TW201408724A - Method of preparation for biodegradable co-polyester resin - Google Patents

Abstract

There is provided a method of preparation for a biodegradable co-polyester resin, the method including forming an oligomer through an esterification reaction of an aliphatic dihydroxy monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer, wherein the esterification reaction includes a primary esterification reaction, and a secondary esterification reaction that is performed at a higher temperature than that of the primary esterification reaction and the aliphatic dihydroxy monomer is further added during the secondary esterification reaction. According to the present invention, by replenishing an aliphatic dihydroxy monomer that is insufficient in a temperature increasing step, non-reacted aromatic dicarboxylic acid is effectively controlled and thus oligomer can be completely formed, resulting in giving sufficient properties to a polymer.

Description

Method for preparing biodegradable copolyester resin

The present invention relates to a method for preparing a biodegradable copolyester resin, and particularly to the preparation of a biodegradable copolyester resin, in order to supplement the aliphatic which may be consumed in the temperature rising step of the esterification reaction. An aliphatic dihydroxy monomer, a preparation method in which a small amount of an aliphatic dihydrocarbyl monomer is additionally added at the end of the esterification reaction to control the unreacted material, thus including complete oligomer formation and imparting to the organism Decomposes the full properties of the copolyester resin.

The biodegradable resin is a synthetic resin developed into a new material, which can be decomposed into water and carbon dioxide or water and methane gas by microorganisms existing in nature such as bacteria, algae or fungi without causing environmental pollution.

The biodegradable resin widely used together with cellulose-based polymers and starch is composed of an aliphatic polyester such as polylactic acid (PLA) or polybutylene succinate (polybutylene succinate). PBS), polyethylene succinate (PES) and polycaprolactone (PCL) resin.

This aliphatic polyester resin has a high degree of biodegradability but has the disadvantage of being poor in mechanical properties. Therefore, in order to enhance the mechanical strength of the aliphatic polyester resin, a synthetic method in which an aromatic monomer is added by a method of adding an aromatic monomer in the preparation of a biodegradable resin is developed to prepare an organism in the form of an aliphatic-aromatic copolymer. A method of decomposing a resin.

Poly(butylene adipate-co-terephthalate (PBAT) is a representative biodegradable resin in the form of the above aliphatic-aromatic copolymer. Adipic acid-pair The phthalic acid-butylene ester copolymer can be firstly removed by condensation polymerization as an aromatic monomer of dimethyl terephthalate (DMT) and 1,4-butanediol as an aliphatic monomer ( The methanol produced by 1,4-butanediol, BDO) is then prepared by removing water produced by condensation polymerization after addition of adipic acid (AA).

The aromatic monomer typically used today is dimethyl terephthalate. Since dimethyl terephthalate has an advantage that it can be reacted at a reaction temperature of 180 ° C or lower, the reaction can be easily carried out. However, dimethyl terephthalate has the disadvantage of being expensive, thus increasing the burden on the cost.

Therefore, there has been a continuous effort to prepare copolymers using aromatic monomers which are less expensive than dimethyl terephthalate. A representative example is a method in which terephthalate (TPA) is used as an aromatic dicarboxylic acid in the synthesis reaction of the copolymer.

However, unlike dimethyl terephthalate, terephthalic acid is high The temperature does not have a melting point and sublimates. Further, in the process of preparing the biodegradable polyester resin, the terephthalic acid in the 1,4-butanediol as a representative aliphatic monomer is present at a normal pressure and at a temperature lower than 225 ° C. The state of the slurry, when the esterification reaction occurs at a temperature of 225 ° C or higher, it is converted into a state of a transparent solution. Therefore, in order to uniformly react terephthalic acid and 1,4-butanediol, the reaction temperature must be 225 ° C or higher. However, under acidic conditions, 1,4-butanediol is converted to tetrahydrofuran (THF) at temperatures above 190 °C. Therefore, the process of preparing a copolymer using an aromatic monomer which requires a high reaction temperature such as terephthalic acid has a drawback in that the amount of 1,4-butanediol converted to tetrahydrofuran needs to be considered, and an excess of 1 is required. , 4-butanediol.

According to the invention, in order to avoid the conversion of such aliphatic dihydrocarbyl monomers Alternatively, the aliphatic dihydrocarbyl mono system is allowed to react with an aliphatic dicarboxylic acid monomer such as adipic acid at a relatively low temperature, and then with an aromatic dicarboxylic acid monomer such as terephthalic acid. reaction.

