WO1997044108A1 - Appareil de distillation par reaction et procede de distillation par reaction - Google Patents
Appareil de distillation par reaction et procede de distillation par reaction Download PDFInfo
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- WO1997044108A1 WO1997044108A1 PCT/JP1997/001685 JP9701685W WO9744108A1 WO 1997044108 A1 WO1997044108 A1 WO 1997044108A1 JP 9701685 W JP9701685 W JP 9701685W WO 9744108 A1 WO9744108 A1 WO 9744108A1
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- reaction
- raw material
- reactive distillation
- equilibrium reaction
- boiling point
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Classifications
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/03—Preparation of carboxylic acid esters by reacting an ester group with a hydroxy group
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00247—Reflux columns
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00539—Pressure
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
- B01J2208/00557—Flow controlling the residence time inside the reactor vessel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Definitions
- the present invention relates to a reactive distillation apparatus and a reactive distillation method that can be applied to a relatively complicated reaction obtained by combining two or more equilibrium reactions.
- the above conventional reactive distillation column is applied only to a relatively simple reaction, and is not applied to a relatively complicated reaction in which an equilibrium reaction is combined in two or more stages. In other words, little is known about a reactive distillation column applicable to a sequential complex reaction. Therefore, there is a need for a reactive distillation apparatus and a reactive distillation method that can be applied to relatively complicated reactions in which equilibrium reactions are combined in two or more stages.
- the present invention has been made in view of the above-mentioned conventional problems, and has as its object to provide a reactive distillation apparatus that can be applied to a relatively complicated reaction in which an equilibrium reaction is combined in two or more steps;
- An object of the present invention is to provide a reactive distillation method capable of efficiently performing a reaction. Disclosure of the invention
- the present inventors have diligently studied a reactive distillation apparatus and a reactive distillation method in order to solve the above conventional problems.
- the first supply unit, the second supply unit, and the third supply unit use the reactive distillation apparatus fi, which is provided in different stages in order from the top of the column, to perform two types of equilibrium reactions.
- the raw material with the higher boiling point first raw material
- second raw material second raw material
- a third raw material for performing a second equilibrium reaction with a product having a boiling point from the first and second raw materials from the first and second raw materials is supplied from a third supply unit, and the product and the third raw material are supplied.
- the present inventors have found that a relatively complicated reaction comprising a combination of two or more equilibrium reactions can be efficiently performed by performing the second equilibrium reaction with .
- the reactive distillation apparatus of the present invention is a reactive distillation apparatus having three or more stages for performing a reaction having two or more equilibrium reactions.
- a first supply unit that supplies a raw material with a higher boiling point (first raw material) and a second supply unit that supplies a raw material with a lower boiling point (second raw material)
- a second supply unit and a third supply for supplying a third raw material for performing the second equilibrium reaction with a product having a higher boiling point than the first and second raw materials among the products generated by the first equilibrium reaction.
- at least a first part, and the first supply part, the second supply part, and the third supply part are provided in different stages in order from the top of the tower.
- the reactive distillation apparatus of the present invention may further include a stage provided with no supply unit between the two stages provided with the supply unit.
- the first supply section, the second supply section, and the third supply section to which different raw materials are supplied are provided in different stages in order from the top of the tower. .
- a reactive distillation apparatus 11 that can be applied to a relatively complicated reaction in which two or more equilibrium reactions are combined, that is, a sequential complex reaction.
- the reactive distillation method of the present invention is a reactive distillation method in which a reaction having two or more equilibrium reactions is performed using a reactive distillation apparatus having three or more stages.
- the raw material with the higher boiling point first raw material
- second raw material second raw material
- the third raw material that causes the second equilibrium reaction with the product having a high level of water is supplied to the third stage below the second stage, and the second equilibrium between the product and the third raw material is obtained. And carrying out a reaction.
- a product having a lower boiling point may be a raw material of the first equilibrium reaction.
- the two kinds of raw materials are subjected to the first equilibrium reaction, and among the products generated by the first equilibrium reaction, the product having a higher boiling point and the third raw material are separated. Allow two equilibrium reactions to take place.
- This can provide a relatively complicated reaction in which the equilibrium reaction is combined in two or more steps, that is, a reactive distillation method applicable to a sequential complex reaction.
- the reactive distillation method of the present invention further comprises the step of: R 1 C 00 R 2 ' ⁇ ' ⁇ '(1)
- R 1 and R 2 each independently represent an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group); and a compound represented by the general formula (2)
- R 3 represents an aromatic group which may have an S-substituent
- R 3 is an ester exchange reaction with an aromatic hydroxy compound represented by the formula:
- R 1 represents an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group, and R 3 represents an aromatic group which may have a protecting group.
- R 4 and R 5 each independently represent an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group).
- R 3 represents an aromatic group which may have a substituent, and represents a substituent selected from the group consisting of R 3 , R 4 and R 5 ). Can be manufactured efficiently.
- the obtained carbonate ester is an industrially useful compound.
- carbon dioxide a kind of carbonic acid ester, is used as a raw material for polycarbonate.
- FIG. 1 is a block diagram showing a schematic configuration of a reactive distillation apparatus according to one embodiment of the present invention.
- the reactive distillation apparatus and the reactive distillation method according to the present invention can also provide a complicated sequential complex reaction in which equilibrium reactions are combined in three or more stages.
