KR101313390B1 - Method of highly efficiently extracting active ingredient from plant or mushroom - Google Patents

Abstract

The present invention relates to a method for extracting the active ingredient of the plant,
The mixture consisting of 1 part by weight of the plant and 2 to 7 parts by weight of water was stirred under conditions of imparting high shear force at a temperature of 100 to 250 ° C. in a closed vessel in terms of pressure, so that the plant had a maximum dimension of 1 to 20 μm. Pulverizing to an average value of to obtain a crushing mixture comprising an aqueous phase comprising the active ingredient and a crushed solid matter residue, and then recovering the aqueous phase to extract the active ingredient.

Description

High efficiency extraction method of active ingredients of plants or mushrooms {METHOD OF HIGHLY EFFICIENTLY EXTRACTING ACTIVE INGREDIENT FROM PLANT OR MUSHROOM}

The present invention is a method for the extraction of active ingredients of plants, especially mushrooms, with high efficiency and low energy consumption.

In the prior art of extracting the active ingredient of the plant, extraction by the so-called herbal medicine decoction method (Non-Patent Documents 1 and 2) that extracts the active ingredient over a long time using hot water 20 to 30 times the weight of the plant. The extract was concentrated and dried to obtain a powder or a pill. Recently, a circulation multistage pressure extraction method has been introduced for the purpose of improving the extraction rate. In this method, the active ingredient is first extracted with a pressurized hot water extractor at 110 to 130 ° C., the solids separated from the extract are heated with saturated steam at 130 to 200 ° C., and the cell membrane is decomposed to 110 to 130 ° C. again. Extraction with a pressurized hot water extractor is repeated according to the strength of the cell membrane, and the obtained extract is concentrated with a reduced pressure concentrator (see Patent Document 1).

This cyclic multistage pressure extraction method has a drawback in that it has a lot of processing steps and takes a lot of time and energy. Therefore, the method of extracting after heat-processing with the oil of 100-300 degreeC for the purpose of destroying a cell membrane and improving extraction efficiency is proposed (refer patent document 2). Pretreatment with this high temperature oil has the drawback that an lipophilic active ingredient elutes into oil from cell membranes and cell fluids destroyed by high heat.

Japanese Laid-Open Patent Publication No. 11-196818 Japanese Laid-Open Patent Publication No. 2005-253330

http://www.mushroom.co.jp/health/mannen.htm http://www.ne.jp/asahi/haru/kenshoudou/agarikususenjihou.htm

The present invention provides a method for extracting the active ingredient of the plant in high yield and energy saving.

The present invention relates to a method for extracting an active ingredient of a plant, particularly a mushroom, wherein the mixture consisting of 1 part by weight of the plant and 2 to 7 parts by weight of water, preferably 2 to 5 parts by weight, is contained in a closed container in terms of pressure. By stirring under conditions imparting high shear force at a temperature of 250 ° C., the plants are crushed to an average value of the largest dimension of 1 to 20 μm, thereby obtaining a crushing mixture comprising the water phase and crushed solid matter residue containing the active ingredient. And then extracting the active ingredient by recovering the aqueous phase. Here, the average value of the maximum dimension refers to the average value of the largest dimension when the size is different depending on the measurement direction.

In the case of containing starch or the like which is susceptible to thermal decomposition as an active ingredient, the crushing is preferably carried out at 100 to 130 ° C. in the shortest time possible. In order to increase the extraction efficiency in the short time, it is 0.5 to inert gas such as nitrogen gas. It is a method which can pressurize to 5 MPa and can increase the shear force by pressurization. In addition, in order to improve the extraction efficiency of the active ingredient as a whole, the crushing at the temperature of 20-100 degreeC (temperature of the range which does not exceed 250 degreeC) higher than the 1st crushing temperature with respect to the 1st filtration residue is 2-3. By repeated times, the extraction amount of the total active ingredient is preferably at least 30% by weight, more preferably at least 45% by weight.

In the case of containing starch or the like which is likely to cause thermal decomposition as an active ingredient, the crushing is preferably performed at 100 to 130 ° C. for as short a time as possible. The extraction rate of the sum total of an active ingredient can be raised by adding the solid substance residue which remains after water phase recovery 1 to 3 times further to the said process. However, it is preferable to perform the said 1-3 process at the temperature which is 20-100 degreeC higher than the temperature of a 1st process, and does not exceed 250 degreeC. The amount of extraction of the sum of the active ingredients is preferably at least 30% by weight, more preferably at least 45% by weight. In order to raise the extraction efficiency in a short time, pressurization is carried out to 0.5-5 MPa with inert gas, such as nitrogen gas, and the shear force by pressurization can be aimed at.

