WO1991009832A1 - Procede de production en continu de carbonate aromatique - Google Patents
Procede de production en continu de carbonate aromatique Download PDFInfo
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- WO1991009832A1 WO1991009832A1 PCT/JP1990/001734 JP9001734W WO9109832A1 WO 1991009832 A1 WO1991009832 A1 WO 1991009832A1 JP 9001734 W JP9001734 W JP 9001734W WO 9109832 A1 WO9109832 A1 WO 9109832A1
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- distillation column
- carbonate
- catalyst
- continuous multi
- aromatic
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C68/00—Preparation of esters of carbonic or haloformic acids
- C07C68/06—Preparation of esters of carbonic or haloformic acids from organic carbonates
Definitions
- the present invention relates to a method for continuously producing an aromatic carbonate. More specifically, the dialkyl force represented by I ⁇ OCOR 1
- Ne one Bok, or a mixture thereof as a starting material aromatic Zokuhi mud alkoxy compounds I Table in A r 1 0H, Al represented by R 3 0C0Ar 3
- the reaction is carried out using killer reel carbonate or a mixture thereof as a reactant, and a transesterification reaction is carried out between the reactant and the starting material to obtain ROCOAr and Z corresponding to the reactant and the reactant.
- the aliphatic carbonate mixture is continuously extracted in liquid form from the lower part of the distillation column, while the by-product as a low-boiling product is continuously distilled off by distillation from the upper part of the distillation column in gaseous form.
- the present invention relates to a method for extracting an aromatic carbonate or a mixture of aromatic carbonates in a continuous and efficient manner.
- Aromatic carbonate is used as a raw material for producing aromatic polycarbonate without using toxic phosgene, or toxic phosgene, which is becoming increasingly useful as an engineering plastic in recent years. It is useful as a raw material for producing various litho-carbonates without using slag.
- the method for producing aromatic carbonates starting from dialkyl carbonate, alkenyl realyl carbonate or a mixture thereof, reacting an aromatic hydroxy compound, alkyl aryl carbonate or a mixture thereof.
- a method for producing a corresponding aromatic carbon or aromatic carbonate mixture by subjecting a substance to a transesterification reaction between a starting substance and a reactant;
- Japanese Patent Laid-Open No. 54-48733 Japanese Patent Laid-Open No. 2736062, Japanese Patent Application Laid-Open No. 54-63023, Japanese Patent Application Laid-Open No. 60-1G 9444 (US Pat. No. 4,554,110), Japanese Patent Application No. 60-169445 ( U.S. Pat. No. 4,552,704), Japanese Patent Application Laid-Open No. 62-277345, Japanese Patent Application Laid-Open No.
- a catalyst for producing a diaryl carbonate by disproportionating the diaryl carbonate and the dialkyl carbonate by the same kind of intermolecular ester exchange reaction of the alkylaryl carbonate.
- a transition metal compound capable of generating noreic acid and ruisic acid Japanese Patent Laid-Open No. 51-75044 (West German Patent Publication No. 2552907, US Patent No. 4045464)]
- a polymeric tin compound Japanese Patent Application Laid-Open No. 60-169444 (US Pat. No. 4,554,110)]
- a general formula R-X ( 0)
- the reactive distillation in these conventional methods is based on the reaction
- an apparatus in which a portion for performing distillation and a portion for performing distillation are separately used is used.
- only distillation is performed in the distillation column, and no reaction is performed.
- the reaction is carried out in the liquid phase in the reactor, but the by-produced low-boiling alcohol is discharged from the liquid phase to the gas phase via the gas-liquid interface. Only after this does the equilibrium of the reaction shift to the production system side, and the reaction proceeds.
- the reactor used in these methods is a tank type, and the reaction is extremely slow because the gas-liquid boundary area is as small as the cross-sectional area of the reactor.
- the present inventors have developed the aromatic carbonates at a high reaction rate and a high reaction rate without the disadvantages of the various methods proposed so far.
- the starting materials and reactants were continuously supplied into a continuous multi-stage distillation column, The transesterification reaction between the two substances is carried out in the presence of a catalyst, and at the same time, aromatic carbonate or a mixture of aromatic carbonates as a high-boiling product to be produced is continuously supplied in a liquid form from the bottom of the distillation column.
- the by-product as a low-boiling product formed on the other hand is removed by distillation.
- one object of the present invention is to provide a novel multi-stage distillation column as a reaction column, a novel process for producing aromatic carbonate efficiently and continuously with a high reaction rate and a high selectivity. In providing a method.
- Another object of the present invention is to provide a method for producing a desired aromatic carbonate more efficiently by using a plurality of continuous multi-stage distillation columns.
- each of R 1 , R 2 and R 3 is independently an alkyl group having 1 to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms or Represents an aralkyl group of 6 to 10, and each of kt 1 , Ar 2 and Ar 3 independently represents an aromatic group having 5 to 30 carbon atoms) and is subjected to a transesterification reaction.
- a reactant selected from a mixture thereof provided that each of R 1 , R 2 and R 3 is independently an alkyl group having 1 to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms or Represents an aralkyl group of 6 to 10, and each of kt 1 , Ar 2 and Ar 3 independently represents an aromatic group having 5 to 30 carbon atoms
- the starting material and the reactant are continuously fed into a continuous multi-stage distillation column, and In the liquid phase or gas-liquid phase in the presence of a catalyst, and at the same time, a high-boiling reaction mixture containing the aromatic carbonate or aromatic carbonate mixture produced.
- the liquid is continuously withdrawn from the lower part of the distillation column in a liquid state, and the low-boiling reaction mixture containing the by-products formed is distilled by distillation. Continuously extracting gaseous gas from the upper part of the distillation tower, thereby making it possible to continuously produce aromatic carbonate or a mixture of aromatic carbonates. A method is provided for doing so.
- reaction included in the method of the present invention is represented by the following reaction formula.
- each ⁇ independently represents Ar 2 or Ar 3
- each R independently represents R 2 Or R 3.
- the reaction is an intermolecular transesterification reaction of the same species, and is usually also referred to as a disproportionation reaction.
- the method of the present invention is characterized in that these reactions are carried out in a continuous multistage distillation column in the presence of a catalyst, and at the same time, low-boiling products produced by the reaction are separated from the reaction system by distillation. For the first time, high selectivity and high Aromatic carbonate can be produced continuously in high yield.
- the reaction of the present invention the equilibrium is biased extremely original system [for example, the equilibrium constants of the reaction of formula (1) is of the order of 1 0 one third to one 0 one 4 ) Can proceed at a high reaction rate, and it is quite unexpected that aromatic aromatic carbonates can be produced continuously with high selectivity and high yield.
- the method of the present invention has a higher reaction rate as compared with the conventional method, and can dramatically improve the selectivity and the yield (or productivity). Although the specific reason is not clear, the following is presumed based on the result of implementing the method of the present invention.
- the reactions of the present invention represented by the above formulas (1) to () are all equilibrium reactions, and all the equilibria are extremely biased toward the original system.
- by-products which are low-boiling products generated by the reaction usually, in the reactions of the formulas (I) and (2), aliphatic alcohols, the formulas (3) and ( In the reaction 4), it is necessary to remove the dialkyl force (one carbonate) from the liquid phase in the reaction system as quickly as possible.
- reaction rate using a reaction vessel equipped with a distillation column at the top could not necessarily increase the reaction rate.
- the catalyst can be present in a wide range within the continuous multi-stage distillation column, and the reaction can proceed in a wide area having a very large gas-liquid boundary area. .
- the supplied liquid substance to be reacted flows down while reacting while repeating the vapor-liquid contact with the vapor rising from below.
- the low-boiling products evaporate from the liquid phase to the vapor phase.
- each component in the continuous multi-stage distillation column has a concentration distribution.
