JPH01305096A - Production of powdery fatty acid ester of sucrose - Google Patents

Abstract

PURPOSE:To industrially and conveniently obtain the high-quality powdery subject compound by adjusting pH of a specific reaction mixture containing a fatty acid ester of sucrose, etc., at the pH within the neutral region, adding a neutral salt, etc., washing resultant precipitates with an acidic water, neutralizing the precipitates and spray-drying the neutralized precipitates. CONSTITUTION:Water is added to a reaction mixture, containing a fatty acid ester of sucrose, unreacted sucrose, unreacted fatty acid methyl ester, catalyst, soap, fatty acid and volatile substance and obtained by a solvent method preferably in a ratio of water : reaction mixture=20:1 (by weight) to adjust a pH to 7.5. This is kept at a temperature of 50-80 deg.C and a neutral salt and sucrose are added to carry out salting out. Temperature-controlled acidic water such as hydrochloric acid is then added to adjust pH to 3.0-5.5 and the temperature to 10-40 deg.C. The resultant precipitates are washed while being finely divided in a dispersion mixer, etc., to afford a purified slurry product of 40-96% solid content. The obtained product is adjusted to the pH of neutral range and spray- dried utilizing a rotary disc to afford the aimed compound.

Description

[Detailed description of the invention] [Industrial application field]

The present invention relates to an industrial method for producing powdered sucrose fatty acid ester. More specifically, the present invention relates to a method for industrially producing powdered high-quality sucrose fatty acid ester without using an organic solvent for purification.

[Conventional technology]