The present inventors attempted to destroy cell membranes by finely pulverizing plants with high temperature, high pressure, and high shear kneader. In this way, it was found that the cell membrane was broken down to 1 to 20 µm by this grinding, and the intracellular liquid easily came out of the cell. The present inventors further preferably reduce the plant as a raw material (hereinafter referred to as the above substance) to an average value of the maximum dimension of 5 to 20 mm in advance, and grind it with a high temperature, high pressure and high shear force kneader (see FIG. 1). For example, if the thickness is reduced to 100 to 500 µm and treated with a kneader under pressure of 0.5 to 5 MPa according to the difference in hardness of the substance, the substance can be made smaller to 1 to 20 µm, A thermocouple measuring the temperature of the workpiece was found to capture an abnormal current corresponding to at least 50 ° C., in particular at least 100 ° C., more particularly at least 200 ° C. higher or lower temperature than the treatment temperature (FIG. 3). Reference). In the conventional decoction method, the transition to the aqueous phase is due to the penetration pressure, so that the amount transferred is only about 8% by weight of the dry raw material. In the present invention, the analysis of the obtained aqueous phase shows that at least 15% by weight of the dry raw material has been extracted into the aqueous phase. Since the amount extracted by the decoction method is up to 8%, the original water-soluble substance is considered to be 10% by weight of the roughness of the dry raw material. It is assumed that the above amount of extraction in the present invention is that the cell constituents are extracted by the destruction of the cell membrane by shearing.

Although not bound by a specific theory, it is assumed that the abnormal current acquired by the thermocouple is that the polymer compound constituting the cell membrane is cleaved by the shear force to generate radicals, and electrons from this radical are captured as the abnormal current. It is considered that the physical cleavage of the chemical bonds of the cell membrane constituents occurred by the crushing to 1 to 20 μm, and the radicals generated thereby caused the efficient hydrolysis reaction of the cell membrane constituent polymer materials. As a result, the cell membrane is broken, the membrane constituent polymer material is hydrolyzed, and the active ingredient is easily extracted, and since the intracellular liquid is released to the hydrothermal side, the extraction of the active ingredient can be performed easily with a low energy consumption compared with the conventional method. It became possible. It is estimated that the generation of radicals and the high molecular compound constituting the cell membrane are lower molecular weight, so that the extraction amount of β-glucan or water-soluble plant fiber has increased 1.5-2.0 times compared to the extraction case in which no generation of radicals occurs.

The generated radicals continue to cause further cleavage of the polymer compound constituting the cell membrane, and at least 15% by weight of the active ingredient, including those in which the active ingredient or cellular constituents in the cell are destroyed and small molecules are produced by this repetition. It is assumed that this has been extracted. The solid matter residue remaining after recovering the aqueous phase preferably has a water content of 40 to 60%. By repeating the above shredding step (the amount of water added is 2 to 7 parts by weight based on 1 part by weight of the water content of the residue), the total amount of active ingredients is preferably at least 30% by weight, more preferably At least 45 weight percent. The number of additional repetitions depends on the hardness of the cell membrane of the material, preferably 1 to 2 times for soft mushrooms and 2 to 3 times for hard plants. Even if the number of treatments is continued four times or more, it is not easy to increase the number of recovery of the active ingredient suitable for the treatment cost.

An apparatus suitable for practicing the present invention is shown in FIG. 1 shows the exterior of a stirring device by breaking the cylindrical vessel 20 at its axial center. A screw 11 sending the material from the material inlet 4 to a rotary shaft 5 connected to the motor 9, a forward vane 12 for axially advancing the non-treatment material and the blood sent forward (Iv) The retracting blade 13 which reverses the flow direction of a process material and returns to the back in the area | region near an axis | shaft is connected. Each forward wing 12 is composed of four impellers mounted at equal intervals in the circumferential direction of the shaft, the direction of the impeller is angled to advance the workpiece when the shaft is rotated. The forward advancing vanes 12 'are supported by four elongated mounting plates 14 mounted at equal intervals in the circumferential direction of the shaft, and the workpieces are interposed between the four elongated mounting plates 14. Can flow. The retracting vanes 13 backflow the workpiece backward when the shaft is rotated. When the pressure in the vessel exceeds a predetermined value due to steam and other gases generated at the time of treatment, part of the steam and other gases are discharged from the discharge pipe 1. The pressure near the inlet is monitored by a Bourdon tube pressure gauge. The temperature of the inlet is monitored by the thermocouple 3. The temperature and pressure of the processing zone of the vessel are monitored by thermocouples, pressure transmitters 6 and sanitary oil-free pressure sensors ASG 702 and thermocouples 7. As described later, an inert gas pipe 8 is provided for introducing a high pressure inert gas for raising the pressure in the container. A jacket is further provided for heating the vessel (not shown).

