WO2015045969A1 - エステル化合物の製造方法 - Google Patents
エステル化合物の製造方法 Download PDFInfo
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- WO2015045969A1 WO2015045969A1 PCT/JP2014/074453 JP2014074453W WO2015045969A1 WO 2015045969 A1 WO2015045969 A1 WO 2015045969A1 JP 2014074453 W JP2014074453 W JP 2014074453W WO 2015045969 A1 WO2015045969 A1 WO 2015045969A1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
- B01J31/122—Metal aryl or alkyl compounds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/62—Use of additives, e.g. for stabilisation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/34—Esters of acyclic saturated polycarboxylic acids having an esterified carboxyl group bound to an acyclic carbon atom
- C07C69/40—Succinic acid esters
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/76—Esters of carboxylic acids having a carboxyl group bound to a carbon atom of a six-membered aromatic ring
- C07C69/80—Phthalic acid esters
- C07C69/82—Terephthalic acid esters
Definitions
- the present invention relates to a method for producing an ester compound, and more specifically, an ester compound that can improve the production efficiency and energy efficiency by shortening the reaction time, and can obtain an ester compound having a good product color tone. It relates to a manufacturing method.
- esterification reaction using acid and alcohol as raw materials is widely used industrially.
- catalysts used for the production of ester compounds are generally acid catalysts such as para-toluenesulfonic acid and sulfuric acid, and organometallic catalysts such as titanium and tin.
- acid catalysts such as para-toluenesulfonic acid and sulfuric acid
- organometallic catalysts such as titanium and tin.
- this esterification reaction is an equilibrium reaction
- the alcohol as the raw material is used in excess of the stoichiometric amount, or the by-product water is discharged out of the system.
- a technique for promoting the equilibrium reaction to the product side such as a method of taking By-product water is separated by rectification column or phase separation of distillate distilled by azeotropic distillation, water and alcohol are separated, water is discharged out of the system, and alcohol reacts. The system is refluxed.
- reaction temperature of the esterification reaction is generally higher than the boiling point of water, a large amount of alcohol is refluxed together with water when carried out under normal pressure. Therefore, the amount of heat is deprived by the latent heat of vaporization, making it difficult for the temperature in the system to rise and the reaction rate to decrease. As a result, the reaction time is extended, causing problems such as a decrease in production efficiency, a further deterioration in product color tone, and a decrease in energy efficiency.
- Patent Document 1 discloses a diester compound of terephthalic acid and 2-ethylhexanol by a pressure reaction under a titanium catalyst, and the effect of shortening the reaction time is disclosed by using the titanium catalyst.
- JP 2002-155026 A Japanese Patent Application Laid-Open No. 60-4151
- Patent Document 1 and Patent Document 2 both show solutions for shortening reaction time and improving production efficiency, and neither disclosure nor suggestion is made for improving product color tone.
- an object of the present invention is to provide a method for producing an ester compound that can shorten the reaction time, improve production efficiency and energy efficiency, and obtain an ester compound having a good product color tone.
- the present inventors have used a predetermined catalyst for producing an ester compound by reacting an organic carboxylic acid or an organic carboxylic acid anhydride with an alcohol, and The inventors have found that the above-mentioned problems can be solved by setting the predetermined reaction conditions, and have completed the present invention.
- the method for producing an ester compound of the present invention is a method for producing an ester compound in which an organic carboxylic acid or an organic carboxylic acid anhydride is reacted with an alcohol.
- a zirconium compound is used as a catalyst, and a part of the entire reaction process is performed under pressure.
- the method for producing an ester compound of the present invention can be suitably applied when an alcohol having 2 to 18 carbon atoms is used.
- the reaction temperature is preferably 300 ° C. or lower.
- the reaction is preferably carried out under a pressurized condition at the initial stage of reaction, and the reaction is carried out under a reduced pressure condition at the latter stage of the reaction.
- the manufacturing method of the ester compound of this invention performs reaction under the pressurization conditions in the said reaction initial stage until the esterification rate represented by following formula (1) becomes 96% or more.
- Esterification rate 100 ⁇ A / B ⁇ 100 (1)
- A represents the residual amount of carboxylic acid or alcohol terminal
- B represents the terminal amount of carboxylic acid or alcohol charged.
- the terminal amount is the number of moles of the terminal functional group, and is an acid anhydride. In the case of, it represents the number of moles of the terminal obtained by hydrolysis, and among the carboxylic acid or alcohol terminals, the one charged with a small number of moles is used.
