WO1997021660A1 - Procede d'elaboration de diarylesters d'acide oxalique - Google Patents
Procede d'elaboration de diarylesters d'acide oxalique Download PDFInfo
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- WO1997021660A1 WO1997021660A1 PCT/JP1996/003636 JP9603636W WO9721660A1 WO 1997021660 A1 WO1997021660 A1 WO 1997021660A1 JP 9603636 W JP9603636 W JP 9603636W WO 9721660 A1 WO9721660 A1 WO 9721660A1
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- oxalate
- reaction
- disproportionation
- distillation column
- alkyl
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/02—Preparation of carboxylic acid esters by interreacting ester groups, i.e. transesterification
Definitions
- the present invention provides diphenyl oxalate (for example, diphenyl oxalate: hereafter abbreviated as DP0) by using an alkyl oxalate (for example, alkylphenyl oxalate) as a starting material and disproportionating it.
- the present invention relates to a process for producing oxalic acid diaryl ester (diaryl oxalate).
- an alkyl oxalate eg, an alkyl phenyl oxalate
- a transesterification reaction of a dialkyl oxalate (dialkyl oxalate) with a phenol oxalic acid diaryl esters
- DP0 disproportionation reaction of the alkyl oxalic ester.
- Diaryl oxalates such as diphenyl oxalate
- diphenyl oxalate are extremely important industrial raw materials in the production of chemicals, such as, for example, olebamate.
- the method (2) or (3) for producing an aryl oxalate by reacting a dialkyl oxalate with an aryl carbonate or an aryl ester of a lower fatty acid is a method in which the raw material diacarbonate is used. It is difficult to produce reels or lower fatty acid aryl esters, which makes them very expensive and difficult to obtain. Since the by-products are produced in a considerably large amount, a very complicated or complicated purification step is required to isolate the diallyl oxalate. Did not. Disclosure of the invention
- An object of the present invention is to provide a process for producing diaryl oxalate, which uses an alkyl oxalate as a starting material, produces little by-products, has high productivity, and is industrially practical. That is what you do.
- the above object can be achieved by the method of the present invention.
- the method for producing diallyl oxalate according to the present invention comprises:
- alkyl oxalate is subjected to a disproportionation reaction in the presence of a disproportionation catalyst, and diaryl oxalate is formed while removing dialkyl oxalate as a by-product. It does. Further, in the method for producing a diallyl oxalate of the present invention, a dialkyl oxalate and a phenol compound are subjected to a transesterification reaction in the presence of a transesterification catalyst to remove a by-produced aliphatic alcohol. Producing alkyl oxalate ester while removing,
- the obtained reaction mixture containing alkyl oxalate is used as a disproportionation catalyst, using the transesterification catalyst described in the above A in the reaction mixture.
- oxalic acid diacid c) ⁇ can be formed.
- FIG. 1 is a process description for carrying out one embodiment of the production method of the present invention.
- FIG. 1 A first figure.
- FIG. 2 is a process explanatory view for carrying out another embodiment of the production method of the present invention.
- the diaryl oxalate (b) and the oxalate are disproportionated by the disproportionation reaction of the alkyl oxalate (a) starting compound.
- the acid dialkyl ester (c) is formed.
- R is an alkyl group, preferably C, -C,. Table showing alkyl groups
- C Ar is ⁇ Li Lumpur group preferred to rather the phenylalanine group or C, -C 6 alkyl group, C, -C e alkoxy group, two collected by filtration group, and a halogen atom, from other substituents of that Represents a selected at least one-substituted phenyl group)
- the disproportionation reaction of the alkyl oxalate is preferably carried out in the liquid phase, and the resulting reaction mixture contains unreacted starting materials, for example, METHYLFU XILOXALATE (MP0) and disproportionation catalyst, target compound such as diphenyloxalate (DP0) and by-product dialkyl oxalate such as dimethyloxalate (DM0) And is mainly contained.
- the target compound for example, difluoroxalate, can be easily separated and collected from such a reaction mixture by a known method, for example, a distillation method.
- the alkyl oxalate (a) used as a starting compound is, for example, as shown in the following reaction formula (2), a dialkyl oxalate (c) and a phenyl oxalate (c).
- the reaction can be carried out by subjecting the metal compound (d) to a transesterification reaction while removing the by-produced aliphatic alcohol (e).
- the alkyl oxalate (a) is obtained by the following reaction formula
- the transesterification reaction of alkyl oxalate with phenolic compound according to (3) produces diaryl oxalate as a target compound and a by-product aliphatic alcohol.
- the transesterification according to the reaction formula (3) has a problem that the reaction rate is low, and is not practical.
- Alkyl groups are methyl, ethyl, n
- reaction formula (1) substituted full et two Le group represented Ri by the Ar to (3) is a substituent having C, and -C e alkyl group, this C,
- ⁇ (: 6 alkyl groups should be selected from methyl, ethyl, n- and iso-propyl, ⁇ - and iso-butyl, ⁇ - and iso-pentyl and ⁇ - and iso-hexyl groups And the substituent is
- the aliphatic alcohol (e) generated by the transesterification reaction corresponds to the R group, and includes, for example, methanol, ethanol, propanol, butanol, and hexanol. And the like.