However, for adipic acid-terephthalate-butadiene copolymer That is, since an aromatic monomer requiring high reaction temperature conditions such as terephthalic acid is added after the reaction of 1,4-butanediol and adipic acid, and 1,4-butanediol is raised to a temperature In the step of the esterification reaction, it is converted to tetrahydrofuran, and 1,4-butanediol is not sufficient. Thus there will be a disadvantage of the presence of a large amount of unreacted terephthalic acid.

In particular, in the step of increasing the temperature, it takes more time to reach a temperature at which the esterification reaction can proceed to increase the amount of tetrahydrofuran produced. because Thus, 1,4-butanediol is not sufficient, so that a sufficient degree of polymerization cannot be obtained in the final condensation polymerization process.

Therefore, due to the need to mention during the terephthalate esterification reaction Equipment that rises in temperature rise rate will also have a cost. Further, when a coil is installed in the reactor, the coil may interfere with the flow of the reactants during agitation, resulting in a decrease in reactivity.

In summary, the process of preparing biodegradable copolyester resin In order to supplement the amount of 1,4-butanediol converted to tetrahydrofuran to cause 1,4-butanediol deficiency in the temperature rising step of the esterification reaction, the present invention proposes to add a small amount at the end of the esterification reaction. The 1,4-butanediol is reacted with all of the unreacted terephthalic acid to include a complete oligomeric polymer.

The invention provides a preparation method of a biodegradable copolyester resin The biodegradable copolyester resin can have sufficient characteristics by including a complete oligomeric polymer, wherein the complete oligomeric polymer is reacted through all unreacted aromatic monomers in the esterification reaction. And formed.

In order to achieve the above object, according to an embodiment of the present invention, a A method for preparing a biodegradable copolyester resin, comprising forming an oligopolymer by esterification reaction of an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer, wherein the esterification reaction comprises Primary esterification reaction and secondary esterification reaction, secondary esterification reaction is carried out at a higher temperature than the first-order reaction, and in the secondary esterification reaction An aliphatic dihydrocarbyl monomer is additionally added.

Regarding the preparation method of the biodegradable copolyester resin of the present invention, the primary and secondary esterification reactions can be carried out by simultaneously adding an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer. Alternatively, it may be carried out by adding an aliphatic dihydrocarbyl monomer and an aliphatic dicarboxylic acid monomer in the first esterification reaction, and then adding an aromatic dicarboxylic acid monomer in the secondary esterification reaction.

The additional aliphatic dihydrocarbyl mono system is preferably in the range of 0.05 mol to 0.5 mol, and the aliphatic divalent, relative to the total of 1 mol of the aliphatic dicarboxylic acid and the aromatic dicarboxylic acid. The hydrocarbyl monomer is preferably additionally added in the secondary esterification reaction when no water is produced from the condenser.

Preferably, the aliphatic dihydrocarbyl mono system is selected from the group consisting of 1,2-ethanediol, 1,3-propanediol, and 1,2-butanediol (1) , 2-butanediol), 1,6-hexanediol, 1,4-hexanediol, 1,4-butanediol, 1,4-cyclohexane A group consisting of 1,4-cyclohexanediol, 1,4-cyclohexane dimethylenediol, neopentyl glycol, or a combination thereof.

Preferably, the aliphatic dicarboxylic acid monomer can be represented by the chemical formula 1 or an anhydride or a derivative thereof: [Chemical Formula 1] HOOC-(CH2)n-COOH

(where n is 2 to 12)

Further, preferably, the aromatic dicarboxylic acid single system comprises one or more selected from the group consisting of phthalic acid (PA), phthalic anhydride, isophthalic acid (IPA). ), a group consisting of terephthalic acid, 2,6-dicarboxylic acid, anhydride, and derivatives thereof.

Further, preferably, the first esterification reaction may be first carried out at a temperature ranging from 160 ° C to 185 ° C, and then the secondary esterification reaction may be carried out at a temperature ranging from 225 ° C to 250 ° C.

Further, in the preparation method of the biodegradable copolyester according to the present invention, preferably, the aliphatic-aromatic oligopolymer obtained by the primary and secondary esterification reaction may additionally have a temperature of from 220 ° C to 250 ° C. Condensation polymerization is carried out for a period of 40 to 300 minutes under a vacuum of less than 2 torr.