- the concentration of the alkyl aryl carbonate and / or diaryl carbonate, which are usually high-boiling products, in the liquid is as follows. From the highest stage where the catalyst is present to the bottom of the tower, the distribution has a gradually increasing distribution.On the other hand, the concentration of aliphatic alcohol, which is a low-boiling product, in the liquid is usually from the top of the column to the bottom of the column. With the distribution gradually decreasing toward the bottom, it is possible to make the concentration in the liquid extremely low near the bottom of the tower. In the vapor phase, the concentration of aliphatic alcohol gradually increases from the bottom to the top of the tower.
- the liquid of diaryl carbonate which is usually a high boiling product
- the concentration in the liquid has a gradually increasing distribution from the highest stage where the catalyst is present to the bottom of the column, while the concentration of dialkyl carbonate, which is a low-boiling product, is usually in the liquid.
- the vapor phase has a distribution in which the concentration of dialkyl carbonate gradually increases from the bottom to the top of the tower.
- these reactions proceed in the continuous multi-stage distillation column.
- the liquid phase in the reaction system is a result of the reaction and the equilibrium composition It is considered that the vapor phase has a composition that is close to the gas-liquid equilibrium state with respect to the liquid phase. Therefore, if the liquid phase stays at this position, the reaction does not proceed any further, but in fact, the liquid phase flows down to lower the concentration of the reaction product with a lower boiling point, thereby lowering the vapor level.
- the gas-liquid contact with the phase allows the reaction to proceed further, further increasing the concentration of the aromatic liquid carbonate, a high boiling product, in the liquid phase
- the conventional method in which a reaction is carried out in a reaction vessel in which a distillation tower is installed at the top is a method in which the reaction proceeds only in the reaction vessel, and the distillation tower simply comes out of a gas phase from a gas-liquid interface in the reaction vessel. It merely plays the role of separating the low-boiling product vapor and the low-boiling raw material compound vapor, allowing the low-boiling raw material compound to flow down in a liquid state, and returning to the reactor.
- the reason that the method of the present invention has an excellent effect as compared with the conventional method is considered to be mainly due to the following points.
- the gas-liquid boundary area can be made very large compared to the reaction type using a reaction vessel, and as a result, mass transfer of by-products, low-boiling products, to the vapor phase is easy. is there.
- dialkyl carbonate used as a starting material of the present invention is represented by the general formula i ⁇ OCO R 1
- R 1 represents an alkyl group having 1 to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms, or an aralkyl group having 6 to 10 carbon atoms. These include, for example, methyl, ethyl, propyl (each isomer), arylbutyl (each isomer), butenyl (each isomer), pentyl (each isomer), Xyl (each isomer), heptyl (each isomer), octyl
- dialkyl carbonate having R 1 examples include, for example, Circa carbonate, getyl carbonate, dipropyl carbonate (each isomer), diaryl carbonate, dibutenyl carbonate (each isomer), dibutyl carbonate (Each isomer), dipentyl carbonate (each isomer), dihexyl carbonate (each isomer), diheptyl carbonate (each isomer), dioctyl carbonate (each isomer), dino Nilka carbonate (each isomer), didecyl carbonate (each isomer), dicyclopentinocarbonate, dicyclohexynolecarbonate, dicycloheptinolecarbonate, dibenzyl Norecarbonate, diphenylethyl carbonate (each isomer), di (phenylphenol pill) carbonate (each isomer), di (phenylbutyl) carbonate
- R 1 in the bets are consisting of lower alkyl group having 4 or less carbon atoms dialkyl Norekabone Todea Li, particularly preferred Shiino, dimethyl It is a chill car bottle.
- the aromatic Zokuhi mud key sheet compound used as a reactant in the present invention the general formula A OH iA r 1 is a one represented by represents an aromatic group having 5 to 30 carbon atoms), Any type may be used as long as the hydroxy group is directly bonded to the aromatic group. Examples of such r 1 include, for example, phenyl and trinole.
- A is single bond, or - 0 -, - S -, -CO-, - S0 2 - a which a divalent group or,
- R 4 , R 5 , R 6 , and R 7 are each independently a hydrogen atom, 1
- a cycloalkylene group such as C (CH 2) k (where k is an integer of 3 to ⁇ , and a hydrogen atom is substituted by a lower alkyl group, an aryl group, a halogen atom, etc.)
- the aromatic ring is formed by a substituent such as a lower alkynole group, a lower anoreoxy group, an ester group, a hydroxyl group, a nitro group, a halogen group or a cyano group. May be substituted.
- Substituted naphthyl (each isomer), methyl naphthyl (each isomer), dimethyl naphthyl (each isomer), chloronaphthyl (each isomer), methoxy naphthyl (Each isomer), naphthyl groups such as cyano naphthyl (each isomer) and various substituted naphthyl groups; pyridyl (each isomer), coumaryl (each isomer), quinolyl (each isomer) ), Methylpyridyl (each isomer), chloropyridyl (each isomer), methylkumalinole (each isomer), methylquinolyl (each isomer), etc.
- Each type of substitution includes tera-aromatic groups.
- Examples of such an aromatic hydroxy compound having Ar 1 include phenol; talesol (each isomer), and xylenol. (Each isomer), trimethyl phenol (each isomer), tetramethyl phenol (each isomer), ethyl phenol (each isomer), Knol (each isomer), butylphenol (each isomer), getinolenophenol (each different I organism), methylethylenophenol (each isomer), methylpropyl enolate (Each isomer), dipropyl phenol (each isomer), methylbutylphenol (each isomer), pentylphenol (each isomer), hexylphenol (each isomer) Various phenols such as isocyanate) and cyclohexylphenol (each isomer); various alcohols such as methoxyphenol (each isomer) and ethoxy phenol (each isomer)
- aromatic ring may be substituted by a substituent such as a lower alkyl group, a lower alkoxy group, an ester group, a nitro group, a cyano group, a nitrogen atom, and the like.
- aromatic hydroxy compounds which can also be used, for example, the aromatic dihydroxy compounds represented by the following formulas, Ar 1 is preferably an aromatic compound having 6 to 10 carbon atoms.
- Aromatic monohydroxy compounds consisting of groups, particularly preferred are phenols
- alkyl aryl carbonate used as a starting material in the present invention is represented by the general formula
- R 2 may be the same or different from R 1 and represents an alkyl group having 1 to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms, or an aralkyl group having 6 to 10 carbon atoms
- 2 may be the same as or different from Ar 1 and represents an aromatic group having 5 to 30 carbon atoms.
- R 2 include the same groups as those exemplified for R 1 above, and examples of Ar 2 include those similar to those exemplified for Ar 1 above. Is mentioned.
- Alkyl carbohydrates having such R 2 and ⁇ r 2 examples include methylphenyl carbonate, ethenolefenenolecarbonate, propinolefenenolecarbonate (different 1 "living organism), arylenophenyl carbonate, butylphenyl carbonate ( Each isomer), pentyl phenyl carbonate (each isomer), hexyl phenyl ninyl carbonate (each isomer), heptyl phenyl carbonate (each isomer), octyl tri-carbonate (each isomer) , Nonyl (ethylphenyl) carbonate (each isomer), decyl (butylphenyl) carbonate (each isomer), methyltriylcarbonate (each isomer), ethyltrilecarbonate (each isomer) ), Propyl toluene carbonate (each isomer), butyl carbonate (
- alkyl carbonyls those in which R 2 is an alkyl group having 1 to 4 carbon atoms and Ar 2 is an aromatic group having 6 to 10 carbon atoms are preferably used. Particularly preferred is methyl carbonate.
