JP2006305450A - Method and system for crystallizing sterols - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for obtaining crystal of sterols in high yield by highly precisely controlling moisture content in a solvent in a continuous crystallization method. <P>SOLUTION: In this method, an organic solvent solution containing sterols is continuously fed to a column-type crystallization apparatus with a cooling part set at the upper part from the lower part of the apparatus; sterols are crystallized at the upper cooling part and settled; and the organic solvent solution after crystallization of sterols is simultaneously made to flow out of an upper flow-out part; and part of the flowing-out organic solvent solution is mixed with water and then returned to the apparatus. Thus, the moisture content in the solvent can be accurately controlled, and coagulated crystal of sterols with good filtration property can be obtained in high yield. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a method and system for crystallizing sterols. More specifically, the present invention relates to a method and a system for continuously crystallizing sterols using a tower type crystallizer.

Sterols are useful substances known as precursors for vitamins and steroid compounds. For example, ergosterol is a kind of sterol contained in fungi and is a precursor of vitamin D2. These sterols are produced by extraction and purification from biological cells, and in many cases, crystallization (recrystallization operation) is used for purification (see, for example, Non-Patent Document 1).
As the crystallization operation, a cooling crystallization method in which crystals are precipitated by gradually cooling the solution, an evaporation crystallization method in which crystals are precipitated by evaporating the solvent, or the solubility of the solute to be purified in the solution is low. An anti-solvent crystallization method in which a solvent is added is known. Moreover, as an apparatus used for crystallization, in addition to a batch crystallization tank provided with a cooling jacket and a stirring device, a continuous crystallization method using a tower crystallization apparatus is known (for example, Non-Patent Document 2).

  For example, in crystallization of ergosterol, a cooling crystallization method is often used, and it is known that a continuous crystallization method can be used (see, for example, Patent Document 1). Furthermore, there is a method that can obtain an agglomerated crystal with good filterability in a high yield by supplying water in the middle using a water-insoluble solvent, and a continuous crystallization method is also used for this method. It is known that it can be performed (for example, refer patent document 2). Specifically, water is supplied to a water-insoluble solvent by humidifying the gas phase portion.

As another field using the continuous crystallization method, for example, there is a technique regarding an apparatus for continuously crystallizing a crystallization material containing bisphenol A (see Patent Document 3). Specifically, a technique is disclosed in which a part of the mother liquor is circulated through the crystallizer to prevent wasteful heating of the mother liquor and suppress the temperature difference between the inlet and outlet of the cooler.
JP 2002-80493 A International Publication No. 2004/046163 Pamphlet JP 2004-168750 A Supervised by Haruhiko Oya, “High Purity Technology Series Vol. 3, High-Purity Substance Manufacturing Process”, Fuji Techno System, P.A. 429 (1997) JWMullin, "Crystallization (Third Edition)", Butterworth-Heinemann (1993)

  According to Patent Document 2, since water is supplied by humidification, there is an effect that it is possible to prevent a state in which a crystal other than the target is generated due to a temporarily non-uniform liquid phase. Further, according to Patent Document 3, since a temperature difference between the inlet and the outlet of the cooler can be suppressed by circulating a part of the mother liquor, the degree of supersaturation is reduced and the accumulation of scale on the heat transfer surface is suppressed. There is an effect that can be made. Therefore, according to the techniques described in those documents, it is possible to expect a certain improvement in the recovery rate of the target substance for continuous crystallization.

  In Patent Document 3, no consideration is given to obtaining aggregated crystals with good filterability by supplying water. On the other hand, in the method of humidifying the gas phase part described in Patent Document 2, it is difficult to strictly control the amount of water in the solvent.

  On the other hand, the inventor of the present application can easily control the amount of water in the liquid phase and improve the recovery rate with respect to crystallization of sterols, and the liquid phase becomes non-uniform. Attempts were made to further improve the method and apparatus for preventing the occurrence of other crystals.