In one embodiment of the present invention, while rotating the shaft 5, the plant and water containing the active ingredient are gradually introduced from the material inlet, and are advanced by the feed screw 11 to introduce the predetermined amount of the material. Close the material inlet. The product outlet 10 is closed.

Plants containing the active ingredient generally have dimensions of several tens of millimeters to several hundreds of millimeters initially, but it is preferable to chop them into dimensions of the average value of the maximum dimension of 5-20 mm in advance. It is preferable to finely grind this to have an average value of the maximum dimension of 100 to 500 m in advance in the apparatus. At this time, Preferably the temperature of the to-be-processed object is set to 0-50 degreeC, More preferably, it is 5-30 degreeC, and a pressure is atmospheric pressure. This process is hereinafter referred to as a preliminary grinding process.

Subsequently, the process according to the present invention will be described. First, in the preliminary grinding process, the material, which has been preliminarily chopped to an average value of the maximum dimension of 5 to 20 mm without adding water, is chopped to have an average value of the maximum dimension of 100 to 500 μm by high shear force. Water is added to this prepulverized plant (the material). The weight ratio of the material and water is set to 1 part by weight of the material and 2 to 7 parts by weight of water, preferably 1 part by weight of the material and 3 to 5 parts by weight of water.

Subsequently, after sealing a container, it heats and makes content temperature 100-250 degreeC, Preferably it is 110-240 degreeC, More preferably, it is 120-230 degreeC. In the process according to the invention, the material is crushed to an average value of a maximum dimension of 1 to 20 μm and at least 15% by weight of the polymer material and the intracellular material constituting the cell membrane in the material are extractable. It is important to apply sufficient shear force to the material. This high shear force does not occur only when the device is operated without special research. A calculated value of a conveyance amount for conveying the mixture in the forward direction by the forward wing, intentionally breaking the balance between the ability to advance the material by the forward wing and the ability to return the material back by the backward wing, and the retract wing The ratio of the calculated value of the return amount of the mixture in the retreat direction is set to 1: 0.6 to 0.9, preferably 1: 0.65 to 0.85, and more preferably 1: 0.7 to 0.8. As a result, the flow of the material is disrupted and the material is severely rubbed. Even if the ratio of the feed amount and the return amount is inverse to the above, it is easy to do the above in the design of the apparatus. If this ratio is outside the above range, for example, 1: 1, the extraction efficiency as high as the present invention intends cannot be realized. This is probably because the forward and return streams flow relatively smoothly, so that no high shear forces occur.

According to the present invention, an active ingredient of a plant containing the active ingredient can be obtained in a large amount (with a high extraction rate), and thus the active ingredient can be produced simply and inexpensively.

Examples of the plant containing the active ingredient in the present invention include ganoderma lucidum, wheat, triticale, peony, licorice root and the like.

In a preferred embodiment of the present invention, the material containing the active ingredient having an average value of a maximum dimension of 5 to 20 mm is preliminarily pulverized to 100 to 500 µm, and then to 1 to 20 µm at a temperature of 100 to 250 ° C. Crushing is carried out. An example of a compact prot type of device suitable for practicing the above-described invention is shown in FIG. 1, which is a hermetic stirring device having a motor of 20 liters, 5.5 kW, and preliminary grinding contains the active ingredient under normal temperature and atmospheric pressure. Grind the material to 100 ~ 500 ㎛. Then, crushing according to the present invention is carried out by raising the pressure in the reaction vessel to 0.5 to 5 MPa with an inert gas for 5 minutes to 3 hours, preferably 30 minutes to 1 hour, for example, 1 hour. Until crushed. At this time, the pressure in the reaction vessel is raised to 0.5 to 5 MPa by inert gas. The pressure at this time is changed according to the hardness of the cell membrane of the substance. Soft ones under low pressure and hard ones under high pressure. This pressurization increases the shear force, and the material containing the active ingredient is easily pulverized to 1 to 20 µm.