- the equilibrium reaction will be described for convenience of explanation.
- An example is a sequential complex reaction in which two steps are combined. That is, using the raw material (A), the raw material (B) and the raw material (E),
- the order of the boiling points of the raw material (A) as the first raw material, the raw material (B), and the raw material (E) as the third raw material is as follows: raw material (A)> raw material (B)> raw material (E ), And the order of the boiling points of the product (C) and the product (D) is as follows: product (C)> product (D), and the boiling points of the product (F) and the product (G) Is assumed to be product (F)> product (G).
- the first equilibrium reaction is referred to as a first-stage reaction
- the second equilibrium reaction is referred to as a second-stage reaction.
- a reactive distillation apparatus (hereinafter, simply referred to as a reactive distillation column) 1 according to the present invention includes a reboiler 1, a condenser 3, a bomb 4, and the like.
- the reactive distillation column 1 has three or more stages.
- the raw material (A) and the raw material (B) are brought into gas-liquid contact with the product (C) and the raw material (E) with gas-liquid contact.
- Reactive distillation column 1 [This is connected to the raw material supply pipe 5 ⁇ 6 ⁇ 7.
- the bottom of the reactive distillation column 1 is connected to the reboiler 2 via an extraction pipe 8 and a conduit 14.
- the top of the reactive distillation column 1 is connected to a condenser 3 via a conduit 12.
- the raw material supply pipes 5, 6, 7 are provided in different stages in order from the top of the reactive distillation column 1. That is, in the reactive distillation column 1, the raw material supply pipe 6 is connected to a lower stage than the raw material supply pipe 5, and the raw material supply pipe 7 is connected to a lower stage than the raw material supply pipe 6.
- the reactive distillation column 1 is provided between a stage to which the raw material supply pipe 5 is connected (first stage) and a stage to which the raw material supply tube 6 is connected (second stage), Between the stage to which the supply pipe 6 is connected and the stage to which the raw material supply pipe 7 is connected (third stage), there may be a stage to which the raw material supply pipe is not connected. More preferred. Further, the raw material supply pipe 7 may be connected to the tower bottom.
- the raw material supply pipe 5 as the first supply unit continuously supplies the raw material (A) to the reactive distillation column 1.
- a raw material supply pipe 6 as a second supply unit continuously supplies the raw material (B) to the reactive distillation column 1.
- a raw material supply pipe 7 as a third supply section continuously supplies the raw material (E) to the reactive distillation column 1.
- the reboiler 2 is connected to the reactive distillation column 1 via the extraction pipe 8 and the conduit 14. T / JP97 / 01685
- the reboiler 2 heats the bottom liquid extracted through the extraction pipe 8 and returns the liquid to the bottom through the conduit 14. That is, the reboiler 2 heats and circulates the bottom liquid. Then, the withdrawal pipe 8 is performing a division technique, so that a part of the bottom liquid can be continuously withdrawn as a bottom liquid outside the reaction system.
- the condenser 3 condenses and liquefies the distillate from the reactive distillation column 1.
- the condenser 3 is connected to the top of the reactive distillation column 1 via a conduit 12, and is connected to the pump 4 via a discharge pipe 9. Further, the condenser 3 is provided with an adjusting pipe 10 provided with a pressure adjusting valve 11. Then, the extraction pipe 9 performs a divisional operation, so that a part of the distillate can be continuously extracted out of the reaction system.
- the pump 4 refluxes the distillate to the reactive distillation column 1 at a predetermined reflux ratio.
- the bomb 4 is connected to the condenser 3 via an extraction pipe 9, and is connected to the top of the reactive distillation column 1 via a conduit 13.
- the raw material (A) is fed through the raw material supply pipe 5, the raw material (B) is fed through the raw material supply pipe 6, and the raw material (E) is fed through the raw material supply pipe 7 to the reactive distillation column 1.
- These raw materials (A), (B), and (E) may be supplied in liquid form, may be supplied in gaseous form, or may be painted in a gas-liquid mixed state.
- the raw material (A) may include a part of the raw material (B), and the raw material (B) may include a part of the raw material (A).
- the raw material (A) and the raw material (B) supplied to the reactive distillation column 1 are subjected to gas-liquid contact, that is, reactive distillation.
- the first-stage reaction proceeds, A product (C) and a product (D) are formed, and both are separated.
- the product (C) flows down in the reactive distillation column 1.
- the product (D) which is a by-product, is continuously extracted as a distillate.
- the product (C) and the raw material (E) are subjected to gas-liquid contact, that is, reactive distillation.
- gas-liquid contact that is, reactive distillation.
- the latter-stage reaction proceeds, and a product (F) and a product (G) are generated and both are separated.
- the by-product (G) rises in the reactive distillation column 1 and is continuously extracted as a distillate.
- the product (G) is the raw material of the first-stage reaction, that is, when the product (G) and the raw material (B) are the same compound, the product (G) is To be served.
- the target product (F) is continuously extracted from the reaction distillation column 1 as a bottom liquid (bottom liquid) outside the reaction system. That is, the product (F) is continuously taken out of the reaction system as a bottom liquid.
- the product (F) By performing the above reaction operations, the product (F) can be efficiently and continuously produced.
- the types of compounds existing in the reactive distillation column 1 are reduced, and the reaction system is simplified.