- reaction time can be shortened, production efficiency and energy efficiency can be improved, and the manufacturing method of an ester compound which can obtain an ester compound with favorable product color tone can be provided. .
- the method for producing an ester compound of the present invention is a method for producing an ester compound by reacting an organic carboxylic acid or organic carboxylic acid anhydride with an alcohol.
- a zirconium compound is used as a catalyst, and a part of the entire reaction process is performed under pressure. Performing part of the whole reaction process under pressure is performed under pressure until a certain stage of the reaction, and thereafter under normal or reduced pressure, or vice versa. This means that a part of the progressing process is performed under pressure.
- the initial stage of the reaction is preferably carried out under pressurized conditions, the initial stage of the reaction is preferably carried out under pressurized conditions, and more preferably after that under reduced pressure conditions.
- the esterification reaction is an equilibrium reaction, and when the reaction proceeds and water as a by-product accumulates in the system, the reaction does not proceed. Therefore, it is preferable to remove water in the system by reducing the pressure.
- the initial reaction in this case means from the start of the ester reaction until a certain amount of ester compound is produced.
- the initial stage of the reaction means that the esterification rate defined by the following formula (1) reaches 96%.
- Esterification rate 100 ⁇ A / B ⁇ 100 (1)
- A represents carboxylic acid or alcohol terminal residual amount
- B represents the charged carboxylic acid or alcohol terminal amount.
- terminal amount refers to the number of moles of the terminal functional group. In the case of an acid anhydride, it means the number of moles of the terminal obtained by hydrolysis. Among the terminal ends of carboxylic acid or alcohol, the one with less charged moles is used. .
- the organic carboxylic acid used in the present invention is not particularly limited.
- acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, enanthic acid, caprylic acid, pelargonic acid, capric acid, lauric acid, myristic acid, palmitic acid Aliphatic monocarboxylic acids such as margaric acid, stearic acid, oleic acid, linoleic acid, linolenic acid, arachidonic acid, docosahexaenoic acid, eicosapentaenoic acid; oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, azelaic acid, Aliphatic polycarboxylic acids such as sebacic acid, fumaric acid and maleic acid; hydroxy acids such as lactic acid, malic acid and citric acid; aromatic monocarboxylic acids such as benzoic acid, salicylic acid, gallic acid and
- aliphatic monocarboxylic acids aliphatic polycarboxylic acids, hydroxy acids, aromatic monocarboxylic acids, and aromatic polycarboxylic acids are preferred, aliphatic monocarboxylic acids, aliphatic polycarboxylic acids, and aromatics.
- Monocarboxylic acid and aromatic polycarboxylic acid are more preferable, acetic acid, benzoic acid, phthalic acid, isophthalic acid, terephthalic acid, trimellitic acid, pyromellitic acid, salicylic acid, cinnamic acid, biphenyldicarboxylic acid, biphenyltetracarboxylic acid, Naphthalenedicarboxylic acid, malonic acid, succinic acid, adipic acid, azelaic acid, sebacic acid, fumaric acid and maleic acid are more preferred.
- the alcohol used in the present invention is not particularly limited, and examples thereof include monoalcohol, dialcohol, trialcohol, polyalcohol, and a mixture thereof. Examples of alcohols that can be used in the present invention are shown below. Particularly, alcohols having 2 to 18 carbon atoms are preferable.
- monoalcohols examples include methanol, ethanol, propanol, butanol, amyl alcohol, hexanol, heptanol, n-octanol, 2-ethylhexanol, nonyl alcohol, decyl alcohol, undecyl alcohol, dodecyl alcohol, isododecyl alcohol, tridecyl.
- Alcohol isotridecyl alcohol, tetradecyl alcohol, pentadecyl alcohol, hexadecyl alcohol, heptadecyl alcohol, octadecyl alcohol, phenol, benzyl alcohol, cresol, ethylene glycol monomethyl ether, diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, polyethylene glycol A monomethyl ether etc. are mentioned.
- dialcohol examples include ethylene glycol, 1,2-propylene glycol, 1,3-propylene glycol, 1,3-butanediol, 1,4-butanediol, 2-methyl-1,3-propanediol, and diethylene glycol. , Dipropylene glycol, triethylene glycol, polyethylene glycol and the like.
