WO2005033052A1 - 3,3’,5,5’−テトラアルキル−4,4’−ビフェノールの製造方法 - Google Patents
3,3’,5,5’−テトラアルキル−4,4’−ビフェノールの製造方法 Download PDFInfo
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- WO2005033052A1 WO2005033052A1 PCT/JP2004/013609 JP2004013609W WO2005033052A1 WO 2005033052 A1 WO2005033052 A1 WO 2005033052A1 JP 2004013609 W JP2004013609 W JP 2004013609W WO 2005033052 A1 WO2005033052 A1 WO 2005033052A1
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- dialkylphenol
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/11—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by reactions increasing the number of carbon atoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C39/00—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C39/00—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring
- C07C39/12—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring polycyclic with no unsaturation outside the aromatic rings
- C07C39/15—Compounds having at least one hydroxy or O-metal group bound to a carbon atom of a six-membered aromatic ring polycyclic with no unsaturation outside the aromatic rings with all hydroxy groups on non-condensed rings, e.g. phenylphenol
Definitions
- the present invention relates to a method for producing a 3,3 ′, 5,5 ′′ -tetraalkyl 4,4′-biphenol, and more particularly, to a method for industrially producing a 2,6-dialkylphenol by oxidizing it.
- the present invention relates to a method for producing an advantageous 3,3 ', 5,5'-tetraalkyl 4,4'-biphenol, which is hereinafter referred to as "tetraalkylbiphenol”. May be abbreviated.
- Tetraalkyl biphenols are compounds useful as raw materials for epoxy resins, polyester resins, polycarbonate resins, etc., and as stabilizers and plasticizers for petroleum products.
- tetraalkylbiphenol which has an alkyl group power of S-methyl group, is useful in the field of electric and electronic devices as a raw material for epoxy resins.
- dialkylphenol As a method for synthesizing a tetraalkylbiphenol, a 2,6-dialkylphenol (hereinafter may be abbreviated as "dialkylphenol”) is oxidized and dimerized in an aqueous solvent in the presence of a metal catalyst and an oxidizing agent.
- dialkylphenol a 2,6-dialkylphenol
- a tetraalkylbiphenol can be obtained in a relatively high yield (for example, see Patent Documents 1 and 2).
- this method comprises the steps of (1) performing an oxidative reaction of a 2,6-dialkylphenol with oxygen or an oxygen-containing gas in the presence of an aqueous solvent and a metal catalyst; Solid-liquid separation of the tetraalkylbiphenol from the obtained reaction mixture (aqueous slurry).
- the reaction solution containing the unreacted raw material dialkylphenol which is produced by the reaction is treated as follows.
- the processing method is not particularly known until now!
- the reaction solution can be heated and azeotropically distilled water and dialkylphenol can be recovered by distillation (see, for example, Patent Documents 3 and 4).
- a mixture of water and dialkylphenol recovered by distillation is reused. It is well known that you can use it! /.
- the present inventors distilled and recovered the above azeotropic mixture of water and dialkylphenol, and tried to reuse it as a part of the raw material as it was. In the quantification reaction, the problem was that the reaction time to the specified conversion gradually increased.
- Patent Document 1 JP-A-53-65834
- Patent Document 2 JP-A-60-152433
- Patent Document 3 JP-A-61-268641
- Patent Document 4 Japanese Patent No. 2861221
- the present invention has been made in view of the above circumstances, and a problem to be solved is that even if unreacted dialkyl phenol is recovered and reused repeatedly, the reaction in the oxidative reaction can be prevented.
- An object of the present invention is to provide an industrially advantageous production method capable of suppressing a decrease in the conversion rate and an increase in the reaction time, and reducing the amount of the reaction solution discarded.
- the first gist of the present invention is to provide a 3,3 ′, 5,5′-tetraalkyl 4,3′-dialkylphenol by an oxidative dimerization reaction of a 2,6-dialkylphenol in the presence of an aqueous solvent and a metal catalyst.
- an aromatic aldehyde represented by the following general formula (I) which is recovered as an unreacted raw material as an 2,6-dialkylphenol and is an unreacted raw material, and as an impurity
- the use of 2,6-dialkylphenols to control the amount of aromatic aldehydes in the reaction mixture to the metal catalyst to 60 moles or less.