(Background) Currently, sucrose fatty acid esters (
Hereinafter (abbreviated as (SE)), sucrose and C8~
022 with higher fatty acid methyl ester in a solvent (dimethylformamide, dimethyl sulfoxide, etc.) under an appropriate catalyst (solvent method: Japanese Patent Publication No. 35-1310
2) Alternatively, sucrose and fatty acid soap can be made into a molten mixture using water without using a solvent, and then reacted with higher fatty acid methyl ester in the presence of a catalyst (water medium method: Japanese Patent Publication No. 51
-14485). However, in both of these two synthetic methods, in addition to the target SE, the reaction mixture contains unreacted sugars, unreacted fatty acid methyl esters, residual catalysts, soaps, free fatty acids, and volatile components. Among these impurities, impurities whose content exceeds the specified amount must be removed before becoming a product, especially among the above-mentioned impurities. Removal of the residual solvent (volatile matter) associated with the latter solvent method is extremely important as it has become increasingly difficult to use ready-made products51). According to the US FDA standards, the allowable residual dimethyl sulfoxide during SE is 2 ppm or less (Fed
,Regist,, 51(214), 40180-1
). By the way, the purification means conventionally used for purifying SH through both of the above methods is the use of a solvent, but the use of this solvent brings about many industrial disadvantages as described below. ■ Risk of explosion or fire. ■ Explosion-proofing of electrical equipment in preparation for ■ above. ■ Seal the manufacturing equipment in preparation for the above ■. ■ The entire building will be made into a fire-resistant structure in preparation for ■ above. ■ Increase in fixed costs due to ■, ■, and ■ above. ■ Increased cost due to solvent wastage. ■ Negative effects due to residual solvent remaining in product SE. ■ Employee 1! This has a negative impact on the floor, which in turn increases the number of people talking and increases costs. Under these circumstances, there has been a pressing need in the industry to develop a purification technique that makes it unnecessary to use a purification solvent during SE purification. (Problems with the Prior Art) Therefore, purification methods that do not use organic solvents have been studied. For example, (1) SE precipitation method using an acidic aqueous solution (British Patent No. 809,815 (1959)
)) (2) A method of precipitating SE using a general neutral salt aqueous solution (Japanese Patent Publication No. 42-8850) is known. However, when, for example, an aqueous hydrochloric acid solution is added to the reaction mixture as in method (1), the SE will immediately precipitate, but the unreacted Si! L sugar is easily decomposed and converted into glucose and fructose, and decomposition cannot be avoided even if it is carried out at low temperatures (0 to 5°C). This makes it difficult to recover and reuse unreacted viscosity. Furthermore, even if an aqueous solution of a neutral salt such as monosalt or mirabilite is added to the reaction mixture as in method (2), SE will immediately precipitate. In this case, unreacted sugars do not decompose, but the monoester, which is a useful component in SE, is dissolved in the aqueous phase, which not only causes a large loss but also increases the It becomes a hindrance when you want to get SE. According to the more recent Japanese Patent Application Laid-open No. 51-29417, a mixed solution of water and a "purified solvent" (especially referred to as such to distinguish it from a reaction solvent) is formed into a light liquid layer (upper layer) and a heavy liquid layer (lower layer).
The property of phase separation is utilized. That is, since the heavy liquid layer (lower layer) generally contains a large amount of water, hydrophilic unreacted sugars, catalyst-derived salts, etc. are dissolved in this heavy liquid layer (lower layer). On the other hand, since the light liquid layer (upper layer) contains a large amount of purified solvent, substances with low polarity such as SE, fatty acids, and unreacted fatty acid methyl esters are dissolved in this light liquid layer. However, reaction solvents such as dimethyl sulfoxide dissolve in the lower heavy liquid layer, but unfortunately they also dissolve in the upper light liquid layer, so it is impossible to completely separate the reaction solvent using this method alone. It is. Therefore, a very large amount of purified solvent is required just for the purpose of removing trace amounts of reaction solvent. Thus, in order to make purification of crude SE using water industrially possible, it is essential to develop a purification method that completely removes the solvent and does not cause loss of sugar or product SH. Next, what should be considered in order to make purification using water industrially possible is the means for drying the water-containing SE that is associated with using water as the purification solvent. That is, the water-containing SE to be dried is usually in the form of an aqueous solution if it has a water content of 80% or more, and in the form of a slurry if it has a water content of less than 80%. The viscosity of these SH hydrates generally increases rapidly from around 40°C and reaches the highest value around 50°C, but the viscosity rapidly decreases when the temperature exceeds 50°C, which is a very unique viscosity behavior. (Published by Applicant Company (Sugar Ester Story), p. 108) In addition, it is virtually impossible to simply heat under vacuum to evaporate water due to the significant foaming property. If the heating temperature is high and the contact time with the heating element is long. SE causes decomposition and not only causes strong coloring and caramelization, but also increases the acid value due to fatty acids liberated by 1 decomposition (see #Publication No. 37-9! 38B). Especially in the final stage of water evaporation, the characteristic of SH having a low softening point or melting point (for example, the softening point of sucrose monostearate is around 52°C, and the melting point of tI!! distearate is around 110°C) Therefore, SE itself has a tendency to retain residual water, which makes dehydration extremely difficult. In addition, compared to the solvent, the Hs heat of evaporation of water is abnormally high (500 Kcal/Kg-H20 or more);
Also, the high evaporation temperature is one of the reasons why drying is difficult. Therefore, even if a so-called flash dryer is used as another type of drying method, in which slurry is heated and continuously supplied to and discharged from a vacuum chamber, the large latent heat of water does not allow sufficient drying. Dehydration and drying are fraught with various difficulties,
Even if these difficulties could be overcome, since the SE is in a molten state after being dehydrated and dried under vacuum, it must be taken out of the dryer and cooled by blowing cold air or the like to below its melting point. It requires many steps, including solidification and finally pulverization in a pulverizer, and the final pulverization step is accompanied by concerns about dust explosions. Therefore, solving one or more of the problems associated with drying is also an important step in realizing the present medium method purification.

[Division WJ that the invention seeks to solve]