Further, preferably, the preparation method of the biodegradable copolyester may be additionally added after the condensation polymerization reaction and the chain extender is allowed to react.

The embodiments of the present invention will be described in detail below. Although the invention has been shown and described with respect to the disclosed embodiments, the invention is Those skilled in the art can make various changes and refinements without departing from the spirit and scope of the present invention.

The present invention relates to a method for preparing a biodegradable copolyester resin, wherein an esterified aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic diamide are produced during the preparation of the biodegradable copolyester resin. a carboxylic acid monomer to form an oligopolymer, but in order to supplement the aliphatic dihydrocarbyl monomer lost in the temperature rising step of the secondary esterification reaction, an aliphatic dihydrocarbyl monomer is additionally added at the end of the secondary esterification reaction The unreacted aromatic dicarboxylic acid monomer is controlled to form a complete oligopolymer.

Such a copolymer is an aliphatic-aromatic polyester obtained by a reaction of an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer.

More precisely, the present invention provides a process for the preparation of a biodegradable copolyester resin comprising esterification via an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer. Forming an oligopolymer, wherein the esterification reaction comprises a primary esterification reaction and a secondary esterification reaction, the secondary esterification reaction is carried out at a higher temperature than the primary esterification reaction, and a fat is additionally added in the secondary esterification reaction Group dihydrocarbyl monomer.

Herein, an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer, and an aromatic dicarboxylic acid monomer may be simultaneously added for primary and secondary esterification, or an aliphatic dihydrocarbyl monomer and fat may be added. The dicarboxylic acid monomer is subjected to a primary esterification reaction, and then an aromatic dicarboxylic acid monomer can be further added for the secondary esterification reaction.

Preparation process of biodegradable aliphatic-aromatic polyester resin Any aliphatic dihydrocarbyl monomer can be used as the aliphatic dihydrocarbyl monomer of the present invention without limitation as long as it can be used as a starting material. In particular, an aliphatic dihydrocarbyl monomer which tends to be converted in a high temperature reaction can be effectively used. More precisely, it is preferred to use a diol having 2 to 6 carbon elements, such as: 1,2-ethanediol, 1,3-propanediol, 1,2-butanediol, 1,6 - hexanediol, 1,4-hexanediol, 1,4-butanediol, 1,4-cyclohexanediol, 1,4-dimethylene glycol cyclohexane, neopentyl glycol or Combination of the above. In particular, it is preferred to use 1,4-butanediol.

Further, an aliphatic dicarboxylic acid monomer generally used in the art to which the present invention pertains can be used, and an aliphatic dicarboxylic acid monomer capable of reacting at a relatively low temperature is preferably used. More precisely, the aliphatic dicarboxylic acid monomer may include a monomer or an anhydride represented by the following Chemical Formula 1: or a derivative thereof: [Chemical Formula 1] HOOC-(CH2)n-COOH

(where n is 2 to 12, and preferably 2 to 8).

As a more precise example, succinic acid (SA), glutaric acid (GA), adipic acid, anhydride or a derivative thereof can be used as the aliphatic dicarboxylic acid monomer.

In the embodiment of the present invention, the aromatic dicarboxylic acid monomer may be selected from, but not limited to, phthalic acid, phthalic anhydride, isophthalic acid, terephthalic acid, 2,6- A group consisting of naphthalene dicarboxylic acid, anhydride or a derivative thereof. As long as it is a fragrance which can initiate an esterification reaction together with an aliphatic dihydrocarbyl monomer, particularly at a high temperature The family monomer can be effectively used to improve the mechanical properties of the biodegradable resin composed of a homopolymer of an aliphatic polyester and an aromatic dicarboxylic acid monomer.

As an example of the aromatic dicarboxylic acid monomer, terephthalic acid has an advantage of being lower in price than dimethyl terephthalate which is generally an aromatic monomer. However, unlike dimethyl terephthalate which can react even at temperatures of 185 ° C or lower, terephthalic acid can only initiate homogeneous esters with aliphatic dihydrocarbyl monomers at temperatures of 225 ° C or higher. Reaction.

However, in the examples of the present invention, since 1,4-butanediol is used as an example of the aliphatic dihydrocarbyl monomer, 1,4-butanediol is converted to tetrahydrofuran at a temperature of 190 ° C or higher. The 1,4-butanediol is converted in the temperature rising step of the secondary esterification reaction.