- the present invention relates to a method for producing 3,3,5,5-tetraalkyl 4,4,1-biphenol.
- R 1 represents — (CO) R 3 (where R 3 represents H or an alkyl group of C 1 to C 4), and R 2 represents H or a C 1 to C 4 Represents an alkyl group.)
- the second gist of the present invention is to carry out an oxidative dimerization reaction of a 2,6-dialkylphenol in the presence of an aqueous solvent and a metal catalyst, and to convert unreacted 2,6-dialkylphenol and the metal catalyst.
- a mixture containing a 2,6-dialkylphenol and the aromatic aldehyde represented by the above general formula (I) as impurities is distilled off and recovered, and a part of the recovered fraction is acidified with acid.
- a method for producing 3, 3 ', 5, 5'-tetraalkyl 4, 4'-biphenol to be supplied to an arsenic reaction The method for producing 3,3 ', 5,5'-tetraalkyl 4,4'-biphenol is characterized in that the amount of the aromatic aldehyde relative to the metal catalyst in the reaction solution is adjusted to 60 moles or less. You.
- a third gist of the present invention is to carry out an oxidative dimerization reaction of 2,6-dialkylphenol in the presence of an aqueous solvent and a metal catalyst, and to convert unreacted 2,6-dialkylphenol and the metal catalyst.
- a mixture containing the aromatic aldehyde represented by (I) is distilled off and recovered, and a part of the recovered fraction is supplied to an Oi-dani-dani-reaction, 3, 3 ', 5, 5 '—Tetraalkyl 4, 4'
- a process for producing biphenol characterized in that the amount of aromatic aldehyde relative to a metal catalyst in a charged reaction solution is adjusted to not more than 60 times the molar amount of a 3,3 ′, 5,5′-tetraalkyl-1 4 , 4,1-biphenol.
- a fourth gist of the present invention is to carry out an oxidative dimerization reaction of a 2,6-dialkylphenol in the presence of an aqueous solvent and a metal catalyst, and to convert unreacted 2,6-dialkylphenol and the metal catalyst.
- a mixture containing a 2,6-dialkylphenol and the aromatic aldehyde represented by the general formula (I) as an impurity is distilled off and recovered, and the aqueous reaction recovered in the step (B) is recovered.
- FIG. 1 is an example of a flow chart showing the production method of the present invention, in which (1), (2), and (3) represent the first, second, and third examples of the present invention, respectively.
- FIG. 4 is an example of a flowchart showing a manufacturing method according to the gist. BEST MODE FOR CARRYING OUT THE INVENTION
- an oxidation dimerization reaction of a 2,6-dialkylphenol is carried out in the presence of an aqueous solvent and a metal catalyst.
- Reaction step (A) to obtain an aqueous slurry in which tetraalkylbiphenol is dispersed in an aqueous reaction solution containing unreacted 2,6-dialkylphenol and a metal catalyst, and the resulting aqueous slurry power is tetraalkylbiphenol.
- step (B) of solid-liquid separation is carried out in the presence of an aqueous solvent and a metal catalyst.
- Step (A) is an oxidation dimerization reaction step of a 2,6-dialkylphenol.
- the 2,6-dialkylphenol is an alkylphenol in which the 2,6-position of phenol is substituted with an alkyl group having 14 to 14 carbon atoms.
- the alkyl group having 14 to 14 carbon atoms include methyl, ethyl, n-propyl, 1-propyl, n-butyl, 1-butyl, s-butyl and t-butyl.
- 2,6-dimethylphenol (2,6-xylenol) an alkyl S-methyl group.
- Water is used as a reaction solvent, and an alkaline substance is preferably added to carry out the reaction under alkaline conditions.
- the alkaline substance include sodium hydroxide, alkali metal hydroxides such as potassium hydroxide, alkali metal carbonates such as sodium carbonate, hydrogen carbonate, sodium borate, boron compounds such as borax, Examples thereof include alkali metal phosphates such as sodium phosphate, sodium hydrogen phosphate, rhodium phosphate, potassium hydrogen phosphate, and the like, and amine bases such as triethylamine and pyridine. Boron compounds, especially borax, are preferred.
- the alkaline substance is usually used in such an amount that the pH of the reaction system is kept in the range of 8-11.