As a result of various experimental studies on the continuous crystallization method of sterols using a tower-type crystallizer, the present inventor has found a method for supplying moisture to a solvent with high accuracy, and has completed the present invention based on this knowledge. I came to let you. The method and system for crystallizing sterols according to the present invention is characterized in that a part of the organic solvent solution flowing out from the tower-type crystallizer is brought into contact with water and then returned to the apparatus.
(1) The method for crystallizing sterols of the present invention includes:
(A) An organic solvent solution containing sterols is continuously supplied from the lower part of the tower-type crystallizer, and (b) the sterols are crystallized in a cooling unit provided at the upper part of the tower-type crystallizer. (C) In the sterol crystallization method of recovering the crystallized sterols from the lower part of the apparatus, (d) the organic solvent solution after the sterols are crystallized (E) at least a part of the organic solvent solution that has flowed out is brought into contact with water and then introduced again into the tower-type crystallizer. It is characterized by doing.

The present invention preferably further has one or more of the following features.
(2) The organic solvent of the present invention is further a water-insoluble organic solvent having a specific gravity of 0.9 or less.
(3) The organic solvent of the present invention is further characterized by being hexane, heptane, octane or a mixture thereof.
(4) The water to which the spilled organic solvent solution of the present invention is brought into contact is further 40 to 80 ° C. warm water.
(5) The ratio of the amount of liquid returned to the apparatus in the spilled organic solvent of the present invention is further 3% to 30% of the effluent volume.
(6) The crystallization system of the present invention is (a) a supply unit provided at the lower part of the apparatus for continuously supplying an organic solvent solution containing sterols, and (b) provided at the upper part of the apparatus. A cooling part for crystallizing and precipitating the sterols, (c) a recovery part provided at the lower part of the apparatus for recovering the crystallized sterols, and (d) provided at the upper part of the apparatus, A tower-type crystallizer comprising an outflow part for allowing the organic solvent solution after sterols to crystallize to flow out of the apparatus, and the crystallizing system is further connected to the outside of the apparatus (e) And an external reflux unit for introducing at least a part of the discharged organic solvent solution into the apparatus again after contact mixing with water.
(7) The (e) external reflux part of the present invention further comprises:
(E-1) a temperature control unit for controlling the temperature of the mixture and / or
(E-2) a flow rate control unit for controlling a flow rate for introducing the mixture into the apparatus;
It is characterized by including.

  According to the present invention, the amount of water in the solvent can be controlled with high accuracy, whereby sterol aggregates with good filterability can be obtained at a high recovery rate.

  The sterol crystallization method and crystallization system of the present invention will be described in detail based on the following embodiments.

1. Sterols The sterols used in the present invention include cholesterol, desmosterol, 7-dehydrocholesterol, α-sitosterol, β-sitosterol, dihydro-β-sitosterol, γ-sitosterol, stigmasterol, ergosterol, and 22-dihydroergo. Examples include sterols. In the following description, ergosterol is exemplified as one embodiment of the “sterols” of the present invention.

2. Crystallization System An example of a tower-type crystallizer used in the present invention is shown in FIG. The organic solvent solution containing ergosterol is supplied from the nozzle 1 as an embodiment of the “supply unit” of the present invention provided at the lower part of the apparatus. The supplied liquid is cooled when passing through the cooling unit 2 provided in the upper portion, and ergosterol is deposited and settled. The cooling unit 2 includes a cooling jacket. The cooling water flows in from the cooling water inlet 18, passes through the inside of the jacket, and flows out from the cooling water outlet 16. The cooling for depositing ergosterol is not limited to a method using cooling water, and other electrical methods can also be used. About the cooling part 2, in order to prevent the adhesion of the crystal | crystallization to a wall surface, the stirring apparatus with a scraping board can also be provided as needed. The stirrer is controlled by a stirrer motor 10.