In view of the above circumstances, the present invention provides a purification method that substantially eliminates loss of SE, even without using a purification solvent, when purifying crude SE synthesized by a solvent method, and a method that eliminates the risk of quality deterioration during the drying process. The aim is to solve all the problems caused by the use of solvents by developing drying means that are free of solvents. (Concept of the Invention) Therefore, the present inventor has proposed (a) not only to minimize the amount of SE dissolved in the aqueous phase side, but also to set the amount to zero and precipitate the entire amount of SE if possible; As a result of conducting many salting-out experiments with the goal of solving the following three points: avoiding decomposition of unreacted sugar, and (c) separating the remaining reaction solvent from SE by dissolving it outside the aqueous phase. When sorghum and a neutral salt are dissolved in an aqueous solution of the reaction mixture, under the appropriate combination of pH 1 temperature, concentration of the neutral salt and sucrose, and amount of water, not only almost the entire amount of SE will precipitate. Surprisingly, we discovered a convenient phenomenon in which the reaction solvent was dissolved in the aqueous phase in addition to the unreacted axes. Therefore,
Taking advantage of this phenomenon, after dissolving the precipitated SE in water again,
By repeating the precipitation operation with a neutral salt and sucrose aqueous solution, the remaining volatiles (residual reaction solvent) can be completely transferred into the aqueous phase while virtually preventing loss of SE; , Furthermore, neutral salts and salts accompanying the precipitated SE are substantially removed by washing the precipitate with acidic water of an appropriate pH, and purified SE is obtained; It has been found that by spray drying the slurry of SE precipitated above, powdered SE can be produced continuously without any loss in quality. (Summary) The present invention is based on the above discovery, and includes a reaction mixture containing unreacted sugar, unreacted fatty acid methyl ester, catalyst, soap, fatty acid, and volatile components in addition to the target SiW sugar fatty acid ester. , water, neutral salt and salt at a pH in the neutral range.1.
The gist of the present invention is a method for producing a powdered sucrose fatty acid ester, which is characterized in that a precipitate produced by adding i-sugar is washed with acidic water, neutralized, and then spray-dried. below. Discusses various matters related to inventions. (Synthesis of SE by a solvent method) In the synthesis of SH by a solvent method, a mixture of sucrose and fatty acid methyl ester is usually added and dissolved in a reaction solvent, such as dimethyl sulfoxide, in an amount several times the total amount of these. It can easily be heated to 90°C by keeping it at 80°C to 90°C for several hours in a vacuum of 20 to 30 Torr in the presence of an alkaline catalyst such as potassium carbonate (K2COs).
SE at a reaction rate of % or more (based on fatty acid methyl ester)
A reaction mixture forms. Next, in order to eliminate the activity of the alkaline catalyst in the SE reaction mixture, an equivalent amount of an organic acid such as lactic acid or acetic acid or a mineral acid such as hydrochloric acid or sulfuric acid is added to the SE reaction composition. This neutralization converts the catalyst into a potassium salt such as potassium lactate. Finally, the reaction solvent, such as dimethyl sulfoxide, is distilled off under vacuum, resulting in a composition (reaction mixture after neutralization and 7A distillation) approximately having the following composition range. Sucrose fatty acid ester = 15-92% unreacted sugar
= 1.0-80% unreacted fatty acid methyl ester = 0.5-10% neutral salt derived from potassium carbonate
= 0.05-7% stone wine =1.
0-10% fatty acid = 0.5-1O
% volatile content (residual reaction solvent) = 5.0-30% At this time, the ester distribution of SE is monoester 10-75%
(Diester or higher is 90 to 25x). The fatty acid radicals mainly contained in each of the fatty acid methyl ester, the fatty acid, and the fatty acid are saturated and have a common carbon number of CI6 to C22. (Addition of water) Next, water was added to the above reaction mixture, water: reaction mixture = 5:1 to 40:1 (weight ratio)... (1
) More preferably, the ratio is as follows. Water: Reaction mixture = 20: 1 (weight ratio)...
- Add to the ratio of formula (2) and adjust the pH to 8.2~
8.2. The pH is preferably 7.5. In this case, the water addition ratio is outside the above range. For example, if the ratio of water to reaction mixture is less than 5, the resulting aqueous solution will have a high viscosity, making subsequent operations substantially difficult. On the other hand, if too much water is added so that the ratio of water to reaction mixture exceeds 40, the viscosity will decrease and subsequent operations will be easier, and the desired reaction solvent will be Although removal is carried out suitably, on the other hand, a large amount of energy cost is required to remove water when recovering unreacted sugars, etc., resulting in a loss of economic efficiency. Furthermore, the pH of the aqueous solution is preferably adjusted between pH 6.2 and 8.2 in order to avoid decomposition of the target SE. At a hydrogen ion concentration of pH 8.2 or higher, quantitative alkali-based There is a concern that SE decomposition will occur,