- the amount of the disproportionation catalyst used depends on the type of catalyst, the type and size of the reaction apparatus (for example, a multistage distillation column), the type and concentration of each raw material, and the disproportionation reaction. In general, it is preferably about 0.0001 to 50% by weight, particularly preferably 0.001 to 30% by weight, based on the weight of the alkyl oxalate used, although it depends on the reaction conditions. More preferably about 0.005 to 10% by weight Degrees.
- the concentration (C) of the disproportionation catalyst in the raw material mixture or the reaction mixture is determined by adjusting the concentration of the raw material mixture containing the alkyl oxalate or the reaction product. Is preferably about 0.001 to 45% by weight, particularly preferably 0.005 to 25% by weight, more preferably 0.01 to 10% by weight, based on the weight of the reaction mixture containing %.
- the reaction conditions in the disproportionation reaction of the production method of the present invention are not particularly limited, but in particular, the reaction temperature is about 50 to 350 ° C, and the reaction pressure is O.OOlmmHg to 10 kgZcm 2.
- the reaction time (in the case of a distillation column type reactor, this means the residence time of the reaction solution in the column) should be about 0.001 to 100 hours.
- the alkyl oxalate used in the disproportionation reaction of the production method of the present invention is represented by the following formula (a) as described above.
- R is an alkyl group, preferably C, -C,.
- Alkyl group properly favored is La, -C 6 alkyl radical, rather then favored by et, C, represents ⁇ C alkyl group
- Ar is ⁇ rie group, is preferable and rather phenylpropyl group or represents a full Weniru group having 1 or more substituents, the substituents phenyl groups, C as described above, -C 6 alkyl group, C, -C 6 alkoxy group, two collected by filtration groups, and halogen It is preferable to be selected from atoms.
- alkyl oxalate to be subjected to the disproportionation reaction include, for example, methylphenyl oxalate, ethylphenyl oxalate, propylphenyl oxalate, and oxalate.
- Alkylphenyl oxalates such as butylphenyl oxalate, hexylphenyl oxalate, pentylphenyl oxalate, octylphenyl oxalate, and methyl oxalate (P-methylphenyl), methyl oxalate (p -Ethyl oxalate (p-methylphenyl), ethyl oxalate (p-ethylphenyl), methyl oxalate (p-methoxyphenyl), methyl oxalate (p-ethoxyquinyl), Methyl oxalate (p-nitrophenyl), methyl oxalate (p-nitrophenyl), methyl oxalate (p-methyl oxalate (p-methyl oxalate (p-methyl oxalate (p-methyl oxalate (p-methyl oxalate (p-
- Alkyl oxalate substituted phenyl ester such as chlorophenyl
- alkyl oxalates can be respectively synthesized by the transesterification reaction between the dialkyl oxalate and the phenol compound.
- the alkyl oxalate to be subjected to the disproportionation reaction of the method of the present invention includes one ester structure having an alkyl group having about 1 to 4 carbon atoms, a phenyl group (substituent) Does not have)
- Oxalic acid diesters having one ester structure are suitable, and lower alkyl oxalates such as methylphenyl oxalate, ethylphenyl oxalate, propylphenyl oxalate and butylphenyl oxalate are most preferred.
- the diaryl oxalate obtained by the production method of the present invention may be any of those represented by the compound (b) in the above-mentioned reaction formula (1), and examples thereof include diphenyl oxalate and oxalate.
- diphenyl oxalate Bis (p-methylphenyl) oxalate, bis (p-methoxyphenyl) oxalate, bis (oxalate) (p-diphenyl), bis (oxalate) (p-chlorophenyl), etc. are preferred.
- diphenyl oxalate is preferable.
- the catalyst used in the disproportionation reaction of the production method of the present invention may be an alkyl oxalate such as alkyl oxalate or the like. There are no restrictions on the type, composition, etc., as long as it can produce a dialkyl oxalate and a diallyl oxalate by a disproportionation reaction.
- the catalyst used as the disproportionation catalyst is selected from, for example, a transesterification catalyst used in a transesterification reaction between a conventionally known dialkyl dicarboxylate compound and phenols. be able to.
- the disproportionation reaction catalyst used in the present invention is preferably soluble in a disproportionation reaction system such as a reaction mixture containing an alkyl oxalate and / or a target product.
- transesterification catalyst used as the disproportionation catalyst include alkali metal, cadmium, and zirconium compounds and complexes thereof, lead-containing compounds, and copper group compounds.
- Metal-containing compounds, iron-containing compounds, zinc-containing compounds, organotin compounds, and Lewis acid compounds of aluminum, titanium and vanadium can be mentioned, and at least one soluble catalyst is used. It is preferred to use.
- Examples of the compounds and complexes of the above-mentioned alkali metal, potassium or zirconium include lithium carbonate, sodium carbonate, potassium carbonate, dibutylaminolithium, and lithiumdiacetyla. Examples thereof include selenium toner chelates, cadmium dicetyl cetyl acetate toner chelates, zirconium diacetyl acetate toner chelates, and zirconocene.
- the lead-containing compound examples include lead sulfide, lead hydroxides, lead salts such as calcium chloride, lead carbonate or a basic salt thereof, lead organic acid salt and a carbonate or basic salt thereof. Salts, as well as tetrabutyl lead, tetrabutyl lead, tributyl lead halogen, triphenyl lead bromo, and triphenyl lead Examples thereof include alkyl or aryl lead compounds such as nil lead, and alkoxy or aryl oxy lead compounds such as dimethoxy lead, methoxy phenyl lead, and difluoro X oxy lead.