- the alkyl aryl carbonate used as the reactant of the present invention has a general formula
- R 3 0C0Ar 3 It is represented by R 3 0C0Ar 3 , and R 3 may be the same or different from R 1 and R 2, and the number of carbons! Represents an alkyl group having up to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms, or an aralkyl group having 6 to 10 carbon atoms, and Ar 3 may be the same as or different from Ar 1 Ar 2, and may have 5 to 5 carbon atoms. Represents 30 aromatic groups. Examples of such R 3 include the same groups as those exemplified for R 1 above, and examples of ⁇ r 3 include the same groups as those exemplified for ⁇ r 1 above. Is mentioned.
- alkyl carbonates those in which R 3 is an alkyl group having 1 to 4 carbon atoms and Ar 3 is an aromatic group having 6 to 10 carbon atoms are preferably used. Particularly preferred is methanol-free carbonate.
- dialkyl carbonate and alkyl aryl carbonate as starting materials may be used. These compounds may be used as a mixture of two or more, and the aromatic hydroxy compound and the alkyl aryl carbonate as the reactants may be used alone or as a mixture of two or more. You may.
- diaryl carbonate can be obtained from dialkyl carbonate and an aromatic hydroxy compound via alkyl aryl carbonate. This is a particularly preferred embodiment of the invention.
- dialkyl carbonate by-produced in the reaction represented by the formula (6) is recycled as a starting material for the reaction represented by the formula (5), the result is that From one mole of dialkyl carbonate and two moles of aromatic hydroxy compound, one mole of diallyl carbonate and two moles of aliphatic alcohol can be obtained.
- Examples of the catalyst used in the present invention include, for example,
- Pb0, Pb0 2, Pb 3 0 4 lead oxide such as; P1) S, lead sulfide such as Pb 2 S;.
- Pb (0H ) 2, Pb 2 0 2 (OH) lead hydroxide such as 2; Na 2 Pb0 2, K 2 Pb 0 2, NaHPb0 2, zinc acid salts such as KHPb0 2; Na 2 Pb0 3, Na 2 H 2 Pb0 4
- Lead acid salts such as; PbC0 3, 2PbC0 3 'Pb (OH) 2 lead carbonates such as And its basic salts; Pb (0C0CH 3 ) 2 , Pb (OCOCHg) 4 Pb (0C0CH 3 ) 2 ⁇ PbO
- Lead salts and carbonates and basic salts of organic acids such as 3H 2 0; Bu 4 Pb, Ph 4 Pb, Bu 3 PbC U Pli 3 Pl) Br, PhgPb- (also (or P h 6 P b 2), Bu 3 PbOH, organic lead compounds such as Ph 3 PbO (Bu is a butyl group , Ph represents a phenyl group); Pb (OCH 3 ) 2 , (CH 30 ) Pb (OPh), Pb (0Ph) 2, and other alkoxyleads, aryloxyleads; Pb-Na, Pb- Lead alloys such as Ca, Pb-Ba, Pb-Sn, and Pb-Sb; lead minerals such as when ore and phenanite; and hydrates of these lead compounds; (copper group metal compounds )
- Salts and complexes of copper group metals such as (CH 3 ) 3 ] n and [Cu (C 7 H 8 ) C 1] 4 (OAc represents an acetyl group, acac represents an acetyl aceton chelate ligand);
- Li (acac) have i N (C 4 ⁇ 9) 2 or the like alkali metal complex [(acac) Tsuri is as defined above];
- a complex of zirconium such as Zr (acac) 4 (where (acac) is as defined above) or zirconocene;
- Inorganic oxides such as silica, alumina, titania, silica titania, zinc oxide, zirconium oxide, gallium oxide, zeolite, and rare earth oxides; Modified by a method such as reeling;
- These catalysts can be dissolved in the liquid phase of the reaction system. May not be soluble.
- these catalysts can be used as a mixture with a compound or a carrier inert to the reaction, or supported on them.
- these catalyst components are present in the reaction system in organic compounds, such as aliphatic alcohols, aromatic hydroxy compounds, alkylaryl carbonates, diaryl carbonates, and dialkyl carbonates. It may be one that has reacted with a net or the like, or one that has been heat-treated with a starting material, a reactant, or a product as a raw material prior to the reaction.
- Pb0 2 lead oxide such as Pb 3 0 4; Pb (OH ) 2, P b 2 0 2 (OH) 2 aqueous lead oxide such as; PbC0 3, 2PbC0 3 -Pb ( OH) , such as 2 lead basic salts of carbonate and its; Pb (0CH 3) 2, (CH 3 0) Pb (OPh), Pb (0Ph) alkoxy lead such as 2, lead compounds der Li of such ⁇ re Ruokishi lead compounds These include those in which these lead compounds have reacted with organic compounds present in the reaction system, or those in which these lead compounds have been heat-treated with starting materials, reactants, or products as raw materials prior to the reaction. It is preferably used.
- the continuous multi-stage distillation column used in the present invention is a distillation column having a theoretical number of distillation stages of 2 or more, and may be any column as long as continuous distillation is possible.
- Such a continuous multi-stage distillation column includes, for example, a tray column type using a tray such as a bubble bell tray, a perforated plate tray, a valve tray, a counter-current tray, and a Raschig ring. , Filling ring, pole ring, benorenoresa donore, interroxsa donore, dixon knocking, mcmahonno ⁇ 0 packing, ⁇ he knock, snorare packing, merapak etc.
- any type of column usually used as a continuous multi-stage distillation column such as a packed column type, can be used.
- the number of distillation columns in the present invention indicates the number of trays in the case of a tray column, and indicates the number of theoretical plates in a packed tower system or other distillation columns.
- a tray-one-packing-mixing-column system having both a plate portion and a portion filled with the packing material is also preferably used.
- a packed column distillation column in which the solid catalyst is packed instead of part or all of the packing is preferably used.
- the catalyst is present in the continuous multi-stage distillation column, and more preferably, the catalyst is present in two or more stages in the continuous multi-stage distillation column.
- the method for causing the catalyst to be present in such a continuous multi-stage distillation column may be any method.
- the catalyst can be present in the reaction system by continuously supplying the catalyst to the distillation column, or the liquid phase in the distillation column can be used.
- the catalyst can be present in the reaction system by disposing the solid catalyst in the distillation column, and a method using both of them can be used. It may be.
- the raw material When the homogeneous catalyst is continuously supplied to the distillation column, the raw material may be mixed with one or both of the starting material and the reactant, and supplied simultaneously with the supply of the raw material. May be supplied to a different stage. Also, at least from the bottom of the tower
- the catalyst may be supplied to any position as long as it has one or more stages. However, since the reaction actually proceeds in the distillation column usually in a region below the position where the catalyst is supplied, the catalyst is supplied to a region between the column top and the raw material supply position. This is preferred. When a heterogeneous solid catalyst is used, the catalyst can be packed at a required position in the distillation column ⁇ in a required amount, and the number of theoretical plates in the layer where the catalyst is present is at least one. It is sufficient if there are at least two or more stages. This solid catalyst also has the effect of filling the distillation column.
- the method according to the basic aspect of the present invention comprises: R 0Ar 2
- a reactant selected from reel carbonate and a mixture thereof (provided that each of RR 2 and R 3 is independently an alkyl group having 1 to 10 carbon atoms, an alicyclic group having 3 to 10 carbon atoms or 6 to 6 carbon atoms) 10 represents an aralkyl group, and each of Ar 1 , Ar 2 and Ar 3 independently represents an aromatic group having 5 to 30 carbon atoms.
- a transesterification reaction between the two substances is carried out in a liquid phase or a gas-liquid phase in the presence of a catalyst, and at the same time, a high boiling point reaction containing the produced aromatic carbonate or aromatic carbonate mixture.
- the method includes continuously withdrawing the mixture in a liquid state from the lower portion of the distillation column in a liquid state, and continuously withdrawing a low-boiling reaction mixture containing by-products formed in a gaseous state from the upper portion of the distillation column by distillation. Accordingly, it is characterized in that it is possible to continuously produce an aromatic carbonate or a mixture of aromatic carbonates.