Furthermore, even in a weakly acidic region of pH 8.2 or less, there is a risk of acid decomposition if exposed to high temperatures of 30° C. or higher, for example. (Salting out) As above <pH; II! ! The aqueous solution of the prepared SE reaction mixture is kept preferably at 50-80°C, and neutral salt and sucrose are further added. In this case, the neutral salt to be added is
First, it is preferable that the following formula (3) is satisfied. =0.015~0.12 (weight ratio)・・・・・・・・・
(3) Here, total base amount = amount of neutral salt to be added + amount of bases formed from catalyst (4) Total amount of sugar = amount of sucrose to be added + Amount of unreacted sugar from the beginning...
(5) Next, the amount of sucrose to be added is preferably determined by the following formula (6). = 0.025 to 0.20 (weight ratio)...
...(6) Furthermore, in addition to both of the above equations, it is preferable that the ff1fit ratio of the total base amount and the total axial amount also satisfy the following equation (7). The present inventors obtained S
When an aqueous solution containing precipitated H is heated to a temperature of 50 to 80°C, even if the composition of volatile matter (residual reaction solvent) contained in the SE reaction mixture varies greatly from 5.0 to 30.0%. It has been found that approximately the entire amount of SE is precipitated no matter how large the amount of SE is. This phenomenon is a unique phenomenon and has an important value for the purpose of the invention. The attached ttS1 diagram is a ternary graph showing this phenomenon in more detail. In this figure, the weight of SH dissolved in the aqueous phase = Y [gl, the weight of precipitated SH = X [gl Total S E (X + Y) [gl] If the weight percentage of SE present = φ [%], then φ is defined by the following formula (8). Here, the following conditions: Temperature = 80°C, pH -7.5° Water: Reaction mixture = 7.4: 1 (weight ratio) Fatty acid residue = Stearic acid Composition of the reaction mixture Sucrose fatty acid ester = 23% Reacted sugar; 35% Unreacted fatty acid methyl ester = 2% Salt derived from catalyst = 1% Soap 23% Fatty acid = 1% Volatile matter (residual reaction solvent) = 29% Ester distribution in SE: Monoester F 3% diester Above = 27%, how the value of φ changes is shown by triangular coordinates. Here, the total salt is the amount defined by the formula (4), and the total sugar is the amount defined by the formula (5), respectively, and they are expressed as water amount, total base amount, and total lees amount = 100%. The shaded part in Figure 1 is the formula (3) discovered by the inventors.
)1 is an area that simultaneously satisfies equations (8) and (7). By determining the amount of dissolved neutral salt and sucrose that falls within this shaded area, it is possible to precipitate substantially φ=O, that is, approximately the entire amount of SE, and the precipitated SE can be collected by filtration. Or, by centrifugation, volatiles dissolved in the aqueous phase (
(residual reaction mixture) can be completely separated (that is, contaminating volatile components can be completely removed). (Washing) After the above salting-out operation, pH-3.0 to 5.5. temperature 10
The separated SE cake described above is washed using acidic water whose temperature is adjusted to about 40°C. The acid used for this is, for example, 11! Acid, mineral acids such as sulfuric acid, and organic acids such as acetic acid and lactic acid are suitable, but are not limited to those exemplified in the side column. By washing under such conditions, desired impurities can be transferred to the aqueous phase while minimizing the amount of SE redissolved from the cake side to the aqueous phase. When the temperature of the acidic water exceeds 40°C during the above-mentioned cleaning operation, if the operation is continued for a long time, for example, several months, there is a risk that the SE will not only be decomposed by the acid, but also that the viscosity will increase. Operation becomes difficult. On the other hand, maintaining a low temperature of 10° C. or less requires a refrigerator that is not economical. Therefore, it is usually preferable to operate at 10 to 40°C, particularly around room temperature. In addition, when washing the SE cake with this acidic water, 1
It is necessary to remove from the SE cake as much as possible the volatile components (reaction solvent) contained in this cake, unreacted sugars, added neutral salts, and salt surroundings produced by neutralization of the catalyst. Therefore, it is desirable that the SE cake be shredded in the acidic water to the smallest possible particle size.
Homo mixer)), homogenizer or colloid mill (
For example, this can be efficiently achieved using a fragmentation device such as the product name (Mycolloider), and volatile matter (reaction solvent), unreacted sugar,