- trialcohol examples include glycerin, 1,2,3-butanetriol, 1,2,4-butanetriol, 2-methyl-1,2,3-propanetriol, 1,2,3-pentanetriol, 1 2,4-pentanetriol, 1,3,5-pentanetriol, 2,3,4-pentanetriol, 2-methyl-2,3,4-butanetriol, trimethylolethane, 2,3,4-hexanetriol , 2-ethyl-1,2,3-butanetriol, trimethylolpropane, 4-propyl-3,4,5-heptanetriol, pentamethylglycerin (2,4-dimethyl-2,3,4-pentanetriol), etc. It is done.
- polyalcohol examples include pentaerythritol, 1,2,3,4-pentanetetrol, 1,2,4,5-pentanetetrol, 1,3,4,5-hexanetetrol, 2,3, Examples include 4,5-hexanetetrol, diglycerin, ditrimethylolpropane, sorbitan, adonitol, arabitol, xylitol, triglycerin, dipentaerythritol, sorbitol, mannitol, iditol, inositol, dulcitol, talose, allose, and the like.
- n is an integer of 0 to 100
- R 1 and R 3 each independently represents a hydrogen atom, an alkyl group having 1 to 20 carbon atoms, or an aromatic group having 6 to 20 carbon atoms.
- R 2 represents an alkylene group having 2 to 4 carbon atoms, provided that when n is 0, R 1 and R 3 are not simultaneously hydrogen atoms, and when n is 1 or more, R 2 One or both of 1 and R 3 are hydrogen atoms.
- Examples of the alkyl group having 1 to 20 carbon atoms that R 1 and R 3 can take include, for example, a methyl group, an ethyl group, a propyl group, an isopropyl group, a butyl group, an isobutyl group, a tertiary butyl group, a pentyl group, and an isopentyl group.
- Examples of the alkylene group having 2 to 4 carbon atoms that R 2 can take include an ethylene group, a propylene group, and a butylene group.
- R 1 and R 3 can take include, for example, phenyl group, toluyl group, xylyl group, cumenyl group, mesityl group, benzyl group, phenethyl group, styryl group, cinnamyl group, Benzhydryl group, trityl group, ethylphenyl group, propylphenyl group, butylphenyl group, pentylphenyl group, hexylphenyl group, heptylphenyl group, octylphenyl group, nonylphenyl group, decylphenyl group, undecylphenyl group, dodecylphenyl group Styrenated phenyl group, p-cumylphenyl group, phenylphenyl group, benzylphenyl group, ⁇ -naphthyl group, ⁇
- the zirconium compound used as the catalyst is not particularly limited, but tetrapropylzirconium, tetrabutylzirconium, oxozirconium n-propylate, oxozirconium octylate, oxozirconium stearate, tetraacetylacetonatozirconium, zirconium chloride, etc. Is mentioned.
- tetrapropylzirconium, tetrabutylzirconium, oxozirconium n-propylate, oxozirconium octylate, oxozirconium stearate, and tetraacetylacetonatozirconium are preferred.
- Zirconium, oxozirconium octylate, and tetraacetylacetonatozirconium are more preferable, and tetrapropylzirconium, tetrabutylzirconium, oxozirconium n-propylate, and oxozirconium octylate are still more preferable.
- the concentration of the zirconium catalyst used in the present invention is not particularly limited, but it is preferably added so that the zirconium concentration is 0.00001 to 1.0 mass% with respect to the ester compound obtained. 0.1% by mass is more preferable, and 0.0001 to 0.05% by mass is still more preferable. When the zirconium concentration is less than 0.00001% by mass, the esterification reaction may not proceed sufficiently. When the zirconium concentration is more than 1.0% by mass, the color tone may deteriorate and the hydrolysis resistance may decrease.
- the pressure during pressurization is not limited, but is preferably 102 to 1013 kPa, more preferably 102 to 507 kPa, and still more preferably 102 to 304 kPa.
- the pressure is less than 102 kPa, the mixture of alcohol and by-product water tends to azeotrope, and the reaction time takes a long time.
- the purpose is achieved if the pressure at a predetermined temperature is higher than the vapor pressure exhibited by the mixture of alcohol and by-product water, so the effect does not change even if the pressure exceeds 1013 kPa,
- the above range is preferable from the viewpoint of energy cost.