- Examples of the copper group metal-containing compound include copper acetate, copper diacetyl acetate toner chelates, organic acid salts of copper such as copper oleate, alkyl copper compounds such as butyl copper, and alkoxy copper compounds such as dimethoxy copper. And copper compounds such as copper halide, and silver compounds such as silver nitrate, silver bromide, and silver picrate.
- examples of the iron-containing compound include iron hydroxide, iron carbonate, triacetoxy iron, trimethyoxy iron, and triphenoxy iron.
- examples of the zinc-containing compound include zinc diacetyl acetate chelate, diacetoxy zinc, dimethoxy zinc, dietine zinc, and diphenoxy zinc.
- organotin compound examples include (Ph) 4 Sn, (0C0CH 3 ) 4 Sn, (MeO) 4 Sn, (EtO) 4 Sn, (PhO) 4 Sn, (Me) 3 SnOCOCH 3 , (Et) 3 Sn (0C0CH 3 ).
- Examples of the aluminum ruisic acid compound include AKX)
- titanium Lewis acid compounds include, for example, Ti (X) 3 , Ti (0C0CH 3 ) 3 , Ti (0 e) 3 , Ti (0Et) 3 ,
- V (X) 4 can and this include the You.
- C0CH 3 is Asechiru group
- M e is methyl
- E t is Echiru group
- B u is butyl
- Ph is phenylalanine group
- X represents a halogen atom.
- the disproportionation catalyst used in the production method of the present invention it is particularly preferable to use a lithium compound and a complex thereof, a zirconium complex, an organotin compound, a Lewis acid compound of titanium, and the like. In particular, it is more preferable to use an organic tin compound or a Lewis acid compound of titanium.
- the disproportionation reaction of the alkyl oxalate can be carried out in the presence of a phenol compound.
- the molar ratio of the alkyl oxalate ester to the phenol compound is such that the molar ratio of the phenol compound to the alkyl oxalate ester in the feedstock is 1: 0. 01 to 1: preferably 1 000, 1 ... 0.1 to 1: 100 more preferably, more preferably 1: 0.5 to 1 : About 20.
- a phenol compound which may be used in combination in the disproportionation reaction of the production method of the present invention a phenol compound which can be used in a transesterification reaction between a dialkyl oxalate and a phenol compound described later. You can choose from a group of chemical compounds.
- the reactor used in the production method of the present invention performs the disproportionation reaction of the alkyl oxalate ester while immediately removing the low-boiling dialkyl oxalate produced as a by-product from the reaction mixture.
- the distillation column type reactor uses the liquid phase disproportionation reaction of alkyl oxalate and the evaporative removal of by-product dialkyl oxalate.
- the device can perform the following.
- the distillation column type reaction device for example, it is preferable to use a reaction device including a multi-stage distillation column (a continuous reaction device or a batch device).
- the reactor including the multi-stage distillation column described above has a theoretical plate number of at least two or more, especially 5 to 100 plates, especially? It is preferable to use a reaction apparatus having a multi-stage distillation column having up to 50 stages (also referred to as a reactive distillation column).
- examples of the multi-stage distillation column reactor include a reactor having a tray-type distillation column using a bubble tray tray, a perforated plate tray, a bubble tray or the like; It is possible to use one having a packed distillation column packed with various packing materials such as ring, leasing ring, and pole ring. Further, a reactor including a distillation column having both a tray type and a packed type can be used for the disproportionation reaction of the method of the present invention.
- the production method of the present invention will be further described with reference to the accompanying drawings.
- a reactor consisting of a multistage distillation column 1 having a number of trays 2 (particularly a portion where the shelf 2 of the multistage distillation column 1 is installed)
- the raw material supplied from the raw material supply line 5 is used.
- the alkyl aryl oxalate is heated to the set temperature, and subjected to the disproportionation reaction represented by the above reaction formula (1) in the presence of the disproportionation catalyst, thereby producing dialkyl oxalate as a by-product.
- the low-boiling products are withdrawn by a withdrawal line 1b connected to the top 1a of the distillation column by distillation, and are coagulated by a cooler 4 as necessary.
- the condensate may be refluxed to the upper part 1c of the multistage distillation column via the circulation line 9.
- the reflux ratio is preferably 20 or less, and more preferably 10 or less. At this time, it is preferable that a part or the whole of the condensed liquid (mainly composed of dialkyl oxalate) condensed in the cooler 4 is removed to the outside of the system via the extraction line 6.
- the raw material and the catalyst supplied to the disproportionation reaction of the production method of the present invention are supplied from the raw material supply line 5 in a liquid phase.
- the connection position of the raw material supply line 5 is set at “from the lowest platen in the multistage distillation column i”. It is preferable that the height be in the range from the shelf of about 1 Z 4 above the shelf to the shelf of about 1 Z 20 below the top shelf. More preferably, it is within the range from “central shelf” to ⁇ top shelf from about 110 lower than all shelves.
- the raw material mixture (or reaction mixture) flows down each of the trays 2 in the distillation section of the first reactive distillation column 1 while disproportionating at each of the tray sections (distillation section) and the bottom of the column. Receive a reaction.