  When the crystals generated in the cooling section settle in the apparatus, they are countercurrently contacted with the supply liquid, dissolved and recrystallized repeatedly, and then settled in the lower part of the apparatus. The crystals are discharged from the nozzle 3 as a slurry, and the crystals are recovered by the solid-liquid separator 4. The nozzle 3 and / or the solid-liquid separator 4 function as an embodiment of the “recovery unit” of the present invention.

  On the other hand, the liquid from which ergosterol (or a part thereof) is removed flows out from the upper nozzle (or liquid outlet nozzle) 5 as one embodiment of the “outflow portion” of the present invention. The solution that has flowed out is sent to the next step, but a part of the solution 12 enters the mixing tank 6 and is mixed with water 14 in contact. The mixing means can be performed by, for example, a stirring operation through the stirrer motor 20. Thereby, the solvent dissolves water. Thereafter, the mixed solution that has entered the mixing tank 6 is returned again into the apparatus by the pump 7. By this operation, water is supplied into the apparatus. The mixing tank 6 (including the connection from the upper nozzle 5 to the mixing tank 6) and the pump 7 (including the connection from the pump 7 to the inside of the apparatus) function as an embodiment of the “external reflux section” of the present invention.

3. Organic Solvent As the organic solvent of the present invention, an organic solvent suitable for increasing the degree of purification when the crystal settles in the apparatus and making the shape into an aggregated crystal having good filterability can be used. Examples of organic solvents include hexane, heptane, octane, methyl alcohol, ethyl alcohol, isopropyl alcohol, or mixtures thereof. An appropriate organic solvent can be selected based on, for example, sterols to be crystallized, a required degree of purification, a required crystal shape, or the like.

  In the embodiment, a water-insoluble organic solvent having a specific gravity of 0.9 or less is exemplified. Specific examples include hexane, heptane, octane, or a mixture thereof, and hexane is more preferable. In addition, as the organic solvent, those having a saturated solubility of water of about several hundred ppm at a temperature of 40 to 80 ° C. are preferable in that an appropriate crystal shape as described later can be obtained. Specifically, for example, a saturated solubility of preferably 100 to 1000 ppm, more preferably 100 to 500 ppm is preferable.

4). Control in the external reflux portion In the mixing tank 6, the water to be brought into contact with the organic solvent solution that has flowed out cannot sufficiently contain water in the organic solvent if the temperature is low, and at the same time, the ergosterol in the solution in the mixing tank This causes the problem of precipitation. On the other hand, when the temperature is high, more water can be contained in the organic solvent and returned to the device, but if the amount of water in the device increases too much, the crystal shape of ergosterol changes to a needle shape. Arise. In addition, water-insoluble organic solvents such as hexane, heptane, and octane have an azeotropic point with water. It is about 61 ° C. for hexane, about 79 ° C. for heptane, and about 90 ° C. for octane. Exceeding the azeotropic point is not preferable because water in the mixing tank is lost by evaporation. Accordingly, the water to be brought into contact with the organic solvent in the mixing tank is preferably warm water of 40 to 80 ° C., but a more preferable value varies depending on the solvent. For example, in the case of hexane, 40-60 ° C., which is lower than the above azeotropic point, is a more preferable value.

  The amount of water supplied to the device can be accurately controlled by the temperature of the water and the amount of solution returned to the device. The method for controlling the temperature of water is not particularly limited, and can be achieved, for example, by providing a mixing tank with a temperature-controllable jacket by using a temperature control component such as an electric heater or hot water. These temperature control parts and / or a temperature controllable jacket (or a mixing tank 6 with the jacket) function as an embodiment of the “temperature control unit” of the present invention.