- the amount of the alkaline aqueous solvent used is usually 100-1000 ml, preferably 100-500 ml per 2,6-dialkylphenol.
- a surfactant to the reaction solvent.
- fatty acid salts include alkyl sulfonates, alkyl benzene sulfonic acids, and alkyl sulfates.
- sodium lauryl sulfate is preferred from the viewpoint of reaction rate and foamability.
- the amount of the surfactant to be used is usually 0.1 to 50 mmol per 1 mol of 2,6-dialkylphenol.
- the metal catalyst various transition metal compounds can be used, and among them, a copper compound is preferably used. Copper compounds can be monovalent or divalent, and include copper halides, water Examples thereof include copper oxide, copper sulfate, copper nitrate, copper carboxylate, and copper alkyl sulfate.
- the amount of the metal catalyst used is usually 0.005 to 0.04 mmol, preferably 0.01 to 0.04 mmol, per 1 mol of 2,6-dialkylphenol.
- an oxygen-containing gas such as oxygen gas or air is used.
- the reaction temperature of the oxidative dimerization reaction is usually 50 to 100 ° C, and the reaction pressure is usually in the range of atmospheric pressure to 130 atm, depending on the oxygen concentration in the gas phase. Usually 5-15 hours. Terminate the reaction by stopping the supply of oxygen gas or oxygen-containing gas
- the obtained reaction solution is an alkaline aqueous solution containing an unreacted 2,6-dialkylphenol, a surfactant, a metal catalyst, and an aromatic aldehyde represented by the above formula (I) which is by-produced as an impurity.
- An aqueous slurry in which the tetraalkylbiphenol is dispersed in the reaction solution is added.
- aromatic aldehydes are formed by oxidizing the alkyl chain of the alkyl phenols during the oxidation reaction.
- Aromatic aldehydes have similar properties, such as boiling point and solubility, when distilling and recovering unreacted 2,6-dialkylphenol, which will be described later. It is mixed in and accumulates when collection is repeated. If aromatic aldehydes are present in a large amount in the recovered fraction, the oxidative dimerization of 2,6-dialkylphenol is inhibited when unreacted 2,6-dialkylphenol is recovered and reused.
- aromatic aldehydes are particularly liable to be formed and concentrated, and have a large effect of inhibiting an oxidative dimerization reaction. For example, when 2,6-xylenol is used as a raw material, 3-methylsalicylaldehyde accumulates in the recovered fraction and greatly inhibits the acid dimerization reaction.
- the residual ratio of unreacted 2,6-dialkylphenol in the aqueous slurry after the oxidative dimerization reaction varies depending on the type of the alkyl group. Generally, the residual ratio is in the range of 5 to 50% by weight, and in particular, the residual ratio is 10 to 10%. The case of 20% by weight is preferred from the viewpoint of the yield and selectivity of the tetraalkylbiphenol.
- the residual rate of unreacted 2,6-dialkylphenol can be controlled by the amount of oxidizing agent (oxygen) supplied.
- the aqueous slurry obtained in the step (A) may be supplied as it is to the next solid-liquid separation step (B). However, by performing the post-treatment described below before the solid-liquid separation, the efficiency is improved. It is preferable because tetraalkyl biphenol of high purity can be obtained well.
- the supply of the oxygen-containing gas to the aqueous slurry is stopped, and the oxygen in the reactor is preferably replaced with an inert gas such as nitrogen to remove the acid.
- the pH of the aqueous slurry is adjusted so that the pH during the subsequent heat treatment is 7 or less, preferably in the range of 6-7. This pH adjustment prevents an increase in heavy impurities such as polyphenylene ether by-produced during the heat treatment.
- the acid used for pH adjustment is not particularly limited, but generally a mineral acid is used, and sulfuric acid or hydrochloric acid is preferred.
- the heat treatment is usually performed at a temperature of 60-120 ° C under normal pressure, and the treatment time is usually within 10 hours.
- an acid is further added to the heat-treated aqueous slurry to adjust the pH of the reaction solution to preferably 2.5 to 5 (especially, when the 2,6-dialkylphenol as the raw material is 2,6-xylenol, preferably 3 to 5). — 4.5).