The salts and neutral salts from the catalyst are transferred from the cake of precipitated SE into the acidic aqueous phase. However, although it is said to be a substantially small amount, it is inevitable that some SE will elute into the acidic aqueous phase. Therefore, it can be effectively suppressed by relatively increasing the diester or triester content. The above-mentioned washing of the SE cake with acidic water becomes more complete by increasing the number of washings and increasing the amount of washing water, thus making it possible to obtain purified SE that is virtually pure. (Slurry concentration) The water-containing SE purified in this way is slurry-like, but as it is, the pH is biased toward the acidic side, so the slurry is adjusted to have a pH near neutrality. does not contain unreacted sugars, salts originating from the catalyst, volatile components, and sucrose and neutral salts added during salting out, but S
E contains unreacted fatty acid methyl ester, stone and fatty acid surroundings, and often has a solid content of 1 to 50% and a water content of 99 to 50%. The amount of solids in this slurry is preferably about 40% or less for drying purposes, which will be described later.However, an excessively small amount of solids is undesirable from the viewpoint of energy costs for drying, and is usually , a value of 4% or more is economical. (Spray Drying) In the present invention, a spray drying method is particularly used for drying the SE slurry. The usefulness of this drying means is 1. The present inventor has found from numerous experiments that it is the most suitable method for dehydrating and drying SE slurry having a solid content of 40 to 86%. Incidentally, as mentioned above, Tokogl? Also when using a regular vacuum dryer such as a groove-type agitation dryer. Also, the slurry is continuously supplied, heated and discharged into the vacuum chamber. Even when using a so-called flash dryer, SE
Because of its viscosity characteristics and low melting point,
It is impossible to avoid quality deterioration phenomena such as an increase in acid value, coloration, and caramelization, and in the latter case, the risk of powder explosion cannot be ignored. However, by employing the spray drying means discovered by the inventor, the drawbacks of the existing drying means can be solved at once. In the drying process of the present invention, the hydrous sucrose fatty acid ester in the form of a slurry is continuously supplied to the spray drying tower via a pump, and is turned into fine atomized particles by spraying from a nozzle or centrifugal force from a rotating disk. Divide and contact with drying air stream. This significantly increases the area for water evaporation, which results in dehydration within an extremely short period of time (within a few seconds after spraying). Drying may be completed. Note that as the atomization means, it is desirable to use a rotating disk because the viscosity of the hydrous sucrose fatty acid ester is high. (Spray drying conditions) The supply temperature of the sucrose fatty acid ester solution or slurry was 40°C.
Although the temperature can be changed arbitrarily between 80° C. and 80° C., it is preferable to select a temperature within the range of 40° C. to 60° C. from the viewpoint of quality. When the above solution or slurry is atomized by a rotating disk 1 For example, when the diameter of the disk is 5 to 10 c + mφ, 15.0
A rotational speed of 00 to 24,000 rpm+ is suitable. The air blown into the tower should have more than the amount of heat needed to evaporate the water in the solution or slurry, so if the air temperature is low, a larger amount of air is required. The air temperature at this time may be in a wide range of 10 to 100°C, but it is advantageous to select a temperature between 60 and 80°C in consideration of drying efficiency and prevention of thermal decomposition of the target sucrose fatty acid ester. be. The humidity in the blown air is also related to the drying efficiency along with the air temperature. The absolute humidity suitable for work is approximately: Absolute humidity = o, ooa ~ 0.05 kg ° water kg /
Although the range is for dry air, it is especially economical to use the following range: absolute humidity = 0.01 to 0.04 Kg° water/dry air. When the solid content concentration in the slurry sent to the spray drying tower exceeds 40%, the viscosity increases significantly, and as a result, the particle size of the sprayed slurry becomes relatively large, which slows down the drying of the water. As a result, it tends to adhere to the inner wall of the drying tower. Therefore, it is better to adjust the solid content concentration in the slurry to 40% or less. If the solid content concentration of the slurry is 40% or less, the diameter of the sprayed droplets will be smaller than if it exceeds 40%.
Since it becomes easier to dry, there is no fear of it adhering to the inner wall of the drying tower. However, if the solid content concentration of the slurry is, for example, 3%
If the size is less than 1, drying becomes easier, but it is uneconomical in terms of the energy required. Therefore, the concentration of slurry supplied to the spray drying tower is 4.
A range of % to 40% is suitable. Conditions such as the required volume, required tower length, and required height of the spray drying tower are designed on the premise of the above spray conditions. If the tower design and operating conditions are suitable, powdered dry sucrose fatty acid ester with a moisture content of less than 5% is continuously discharged from the bottom of the spray drying tower. The resulting product has a short thermal history and is of excellent quality, and requires almost no drying personnel.