- the supply amount of the raw material (B) supplied through the raw material supply pipe 6 can be reduced, the above-described sequential complex reaction can be performed more efficiently.
- the catalyst is continuously supplied to the reactive distillation column 1 together with the raw materials (A) and Z or the raw material (B).
- the catalyst may be separated and recovered from the product (F) by using a known method such as distillation.
- the catalyst is held inside the reactive distillation column 1.
- a heterogeneous catalyst may be charged instead of a part or all of the charged material in the reactive distillation column 1. Wear.
- a tray column (to be described later) is used as the reactive distillation column 1, the unevenness—the catalyst may be held in a plate or a downcomer.
- the catalyst used in the first-stage reaction and the catalyst used in the second-stage reaction may be the same as each other, or may be different from each other.
- a solvent supply tube (not shown) may be separately provided in the reactive distillation column 1, and the solvent may be continuously supplied through the solvent supply tube.
- the reactive distillation column 1 has a structure in which a gas phase is present in the reactive distillation column 1 and the generated low-boiling components can be continuously separated and removed from the gas phase, ie, so-called Any structure that can carry out reactive distillation may be used.
- a distillation column having three or more stages excluding the top (top) and the bottom (bottom) is preferable.
- Such distillation towers were filled with, for example, Raschig ring, ball ring, Inox rock saddle, Dixonno, 'packing, McMahon packing, sludge packing, etc.
- Packing tower A commonly used distillation tower such as a tray tower using a tray such as an bubble bell tray, a sieve tray, or a valve tray can be used.
- a combined distillation column having both a tray and a packed bed can also be employed.
- the number of plates mentioned above indicates the number of plates in a tray column, and indicates the number of theoretical plates in a packed column.
- the reactive distillation apparatus is not limited to the configuration shown in FIG. .
- the reactive distillation apparatus and the reactive distillation method according to the present invention are not only applied to the sequential complex reaction in which the equilibrium reactions are combined in two stages, but the complex sequential reaction in which the equilibrium reactions are combined in three or more stages. It can also be used for complex reactions. In this case, the same number of raw material supply pipes as the types of raw materials may be provided in the reactive distillation column.
- the reactive distillation apparatus and the reactive distillation method according to the present invention will be described in more detail below by giving specific examples.
- the first-stage reaction is represented by the general formula (1)
- R 1 and R 2 each independently represent an alkyl group, an alicyclic hydrocarbon group or an alkyl group), and a single-arm type (2)
- R 3 represents an aromatic group which may have a substituent
- R 3 is a transesterification reaction with an aromatic hydroxy compound represented by the formula:
- R 1 represents an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group, and R 3 represents an aromatic group which may have a substituent).
- R 4 and R 5 each independently represent an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group). It shall be. Therefore, one of the carboxylic acid ester represented by the one-branch type (1) and the aromatic hydroquine compound represented by the general formula (2) corresponds to the raw material (A), and the other corresponds to the raw material (A). (B). Further, the carboxylate represented by the one-branch type (3) corresponds to the product (C), and the carbonate represented by the general formula (4) corresponds to the raw material (E).
- R 3 represents an aromatic group which may have a substituent
- R s represents a substituent selected from the group consisting of R 3 , R 4 and RS.
- Esters are formed. Therefore, the carbonate represented by the single branch (5) corresponds to the product (F).
- carbonates (5) which are the target substances
- R 6 is represented as necessary.
- the carbonic acid ester (5) in which the substituted annulable group is S-substituent R 4 or the substituent RS is called a carbonic acid monoester
- the latter reaction proceeds in two stages: a reaction in which a carbonate monoester is formed and a reaction in which a ester carbonate is formed. That is, first, one of the substituents R 4 and R 5 of the carbonate represented by the general formula (4) (hereinafter referred to as carbonate (4)) is represented by the general formula (3).
- the ester is transesterified with a substituent R 3 of a carboxylic acid ester (hereinafter referred to as a carboxylic acid ester (3)).
- a monoester of carbonic acid is formed, and a single-branch type (6)
- R ′ represents an alkyl group, an alicyclic hydrocarbon group or an arylalkyl group, and R 7 represents a substituent selected from the group consisting of R 4 and R s ).
- Acid esters hereinafter referred to as carboxylic acid esters (6) are by-produced.
- the remaining S-substituent R 4 (R 5 ) of the carbonate monoester is transesterified with the substituent R 3 of the carboxylate (3).
- a carbonic acid diester is generated, and a carboxylic acid ester (6) is by-produced.
- the carboxylate (6) corresponds to the product (G).
- the carboxylic acid ester represented by the general formula (1) (hereinafter, referred to as carboxylic acid ester (1)) is not particularly limited, but the substituent represented by R 1 or R 2 is not particularly limited.
- R 1 or R 2 is not particularly limited.
- the alkyl group preferably has 1 to 10 carbon atoms
- the alicyclic hydrocarbon group preferably has 3 to 10 carbon atoms
- the arylalkyl group preferably has 7 to 10 carbon atoms.
- carboxylate (1) examples include, for example, methyl acetate, ethyl acetate, propyl acetate, butyl acetate, cyclohexyl acetate, benzyl acetate, benzyl acetate, 12-ethylhexyl acetate, and propion.