- the acid used for pH adjustment is not particularly limited, but generally a mineral acid is used, and sulfuric acid or hydrochloric acid is preferred. Adjusting the pH after the heat treatment is effective in preventing the entry of inorganic impurities such as metal catalysts into the product tetraalkylbiphenol.
- Alcohol is added to the pH-adjusted aqueous slurry, followed by mixing and stirring.
- the amount of alcohol added is preferably such that the weight ratio of water Z alcohol is 5Z5-8Z2.
- the weight ratio of water Z alcohol is 5Z5-8Z2.
- water Z It is preferable to add alcohol so that the weight ratio becomes 6Z4-7Z3! / ,.
- a lower alcohol having 14 to 14 carbon atoms such as methanol, ethanol, n-propyl alcohol, isopropyl alcohol, and n- butanol can be suitably used.
- the solubility of the tetraalkylbiphenol can be reduced, the recovery rate can be kept high, and the solubility of the impurities to be removed can be kept sufficiently high.
- the mixing and stirring after the addition of the alcohol is carried out at a temperature of usually 40 to 100 ° C, preferably 50 to 90 ° C, usually for 0.1 to 5 hours, preferably for 0.5 to 3 hours.
- the concentration of the tetraalkylbiphenol in the mixture containing the alcohol is usually 5 to 50% by weight.
- step (B) the solid-liquid separation step (B) is abbreviated as step (B).
- the product, tetraalkylbifunol is separated by solid-liquid separation of the aqueous or alcohol-containing aqueous slurry obtained through the step (A) or the mashing step such as heat treatment.
- the solid-liquid separation method is not particularly limited, and ordinary methods such as filtration and centrifugation can be used.
- the temperature of the slurry at the time of solid-liquid separation is usually 35 to 70 ° C, preferably 40 to 65 ° C. When the temperature is too high, the organic impurities are easily removed, but the product yield tends to decrease, and when the temperature is too low, the content of the organic impurities in the tetraalkylbiphenol tends to increase.
- the solid phase containing the tetraalkylbiphenol obtained by the solid-liquid separation usually contains a liquid content of 10 to 30%.
- This liquid component contains unreacted 2,6-dialkylphenol, reaction by-products such as heavy impurities, and surfactants.
- it when purified by washing with alcohol before performing step (B), it contains the alcohol subjected to washing. Therefore, it is usually preferable to further purify the product to obtain a high-purity product.
- As an additional purification method for obtaining a high-purity product rinsing and washing the solid phase after solid-liquid separation with warm water is industrially simple and preferable.
- the temperature of the hot water is usually 35-90 ° C, preferably 40-65 ° C.
- the amount of hot water is usually 0.5 to 3 times (weight ratio) the solid phase, depending on the temperature and the method of washing.
- the solid phase after solid-liquid separation may be mixed and washed with warm water or an organic solvent, and solid-liquid separation may be performed again to separate the solid phase and the liquid phase.
- the aqueous reaction solution recovered in the solid-liquid separation includes water, unreacted 2,6-dialkylphenol, a surfactant, a metal catalyst, and an aromatic compound represented by the above formula (I) as an impurity. It is an alkaline aqueous reaction solution containing aldehydes, and if it has undergone an additional step such as heat treatment and purification by alcohol prior to step (B), it is an acidic aqueous reaction solution containing alcohol.
- the 2,6-dialkylphenol recovered as an unreacted raw material is an aromatic aldehyde represented by the general formula (I) as an impurity as described above.
- 2,6-dialkylphenol is 2,6-xylenol
- 3-methylsalicylaldehyde is accompanied by 2,6-dialkylphenol.
- the presence of aromatic aldehydes represented by salicylaldehydes such as 3-methyl salicylaldehyde causes an oxidation dimerization reaction. Affected, reaction time increases.
- the amount of the aromatic aldehyde which is acceptable is defined by the amount based on the metal catalyst.
- the amount of the aromatic aldehyde relative to the metal catalyst is adjusted to 60 times or less.
- the amount of the aromatic aldehyde to the metal catalyst in the charged reaction solution means the ratio in the solution before the start of the reaction (the same applies to the following).
