JP2007269765A - Method for producing acyl compound of saccharide and apparatus therefor - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for continuously synthesizing an acyl compound of saccharide from a carboxylic acid anhydride and a saccharide in the absence of a catalyst in a short time in a high yield/in high selectivity, to obtain a reaction composition thereof and to provide a simultaneous acylation technology with conversion to a saccharified of high additional value. <P>SOLUTION: The method for producing an acyl compound of saccharide comprises using a subcritical fluid or a supercritical fluid at 100-400°C under 0.1-40 MPa pressure as a reaction solvent, introducing a substrate and the reaction solvent into a circulation type high-temperature and high-pressure apparatus in the absence of a catalyst and changing conditions of temperature and an amount of carboxylic acid anhydride to continuously synthesize an acyl compound of saccharide from a carboxylic acid anhydride and a saccharide in a high yield in high selectivity at a high speed. The reaction composition thereof is obtained. The apparatus therefor is provided. Consequently, the method for producing an acylated saccharide having a high additional value by simultaneous acylation with conversion to a saccharide having a high additional value is provided. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to an acyl compound of a saccharide, a process for producing the same, and more specifically, and more specifically, a high-temperature and high-pressure water or acetic acid mixed solvent is used as a reaction solvent, and the saccharide acyl compound is non-catalyzed in one step. It relates to a method of manufacturing. In the present invention, water or acetic acid at a temperature of 100 to 400 ° C., a pressure of 0.1 to 40 MPa, a mixed solvent thereof is used as a reaction solvent, and a saccharide acyl compound from carboxylic anhydride and saccharide is added in one step in a short time without adding a catalyst. The present invention provides a continuous synthesis method and a reaction composition thereof. Here, examples of the saccharide include monosaccharides, disaccharides, and polysaccharides. Specific examples of the saccharide include glucose, mannose, galactose, and fructose. Examples of the disaccharide include saccharose and the like. Examples thereof include cellulose.

  Saccharic acyl compounds are useful in the field of flavors, pharmaceuticals, foods, and the like because they improve and improve the functionality of raw materials or substrates and add added value. In general, when synthesizing acyl compounds of sugars, the conventional method requires an acid / base catalyst in addition to the aprotic organic solvent. When used in foods and pharmaceuticals, the remaining organic solvent and catalyst are removed. Requires a lot of labor and has problems such as being harmful to the living body as well as affecting the environment. The present invention provides a method for synthesizing an acyl compound of a saccharide only from a carboxylic anhydride and a saccharide without using a catalyst and a process using water, and a reaction composition thereof. The present invention can also be applied to synthesis of chemical products, and can efficiently produce and provide saccharide acyl compounds in a short time.

Conventionally, various methods for synthesizing sugar acyl compounds from carboxylic anhydrides and saccharides have been reported (see, for example, Non-Patent Document 1). Here, if a technique for synthesizing a sugar acyl compound from a saccharide and a carboxylic anhydride is completed, an acyl compound from an amino sugar can usually be synthesized. Therefore, a technique for synthesizing a sugar acyl compound using glucose in particular. Has been reported. According to the prior art document, glucose pentaacetate is obtained in 90% yield with 10 equivalents of acetic anhydride and CoCl ₃ catalyst in a solvent-free or aprotic organic solvent (Non-patent Document 2). In addition, the discovery of DMAP that activates an acyl group via the formation of a stable N-acyl intermediate is considered an innovative technique, and acylation of some saccharides has been reported (Non-patent Document 3). ).

However, since DMAP uses one or more equivalents of amine, metal triflate, which is a Lewis acid, is proposed, and Me ₃ SiOTf (Non-patent Document 4) provides a corresponding acylated product from diacetone-D-glucose. In the case of Bi (OTf) ₃ , tribenzoate was obtained from diacetone-D-glucose in a yield of 91% and from uridine in 99% (Non-patent Document 5). Furthermore, V (OTf) ₃ did not show catalytic activity, but its oxo compound V (O) (OTf) ₂ was found to have catalytic activity, and attention was paid to catalytic activation of V = O. (Patent Literature 3, Non-Patent Literature 6). Monoacetate from diacetone-D-glucose in 75% yield, 3 equivalents of acetic anhydride as acylating agent, D-maltose from D-maltose octaacetate in 85% yield, 90% from β-cyclodextrin % Yield of the corresponding acyl compound (FIG. 1).

  Here, in the above prior art documents, an organic solvent in addition to a catalyst such as an organic base, a Lewis acid, and a solid acid is indispensable for acylation of saccharides. Moreover, it is said that the acylation of saccharides is optimally performed at room temperature because impurities are generated under high temperature conditions and the selectivity is lowered, and high temperature conditions are unsuitable (Patent Documents 1 and 2). . On the other hand, regarding the possibility of water as a solvent in the acylation of saccharides, generally, a method of acylating saccharides under anhydrous conditions by adding a saccharide acylating agent to the crude product, (Patent Document 4). In one document, water is listed as a solvent, but it is not actually used (see Patent Documents 1 and 2).