  If the amount of ergosterol solution returning to the apparatus through the mixing tank is too small, the amount of water supplied into the apparatus is insufficient. On the other hand, if the amount is too large, the amount of liquid flowing out from the apparatus will decrease, and the capacity of the apparatus will decrease. Therefore, 3% to 30% of the effluent amount is preferable, and more preferably 5 to 15%. As a method for controlling the flow rate of the ergosterol solution returned into the apparatus, a method using the pump 7 is exemplified in the embodiment. The pump 7 functions as an embodiment of the “flow rate control unit” of the present invention. The embodiment of the “flow rate control unit” is not limited to the pump 7, and means known to those skilled in the art such as a flow rate control valve or a flow rate control valve may be used.

  Although the density | concentration of the ergosterol solution supplied to an apparatus changes with solvents to be used, for example, when using hexane, it is 0.5-20 g / L, Preferably it is 2-10 g / L.

  The supply rate of the ergosterol solution may be appropriately determined according to the capacity of the apparatus and the residence time. If the residence time is too short, the precipitated crystals do not settle well or pass through the apparatus with insufficient precipitation. Conversely, if the residence time is too long, there is a problem that the apparatus becomes too large. A suitable average residence time in the present invention is 10 minutes to 5 hours, preferably 30 minutes to 2 hours.

  Hereinafter, an embodiment of the present invention in the case of using the tower type crystallizer exemplified in FIG. 1 will be described.

Example 1
An ergosterol / hexane solution having a temperature of 60 ° C. and a concentration of 3 g / L was continuously supplied to a tower-type crystallizer having an inner diameter of 40 mm, a height of 630 mm, and an upper cooling part length of 210 mm to crystallize ergosterol. The operation of the crystallizer is performed at a cooling unit jacket (cooling unit 2) temperature of 2 ° C., a crystallizer agitator motor agitation rotational speed of 60 rpm, a liquid supply rate of 10 ml / min from the nozzle 1, and an average residence time of about 60 minutes. It was. The liquid flowing out from the upper nozzle 5 was mixed with 40 ° C. warm water in a mixing tank 6. A sufficient amount of water that does not disappear during the desired crystallization operation is accumulated in the mixing tank 6, but water may be added to the mixing tank 6 as necessary. By this contact mixing, the ergosterol / hexane solution dissolves water. The amount of water to dissolve can be determined based on the saturated solubility of the ergosterol / hexane solution.

  The ergosterol / hexane solution containing water that was contact-mixed in the mixing tank 6 was returned to the apparatus from the lower end of the cooling unit 2 at 1 ml / min using the operation of the pump 7. The amount of moisture returned into the apparatus can be accurately controlled by the temperature of the ergosterol / hexane solution and the operation of the pump 7.

After continuous operation for about 1 hour, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured by HPLC under the conditions described later, and it was 0.67 g / L (ergosterol weight / ergosterol hexane solution amount). The recovery rate of ergosterol at the time point was calculated as 78% (= 100 × (3−0.67) / 3). Further, after continuous operation for 2 hours, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured and found to be 0.99 g / L, and 67% (= 100 × (3-0.99) / 3) of ergosterol was found. It was found that it was recovered. The simultaneous point is the point of 3 hours after the operation, and is generally the time when the operation of the apparatus is expected to be stable according to the residence time of the ergosterol / hexane solution in the apparatus. Further, 30 minutes later, when the ergosterol concentration at the liquid outlet was measured, it was 1.00 g / L, and it was confirmed that the operation was stable. The obtained ergosterol crystals were agglomerated crystals.
(HPLC measurement conditions)
Column: Nacalai Tesque COSMOSIL 5C18-MS
250 mm x 4.6 mm I.D. D.
Column temperature: 35 ° C
Mobile phase: methanol feed rate: 1.0 ml / min
Detector: UV detector, detection wavelength 282 nm
(Example 2)
In Example 2, ergosterol was crystallized in the same manner as in Example 1 except that the temperature of the hot water mixed with the liquid flowing out from the upper nozzle 5 was 50 ° C. After continuous operation for about 1 hour, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured by HPLC, which was 0.62 g / L. The recovery rate at this point was 79% (= 100 × (3-0. 62) / 3). Further, after the continuous operation for 2 hours, the concentration of ergosterol at the liquid outlet was measured and found to be 0.84 g / L, and 72% (= 100 × (3-0.84) / 3) of ergosterol was recovered. I understood it. Further, 30 minutes later, the concentration of ergosterol at the liquid outlet was measured and found to be 0.86 g / L, confirming stable operation. The obtained crystal was an agglomerated crystal.

