wing.
10. terephthalic acid, it is characterized in that: median size is 50～150 μ m, and its standard deviation is 30～50.
11. a terephthalic acid is characterized in that: it utilizes each described method manufacturing in the claim 1～9, and median size is 50～150 μ m, and its standard deviation is 30～50.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP205951/2003 | 2003-08-05 | ||
| JP2003205951 | 2003-08-05 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1832914A true CN1832914A (en) | 2006-09-13 |
| CN100393688C CN100393688C (en) | 2008-06-11 |
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| CNB2004800223409A Active CN100393688C (en) | 2003-08-05 | 2004-07-16 | Method for producing terephthalic acid and terephthalic acid |
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| Country | Link |
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| JP (1) | JPWO2005012218A1 (en) |
| KR (1) | KR100807762B1 (en) |
| CN (1) | CN100393688C (en) |
| TW (1) | TWI322803B (en) |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106457061A (en) * | 2014-03-28 | 2017-02-22 | 艾路卡技术股份有限公司 | Discontinuous crystallization unit for preparing spherical crystals |
| US10273197B2 (en) * | 2015-07-22 | 2019-04-30 | Mitsubishi Gas Chemical Company, Inc. | Method for producing high-purity terephthalic acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP4087017B2 (en) * | 1999-07-15 | 2008-05-14 | 本田技研工業株式会社 | Four-wheel vehicle equipped with a turning mechanism |
| JP2005053799A (en) * | 2003-08-05 | 2005-03-03 | Satake Chemical Equipment Mfg Ltd | Terephthalic acid crystallizer |
| JP5114195B2 (en) * | 2006-02-03 | 2013-01-09 | 三菱レイヨン株式会社 | Method for producing carboxylic acid |
| WO2009038045A1 (en) * | 2007-09-19 | 2009-03-26 | Mitsui Chemicals, Inc. | Process for producing aromatic carboxylic acid |
| US20100278007A1 (en) * | 2007-09-25 | 2010-11-04 | Sumitomo Heavy Industries Process Equipment Co. , | Stirring Apparatus |
| RU2730455C2 (en) * | 2011-07-26 | 2020-08-24 | ДСМ АйПи АССЕТС Б.В. | Method of producing diamine/dicarboxylic acid salt |
| JP6282802B2 (en) * | 2013-03-12 | 2018-02-21 | ユニチカ株式会社 | Semi-aromatic polyamide powder and method for producing the same |
| JP6690485B2 (en) * | 2016-09-20 | 2020-04-28 | 住友金属鉱山株式会社 | Chemical reactor and method for producing particles using the chemical reactor |
| TWI708761B (en) * | 2019-09-26 | 2020-11-01 | 遠東新世紀股份有限公司 | Method for manufacturing terephthalic acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3319032B2 (en) * | 1993-05-25 | 2002-08-26 | 三菱化学株式会社 | Method for producing terephthalic acid with excellent powder properties and slurry properties |
| JPH08208561A (en) * | 1994-11-16 | 1996-08-13 | Mitsubishi Chem Corp | Production of terephthalic acid |
| US5567842A (en) * | 1994-11-16 | 1996-10-22 | Mitsubishi Chemical Corporation | Process for producing terephthalic acid |
| JPH08225489A (en) * | 1994-11-16 | 1996-09-03 | Mitsubishi Chem Corp | Production of terephthalic acid |
| JP3224498B2 (en) * | 1995-09-11 | 2001-10-29 | 綜研化学株式会社 | Stirrer |
| JPH0975697A (en) * | 1995-09-18 | 1997-03-25 | Dainippon Seiki:Kk | Agitator for liquid mixed with powdery sample |
| KR100455952B1 (en) * | 1998-03-31 | 2004-11-06 | 스미도모쥬기가이고교 가부시키가이샤 | Vertical agitating apparatus |
| JP3820313B2 (en) * | 1998-03-31 | 2006-09-13 | 住重機器システム株式会社 | Agitator blade structure of vertical agitator |
| JP3632827B2 (en) * | 1998-11-11 | 2005-03-23 | リンテック株式会社 | Stirrer |
| JP2000262880A (en) * | 1999-03-15 | 2000-09-26 | Satake Chemical Equipment Mfg Ltd | Stirring blade |
| JP2002308906A (en) * | 2001-04-11 | 2002-10-23 | Sekisui Chem Co Ltd | Agitating apparatus and method for manufacturing polymer particle |
| JP2002306902A (en) * | 2001-04-13 | 2002-10-22 | Mitsubishi Chemicals Corp | Method for crystallizing and/or refining organic compound |
| JP2003128598A (en) * | 2001-10-16 | 2003-05-08 | Teijin Ltd | Method for controlling particle diameter of terephthalic acid |
| JP2004203864A (en) * | 2002-12-09 | 2004-07-22 | Mitsubishi Chemicals Corp | Method for supplying crude terephthalic acid solution to reaction vessel |
| JP2004202318A (en) * | 2002-12-24 | 2004-07-22 | Mitsubishi Chemicals Corp | Crystallization tank having anchor type stirring blade |
| JP2004255291A (en) * | 2003-02-26 | 2004-09-16 | Toray Ind Inc | Stirring apparatus |
-
2004
- 2004-07-16 JP JP2005512486A patent/JPWO2005012218A1/en active Pending
- 2004-07-16 KR KR1020067000971A patent/KR100807762B1/en active IP Right Grant
- 2004-07-16 WO PCT/JP2004/010576 patent/WO2005012218A1/en active Application Filing
- 2004-07-16 CN CNB2004800223409A patent/CN100393688C/en active Active
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106457061A (en) * | 2014-03-28 | 2017-02-22 | 艾路卡技术股份有限公司 | Discontinuous crystallization unit for preparing spherical crystals |
| CN106457061B (en) * | 2014-03-28 | 2020-05-19 | 艾路卡技术股份有限公司 | Discontinuous crystallization unit for preparing spherical crystals |
| US10273197B2 (en) * | 2015-07-22 | 2019-04-30 | Mitsubishi Gas Chemical Company, Inc. | Method for producing high-purity terephthalic acid |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2005012218A1 (en) | 2005-02-10 |
| KR20060041237A (en) | 2006-05-11 |
| JPWO2005012218A1 (en) | 2006-09-14 |
| TWI322803B (en) | 2010-04-01 |
| TW200517371A (en) | 2005-06-01 |
| CN100393688C (en) | 2008-06-11 |
| KR100807762B1 (en) | 2008-02-28 |
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