However, the correlation between the catalytic activity for the aldol reaction and the stability of Lewis acid in water is systematically compared for each element, and there is an example suggesting the applicability to other reactions (Non-patent Document 7). . Furthermore, when Bi (OTf) ₃ is a catalyst, there is a document in which a wet organic solvent containing water that has not been dehydrated promotes the reaction and an improvement in yield is observed (non-patent document). 5). Thus, the effectiveness of water as a solvent for saccharide acylation has not been clear and implemented before. On the other hand, it has been reported that under the solvent-free conditions when Bi (OTf) ₃ is used as a catalyst, the yield decreases and an organic solvent is required (Non-patent Document 5).

  After the reaction, the post-treatment is performed by adding a neutralizing agent to the reaction mixture to neutralize the saccharide in the normal catalyst / organic solvent. After neutralization, the extraction solvent and water or saturated saline are added to separate the solvent layer. After that, the desired product is obtained by the process of drying, solvent removal, distillation or rectification. In addition to water, the water layer contains catalyst, organic solvent, acetic acid, substrate, product, by-product, inorganic substance. A complex mixture is contained. Here, when the separation of the catalyst from the aqueous layer is easy, it is recovered and regenerated and reused, but when the separation is difficult, it is discarded and disposed as it is (FIG. 2). As in the case of acylation of sugars in non-catalyzed high-temperature and high-pressure water, if the water layer contains no catalyst or organic solvent but only water, acetic acid, and product, the product is separated by decantation. Then, it can be separated into water and glacial acetic acid by performing azeotropic distillation in which a substance that forms an azeotropic mixture is added to the aqueous layer (Patent Document 5). This means that the water can be regenerated and is a process of reducing the environment as compared with the normal method (FIG. 3). However, a method of converting a D-glucose into a high-value-added sugar such as D-mannose and simultaneously obtaining a chemically stable acylated sugar (simultaneous acylation with conversion to a high-value-added sugar) Not reported until.

  By the way, regarding the conversion from an inexpensive sugar such as glucose to a high-functional and high-value-added sugar such as mannose, many cases have been reported by an enzymatic method. In particular, there are many reports on conversion of D-fructose to D-mannose by mannose isomerase. In general, isomerase in this case does not use glucose as a substrate (for example, Patent Documents 6, 7, and 8). Therefore, when synthesizing D-mannose from inexpensive D-glucose, fructose isomerase is used to produce D-glucose. Conversion to D-fructose is required, and many fructose isomerases have been discovered (for example, Patent Documents 9, 10, and 11). On the other hand, it is known that D-mannose can be obtained from D-glucose in a yield of 32% when a molybdate catalyst aqueous solution is mixed with a glucose aqueous solution in a flow-type apparatus and then reacted at 130 ° C. (Patent Document 12). ).

  As described above, in the conventional method, in the case of simultaneous acylation accompanied by acylation of saccharides and conversion to high-value-added sugars, a catalyst and an organic solvent are required. In addition, it is necessary to remove the catalyst, the organic solvent, and the carboxylic acid, and the aqueous layer after the separation operation tends to be waste, which causes a problem of waste liquid. In addition, due to consideration for environmental impacts and harmfulness to living organisms, and for the safety of foods and pharmaceuticals that are orally administered by humans, more advanced separation of catalysts and organic solvents is required. It is difficult to get out of the enzymatic method that requires Here, the cost required for high-level separation is comparable to that of the synthesis operation, and it is preferable not to use a catalyst and an organic solvent. In view of the above, in this technical field, a continuous synthesis of acyl compounds of saccharides that can be easily and highly separated by a simple, low-cost, environmentally-reduced synthesis process, with no catalyst or organic solvent remaining. There has been a strong demand for a synthesis method that enables this.

JP 9-169690 A Japanese Patent Laid-Open No. 9-176081 US Pat. No. 6,541,659 US Pat. No. 6,005,122 US Pat. No. 5,980,696 JP 2001-245691 A Japanese Patent Laid-Open No. 06-292578 Japanese Patent Laid-Open No. 11-075836 JP 09-191894 A Japanese Patent Laid-Open No. 08-187080 Japanese Patent Laid-Open No. 06-046853 JP-A-56-068696 W. Green, P.M. G. Wuts, Protective Groups in Organic Synthesis, 3rd ed. , Wiley, New York, 1999, p150 S. Ahmad, J. et al. Iqbal, Chem. Commun. , 1987, 114. G. Hofle, W.M. Steglich, H.M. Vorbruggen. , Angrew. Chem. Int. Ed. 1978, 17, 569. b) A. Hassner, L .; R. Krepski, V.M. Alexian, Tetrahedron, 1978, 34, 2069 P. A. Procopiu, S.M. P. D. Baugh, S.M. S. Flack, G.M. G. A. Inglis, J. et al. Org. , Chem. 1998, 63, 2342 J. et al. Otera, A .; Orita, C.I. Tanahashi, A .; Kakuta, Angrew. Chem. Int. Ed. 2000, 39, 2877 CT Chen, JH. Kuo, C-H. Li, N .; B. Barhate, SW. Hon, TW. Li, SD. Chao, CC. Liu, YC. Li, I-H. Chang, JS. Lin, CJ. Liu and YC. Chou, Org. Lett. , 2001, 3, 3729 S. Kobayashi, S .; Nagayama, T .; Busimama, J .; Am. Chem. Soc. 1998, 120, 8287

  Under such circumstances, in view of the above prior art, the present inventors are able to continuously synthesize acyl compounds of the above sugars with a simple high-speed synthesis process that is low in cost and friendly to the environment. As a result of intensive research with the goal of developing a synthesis method, high-temperature and high-pressure water, subcritical water or supercritical water is used as a reaction solvent, so that saccharide acyl compounds from carboxylic anhydrides and sugars can be produced without catalyst. The inventors have found that they can be synthesized and have completed the present invention. An object of the present invention is to provide a method for continuously synthesizing an acyl compound of a saccharide from a carboxylic anhydride and a saccharide under a non-catalyst under a short reaction condition and a reaction composition thereof.

