TWI632128B - 1,4-butanediol, method for producing polyester using the composition containing 1,4-butanediol, and storage method for composition containing 1,4-butanediol - Google Patents

Abstract

The present invention provides a 1,4-butanediol (hereinafter abbreviated as "BG") which is capable of obtaining a polyester having excellent color tone and having a low quality deterioration even when stored in an oxygen-containing atmosphere. The BG of the present invention contains 2-methyl-1,3-propanediol in an amount of 1 part by weight or more, and contains 1 part by weight or more and 50 parts by weight or less of a cyclic acetal compound.

Description

Composition containing 1,4-butanediol, method for producing polyester using the composition containing 1,4-butanediol, and storage method for composition containing 1,4-butanediol

The present invention relates to a 1,4-butanediol which can obtain a polyester having excellent color tone and which is less deteriorated in quality even when stored in an oxygen-containing environment, a method for producing a polyester using the 1,4-butanediol, and the like. Storage method of 1,4-butanediol.

It is known that 1,4-butanediol (hereinafter referred to as "BG") is an extremely useful material which is used as a raw material of various solvents and derivatives. One of them is a polyester obtained by using BG as a raw material of a diol component, and esterification reaction,/or transesterification reaction, and polycondensation reaction with a dicarboxylic acid, and can be utilized for various uses.

In particular, polybutylene terephthalate and polybutylene succinate have been widely used in recent years.

In particular, the main component of the dicarboxylic acid component is polybutylene terephthalate (hereinafter referred to as "PBT"), which has excellent mechanical properties, heat resistance, formability, and recyclability, and mechanical strength. Because it is also high in resistance and excellent in chemical resistance, it is widely used as a material for industrial molded articles such as connectors, relays, and switches for automobiles and electric/electronic equipment. Further, it is also widely used as a film, a sheet, a fiber, etc., and PBT having a good color tone is required in response to this phenomenon.

Various methods have been developed for industrially manufacturing BG. Among them, a method in which allyl alcohol is obtained by oxidation of propylene or acetoxylation, and then subjected to oxo reaction and hydrogenation to obtain BG is known (for example, see Patent Document 1).

Further, in Patent Documents 2 and 3, BG containing a cyclic acetal having a trace degree which cannot be quantitatively analyzed is described.

[Previous Technical Literature] [Patent Literature]

Patent Document 1: Japanese Patent Laid-Open No. Hei 6-234679

Patent Document 2: Japanese Patent Laid-Open No. Hei 6-305997

Patent Document 3: Japanese Patent Laid-Open No. Hei 6-305998

However, the polyester obtained by using the BG produced by the method of Patent Document 1 may have a poor color tone. Further, after the BG is stored for a long period of time, the color tone of the polyester obtained by using the BG may become worse.

On the other hand, the color tone of the polyester obtained by using BG described in Patent Document 2 or 3 may be worse.

In view of the above, it is an object of the present invention to provide a BG which is excellent in color tone and which has little deterioration in quality even when stored in an oxygen-containing environment.

Furthermore, it is an object of the present invention to provide a method for efficiently producing PBT having good color tone.

The 1,4-butanediol which is the subject of the present invention is 1,4-butanediol (BG) containing 2-methyl-1,3-propanediol, and contains 1 part by weight or more and 50 parts by weight or less of ring-shaped shrinkage. Aldehyde compound. The above BG is preferably a carbonyl value of 0.50 mgKOH/g or less as measured by potentiometric titration.

Furthermore, the method for producing a polyester according to the present invention is to use BG as a diol component. The main ingredient. The above polyester is preferably polybutylene terephthalate.

Further, the storage method of the BG of the present invention is a method of storing the above BG in an oxygen-containing environment, and the oxygen concentration of the environment is 0.1% by volume to 10% by volume.

Further, the method for producing PBT according to the present invention is produced by containing a dicarboxylic acid component containing a para-citric acid and/or a para-alkyl phthalate as a main component, and a diol component containing BG as a main component. The PBT method, wherein the BG system contains a cyclic acetal compound in an amount of 50 to 600 ppm by weight, and the alkali compound is added before the esterification reaction step and/or the transesterification reaction step.

According to the present invention, BG which is less deteriorated in quality even when stored in an oxygen-containing environment can be obtained, and a polyester having a good color tone can be obtained by using BG having less deterioration in quality. Moreover, quality degradation can be reduced by using specific storage conditions.

Further, according to the present invention, even if BG having a highly purified cyclic acetal compound is not used, PBT having a good color tone can be obtained.

1‧‧‧Material supply pipeline

2‧‧‧Recycling pipeline

3‧‧‧catalyst supply pipeline

4‧‧‧ oligomer extraction line

5‧‧‧Distillation line

6‧‧‧Extracted pipeline

7‧‧‧Circular pipeline

8‧‧‧Extracted pipeline

9‧‧‧Exhaust pipeline

10‧‧‧condensate line

11‧‧‧Extracted pipeline

12‧‧‧Circular pipeline

13‧‧‧Extracted pipeline

14‧‧‧Exhaust line

15‧‧‧catalyst supply pipeline

16‧‧‧catalyst supply pipeline

A‧‧‧Esterification reaction tank

B‧‧‧Extraction pump

C‧‧‧Rectifier

D, E‧‧ pump

F‧‧‧ slot

G‧‧‧Condenser

L1, L3‧‧‧ withdrawal pipeline

L2, L4, L6‧‧‧ exhaust lines

L5‧‧‧ polymer extraction pipeline

L7‧‧‧ metal compound supply pipeline

L8‧‧‧BG supply pipeline

A‧‧‧1st polycondensation reaction tank

c, e, m‧‧‧ gear pump for extraction

D‧‧‧2nd polycondensation reaction tank

g‧‧‧Snail head

h‧‧‧Rotary cutter

K‧‧‧3rd polycondensation reaction tank

R, S, T, U‧‧‧ filters

Fig. 1 is an explanatory view showing an example of an esterification reaction step employed in the present invention.

Fig. 2 is an explanatory view showing an example of a polycondensation reaction step employed in the present invention.

Hereinafter, the embodiments of the present invention will be described in detail, but the description of the constituent elements described below is only an example (representative example) of the embodiment of the present invention, and is not intended to be specific.

In the present specification, the numerical range expressed by "~" means a range including the numerical values described before and after "~" as the lower limit and the upper limit. In addition, the lower limit or the upper limit in this specification is a range including the value of the lower limit or the upper limit.

The BG system is produced by any one of a method including a petrochemical method and a fermentation step derived from biomass resources, or a combination thereof. For example, using the raw material butadiene, acetic acid and oxygen to carry out the oxime oxidation reaction, to obtain the diethyl ether oxybutene which is an intermediate, and then the diethyl ethoxybutene is hydrogenated and hydrolyzed to obtain BG; BG obtained by hydrogenating using maleic acid, succinic acid, maleic anhydride and/or fumaric acid as raw materials; using acetylene as a raw material, contacting with aqueous formaldehyde solution to obtain butyne a diol (butynediol), which is obtained by hydrogenating BG; an allylic alcohol obtained by oxidation of propylene or acetonitrile to obtain allyl alcohol, which is then subjected to a carbonyloxy reaction and hydrogenation; BG in which succinic acid is hydrogenated, BG obtained by direct fermentation from biomass such as sugar, and the like.

<BG>

The BG of the present invention contains an impurity of 2-methyl-1,3-propanediol and a cyclic acetal. Most of these impurities are contained in the BG by the process of preparing allyl alcohol. In the BG obtained by the production method, an acetal compound or a carbonyl compound can be produced by the presence of an alcoholic OH or an aldehyde in the formation reaction.

Further, according to the production method of BG, for example, when the raw material is butadiene, there is a case where 2-methyl-1,3-propanediol in BG is not detected (not contained), but if the BG is Significant quality deterioration occurs during storage in an oxygen environment.

The content of 2-methyl-1,3-propanediol in the BG of the present invention is usually a lower limit of 1 ppm by weight, preferably 2 ppm by weight. If the lower limit is not reached, there will be an excessive cost when refining or the like.

Further, the content of 2-methyl-1,3-propanediol in BG is usually 500 ppm by weight, preferably 400 ppm by weight. If the upper limit is exceeded, the polyester produced by the BG is used. The hue will tend to deteriorate.

The upper limit of the content of the cyclic acetal compound in the BG of the present invention is 50 ppm by weight, preferably 40 ppm by weight. From the viewpoint of purification efficiency, the lower limit is 1 ppm by weight, preferably 3 ppm by weight, more preferably 5 ppm by weight. If it is less than 1 ppm by weight, it is not preferable because the component polymerized by the acetal compound or the component which is not calculated into the hydrazine carbonyl value is increased.

The upper limit of the ruthenium carbonyl value measured by the potentiometric titration method is preferably 0.50 mgKOH/g, more preferably 0.40 mgKOH/g. From the viewpoint of purification efficiency, the lower limit is usually 0.01 mgKOH/g.

The method for determining the hydrazine carbonyl value is described in detail in the examples. Further, a compound such as an acetal, an aldehyde or a ketone which is regarded as a carbonyl component by this method and is quantitatively referred to is referred to as a "hydrazine carbonyl compound".