- Methyl ester ethyl propionate, propyl propionate, butyl propionate, methyl butyrate, ethyl butyrate, propyl butyrate, methyl isobutyrate, ethyl ethyl isobutyrate, propyl isoformate, methyl valerate, Ethyl valerate, propyl valerate, methyl isovalerate, ethyl ethyl valerate, propyl isovalerate, methyl hexate, ethyl hexate, propyl hexate, methyl heptanoate Ethyl propionate and the like.
- the carboxylate (6) is preferably reusable as the carboxylate (1). Therefore, it is preferable that the substituent R 2 of the carboxylic acid ester (1) and the substituents R 4 and R 5 of the carbonate (4) are the same as each other.
- the carboxylic acid ester (6) can be easily separated and recovered.
- the carboxylic acid ester (1) is not substantially consumed.
- R 2 represents an alkyl group, an alicyclic hydrocarbon group or an alkyl group
- R 2 represents an alkyl group, an alicyclic hydrocarbon group or an alkyl group
- the carboxylic acid ester (1) having a boiling point higher than that of the by-produced alcohol is more preferable among the above exemplified compounds.
- the alcohol represented by the general formula (7) corresponds to the product (D).
- a carboxylic acid ester (1) which does not form an azeotropic composition with an alcohol represented by the general formula (7) (hereinafter simply referred to as an alcohol) is required. It is preferable to use.
- Carboxylic esters that do not form azeotropic compositions (1) include ethyl butyrate, butyl butyrate, and isovalerate and valerate esters. Compounds having 4 or more carbon atoms on the side of the acyl group such as xanates (or compounds having 3 or more prime numbers of the S-substituent group R 1 ) are mentioned.
- the aromatic hydroxy compound represented by the general formula (2) is not particularly limited, but is a compound in which the substituent represented by R 3 is an aromatic group.
- the above aromatic group may have a substituent.
- aromatic hydroxy compound examples include, for example, phenol, 0 — creso-nore, m-tarreteil, p — cresol, 0 — cro-mouth phenol, m-chloro Mouth phenol, p—clo phenol, 0—ethyl phenol, m—ethyl phenol, p—ethyl phenol, 0—isop bil phenol, m—isopropy crizol, p—isoprobiphenol, 0—methoxyphenol, m—methoxyphenol, p-methoxyphenol, xylenols, Hiichi Naphthol, -naphthol and the like.
- aromatic hydroquine compounds may be appropriately mixed and used.
- phenol is preferred from the industrial viewpoint.
- a carboxylic acid ester (1) having a boiling point lower than that of the carboxylic acid ester (3) it is preferable to use.
- Examples of such a combination of the carboxylic acid ester (1) and the aromatic hydroxy compound include a combination other than the combination of mono-ethylhexyl acetate and phenol, and the combination of benzyl benzoate and phenol. .
- an acetic acid ester in which the alcohol has 7 or less carbon atoms or a propionate in which the alcohol has 8 or less carbon atoms is used as the carboxylic acid ester (1), All combinations with aromatic hydroxy compounds are possible.
- the above-mentioned carboxylate (1) and carboxylate (3) may be azeotropic.
- carboxylic acid ester (3) obtained by the above-mentioned first-stage reaction include, for example, phenyl nitrate, each isomer of methyl acetate, each isomer of ethyl phenyl acetate, Each isomer of mouth phenol, each isomer of isopropyl phenyl acetate, each isomer of methoxyphenyl acetate, each isomer of dimethyl phenyl acetate, each isomer of naphthyl acetate, and each isomer of naphthyl acetate Each isomer of urel, phenyl butyrate, phenyl oxobutyrate, phenyl valerate, each isomer of methyl valerate, phenyl isovalerate, phenyl hexanoate, Phenyl heptanoate and the like.
- the carbonate ester (4) is not particularly limited.
- the substituents represented by R 4 and RS each independently represent an alkyl group, an alicyclic hydride group or an arylalkyl group. It is a compound composed of a group.
- the alkyl group preferably has 1 to 10 carbon atoms
- the alicyclic hydrocarbon group preferably has 3 to 10 carbon atoms
- the arylalkyl group has 1 to 10 carbon atoms. ⁇ 10 is preferred.
- the carbonate ester (4) include, for example, dimethyl carbonate, getyl carbonate, di-n-propyl carbonate, diisopropyl carbonate, each isomer of dibutyl carbonate, each isomer of dipentyl carbonate, and dicarbonate.
- These carbonates (4) may be appropriately mixed and used.
- dimethyl carbonate is preferred from the industrial viewpoint.
- the boiling point of the compound exemplified above is higher than the boiling point of the carboxylic acid ester (6).
- Carboxylic acid esters (3) are more preferred. Examples of such a combination of the carboxylate (3) and the carbonate (4) include, when the substituent R 3 of the carboxylate (3) is a phenyl group, the substituent R of the carbonate (4) 4 ⁇ When R 5 is linear, it has 7 or less carbon atoms.
- a carboxylic acid ester (3) having a boiling point lower than that of the carbonate (5) In order to continuously extract the produced carbonate (5) out of the reaction system, it is preferable to use a carboxylic acid ester (3) having a boiling point lower than that of the carbonate (5).
- a carboxylate (3) for example, a compound having 7 or less carbon atoms when the S-substituent R 1 is linear.