The present invention for solving the above-described problems comprises the following technical means.
(1) A reaction composition of a carboxylic anhydride and a saccharide, wherein the saccharide acyl compound composition is characterized by having no catalyst and no organic solvent remaining.
(2) A method for synthesizing an acyl compound of a saccharide from a carboxylic anhydride and a saccharide using a subcritical fluid or a supercritical fluid in a high temperature and high pressure state as a reaction solvent, and without using a catalyst, the carboxylic anhydride and the saccharide A method for producing a saccharide acyl compound, comprising synthesizing a saccharide acyl compound by a one-step synthesis reaction.
(3) The method according to (2) above, wherein subcritical or supercritical water in a high temperature and high pressure state is used as a reaction solvent.
(4) The method according to (2) above, wherein a monosaccharide, a disaccharide or a polysaccharide is used as the saccharide.
(5) The method according to (2) above, wherein a subcritical fluid or supercritical fluid having a temperature of 100 to 400 ° C. and a pressure of 0.1 to 40 MPa is used as a reaction solvent.
(6) The method according to (2) above, wherein water, acetic acid, another inorganic solvent, an organic solvent, or a mixed solvent of an inorganic solvent and an organic solvent is used as the subcritical fluid or supercritical fluid.
(7) The method of (2), wherein the reaction is carried out after dissolving or dispersing the saccharide and mixing with carboxylic anhydride at room temperature.
(8) The method according to (2) above, wherein a high-value-added acylated sugar is produced by simultaneous acylation while converting from an inexpensive sugar to a high-functional and high-value-added sugar.
(9) The method according to (2) above, wherein the selectivity is changed by adding an inorganic salt to the saccharide.
(10) The method according to (2) above, wherein the synthesis reaction is carried out by introducing a substrate and a reaction solvent into a flow-type high-temperature and high-pressure apparatus and changing the reaction time in the range of 3 to 60 seconds.
(11) A water feed pump for feeding water, a water heating coil, a high temperature and high pressure flow cell, a reactant feed pump for feeding a substrate, a furnace body, a reactant introduction pipe for introducing the reactant into the furnace body, a reaction An apparatus for synthesizing an acyl compound of a saccharide, comprising a drain line for discharging a solution, a cooling flange, and a back pressure valve for setting a pressure.
(12) In the method described in (2) above, after acylation, water is injected into the recovered aqueous solution, followed by decantation. After separation into an oil / water bilayer solution, an oil layer containing an acyl compound of a saccharide is separated and recovered. On the other hand, a simple continuous separation method in which acetic acid and water are separated and recovered from the aqueous layer by azeotropic distillation.

Next, the present invention will be described in more detail.
According to the present invention, an acyl compound of a saccharide as shown in Chemical Formula 3 is continuously formed from a carboxylic acid anhydride of Chemical Formula 1 and a saccharide of Chemical Formula 2 in a one-step reaction process without adding a catalyst and in a short reaction condition. It is characterized by synthesizing automatically. In the present invention, a subcritical fluid or a supercritical fluid having a temperature of 100 to 400 ° C. and a pressure of 0.1 to 40 MPa is used as the reaction solvent, and subcritical water is preferably used. The reaction conditions are preferably adjusted to a temperature of 200 to 250 ° C., a pressure of 5 MPa, a reaction time of 3 to 60 seconds, and more preferably about 10 seconds. In the formula of Chemical Formula 1, R is an alkyl group or a substituent containing a hetero atom other than an alkyl group. In the formula of Chemical Formula 2, R is a substituent containing a hetero atom other than an alkyl group or an alkyl group, and Q is Carbon or a heteroatom other than carbon or a substituted heteroatom, specifically, oxygen (O), hydrogen nitride (NH), or alkyl-substituted nitrogen (NR ′).

  In the present invention, the substrate and the reaction solvent are introduced into a reaction vessel and a synthesis reaction is carried out in a predetermined reaction time. Therefore, as the reactor, for example, a batch-type high-temperature and high-pressure reaction vessel and a continuous flow-type high-temperature and high-pressure reactor can be used, but the present invention is particularly limited to these reactor types. Not.