When the content of the cyclic acetal compound and the ruthenium carbonyl value are within the above range, even if BG is stored in an oxygen-containing atmosphere, the quality deterioration such as an increase in a carbonyl compound or an acetal compound is small, and the color tone of the polyester used therein is small. There will be a tendency to not deteriorate.

The content of 2-methyl-1,3-propanediol, the cyclic acetal compound, and the hydrazine carbonyl value in the BG of the present invention can be adjusted by, for example, purification conditions including hydrogenation and distillation.

The 2-methyl-1,3-propanediol content in the BG of the present invention can be adjusted by the step of purifying the BG. In other words, 2-methyl-1,3-propanediol can be adjusted by the distillation conditions such as an increase in the reflux amount or an increase in the amount of extraction of the light-boiling component during the distillation purification of BG, whereby the content of BG can be adjusted. When the production efficiency is considered, it is not preferable to be excessively burdensome for the separation of the distillation in order to completely separate and remove it, which is not preferable because it is industrially disadvantageous.

In reality, 2-methyl-1,3-propanediol tends to exist as an impurity in BG. The pressure at the time of distillation is preferably under normal pressure or reduced pressure, and the preferred absolute pressure is 0.01 kPa or more and 760 kPa or less, and particularly preferably 0.1 kPa or more and 400 kPa or less. If the pressure is too high, the temperature at the bottom of the column will be too high, resulting in tetrahydrofuranization due to decomposition of BG, which is not preferable in terms of consumption rate. Moreover, if the pressure is too low, a high degree of vacuum equipment is required, resulting in a very high price, which is not industrially preferable. The liquid temperature in the bottom of the distillation column of the present invention is preferably 80 ° C or more and 230 ° C or less, more preferably 100 ° C or more and 180 ° C or less. If the temperature at the bottom of the column is too high, tetrahydrofuranization is carried out due to decomposition of BG, which is not preferable in terms of consumption rate. If the temperature at the bottom of the column is too low, the pressure inside the column will increase, resulting in the necessity of decompression, requiring a high degree of vacuum equipment, thus resulting in a very high price of the equipment, which is not industrially preferable.

In the present invention, the content of the cyclic acetal compound in BG and the ruthenium carbonyl value can be adjusted by strengthening the hydrogenation reaction in the formation of BG and the BG purification step after the hydrogenation reaction.

The hydrogenation reaction system is, for example, a known hydrogenation catalyst such as Pd, Pt, Ni or Ru, which is carried out at a hydrogen partial pressure of 0.5 MPk to 2 MPa, at 40 ° C or more and 250 ° C or less, preferably 50 ° C or more and 150 ° C or less. The hydrogenated BG is subjected to distillation purification.

The content of the cyclic acetal compound and the ruthenium carbonyl value in BG can be adjusted by distillation conditions such as a hydrogenation reaction pressure, a hydrogenation condition such as a temperature reaction time, a reflux ratio at the time of distillation, and a light boiling extraction amount. Since the cyclic acetal compound and the ruthenium carbonyl compound also have a component close to the boiling point of BG, it is burdened with distillation separation if it is completely separated and removed, which is disadvantageous to industrial properties. Therefore, in consideration of production efficiency, a practical cyclic acetal compound and a ruthenium carbonyl compound exist in the form of impurities.

Further, according to the production method of BG, for example, when the raw material is butadiene, there is a case where the cyclic acetal compound in BG is not detected (not contained), but the BG is stored in an oxygen atmosphere. There is a significant deterioration in quality.

The cyclic acetal compound of the present invention may specifically be, for example, a compound represented by the following formula (I).

(In the above formula (I), R ₁ and R ₂ are each independently a hydrogen atom, an alkyl group having 1 to 3 carbon atoms, and n is a natural number of 2 to 6.)

The compound represented by the above formula (I) can be, for example, 2-methyl-1,3-di Pentane, 2-ethyl-1,3-di Pentane, 2-propyl-1,3-di Pentane, 2-methyl-1,3-di Alkane, 2-ethyl-1,3-di Alkane, 2-propyl-1,3-di Alkane, 2-methyl-1,3-di Heptane, 2-ethyl-1,3-di Heptane, 2-propyl-1,3-di Heptane, 2-ethyl-1,3-di Octane, 2-propyl-1,3-di Butane and so on.

When the BG of the present invention is stored in an oxygen-containing environment, the oxygen concentration of the environment is preferably from 0.1% by volume to 10% by volume. More preferably, it is 0.1% by volume to 7% by volume or less, and particularly preferably 0.1% by volume to 5% by volume or less.

Next, the polyester produced by the present invention will be described.

In the present specification, the "structural unit" of the polyester means a structural unit derived from a specific monomer in the polyester.

In addition, in this specification, "main component" means 70 mol% or more of this component. For example, "a diol compound containing BG as a main component" means that 70 mol% or more of the total diol component is BG.

In the present specification, the step of performing the esterification reaction and/or the transesterification reaction is referred to as "esterification reaction". Should be stepped."

[1] Polyester raw materials

The polyester of the present invention has a structure in which an ester bond is formed by a structural unit derived from a dicarboxylic acid component and a structural unit derived from a diol component. Here, the "dicarboxylic acid component" means a dicarboxylic acid and/or an ester-forming derivative thereof as a raw material for producing a polyester, and the "diol component" means a diol which is a raw material for producing a polyester. And / or its derivatives.

The polyester of the present invention is esterified and/or transesterified by using a dicarboxylic acid component containing a dicarboxylic acid and/or a dicarboxylic acid alkyl ester as a main component and a diol component containing BG as a main component. The reaction can be carried out by further performing a polycondensation reaction.

The polyester using the BG of the present invention is preferably a PBT.

<diol component>

When the BG of the present invention is used in the production of a polyester, the proportion of BG in the total diol component is preferably 80 mol% or more, more preferably 90 mol% or more, and particularly preferably 99 mol% or more. When the proportion of the total diol component in the total diol component is at least the above lower limit value, the molecular chain alignment crystallization due to elongation at the time of molding into a film, a fiber or the like is obtained from the viewpoint of crystallization during molding of an electric component or the like. From the viewpoint of the above, it is easier to make the molded body excellent in mechanical strength, heat resistance, aroma retaining property, and the like.

(diol component other than BG)

When the BG of the present invention is used in the production of a polyester, the raw material diol component may contain a diol component other than BG.

The diol component other than BG may be, for example, ethylene glycol, diethylene glycol, polyethylene glycol, 1,2- Propylene glycol, 1,3-propanediol, polypropylene glycol, polybutanediol, dibutylene glycol, 1,5-pentanediol, neopentyl glycol, 1,6-hexanediol, 1,8 a linear aliphatic diol such as octanediol; 1,2-cyclohexanediol, 1,4-cyclohexanediol, 1,1-dimethylolcyclohexane, 1,4-dihydroxyl a cyclic aliphatic diol such as cyclohexane; a diol, 4,4'-dihydroxybiphenyl, 2,2-bis(4-hydroxyphenyl)propane, bis(4-hydroxyphenyl)anthracene An aromatic diol; a diol derived from a plant material such as isosorbide, dehydrated mannitol, isoidide, or erythritan. Further, ethylene glycol, 1,3-propanediol or the like can also be used from biomass resources. From the physical properties of the obtained polyester, other diol components are preferably ethylene glycol, 1,3-propanediol, polybutanediol, and 1,4-dimethylolcyclohexane. These diol components may be used singly or in combination of two or more.

<Dicarboxylic acid component>

In the case of producing a polyester using the BG of the present invention, the dicarboxylic acid component may be a dicarboxylic acid and/or an ester thereof obtained according to any one of a method of petrochemical method and a process comprising a fermentation step derived from biomass resources. The form-forming derivative can also be produced by a combination method. The ester-forming derivative of the dicarboxylic acid is preferably an acid anhydride such as a lower alcohol ester of a dicarboxylic acid or an ester-forming derivative such as an acid chloride. Here, the "lower alcohol" generally means a linear or branched chain alcohol having 1 to 4 carbon atoms. The dicarboxylic acid component is provided before the conditions are satisfied, and the monomer component is not limited. For example, specific examples of the dicarboxylic acid may be, for example, p-citric acid, isophthalic acid, 4,4'-diphenyldiene. Carboxylic acid, 4,4'-diphenyl ether dicarboxylic acid, 4,4'-diphenyl ketone dicarboxylic acid, 4,4'-diphenoxy ethane dicarboxylic acid, 4,4'-diphenyl An aromatic dicarboxylic acid such as a sulfodicarboxylic acid or a 2,6-naphthalene dicarboxylic acid; 1,2-cyclohexanedicarboxylic acid, 1,3-cyclohexanedicarboxylic acid, 1,4-cyclohexane Alicyclic dicarboxylic acids such as dicarboxylic acid and isophorone dicarboxylic acid; malonic acid, succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, etc. Aliphatic dicarboxylic acid and the like. Among them, from heat resistance, From the viewpoint of mechanical properties, an alicyclic dicarboxylic acid or an aromatic dicarboxylic acid is preferred, and an aromatic dicarboxylic acid is more preferred. Further, from the viewpoint of crystallinity and heat resistance, tannic acid is preferred.