[Effect]

Unreacted sugar, unreacted fatty acid methyl ester. Catalyst 1 Add acid to the sucrose fatty acid ester producing reaction mixture containing brass, fatty acids, and volatile matter (residual reaction solvent) to adjust the pH to a neutral range, then add water, neutral salts, and sucrose to the appropriate temperature. When salted out at a certain temperature, sucrose fatty acid ester,
Unreacted fatty acid methyl ester, soap, and fatty acid are precipitated, and volatile components (residual reaction solvent) are transferred to the aqueous phase, so that residual volatile components can be removed without using any organic solvent. In particular, by operating so as to satisfy the conditions of formula (3), formula (8), and formula (7), the residual solvent can be removed with virtually no loss of SE. Next, by washing this precipitate with acidic water, impurities such as volatile components, unreacted sugars, added neutral salts, and salts produced by neutralization of the catalyst are removed. A slurry of purified SE is removed. By spray drying this purified slurry, powdered SE with a moisture content of 5% or less is continuously produced.

【Example】

The embodiments and effects of the invention will be explained below using Examples and Comparative Examples, but the examples are of course for explanation and are not intended to limit or limit the idea of the invention. After the reaction solvent was distilled off from the solvent method SE reaction mixture represented by the composition shown in Table 1 below, the residual liquid was neutralized with lactic acid. 2,000 g of water was added to 100 g of the dried material to dissolve it. To this aqueous solution, 82.5 g of sucrose and 97.8 g of 50% potassium lactate were added, heated to 75° C., and the precipitated cake was filtered off to obtain a cake with a solid content of 53%. In addition, SE was not substantially contained in the filtrate. (Left below) Table 1: Distribution of esters: 70% monoester, 30% diester or higher. Add room temperature hydrochloric acid water (pH 3, 5) to the top cake 2. QOO
When g was added, SE was immediately precipitated as a white precipitate. Next, the acidic aqueous solution (pH 3, 5) containing this precipitate was sufficiently stirred with a homomixer (manufactured by Tokushu Kiki Kogyo ■), and then the precipitate was discharged. After adding hydrochloric acid water again to this precipitate and washing it twice, pH 7.5 was added with caustic soda.
The purified cake obtained by adjusting. 1i150.8. The dry product contained 25% solids and had the composition shown in Table 2 below. In addition, washing liquid (i!
! The liquid contained a small amount of SE. Table 2 This slurry was supplied to a pilot spray drying tower while being maintained at 50°C, and was spray dried. The drying conditions are as follows: Diameter of spray drying tower: 2.0-φ Length of straight cylinder part + 1.5 m Rotating disk (disc) diameter: 10 cmφ Disk rotation speed: 2
The temperature of the air entering the garden at 4,00°C was 260°C. The powdered SE obtained from the bottom of the spray drying tower had a moisture content of 1.
81%, bulk ratio i0.41, no coloring due to overheating, and good fluidity. Stable drying! There were no problems such as powder adhering to the internal walls of the spray drying tower, which were initially feared. The amount of monoester in SE was 68% before and after drying.
2, and there was no change in the acid value. The precipitated cake (slurry) with a solid content of 25% obtained in Example-1 was kept at a temperature of 50°C, the inlet air temperature was 40°C, and the slurry feeding rate was 0.5 kg/ Spray drying was performed in the same manner as in the spin-down process, except that the time was changed. The obtained SE grain powder, moisture content 1.82%, bulk specific gravity Q,
42, the fluidity was good, and there was no coloration due to overheating. The amount of monoester in SE was 68%, which remained unchanged before and after drying, and the same was true for the acid value. Furthermore, no SE grain powder was observed to adhere to the inner wall of the spray drying tower.

【Effect of the invention】

As explained above, the present invention has developed a series of techniques for industrially producing powdered purified sucrose fatty acid ester from a crude sucrose fatty acid ester reaction mixture without using an organic solvent for purification. This brings about the following great effects. (1) SE can be purified using only inexpensive water. (2) Since SE can be dried under normal pressure within a short time, there is no thermal deterioration of the product. (3) There is no need to worry about solvent explosion or fire, and therefore there is no need for expensive explosion-proof electrical equipment. (4) There is no concern that the purification solvent will mix into the product. (5) Improve the sanitary environment of the NA field. (6) It can be industrialized at low cost.