  In the method of the present invention, the subcritical fluid and supercritical fluid in the high temperature and high pressure state are used as the reaction solvent. Specifically, subcritical carbon dioxide (normal temperature or higher, 0.1 MPa or higher), subcritical water is used. (100 ° C. or higher, 0.1 MPa or higher), subcritical methanol (100 ° C. or higher, 0.1 MPa or higher), subcritical ethanol (100 ° C. or higher, 0.1 MPa or higher), supercritical carbon dioxide (34 ° C. or higher, 7. 38 MPa or more), supercritical water (375 ° C. or more, 22 MPa or more), supercritical methanol (239 ° C. or more, 8.1 MPa or more), supercritical ethanol (241 ° C. or more, 6.1 MPa or more), a mixed solvent in the same state It is illustrated and subcritical water (200-250 degreeC, 5 Mpa or more) is used suitably. As a reaction solvent, an organic solvent or an inorganic solvent other than those described above can be contained in any ratio. Specifically, a reaction solution containing acetone, acetonitrile, tetrahydrofuran, etc. as an organic solvent, and acetic acid, ammonia, etc. as an inorganic solvent. It is also possible to substitute.

  In the present invention, by adjusting the composition of the reaction solvent of the subcritical fluid and supercritical fluid, the temperature and pressure conditions, the type and amount of the substrate used, and the reaction time, the reaction product can be efficiently produced in a short time. Can be synthesized. Moreover, in this invention, a predetermined | prescribed reaction product can be synthesize | combined by introduce | transducing a substrate and a reaction solvent into a flow-type high temperature / high pressure apparatus, and changing those reaction time in the range of 3 to 60 second, for example. The reaction conditions can be appropriately set depending on the starting material used, the type of the desired reaction product, and the like.

  In the method of the present invention, the synthesis of an acyl compound of a saccharide from a carboxylic acid anhydride and a saccharide, which has heretofore been carried out in the presence of a catalyst, can be carried out continuously at a high speed and without a catalyst. Can be made more efficient. Further, in the method of the present invention, since a conventionally used catalyst is not used at all, there is no need for post-treatment / disposal such as neutralization treatment and detoxification treatment of the solution after the reaction, and environmental load reduction can be achieved. . Further, after the reaction, only a stationary separation operation such as decantation is performed, so that there is no need to separate and recover the catalyst and the organic solvent, and the product separation becomes easy. According to the present invention, an acyl compound of a saccharide can be synthesized in a short time of about 10 seconds without addition of a catalyst with a conversion rate of 99% and a total selectivity of 97%. The synthesis method of the present invention is useful as a method that enables efficient and continuous production of saccharide acyl compounds that can be used in fragrances, pharmaceuticals, and foods in large quantities at high speed.

  Conventionally, an example in which saccharide acylation using a lipase or a catalyst is performed using a subcritical fluid such as carbon dioxide or a supercritical fluid has been reported. However, there is no example demonstrating that a saccharide acyl compound can be synthesized in high yield from a carboxylic acid anhydride and a saccharide in a non-catalytic subcritical water process. The method has been proved by the present inventors for the first time. Moreover, the saccharide acyl compound synthesized from the carboxylic acid anhydride and the saccharide by the conventional method had a problem of remaining catalyst and organic solvent, but the reaction composition synthesized from the carboxylic acid anhydride and the saccharide in the present invention. The product has no catalyst and no organic solvent remaining, and the saccharide acyl compound composition of the present invention has advantages not found in conventional products.

  In the present invention, in order to realize a synthesis reaction of carboxylic anhydride and saccharide under non-catalytic conditions, for example, a solution in which a substrate is dissolved in a solvent in advance is fed, and the reaction progress in a subcritical fluid and a supercritical fluid is increased to a high temperature. It is also possible to use a flow-type high-temperature high-pressure infrared spectroscopic in-situ measuring device (FIG. 5) that is observed by infrared spectroscopic analysis with a high-pressure infrared flow cell (FIG. 4). However, it is better to replace the high-temperature and high-pressure infrared flow cell with a windowless high-temperature and high-pressure flow cell (FIG. 6) and arrange the piping so that the reactant flow directly contacts the supercritical fluid flow. There is no problem such as leakage in the vicinity of the cell window in the flow cell, and synthesis can be performed in a short time at a higher flow rate. For these reasons, an apparatus equipped with this windowless high-temperature and high-pressure flow cell was used in Examples described later.

  Here, the windowless high-temperature high-pressure flow cell main body (FIG. 6) can be fixed to a temperature sensor sheath (12 in FIG. 7) described below by, for example, cutting a screw in a commercially available SUS316 cloth 1. To. Without measuring the temperature of the furnace body atmosphere, the temperature sensor is adjusted to indicate the cell temperature, and is fixed with a case fixing screw and a male screw 3. The pipe 4 of SUS316 is connected to the cross 1 with a taper screw 2 with a one-ring ferrule. Of course, the cloth 1 can also be used as a tee by closing one flow path with an end screw.

  FIG. 7 shows a reactor body portion of a flow-type high-temperature high-pressure reactor equipped with a windowless high-temperature high-pressure flow cell, which is a reactor main body. If this is installed in the shaded position of the flow-type high-temperature and high-pressure fluid in-situ infrared spectrometer shown in Fig. 5, the infrared spectroscopy cannot be measured, but subcritical / supercritical fluid contact synthesis with variable temperature, pressure and flow rate. It can be used as a reactor. In this case, the observation of the reaction was performed by collecting the aqueous solution after discharge, quantifying from a calibration curve using a pure product by GC-FID, and qualitatively analyzing by GC / MS.