- the amount of the aromatic aldehydes in the charged reaction solution relative to the metal catalyst is adjusted by analyzing the concentration of the aromatic aldehydes in the reaction solution as follows: (1) A method of changing the amount of the metal catalyst to be present in the reaction solution while keeping the amount of the 2,6-dialkylphenol recovered as a raw material and containing an aromatic aldehyde substantially constant, or The method can be carried out by making the amount of the metal catalyst substantially constant and changing the amount of the 2,6-dialkylphenol as described above. Such a method is mainly used when the oxidative dimerization reaction is performed in a batch mode.
- the quantitative analysis of aromatic aldehydes can be performed by gas chromatography or the like.
- the aqueous slurry after the oxidation reaction is distilled to mainly react with water and unreacted 2,6-dialkylphenol alcohol as an aromatic aldehyde as impurities.
- Distillation of a mixture containing phenols and a part of the recovered fraction is fed to the oxidative dimerization reaction, which is reused as a part of the reaction raw material 2,6-dialkylphenol.
- the amount of the aromatic aldehyde relative to the metal catalyst in the charged reaction solution is adjusted to 60 times or less.
- the charged reaction liquid refers to a reaction liquid after a part of the recovered fraction is supplied to the oxidation dimerization reaction (the same applies to the following!).
- the recovered fraction contains aromatic aldehydes !, but (for example, when 2,6-dialkylphenol is 2,6-xylenol, 3-methylsalicyl is added to the recovered fraction.
- aromatic aldehydes in the oxidation dimerization reaction solution is suppressed (all of the recovered fraction is constantly subjected to acid hydration reaction).
- the conversion rate in the oxidative dimerization reaction is reduced and the reaction time is not prolonged, and the unreacted raw material 2,6-dialkylphenol to be disposed of is treated. Can be reduced, which is an industrially advantageous production method.
- the pH of the aqueous slurry is usually adjusted to 7 or less, preferably 6 to 7, and then the pH of the aqueous slurry is adjusted before adding the alcohol.
- the aqueous slurry is distilled at the same time as the heating operation in the heat treatment step, and the unreacted xylenol is recovered by distillation.
- the temperature and pressure for distillation of the aqueous slurry may be determined by selecting conditions under which water and 2,6-dialkylphenol are azeotropically distilled, and the distillation may be performed under increased or reduced pressure as needed.
- the 2,6-dialkylphenol is 2,6-xylenol
- it may be distilled at normal pressure at about 100 ° C.
- simple distillation may be used.However, the reflux ratio is increased by the rectification method to concentrate and separate aromatic aldehydes. You can do it. If the concentration of the aqueous slurry becomes too high at the time of distillation to make operation such as stirring difficult, the distillation may be carried out while adding water or steam to the system.
- the ratio of the recovered fraction supplied to the acid-in-hydene reaction is greatly fluctuated each time, but the average in a plurality of reaction cycles. It can be expressed as an average. It is preferable to adopt the most efficient number and supply amount in consideration of the reaction time in each time, the concentration of the aromatic aldehydes, and the waste amount of the recovered fraction not reused in the reaction.
- the ratio of the recovered fraction to be supplied to the oxidation-dimerization reaction can be substantially stably performed each time. In this case as well, it is preferable to adopt the most efficient supply ratio while considering the reaction time, the concentration of the aromatic aldehydes, and the amount of the recovered fraction not reused in the reaction.
- the ratio of the recovered fraction supplied to the oxidative dimerization reaction depends on the distillation recovery conditions, but unreacted 2,6-dialkylphenol in the recovered fraction is used. To 99% by weight, preferably 50 to 99% by weight, more preferably 90 to 99% by weight. Ratio). If the proportion of the recovered fraction supplied to the oxidative dimerization reaction is too large, the amount of unreacted raw material 2,6-dialkylphenol to be discarded further decreases, but aromatic aldehydes accumulate in the oxidative dimerization reaction However, the conversion in the oxidative dimerization reaction decreases, and the reaction time increases.
- the concentration of impurities in the 2,6-dialkylphenol in the recovered fraction is likely to be high.
- the proportion must be relatively low, usually less than 95% by weight, preferably 50-90% by weight.
- the recovered fraction excluding the fraction in which the aromatic aldehydes as impurities are concentrated can be supplied to the oxidizing reaction.