- a reaction vessel charged with reaction raw materials and a catalyst is sealed, and an inert gas such as nitrogen is allowed to flow in under pressure, an amount of gas flowing out of the reaction vessel,
- a method for controlling the outflow amount so that the amount of gas flowing into the reaction vessel is balanced in a pressurized state, a method for thermally expanding the gas in the reaction vessel by heating after sealing the reaction vessel Although it is possible to use a method such as a method of generating pressure under such a condition, it is not particularly limited.
- the pressure can be applied from the outside with an inert gas such as nitrogen, but if the reactor is sealed, it can be pressurized to some extent by the vapor pressure of the reaction liquid in the system. It is. The latter method is preferable from the viewpoint of cost.
- the period for carrying out the reaction under pressure is preferably the period from the start of the reaction until the esterification rate reaches 96% or more.
- the esterification rate is represented by the following general formula (1).
- Esterification rate 100 ⁇ A / B ⁇ 100 (1)
- A represents carboxylic acid or alcohol terminal residual amount
- B represents the charged carboxylic acid or alcohol terminal amount.
- terminal amount refers to the number of moles of the terminal functional group. In the case of an acid anhydride, it means the number of moles of the terminal obtained by hydrolysis. Of the carboxylic acid or alcohol terminals, the number of moles charged is small. Is used.
- the pressure during decompression is not limited, but is preferably 0.2 to 101 kPa, more preferably 20 to 90 kPa, and even more preferably 30 to 80 kPa. This makes it possible to increase the yield of the reaction. If the pressure is less than 0.2 kPa, it is not preferable because it costs a commercial energy, and if the pressure exceeds 101 kPa, many unreacted substances and impurities remain, which is not preferable.
- the period for performing the reaction under pressure is not particularly limited as long as the esterification rate is 96% or more from the start of the reaction, but it is about 0.5 to 100 hours, preferably 0.5 to 80 hours. 0.5 to 60 hours is more preferable, and 0.5 to 50 hours is still more preferable.
- the time for the reduced pressure reaction is not particularly limited, but is about 0.5 to 100 hours, preferably 0.5 to 80 hours, more preferably 0.5 to 60 hours, and 0.5 to 50 hours. Further preferred.
- the reaction temperature is not particularly limited, but the reaction temperature is preferably 300 ° C. or lower, more preferably 100 ° C. or higher and 280 ° C. or lower, from the viewpoint of further by-product formation or color deterioration. More preferably, the temperature is from °C to 260 °C.
- Types of treatment agents include silica gel, silicate gel, diatomaceous earth, high surface area aluminum oxides and aluminum oxide hydrate, clay, carbonate, activated carbon, activated clay, silica gel, silicate gel, diatomaceous earth, high surface area aluminum oxides And aluminum oxide hydrate, clay, activated carbon and activated clay are preferred, clay, activated carbon and activated clay are more preferred, and activated carbon and activated clay are more preferred.
- the amount of the treating agent is preferably 0.01 to 5.0% by mass, more preferably 0.1 to 3.0% by mass, and further 0.5 to 1.0% by mass with respect to the ester compound obtained. preferable.
- an ester whose terminal is sealed with an organic carboxylic acid by reacting with a monocarboxylic acid after the reaction is completed. It can also be a compound. Since the ester compound produced with an excess of polyvalent carboxylic acid has a carboxylic acid at the end, after completion of the reaction, react with the monohydroxy compound to make the ester compound sealed at the end with the monohydroxy compound. You can also.
- the production method of the present invention can also be applied to both the production of an ester compound as an intermediate and the production of an ester compound as a final target product. Depending on the case, the zirconium catalyst can be used as it is.
- the color tone is based on the Standard Oil Analysis Test Method II. C. 1.5. This was performed based on the APHA method (American Public Health Association).
- Example 1 First, succinic acid (221 g, 1.9 mol), terephthalic acid (317 g, 1.9 mol), then ethylene glycol (207 g, 3.3 mol), propylene glycol (254 g, 3.3 mol), rectification tower, condensation The reaction was started at the time when the oxyzirconium octylate (0.0025% by mass with respect to the total amount) was charged into a 3 L pressurized reactor equipped with a vessel and decanter, and after substituting with reduced pressure nitrogen. Started. The pressure reached about 111 kPa 60 minutes after the start of the reaction.
- the temperature was reduced to 1.0 kPa or less over 1.5 hours at a temperature of 180 ° C., and the reaction was terminated when the hydroxyl value reached 209 mgKOH / g. APHA of the obtained ester was 50.