  Hereinafter, with reference to FIG. 7, water is fed from the water feed pump 5, and after passing through the cooling flange 8, is sent to the furnace body 13. After passing through the tube coil 9, it is introduced into a high-temperature / high-pressure flow cell 14 supported and fixed to a temperature sensor case 12 in which a temperature sensor 11 is inserted in a high-temperature / high-pressure state. On the other hand, the reactants are fed from the reactant feed pumps 6 and 7, mixed by the tee 18, passed through the cooling flange 8, and then sent to the furnace body 13. After passing through the coiled reactant introduction tube 10, it is introduced into a high-temperature and high-pressure flow cell 14 fixed to the temperature sensor case 12. The solution that has passed through the high-temperature and high-pressure flow cell passes through the piping 17 and then passes through the cooling flange 8 and passes outside the furnace body while being air-cooled. Thereafter, the discharged liquid from the back pressure valve 19 for which the pressure is set is collected and used as a sample. Here, in order to eliminate the influence of heating of the discharge liquid containing the reactants and products, rapid heating is performed, and the piping of the reactant introduction line 10 and the discharge liquid line 17 is made as short as possible so that the water heating coil It is desirable to make 9 as long as possible. The present invention is not limited to these, and any reaction apparatus having the same effect as these can be used in the same manner.

The following effects are exhibited by the present invention.
(1) An acyl compound of a saccharide can be synthesized continuously at high speed from a carboxylic acid anhydride and a saccharide.
(2) A synthesis process without using a catalyst and an organic solvent can be realized.
(3) It can be converted into high-value-added sugars.
(4) Therefore, it is possible to provide a highly safe saccharide acyl compound composition that is free of residual catalyst and organic solvent and is not harmful to the living body.
(5) When the product does not dissolve in water, water is injected into the discharged oil-water dispersion aqueous solution to separate the oil and water into two layers while washing, and a high-purity product can be easily obtained. Can be recovered.
(6) As a new mass production process of saccharide acyl compounds useful as fragrances, pharmaceuticals, and foods, a new production technology that can replace existing production processes can be provided.

  EXAMPLES Next, although this invention is demonstrated concretely based on an Example, this invention is not limited at all by the following Examples.

(Example 1-6)
In this example, the effect of temperature was examined with the synthesis conditions set to no catalyst, a pressure of 5 MPa, and a residence time of 9.9 seconds. First, pure water is sent at a flow rate of 5.0 ml / min to the apparatus in which the main body (main part) of the flow-type high-temperature and high-pressure reactor shown in FIG. Submerged and set to a predetermined temperature and a pressure of 5 MPa to obtain subsupercritical water. Thereafter, toluene was added as an internal standard (5 mol% of the substrate) and acetic anhydride was fed from the pump 6 and a 33 wt% saturated aqueous glucose solution was fed from the pump 7 so that the mixed solution was 0.5 ml / min (mixed) Later glucose concentration: 0.18 mol / kg, glucose / acetic anhydride = 1/35 mol equivalent).

  1 ml of the aqueous solution discharged from the back pressure valve 30 minutes after the substrate feeding was collected. When the internal volume of the pipe from the heating furnace to the back pressure valve outlet was the reaction volume, the reaction time was 9.9 seconds. 1 ml of acetone is added to 1 ml of the collected aqueous solution, shaken, and composition analysis is performed using a GC / MS analyzer (HP 6890, Hewlett Packard, column HP-5, inlet temperature 150 ° C., initial column temperature 60 ° C. (retained) Time 2 minutes), temperature rising rate 10 ° C./min, final column temperature 250 ° C. (holding time 2 minutes)), and the mass spectrum obtained was confirmed by the Willy database with a concordance of 90% or higher. did. In addition, quantitative analysis and qualitative analysis in the case where there are commercially available reagents are GC-FID (GC6890 manufactured by Agilent, column DB-WAX, inlet temperature 230 ° C., split ratio 5.61, initial column temperature 50 using toluene as an internal standard. C. (retention time 0.5 minutes), temperature increase rate 20 ° C./min, final column temperature 230 ° C. (retention time 20 minutes)).

  As a result of examining five temperatures of 150 ° C., 160 ° C., 170 ° C., 180 ° C., 190 ° C., and 200 ° C., the total yield of pentaacetate reached a maximum of 82% at a temperature of 180 ° C. (FIG. 8). At this time, the conversion was 99.7%, the selectivity was α-glucose pentaacetate (α-GAc5) 16%, β-glucose pentaacetate (β-GAc5) 15%, α-mannose pentaacetate (α-MAc5). 19%, β-mannose pentaacetate (β-MAc5) 10%, α-fructose pentaacetate (α-FAc5) 6%, β-fructose pentaacetate (β-FAc5) 15% (FIG. 9).

(Example 7-9)
In this example, the effect of pressure was examined with the synthesis conditions set to no catalyst, a temperature of 200 ° C., and a residence time of 9.0 seconds. First, pure water is sent at a flow rate of 5.0 ml / min to the apparatus in which the main body (main part) of the flow-type high-temperature and high-pressure reactor shown in FIG. 7 is installed in the flow-type high-temperature and high-pressure fluid in situ infrared spectrometer shown in FIG. Submerged and set to a temperature of 200 ° C. and a predetermined pressure of 2 MPa, 5 MPa or 15 MPa to obtain subsupercritical water. Thereafter, toluene was added as an internal standard (5 mol% of the substrate) and acetic anhydride was fed from the pump 6 and a 33 wt% saturated aqueous glucose solution was fed from the pump 7 so that the mixed solution became 1.0 ml / min (mixed) Later glucose concentration: 0.36 mol / kg, glucose / acetic anhydride = 1/30 mol equivalent).