- the method of continuously feeding the starting material and the reactant to the continuous multi-stage distillation column may be supplied in at least one stage, preferably at least two stages of the distillation column. However, any method may be used as long as it can be brought into contact with the catalyst.
- the starting material and the reactant can be continuously supplied from a required number of inlets to a required stage of a continuous multi-stage distillation column, and the starting material and the reactant can be supplied to the distillation column in a continuous multi-stage distillation column. They may be introduced in the same stage, or may be introduced in different stages.
- the starting material and the reactant are continuously supplied as a liquid, a gas, or a mixture of a liquid and a gas.
- the gaseous starting material and / or the reactant may be additionally intermittently or continuously fed from the bottom of the distillation column. It is also preferable to supply them on a regular basis.
- a raw material having a higher boiling point, out of the raw material composed of the starting material and the reactant ⁇ , is continuously supplied to the distillation column in a liquid or gas-liquid mixed state in the upper stage of the stage where the catalyst is present.
- the high-boiling material supplied from the upper portion may of course contain a low-boiling material.
- the product aliphatic alcohol and alkylaryl carbonate or diaryl carbonate for the reaction of formula (1) or (2)
- dialkyl carbonate and alkyl although it may include a reel carbonate (in the case of the reaction of the formula (3) or (4)), the reactions of the formulas (1) to (4) included in the present invention are reversible reactions. Therefore, when the concentration of these products is too high, it is not preferable because the reaction rate of the raw material is reduced.
- the ratio of the starting material to the reactant supplied to the continuous multi-stage distillation column can vary depending on the type and amount of the catalyst and the reaction conditions, but usually the molar ratio of the reactant to the starting material is 0 in molar ratio. . 0 1 ⁇
- a range of 1000 times is preferred.
- a starting material reacts with a reactant in the presence of a catalyst, and a corresponding target product, aromatic carbonate, and a corresponding by-product, month: Aliphatic alcohol [for the reaction of formulas (1) and (2)] or dialkyl carbonate [the reaction of formulas (3) and (4)] Of these target products or by-products, the lower-boiling product having the lower boiling point is continuously removed in gaseous form from the distillation column.
- the aliphatic alcohol or the dialkyl carbonate, which is a by-product usually has a lower boiling point than the aromatic carbonate, which is a target product.
- the material is continuously extracted from the distillation column in a gaseous state.
- the gaseous extract may be a low-boiling by-product alone, a mixture of the starting material and Z or a reactant, or, in some cases, an aromatic carbonate that is a high-boiling product May be contained in small amounts.
- the outlet for extracting gaseous substances containing low-boiling by-products from the continuous multi-stage distillation column can be provided at an appropriate position other than the bottom of the column, but the concentration of low-boiling by-products in the vapor phase is as follows: It usually increases as you go to the top of the tower. Therefore, it is preferable that the outlet for the gaseous substance is provided above the supply positions of the starting material and the reactant as the raw material, and between the supply position and the top of the tower, or It should be located at the top, particularly preferably at the top of the tower.
- the gaseous component extracted in this manner may be liquefied by cooling or the like, and a part of the gaseous component may be returned to the upper portion of the distillation column, that is, a so-called reflux operation may be performed.
- a so-called reflux operation may be performed.
- Increasing the reflux ratio by this reflux operation increases the efficiency of distillation of low-boiling by-products into the vapor phase Therefore, the concentration of low-boiling by-products in the extracted gas component can be increased.
- the reflux ratio is usually from 0 to 20, preferably from 0 to 10.
- Aromatic carbonate which is the target product produced by the method of the present invention, is continuously withdrawn as a high-boiling product in a liquid form from the lower part of the continuous multistage distillation column.
- the liquid extract may be an aromatic carbonate alone, a mixture of the starting material and Z or a reactant, or may contain a small amount of a low-boiling product.
- the liquid extract also includes the catalyst.
- An outlet for extracting a liquid substance containing an aromatic product, which is an aromatic carbonate, from the continuous multi-stage distillation column is provided at the lower portion of the column, particularly preferably at the bottom of the column.
- the liquid substance thus extracted may be returned to the lower part of the distillation column in a gaseous or gas-liquid mixture state by heating a part of the liquid substance with a reboiler. .
- the amount of the catalyst used in the present invention depends on the type of the catalyst to be used, the type of the continuous multi-stage distillation column, the types and the ratios of the starting materials and the reactants, and the reaction conditions such as the reaction temperature and the reaction pressure.
- the catalyst is continuously supplied to the reaction zone of the continuous multi-stage distillation column, the total amount of the starting material and the reactants as the feed materials is not sufficient. Expressed as a percentage of the total weight, it is usually used at 0.000.50% by weight.
- a catalyst amount of 0.01 to 75% by volume based on the empty space of the distillation column is preferably used.
- the reaction takes place in a continuous multi-stage distillation column in which a catalyst is present, and thus, the amount of the generated reaction product usually depends on the amount of the hold-up liquid in the distillation column.
- a distillation column having the same height and diameter a distillation column with a large amount of hold-up liquid can make the residence time of the liquid phase, that is, the reaction time relatively long, in the sense of the above. I like it.
- the amount of the hold-up liquid is too large, the residence time becomes longer, so that a side reaction progresses and flooding is liable to occur.
- the hold-up liquid volume of the distillation column used in the present invention can vary depending on the distillation conditions and the type of distillation column, it is expressed by the volume ratio of the hold-up liquid volume to the empty column volume of the continuous multi-stage distillation column. Usually, it is performed at 0.005 to 0.75.
- the average residence time of the liquid phase in the continuous multi-stage distillation column varies depending on the reaction conditions, the type of the continuous multi-stage distillation column, and the internal structure (for example, the type of the tray and the packing).
- the reaction temperature is the temperature in the continuous multi-stage distillation column, which varies depending on the type of starting materials and reactants used, but is usually 50 to 350 ° C. It is preferably carried out in the range of 100 to 280 ° C.
- the reaction pressure varies depending on the type of starting materials and reactants used, the reaction temperature, etc., but may be reduced pressure, normal pressure, or increased pressure.
- an inert solvent suitable for the purpose of facilitating the reaction operation for example, ethers, aliphatic hydrocarbons, aromatic hydrocarbons, Halogenated aliphatic hydrocarbons, halogenated aromatic hydrocarbons, and the like can be used as the reaction solvent.
- an inert gas such as nitrogen, helium, or argon may be allowed to coexist in the reaction system as a substance inert to the reaction, or may be continuously used for the purpose of accelerating the distillation of generated low-boiling by-products.
- the inert gas or the low-boiling organic compound inert to the reaction may be introduced in a gaseous state from the lower part of the multistage distillation column.
- a raw material mixture comprising a starting material and a reactant and a catalyst are fed through a pre-heater 5 through an inlet pipe 2 to a continuous multi-stage distillation equipped with a reboiler 10 and a condenser 13.
- the liquid is continuously introduced into the tower 1, and the bottom liquid is heated again by the reboiler 10.
- Aromatic car a high-boiling product produced in the presence of a catalyst inside a continuous multistage distillation column
- the liquid component containing the boron is continuously withdrawn as a bottom liquid 19 from the bottom of the column.
- Gas phase components containing low-boiling products, which are by-products of the reaction, are continuously extracted as a top gas 12, condensed in a condenser 13, and then converted to a top liquid 16. Are continuously extracted. A portion of the top liquid can be refluxed from 15 to the top of the continuous multistage distillation column.
- a raw material mixture and a catalyst composed of a starting material and a reactant are continuously introduced into a continuous multi-stage distillation column 1 through a preheater 5 through an introduction pipe 2, and simultaneously a starting material or In one of the reactants, a low-boiling compound is introduced into the introduction pipe 8 ′, vaporized in the evaporator 10 ′, and then continuously introduced into the lower part of the continuous multi-stage distillation column 1. I do. In this way, the reaction and distillation are performed.