In accordance with an embodiment of the present invention, in order to complement the conversion of the aromatic dicarboxylic acid monomer, an aliphatic dihydrocarbyl monomer is additionally added at the end of the secondary esterification reaction to initiate complete oligomeric polymer formation.

At the same time, the aliphatic dihydrocarbyl monomer reacts first with the aliphatic dicarboxylic acid single system, thereby minimizing the amount of the aliphatic dihydrocarbyl monomer present in the monomer state. Therefore, in the subsequent high-temperature reaction with the aromatic dicarboxylic acid, the amount of conversion of the aliphatic dihydrocarbyl monomer may be lowered.

The two carboxylic acids contained in the aliphatic dicarboxylic acid monomer are esterified with one hydrocarbon group contained in the aliphatic dihydrocarbyl monomer. In this case, by adjusting the equivalent of the aliphatic dicarboxylic acid monomer relative to the aliphatic dihydrocarbyl monomer (equivalent Weight), an aliphatic dihydrocarbyl monomer may be bonded and bonded to an aliphatic dicarboxylic acid monomer or two aliphatic dihydrocarbyl monomers may be used to bond and bond thereto.

More precisely, in the examples of the present invention, 1,4-butanediol is used. The aliphatic dihydrocarbyl monomer is reacted with adipic acid to form an AA-BDO oligopolymer or a BDO-AA-BDO oligopolymer.

Mainly in the aliphatic dihydrocarbyl monomer and the aliphatic dicarboxylic acid monomer The first esterification reaction produced is terminated when the water flowing out of the esterification reaction reaches a theoretically calculated amount, so that no more water flows out (ie, corresponding to the total mole of the carboxylic acid contained in the aliphatic dicarboxylic acid monomer). The amount of water).

The primary esterification reaction can be, preferably, from 160 degrees C to 185 degrees The temperature range of C is carried out. The secondary esterification reaction carried out at a temperature higher than the primary esterification reaction can be carried out at a temperature ranging from 225 ° C to 250 ° C. More precisely, if terephthalic acid is used as the aromatic dicarboxylic acid monomer, the esterification reaction proceeds uniformly at a temperature of 225 ° C or higher. Therefore, it is preferred to carry out the secondary esterification reaction in a temperature range from 225 ° C to 250 ° C.

As described above, the aliphatic dihydrocarbyl monomer is, for example, a 1,4-butanediol system. Conversion to tetrahydrofuran at a temperature of 190 ° C or higher. Therefore, since 1,4-butanediol which forms an oligopolymer with an aromatic dicarboxylic acid monomer is converted during the secondary esterification reaction, there may be an unreacted aromatic dicarboxylic acid residue. In order to react with the unreacted aromatic dicarboxylic acid, a small amount of an aliphatic dihydrocarbyl monomer such as 1,4-butanediol is additionally added at the end of the secondary esterification reaction to initiate formation of a complete oligopolymer.

In this case, the number of additional aliphatic dihydrocarbyl monomers added The amount can be selected in consideration of the conversion ratio of the aliphatic dihydrocarbyl monomer. Preferably, the additional aliphatic dihydrocarbyl mono-system is in the range of 0.05 moles to 0.5 moles relative to the total of 1 mole of the aliphatic dicarboxylic acid monomer to the aromatic dicarboxylic acid monomer. At this time, when it is less than 0.05 mol, the effect of the addition cannot be exhibited, and when it exceeds 0.5 mol, the purpose of minimizing the amount of 1,4-butanediol desired in the examples of the present invention is exceeded.

The aliphatic dihydrocarbyl mono system is preferably added after the secondary esterification reaction, when no more water from the condenser is discharged.

The range of the amount of the aliphatic dihydrocarbyl monomer used can be adjusted in accordance with the desired esterification reaction. An aliphatic dicarboxylic acid monomer having a total molar content of 1 mol and an aromatic dicarboxylic acid monomer may be added with 1.0 mol or more of an aliphatic dihydrocarbyl monomer, and preferably, 1.3 mol may be added. Or more aliphatic dihydrocarbyl monomers. A preferred molar ratio of the aliphatic dicarboxylic acid monomer to the aromatic dicarboxylic acid monomer is from 0.4 to 0.9 to 0.6 to 0.1, more preferably, in terms of mechanical properties and biodegradability, molar ratio It is 0.52 to 0.48. If biodegradability is not required, the aliphatic dicarboxylic acid monomer and the aromatic dicarboxylic acid monomer can react with each other at different molar ratios.