(for tannic acid)

When the BG of the present invention is used in the manufacture of PBT, the citric acid component (p-citric acid and/or its ester-forming derivative) can be obtained according to a conventional petrochemical method or a fermentation method derived from biomass resources. . In the present invention, the proportion of the phthalic acid component in the total dicarboxylic acid component is preferably 80 mol% or more, more preferably 90 mol% or more. When the ratio of the bismuth acid component is at least the above-mentioned lower limit value, it is easier from the viewpoint of crystallization during molding of an electric component or the like, and the viewpoint of molecular chain alignment crystallization due to stretching when formed into a film or a fiber. The mechanical strength, heat resistance, fragrance retention, and the like of the molded body are good.

(dicarboxylic acid component other than citric acid component)

When the BG of the present invention is used in the production of PBT, the raw dicarboxylic acid component may contain a dicarboxylic acid component other than the citric acid component.

When the BG of the present invention is used in the production of PBT, a dicarboxylic acid component other than the citric acid component may be used, specifically, for example, oxalic acid, succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid. An aliphatic chain dicarboxylic acid such as azelaic acid, sebacic acid, undecanedicarboxylic acid or dodecanedicarboxylic acid and an ester-forming derivative thereof; hexahydroterephthalic acid, hexahydrogen An alicyclic dicarboxylic acid such as isophthalic acid and an ester-forming derivative thereof; citric acid, isophthalic acid, dibromoisophthalic acid, sodium sulfoisophthalate, phenylenedioxy dicarboxylic acid, 4, 4 '-Diphenyldicarboxylic acid, 4,4'-diphenyl ether dicarboxylic acid, 4,4'-diphenyl ketone dicarboxylic acid, 4,4'-diphenoxyethane dicarboxylic acid, 4 An aromatic dicarboxylic acid such as 4'-diphenylsulfonic acid or 2,6-naphthalene dicarboxylic acid or an ester-forming derivative thereof. Further, the above ester-forming derivative is preferably, for example, A dehydrated product such as succinic anhydride or adipic anhydride or a lower alcohol ester thereof.

Among them, from the physical properties of the obtained polyester, the dicarboxylic acid component other than citric acid is preferably an aromatic dicarboxylic acid component such as isophthalic acid or naphthalene dicarboxylic acid; succinic acid or adipic acid; An aliphatic dicarboxylic acid component such as sebacic acid or dodecanedicarboxylic acid. These dicarboxylic acid components may be used alone or in combination of two or more.

<Other copolymerizable ingredients>

When the BG of the present invention is used in the production of PBT, in addition to the above diol component and the dicarboxylic acid component, other copolymerizable components can be further used as a raw material for the production of the polyester. Other copolymerizable components which can be used in the present invention are, for example, glycolic acid, p-hydroxybenzoic acid, p-β-hydroxyethoxybenzoic acid or the like, or a hydroxycarboxylic acid or alkoxycarboxylic acid; stearyl alcohol, hydrazine Monofunctional carboxylic acid such as heneicosanol, octadecyl alcohol, benzyl alcohol, stearic acid, eucalyponic acid, benzoic acid, t-butyl benzoic acid, benzhydryl benzoic acid; 1,2,3- a trifunctional or higher polyfunctional carboxylic acid such as tricarballylic acid, trimellitic acid, trimesic acid, pyromellitic acid, naphthalenetetracarboxylic acid or gallic acid; trimethylolethane A trifunctional or higher polyfunctional alcohol such as trimethylolpropane, glycerin, pentaerythritol or sucrose ester. These other copolymerizable components may be used singly or in combination of two or more.

<Catalysts and Additives> (esterification reaction or transesterification catalyst)

When the BG of the present invention is used in the production of a polyester, an esterification reaction or a transesterification reaction uses a catalyst. The catalyst system may be, for example, a ruthenium compound such as antimony trioxide; a ruthenium compound such as ruthenium dioxide or osmium tetroxide; or a titanium alkoxide such as tetramethyl titanate, tetraisopropyl titanate or tetrabutyl titanate. a titanium compound such as titanium phenolate such as tetraphenyl titanate; Butadiene tin, oxidized methyl benzophenone, tetraethyltin, hexaethyltin oxide, cyclohexahexyl ditin oxide, didodecyl tin oxide, triethyl hydroxide Tin, triphenyltin hydroxide, triisobutyltin acetate, dibutyltin diacetate, tin diphenyl dilaurate, monobutyltin trichloride, tributyltin chloride, diwsulfide, oxidized Tin compounds such as butylhydroxy tin oxide, methylstannonic acid, stannic acid, butyl stannic acid; magnesium compounds such as magnesium acetate, magnesium hydroxide, magnesium carbonate, magnesium oxide, magnesium alkoxide, magnesium hydrogen phosphate Or a calcium compound such as calcium acetate, calcium hydroxide, calcium carbonate, calcium oxide, calcium alkoxide or calcium hydrogen phosphate; a long-period periodic table (hereinafter also referred to as "period"), a metal compound of Group IIA, in addition to For example, a manganese compound, a zinc compound, or the like. Among them, a titanium compound and a tin compound are preferred, and a tetrabutyl titanate is more preferred. These catalysts may be used singly or in combination of two or more.

When the BG of the present invention is used in the production of a polyester, the amount of the esterification reaction or the transesterification reaction catalyst used is not particularly limited, and the concentration of the metal contained in the obtained polyester is usually 1 ppm by weight or more, preferably 5 The weight is ppm or more, more preferably 10 ppm by weight or more, particularly preferably 20 ppm by weight or more, and most preferably 30 ppm by weight or more. On the other hand, the upper limit of the amount of catalyst used is usually 300 ppm by weight or less, preferably 200 ppm by weight or less, more preferably 150 ppm by weight or less, and particularly preferably 100 ppm by weight. Hereinafter, it is preferably 90 ppm by weight or less, and most preferably 60 ppm by weight or less. When the amount of the catalyst used is less than or equal to the above upper limit, it is difficult to cause foreign matter, and there is a tendency that the deterioration reaction and the gas are less likely to occur when the obtained polyester is thermally stagnation; if it is at least the above lower limit, it may be difficult. The tendency to initiate side reactions.

(polycondensation catalyst)

When the BG of the present invention is used in the production of a polyester, the polycondensation reaction uses a catalyst. touch The medium can directly use the catalyst for the esterification reaction or the transesterification reaction as a polycondensation reaction catalyst, and the above catalyst can be further added. The amount of the polycondensation reaction catalyst to be used is not particularly limited, and the metal concentration in the obtained polyester is usually 0.5 ppm by weight or more, preferably from the same reason as the above-mentioned esterification reaction or transesterification catalyst. 1 ppm by weight or more, more preferably 3 ppm by weight or more, particularly preferably 5 ppm by weight or more, and most preferably 10 ppm by weight or more. On the other hand, the upper limit of the amount of catalyst used is usually 300 ppm by weight or less, preferably 200 ppm by weight or less, more preferably 100 ppm by weight or less, and particularly preferably 50 ppm by weight. The following is preferably 30 ppm by weight or less.

In the case where the catalyst is a titanium compound, the concentration of the titanium metal contained in the finally obtained polyester is preferably 250 ppm by weight or less, more preferably 100 ppm by weight or less, from the viewpoint of suppressing foreign matter. 60 ppm by weight or less, preferably 50 ppm by weight or less.

The metal concentration (weight) of the polyester is measured by a method such as wet ashing, and then the metal contained in the polyester is used, and then measured by atomic luminescence or Induced Coupled Plasma (ICP).

(reagent)

In the esterification reaction, the transesterification reaction, and the polycondensation reaction described later, in addition to the above-mentioned catalyst, for example, orthophosphoric acid, phosphorous acid, hypophosphorous acid, polyphosphoric acid, and the like may be added as a reaction aid. a phosphorus compound such as an ester or a metal salt; a sodium compound such as sodium hydroxide, sodium acetate or sodium benzoate; a potassium compound such as lithium acetate, potassium hydroxide or potassium acetate; a compound of a metal element of Group IA of the periodic table; magnesium acetate and acetic acid A compound of a metal element of Group IIA of the periodic table such as calcium.

(other additives)

Further, in the esterification reaction, the transesterification reaction, and the polycondensation reaction described later, for example, 2,6-di-t-butyl-4-octylphenol or pentaerythritol-tetra[3-(3',5'- may also be used. a phenol compound such as a third butyl-4'-hydroxyphenyl)propionate; a dilauryl ester of 3,3'-thiodipropionate, pentaerythritol-tetrakis(3-laurylthiodipropionate), etc. Sulfide compound; phosphorus compound such as triphenyl phosphite, tris(phenylphenyl) phosphite, tris(2,4-di-t-butylphenyl) phosphite, etc.; antioxidant; paraffin, microcrystalline wax , long-chain fatty acids and esters thereof represented by polyethylene wax, octadecanoic acid, and octadecanoic acid ester; release agents such as polyoxygenated oil and the like.