- the liquid component containing aromatic carbonate which is generated in the continuous multi-stage distillation column in the presence of the catalyst and has a high boiling point and is produced is continuously extracted from the lower part of the column as a bottom liquid 19.
- Gas phase components containing low-boiling products, which are reaction by-products, are continuously extracted as overhead gas 12 and condensed in a condenser 13, and then continuously as overhead liquid 16. It is extracted to the target.
- the continuous multi-stage distillation column is used as a first continuous multi-stage distillation column, and has a second continuous multi-stage distillation column coupled thereto, and is continuously supplied to the first distillation column.
- a dialkyl carbonate Natick preparative represented by 1 anti JSAP matter is ⁇ Li fragrant Zokuhi Dorokishi compounds represented by a OH, continuously withdrawn from the first distillation column bottom is produced that
- the aromatic carbonate or the aromatic carbonate mixture contained in the high boiling reaction mixture is an alkyl aryl carbonate represented by R COAr 1 (R 1 and Ar 1 are as defined above), and the first distillation column byproduct aliphatic alcohol in ⁇ Li represented by R 1 0H from the top contained in continuous low-boiling reaction mixture withdrawn Te, R COAr 1 (provided that, R 1 and Ar 1 Is the communication defined above.
- R 3 0C0R 3 dialkyl force one Bone preparative byproducts or dialkyl carbonate Ne Ichito mixture byproducts second by distillation a low boiling point reaction mixture containing a represented by
- a method is further provided which comprises continuously withdrawing gaseous from the top of the continuous multi-stage distillation column.
- the catalyst is a catalyst that can be dissolved in the liquid phase, and is contained in at least one of the first continuous multistage distillation column and the second continuous multistage distillation column.
- the continuous multi-stage distillation column is used as a first continuous multi-stage distillation column, and a second continuous multi-stage distillation column is coupled thereto.
- the aromatic carbonate or aromatic contained in the high-boiling reaction mixture that is produced and continuously extracted from the lower part of the first distillation column, and the carbonate mixture is R 10 C 0A r 1 (R 1 and lambda r 1 is a Arukirua reel carbonate Natick Bok represented by Tsuri) as defined above, by-products in the low boiling point reaction mixture withdrawn generated from the first distillation column upper portion continuously aliphatic alcohols der to things represented by R 1 0H Li, R 1 0 C0 A
- the high-boiling reaction mixture is continuously withdrawn in a liquid state from the lower part of the second continuous multistage distillation column, while the generated carbonyl carbonate represented by R COK 1 is formed.
- a method is further provided which comprises continuously withdrawing the low boiling reaction mixture containing the product in the gaseous form from the top of the second continuous multi-stage distillation column by distillation.
- the low-boiling reaction product comprising dialkyl carbonate Ne one preparative represented by I ⁇ O CO R 1 withdrawn Li by the upper portion of the second continuous multi-stage distillation column into the first continuous multi-stage distillation column Recirculation is preferred.
- the catalyst is a catalyst that can be dissolved in the liquid phase, and the catalyst is contained in at least one of the first continuous multistage distillation column and the second continuous multistage distillation column.
- the force existing in the liquid phase and Z or the catalyst is a solid catalyst substantially insoluble in the liquid phase, and is at least in the first continuous multistage distillation column and the second continuous multistage distillation column. It is preferable that one of the distillation columns is disposed without being dissolved in the liquid phase.
- the catalyst is soluble in the liquid phase, it is preferable that the catalyst is dissolved in each liquid phase in both the first continuous multistage distillation column and the second continuous multistage distillation column.
- the respective catalysts in the first and second distillation columns may be the same or different from each other.
- part or all of the evaporant is continuously supplied to a second continuous multi-stage distillation column.
- a part or all of the residual liquid containing is recycled to the first continuous multi-stage distillation column.
- a small amount of a starting compound (dialkyl carbonate and / or aromatic hydroxy compound) and an aromatic carbonate (alkyl alcohol) (Reel carbonate and / or ⁇ aryl carbonate) and other high-boiling by-products in addition to the catalyst component, a small amount of a starting compound (dialkyl carbonate and / or aromatic hydroxy compound) and an aromatic carbonate (alkyl alcohol) (Reel carbonate and / or ⁇ aryl carbonate) and other high-boiling by-products.
- a part or all of the catalyst present in the second continuous multi-stage distillation column is dissolved in the liquid phase so as to be present, and is withdrawn from the lower part of the second distillation column.
- the liquid high-boiling reaction mixture is led to a second evaporator, and separated into an evaporate containing diaryl carbonate represented by A ⁇ OCOA r 1 and a residual solution containing the dissolving catalyst, and then dissolving the solution. It is preferable to recycle part or all of the residual liquid containing the catalyst to the second continuous multistage distillation column.
- a small amount of an aromatic hydroxy compound, an alkyl aryl carbonate, diaryl carbonate, or other high boiling point By-products may be included.
- Such a separation / recirculation step of the catalyst may be performed using either the liquid high-boiling reaction mixture withdrawn from the bottom of the first continuous multi-stage distillation column or the liquid high-boiling reaction mixture withdrawn from the bottom of the second continuous multi-stage distillation column. It may be carried out on one of the two or both.
- the residual liquid containing the catalyst contains a high-boiling by-product other than the target product
- the residual liquid Prior to recirculation, it is possible to extract part or all of it and separate and remove high-boiling by-products
- the high-boiling reaction mixture containing the desired aromatic carbonate extracted from the lower part of the continuous multi-stage distillation column is subjected to ordinary separation and purification methods such as distillation and crystallization. As a result, a desired aromatic carbonate can be isolated.
- a continuous multistage consisting of a packed tower with a tower height of 4 ⁇ and a tower diameter of 3 inches, filled with stainless steel Dickson packing (about 6 mm in diameter) as the packing material
- a mixture comprising dimethyl carbonate, phenol and a catalyst was continuously supplied in liquid form from the inlet pipe 2 to the distillation column 1 via the preheater 5 and the conduit 6 to a position lm from the column of the distillation column.
- the amount of heat required for the reactive distillation was supplied by heating the liquid at the bottom of the column with a reboiler 10 and circulating it through a conduit 11. Table 1 shows the reaction conditions.
- a liquid containing the catalyst component and the reaction products methylphenyl carbonate and diphenyl carbonate was continuously withdrawn from the bottom 18 of the distillation column via conduits 8 and 19.
- Table 1 shows the results of the reaction.
- the reaction solution (reaction mixture) contained 0.02% by weight of anisol which was considered to be generated by a side reaction (decarboxylation reaction) of methylphenyl carbonate. This result indicates that the selectivity of anisol based on phenol is 0.8 o / o.
- Ma The gas distilled from the conduit 12 provided in the tower section 17 was condensed in the condenser 13. A part of the condensate was refluxed to the distillation column 1 via the conduit 15, and the remaining liquid was continuously extracted from the conduit 16. Methanol, a low-boiling reaction product, was obtained from this condensate.
- a 15-liter capacity column equipped with a distillation column 63 (filled with stainless steel Dickson packing (about 6 mm in diameter)) and a stirrer ⁇ as shown in Fig. 6 with a column height of lm and a column diameter of 1 inch 12.6 kg of a liquid having the same composition as that used in Example 1 was charged from a conduit 61 into an autoclave type reaction vessel 62 of Torr. The reaction was carried out while heating the reactor 62 using an electric furnace 70 with stirring so that the liquid temperature became constant at 204 ° C. The gas distilled from the top 69 of the distillation column 63 was condensed in the condenser 65 via the conduit 64.
- a part of the condensate was refluxed through conduits 66 and 67, and the remaining liquid was continuously withdrawn at a rate of 2.1 kg / hr from conduit 68.