The stirring device may be either a batch type or a continuous type closed at the point of pressure. The continuous stirring device is capable of injecting and extracting inert gases such as carbon dioxide and nitrogen used for extraction and pressurization of the extract including the active substance and extraction of the extraction residue. What is necessary is just to be able to carry out continuously, maintaining a predetermined condition.

The upper limit of heating temperature is 250 degreeC, Preferably it is 240 degreeC, More preferably, it is 230 degreeC, A minimum is 100 degreeC, Preferably it is 110 degreeC, More preferably, it is 120 degreeC. If the temperature exceeds the upper limit, the material containing the active ingredient is pyrolyzed and the apparatus cost is significantly higher, and below the lower limit, a sufficient effect of hydrothermal extraction is not obtained. The heating time is preferably an upper limit of 3 hours, more preferably 2 hours, more preferably 1.5 hours, particularly preferably 1 hour, and the lower limit is preferably 5 minutes, more preferably 15 minutes, more preferably. It is 20 minutes. The cell membrane-constituting polymer material is destroyed by the hydrolysis by radicals generated by physical chemical bond cleavage caused by the pulverization of the substance containing 1 to 20 μm of the substance including the active ingredient by the heating, and the intracellular substance comes out of the cell. The active ingredient is converted into an extractable substance.

The lower limit of the pressure during crushing is 0.5 MPa, preferably 1.0 MPa, more preferably 1.5 MPa. The upper limit is 5.0 MPa, preferably 4.5 MPa, more preferably 4.0 MPa because of the manufacturing cost of the device. The pressurization to a predetermined pressure is preferably to control the pressure applied to the sample using an inert gas, for example nitrogen gas, within the above range.

In the present invention, the shear force is higher by the press as described above. The upper limit of shear force at the time of crushing (and preliminary grinding) according to the invention is 20 MPa, preferably 10 MPa, more preferably 5 MPa, more preferably 3 MPa, and the lower limit is 0.1 MPa, preferably 0.3 MPa, more preferably 0.5 MPa. When the upper limit is exceeded, the motor power load is increased, thereby increasing the processing cost. Below the said lower limit, preliminary grinding | pulverization is inadequate, and also the decomposition | disassembly of the said substance at the time of grinding | pulverization which concerns on this invention does not generate | occur | produce sufficiently. The shear force is imparted by a stirring impeller provided in the stirring device.

The shear force was measured by the method described in PCT / JP2004 / 013551. A standard material for which viscosity (20 ° C.) is already known, for example, the standard solution for viscosity calibration made by Nippon Grease Co., Ltd. (JISZ8809) JS100 viscosity 86 mPa · s, JS14000 viscosity 12 Pa · s and JS160000 viscosity 140 Pa · s, respectively The torque applied to the rotating shaft was measured by rotating the stirring impeller provided at a temperature of 20 ° C. in the stirring device shown in FIG. 1 at 20 revolutions / minute. For values exceeding 140 Pa · s of viscosity (20 ° C), a mixed liquid prepared by mixing kerosene with asphalt (for example, viscosity (20 ° C) measured using a BS type viscometer manufactured by Toki Sangyo Co., Ltd.) Torque is measured in the same manner as above using 6400 Pa · s mixed liquid). Here, the measurement liquid is added until the whole stirring impeller in the stirring apparatus is completely submerged in the liquid. Moreover, the torque in the empty state which does not put a measuring liquid in a stirring apparatus is measured (shear force at this time is made into 0). In this way, the torque of each measurement liquid of known viscosity is read, and the shear force is obtained by the following formula (1) to obtain the relationship between the torque and the shear force shown in FIG. 2, for example.

In Equation 1, the shear rate is represented by Equation 2 below. In Equation 2, sin3.0 ° is a device-specific value shown in FIG. 1. The said value is calculated | required by the shape of a stirring impeller, and differs according to the shape of a stirring impeller.

Thus, the shear force can be calculated | required by measuring the torque applied to a rotating shaft from the said relationship. The axial torque of the stirring device with the stirring impeller is unique to the device, so the torque also changes when the device is changed. Therefore, the relationship between the torque and the shear force as shown in FIG. 2 may be obtained for each device used. In this manner, the shearing force can be obtained by measuring the torque applied to the rotating shaft in any apparatus.

In the apparatus shown in FIG. 1, the flow from the inlet direction and the flow from the outlet direction collide to create a flow toward the outer wall of the stirring apparatus, and the intensity of the flow can be detected as a pressure at a position of seven. It can be seen that the shear force obtained in FIG. 2 using this detected pressure value and the measured value of the axial torque is the same as the value measured using Sanitai's sanitary oil-free pressure sensor ASG702.