The primary and secondary esterification reactions can be carried out batchwise or continuously under normal pressure.

According to an embodiment of the present invention, after obtaining the aliphatic-aromatic copolyester from the primary and secondary reactions, a condensation polymerization reaction or a chain extending reaction is carried out to increase the molecular weight. Therefore, a biodegradable resin having desired characteristics can be obtained.

In the embodiment of the present invention, preferably, the degree of vacuum is less than 2 Torr, The aliphatic-aromatic oligopolymer obtained by the primary and secondary reactions is subjected to a condensation polymerization reaction for 40 minutes to 300 minutes at a temperature ranging from 220 ° C to 250 ° C.

Condensation polymerization is used to initiate the failure of primary and secondary reactions The degree of reaction of the resulting oligomeric polymer, or the reaction between polymers that do not have the desired molecular weight. In order to do so, the condensation polymerization must be carried out together with functional groups which do not react but remain at the end of the polymer or on the chain of the polymer. Therefore, the condensation polymerization reaction is carried out in a vacuum at a high temperature. The time of the condensation polymerization reaction can be adjusted depending on the amount of the catalyst described later and the method of adding the catalyst.

Further, in the embodiment of the present invention, a chain growth reaction may be performed, A chain extender is added to join the two or more condensed polymerized aliphatic-aromatic copolyesters obtained from the primary and secondary reactions. As the chain extender, a polyvalent isocyanate monomer, an aromatic amine-based monomer or the like can be used. Preferably, 0.1 to 0.5 part by weight of a chain extender is used relative to the copolyester.

The polyvalent valence isocyanate monomer may include at least one selected from the group consisting of 2,4-toluene diisocyanate, 2,6-toluene diisocyanate, and diphenylmethane diisocyanate. (diphenylmethane diisocyanate), xylylene diisocyanate, 1,5-naphthylene diisocyanate, hexamethylene diisocyanate, triphenylmethane Triphenylmethane triisocyanate and a group of monomers which may be an aromatic amine base of diethyltoluenediamine 80 (DETDA 80) manufactured by Lonza. The DETDA 80 product is 20 to 80 parts by weight. 3,5-Diethyl-2,4-diamine toluene (3,5-diethyl-2,4-diaminotoluene) and 3,5-diethyl-2,6-diamine toluene (3,5- A mixture of diethyl-2,6-diaminotoluene).

One stage esterification reaction, secondary esterification reaction, shrinkage In the polymerization reaction and the chain extension reaction, a monomer having a divalent or higher valent functional group (branching agent) can be optionally added to the branching reaction, so that the molecular weight can be increased and can be prepared. A polymer of branched structure.

The branching agent may comprise one or more multifunctional monomers selected from the group consisting of three One or more functional polyvalent valent alcohols, polyvalent carboxylic acids having three or more functional groups or anhydrides thereof, hydrocarbyl carboxylic acids having three or more functional groups (hydroxy carboxylic acid) Acid) and a group of polyatomic amines having three or more functional groups. Preferably, 0.1 to 0.3 g of a branching agent can be used with respect to 1 mol of the aliphatic dicarboxylic acid monomer and the aromatic dicarboxylic acid monomer.

In the embodiment of the present invention, whether to use a branching agent or a branching agent The amount is a factor that significantly affects the properties of the biodegradable resin, and the characteristics of the biodegradable resin are expressed by a melt flow index, a tension/tearing strength, and the like. Therefore, in the examples of the present invention, it is determined whether or not the amount of the branching agent and the branching agent used is used in each reaction for preparing the resin to adjust the characteristics of the resin.

Further, in the embodiment of the invention, a catalyst or thermal stabilization may be used. A thermal stabilizer improves the efficiency of the above reaction by accelerating and stabilizing the reaction.

Calcium acetate, manganese acetate, magnesium acetate, zinc acetate, monobutyltin oxide, dibutyltin oxide, Monobutyl hydroxy tin oxide, octyltin, dibutyltin dichloride, tetraphenyltin, tetrabutyltin, tetrabutyl titanate Tetrabutyl titanate, tetramethyl titanate, tetraisopropyl titanate, and tetra(2-ethylhexyl)titanate are used as catalysts. Preferably, tetrabutyl titanate (Ti(OC ₄ H ₉ ) ₄ ) or an organotitanium catalyst such as Vertec® VEXP 0641 (titanium type catalyst, Johnson Matthey Corporation) can be used. Preferably, 0.1 to 1.5 grams of the catalyst can be used with respect to 1 mole of the aliphatic dicarboxylic acid monomer and the aromatic dicarboxylic acid monomer.