- the reflux ratio was 0.8.
- the reactor 62 was cooled and the reaction solution was withdrawn from the conduit 72.
- the weight was 8.4 kg.
- the ratio of the charged liquid amount to the liquid amount remaining in the kettle portion was the same as the ratio of the supply amount from the conduit 6 and the column bottom liquid withdrawal amount from the conduit 19 in Example 1.
- the distillation rate of the distillate in which the gas components were condensed was also the same. As a result of the analysis, 1.8% by weight of methylphenyl carbonate and diphenyl carbonate were contained in the reaction solution.
- reaction solution 1 The production rate per kg per hour was 9 g / kg 'for methylphenyl carbonate and 0.05 g / kg'hr for diphenyl carbonate.
- the selectivity of aromatic carbonates based on phenol was 94% for methyl phenyl carbonate and 1% for diphenyl carbonate.
- the selectivity of by-product anisol based on phenol was 5%. After a similar reaction for 4 hours, the selectivity for by-product anisol was 7%.
- Example 1 show that the amount of methyl phenyl carbonate produced was 34 g / kg'hr (selectivity 97%) and the amount of phenyl phenyl carbonate produced was 0.5 g / kg'hr (selectivity 2%) and the selectivity for by-product anisol is 8% (constant without changing over time), so a method using a batch-type reactor with a distillation column installed at the top is simply used.
- the method of the present invention is superior in that aromatic carbonate can be produced continuously at a high reaction rate and high yield (high production per unit time), high selectivity, and high selectivity. That's how it works.
- Fig. 2 it is a packed tower with a height of 4m and a diameter of 3 inches, filled with stainless steel Dickson packing (approximately 6 strokes in diameter).
- Lm from the column of continuous multistage distillation column 1 To the distillation column 1 through the pre-heater 5 from the introduction pipe 2 to the distillation column 1 continuously in the form of a liquid, and the dimethyl carbonate (a small amount of phenol) ) was introduced through an inlet pipe 8 ′ and continuously supplied to the bottom of the distillation column 1 in gaseous form via an evaporator 10.
- Table 2 shows the reaction conditions.
- Example 1 As a continuous multi-stage distillation column as shown in Fig. 2, a tray column with a height of 6 m and a diameter of 10 inches, equipped with a 20-stage sieve tray, was used instead of the packed column.
- the reaction was carried out in the same manner as in Example 5, except that the reaction was carried out under the reaction conditions shown in Table 2.
- the raw material mixture and the catalyst introduced from the introduction pipe 2 through the preheater 5 were continuously supplied into the tower at a position of 0.5 m from the top of the tower. The results are shown in Table 2.
- Example 1 1
- the ratio of the amount of condensate withdrawn in this comparative example to the amount of liquid withdrawn from the reactor was the same as the amount of condensate withdrawn in Example 11 It was the same as the ratio of the amount of bottom liquid drawn out.
- 67.3% by weight of diphenyl carbonate was formed in the reaction solution.
- the amount of diphenyl carbonate produced per kg of the reaction solution per hour was 224 g / kg'hr.
- the selectivity of diphenyl carbonate based on methylphenyl carbonate was 95%.
- anisole a by-product of the reaction, was detected.
- the selection rate of anisol based on methyl phenyl carbonate was 5%. Comparison of this result with Example 11 shows that the method of the present invention allows to obtain diallyl carbonate with high yield and selectivity.
- Example 5 Using the same apparatus as that used in Example 5, a mixture composed of methyl phenyl carbonate and a catalyst was continuously supplied from the introduction pipe 2 through the preheater 5, and further, methyl phenyl carbonate was added.
- the reaction was carried out in the same manner as in Example 5 in which the gas was introduced from the introduction pipe 8 ′ and continuously supplied in gaseous form to the bottom of the distillation column 1 via the evaporator 10 ′ and the conduit 11.
- Table 4 shows the reaction conditions. From the bottom of the continuous multi-stage distillation column, a liquid containing diphenyl carbonate as a reaction product was continuously extracted. The gas distilled from the top of the tower is condensed in the condenser 13 and continuously extracted through the conduit 16. Dimethyl carbonate, a low-boiling reaction product, was obtained from the liquid obtained. Table 4 shows the results of the reaction.
- Example 19 phenol was introduced from the introduction pipe 8 'to carry out the reaction, so that methanol and dimethyl carbonate were contained in the overhead condensate.
- Example 10 The same tray column used in Example 10 was used as a continuous multistage distillation column. The raw material and catalyst were continuously supplied to a position 0.5 m from the top of the column. The reaction was carried out in the same manner as in Example 18 except that the reaction was carried out under the following reaction conditions. The results are shown in Table 4.
- An apparatus including two continuous multistage distillation columns shown in Fig. 3 was used. It consists of a packed tower with a height of 4 m and a diameter of 3 inches, packed with stainless steel DEXON packing (approximately 6 strokes in diameter). A mixture of dimethyl carbonate, phenol and catalyst A was introduced into the position 1 lm from the top 17 of the first continuous multi-stage distillation column 1 'in the form of a liquid through the feed line 2, the conduit 4, the preheater 5, and the conduit 6. The reaction was carried out by continuously feeding and flowing down the first continuous multistage distillation column.
- the amount of heat required for the reaction and the distillation was supplied by heating the liquid at the bottom of the column through the conduits 8 and 9 in the reboiler 10 and circulating through the conduit 11.
- the gas continuously distilled from the top ⁇ was condensed in a condenser 13 via a conduit 12.
- a part of the condensate was refluxed to the first continuous multistage distillation column via conduits 14 and 15, and the remainder was continuously extracted from conduit 16. From this condensate, a low-boiling component containing methanol, which is a low-boiling reaction product, was obtained.
- High-boiling components including the catalyst component and methylphenyl carbonate were continuously extracted from the bottom 18 via conduits 8 and 19.
- the top of the second continuous multi-stage distillation column 20 consisting of a packed column with a height of 4 m and a diameter of 3 inches packed with stainless steel Dickson packing (diameter of about 6 mm) as the packing material 26
- the first reaction to the position of lm from the bottom of the first reaction distillation column is continuously supplied in a liquid state through a conduit 19 and flows down in the second continuous multistage distillation column to carry out the reaction, and the amount of heat required for distillation Was supplied to the lower part of the tower by heating the liquid in a reboiler 30 via conduits 28 and 29 and circulating through a conduit 31.
- Example 2 4 The same operation as in Example 22 was carried out using the same apparatus as that used in Example 22 except that catalyst B was used instead of catalyst A. Table 5 shows the reaction conditions and the results after the steady state. Example 2 4
- the apparatus shown in FIG. 4 was used.
- the first continuous multi-stage distillation column which is packed with stainless steel Dixon packing (diameter of about 6 min) and has a height of 4 m and a diameter of 3 inches, is filled with lm from the top 17 of the column.
- the mixture consisting of dimethyl carbonate, phenol and catalyst C is continuously supplied to the position in liquid form from the raw material introduction pipe 2 via the conduit 4, the preheater 5, and the conduit 6, and the first continuous multistage distillation
- the reaction was carried out by flowing down the tower.
- the amount of heat required for the reaction and distillation is part of the low-boiling components including dimethyl carbonate newly introduced from the conduit 8 'and dimethyl carbonate recycled from the second continuous multistage distillation column 20, which will be described later.
- a second continuous multi-stage distillation column 20 consisting of a packed column having a height of 4 m and a diameter of 3 inches packed with stainless steel dixon packing (about 6 diameters mentioned) was used as the packing material.
- First continuous from tower top 26 to lm The liquid taken out from the bottom of the multistage distillation column is continuously supplied in the form of a liquid via a conduit 19, and the reaction is carried out by flowing down 20 in the second continuous multistage distillation column.