(Comparative Example 1)
As Comparative Example 1, ergosterol was crystallized in the same manner as in Example 1 except that the liquid flowing out from the upper nozzle 5 was not returned to the apparatus. After continuous operation for about 1 hour, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured by HPLC. As a result, it was 1.01 g / L, and the recovery rate at this point was 66% (= 100 × (3-1. 01) / 3). Further, after continuous operation for 2 hours, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured and found to be 1.23 g / L, and the recovery rate was 59% (= 100 × (3-1.23) / 3). It was low. After further 30 minutes, the ergosterol concentration at the liquid outlet of the upper nozzle 5 was measured and found to be 1.32 g / L, and the recovery rate was up to 56% (= 100 × (3-1.32) / 3). It was falling. The obtained crystal was not clear in shape, and the solution became cloudy.

The structure of the tower-type crystallizer as one embodiment of this invention is shown.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Liquid inlet nozzle 2 Cooling part 3 Slurry outlet nozzle 4 Solid-liquid separator 5 Liquid outlet nozzle 6 Mixing tank 7 Pump 10 Stirrer motor 12 Solution 14 Water 16 Cooling water outlet 18 Cooling water inlet 20 Stirrer motor

Claims (7)

(A) An organic solvent solution containing sterols is continuously supplied from the lower part of the tower-type crystallizer,
(B) Crystallizing and precipitating the sterols in a cooling unit provided at the top of the tower-type crystallizer,
(C) recovering the crystallized sterols from the lower part of the apparatus;
In the sterol crystallization method,
(D) The organic solvent solution after sterols are crystallized is caused to flow out from an outflow portion provided at the top of the tower-type crystallizer,
(E) at least part of the organic solvent solution that has flowed out is brought into contact with water and then introduced into the tower-type crystallizer again;
A method for crystallizing sterols characterized by the following.   The method according to claim 1, wherein the organic solvent is a water-insoluble organic solvent having a specific gravity of 0.9 or less.   The method according to claim 1 or 2, wherein the organic solvent is hexane, heptane, octane or a mixture thereof.   The method according to any one of claims 1 to 3, wherein the water brought into contact with the spilled organic solvent solution is warm water of 40 to 80 ° C.   The method according to any one of claims 1 to 4, wherein the ratio of the amount of liquid returned to the apparatus in the spilled organic solvent is 3% to 30% of the effluent amount. A crystallization system including a tower type crystallizer for crystallizing sterols,
The tower-type crystallizer
(A) a supply unit for continuously supplying an organic solvent solution containing sterols provided at the lower part of the apparatus;
(B) a cooling unit provided in the upper part of the apparatus for crystallizing and precipitating the sterols;
(C) a recovery unit for recovering the crystallized sterols provided at the lower part of the apparatus;
(D) an outflow part provided at the upper part of the apparatus for allowing the organic solvent solution after sterols to crystallize to flow out of the apparatus;
With
The crystallization system further comprises:
(E) an external reflux unit that is connected to the outside of the apparatus and that is introduced into the apparatus again after bringing at least a portion of the organic solvent solution that has flowed out into contact with water;
A crystallization system characterized by comprising: The (e) external reflux part in claim 6 further comprises:
(E-1) a temperature control unit for controlling the temperature of the mixture and / or
(E-2) a flow rate control unit for controlling a flow rate for introducing the mixture into the apparatus;
A crystallization system characterized by comprising:

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