- a reaction liquid containing diallyl oxalate at a high concentration is accumulated at the bottom 1 d (bottom) of the second reactive distillation column 1.
- a low-boiling substance containing a dialkyl oxalate by-produced at the same time evaporates in each tray 2, which is led to the upper tray as a vapor phase and goes to the upper tray.
- the concentration of dialkyl oxalate in the vapor phase rises, is rectified, and is separated and removed from the reaction system.
- the reaction solution is heated by the heater 3 installed in the circulation line 8 to heat the reaction solution collected at the bottom (bottom) of the multi-stage distillation column 1 and circulated. This can be done by circulating in line 8. Then, the reaction mixture containing the target substance, oxalic acid diallyl ester, is withdrawn from the system from the withdrawal line 7 and sent to a purification step (not shown). Diaryl oxalate is separated and recovered.
- the reaction temperature is determined from the mixed solution containing each raw material and the reaction product. It is preferable that the reaction temperature is higher than the temperature at which the resulting reaction solution melts, and the temperature is such that the target product, diallyl oxalate, is not thermally decomposed.
- the reaction temperature of the disproportionation reaction in the method of the present invention is preferably about 50 to 350 ° C, more preferably 80 to 300 ° C, and 100 to 28 ° C. More preferably, it is about 0.
- reaction pressure of the disproportionation reaction of the method of the present invention may be any of reduced pressure, normal pressure, and pressurized condition, but at a temperature and a pressure at which dialkyl oxalate as a by-product can be removed by evaporation.
- reaction temperature is from about 50 to 350 ° C
- reaction pressure is rather to preferred and the Dearuko 0.01mmHg ⁇ 2 kgZcni 2, 0. lmmHg ⁇ 1 kg / cm 2 is more preferable, and more preferably about 50-500 mmHg.
- the reaction time of the disproportionation reaction (residence time in the distillation column when a multi-stage distillation column is used) varies depending on the reaction conditions, the type of the reactor, and the operating conditions. At ⁇ 350 ° C, the reaction time is preferably from about 0.01 to 50 hours, more preferably from 0.02 to 10 hours, and even more preferably from about 0.05 to 5 hours.
- the disproportionation reaction described above enables the production of diallyl oxalate in a sufficient yield (high yield), and the formation of the produced oxalate. Satisfies the two requirements that the acid diaryl ester is not consumed by decomposition or polymerization due to high temperature and long-term heat history, for example, at a high rate (decomposition rate) of 1 to 5% by weight.
- reaction temperature (T) reaction temperature
- H residence time of the reaction solution
- concentration of the disproportionation catalyst in the reaction solution (C), etc. concentration of the disproportionation catalyst in the reaction solution
- the disproportionation reaction temperature (T) of the alkyl aryl oxalate is controlled in the range of 100 ° C to 280 ° C, and the concentration of the disproportionation catalyst (C When the disproportionation reaction of the alkyl oxalate is controlled by controlling the concentration of the catalyst in the reaction mixture to 0.001% by weight to 45% by weight, ( a ) the disproportionation reaction temperature (T) When the temperature is 100 ° C or higher and lower than 220 ° C, control the residence time (H) of the reaction solution at that temperature to 0.01 to 10 hours, preferably 0.05 to 5 hours, and (b) ) If the disproportionation reaction temperature (T) is 220 ° C or higher and lower than 250 ° C, set the residence time (H) of the reaction solution at that temperature to 0.01 to 2 hours, preferably 0.05 to 1 hour.
- the residence time (H) of the reaction solution at that temperature is preferably 0.01 to 0.5 hours.
- the yield of the disproportionation reaction of the alkyl oxalate can be kept at a suitable value, and the heat described above can be maintained. The loss (consumption) of diaryl oxalate due to history can be prevented.
- the disproportionation reaction temperature (T) is 120 ° C. or more and less than 220 ° C., particularly about 125 ° C. to 215 ° C.
- the concentration of the disproportionation catalyst (C: (Catalyst concentration) is 0.005 to 25% by weight, particularly 0.01 to 10% by weight, and more preferably about 0.05 to 5% by weight
- the residence time (H) of the reaction solution at this temperature is 0.05 to 10 hours, particularly 0.05 It is industrially optimal that the time is between 5 and 5 hours, more preferably between 0.1 and 5 hours.
- reaction conditions deviate from the above-mentioned conditions, decomposition of the oxalic acid diaryl ester in the reaction solution and Z or polymerization occur at a high rate, and Since loss may occur, it is not industrially preferable, and if it falls below each lower limit, the rate of the disproportionation reaction decreases, and the reaction may not be completed within a practical time. Not preferred.
- a dialkyl oxalate and a phenol compound are subjected to a transesterification reaction to produce an alkyl oxalate, and then the reaction solution is subjected to a disproportionation reaction to produce a reaction.
- Disproportionation of the alkyl oxalate ester in the reaction solution to oxalic acid In the case of producing a diaryl ester, the transesterification reaction between the dialkyl oxalate and the phenol compound in the first step is carried out in the presence of a transesterification catalyst in the presence of a transesterified aliphatic alcohol.
- alkyl oxalate diesters such as alkyl oxalate
- disproportionation reaction of the alkyl oxalate as described above.