- the lower liquid was heated in a reboiler 30 via conduits 28 and 29 and fed to the circulation via conduit 31.
- the one used as the aryl carbonate catalyst in the first continuous multistage distillation column ⁇ ⁇ was used as it was without separation. Was done.
- the gas containing dimethyl carbonate continuously distilled from the top 26 was condensed in the condenser 22 via the conduit 21. Part of the condensate was refluxed to the second reactive distillation column 20 via conduits 23 and 24. The remaining condensate was continuously withdrawn from conduits 23 and 25 and circulated through conduits 3 and 4, preheater 5 and conduit 6 to the first continuous multistage distillation column ⁇ . A part of the condensate extracted from the conduit 25 was recirculated from the lower part of the first continuous multistage distillation column 1 ′ through the conduit 7 and the evaporator 10 ′. A high-boiling reaction mixture containing a catalyst and diphenyl carbonate was continuously extracted from the bottom 27 of the second continuous multi-stage distillation column 20 via conduits 28 and 32. Table 5 shows the reaction conditions and the results after the steady state.
- Example 2 5 shows the reaction conditions and the results after the steady state.
- Example 26 Using the same apparatus as used in Example 24, the same operation as in Example 24 was performed, except that ⁇ -cresol was used instead of phenol. Table 5 shows the reaction conditions and the results after the steady state. Example 26.
- Example 24 The same operation as in Example 24 was performed using the same apparatus as used in Example 24, except that getyl carbonate was used instead of dimethyl carbonate.
- Table 5 shows the reaction conditions and the results after the steady state.
- Example 2 9 The same operation as in Example 24 was performed using the same apparatus as that used in Example 24, except that tetrafluoroethoxytitanium was used instead of the catalyst C. Table 5 shows the reaction conditions and the results after the steady state. Example 2 9
- a catalyst was prepared by heating 20 kg of phenol and 4 kg of lead monoxide at 180 ° C for 10 hours, and distilling off the generated water together with the phenol (catalyst E).
- the first continuous multi-stage distillation column consisting of a 10-inch tray with a height of 6 ⁇ and a diameter of 10 inches equipped with a 20-sheet sieve tray was placed 0.5 m from the top 17 of the first continuous multi-stage distillation column.
- the mixture consisting of catalyst E is continuously supplied in liquid form from feed inlet pipe 2 through conduits 4 and 39, preheater 5, and conduit 6, and is reacted by flowing down the first continuous multistage distillation column 1 '.
- the amount of heat required for the reaction and distillation is determined by the newly introduced dimethyl carbonate from conduits 8 'and 9' and the dimethyl carbonate circulated through conduits 24, 25 and 7 from the second continuous multistage distillation column 20 described below.
- a portion of the low-boiling reaction mixture containing the heat was heated in an evaporator (10) and fed through a conduit (11).
- the gas distilled from the top 17 was condensed in the condenser 13 via the conduit 12 and was continuously extracted from the conduit 16.
- a low-boiling reaction mixture containing methanol, a low-boiling reaction product was obtained.
- the reaction liquid continuously withdrawn from the bottom 18 was introduced into the first evaporator 33 via the conduit 19.
- the residual liquid containing the methylphenyl carbonate-forming catalyst is located at the bottom of the evaporator 33.
- the supply of the catalyst E introduced from the conduit 2 was stopped when the recirculated catalyst reached a predetermined concentration.
- the methylphenyl carbonate evaporated from the evaporator 33 is removed.
- the evaporant containing gas is passed through a conduit 40 from an inlet pipe 41 provided 1.5 m from the top 26 from a tower 26.
- a second continuous multi-stage distillation column 20 consisting of Giryl carbonate catalyst
- Catalyst E was continuously supplied in a liquid state to the second continuous multi-stage distillation column 20 through a conduit 51 from an introduction pipe 48 provided 1.5 m from the top of the column. Most of the gaseous methyl phenyl carbonate supplied to the second continuous multi-stage distillation column 20 becomes liquid in the column, and the reaction is performed by flowing down the catalyst and the column. The amount of heat required for the reaction and the distillation was supplied by heating the lower part of the column in a reboiler 30 via conduits 28 and 29 and sending it to a distillation column 20 via a conduit 31. The low-boiling reaction mixture containing dimethyl carbonate, continuously distilled off from the top 26, was condensed in the condenser 22 via the conduit 21.
- the evaporant evaporated from the evaporator 42 is transferred to the conduit. It was continuously withdrawn in liquid form via 52 and condenser 49 and conduit 50. This evaporate contained diphenyl carbonate as a main component.
- the residual liquid containing the diallyl carbonate catalyst was recycled from the bottom of the evaporator 42 to the second continuous multi-stage distillation column 20 via the conduits 43, 47, and 48. When the circulating catalyst reached a predetermined concentration, the supply of the catalyst E introduced from the conduit 51 was stopped. Table 6 shows the flow rate and composition of each part. Table 7 shows the reaction conditions and the results after the steady state.
- ⁇ -alumina manufactured by JGC Corporation, part number N611N
- the cylinder was set in a tubular furnace. After purging with nitrogen, the mixture was heated at 200 ° C. for 5 hours to dry ⁇ -alumina.
- a benzene solution (20 wt%) of tetramethoxysilane was added at 50 m ⁇ / hr.
- the y-alumina was treated by addition at a flow rate for 10 hours.
- the catalyst was prepared by releasing it in a nitrogen atmosphere (catalyst F).
- Each of the first and second continuous multi-stage distillation columns uses a packed column with a diameter of 1.5 inches and a height of 2 m, and those packed with catalyst F are used as the packing materials. Except for the above, the same operation as in Example 24 was performed. Table 5 shows the reaction conditions and the results after the steady state.
- the ratio of the charged liquid amount to the liquid amount remaining in the kettle in Comparative Example 3 is the same as the ratio between the supply amount from the conduit 6 and the column liquid withdrawal amount from the conduit 28 in Example 23.
- 14.0% by weight of diphenyl carbonate was formed in the reaction solution.
- the amount of diphenyl carbonate generated per 1 kg of the reaction solution per 1 hour was 12 g / kg.
- Selection of diphenol carbonate based on phenol was 83%.
- Analysis of the overhead condensate revealed that anisol was by-produced at a selectivity of 8% based on phenol.
- the catalyst concentration was analyzed using ICP (high frequency inductively coupled plasma emission spectrometer).
- the amount of aromatic carbonate produced is expressed in g per 1 hour per lkg of bottom liquid.
- Aromatic carbonate selectivity is based on the aromatic hydroxy compound used as the raw material.
- the catalyst concentration was analyzed using 1 CP (high frequency inductively coupled plasma emission spectrometer).
- the amount of aromatic carbonate produced was expressed in terms of g per hour and per kg of the bottom liquid.
- Aromatic carbonate selectivity is based on the aromatic hydroxy compound used as the raw material.
- the catalyst concentration was analyzed using ICP (high frequency inductively coupled plasma emission spectrometer).
- the amount of gallyl carbonate produced was expressed in g per 1 hour per 1 kg of the bottom liquid.
- the catalyst concentration was analyzed using 1 CP (high frequency inductively coupled plasma emission spectrometer).
- the amount of diaryl carbonate produced was expressed in g per 1 kg of bottom liquid, per hour.
- diaryl carbonate is based on the raw material alkylaryl carbonate.
- the catalyst concentration is expressed as the concentration (wt%) of Pb in the solution measured using ICP (high frequency inductively coupled plasma emission spectrometer)
- the amount of diaryl carbonate produced was expressed in terms of g per hour, and 50 kg of the drawn-out pipe 50 per kg.