  1 ml of the aqueous solution discharged from the back pressure valve 30 minutes after the substrate feeding was collected. When the internal volume of the pipe from the heating furnace to the back pressure valve outlet was the reaction volume, the reaction time was 9.9 seconds. 1 ml of acetone was added to 1 ml of the collected aqueous solution and shaken, and composition analysis was performed using a GC / MS analyzer (HP 6890 manufactured by Hewlett Packard, column HP-5, inlet temperature 150 ° C., initial column temperature 60 ° C. (retention time) 2 minutes), temperature rising rate 10 ° C./min, final column temperature 250 ° C. (holding time 2 minutes)), and the obtained mass spectrum was confirmed by the Willy database with a concordance of 90% or more. . In addition, quantitative analysis and qualitative analysis in the case where there are commercially available reagents are GC-FID (GC6890 manufactured by Agilent, column DB-WAX, inlet temperature 230 ° C., split ratio 5.61, initial column temperature 50 using toluene as an internal standard. C. (retention time 0.5 minutes), temperature increase rate 20 ° C./min, final column temperature 230 ° C. (retention time 20 minutes)).

  As a result, the conversions were all 99%, which were almost the same as the total yields of 56%, 62% and 62%. The products are the same α-glucose pentaacetate (α-GAc5), β-glucose pentaacetate (β-GAc5), α-mannose pentaacetate (α-MAc5), β-mannose pentane as in the case of the temperature dependence study. Acetate (β-MAc5), α-fructose pentaacetate (α-FAc5) and β-fructose pentaacetate (β-FAc5) were produced, and the effect due to pressure was hardly observed (FIG. 10).

(Examples 10-19)
In this example, the effect of the amount of acetic anhydride was examined with the synthesis conditions set to no catalyst, temperature 200 ° C., pressure 5 MPa, and residence time 9.0 seconds. First, pure water is sent at a flow rate of 5.0 ml / min to the apparatus in which the main body (main part) of the flow-type high-temperature and high-pressure reactor shown in FIG. Submerged and set to a predetermined temperature and a pressure of 5 MPa to obtain subsupercritical water. Thereafter, toluene was added as an internal standard (5 mol% of the substrate) and acetic anhydride was fed from the pump 6 and a 33 wt% saturated aqueous glucose solution was fed from the pump 7 so that the mixed solution became 1.0 ml / min (mixed) Later glucose concentration: 0.01-0.54 mol / kg).

  1 ml of the aqueous solution discharged from the back pressure valve 30 minutes after the substrate feeding was collected. When the internal volume of the pipe from the heating furnace to the back pressure valve outlet was the reaction volume, the reaction time was 9.9 seconds. 1 ml of acetone is added to 1 ml of the collected aqueous solution, shaken, and composition analysis is performed using a GC / MS analyzer (HP 6890, Hewlett Packard, column HP-5, inlet temperature 150 ° C., initial column temperature 60 ° C. (retained) Time 2 minutes), temperature rising rate 10 ° C./min, final column temperature 250 ° C. (holding time 2 minutes)), and the mass spectrum obtained was confirmed by the Willy database with a concordance of 90% or higher. did. In addition, quantitative analysis and qualitative analysis in the case where there are commercially available reagents are GC-FID (GC6890 manufactured by Agilent, column DB-WAX, inlet temperature 230 ° C., split ratio 5.61, initial column temperature 50 using toluene as an internal standard. C. (retention time 0.5 minutes), temperature increase rate 20 ° C./min, final column temperature 230 ° C. (retention time 20 minutes)).

5.5, 10, 15, 20, 25, 30, 35, 40, 45, 50 molar equivalents. As a result, 15 molar equivalents gave a conversion of about 99% and the total yield was 20 molar equivalents. 36% nearby
Subsequent 25 equivalents improved slightly to 54%, and 50 molar equivalents to 83% (FIG. 11). α-glucose pentaacetate (α-GAc5), β-glucose pentaacetate (β-GAc5), α-mannose pentaacetate (α-MAc5), β-mannose pentaacetate (β-MAc5), α-fructose pentaacetate ( α-FAc5) and β-fructose pentaacetate (β-FAc5) were produced. Selectivities up to around 20 molar equivalents, α-GAc5, β-GAc5, α-MAc5, α-FAc5 decreased with increasing amount of acetic anhydride, but all pentaacetates increased above 20 molar equivalents. (Fig. 12)

(Examples 20-22)
In this example, the effect of the inorganic salt was examined with the synthesis conditions set to no catalyst, temperature 200 ° C., pressure 5 MPa, and residence time 9.0 seconds. First, pure water is sent at a flow rate of 5.0 ml / min to the apparatus in which the main body (main part) of the flow-type high-temperature and high-pressure reactor shown in FIG. 7 is installed in the flow-type high-temperature and high-pressure fluid in situ infrared spectrometer shown in FIG. Submerged and set to a predetermined temperature and a predetermined pressure to obtain subsupercritical water. Thereafter, acetic anhydride to which toluene was added as an internal standard (5 mol% of the substrate) was added from the pump 6, and a 33 wt% saturated aqueous glucose solution (glucose / inorganic salt = 1/1 mol equivalent) in which the inorganic salt was dissolved was pump 7. The solution was fed so that the mixed solution was 1.0 ml / min (glucose concentration after mixing: 0.36 mol / kg, glucose / acetic anhydride = 1/35 mol equivalent).