[2] Method for producing polyester

When the BG of the present invention is used in the production of a polyester, a cyclic acetal compound containing 2-methyl-1,3-propanediol and containing 1 ppm by weight or more and 50 ppm by weight or less is used, and potentiometric titration is used. The measurement of the ruthenium carbonyl value of 0.50 mgKOH/g or less is not particularly limited, and a known method for producing a polyester can be used. Hereinafter, an example of the production method will be described, but the method for producing the polyester of the present invention is not limited thereto.

Hereinafter, the polyester PBT will be described as an example.

<manufacturing procedure>

The production method of PBT is roughly classified into a so-called "direct polymerization method" in which a main raw material is subjected to an esterification reaction with citric acid, and a so-called "transesterification method" in which a main material is a dialkyl phthalate and a transesterification reaction is carried out. . The difference between the two is that the former generates water during the initial esterification reaction, while the latter produces alcohol in the initial transesterification reaction, and the stability is obtained from the raw material, the ease of treatment of the distillate, and the raw material consumption rate are compared. Large and caused by the present invention The viewpoint of the improvement effect is preferably a direct polymerization method.

The direct polymerization method can, for example, be an esterification reaction using an esterification reaction catalyst in a single or multiple stages of esterification reaction tank of citric acid and BG, and then shifting the oligomer of the obtained esterification reaction product. In the polycondensation reaction tank, a polycondensation reaction catalyst is used in a polycondensation reaction tank of a plurality of stages to carry out a polycondensation reaction.

On the other hand, the transesterification method can be, for example, transesterification of a dialkyl phthalate such as dimethyl phthalate with BG in a singly or plural esterification reaction tank using a transesterification catalyst. In the reaction, the oligomer of the obtained transesterification reaction product is transferred to a polycondensation reaction tank, and a polycondensation reaction catalyst is used to carry out a polycondensation reaction in a polycondensation reaction tank of a plurality of stages.

(esterification reaction conditions)

An example of the esterification reaction is usually 180 ° C or higher, preferably 200 ° C or higher, more preferably 210 ° C or higher, and usually 260 ° C or lower, preferably 250 ° C or lower, more preferably 245 ° C or lower. Further, the pressure of the esterification reaction is usually 10 kPa or more, preferably 13 kPa or more, and usually 120 kPa or less, preferably 110 kPa or less.

Further, the time required for the esterification reaction is a measure of the esterification rate of the obtained oligomer, and is adjusted in a certain manner according to the range thereof, and is usually 0.5 hours or longer, preferably 1 hour or longer, and usually 5 hours. Hereinafter, it is preferably 3 hours or less. The esterification reaction rate is usually adjusted to 92% or more. When the esterification step is carried out continuously, the average residence time in the esterification reaction tank is regarded as the time required for the esterification reaction. Accordingly, an oligomer belonging to the esterification reaction product was produced. Further, the esterification reaction system may be carried out in batch form or in a continuous manner.

Next, the oligomer obtained by the esterification reaction is moved to a polycondensation reaction tank, and in the polycondensation reaction The polycondensation reaction is carried out in the presence of a catalyst.

(transesterification reaction conditions)

In the case of the transesterification reaction, the temperature is usually 110 ° C or higher, preferably 140 ° C or higher, more preferably 180 ° C or higher, and usually 260 ° C or lower, preferably 245 ° C or lower, more preferably 220 ° C or lower. Further, the pressure is usually 10 kPa or more, preferably 13 kPa or more, more preferably 60 kPa or more, and is usually 133 kPa or less, preferably 120 kPa or less, and more preferably 110 kPa or less.

Further, the time required for the transesterification reaction is adjusted, for example, by the amount of the distillate in the transesterification reaction, and is usually 0.5 hours or longer, preferably 1 hour or longer, and usually 5 hours or shorter, preferably 3 hours. the following. When the transesterification step is carried out in a continuous manner, the average residence time in the transesterification reaction tank is regarded as the time required for the transesterification reaction. Accordingly, an oligomer belonging to the transesterification reaction product was produced. Further, the transesterification reaction can be carried out in batches or in a continuous manner.

Next, the oligomer obtained by the transesterification reaction is transferred to a polycondensation reaction tank, and a polycondensation reaction is carried out in the presence of a polycondensation reaction catalyst.

(Esterification reactor / transesterification reactor)

The esterification reaction tank or the transesterification reaction tank system may be a known one, and may be any one of a vertical stirring complete mixing tank, a vertical heat convection mixing tank, a tower type continuous reaction tank, or the like, and may be a single tank or may be A plurality of slots in which the same or different types of slots are connected in series. Among them, a reaction tank having a stirring device is preferable, and the stirring device is not limited to a general form composed of a power portion, a bearing, a shaft, and a stirring blade, and a turbine stator type high-speed rotary mixer or a disc crushing type can also be used. A mixer, a rotor mill type mixer, etc. are in the form of high-speed rotation.

The form of stirring is not limited, and in addition to the usual stirring method of directly stirring the reaction liquid in the reaction tank from the upper portion, the lower portion, and the side portion of the reaction vessel, it is also possible to take a part of the reaction liquid by piping or the like. The outside of the reactor is stirred by a line mixer or the like, and the reaction liquid is circulated.

The type of the agitating blade may also be selected from known ones, specifically, for example, a propeller blade, a screw impeller, a turbine blade, a fan turbine impeller, a disk turbine, a Pfaudler blade, FULLZONE® blades, Maxblend blades, etc.

(polycondensation reaction conditions)

The polycondensation reaction system can be carried out in batches or in a continuous manner.

An example of the polycondensation reaction is usually 210 ° C or higher, preferably 220 ° C or higher, and usually 260 ° C or lower, preferably 250 ° C or lower, more preferably 245 ° C or lower. Further, the pressure of the polycondensation reaction is usually 27 kPa or less, preferably 20 kPa or less, more preferably 13 kPa or less, and at least one of the polycondensation reaction tanks is preferably under a reduced pressure of 2 kPa or less. The polycondensation reaction was carried out while stirring. The time required for the polycondensation reaction is determined by measuring the melt viscosity and the intrinsic viscosity of the obtained polyester, and adjusting the range thereof to be constant, usually 2 to 12 hours, preferably 2 to 10 hours. When the polycondensation reaction is carried out continuously, the average residence time in the polycondensation reaction tank is regarded as the time required for the polycondensation reaction.

(polycondensation reaction device)

The polycondensation reaction tank in which the polycondensation reaction is carried out usually uses a heating medium jacket for controlling the temperature, and it is easy to control the temperature, and a heating medium coil may be provided inside the polycondensation reaction tank. The polycondensation reaction tank is usually provided with a vertical or horizontal direction as a center line. Stirring device. When the agitating blade is a stirring device centered on the vertical direction, for example, an anchor claw, a paddle blade, a Pfaudler blade or the like can be used, and when the stirring device is centered on the horizontal direction, for example, an eyeglass blade or a wheel can be utilized. Various kinds of blades have been known before.

The polycondensation reaction tank may be, for example, a known product such as a vertical agitation polymerization tank, a horizontal agitation polymerization tank, or a thin film evaporative polymerization tank. In the late stage of polycondensation where the viscosity of the reaction liquid rises, there is a tendency for the substance to move to become a dominant factor of the molecular weight increase as compared with the reaction rate. Therefore, the side reaction can be suppressed and the main reaction can be suppressed, and the temperature is lowered as much as possible. It is advantageous to achieve the object of the present invention by improving the surface renewability, and it is preferable to select a singular or plural horizontal stirring polymerization machine having a thin film evaporation function excellent in surface renewability, column flowability, and self-cleaning property.

(PBT granules)

The PBT obtained by the above polycondensation reaction is usually transferred from the bottom of the polycondensation reaction tank to a polymer withdrawing die and taken out in a strand shape, and after being cooled by water or water, it is cut by a cutting blade to form a pellet. Or fragmented granules. The obtained granulated body is then subjected to solid phase polycondensation by a known method or the like, and the intrinsic viscosity can also be improved.

(manufacturing program example)

Hereinafter, preferred embodiments of the manufacturing method of the PBT of the present invention will be described based on the drawings. Fig. 1 is an explanatory view showing an example of an esterification reaction step used in the present invention, and Fig. 2 is an explanatory view showing an example of a polycondensation step used in the present invention.

In Fig. 1, the phthalic acid of the raw material is usually mixed with BG in a raw material mixing tank (not shown), and supplied to the esterification reaction tank (A) from the raw material supply line (1) in the form of a slurry.

Furthermore, the catalyst of the present invention preferably forms a BG solution in a catalyst adjusting tank (not shown). After the liquid, it is supplied from the catalyst supply line (3). Fig. 1 shows a state in which the catalyst supply line (3) is connected to the recycle line (2) of the recycled BG, and the mixture is mixed and supplied to the liquid phase portion of the esterification reaction tank (A).

The gas distilled from the esterification reaction tank (A) is separated into a high boiling component and a low boiling component by a distillation column (C) via a distillation line (5). Usually, the main component of the high boiling component is BG, and the main component of the low boiling component is water and THF.