Example 1

Hereinafter, although an Example demonstrates this invention in more detail, this invention is not limited by an Example.

The ganoderma used in Example 1 has the properties of Table 1 below.

In Table 1, moisture was measured using an infrared moisture meter FD-720 manufactured by Ketsu Institute of Science and Technology.

In the following, the sanitary oil-free pressure sensor ASG702 by Yamatake was used for the measurement of the shear force.

As the stirring device, the stirring device shown in FIG. 1 was used. The stirring impeller used the thing of the return 0.8 with respect to the feed 1.0 as the calculated value of the return amount from the opposite side to the calculated value of the feed amount of the screw feeder of the sample inlet 4. The inner volume is 20 liters and a 5.5 kW motor is provided. First, 4 kg of ganoderma pulverized to 100 to 500 µm and 12 kg of water are gradually added by preliminary grinding under a condition of applying a maximum shear force of 1.0 MPa at room temperature and atmospheric pressure while rotating the stirring impeller at 20 rpm. The instruction | indication of the sensor ASG702 (7 in FIG. 1) showed 0.8 MPa (gauge pressure shown of the pressure sensor 7). The motor current value at this time rose to around 25 amperes. Subsequently, after pressurizing to 2.0 MPa with nitrogen gas (refer FIG. 5), maintaining rotation of an impeller at 20 rpm, heating was started and process temperature was adjusted to 120 degreeC. After reaching the temperature, the pressure gauge 2 on the inlet 4 side shows 2.0 MPa at this temperature, but the indication of the pressure sensor 7 at the intermediate position of the stirring device is 2.3 MPa, and the motor current value is 19.5. Ampere (70.1% of maximum load) (see FIG. 4). However, as time goes by, grinding to 20 µm or less proceeds, and the instruction of the pressure sensor 7 (measures the shear force) is the same as that of the pressure gauge 2 of the inlet 4 as the viscosity of the slurry-like processing object decreases. Instruction was indicated. The treatment was performed for 20 minutes while maintaining the temperature and the motor rotation speed in the vessel at 20 rpm. Thereafter, the mixture was cooled to an environmental temperature, and the crushed mixture solid containing the aqueous phase and the crushed solid substance residue containing the active ingredient was taken out. The extract was treated with "centrifugal dehydration" below in FIG.

As a reference example, the experiment which did not pressurize with nitrogen gas was also performed. That is, the flow of the experiment is the same as in Example 1 (Fig. 6), but there is no pressurization of 2 MPa by nitrogen gas. Although the peak of the kneader current value indicating the appearance of the shear force was observed in the embodiment pressed after the material injection (FIG. 4), the peak of the kneader current value did not appear in the reference example without pressing (FIG. 7), FIG. 3. The abnormal current acquired by the thermocouple shown in Fig. 8 did not appear (Fig. 8). The data of this reference example are also shown in Table 2 above.

The lyophilized article of the aqueous phase of Example 1 and Reference Example was subjected to component analysis, and the results are shown in Table 2 above. In addition, as a comparative example, extraction conditions, extraction rates, and component analysis values of the market distribution of Ganoderma lucidum extract were performed, and the results are also shown in Table 2 above.

As can be seen from Table 2, the extraction rate of the reference example is 27.3%, but the extraction rate of Example 1 is 38.6% increased by 40%. In addition, the extraction amount of β-glucan, which is said to be helpful for the maintenance of health, is increased by 50% in Example 1, and the extraction amount of water-soluble plant fiber which helps to clean up the intestinal environment is also increased by 2.25 times.

Comparing the present invention with the comparative example (the conventional method) (see Table 2 above), the amount of water used for extraction is 30 kg of this 7.5 times as compared to 4 kg of the present invention per kg of ganoderma lucidum. In the conventional method, this 7.5-fold amount of water is heated to near 100 degreeC, it is hold | maintained for 30 minutes, it concentrates by distillation under reduced pressure, and freeze-dried to produce the powder of ganoderma lucidum extract. In comparison, the present method has the advantage that the concentration process by vacuum distillation is unnecessary due to the small amount of water of 7.5 / 7.5 and applied to direct freeze-drying, and also caused by the friction of the material during the grinding process by the shear force. Since the temperature of the material rises to 100 ° C. by heat, the amount of energy required for heating is almost the same as in the conventional method in consideration of the energy consumption of the motor for the stirrer. Since it is less than the conventional method, it is possible to save energy significantly.