- the weight of the recovered fraction (remaining portion) not supplied to the dani reaction is compared with that of the remaining portion obtained by simple distillation. However, it can be reduced to a small amount (usually 1Z5— ⁇ ), that is, it is possible to increase the ratio of the recovered fraction supplied to the oxidative dimerization reaction.
- a part of the unreacted starting material, 2,6-dialkylphenol may be further supplied from the remaining part to the acid hydrin reaction.
- the concentration of the aromatic aldehyde in the recovered unreacted raw material 2,6-dialkylphenol is preferably less than 5% by weight, more preferably less than 2% by weight.
- the recovered unreacted raw material 2,6-dialkylphenol is supplied to the oxidative dimerization reaction together with the new raw material 2,6-dialkylphenol.
- the amount of the aromatic aldehyde relative to the metal catalyst in the charging reaction solution is adjusted to 60 times or less.
- the adjustment of the aromatic aldehydes in the charged reaction solution is carried out by using the above-mentioned various methods of supplying a part of the recovered fraction to the oxidation reaction. Also, the above-mentioned method of adjusting the amount of the metal catalyst added to the reaction solution may be used.
- the aqueous reaction solution recovered in the step (B) is distilled, and is mainly converted to water and unreacted 2,6-dialkylphenol and as impurities.
- a mixture containing aromatic aldehydes is distilled off, a part of the recovered fraction is supplied to an oxidation dimerization reaction, and reused as a part of the reaction raw material 2,6-dialkylphenol. Do. Then, the amount of the aromatic aldehyde relative to the metal catalyst in the charged reaction solution is adjusted to 60 times or less. By this operation, the same effect as the effect described in the second aspect can be obtained, and the production method is industrially advantageous.
- the aqueous reaction solution contains a lower alcohol and the like.
- a recovery operation of 2,6-dialkylphenol is performed.
- the aqueous reaction solution is acidic, it is necessary to neutralize the aqueous reaction solution using an alkali such as sodium hydroxide before heating by distillation in order to prevent corrosion of the apparatus. preferable.
- the temperature and pressure for distillation of the aqueous reaction solution may be determined by selecting conditions under which water and 2,6-dialkylphenol are azeotropically distilled, and the distillation may be performed under increased or reduced pressure as necessary.
- the distillation method may be simple distillation, but the aqueous reaction solution contains a lower alcohol or the like. In this case, the rectification method is particularly preferred. By employing a rectification method, not only can alcohol be recovered and reused, but also aromatic aldehydes can be concentrated and separated by increasing the reflux ratio. In the case of distillation, when the concentration of the aqueous slurry becomes too high and it becomes difficult to perform operations such as stirring, distillation may be performed while adding water or steam to the system.
- the aqueous slurry is recovered by the distillation and recovery operation (pre-distillation step) from the aqueous slurry described in the second gist and the process (B) described in the third gist.
- the aqueous reaction solution is subjected to a distillation recovery operation (second-stage distillation step).
- the distillation recovery method in each recovery operation can be performed in the same manner as described in the second and third aspects. By this operation, the same effect as that described in the second aspect can be obtained, and an industrially advantageous manufacturing method can be obtained.
- the operations in the first-stage distillation step and the second-stage distillation step can be performed by simple distillation or precision distillation as described in the gist of the second and third inventions, but precision distillation is more preferable. This is preferable because an unreacted raw material having less impurities can be recovered.
- the former distillation step can be carried out by simple simple distillation without any inconvenience.
- simple distillation is also possible, but when the aqueous slurry contains a lower alcohol, precision distillation is preferred in order to separate the lower alcohol and to concentrate and separate aromatic aldehydes.
- the rate at which the recovered fraction obtained in the first-stage distillation step and the second-stage distillation step is supplied to the oxidative dimerization reaction depends on the method of distillation and recovery. Unreacted 2,6-dialkylphenol in the total recovered fraction To 99% by weight or less, preferably 50-99% by weight, more preferably 90-99% by weight. In particular, when the aromatic aldehydes are concentrated and recovered during the precision distillation in the second-stage distillation step, the recovered fraction excluding the concentrated fraction is supplied to the oxidizing reaction to reduce the supply ratio. Can be higher.
- the manufacturing method according to the fourth aspect of the present invention can be said to be an industrially very efficient manufacturing method.
