阅读说明：本技术 一种提取薯蓣皂苷元的生产工艺 (Production process for extracting diosgenin ) 是由 李雁青 付宏征 于 2020-10-15 设计创作，主要内容包括：本发明公开了一种提取蓣皂苷元的生产工艺,包括如下步骤：原料的预处理：将新鲜的薯蓣植物去毛根后清洗去除泥沙,并切成0.1～1cm厚度的段,然后用水清洗,将淀粉和薯蓣残渣分离；溶剂提取：收集薯蓣残渣,经过溶剂提取得到薯蓣皂苷；将薯蓣皂苷水解；将水解物进行萃取、提纯、重结晶。采用本发明的薯蓣皂苷元的生产工艺,可以解决目前酸水解和汽油提取浪费及环境污染的问题,而且可以回收利用药渣,并提高提取得到的薯蓣皂苷元的提取率和纯度。(The invention discloses a production process for extracting diosgenin, which comprises the following steps: pretreatment of raw materials: removing hair roots of fresh yam plants, cleaning to remove silt, cutting into sections with the thickness of 0.1-1 cm, cleaning with water, and separating starch from yam residues; solvent extraction: collecting rhizoma Dioscoreae residue, and extracting with solvent to obtain dioscin; hydrolyzing dioscin; and extracting, purifying and recrystallizing the hydrolysate. The production process of diosgenin can solve the problems of waste and environmental pollution of acid hydrolysis and gasoline extraction at present, can recycle medicine dregs, and improves the extraction rate and purity of the extracted diosgenin.)

1. A production process for extracting diosgenin is characterized by comprising the following steps:

s1, pretreatment of raw materials: cleaning fresh rhizoma Dioscoreae plant, cutting into segments, cleaning with water, and separating starch and rhizoma Dioscoreae residue;

s2, solvent extraction: collecting the dioscorea opposita residue in the step S1, and extracting the dioscorea opposita residue by using a solvent to obtain dioscin;

s3, hydrolyzing the diosgenin to obtain diosgenin;

and S4, extracting, purifying and recrystallizing the hydrolysate in the step S3 to prepare a diosgenin pure product.

2. The diosgenin production process according to claim 1, wherein in step S2, the solvent is an organic solvent.

3. The diosgenin production process according to claim 2, wherein the solvent is 70% ethanol solution in step S2.

4. The diosgenin production process according to claim 1, wherein in step S2, the solvent extraction is combined with microwave and ultrasound.

5. The diosgenin production process according to claim 4, wherein in step S2, the solvent extraction time is 300S, the microwave power is 450-500W within 0-60S, the microwave power is 400-450W within 60-150S, and the microwave power is 600W within 150-300S.

6. The process according to claim 1, wherein in step S3, the diosgenin is obtained by hydrolyzing diosgenin with a glycosidase selected from at least one of alpha-glucosidase, beta-glucosidase, rhamnosidase, phlorizin hydrolase, glucuronidase, and acetylglucosaminidase.

7. The diosgenin production process according to claim 1, wherein CO is used in step S4₂Extracting by supercritical technology.

8. The diosgenin production process according to claim 7, wherein the CO is₂The supercritical extraction equipment comprises an extraction kettle, a separation column and a separation kettle, wherein the extraction pressure is 25-40 MPa, the extraction temperature is 53-62 ℃, and the extraction time is 2-3 h; the pressure of the separation column is 18-26 MPa, and the temperature is 40-60 ℃; of two separate vesselsThe conditions are respectively as follows: the pressure is 10-15 MPa, the temperature is 48-55 ℃, the pressure is 5-6 MPa, and the temperature is 30-40 ℃.

9. The diosgenin production process according to claim 8, wherein the extraction pressure is 30MPa, the extraction temperature is 55 ℃, and the extraction time is 2.5 h; the pressure of the separation column is 20MPa, and the temperature is 45 ℃; the conditions of the two separation kettles were: the pressure is 11MPa, the temperature is 50 ℃, the pressure is 5.6MPa, and the temperature is 35 ℃.

Technical Field

The invention relates to the technical field of dioscorea opposita extraction, in particular to a production process for extracting diosgenin.