Further, a phosphorus-containing compound such as triphenyl phosphate or trimethyl phosphate may be added as a thermal stabilizer. When the molecular weight increases at a high temperature, the phosphorus-containing compound stably maintains the reaction by preventing thermal decomposition.

Hereinafter, the present invention will be described in detail with reference to the embodiments. However, it is to be understood that the embodiments are provided solely for the purpose of understanding the invention and are not intended to limit the invention.

Example 1

Mixing 39 moles of 1,4-butanediol, 15.6 moles of adipic acid, 9 grams of tetrabutyl titanate, 3 grams of triphenyl phosphate, and as a branching agent in a 20 liter reaction tank 9 grams of alkalic acid succinic acid (malic acid). Next, a primary esterification reaction was carried out at 175 °C. When the amount of water flowing out of the primary esterification reaction reaches a theoretically calculated value, the primary esterification reaction is stopped.

Next, 14.4 moles of terephthalic acid was added to the reaction tank, and the secondary esterification reaction was carried out for 80 minutes while the temperature of the reaction tank reached 230 °C. Thereafter, after the start of the secondary reaction, when no water generated from the condenser flows out, 6 mol of 1,4-butanediol is additionally added, and then the reaction is continued. The reaction is terminated when there is no more water flowing out and the temperature of the portion above the condenser drops to 90 degrees C or lower.

After that, the reactants obtained from the primary and secondary esterification reactions (ES) were subjected to a condensation polymerization (PC) at a temperature of 230 ° C and a vacuum of less than 1 Torr for 135 minutes. Thereby a biodegradable resin is obtained.

Example 2

Add 39 moles of 1,4-butanediol, 15.6 moles of adipic acid, and 14.4 moles of terephthalic acid to a 20 liter reaction tank, followed by mixing 9 grams of titanium in a 20 liter reaction tank. Tetrabutyl acid, 3 grams of triphenyl phosphate, and 9 grams of hydrocarbyl succinic acid as a branching agent. Next, a primary esterification reaction was carried out at 180 °C. The primary esterification reaction is stopped when the amount of water flowing from the primary esterification reaction via the condenser reaches a theoretically calculated value and no more water is produced from the condenser. then, The secondary esterification reaction was carried out for 80 minutes when the temperature of the reaction vessel reached 230 °C. Thereafter, after the start of the secondary esterification reaction, when no water generated from the condenser flows out, 6 mol of 1,4-butanediol is additionally added, and then the reaction is continued. The reaction is terminated when there is no more water flowing out and the temperature of the portion above the condenser drops to 90 degrees C or lower.

After that, the reactants obtained from the primary and secondary esterification reactions were subjected to a condensation polymerization reaction at a temperature of 243 ° C and a vacuum of less than 1 Torr for 135 minutes. Thereby a biodegradable resin is obtained.

Comparative example 1

The biodegradable resin obtained by the reaction in the same manner as in Example 1 except that 1,4-butanediol was not additionally added.

Comparative example 2

The biodegradable resin obtained by the reaction in the same manner as in Example 1 was used, except that 1,4-butanediol was additionally added, and 45 mol of 1,4-butanediol was initially added.

Experimental example 1

The following properties were evaluated using the biodegradable resins obtained in Examples 1, 2 and Comparative Examples 1, 2. The results are shown in Tables 1 and 2 below.

THF conversion rate: Gas chromatography was used to measure the THF content produced during the esterification reaction.

Weight-average molecular weight: After preparing a 0.1% chloroform solution relative to the weight of the resin, use The weight average molecular weight was measured at 35 ° C at a flow rate of 1 ml per minute using a Gel Permeation Chromatography (GPC) (Agilent, HP 1100).

As shown in Table 1 above, since the biodegradable copolyester resin of the embodiment of the present invention has a molecular weight of 140,000 to 170,000, the molecular weight is higher than that of the control group. It can be confirmed that the formation of the oligopolymer is completely carried out.