The high boiling component separated by the rectification column (C) is withdrawn from the extraction line (6) via a pump (D), a portion of which is recycled from the recirculation line (2) to the esterification reaction tank (A), a portion of which is Return to the rectification column (C) from the recycle line (7). Further, the remaining components are extracted from the outside of the extraction line (8). On the other hand, the light boiling component separated by the rectification column (C) is taken out from the suction line (9), condensed by the condenser (G), and temporarily retained in the tank (F) via the condensate line (10). in. A portion of the light boiling component collected by the tank (F) is returned to the rectification column (C) via the extraction line (11), the pump (E) and the circulation line (12), and the remainder is withdrawn through the extraction line (13). Externally. The condenser (G) is connected to an exhaust device (not shown) via an exhaust line (14). The oligomer produced in the esterification reaction tank (A) is withdrawn through an extraction pump (B) and an extraction line (4) of the oligomer.

In the step shown in Figure 1, the recycle line (2) is connected to the catalyst supply line (3), but the two can also be independent. Further, the raw material supply line (1) may be connected to the liquid phase portion of the esterification reaction tank (A).

Next, the oligomer supplied to the first polycondensation reaction tank (a) via the extraction line (4) of the oligomer in Fig. 2 is subjected to polycondensation under reduced pressure to form a prepolymer, and then passed through a gear pump for extraction ( c) and the withdrawal line (L1) is supplied to the second polycondensation reaction tank (d). In the second polycondensation reaction tank (d), polycondensation is generally carried out at a lower pressure than the first polycondensation reaction tank (a) to form a polymer. The obtained polymer is supplied to the third via the extraction gear pump (e) and the extraction line (L3). Polycondensation reaction tank (k). The third polycondensation reaction tank (k) is composed of a plurality of stirring blade blocks, and is provided with a horizontal reaction tank having a two-axis self-cleaning stirring blade. The polymer introduced into the third polycondensation reaction tank (k) from the second polycondensation reaction tank (d) via the extraction line (L3) is further subjected to a polycondensation reaction, and then passed through a gear pump (m) for extraction and polymerization. The material extraction line (L5) is taken out from the screw head (g) in the form of molten strands, cooled by water or the like, and then cut into pellets by a rotary cutter (h). The component symbols (L2), (L4), and (L6) are exhaust lines of the first polycondensation reaction tank (a), the second polycondensation reaction tank (d), and the third polycondensation reaction tank (k), respectively. The filters (R), (S), (T), and (U) are not necessarily all provided, and may be appropriately set after considering the foreign matter removal effect and the operational stability.

[3] Physical properties of PBT

The preferred physical properties of PBT used in the production of PBT for the above-described BG of the present invention are described below.

(inherent viscosity)

The intrinsic viscosity is not particularly limited, and is preferably 0.50 dL/g or more, and more preferably 0.70 dL/g or more from the viewpoints of mechanical properties, granulation stability, and moldability. When the intrinsic viscosity of the PBT of the present invention is at least the above lower limit value, the mechanical properties of the molded article tend to be better. On the other hand, the intrinsic viscosity of PBT is preferably 1.50 dL/g or less, more preferably 1.35 dL/g or less. When the intrinsic viscosity of PBT is less than or equal to the upper limit, it tends to be preferable from the viewpoint of formability.

The intrinsic viscosity of the PBT of the present invention can be measured in accordance with the method described in the Examples below.

(hue b value)

The hue is expressed by the b value in the L, a, b color system. The b value is not particularly limited, and the lower limit is usually -5.0 or more, preferably -3.0 or more. On the other hand, the upper limit is usually 5.0 or less, preferably 3.0 or less.

The color tone of the PBT of the present invention can be measured by a colorimetric color difference meter as described in the following examples.

[4] Composition of PBT

In the PBT obtained by the use of the BG of the present invention in the production of PBT, various additives described below or resins other than PBT may be added as necessary to form a composition of PBT. Further, the composition can be used to form a molded body.

(stabilizer)

Various stabilizers can be added as needed. The stabilizer can be, for example, 2,6-di-t-butyl-4-octylphenol, pentaerythritol-tetrakis[3-(3',5'-t-butyl-4'-hydroxyphenyl)propionate a phenolic compound; a thioether compound such as 3,3'-dilaucurium dithiolate or pentaerythritol-tetrakis(3-laurylthiodipropionate); triphenyl phosphite, tris(phosphoric acid) Phosphorus compounds such as phenyl phenyl ester), tris(2,4-di-t-butylphenyl) phosphite, and the like, and the like. These stabilizers may be used alone or in combination of two or more. In order to obtain the effect of adding the stabilizer, the stabilizer is preferably added in an amount of 0.01 part by weight or more, more preferably 0.05 part by weight or more, based on 100 parts by weight of the PBT. On the other hand, from the viewpoint of economy, the stabilizer is preferably added in an amount of 1 part by weight or less based on 100 parts by weight of the PBT.

(release agent)

Various release agents can be added as needed. The release agent may be, for example, paraffin wax, microcrystalline wax, polyethylene wax; or a long-chain fatty acid represented by octacosic acid, octadecanoic acid ester and an ester thereof; a release agent such as polyoxyxanic oil; and the like. These release agents may be used alone or in combination of two or more. In order to obtain the effect of adding the release agent, the release agent is usually preferably added in an amount of 0.01 part by weight or more, more preferably 0.05 or more, based on 100 parts by weight of the PBT. On the other hand, from the viewpoint of economy, the release agent is preferably added in an amount of 1 part by weight or less based on 100 parts by weight of the PBT.

(filler)

It can be blended into a reinforced filler. The reinforcing filler is not particularly limited and can be, for example, glass fiber, carbon fiber, cerium oxide. Inorganic fibers such as alumina fibers, zirconium dioxide fibers, boron fibers, boron nitride fibers, potassium strontium titanate potassium fibers, metal fibers; organic fibers such as aromatic polyamide fibers, fluororesin fibers, and the like. These reinforcing fillers may be used alone or in combination of two or more. Among the above-mentioned reinforced fillers, inorganic fillers are preferred, and glass fibers are more preferred.

When the filler is an inorganic fiber or an organic fiber, the average fiber diameter is not particularly limited, and is usually 1 to 100 μm, preferably 2 to 50 μm, more preferably 3 to 30 μm, and particularly preferably 5 to 20 μm. Further, the average fiber length is not particularly limited, but is usually 0.1 to 20 mm, preferably 1 to 10 mm.

The reinforced filler material is used to improve the interface between the PBT and the PBT. It is preferably used after surface treatment with a sizing agent or a surface treatment agent. The sizing agent or the surface treatment agent may be, for example, a functional group compound such as an epoxy compound, an acrylic compound, an isocyanate compound, a decane compound or a titanate compound. These compounds may be used alone or in combination of two or more. Reinforced fillers can use a sizing agent or The surface treatment agent may be subjected to a surface treatment in advance, or a surface treatment may be performed by adding a sizing agent or a surface treatment agent when preparing the PBT composition. The amount of the reinforcing filler to be added is usually 150 parts by weight or less, preferably 5 to 100 parts by weight, based on 100 parts by weight of the PBT.

The reinforced filler material can be blended with other filler materials. Other filler materials to be blended may be, for example, plate-like inorganic filler, ceramic beads, asbestos, strontite, talc, clay, mica, zeolite, kaolin, potassium titanate, barium sulfate, titanium oxide, cerium oxide, aluminum oxide. , magnesium hydroxide, etc. These fillers may be used alone or in combination of two or more. By blending the plate-shaped inorganic filler, the anisotropy and warpage of the molded article can be reduced. The plate-like inorganic filler may be, for example, glass cullet, mica, metal foil or the like. It is preferable to use glass shards among these. The amount of the other filler to be added is usually 150 parts by weight or less, preferably 5 to 100 parts by weight, more preferably 10 to 70 parts by weight, based on 100 parts by weight of the PBT.

(flammable agent)

In order to impart flame retardancy, it can be incorporated into a flame retardant. The flame retardant is not particularly limited, and specific examples thereof include an organic halogen compound, an antimony compound, a phosphorus compound, other organic flame retardants, inorganic flame retardants, and the like. The organic halogen compound may be, for example, a brominated polycarbonate, a brominated epoxy resin, a brominated phenoxy resin, a brominated polyphenylene ether resin, a brominated polystyrene resin, a brominated bisphenol A, or a polybromobenzyl bromide. Ester and the like. The hydrazine compound may be, for example, antimony trioxide, antimony pentoxide, sodium citrate or the like. The phosphorus compound may be, for example, a phosphate, a polyphosphoric acid, an ammonium polyphosphate, a red phosphorus or the like. Other organic flame retardants may be, for example, nitrogen compounds such as melamine, cyanuric acid, and the like. Other inorganic flame retardants may be, for example, aluminum hydroxide, magnesium hydroxide, barium compounds, boron compounds, and the like. These flame retardants may be used alone or in combination of two or more. The amount of the flame retardant to be added is usually 50 parts by weight or less, preferably 10 to 40 parts by weight, per 100 parts by weight of the PBT.