- the difference in boiling point between the carboxylic acid ester (3) and the carbonate (5) should be relatively large so that the generated carbonate (5) and the carboxylic acid ester (3) can be easily separated. Is preferred.
- the difference in boiling point between the carboxylic ester (3) and the carboxylic ester (4) is relatively small. It is preferable that the boiling point difference between the acid ester (3) and the carboxylic acid ester (6) is relatively large. 1 5
- the equilibrium of the transesterification reaction advantageously to the product system side reaction efficiency
- the carboxylic acid ester (6) When the carboxylic acid ester (6) is distilled off, it is preferable that the carboxylic acid ester (6) and the carboxylic acid ester (3) are sufficiently separated. However, when the carboxylate (6) and the carboxylate (1) are the same compound, it is not necessary to extract the carboxylate (6) out of the reaction system.
- the carboxylic acid ester (1) and the aromatic hydroxy compound are transesterified in the presence of a catalyst (first-stage reaction). Further, the carboxylate (3) and the carbonate (4) are transesterified in the presence of a catalyst (second reaction).
- the catalyst used in the first-stage reaction and the catalyst used in the second-stage reaction may be the same as each other, or may be different from each other.
- Examples of the above catalyst include mineral acids such as sulfuric acid; Rufonic acids: solid acids such as ion-exchange resins and zeolite; bases such as sodium hydroxide; metal alkoxides such as titanate trisopropoxide and zirconium (IV) isobrobox; aluminum chloride and titanium tetrachloride Lewis acids and compounds that generate Lewis acids, etc .; Metal phenoxides such as phenoxy lead, pentoxy titanium, etc .: Lead oxides; Lead salts such as lead carbonate; Zirconium ([V) cetylacetone) Metal, acetyl acetonate Metal acetyl acetonate complex such as copper (I [), zinc (II) acetyl acetate, lithium acetyl acetonate: organic tin compound such as dibutyltin oxide Titano silicate, metal-substituted aluminum phosphate, and the like.
- mineral acids such as sulfuric acid
- Rufonic acids solid acids
- ordinary protonic acid, protonic base, solid acid, and solid base can also be used as a catalyst.
- metal alkoxides; Lewis acids and compounds generating Lewis acids metal phenoxides; organotin compounds; titanium silicates; I like it.
- a mixed solution of the catalyst is supplied to one part of the reactive distillation column.
- the catalyst can be supplied by mixing at least one of the carboxylic acid ester (1), the aromatic hydroxy compound and the carbonate (4).
- the mixed solution of the catalyst may be supplied to the supply stage of the carboxylic acid ester (1), the aromatic hydroquine compound or the carbonate ester (4), or may be supplied to a stage different from the supply stage. .
- the reactive distillation column 1 as the area (stage) where the catalyst is present is larger, the frequency of contact between the reaction solution and the catalyst is increased, and the reaction efficiency is improved. For this reason, it is preferable that the catalyst be supplied to the upper stage of the reactive distillation column 1 as much as possible.
- the lower limit is 0.1 ppm, preferably 1 ppm, and more preferably 1 ppm.
- the upper limit is the amount that is dissolved in the reaction solution inside the reactive distillation column 1 in a saturated state, and is about 10% by weight, preferably 5% by weight, and more preferably 1% by weight.
- the lower limit of the amount of the catalyst is 0.1% by weight, preferably 0.5% by weight, more preferably 0.5% by weight, based on the total amount of the carboxylate (1) and the aromatic hydroxy compound. Preferably, it is 1% by weight.
- the upper limit is 40% by weight, preferably 30% by weight, and more preferably 20% by weight.
- the method of supplying the raw materials to the reactive distillation column 1 is not particularly limited.
- the carboxylate (1), the aromatic hydroxy compound, and the carbonate (4) may be supplied in a liquid form, in a gaseous form, or in a gas-liquid mixed state. May also be supplied.
- the carboxylate (1) may contain a part of the aromatic sigma-oxy compound, and the aromatic hydroxyquine compound may contain a part of the carboxylate (1). May be included.
- the molar ratio between the carboxylic acid ester (1) and the aromatic hydroxy ⁇ -oxy compound in the first-stage reaction depends on the type and amount of the catalyst used, the reaction conditions, and the like. A range of 0: 1 is preferred, a range of 1:20 to 20: 1 is more preferred, and a range of 1: 5 to 5: 1 is even more preferred.
- the first-stage reaction is an equilibrium reaction that is extremely biased toward the original system. Therefore, by using one of the carboxylic acid ester (1) and the aromatic hydroxy compound in a large excess, the reaction efficiency (equilibrium conversion) of the other is reduced. Can be enhanced. However, when the molar ratio of the two is out of the above range, the carboxylic acid ester (1) or the aromatic hydroxy compound used in a large excess must be recovered and recycled. This is industrially disadvantageous and not preferred.
- the molar ratio of the carboxylic acid ester (3) to the carbonate ester (4) in the latter reaction depends on the type and amount of the catalyst used, the reaction conditions, and the like, but ranges from 1:50 to 50: 1. Is preferable, the range of 1:20 to 20: 1 is more preferable, and the range of 1: 5 to 5: 1 is even more preferable.