- Example 2 Except that the amount of the catalyst was changed to 0.00125% by mass, the charging and the reaction were carried out in the same manner as in Example 1. As a result, the APHA of the obtained ester was 25.
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Abstract
Description
触媒としてジルコニウム化合物を用い、全反応過程のうち、一部を加圧条件下で行うことを特徴とするものである。
エステル化率=100-A/B×100・・・・(1)
(式(1)中、Aは、カルボン酸またはアルコール末端残存量を表し、Bは、仕込んだカルボン酸またはアルコール末端量を表す。末端量とは末端官能基のモル数であり、酸無水物の場合は加水分解して得られる末端のモル数を表わし、カルボン酸またはアルコール末端のうち、仕込んだモル数の少ないものを用いるものとする。)
エステル化率=100-A/B×100・・・・(1)
ここで、式(1)中、Aは、カルボン酸またはアルコール末端残存量を表し、Bは、仕込んだカルボン酸またはアルコール末端量を表す。末端量とは末端官能基のモル数であり、酸無水物の場合は加水分解して得られる末端のモル数を意味し、カルボン酸またはアルコール末端のうち、仕込んだモル数の少ないものを用いる。
(式(2)中、nは0~100の整数であり、R1およびR3は各々独立に水素原子、炭素原子数1~20のアルキル基、炭素原子数6~20の芳香族基を表わし、R2は炭素原子数2~4のアルキレン基を表す。ただし、nが0の時は、R1およびR3が同時に水素原子になることはなく、nが1以上の時は、R1およびR3のいずれか一方、もしくは両方が水素原子である。)
エステル化率=100-A/B×100・・・・(1)
ここで、式(1)中、Aは、カルボン酸またはアルコール末端残存量を表し、Bは、仕込んだカルボン酸またはアルコール末端量を表す。また、末端量とは末端官能基のモル数であり、酸無水物の場合は加水分解して得られる末端のモル数を意味し、カルボン酸またはアルコール末端のうち、仕込んだモル数の少ないものを用いる。
色調は、日本油化学会の基準油脂分析試験法II.C.1.5.APHA法(American Public Healthy Association)に基づいて行なった。
まずコハク酸(221g、1.9mol)、テレフタル酸(317g、1.9mol)を、次にエチレングリコール(207g、3.3mol)、プロピレングリコール(254g、3.3mol)を、精留塔、凝縮器、デカンターを備えた容量3Lの加圧反応槽に仕込み、減圧窒素置換後にオクチル酸オキソジルコニウム(全量に対して0.0025質量%)を仕込んだ時点を反応開始点とし、加圧昇温を開始した。反応開始後60分で圧力は約111kPaに到達した。引き続き、反応温度が230℃に到達した後、圧力と温度を保持したまま、グリコールの還流を続けた(副生する水とグリコールは精留塔により分離し、デカンターにより水は系外に留去、グリコールは還流ラインから系内に戻した)。反応開始から230分で副生する水の留出率が100%に到達した。その時点で加圧反応を終了し、このときの酸価は8.0mgKOH/gであった。その後、徐々に減圧し酸価が0.2mgKOH/g以下となった時点で、減圧反応を終了した。その後、過剰のアルコールを留去する為に、温度を180℃にして1.5時間かけて1.0kPa以下まで減圧し、水酸基価が209mgKOH/gとなった時点で反応を終了した。得られたエステルのAPHAは50であった。
触媒量を0.00125質量%に変えて行なった以外は、実施例1と同様に仕込みおよび反応を行なった結果、得られたエステルのAPHAは25であった。
触媒をテトライソプロピルチタネート(全量に対して0.0025質量%)に変えて行なった以外は、実施例1と同様に仕込みおよび反応を行なった結果、得られたエステルのAPHAは100であった。
触媒をジブチルスズオキサイド(全量に対して0.0025質量%)に変えて行なった以外は、実施例1と同様に仕込みおよび反応を行なった結果、得られたエステルのAPHAは90であった。
Claims (5)
- 有機カルボン酸または有機カルボン酸無水物とアルコールとを反応させるエステル化合物の製造方法において、
触媒としてジルコニウム化合物を用い、全反応過程のうち、一部を加圧条件下で行うことを特徴とするエステル化合物の製造方法。 - アルコールが炭素原子数2~18である請求項1記載のエステル化合物の製造方法。
- 反応温度が、300℃以下である請求項1記載のエステル化合物の製造方法。
- 反応初期は加圧条件下で反応を行い、反応後期は減圧条件下で反応を行う請求項1記載のエステル化合物の製造方法。
- 前記反応初期における加圧条件下での反応を、下記の式(1)で表されるエステル化率が96%以上になるまで行う請求項4記載のエステル化合物の製造方法。
エステル化率=100-A/B×100・・・・(1)
(式(1)中、Aは、カルボン酸またはアルコール末端残存量を表し、Bは、仕込んだカルボン酸またはアルコール末端量を表し、末端量とは末端官能基のモル数であり、酸無水物の場合は加水分解して得られる末端のモル数を表し、カルボン酸またはアルコール末端のうち、仕込んだモル数の少ないものを用いるものとする。)
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CN201480053138.6A CN105579430A (zh) | 2013-09-25 | 2014-09-16 | 酯化合物的制造方法 |
JP2015539132A JPWO2015045969A1 (ja) | 2013-09-25 | 2014-09-16 | エステル化合物の製造方法 |
KR1020167006995A KR20160060641A (ko) | 2013-09-25 | 2014-09-16 | 에스테르 화합물의 제조 방법 |