(other additives)

It can be blended into other conventional additives and the like as needed. The additive is not particularly limited, and examples thereof include a stabilizer such as an antioxidant and a heat stabilizer, and further, for example, a slip agent, a catalyst deactivator, a crystal nucleating agent, a crystallization accelerator, and the like. These additives can be added during or after the polymerization. Further, in PBT, in order to impart desired properties, it is also possible to incorporate, for example, a stabilizer such as a UV absorber or a weather stabilizer; a colorant such as a dye; an antistatic agent, a foaming agent, a plasticizer, and impact resistance. Improver, etc. These additives may be used alone or in combination of two or more. The amount of the other additive to be added is usually 5 parts by weight or less, preferably 0.05 to 2 parts by weight, per 100 parts by weight of the PBT.

(resin other than PBT)

A resin other than PBT may be blended as needed. Resins other than PBT can be, for example, polyethylene, polypropylene, polystyrene, polyacrylonitrile, polymethacrylate, ABS resin, polycarbonate, polyamide, polyphenylene sulfide, liquid crystal polyester, polycondensation. A thermoplastic resin such as an aldehyde or a polyphenylene ether; a thermosetting resin such as a phenol resin, a melamine resin, a polyoxyxylene resin, or an epoxy resin. These thermoplastic resins and thermosetting resins may be used in combination of two or more kinds. The amount of the resin to be added other than PBT is usually 90 parts by weight or less, preferably 1 to 70 parts by weight, more preferably 3 to 50 parts by weight, per 100 parts by weight of PBT.

(mixing method)

The method of blending the above various additives and resins is not particularly limited, and it is preferable to use a uniaxial or biaxial extruder having a defoaming device capable of being discharged from an exhaust port as a kneading machine. Each component may be supplied to the kneading machine in an integrated manner, including additional components, or It can also be supplied in order. Further, two or more components selected from the respective components, including the additional components, may be previously mixed.

(forming method)

The PBT and the composition thereof obtained by using the BG of the present invention for the production of PBT can be formed by a general molding method (that is, injection molding, hollow molding, extrusion molding, press molding, or the like) of the related thermoplastic resin. A shaped body is formed.

Next, a method of manufacturing PBT according to the gist of the present invention will be described. The method for producing PBT is a method for producing PBT from a dicarboxylic acid component containing a terpenic acid and/or a paraphthalic acid alkyl ester as a main component, and a diol component containing BG as a main component. The BG system contains a cyclic acetal compound in an amount of 50 to 600 ppm by weight, and the alkali compound is added before the esterification reaction step and/or the transesterification reaction step.

[1] Polyester raw materials

The PBT of the present invention is subjected to esterification reaction and/or transesterification of a dicarboxylic acid component containing a tert-citric acid and/or a para-alkyl phthalate as a main component, and a diol component containing a BG as a main component. After the reaction, it is obtained by a polycondensation reaction.

The description of the <dicarboxylic acid component>, (p-citric acid component), and (dicarboxylic acid component other than the phthalic acid component) is the same as the above description.

<diol component>

In the present invention, a diol component containing BG as a main component is used.

(BG)

In the present invention, the BG system utilizes petrochemical methods and/or includes fermentation derived from biomass resources. The manufacturing process of the steps is carried out. For example, using the raw material butadiene, acetic acid and oxygen to carry out the oxime oxidation reaction, to obtain the diethyl ether oxybutene which is an intermediate, and then the diethyl ethoxybutene is hydrogenated and hydrolyzed to obtain BG; BG obtained by hydrogenating using maleic acid, succinic acid, maleic anhydride and/or fumaric acid as raw materials; using acetylene as a raw material, contacting with aqueous formaldehyde solution to obtain butyne a diol obtained by subjecting a diol to hydrogenation; a propylene obtained by oxidizing or acetylating propylene to obtain an allyl alcohol, which is subjected to a carbonyloxy reaction and hydrogenation; and a succinic acid obtained by a fermentation method, BG which is hydrogenated again; BG obtained by directly fermenting biomass such as sugar

The BG obtained by these methods forms an acetal compound by the presence of an alcoholic OH or an aldehyde in the formation reaction. Various acetals can be produced by using a raw material in the production of BG, and the cyclic acetal compound content in the BG of the present invention is 50 to 600 ppm by weight.

The content of the cyclic acetal compound in BG used in the present invention can be adjusted by, for example, purification conditions including hydrogenation and distillation when BG is produced by a petrochemical method.

The content of the cyclic acetal compound in the BG used in the present invention is 50 to 600 ppm by weight, and if it is at least the above lower limit value, it can be used for the production of PBT without reinforcing the BG purification step. Both the energy unit level and the cost level are advantageous. On the other hand, the upper limit is preferably 600 ppm by weight or less. More preferably, it is 300 ppm by weight or less, and particularly preferably 150 ppm by weight or less. If it is below the above upper limit value, the color tone of the PBT tends to be less likely to deteriorate.

Further, the cyclic acetal compound of the present invention may, for example, be a compound represented by the above formula (I).

The reason is that the cyclic acetal compound is decomposed during the reaction to form an aldehyde compound, and the aldol is condensed to form a coloring matter, and it is judged that the color tone of PBT is deteriorated. reason.

The BG content in the diol component of the present invention is the same as that described in <diol component>.

Description of (diol component other than BG), <other copolymerizable component>, and <catalyst and additive> (esterification reaction or transesterification catalyst) and (polycondensation catalyst) Same as the previous description.

(alkali compound)

In the present invention, the alkali compound is added before the esterification reaction step.

The alkali compound may, for example, be a metal element of Group IA of the periodic table and/or a metal element of Group IIA of the periodic table. Further preferred is a compound containing a hydroxyl group.

Among them, sodium hydroxide and potassium hydroxide are preferred from the viewpoints of solubility in the reaction system and color tone of the obtained PBT.

Other alkali compounds other than this may be, for example, ammonia, an amine, and the like.

Among them, from the viewpoint of the solubility to the reaction system and the color tone of the obtained PBT, tetramethylammonium hydroxide is preferred.

In the present invention, the alkali compound is preferably added to at least one of BG, a slurry of BG and p-citric acid, an esterification reaction step, and the like.

When the alkali compound contains a metal element of Group IA of the periodic table and/or a metal element of Group IIA of the periodic table, the metal element preferably contains 0.1 to 15 ppm by weight in the obtained PBT. More preferably, it is 1 to 10 ppm by weight. If it is within this range, it is easy to obtain a PBT having a good hue.

Further, the content of the above metal element is the weight of the metal element in the alkali compound, Divided by the weight of the PBT assumed to be obtained from the dicarboxylic acid component used and its equivalent amount of the diol component.

When a cyclic acetal compound is present in BG, the cyclic acetal compound is decomposed by water generated in the esterification reaction or an acid component in the system to form an aldehyde compound. The aldehyde compound generates a coloring matter by condensation of an aldol. The alkali addition is an acidic component in the neutralization system, and as a result, the effect of suppressing the formation reaction of the aldehyde compound is exhibited. However, the excessive addition of the base causes a reaction to form an aldehyde compound, and it is necessary to determine an appropriate amount of the added amount.

(manufacturing procedure), (esterification reaction conditions), (transesterification reaction conditions), (esterification reaction apparatus / transesterification reaction apparatus), (esterification reaction apparatus / transesterification reaction apparatus) in the production method of (reaction aid), (other additives), PBT, (polycondensation reaction conditions), (polycondensation reaction device), (PBT granules) and (manufacturing program examples), PBT physical properties (inherent viscosity) and (hue b value), and PBT composition items Description of (stabilizer), (release agent), (filler), (flammable agent), (other additives), (resin other than PBT), (mixing method), and (forming method) Description.

[Examples]

Hereinafter, the present invention will be described in more detail by way of examples, but the present invention is not limited to the following examples. In addition, the physical properties and the measurement methods of the evaluation items used in the following examples are as follows.

<Analysis method> (1) Content of 2-methyl-1,3-propanediol and cyclic acetal compound in BG

A gas chromatograph (GC-2025 model manufactured by Shimadzu Corporation) was used, and a polar column ("DB-WAX" manufactured by J&W Co., Ltd.) and a non-polar column ("DB-1" manufactured by J&W Co., Ltd.) were used. The component content of each peak contained in the BG was determined in accordance with the corrected area percentage method calculated from the effective carbon coefficient. Further, since the amount of the cyclic acetal component is a trace amount, it is injected into the gas phase chromatography analyzer without performing sample dilution using a solvent.

Further, the cyclic acetal compound can be detected by GC-MS and can be distinguished from other components contained in BG. The representative cyclic acetal compound used in the analysis is as follows, and it is not necessary to assign all fragments and signals.

2-ethyl-1,3-two Heptane (cyclic acetal)

GC-MS (E1): 71, 83, 101, 102

Furthermore, 2-ethyl-1,3-di using a gas chromatography layer analysis device is described. A method for calculating the representative concentration of heptane. First, using the measurement using a polar column (Condition 1), 2-methyl-1,3-propanediol and 2-ethyl-1,3-di were determined from the peak area of the retention time of 38 minutes. The total concentration of heptane (because the spikes of the two substances are repeated). Next, using a measurement using a nonpolar column (Condition 2), the concentration of only 2-methyl-1,3-propanediol was determined from the peak area of the residence time of 14 minutes. From 2-methyl-1,3-propanediol to 2-ethyl-1,3-di In the total concentration of heptane, after subtracting the concentration of 2-methyl-1,3-propanediol, 2-ethyl-1,3-di was obtained. The concentration of heptane.