  1 ml of the aqueous solution discharged from the back pressure valve 30 minutes after the substrate feeding was collected. When the internal volume of the pipe from the heating furnace to the back pressure valve outlet was the reaction volume, the reaction time was 9.9 seconds. 1 ml of acetone is added to 1 ml of the collected aqueous solution, shaken, and composition analysis is performed using a GC / MS analyzer (HP 6890, Hewlett Packard, column HP-5, inlet temperature 150 ° C., initial column temperature 60 ° C. (retained) Time 2 minutes), temperature rising rate 10 ° C./min, final column temperature 250 ° C. (holding time 2 minutes)), and the mass spectrum obtained was confirmed by the Willy database with a concordance of 90% or higher. did. In addition, quantitative analysis and qualitative analysis in the case where there are commercially available reagents are GC-FID (GC6890 manufactured by Agilent, column DB-WAX, inlet temperature 230 ° C., split ratio 5.61, initial column temperature 50 using toluene as an internal standard. C. (retention time 0.5 minutes), temperature increase rate 20 ° C./min, final column temperature 230 ° C. (retention time 20 minutes)).

  When lithium chloride, sodium chloride, and potassium chloride were used as inorganic salts, the conversion rates were 90%, 99%, and 98%, respectively, and the overall yields were 69%, 92%, and 77%, respectively. It was done. In addition to the overall yield improvement, surprisingly, the selectivity changed significantly. The selectivity is α-glucose pentaacetate (α-GAc5) 26%, 24%, 21%, β-glucose pentaacetate (β-GAc5) 28%, 38%, 30%, α-mannose pentaacetate (α-MAc5). ) 13%, 16%, 14%, β-mannose pentaacetate (β-MAc5) 8%, 9%, 8%, α-fructose pentaacetate (α-FAc5) 0%, 1%, 2%, β- Fructose pentaacetate (β-FAc5) was 0%, 5%, and 4% (FIG. 13).

  For comparison, selectivity α-GAc5 20% when the maximum value is obtained when the inorganic salt is not converted (temperature 200 ° C., pressure 5 MPa, residence time 9 seconds, glucose / acetic anhydride = 1/50 molar equivalent), β-GAc5 19%, α-MAc5 19%, β-MAc5 11%, α-FAc5 5%, β-FAc5 9% compared to α-MAc5, β-MAc5, α-FAc5, β-FAc5 The selectivity decreased and the selectivity of α-GAc5 and β-GAc5 improved. There was a tendency for the production of β-isomer to be better than that of α-isomer.

  The reaction mechanism estimated from the above results is shown in FIG. In general, in sugars such as glucose and mannose, α-form and β-form are interconverted via aldose by epimerization. However, at the aldose-ketose rearrangement from aldose, ketose is produced and is associated with fructose. Considering from this reaction mechanism, mannose production is a specific result of going through the same aldose intermediate, indicating the possibility of converting an inexpensive sugar to a high added value as a process. On the other hand, the effect of the inorganic salt is that the selectivity is in the order of β-glucose> α-glucose, and since the inorganic salt is dissolved in the subcritical water, it is acylated in a state in which the sugar is hardly dissolved. It is considered that the reaction is close to normal acylation without the specificity of.

  From the above examples, it was revealed that an acyl compound of a saccharide can be synthesized in a high yield without using a catalyst with high-temperature and high-pressure water as a reaction solvent. After acylation of saccharides, water is injected into the recovered aqueous solution and decanted, and after separation into an oil / water bilayer solution, an oil layer containing saccharide acyl compounds is separated and recovered, while acetic acid and It became clear that a simple continuous separation method for separating and recovering water by azeotropic distillation could be constructed.

  As described above in detail, the present invention provides a method for synthesizing an acyl compound of a saccharide without using an organic solvent from a carboxylic acid anhydride and a saccharide using a high-temperature and high-pressure fluid as a reaction solvent, and a reaction composition thereof. In the conventional method, synthesis of an acyl compound of a saccharide from a saccharide and a carboxylic acid anhydride required a reaction for several hours by adding a catalyst to an organic solvent. By using a fluid / supercritical fluid, it becomes possible to synthesize acyl compounds of saccharides continuously at a high speed without using a catalyst and without using an organic solvent. This brings about the merit that acyl compounds of saccharides useful as fragrances, pharmaceuticals, and foods can be continuously produced in large quantities in a short time.