- the transesterification reaction capable of producing an acid diaryl ester for example, the transesterification of a dialkyl oxalate (c) with a phenol compound (d) is carried out according to the above reaction formula (2).
- the alkyl oxalate (a) produced further undergoes a disproportionation reaction to form a diaryl oxalate. Also occurs.
- the dialkyl oxalate is an oxalate diester having two ester structures having an alkyl group having 1 to 10 carbon atoms, preferably 1 to 6 carbon atoms, and more preferably 1 to 4 carbon atoms.
- dimethyl oxalate, getyl oxalate, dipropyl oxalate, dibutyl oxalate, dihexyl oxalate, dioctyl oxalate, methylethyl oxalate and the like can be mentioned.
- dialkyl oxalate having about 1 to 4 carbon atoms in the alkyl group is used.
- an aliphatic alcohol by-produced in the transesterification reaction can be easily removed.
- the phenolic compound used in the above transesterification reaction includes phenol, an alkyl group having 1 to 6 carbon atoms, an alkoxy group, a nitro group, and a halogen atom having 1 to 6 carbon atoms.
- a phenol that may have at least i substituents, or the most preferred is a phenol.
- o-, m- or p-cresole, xylenol (dimethylphenol), dipropylphenol, and methylethylphenol are used as phenol compounds other than phenol.
- Enol trimethyl phenol, tetramethyl phenol, ethyl propyl, propyl phenol, butyl phenol, hexyl phenol, etc.
- Alkyl phenols such as rutile phenols, 0—, m— or p—hydroxy phenols, ethoxy phenols, etc., p—Chloro phenols, 3, 5—dibromophenols Examples thereof include norophenols such as phenol and o-, m-, or p-nitrophenols such as nitrophenol.
- the transesterification catalyst used in the above transesterification reaction is not particularly limited as long as it can generate an alkyl oxalate ester by a transesterification reaction between a dialkyl oxalate and a phenol compound.
- a transesterification catalyst may be used, or the transesterification catalyst specifically exemplified as the one which can be used in the above-described disproportionation reaction of the alkyl oxalate gestester may be used as it is. it can.
- the ester exchange reaction of the dialkyl oxalate and the phenol compound and the disproportionation reaction of the alkyl oxalate are carried out.
- the catalysts used in the reaction are preferably the same type of catalyst (particularly preferably exactly the same catalyst).
- the reaction solution supplied to the next stage of disproportionation reaction includes the reaction raw materials and the catalyst used for the transesterification reaction, the desired product alkyl oxalate (eg, MP0) and dioxalate. It mainly contains reel esters (eg, DP0) and methyl alcohol, a by-product.
- the ratio of the dialkyl oxalate to the phenol compound used varies depending on the type and amount of the catalyst and the reaction conditions.
- the molar ratio of the phenolic compound to the dialkyl ester is preferably from 0.01: 1 to 1000: 1, particularly preferably from 0.1: 1 to 100: 1, and more preferably from 0.5: 1. 1-2: More preferably, it is 1.
- the amount of the catalyst used in the transesterification reaction varies depending on the type of the catalyst, the type and size of the reaction apparatus (for example, a multistage distillation column), the type and composition of each raw material, and the reaction conditions of the transesterification reaction. Usually, it is preferably about 0.0001 to 50% by weight, more preferably 0.001 to 30% by weight, and more preferably 0.005 to 10% by weight, expressed as a ratio to the total amount of the dialkyl oxalate and the phenol compound. Heavy More preferably, it is about% by volume.
- the reaction conditions in the transesterification reaction is not particularly limited, a reaction temperature In general about 50 to 350 ° C, the reaction pressure was 0.00 1 hide H g ⁇ 200 kg / cm 2, The reaction time is preferably about 0.001 to 100 hours.
- the reaction conditions in the transesterification reaction should not adversely affect the subsequent disproportionation reaction of alkyl oxalate.
- the reaction conditions (catalyst concentration, reaction temperature, etc.) in the disproportionation reaction be very close.
- the dialkyl oxalate and the phenolic compound are immediately removed from the reaction solution while aliphatic alcohols, which are low-boiling products produced as a by-product of this reaction, are immediately removed.
- any reactor may be used.
- a distillation column reactor is used to remove aliphatic alcohol produced as a by-product.
- the apparatus is capable of performing a transesterification reaction in a reaction solution in a liquid phase while the distillation column-type reaction apparatus is, for example, a reaction in the aforementioned disproportionation reaction.
- a reactor composed of a continuous multi-stage distillation column can be suitably cited, and the reactor composed of the multi-stage distillation column has a theoretical plate number of at least two or more, especially 5 to 5. It is preferable to use a multistage distillation column type reactor having 100 stages, particularly 7 to 50 stages.
- Examples of the multistage distillation column-type reactor in the transesterification reaction include, for example, a bubble tray, a perforated plate tray, a bubble tray, and the like, as in the reactor in the disproportionation reaction described above. It is possible to use a tray type distillation column used, or a packed distillation column filled with various packing materials such as Raschling, Lessing ring, and Polling. A distillation column having both a tray type and a packed type can be used.
- a reaction apparatus shown in FIG. 2 is used to evaporate and remove by-produced aliphatic alcohol in a first distillation reaction column (multistage distillation column) 10 in the presence of a transesterification catalyst.