- the reaction efficiency equilibrium conversion
- the carboxylate (3) or carbonate (4) used in a large excess must be recovered and recycled. For this reason, it is industrially disadvantageous and unfavorable.
- the reaction system may contain a carboxylic acid ester (1), an aromatic hydroxy compound, or the like, which is an unreacted product in the first-stage reaction.
- a carboxylic acid ester (1) an aromatic hydroxy compound, or the like, which is an unreacted product in the first-stage reaction.
- the content of the carboxylate (3) in the total amount of the carboxylate (3), the carboxylate (1) and the aromatic hydroxy compound is required. Is preferably at least 10 mol%, more preferably at least 20 mol%, and even more preferably at least 30 mol%.
- Factors that determine the operating conditions when operating the above reactive distillation column 1 include, for example, the number of stages, operating temperature (reaction temperature), operating pressure, liquid residence time, reflux ratio, and liquid hold-up. And the like. That is, in the first equilibrium reaction, a product having a higher boiling point than each of the first and second raw materials among the respective products generated by the first equilibrium reaction is converted from the first and second raw materials. It is adjusted to a temperature and pressure that can be separated by the difference of each boiling point.
- the first equilibrium reaction among the products produced by the first equilibrium reaction, products having a lower boiling point than the first and second raw materials are separated and removed according to the difference in each boiling point. Thus, the temperature and pressure are adjusted so as to promote the first equilibrium reaction.
- the more specific operation temperature depends on the type of the carboxylic acid ester (1), the aromatic hydroxy compound and the carboxylic acid ester (4), the type and amount of the catalyst, and other conditions (factors).
- the lower limit temperature is 100 ° C., preferably 140 ° C., more preferably 160 ° C.
- the upper limit temperature is 350 ° C., preferably 300 ° C.
- the operating temperature is lower than 100 ° C., the catalytic activity becomes lower, so that the reaction time becomes longer and the productivity is lowered, which is not preferable. If the operating temperature is higher than 350, the dehydration reaction or decarboxylation reaction This is not preferred because side reactions such as the production of ethers (diaryl ethers, alkyl aryl ethers, etc.) are likely to occur. Further, the pressure inside the reactive distillation column 1 is too high, which is not preferable.
- the more specific operating pressure may be any of depressurizing pressure, normal pressure, and pressurizing.
- the type of carboxylate (1), aromatic hydroxy compound and carbonate (4), and the type of catalyst The lower limit is 100 mmHg, preferably 500 mmHg, more preferably 760 mmHg (normal pressure), depending on the type, amount, and other conditions (factors). Yes, and the upper limit is 100 kg no c in 2 , preferably 50 kg g cm 2 , more preferably 10 kg g cm 2 .
- the amount of hall tongue divided by the number of stages is closely related to the reaction time, that is, the residence time.
- the residence time In other words, to increase the equilibrium conversion, it is necessary to lengthen the residence time to some extent, and to increase the residence time, it is necessary to increase the hold-up amount or increase the number of stages . Of these, it is preferable to increase the hold-up amount, but if it is increased to a certain degree or more, flooding occurs.
- the hold-up amount with respect to the empty column volume (volume) of the reactive distillation column 1 is preferably in the range of 0.05 to 0.75 by volume ratio, and in the range of 0.01 to 0.5. Inside is more preferred.
- the number of plates is preferably from 5 to 100, taking into account the cost and height limitation of the reactive distillation column 1, utility costs, fixed costs, and the like. .
- the difference in boiling point between the carboxylic acid ester (1) and the alcohol in the first-stage reaction is relatively small, and in the second-stage reaction, the carboxylic acid ester (3) and the monoester or carboxylic acid carbonate are used.
- the boiling point difference from the ester (6) is relatively small, the efficiency of gas-liquid separation is improved.
- the far flow ratio is preferably in the range of 0 to 100, more preferably in the range of 0 to 50, and even more preferably in the range of 0 to 25.
- the reflux ratio is preferably 0 or a relatively small value.
- the reflux ratio is preferably set to a relatively large value in consideration of utilities and fixed costs.
- heterogeneous catalyst In the case of using a heterogeneous catalyst, there is no need to separate the catalyst if the catalyst is kept in a reactive distillation column. By using a known method, the heterogeneous catalyst can be easily removed and recovered from the reaction solution.
- the homogeneous catalyst when a homogeneous catalyst is used, the homogeneous catalyst can be easily separated and recovered from the reaction solution by using a known method such as distillation after completion of the reaction.
- the catalyst is separated by the above-mentioned method, and then the known method such as distillation, extraction, and recrystallization is used to obtain the carbonate ester (5), that is, the desired carbonic acid. Diesters can be easily singulated.
- carboxylic acid ester (6) or carbonate monoester, or carbonate (4) as by-product, or aromatic or hydroxy compound as unreacted material can be easily separated and recovered. be able to.
- a solvent may be added to the reaction system, that is, the reaction solution, if necessary.
- the solvent to be added include compounds inert to the above reaction system, for example, ethers, aliphatic hydrocarbons, aromatic hydrocarbons, halogenated hydrocarbons, and the like.
- an azeotropic composition having an azeotropic point lower than the azeotropic point of the azeotropic composition is formed with the alcohol.
- a solvent coexist in the reaction system.
- suitable solvents include compounds such as benzene-cyclohexane.