The details of the GC conditions are as follows.

Condition 1 (polar column)

. Analysis column: J&W DB-WAX, 60m×0.320mmid, df=0.5μm

. Column flow: 1mL/min

. Split ratio: 1/90

. Oven temperature: 70 ° C (15 min) → 10 ° C / min → 150 ° C, 175 ° C × 45 min

. Sample chamber, detector temperature: 240 ° C

. Injection volume: 1μL

. Carrier gas: nitrogen

Condition 2 (non-polar column)

. Column: J&W DB-1, 60m×0.25mmid, df=1μm

. Column temperature: 50 ° C (7 min) → 10 ° C / min → 250 ° C (20 min)

. Injection mode: split (1/100)

. Sample chamber, detector temperature: 240 ° C

. Injection volume: 0.8μL

. Carrier gas: nitrogen

Further, the content of the cyclic acetal compound was calculated from the ratio of the area value of BG to the area value of the cyclic acetal compound when the correction was performed without using the effective carbon coefficient.

(2) Method for determination of ruthenium carbonyl (CO) valence

The hydrazine carbonyl value is obtained by heating BG under acidic conditions, and then hydrolyzing the acetal compound in BG to a carbonyl component, and then reacting with hydroxylamine hydrochloride to measure the produced hydrochloric acid by potentiometric titration. The value of the total amount of the carbonyl component in the sample is obtained.

5 g of BG sample was weighed in a 100 mL conical beaker, and 10 mL of hydroxylamine hydrochloride solution was correctly added to the sample and the blank beaker by using a porous pipette [50 g of hydroxylamine hydrochloride (reagent grade) was dissolved in 100 mL of water, and hydrochloric acid was added. 8.5 mL, and further adding ethanol (reagent grade) to make a total amount of 1 L of the solution], it was covered with a cooling tube, and heated at 60 ° C for 2 hours in an oil bath. After cooling to room temperature, 40 mL of methanol was added to the measuring cylinder, and the mixture was titrated using an automatic titrator ("AUT-501" manufactured by Toago DKK Co., Ltd.) while stirring. The titration solution was a 0.1 N methanolic potassium hydroxide solution. After the end of the titration, the hydrazine carbonyl value is calculated using the following formula (2).

Σ carbonyl value = (A1-B1) × f × 5.6 / S1 (mgKOH / g). . . (2)

(The amount of 0.1N potassium hydroxide required for titration of A1 is (mL); the titration of 0.1N potassium hydroxide (mL) required for titration of B1 in the blank; the amount of S1 sample (g) ;f is a factor of 0.1N potassium hydroxide.)

(3) Intrinsic viscosity (IV)

Use the Uberode viscometer to find the following essentials. That is, using a mixed solvent of phenol/tetrachloroethane (weight ratio of 1/1), the concentration of 1.0 g/dL of the polymer solution and the solvent-only drop time were measured at 30 ° C, and the following formula (4) was obtained. take.

IV=((1+4KH η ^sp )0.5-1)/(2KHC). . . (4)

(where η ^SP = η / η ⁰ -1; η-based polymer solution drop seconds; η ^0- based solvent drop seconds; C-based polymer solution concentration (g/dL); KH-based Huggins constant. KH is 0.33.)

(4) The terminal carboxyl group concentration of PBT (equivalent/ton)

0.5 kg of PBT was dissolved in 25 mL of benzyl alcohol, and titrated with a 0.01 mol/L benzyl alcohol solution of sodium hydroxide, and calculated according to the following formula.

Terminal carboxyl concentration = (A-B) × 0.1 × f / W (equivalent / ton)

Among them, the amount of benzyl alcohol solution (μL) of 0.01N sodium hydroxide required for the titration of the A system; the amount of benzyl alcohol solution (μL) of 0.01 mol/L sodium hydroxide required for the titration of the B system in the blank; PBT sample amount (g); f is 0.01 mol/L sodium hydroxide titer.

(5) particle tones

The granular polyester is filled in a cylindrical powder measuring tank having an inner diameter of 30 mm and a depth of 12 mm. In the measurement of the color difference meter Z300A (manufactured by Nippon Denshoku Industries Co., Ltd.), the b value specified by the Hunter color difference color coordinates in the system is described in Reference Example 1 of JIS Z8730 (1980). By using the reflection method, the measurement tank was measured by measuring the values of four places at a total of 90 degrees per rotation, and obtaining a simple average value.

(6) Metal atom concentration in PBT

PBT was subjected to wet decomposition using high-purity sulfuric acid and nitric acid for the electronics industry, and was measured using a high-resolution ICP (Iductively Coupled Plasma)-MS (Mass Spectrometer) (manufactured by Thermo Quest).

(Reference example)

BG (1000 parts by weight) produced by the allyl alcohol method was subjected to simple distillation at a pressure of 0.2 kPa and an internal temperature of the flask of 102 °C. Each of the preliminary fraction-1 (500 parts by weight) and the preliminary fraction-2 (200 parts by weight) were distilled off, and then 250 parts by weight of a middle distillate component was obtained. 50 parts by weight of the remaining component of the bottom of the pot was obtained.

The obtained middle distillate component was further subjected to simple distillation, and after 175 parts by weight of the preliminary fraction was taken, 62.5 parts by weight of a middle distillate component was obtained.

Among them, each fraction obtained in the analysis and the bottom of the pot were analyzed and determined according to the following. The quality is shown in Table 1.

BG produced by the allyl alcohol method is referred to as "BG-C", the preliminary fraction-1 is referred to as "BG-D", the preliminary fraction-2 is referred to as "BG-E", and the middle distillate component is referred to as "BG-E". The "BG-A", the residual component at the bottom of the pot is called "BG-F", and the middle distillate component which is simply distilled from the middle distillate component is called "BG-B".

(Example 1)

BG-A is stored in an oxygen-containing environment.

In other words, BG is charged into the three stainless steel bottles in such a manner that the volume of the gas phase portion is the same as the volume of the BG, and the air is replaced by a tank, and nitrogen is continuously supplied from the cylinder to a predetermined oxygen concentration, and the gas phase portion of the bottle is replaced. Until it is measured by an oxygen concentration meter to a predetermined oxygen concentration, and then blocked.

By this method, the gas phase portion was formed into an environment in which nitrogen of 3% air (oxygen concentration: 0.63%), nitrogen of 5% air (oxygen concentration: 1.05%), and nitrogen of 10% of air (oxygen concentration: 2.1%) were mixed. These were kept at 60 ° C for 10 days. The cyclic acetal content and the hydrazine carbonyl value of each BG were measured. The results are shown in Table 1. In addition, the "%" of the gas means "% by volume".

(Example 2)

BG-B was stored in an oxygen-containing environment in the same manner as in Example 1. The results are shown in Table 1.

(Comparative Example 1)

BG-C was stored in an environment containing 1.05% of oxygen in the same manner as in Example 1. The results are shown in Table 1.

(Comparative Example 2)

BG-D was stored in an environment containing 1.05% of oxygen in the same manner as in Example 1. The results are shown in Table 1.

(Comparative Example 3)

BG-E was stored in an environment containing 1.05% of oxygen in the same manner as in Example 1. Result list 1 is shown.

(Comparative Example 4)

BG-F (the amount of the cyclic acetal compound "<1" means the measurement limit (less than 1 ppm by weight), and was stored in an atmosphere containing 1.05% of oxygen in the same manner as in Example 1. The results are shown in Table 1.

(Example 3)

In a reaction vessel equipped with a stirring device, a nitrogen inlet, a heating device, a thermometer, a distillation tube, and a decompression exhaust port, 113 parts by weight of p-phthalic acid, 133 parts by weight of BG-A, and the like are charged. 0.7 parts by weight of a 6 wt% BG solution of tetra-n-butoxytitanium for the catalyst was replaced by nitrogen-pressure reduction to form a nitrogen atmosphere in the system.

Next, the system was heated to 150 ° C while stirring, and then the temperature was raised to 220 ° C over 1 hour under atmospheric pressure, and the produced water was distilled off over 2 hours to carry out an esterification reaction.

Next, magnesium acetate tetrahydrate was dissolved in water, followed by addition of a BG solution (magnesium acetate tetrahydrate, water, BG weight ratio 1:2:97) prepared by adding magnesium acetate tetrahydrate to 1% by weight. Parts by weight.

Next, after maintaining at 220 ° C for 0.25 hours, it was maintained at 245 ° C for 0.75 hours. On the other hand, the pressure was reduced to 0.07 kPa from the start of the polymerization for 1.5 hours, and the polycondensation reaction was carried out for 0.8 hours under the same degree of decompression. Then, a nitrogen pressure is applied to return the reaction system to normal pressure and the polycondensation is ended.

The obtained PBT was taken out from the bottom of the reaction tank into a strand, and after diving into water at 10 ° C, the strand was cut by a cutter to obtain pelletized PBT.

The intrinsic viscosity of the obtained PBT was 0.83 dL/g, the terminal carboxyl group concentration was 6 equivalent/ton, and the color tone Co-b was 2.3, and the color tone was excellent. The results are shown in Table 2.