- the transesterification catalyst is used as a disproportionation reaction catalyst to evaporate dialkyl oxalate (mainly a by-product) and a phenol compound.
- dialkyl oxalate mainly a by-product
- the diaryl oxalate is continuously produced from the dialkyl oxalate and the phenol compound.
- This method is industrially preferred.
- the first reactive distillation column (multi-stage distillation column) 10 and the second reactive distillation column (multi-stage distillation column) 1 composed of a multi-stage distillation column are formed at the bottom of the first distillation reaction column 10 (multi-stage distillation column).
- the bottom is connected by a 1 d can liquid extraction line (pipe) 17 and a supply line 5 to the second reactive distillation column 1.
- the first reactive distillation column 10 and the second reactive distillation column 1 were used to produce an alkyl oxalate ester by ester exchange reaction and dioxalate by disproportionation reaction.
- Real ester generation can be performed continuously.
- the condensate or vapor of the dialkyl oxalate extracted through the extraction line 6 of the multistage distillation column (second reactive distillation column) 1 for the disproportionation reaction is subjected to a transesterification reaction.
- the first reactive distillation column 10 shown in FIG. 2 a number of distillation trays 12 are arranged, and a dialkyl oxalate and a phenol compound are passed through a raw material supply line 15. And the raw material containing the transesterification catalyst is supplied.
- a transesterification reaction is carried out, and the by-produced aliphatic alcohol is distilled, withdrawn from the top 10 a via a line 10 b, and condensed by a cooler 14. .
- This condensate is extracted out of the system by the line 16, and a part of the condensate may be refluxed to the column top 10 c by the line 19 if necessary.
- the return ratio at this time is preferably 20 or less, and more preferably 10 or less.
- the raw material (dialkyl oxalate, phenol compound) and the transesterification catalyst supply line 15 supplied to the transesterification reaction are the same as those described in “multi-stage distillation column 10 in FIG.
- the reaction solution is heated by a heater 13 provided in the circulation line 18 so that the reaction solution collected at the bottom of the multistage distillation column 10 is circulated through the circulation line 18. This can be done by heating while heating.
- the reaction solution containing the alkyl oxalate formed as a reaction intermediate is extracted from the reaction solution. It was withdrawn from the system from 17 and supplied to the second reactive distillation column via the raw material supply line 5 for the above-mentioned disproportionation reaction in the next step, which was already explained in detail. It can be subjected to a disproportionation reaction (step) to disproportionate the alkyl oxalate to produce the desired diaryl oxalate.
- the reaction temperature is equal to or higher than the temperature at which the reaction mixture containing each raw material and the reaction product melts.
- the temperature is preferably within a temperature range in which the product, such as alkyl oxalate, is not thermally decomposed.
- the reaction temperature of the transesterification reaction is preferably about 50 to 350 ° C, more preferably 100 to 280 ° C, and about 125 to 215 ° C. Even better
- Phenol, dimethyl oxalate and tetrafluoroethylene are added to the bottom of a 50-stage (actual stage) old-short (multi-stage reactive distillation column) with a column diameter of 32 strokes.
- a 500-milliliter mixture of enoxycitane (TPT) in a molar ratio of 1.5: 1: 0.002 was charged, and the bottom was placed in a mantle-filled solution for about 19%. (Heating up to TC, refluxed under normal pressure.
- a liquid having the same composition as above is fed at a flow rate (flow rate) of 300 milliliters per hour on the first and second tiers from the top of the old one, and refluxed.
- the ratio is set to about 5, and the methanol vapor generated from the top is continuously extracted, and the liquid volume in the old-shoulder bottom is reduced to 500 milliliters.
- the reaction solution continuously to maintain While extracting, the transesterification reaction was continuously performed for 10 hours. In the transesterification reaction in the above-mentioned Older Show, the residence time of the reaction solution was about 2 hours.
- the reaction solution of Reference Example 1 is applied hourly to the 12th row from the top of the Older Show.
- the dimethyl oxalate, phenol and a small amount of methanol, which are supplied at a flow rate (flow rate) of 300 milliliters and evaporate from the top without reflux, are continuously discharged.
- the disproportionation reaction is continuously performed while continuously withdrawing the reaction liquid from the bottom so as to maintain the volume of the bottom liquid of the old show at 500 milliliters. This was performed for 10 hours.
- dimethyl oxalate 49.21 weight
- phenol 50.12% by weight
- methanol 0.53% by weight
- methylphenyl oxalate 0.
- a low-boiling liquid mixture having a composition of 25% by weight was distilled at a flow rate of 190 g Z hr, and from an Older shower bottle, 13.54% by weight of phenol was added.
- Reaction solution containing 2.55% by weight of dimethyl dimethyl, 18.70% by weight of methylphenyl oxalate, and 6.4.3% by weight of diphenyl oxalate [catalyst concentration (as TPT): Approximately 0.9 wt%], with a force of 125 g / hr.
- Disproportionation was carried out in the same manner as in Example 1, except that the feed position of the raw material (mixture of phenol, methylphenyl oxalate and TPT) was changed from the 12th stage of the old shot to a bottom. The reaction was performed. In the state where the compositions of the distillate and the withdrawn liquid were stable, the flow rates and compositions of these liquids were as follows.