- the solvent forms an azeotropic composition having a relatively low azeotropic point with methanol. For this reason, the azeotrope of the carboxylic acid ester (1) and methanol is suppressed, so that separation of both can be facilitated and the equilibrium conversion can be improved. Even when the carboxylic acid ester (1) and the alcohol do not form an azeotropic composition, an azeotropic composition having a low azeotropic point is mixed with the alcohol in order to further facilitate the separation of the two.
- the solvent formed in the reaction may be allowed to coexist in the reaction system.
- an inert gas such as nitrogen gas
- an inert gas can be introduced into the reaction system from the lower part of the reactive distillation column 1.
- the aromatic hydroxy compound is fed to the reactive distillation column 1 via the raw material supply pipe 5, the carboxylic acid ester (1) via the raw material supply pipe 6, and the carbonate ester (4) via the raw material supply pipe 7. Each is supplied continuously.
- the carboxylate (3) and the carbonate (4) are brought into gas-liquid contact, that is, reactive distillation.
- the latter-stage reaction proceeds, and ester carbonate (5) and carboxylic acid ester (6) are formed, and both are separated.
- the carboxylic acid ester (6) as a by-product rises in the reactive distillation column 1 and is continuously extracted as a distillate.
- the carboxylic acid ester (6) and the carboxylic acid ester (1) are the same compound, the carboxylic acid ester (6) is subjected to the above-mentioned first-stage reaction.
- the desired carbonic acid ester (5) is continuously extracted from the reaction distillation column 1 as a bottom liquid (bottom liquid) outside the reaction system. That is, the carbonate ester (5) is continuously taken out of the reaction system as a bottom liquid.
- Example 1 Using the reactive distillation apparatus S shown in Fig. 1, a sequential complex reaction in which the equilibrium reaction was combined in two steps was performed.
- a stainless steel distillation column was connected to a stainless steel plate column, and a column was used.
- the tray tower mentioned above has an inner diameter of 20 mm and has 60 stages. Then, the raw material supply pipe 5 is connected to the uppermost stage (the 60th stage), that is, to the top of the tower, and the raw material supply tube 6 is connected to the 20th stage, and the lowermost stage (the first stage) is connected.
- the raw material supply pipe 7 was connected to the bottom, that is, to the bottom of the tower.
- the tray column is the reaction section.
- the above distillation column had a height of lm, an inner diameter of 20 mni, and was filled with 1.5 mm 0 stainless steel disc packing. Therefore, the distillation tower is the enrichment section.
- the heat required for distillation was supplied by heating the bottom of the tray column with a heater.
- the operating conditions for the reactive distillation column 1 were as follows: the bottom temperature was 240, and the top pressure was 3.4 kg / cm 2 (gauge pressure).
- the reflux operation was not performed, a part of the distillate was condensed inside the distillation column due to heat release, and a slight internal reflux occurred.
- phenol as the raw material (A) and titanate enantioxide “T i (0 Ph) 4 J as a raw material (A) are fed into the reactive distillation column 1 via a raw material supply pipe 5.
- the amount of the raw material liquid supplied per hour was 60 g.
- the raw material (B) was supplied to the reactive distillation column via the raw material supply pipe 6.
- Methyl valerate was continuously supplied in gaseous form as part of the reaction.
- the amount of methyl valerate supplied per hour was set at 128 g.
- the amount of titanium added to the total amount of methyl valerate and phenol) was adjusted so as to be SOO ppm.
- Methyl was continuously supplied in gaseous form.
- the amount of dimethyl carbonate supplied per hour was set to 18.6 g.
- the composition was as follows: phenyl valerate 25.6%, methyl phenyl carbonate 17.3%, diphenyl carbonate 14.0%, dimethyl carbonate 4.5% The content was 12.3% of methyl valerate and 26.2% of phenol. The conversion of phenol was 59.6%, and the conversion of dimethyl carbonate was 75.5%.
- Example 2 Using the same reactive distillation apparatus as that of Example 1, the supply amount of methyl valerate in Example 1 per hour was reduced from 128 g to 124 g. 2 ⁇
- the withdrawal amount of the bottoms per hour was 96 g.
- the amount of the distillate withdrawn per hour was 11 Ig.
- the composition was as follows: phenyl valerate 21.5%, methylphenyl carbonate 20.4%, diphenyl carbonate 14.4%, dimethyl carbonate 6.7% And methyl valerate 12.4% and phenol 24.7%.
- the conversion of phenol was 60.0%, and the conversion of dimethyl carbonate was 71.5%.
- Example 1 Using the same reactive distillation apparatus as in Example 1, the feed rate per hour of the phenol-containing raw material liquid in Example 1 was changed from 60 g to 63 g, and the amount of methyl valerate was changed from 60 g to 63 g.
- a sequential complex reaction was performed under the same reaction conditions.
- the withdrawal amount of the bottoms per hour was 115 g.
- the amount of the distillate withdrawn per hour was 101 g.
- the composition was found to be 29.4% for phenyl valerate, 14.9% for methylphenyl carbonate, 0% for diphenyl carbonate 1, 3.9% for dimethyl carbonate, 13.3% of methyl valerate and 27.5% of phenol.
- the conversion of phenol was 58.5%, and the conversion of dimethyl carbonate was 80.0%.