(Example 4)

In the third embodiment, BG-A was used in a state in which the gas phase portion of the storage container was filled with nitrogen (oxygen concentration: 1.05 vol%) mixed with 5% by volume of air, and BG was maintained at 60 ° C for 10 days. The same operation as in Example 3 was carried out, and the obtained PBT had an intrinsic viscosity of 0.83 dL/g, a terminal carboxyl group concentration of 6 equivalent/ton, and a color tone Co-b of 2.6, and was excellent in color tone. The results are shown in Table 2.

(Example 5)

Except that in Example 3, the same operation as in Example 3 was carried out except that BG-A was used instead of BG-B, and the intrinsic viscosity of the obtained PBT was 0.83 dL/g, and the terminal carboxyl group concentration was 6 equivalents. / ton, the color tone Co-b is 1.8, and the color tone is excellent. The results of the b value are shown in Table 2.

(Example 6)

Except that in Example 4, the same operation as in Example 4 was carried out except that BG-A was used instead of BG-B, and the obtained PBT had an intrinsic viscosity of 0.83 dL/g and a terminal carboxyl group concentration of 6 equivalents. / ton, the solution haze is 0.1%, the color tone Co-b is 2.0, and the color tone is excellent. The results of the b value are shown in Table 2.

(Comparative Example 5)

Except that in Example 3, the same operation as in Example 3 was carried out except that BG-A was used instead of BG-C, and the intrinsic viscosity of the obtained PBT was 0.83 dL/g, and the terminal carboxyl group concentration was 6 equivalents. / ton, color Co-b is 3.0. The results of the b value are shown in Table 2.

(Comparative Example 6)

Except that in Example 4, the same operation as in Example 4 was carried out except that BG-A was used instead of BG-C, and the intrinsic viscosity of the obtained PBT was 0.83 dL/g, and the terminal carboxyl group concentration was 6 equivalents. / ton, color Co-b is 3.6. The results of the b value are shown in Table 2.

(Comparative Example 7)

Except that in Example 3, the same operation as in Example 3 was carried out except that BG-A was used instead of BG-D, and the intrinsic viscosity of the obtained PBT was 0.83 dL/g, and the terminal carboxyl group concentration was 6 equivalents. / ton, color Co-b is 4.1. The results of the b value are shown in Table 2.

(Comparative Example 8)

Except that in Example 4, the same operation as in Example 4 was carried out except that BG-A was used instead of BG-E, and the intrinsic viscosity of the obtained PBT was 0.83 dL/g, and the terminal carboxyl group concentration was 6 equivalents. / ton, color Co-b is 4.7. The results of the b value are shown in Table 2.

(Comparative Example 9)

Except that in Example 3, the same operation as in Example 3 was carried out except that BG-A was used instead of BG-E, and the obtained PBT had an intrinsic viscosity of 0.83 dL/g and a terminal carboxyl group concentration of 6 equivalents. / ton, color Co-b is 2.5. The results of the b value are shown in Table 2.

(Comparative Example 10)

Except that in Example 4, the same operation as in Example 4 was carried out except that BG-A was used instead of BG-D, and the intrinsic viscosity of PBT obtained was 0.83 dL/g, terminal carboxylate. The base concentration was 6 equivalents/ton, and the color tone Co-b was 3.0. The results of the b value are shown in Table 2.

(Comparative Example 11)

Except that in Example 3, the same operation as in Example 3 was carried out except that BG-A was used instead of BG-F, and the obtained PBT had an intrinsic viscosity of 0.83 dL/g and a terminal carboxyl group concentration of 6 equivalents. / ton, color Co-b is 8.0. The results of the b value are shown in Table 2.

(Comparative Example 12)

Except that in Example 4, the same operation as in Example 4 was carried out except that BG-A was used instead of BG-D, and the obtained PBT had an intrinsic viscosity of 0.83 dL/g and a terminal carboxyl group concentration of 6 equivalents. / ton, color Co-b is 9.1. The results of the b value are shown in Table 2.

From the results of Tables 1 and 2, it was found that the effects of suppressing the increase in the carbonyl group value of the cyclic acetal and the oxime were clearer than those of Comparative Examples 1 and 2. Similarly, in Examples 4 and 6, the effect of suppressing the increase in the b value of PBT was clearer than in Comparative Examples 10 and 12.

(Example 7)

In a reaction vessel equipped with a stirring device, a nitrogen inlet, a heating device, a thermometer, a distillation tube, and a decompression exhaust port, 113 parts by weight of p-phthalic acid and a cyclic acetal compound (2- Ethyl-1,3-di Heptane) [Prepared to obtain PBT as NaOH for alkali compound, in a form of 1.4 ppm by weight of Na] 187 ppm of BG (183 parts by weight), and more filled with tetra-positive as a catalyst 0.7 parts by weight of a 6 wt% BG solution of butoxide titanium, which was replaced by nitrogen-pressure reduction to form a nitrogen atmosphere in the system.

Next, the system was heated to 150 ° C while stirring, and then the temperature was raised to 220 ° C over 1 hour under atmospheric pressure, and the produced water was distilled off over 2 hours to carry out an esterification reaction.

Next, magnesium acetate tetrahydrate was dissolved in water, followed by addition of a BG solution (magnesium acetate tetrahydrate, water, BG weight ratio 1:2:97) prepared by adding magnesium acetate tetrahydrate to 1% by weight. Parts by weight.

Next, after maintaining at 220 ° C for 0.25 hours, it was maintained at 245 ° C for 0.75 hours. On the other hand, the pressure was reduced to 0.07 kPa from the start of the polymerization for 1.5 hours, and the polycondensation reaction was carried out for 0.8 hours under the same degree of decompression. Then, a nitrogen pressure is applied to return the reaction system to normal pressure and the polycondensation is ended.

The obtained PBT was taken out from the bottom of the reaction tank into a strand, and after diving into water at 10 ° C, the strand was cut by a cutter to obtain pelletized PBT.

The intrinsic viscosity of the obtained PBT was 0.83 dL/g, the terminal carboxyl group concentration was 6 equivalent/ton, the solution haze was 0.1%, and the color tone Co-b was 2.6, and the color tone and transparency were excellent. Result sorting as shown in Table 3.

(Example 8 to Example 11, Comparative Example 13 to Comparative Example 15, and Reference Example 1 to Reference Example 4)

In the same manner as in Example 7, except that the content of the cyclic acetal compound in BG and the amount of the alkali compound added were changed as shown in Table 3, PBT was obtained.

The results are shown in Tables 3 and 4.

Here, ΔCo-b shows the difference between the Co-b values of Reference Example 1 in Examples 7 to 10, and the difference between the Co-b values of Reference Example 2 in Example 11 is compared. In Examples 13 and 14, the difference from the Co-b value of Reference Example 3 is shown, and in Comparative Example 15, the difference from the Co-b value of Reference Example 4 is shown.

Comparison of Examples 7 to 10 with Reference Example 1 and comparison between Example 11 and Reference Example 2 revealed that the effect of adding an alkali compound was clear.

On the other hand, when BG having a cyclic acetal compound content of 0 was used (Comparative Examples 13 and 14), there was no effect of adding an alkali compound, and the opposite Co-b value was increased. Further, when the content of the cyclic acetal compound was 30 ppm by weight (Comparative Example 15), the effect of adding an alkali compound was not observed.

The present invention has been described with reference to the detailed and specific embodiments thereof, and various changes and modifications may be added without departing from the spirit and scope of the invention. The present application is based on a Japanese patent application filed on Jul. 2, 2013 (Japanese Patent Application No. 2013-139140), and Japanese Patent Application No. 2013-194195 filed on Sep. 19, 2013. Refer to its content and refer to it in this case.

(industrial availability)

According to the present invention, when the BG is stored, if it is difficult to completely replace the nitrogen phase, even if it is in contact with the remaining oxygen for a long period of time, BG having less deterioration in quality can be obtained, and a polyester having a good color tone can be obtained.

According to the present invention, even when BG containing a certain amount of a cyclic acetal compound is used, PBT having a good color tone can be obtained, and the BG purification cost and the like can be greatly reduced.

Claims (5)

A composition containing 1,4-butanediol, which contains 2-methyl-1,3-propanediol, and contains 1 part by weight or more and 50 parts by weight or less of a cyclic acetal compound. The 1,4-butanediol-containing composition according to the first aspect of the invention, wherein the ruthenium carbonyl value measured by the potentiometric titration method is 0.50 mgKOH/g or less. A method for producing a polyester by using a dicarboxylic acid component containing a dicarboxylic acid and/or an alkyl dicarboxylate as a main component, and a 1,4-butylene containing the first or second aspect of the patent application scope The diol component having the composition of the diol as a main component is subjected to an esterification reaction and/or a transesterification reaction, followed by a polycondensation reaction to obtain a polyester. A method for producing a polyester according to claim 3, wherein the polyester is polybutylene terephthalate. A method for storing a composition containing 1,4-butanediol, which is a method for storing a composition containing 1,4-butanediol of claim 1 or 2 in an oxygen-containing environment, and The oxygen concentration of the environment is from 0.1% by volume to 10% by volume.