- Example 2 The reaction mixture obtained in Example 1 was distilled under reduced pressure (20 mmHg) to distill off phenol and dimethyl oxalate, and then methylphenyl oxalate was separated by distillation to have a purity of about 100. % Of methylphenyl oxalate (containing no catalyst) was obtained.
- a 500-milliliter three-necked flask was equipped with a stirrer, a thermometer, and a 30 cm long double-grain distillation tube, to which methylphenyl oxalate obtained as described above was used: 300 g and TPT: l. Og were added, and the mixture was heated by immersion in an oil vise, and disproportionation reaction was performed at 180 ° C under normal pressure while extracting dimethyl oxalate.
- reaction solution [catalyst concentration (as TPT): 0.49% by weight] was composed of dimethyl oxalate: 0.12% by weight, methylphenyl oxalate: 7.73% by weight, and diphenyl oxalate: 93.07% by weight. It had.
- TPT Disproportionation reaction was carried out in the same manner as in Example 3 except that zirconium acetyl acetate toner l.lg was used instead of l.Og. About 4 hours after the start of extraction, 95 g of dimethyl oxalate was extracted. At this time, the reaction solution (catalyst concentration (as zirconium acetyl acetate): 0.54% by weight) was as follows: dimethyl oxalate: 0.18% by weight, methylphenyl oxalate: 9.61% by weight, diphenyl oxalate: : Had a composition of 91.55% by weight.
- the disproportionation reaction was carried out in the same manner as in Example 3 except that 0.8 g of tetrafluoroenyltin was used instead of 1.0 g of TPT.
- reaction solution (catalyst concentration (as tetraphenyltin): 0.39% by weight) was as follows: dimethyl oxalate: 0.09% by weight, methylphenyl oxalate: 5.79% by weight, diphenyl oxalate: It had a composition of 94.59% by weight.
- the disproportionation reaction was carried out in the same manner as in Example 1 except that the reaction temperature of the disproportionation reaction was 200 ° C and the residence time of the reaction solution in the disproportionation reaction was about 4.5 hours.
- reaction solution Catalyst concentration (as TPT): 0.92% by weight
- the reaction solution had a composition of dimethyl oxalate: 1.32% by weight, methylphenyl oxalate: 20.05% by weight, diphenyl oxalate: 73.94% by weight, and phenol 2.2% by weight.
- the first reactive distillation column and the second reactive distillation column are composed of two old-short (multi-stage reactive distillation columns) with a column diameter of 32 mm, 50 stages (actual stages), and a bottle capacity of 1 liter.
- Figure 2 shows the reactor connected (with the exception that the condensate from withdrawal line 6 was not connected to the first reactive distillation column). Using the reactor, the transesterification reaction and the disproportionation reaction were performed continuously.
- phenol, dimethyl oxalate, and tetrafluoroethoxy titan (TPT) were added to the bottom of the Oldershaw (multistage reactive distillation column: the first reactive distillation column) at a molar ratio of 1.5: 1: 500 milliliters of the raw material mixture mixed at a rate of 0.002 was charged, and the bottom was heated to about 190 ° C in a mantle heater to create a reflux state under normal pressure.
- a raw material mixture having the same composition as above is fed at a flow rate (flow rate) of 300 milliliters per hour on the first and second tiers from the top of the Older Show, and the reflux ratio is adjusted. Adjust the reaction solution to about 5 and continuously extract the generated methanol from the top, and keep the volume of the old shot bottom at 500 milliliters. A transesterification reaction was performed while extracting. When the composition of the distillate and the eluate becomes stable (after about 5 hours from the start of the reaction), almost 100% of methanol power is obtained from the top of the old short shot. The distillate was distilled at a flow rate of 22.7 g / hr.
- reaction liquid catalyst concentration: 0.34% by weight
- Nirca 30.74% by weight
- 6.81% by weight of diphenyl oxalate was withdrawn at a flow rate of 296 g Zhr, and this was subjected to the second reactive distillation.
- the reaction was once stored in an intermediate vessel to feed the column at a flow rate of 316 g Z hr.
- the first stage from the top of the Older Shaw (second reactive distillation column) The supply of the above-mentioned ligated reaction solution (ester exchange reaction solution) extracted from the bottom of the first reactive distillation column is started at a flow rate (flow rate) of 300 milliliters per hour and refluxed. While continuously extracting dimethyl oxalate, phenol and a small amount of methanol that evaporate from the uppermost part and remove it, an old shot (second reaction)
- the reaction liquid (disproportionation reaction liquid) is continuously withdrawn from the bottom of the second reactive distillation tower so that the liquid volume of the bottom liquid in the distillation tower is maintained at 500 milliliters. Meanwhile, the disproportionation reaction was continuously performed at 190 ° C. for 10 hours.
- the residence time of the reaction solution was about four hours.
- a mixture of low-boiling substances having the following composition is distilled at a flow rate of about i 90 g and Z hr. From the bottom of the rudder show (second reactive distillation column)
- reaction solution (catalyst concentration: about 0.90 weight) was withdrawn at a flow rate of 124 g Zhr.
- the present invention industrially converts diaryl oxalate (particularly diphenyl oxalate), which is important as a raw material for a chemical reaction, from an alkyl oxalate (particularly methylphenyl oxalate) by a disproportionation reaction. It is the first to provide a manufacturing method.