- Diaryl carbonate selectivity (%) (Selectivity of first step based on aromatic hydroxy compound (%) X
- the distillation column as shown in Fig. 2 is the first continuous multi-stage distillation column, a mixture consisting of dimethyl carbonate, paracresol, and Pb (OPh) 2 from the inlet 2 via the preheater 5. (46% by weight of dimethyl carbonate, 54% by weight of paracresol, 2 lOmmo 1 / kg of Pb (OPh)) were continuously supplied at 7.0 kg / hr, and the evaporator 10 'and the conduit 11 were simultaneously supplied from the inlet 8'.
- the distillation column as shown in Fig. 1 was used as the second continuous multi-stage distillation column, and the bottom liquid of the first continuous multi-stage distillation column was introduced into the second continuous multi-stage distillation column from inlet 2 to preheater 5 and conduit. It was introduced continuously at 4.8 kg / hr through 6. At the same time, the bottom liquid containing the above ethyl phenyl carbonate was continuously supplied at 5.0 kg / hr from the same inlet 2.
- the bottom temperature of the second continuous multistage distillation column was 200 ° C, and the pressure at the top of the column was 200 Hg.
- the bottom liquid containing methyl carbonate from methyl carbonate and norlacresole was continuously fed at 4.8 kg / hr. This was withdrawn and continuously supplied to the second continuous multi-stage distillation column, and simultaneously, methyl-nyl carbonate was continuously supplied to the second continuous multi-stage distillation column via the conduit 19 at a rate of 1.36 kg / hr.
- the reaction conditions in the second continuous multistage distillation column were the same as in Example 25. From the time of the addition of methyl carbonate, the amount of dimethyl carbonate in the feed introduced from conduit 2 was gradually reduced to 0.38 kg / hr.
- the amount of dimethyl carbonate in the feed from conduit 6 increased by 0.36 kg / hr. This is a reaction in the second continuous multi-stage distillation column, in which transesterification reaction between methyl tolyl carbonate and methyl; ⁇ -nyl carbonate produces dimethyl carbonate as a low-boiling by-product. Increased It is.
- FIG. 1, FIG. 2, FIG. 3, FIG. 4, and FIG. 5 are schematic diagrams showing examples of various processes for implementing the method of the present invention
- FIG. 6 is a schematic diagram of a reactor used in the conventional method shown in Comparative Examples 1, 2, and 3.
- the method of the present invention which is capable of continuously producing aromatic carbonate at a high reaction rate, high selectivity and high yield by using a continuous multi-stage distillation column, has been used as engineering plastics.
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Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
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EP91901641A EP0461274B1 (en) | 1989-12-28 | 1990-12-28 | Process for continuously producing aromatic carbonate |
DE69009992T DE69009992T2 (de) | 1989-12-28 | 1990-12-28 | Kontinuierliches verfahren zur herstellung aromatischer karbonate. |
KR1019910700563A KR940005956B1 (ko) | 1989-12-28 | 1990-12-28 | 방향족 카르보네이트의 연속 제조방법 |
CA002041646A CA2041646C (en) | 1989-12-28 | 1990-12-28 | Process for continuously producing an aromatic carbonate |
SU4895722/04A RU2041869C1 (ru) | 1989-12-28 | 1991-06-03 | Способ получения ароматического карбоната |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
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JP33817989 | 1989-12-28 | ||
JP33818089 | 1989-12-28 | ||
JP1/338179 | 1989-12-28 | ||
JP1/338180 | 1989-12-28 | ||
JP3843690 | 1990-02-21 | ||
JP2/38436 | 1990-02-21 |
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WO1991009832A1 true WO1991009832A1 (fr) | 1991-07-11 |
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PCT/JP1990/001734 WO1991009832A1 (fr) | 1989-12-28 | 1990-12-28 | Procede de production en continu de carbonate aromatique |
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US (1) | US5210268A (ja) |
EP (1) | EP0461274B1 (ja) |
KR (1) | KR940005956B1 (ja) |
AT (1) | ATE107273T1 (ja) |
CA (1) | CA2041646C (ja) |
DE (1) | DE69009992T2 (ja) |
ES (1) | ES2054488T3 (ja) |
RU (1) | RU2041869C1 (ja) |
WO (1) | WO1991009832A1 (ja) |
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WO2006025424A1 (ja) * | 2004-09-02 | 2006-03-09 | Asahi Kasei Chemicals Corporation | 高純度ジフェニルカーボネートの工業的製造法 |
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Publication number | Priority date | Publication date | Assignee | Title |
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GB2255972A (en) * | 1991-04-12 | 1992-11-25 | Davy Res & Dev Ltd | Production of diaryl carbonates. |
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WO2006006568A1 (ja) * | 2004-07-13 | 2006-01-19 | Asahi Kasei Chemicals Corporation | 芳香族カーボネート類を工業的に製造する方法 |
EA010671B1 (ru) * | 2004-07-13 | 2008-10-30 | Асахи Касеи Кемикалз Корпорейшн | Промышленный способ производства ароматического карбоната |
WO2006006566A1 (ja) * | 2004-07-13 | 2006-01-19 | Asahi Kasei Chemicals Corporation | 芳香族カーボネート類の工業的製造法 |
EA010033B1 (ru) * | 2004-07-14 | 2008-06-30 | Асахи Касеи Кемикалз Корпорейшн | Способ промышленного производства ароматического карбоната |
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WO2006006585A1 (ja) * | 2004-07-14 | 2006-01-19 | Asahi Kasei Chemicals Corporation | 芳香族カーボネート類を工業的に製造する方法 |
WO2006006588A1 (ja) * | 2004-07-14 | 2006-01-19 | Asahi Kasei Chemicals Corporation | 芳香族カーボネート類を工業的に製造する方法 |
WO2006022294A1 (ja) * | 2004-08-25 | 2006-03-02 | Asahi Kasei Chemicals Corporation | 高純度ジフェニルカーボネートの工業的製造方法 |
EA010066B1 (ru) * | 2004-08-25 | 2008-06-30 | Асахи Касеи Кемикалз Корпорейшн | Способ производства высокочистого дифенилкарбоната в промышленном масштабе |
WO2006025424A1 (ja) * | 2004-09-02 | 2006-03-09 | Asahi Kasei Chemicals Corporation | 高純度ジフェニルカーボネートの工業的製造法 |
WO2006025478A1 (ja) * | 2004-09-03 | 2006-03-09 | Asahi Kasei Chemicals Corporation | 高純度ジアリールカーボネートの工業的製造方法 |
EA012179B1 (ru) * | 2004-09-03 | 2009-08-28 | Асахи Касеи Кемикалз Корпорейшн | Промышленный способ получения высокочистого диарилкарбоната, высокочистый дифенилкарбонат и установка для получения высокочистого диарилкарбоната |
WO2006067982A1 (ja) * | 2004-12-24 | 2006-06-29 | Asahi Kasei Chemicals Corporation | 芳香族カーボネートの製造方法 |
KR100863662B1 (ko) * | 2004-12-24 | 2008-10-15 | 아사히 가세이 케미칼즈 가부시키가이샤 | 방향족 카르보네이트의 제조 방법 |
US8138367B2 (en) | 2004-12-24 | 2012-03-20 | Asahi Kasei Chemicals Corporation | Process for production of aromatic carbonate |
Also Published As
Publication number | Publication date |
---|---|
KR920701115A (ko) | 1992-08-11 |
DE69009992D1 (de) | 1994-07-21 |
EP0461274A1 (en) | 1991-12-18 |
ES2054488T3 (es) | 1994-08-01 |
EP0461274A4 (en) | 1992-06-03 |
CA2041646A1 (en) | 1991-06-29 |
US5210268A (en) | 1993-05-11 |
KR940005956B1 (ko) | 1994-06-25 |
CA2041646C (en) | 1999-06-15 |
EP0461274B1 (en) | 1994-06-15 |
ATE107273T1 (de) | 1994-07-15 |
DE69009992T2 (de) | 1995-01-12 |
RU2041869C1 (ru) | 1995-08-20 |
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