[Brief explanation of the drawing]

Figure 1 shows the changes in total water and total salt, and the amount of salt dissolved in the water phase. It is a triangular graph showing the relationship with the amount of fatty acid ester in the morning. Patent applicant No. Kogyo Seiyaku Co., Ltd. Tako 1 Figure 1 Total salt C'l. ) 7 now total jA◆Reimeter = 100

Claims (1)

[Claims] 1. In addition to the target sucrose fatty acid ester, unreacted sugar,
A reaction mixture containing unreacted fatty acid methyl ester, catalyst, soap, fatty acid, and volatile components is adjusted to a pH in the neutral range, and water, a neutral salt, and sucrose are added, and the resulting precipitate is removed with acidic water. A method for producing powdered sucrose fatty acid ester, which comprises washing, neutralizing, and spray drying. 2 The composition of the reaction mixture is: Unreacted sucrose = 1.0-80.0% Unreacted fatty acid methyl ester = 0.5-10.0% Catalyst = 0.05-7.0% Soap = 1. The method according to claim 1, wherein: 0 to 10.0% fatty acid = 0.5 to 10.0% volatile content (residual reaction solvent) = 3.0 to 50.0%. 3. The method according to claim 1, wherein the reaction mixture is adjusted to a pH of 6.2 to 8.2. 4. The method according to any one of claims 1 to 3, wherein the reaction mixture after pH adjustment is heated to 50 to 80°C. 5. The method according to claim 1, wherein the weight ratio of water added to the reaction mixture and the reaction mixture is water:reaction mixture = 5:1 to 40:1. 6. The method of claim 1 or 3, wherein the neutral salt and sucrose are added to the reaction mixture according to the relationship: Total salt amount / (water amount + total salt amount + total sugar amount) = 0.015
~0.12 and total sugar amount/(water amount + total salt amount + total sugar amount) = 0.025
~0.20 and total salt amount/total sugar amount = 0.4 to 0.8 where, total salt amount = neutral salt amount to be added + salt generated by neutralization of catalyst Total sugar amount = addition amount of sucrose to be added + amount of unreacted sugar from the beginning 7 The acid used to adjust the pH of the reaction mixture is lactic acid,
4. The method according to claim 1, wherein the acid is any acid selected from the group consisting of acetic acid, hydrochloric acid and sulfuric acid. 8 The fatty acid radical mainly contained in each of the fatty acid methyl ester, soap, and fatty acid in the reaction mixture has a carbon number of 1.
3. A method according to claim 1 or 2, having from 6 to 22 common saturated fatty acid roots. 9. The method according to claim 1 or 2, wherein the volatile component (residual reaction solvent) in the reaction mixture is dimethyl sulfoxide or dimethylformamide. 10 The neutral salt added to the reaction mixture is common salt, mirabilite,
7. The method according to claim 1, wherein the salt is selected from the group consisting of potassium lactate and potassium acetate. 11 The ester distribution of sucrose fatty acid ester is 10 to 75% as monoester content (diester or more is 8%).
7. The method according to claim 1, 2 or 6. 12. The method according to claim 1, wherein the acidic water has a pH value of 3.0 to 5.5. 13. Claim 1, wherein the temperature of the acidic water is 10 to 40°C.
Or the method described in 12. 14. The method according to claim 1, wherein the slurry of the precipitate to be spray dried has a solid content of 4 to 40% and a moisture content of 96 to 60%. 15 The humidity and temperature of the blown air during spray drying are as follows: absolute humidity = 0.008 to 0.05 [(kg・water)/(k
The method according to claim 1, wherein the temperature is within the range of 10.0 to 100.0°C. 16. The manufacturing method according to claim 1, wherein the composition of the powdered sucrose fatty acid ester of the product is within the following range. Moisture = 0.5-5.0% Unreacted fatty acid methyl ester = 0.5-10.0% Soap = 0.5-60.0% Fatty acid = 0.5-10.0% Sucrose fatty acid ester = 98 .0~15.0%