  After acylation of saccharides, water is injected into the recovered aqueous solution and decanted, and after separation into an oil / water bilayer solution, an oil layer containing saccharide acyl compounds is separated and recovered, while acetic acid and By a simple continuous separation method in which water is separated and recovered by azeotropic distillation, glacial acetic acid and water can be separated and water can be recycled. From these facts, it is possible to compress the initial cost and running cost of the process by simplifying the synthesis / separation process. Furthermore, post-treatment of the neutralization treatment is unnecessary, and environmentally conscious production becomes possible. INDUSTRIAL APPLICABILITY The present invention can replace existing production processes as a new mass production process for saccharide acyl compounds useful as fragrances, pharmaceuticals, and foods.

The acylation of saccharides of saccharides using a catalyst / organic solvent is shown. The post-process flowchart of acylation of the saccharide | sugar using a catalyst and an organic solvent is shown. The post-process flowchart of acylation of the saccharide | sugar using a non-catalyst and a water solvent is shown. A high-temperature high-pressure infrared flow cell is shown. 1 shows a flow-type high-temperature and high-pressure fluid in-situ infrared spectrometer used in the examples. 1 shows a high temperature and high pressure flow cell without a window. The main part of the flow-type high temperature / high pressure reactor used in the examples is shown. The temperature dependence in the acylation of the saccharide | sugar in an Example is shown. The product distribution by the temperature in acylation of the saccharide | sugar in an Example is shown. The pressure dependence in acylation of the saccharide | sugar in an Example is shown. The effect of the amount of acetic anhydride in the acylation of the saccharide in an Example is shown. The product distribution with respect to the acetic anhydride amount in acylation of the saccharide | sugar in an Example is shown. The salt dependence in acylation of the saccharide | sugar in an Example is shown. The presumed reaction mechanism in the acylation of the saccharide | sugar in the case of an Example is shown.

Explanation of symbols

1 Tee or cloth (one side opening φ4mm threaded)
2 φ4mm × 5.0mmL hexagonal screw 3 Male screw with one ring ferrule 4 SUS316 tube 5 Water feed pump 6 Reactant feed pump 7 Reactant feed pump 8 Cooling flange (cooling water circulates)
9 Water Heating Coil 10 Reactant Introduction Pipe 11 Temperature Sensor 12 Temperature Sensor Case 13 Furnace Body 14 High Temperature and High Pressure Flow Cell (Tee Type for Normal Temperature Increase, Cross Type for Rapid Temperature Increase)
15 ZnSe window 16 Piping 17 Discharge piping 18 Tee 19 Back pressure valve 21 Aqueous solution 22 Washing water 23 Aqueous solution pump 24 Cleaning pure water feed pump 25 Furnace heating system 26 Furnace 27 High-temperature high-pressure infrared flow cell 28 Cooling water (inlet) )
29 Cooling water (exit)
30 Back pressure valve 31 Drained aqueous solution receiver 32 Movable mirror 33 Movable mirror 34 Interferometer 35 Light source 36 Infrared laser
37 MCT receiver 38 TGS receiver 39 Analysis monitor
40 SUS316 tube 41 cap 42 temperature sensor 43 union

Claims (12)

  A reaction composition of a carboxylic anhydride and a saccharide, wherein there is no remaining catalyst and organic solvent, and the saccharide acyl compound composition.   A method of synthesizing an acyl compound of a saccharide from a carboxylic anhydride and a saccharide, using a subcritical or supercritical fluid in a high temperature and high pressure state as a reaction solvent, and one step from the carboxylic anhydride and the saccharide without using a catalyst. A method for producing an acyl compound of a saccharide comprising synthesizing an acyl compound of a saccharide by the synthesis reaction of   The method according to claim 2, wherein subcritical or supercritical water in a high temperature and high pressure state is used as a reaction solvent.   The method according to claim 2, wherein a monosaccharide, a disaccharide or a polysaccharide is used as the saccharide.   The method according to claim 2, wherein a subcritical fluid or supercritical fluid having a temperature of 100 to 400 ° C and a pressure of 0.1 to 40 MPa is used as a reaction solvent.   The method according to claim 2, wherein water, acetic acid, other inorganic solvent, an organic solvent, or a mixed solvent of an inorganic solvent and an organic solvent is used as the subcritical fluid or supercritical fluid.   The method according to claim 2, wherein the reaction is carried out after dissolving or dispersing the saccharide and mixing with carboxylic anhydride at room temperature.   The method according to claim 2, wherein a high-value-added acylated sugar is produced by simultaneous acylation while converting from an inexpensive sugar to a high-functional and high-value-added sugar.   The method according to claim 2, wherein the selectivity is changed by adding an inorganic salt to the saccharide.   The method according to claim 2, wherein the synthesis reaction is carried out by introducing a substrate and a reaction solvent into a flow-type high-temperature and high-pressure apparatus and changing the reaction time in the range of 3 to 60 seconds.   Water feed pump for feeding water, coil for water heating, high-temperature and high-pressure flow cell, reactant feed pump for feeding substrate, furnace body, reactant introduction pipe for introducing reactant into the furnace body, discharging reaction solution An apparatus for synthesizing acyl compounds of sugars, comprising a drain line for cooling, a cooling flange, and a back pressure valve for setting pressure.   3. The method according to claim 2, wherein after acylation, water is injected into the recovered aqueous solution and decanted, and after separation into an oil / water bilayer solution, an oil layer containing an acyl compound of a saccharide is separated and recovered, while an aqueous layer A simple continuous separation method that separates and recovers acetic acid and water by azeotropic distillation.

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