- the reactive distillation apparatus S of the present invention can provide a reaction distillation apparatus that can be applied to a relatively complicated reaction in which two or more equilibrium reactions are combined, that is, a sequential complex reaction.
- the reactive distillation method of the present invention can provide a relatively complicated reaction in which two or more equilibrium reactions are combined, that is, a reactive distillation method that can be applied to a sequential complex reaction.
- a useful carbonic acid ester can be efficiently produced.
- diphenyl carbonate which is one of the above-mentioned carbonates, is used as a raw material for industrially useful polycarbonate.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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EP97922103A EP0842685A4 (en) | 1996-05-21 | 1997-05-20 | APPARATUS AND REACTION DISTILLATION METHOD |
US09/000,009 US6057470A (en) | 1996-05-21 | 1997-05-20 | Reaction distillation apparatus and reaction distillation method |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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JP8/126035 | 1996-05-21 | ||
JP8126035A JP2854279B2 (ja) | 1996-05-21 | 1996-05-21 | 反応蒸留装置および反応蒸留方法 |
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WO1997044108A1 true WO1997044108A1 (fr) | 1997-11-27 |
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PCT/JP1997/001685 WO1997044108A1 (fr) | 1996-05-21 | 1997-05-20 | Appareil de distillation par reaction et procede de distillation par reaction |
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US (1) | US6057470A (ja) |
EP (1) | EP0842685A4 (ja) |
JP (1) | JP2854279B2 (ja) |
WO (1) | WO1997044108A1 (ja) |
Cited By (1)
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CN104645896A (zh) * | 2015-01-09 | 2015-05-27 | 烟台大学 | 一种偶相催化反应-非均相共沸精馏系统及方法 |
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JP2922848B2 (ja) * | 1996-06-14 | 1999-07-26 | 株式会社日本触媒 | 芳香族炭酸エステルの製造方法 |
US6413413B1 (en) * | 1998-12-31 | 2002-07-02 | Catalytic Distillation Technologies | Hydrogenation process |
US6600061B1 (en) | 2000-11-15 | 2003-07-29 | General Electric Company | Method for the continuous production of aromatic carbonates |
CN1628090A (zh) * | 2002-02-05 | 2005-06-15 | Lg化学株式会社 | 使用非均相催化剂制备芳香族碳酸酯的连续方法及其反应设备 |
JP5271598B2 (ja) * | 2007-05-09 | 2013-08-21 | 花王株式会社 | オキサゾリン化合物の製造方法 |
US20150027873A1 (en) * | 2013-06-18 | 2015-01-29 | University Of Houston System | Iterative reactive distillation of dynamic ester mixtures |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
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JPS523923B1 (ja) * | 1969-12-25 | 1977-01-31 | ||
JPS59500671A (ja) * | 1982-04-26 | 1984-04-19 | イ−ストマン コダツク カンパニ− | 酢酸メチルの製造方法 |
JPH04261142A (ja) * | 1991-02-14 | 1992-09-17 | Asahi Chem Ind Co Ltd | 芳香族カーボネート類の連続的製造法 |
JPH07206781A (ja) * | 1993-12-23 | 1995-08-08 | Bayer Ag | 炭酸ジメチルの製造方法 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
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JPS523923A (en) * | 1975-06-26 | 1977-01-12 | Nissan Motor Co Ltd | Intake passage device of torch-type ignition engine |
ATE107273T1 (de) * | 1989-12-28 | 1994-07-15 | Asahi Chemical Ind | Kontinuierliches verfahren zur herstellung aromatischer karbonate. |
US5679312A (en) * | 1993-02-17 | 1997-10-21 | China Petro-Chemical Corporation | Multiple stage suspended reactive stripping process and apparatus |
TW310322B (ja) * | 1994-05-25 | 1997-07-11 | Nippon Catalytic Chem Ind |
-
1996
- 1996-05-21 JP JP8126035A patent/JP2854279B2/ja not_active Expired - Fee Related
-
1997
- 1997-05-20 EP EP97922103A patent/EP0842685A4/en not_active Withdrawn
- 1997-05-20 WO PCT/JP1997/001685 patent/WO1997044108A1/ja not_active Application Discontinuation
- 1997-05-20 US US09/000,009 patent/US6057470A/en not_active Expired - Fee Related
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS523923B1 (ja) * | 1969-12-25 | 1977-01-31 | ||
JPS59500671A (ja) * | 1982-04-26 | 1984-04-19 | イ−ストマン コダツク カンパニ− | 酢酸メチルの製造方法 |
JPH04261142A (ja) * | 1991-02-14 | 1992-09-17 | Asahi Chem Ind Co Ltd | 芳香族カーボネート類の連続的製造法 |
JPH07206781A (ja) * | 1993-12-23 | 1995-08-08 | Bayer Ag | 炭酸ジメチルの製造方法 |
Non-Patent Citations (1)
Title |
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See also references of EP0842685A4 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104645896A (zh) * | 2015-01-09 | 2015-05-27 | 烟台大学 | 一种偶相催化反应-非均相共沸精馏系统及方法 |
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US6057470A (en) | 2000-05-02 |
JP2854279B2 (ja) | 1999-02-03 |
EP0842685A4 (en) | 2001-11-07 |
JPH09308801A (ja) | 1997-12-02 |
EP0842685A1 (en) | 1998-05-20 |
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