In addition, the extraction amount of β-glucan, which is said to help health maintenance, is increased by 2.2 times, and the extraction amount of water-soluble plant fiber is increased by 46.8 times when the product obtained by the method according to the present invention is compared with the extraction product by the conventional method. have. In the method according to the present invention, about 18% of the extracted saccharides are β-glucan, which is less than about 8% by the conventional method (Table 2).

As described above, the method according to the present invention not only achieves a significant energy saving compared to the conventional extraction method, but also greatly increases the extraction amount of the active ingredient.

The present invention can extract and produce the active ingredient of the plant with high efficiency and low energy consumption.

BRIEF DESCRIPTION OF THE DRAWINGS Fig.

1 is a schematic diagram of a hermetic stirring device which can be used in the present invention.

2 is a graph showing the relationship between the torque and the shear force of the apparatus shown in FIG.

3 is a graph showing the passage of time of the output current (= indicated temperature) of the thermocouple of Example 1. FIG.

4 is a graph showing the passage of time of the current value of the motor of Example 1. FIG.

FIG. 5 is a graph showing the pressure change in the apparatus due to nitrogen gas pressurization of Example 1. FIG.

6 is a flowchart showing the experimental procedure of Example 1. FIG.

7 is a graph showing the passage of time of the current value of the motor of the reference example.

8 is a graph showing the passage of time of the output current (= indicated temperature) of the thermocouple of the reference example.

1: steam / product gas outlet
2: Bourdon tube pressure gauge
3: thermocouple
4: sample inlet
5: stirring impeller that can impart shear force
6: thermocouple and pressure transmitter
7: Sanitary oil-free pressure sensor ASG702 and thermocouple
8: pressurized line by inert gas
9: motor
10: sample outlet
11: feed wing
12: forward wing
13: retreat wing
14: mounting plate
20: cylindrical container

Claims (13)

As a method of extracting the active ingredient of a plant,
The mixture comprising 1 part by weight of the plant and 2-7 parts by weight of water was stirred under conditions of imparting high shear force at a temperature of 100-250 ° C. in a closed vessel in terms of pressure, so that the plant had a maximum of 1-20 μm. Pulverizing to an average value of the dimensions, thereby obtaining a crushing mixture comprising an aqueous phase containing the active ingredient and a crushed solid matter residue, and subsequently extracting the active ingredient by recovering the aqueous phase; The container has a rotating shaft extending in the central axis direction, a forwarding blade and a retracting blade provided on the rotating shaft, the calculated value of the conveying amount carrying the mixture in the forward direction by the forwarding blade, and the retracting blade by the retracting blade. The ratio of the calculated value of the return amount conveying the mixture in the direction is 1: 0.6 to 0.9. The method of claim 1,
The solid matter residue remaining after the water phase is recovered is added to the process according to claim 1 in addition to one or three times, except that the one to three additional steps are at a temperature of 20 to 100 ° C. higher than the first process temperature and 250 ° C. Method at a temperature not exceeding. 3. The method according to claim 1 or 2,
The container is cylindrical. The method of claim 1,
The ratio is characterized in that 1: 0.65 ~ 0.85. The method of claim 1,
The ratio is 1: 0.7 to 0.8. 3. The method according to claim 1 or 2,
A shearing force of 0.1-20 MPa is applied to the mixture by stirring. The method according to claim 6,
Shear force is 0.3 to 10 MPa characterized in that the method. 3. The method according to claim 1 or 2,
A thermocouple measuring the temperature of the mixture at the time of stirring captures an abnormal current corresponding to a temperature at least 50 ° C. higher or at least 50 ° C. lower than the temperature of the mixture. 3. The method according to claim 1 or 2,
And wherein the thermocouple measuring the temperature of the mixture upon stirring captures an ideal current corresponding to a temperature at least 100 ° C. higher or at least 100 ° C. lower than the temperature of the mixture. 3. The method according to claim 1 or 2,
The plant is characterized in that it has an average value of the maximum dimensions of 5-20 mm. 3. The method according to claim 1 or 2,
Pressurizing the pressure in the vessel to 0.5-5.0 MPa using an inert gas. 3. The method according to claim 1 or 2,
The crush extraction process is carried out for 5 minutes to 3 hours. 3. The method according to claim 1 or 2,
The cell membrane is destroyed by the crushing effect generated in the process of crushing the plant to an average value of the maximum dimension of 1 to 20 μm, and the active ingredient contained in the cell is extracted to the aqueous layer.

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