As shown in the above table, it was confirmed that the maximum amount of tetrahydrofuran was generated in the temperature rising step from 200 ° C to 230 ° C. In such a temperature rising step, the reaction rate with respect to the ester is mainly the conversion ratio of tetrahydrofuran, and in the secondary esterification reaction, although tetrahydrofuran is produced, the esterification reaction is dominant. Therefore, in order to supplement the 1,4-butanediol lost in the temperature rising step in the embodiment of the present invention, at the end of the secondary esterification reaction, 1,4-butanediol is additionally added to complete the final esterification reaction.

Embodiments of the invention have the following utility.

First, according to an embodiment of the present invention, in the preparation of the biodegradable copolyester resin, in order to supplement the 1,4-butanediol which is lost to the tetrahydrofuran in the temperature rising step of the second esterification reaction, in the secondary ester At the end of the reaction, a small amount of 1,4-butanediol is additionally added to react with the aromatic dicarboxylic acid which is not reacted with 1,4-butanediol, so that complete oligomeric polymer formation can be achieved.

Second, by effectively controlling the unreacted aromatic dicarboxylic acid, the finally obtained copolyester can have sufficient characteristics.

It will be appreciated by those skilled in the art that various changes and modifications can be made to the above-described embodiments without departing from the spirit and scope of the invention. The scope of the invention, therefore, is intended to cover the scope of the appended claims and their equivalents.

Claims (11)

A method for preparing a biodegradable copolyester resin, which comprises forming an oligomeric polymerization by monoesterification of an aliphatic dihydrocarbyl monomer, an aliphatic dicarboxylic acid monomer and an aromatic dicarboxylic acid monomer And wherein the esterification reaction comprises a primary esterification reaction and a primary and secondary esterification reaction, wherein the secondary esterification reaction is carried out at a higher temperature than the primary esterification reaction, and the secondary esterification is carried out. The aliphatic dihydrocarbyl monomer is additionally added to the reaction. The method of claim 1, wherein the primary esterification reaction is carried out by simultaneously adding the aliphatic dihydrocarbyl monomer, the aliphatic dicarboxylic acid monomer, and the aromatic dicarboxylic acid monomer. The method of claim 1, wherein the esterification reaction is carried out by adding the aliphatic dihydrocarbyl monomer, the aliphatic dicarboxylic acid monomer, and then adding the aromatic dimer. The carboxylic acid monomer is used to carry out the secondary esterification reaction. The method of claim 1, wherein the aliphatic dihydrocarbyl monomer is further added, and the total amount of the aliphatic dicarboxylic acid monomer and the aromatic dicarboxylic acid monomer is 1 mol. The aliphatic dihydrocarbyl monomer in the range of 0.05 moles to 0.5 moles is added. The method of claim 1, wherein after the secondary esterification reaction, the aliphatic dihydrocarbyl monomer is additionally added when water generated from a condenser is no longer discharged. The method of claim 1, wherein the aliphatic dihydrocarbyl group The single system is selected from the group consisting of 1,2-ethanediol, 1,3-propanediol, 1,2-butanediol, 1, 6-hexanediol, 1, 4-hexanediol, 1,4-butanediol, 1,4-cyclohexane A group consisting of 1,4-cyclohexanediol, 1,4-cyclohexane dimethylenediol, neopentyl glycol, or a combination thereof. The method of claim 1, wherein the aliphatic dicarboxylic acid monomer is a monomer represented by the following Chemical Formula 1, or an anhydride or a derivative thereof: [Chemical Formula 1] HOOC- (CH2)n-COOH (where n is 2 to 12). The method of claim 1, wherein the aromatic dicarboxylic acid monomer comprises one or more selected from the group consisting of phthalic acid, phthalic anhydride, and isophthalic acid. (isophthalic acid), terephthalic acid, 2,6-nacarboxylic acid (naphthalene-2,6-dicarboxylic acid), anhydride and its derivatives. The method of claim 1, wherein the first esterification reaction is first carried out at a temperature ranging from 160 ° C to 185 ° C, and then carried out at a temperature ranging from 225 ° C to 250 ° C. Secondary esterification reaction. The method of claim 1, further comprising a condensation polymerization at a temperature range of 220 degrees C to 250 degrees C and a vacuum of less than 2 torr. One of the aliphatic-aromatic copolyesters is obtained by the primary esterification reaction and the secondary esterification reaction for 40 to 300 minutes. The method of claim 10, further comprising adding a chain extender after the condensation polymerization reaction and allowing the chain extender to carry out the reaction.