- the aqueous slurry is purified by heating, and the unreacted 2,6-dialkylphenol is recovered by distillation using the heat treatment, so that some amount of the aqueous slurry is collected before the step (B).
- the unreacted 2,6-dialkylphenol is recovered by distillation, and the remaining unreacted 2,6-dialkylphenol is recovered by distillation from the aqueous reaction solution recovered in step (B).
- the load on distillation is reduced, the distillation recovery time is reduced, and a moderate amount of water is used for distillation of aqueous slurry. It has advantages such as maintaining the slurry concentration. Further, the amount of the aqueous slurry supplied to the step (B) is reduced, the load on the solid-liquid separation step is reduced, and the production time can be shortened.
- the pH of the aqueous slurry is adjusted to 7 or less, and the heat treatment is performed, and at the same time, the pre-distillation step is performed.
- the pH of the aqueous slurry is adjusted to 7 or less, and the heat treatment is performed, and at the same time, the pre-distillation step is performed.
- the 2,6-dialkylphenol After recovering the 2,6-dialkylphenol, mixing the lower alcohol with an acidic pH, performing the solid-liquid separation step (B), and further adjusting the pH of the resulting aqueous reaction solution to 7
- the 2,6-dialkylphenol is recovered in the second-stage distillation step, and a part of the 2,6-dialkylphenol recovered in the first- and second-stage distillation steps is returned to the oxidative dimerization reaction.
- the method used can be mentioned.
- the ratio of the amount of unreacted 2,6-dialkylphenol recovered in the first distillation step to the amount of unreacted 2,6-dialkylphenol recovered in the second distillation step is determined so that the production efficiency is optimal. Should be selected.
- the total amount of unreacted 2,6-dialkylphenol to be recovered by distillation is 100 parts by weight, unreacted 2,6-dialkylphenol recovered in the previous distillation step is obtained.
- the amount of ethyl is usually 20 parts by weight or more, preferably 30 to 50 parts by weight, and the amount of unreacted 2,6-dialkylphenol recovered in the subsequent distillation step is usually 80 parts by weight or less, preferably 70 to 50 parts by weight. Department.
- the aqueous slurry was subjected to solid-liquid separation using a notch-type centrifugal filter, and 59 parts by weight of hot water at 60 ° C was used. Wash the solids in the centrifuge by centrifugation and contain 3,3 ', 5,5'-tetramethyl-4,4'-bifu containing 16% by weight of water. 57 parts by weight of enol were obtained.
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JPS61268641A (ja) * | 1985-05-23 | 1986-11-28 | Mitsubishi Petrochem Co Ltd | 3,3′,5,5′−テトラメチル−4,4′−ジヒドロキシジフエニルの製造法 |
WO1988002745A1 (en) * | 1986-10-14 | 1988-04-21 | Mitsui Petrochemical Industries, Ltd. | Process for producing biphenols |
JPH03275638A (ja) * | 1990-03-22 | 1991-12-06 | Mitsubishi Petrochem Co Ltd | 3,3’,5,5’―テトラメチル―4,4’―ビフェノールの製造方法 |
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- 2004-09-17 CN CNB2004800105883A patent/CN100339346C/zh active Active
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JPS61268641A (ja) * | 1985-05-23 | 1986-11-28 | Mitsubishi Petrochem Co Ltd | 3,3′,5,5′−テトラメチル−4,4′−ジヒドロキシジフエニルの製造法 |
WO1988002745A1 (en) * | 1986-10-14 | 1988-04-21 | Mitsui Petrochemical Industries, Ltd. | Process for producing biphenols |
JPH03275638A (ja) * | 1990-03-22 | 1991-12-06 | Mitsubishi Petrochem Co Ltd | 3,3’,5,5’―テトラメチル―4,4’―ビフェノールの製造方法 |
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CN111960927A (zh) * | 2020-08-28 | 2020-11-20 | 湖南长岭石化科技开发有限公司 | 一种催化加氢制备3,3`,5,5`-四烷基-4,4`-联苯二酚的方法 |
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CN1777570A (zh) | 2006-05-24 |
KR20060055446A (ko) | 2006-05-23 |
CN100339346C (zh) | 2007-09-26 |
KR101141612B1 (ko) | 2012-05-17 |
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