- the types of by-products are smaller than those of the conventionally known production methods of diallyl oxalate, and the isolation and purification of the objective diaryl oxalate are easy.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP96941854A EP0814074B1 (en) | 1995-12-12 | 1996-12-12 | Process for preparing diaryl esters of oxalic acid |
DE69612280T DE69612280T2 (de) | 1995-12-12 | 1996-12-12 | Verfahren zur herstellung von diarylestern der oxalsäure |
US08/875,823 US6018072A (en) | 1995-12-12 | 1996-12-12 | Process for producing a diaryl oxalate |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP32318195 | 1995-12-12 | ||
JP7/323181 | 1995-12-12 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1997021660A1 true WO1997021660A1 (fr) | 1997-06-19 |
Family
ID=18151977
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1996/003636 WO1997021660A1 (fr) | 1995-12-12 | 1996-12-12 | Procede d'elaboration de diarylesters d'acide oxalique |
Country Status (7)
Country | Link |
---|---|
US (1) | US6018072A (ja) |
EP (1) | EP0814074B1 (ja) |
KR (1) | KR100244075B1 (ja) |
CN (1) | CN1078582C (ja) |
DE (1) | DE69612280T2 (ja) |
ES (1) | ES2155214T3 (ja) |
WO (1) | WO1997021660A1 (ja) |
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CN102712564B (zh) * | 2010-01-20 | 2016-01-06 | 宇部兴产株式会社 | 草酸二芳基酯的制造方法 |
IT201800010919A1 (it) | 2018-12-10 | 2020-06-10 | Sacmi | Apparato e metodo per formare un oggetto concavo. |
US11780804B2 (en) * | 2019-05-24 | 2023-10-10 | Ascend Performance Materials Operations Llc | Tricyanohexane purification methods |
KR102684557B1 (ko) | 2023-03-21 | 2024-07-11 | 이대훈 | 사용의 편의성을 증진시킨 도어용 스토퍼 |
KR102691795B1 (ko) | 2023-07-20 | 2024-08-05 | 이대훈 | 도어용 스토퍼 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS4942621A (ja) * | 1972-08-25 | 1974-04-22 | ||
JPS5082027A (ja) * | 1973-11-20 | 1975-07-03 | ||
JPS5243826B1 (ja) * | 1969-05-22 | 1977-11-02 |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1283849B (de) * | 1963-08-10 | 1968-11-28 | Witten Gmbh Chem Werke | Verfahren zur Herstellung von reinen Arylestern von Dicarbonsaeuren |
JPS562541A (en) * | 1979-06-20 | 1981-01-12 | Matsushita Electric Works Ltd | Gas detector |
JPS568019A (en) * | 1979-07-03 | 1981-01-27 | Matsushita Electric Ind Co Ltd | Mixer |
JPS6035266B2 (ja) * | 1980-09-08 | 1985-08-13 | 大日本印刷株式会社 | 熱硬化性樹脂化粧板の製造法 |
US4482732A (en) * | 1982-09-24 | 1984-11-13 | Occidental Chemical Corporation | Process of manufacturing diaryl esters of dicarboxylic acids |
US4451664A (en) * | 1982-09-24 | 1984-05-29 | Occidental Chemical Corporation | Process of manufacturing diaryl esters of dicarboxylic acids |
US4482733A (en) * | 1982-09-24 | 1984-11-13 | Occidental Chemical Corporation | Process of manufacturing diaryl esters of dicarboxylic acids |
-
1996
- 1996-12-12 CN CN96191891A patent/CN1078582C/zh not_active Expired - Lifetime
- 1996-12-12 KR KR1019970705543A patent/KR100244075B1/ko not_active IP Right Cessation
- 1996-12-12 ES ES96941854T patent/ES2155214T3/es not_active Expired - Lifetime
- 1996-12-12 DE DE69612280T patent/DE69612280T2/de not_active Expired - Lifetime
- 1996-12-12 US US08/875,823 patent/US6018072A/en not_active Expired - Lifetime
- 1996-12-12 WO PCT/JP1996/003636 patent/WO1997021660A1/ja active IP Right Grant
- 1996-12-12 EP EP96941854A patent/EP0814074B1/en not_active Expired - Lifetime
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5243826B1 (ja) * | 1969-05-22 | 1977-11-02 | ||
JPS4942621A (ja) * | 1972-08-25 | 1974-04-22 | ||
JPS5082027A (ja) * | 1973-11-20 | 1975-07-03 |
Non-Patent Citations (1)
Title |
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See also references of EP0814074A4 * |
Also Published As
Publication number | Publication date |
---|---|
EP0814074A4 (en) | 1999-03-03 |
EP0814074A1 (en) | 1997-12-29 |
DE69612280D1 (de) | 2001-05-03 |
EP0814074B1 (en) | 2001-03-28 |
KR100244075B1 (ko) | 2000-02-01 |
CN1173861A (zh) | 1998-02-18 |
US6018072A (en) | 2000-01-25 |
KR19980702148A (ko) | 1998-07-15 |
DE69612280T2 (de) | 2001-09-06 |
ES2155214T3 (es) | 2001-05-01 |
CN1078582C (zh) | 2002-01-30 |
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