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EP4219440A4 (en) * | 2020-09-24 | 2024-04-10 | Lg Chem, Ltd. | DISCONTINUOUS PREPARATION PROCESS FOR ESTER-BASED MATERIAL |
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US20230303475A1 (en) * | 2020-09-24 | 2023-09-28 | Lg Chem, Ltd. | Batch preparation method of ester-based material |
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US4767881A (en) * | 1987-07-13 | 1988-08-30 | Hoechst Celanese Corporation | Synthesis of diphenyl phthlates |
JP2002155026A (ja) * | 1998-02-16 | 2002-05-28 | Mitsubishi Chemicals Corp | エステルの製造方法 |
JP2005533645A (ja) * | 2002-07-26 | 2005-11-10 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | チタン−ジルコニウム触媒組成物およびその使用 |
JP2011516466A (ja) * | 2008-04-01 | 2011-05-26 | エスケー ケミカルズ カンパニー リミテッド | 脂肪酸を用いた脂肪酸アルキルエステルの製造方法 |
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JPH0232295B2 (ja) * | 1981-09-29 | 1990-07-19 | Toyo Boseki | Naiburyushiganjuhoriesuterunoseizoho |
JPS58101021A (ja) * | 1981-12-12 | 1983-06-16 | Toyobo Co Ltd | 2軸延伸ポリエステルフイルム |
JPH0871429A (ja) * | 1994-09-06 | 1996-03-19 | Matsumoto Yushi Seiyaku Co Ltd | エステル化触媒およびエステルの製法 |
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2014
- 2014-09-16 KR KR1020167006995A patent/KR20160060641A/ko not_active Application Discontinuation
- 2014-09-16 WO PCT/JP2014/074453 patent/WO2015045969A1/ja active Application Filing
- 2014-09-16 CN CN201480053138.6A patent/CN105579430A/zh active Pending
- 2014-09-16 JP JP2015539132A patent/JPWO2015045969A1/ja active Pending
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US4767881A (en) * | 1987-07-13 | 1988-08-30 | Hoechst Celanese Corporation | Synthesis of diphenyl phthlates |
JP2002155026A (ja) * | 1998-02-16 | 2002-05-28 | Mitsubishi Chemicals Corp | エステルの製造方法 |
JP2005533645A (ja) * | 2002-07-26 | 2005-11-10 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | チタン−ジルコニウム触媒組成物およびその使用 |
JP2011516466A (ja) * | 2008-04-01 | 2011-05-26 | エスケー ケミカルズ カンパニー リミテッド | 脂肪酸を用いた脂肪酸アルキルエステルの製造方法 |
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FRANC,OIS LEVERD: "Study of model esterifications and of polyesterifications catalyzed by various organometallic derivatives-II. Study of esterifications and polyesterifications catalyzed by zirconium derivatives", EUROPEAN POLYMER JOURNAL, vol. 23, no. 9, 1987, pages 699 - 704 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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EP4219440A4 (en) * | 2020-09-24 | 2024-04-10 | Lg Chem, Ltd. | DISCONTINUOUS PREPARATION PROCESS FOR ESTER-BASED MATERIAL |
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CN105579430A (zh) | 2016-05-11 |
KR20160060641A (ko) | 2016-05-30 |
JPWO2015045969A1 (ja) | 2017-03-09 |
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