Background

China is a big country for dioscorea planting. Rhizomes (yellow ginger) of Dioscorea zingiberensis (d.zingiberensis) and rhizomes (Dioscorea nipponica) of Dioscorea zingiberensis (d.nipponica) which are perennial herbs of Dioscorea are two species with the highest diosgenin content in China, and then Dioscorea panthaica (d.panthaica), Dioscorea zingiberensis (d.nipponica), Dioscorea triangularis (d.deltoidea) and the like are included. The plants are easy to plant and have large annual output, so the plants become the most main traditional Chinese medicine raw materials for producing the diosgenin in the industry at present. Diosgenin, known industrially as diosgenin, is the aglycone of diosgenin, is linked to glycosyl at the C-3 position via an glycosidic bond, exists in the rhizome of dioscorea plants mainly in the form of diosgenin, and is tightly bound to cellulose in the cell wall. Diosgenin is an ideal precursor for synthesizing various steroid hormones and steroid contraceptives, and more than 60% of steroid hormones produced in various countries in the world are produced by using diosgenin as a raw material. It also has hemolytic, blood lipid reducing, antitumor, antibacterial, and antiinflammatory effects. The demand for diosgenin is great at home and abroad, so that the development of a new production process for extracting the diosgenin has important value and wide market potential.

At present, diosgenin is mainly produced by natural extraction. The diosgenin extracted from natural plant has advantages of low toxicity and less side effects compared with chemically synthesized diosgenin. At present, diosgenin is generally industrially prepared by extracting diosgenin by pre-fermentation, acid hydrolysis and gasoline reflux extraction. The method comprises breaking cell structure and composition of dioscorea opposita with hydrochloric acid or sulfuric acid, breaking glycosidic bond between diosgenin and sugar (cellulose), dissociating diosgenin, and extracting with 120# gasoline or petroleum ether by using its water-insoluble and organic solvent-soluble properties. The traditional acid hydrolysis method has the disadvantages of complicated operation, long consumption time and low diosgenin yield. And as the medicinal materials have large volume, the acid consumption is large, and the organic matters degraded by the acid are more, the sewage quantity is large, the environmental pollution is large, and the development of the diosgenin industry is seriously hindered. The hydrolysate is extracted by gasoline or petroleum ether, and the using amount is large. And the 120# gasoline is a first-grade explosion-proof solvent and has high danger coefficient.

Therefore, in order to simplify the process, save raw materials, reduce pollution, improve the yield of the diosgenin and the utilization of waste materials, the production development of the medicinal raw material diosgenin in China is promoted. Meanwhile, the production process for developing the green environment-friendly diosgenin and the quality of the raw material medicines meet the international standard, high-quality raw material medicines are provided for the medicine production at home and abroad, the development of yam planting is promoted, and rural economy is developed.

Disclosure of Invention

In view of the above, the present invention is directed to a process for extracting diosgenin, which is used for extracting diosgenin from dioscorea plants through an environment-friendly process, and improving the extraction rate and purity.

In order to achieve the purpose, the technical scheme of the invention is realized as follows:

a production process of diosgenin comprises the following steps:

s1, pretreatment of raw materials: removing hair roots of fresh yam plants, cleaning to remove silt, cutting into sections, cleaning with water, and separating starch from yam residues;

s2, solvent extraction: collecting the dioscorea opposita residue in the step S1, and extracting the dioscorea opposita residue by using a solvent to obtain dioscin;

s3, hydrolyzing the diosgenin to obtain diosgenin;

and S4, extracting, purifying and recrystallizing the hydrolysate in the step S3.

Further, in step S2, the solvent is an organic solvent.

Further, in step S2, the solvent is a 70% ethanol solution.

Further, in step S2, the solvent extraction combines microwave and ultrasound.

Further, in step S2, the solvent extraction time is 300S, the microwave power is 450-500W within 0-60S, the microwave power is 400-450W within 60-150S, and the microwave power is 600W within 150-300S.

Further, in step S3, the diosgenin is obtained by hydrolyzing the diosgenin with a glycosidase selected from at least one of α -glucosidase, β -glucosidase, rhamnosidase, phlorizin hydrolase, glucuronidase, and acetylglucosaminidase.

Further, in step S4, CO is used₂Extracting by supercritical technology.

Further, said CO₂The supercritical extraction equipment comprises an extraction kettle, a separation column and a separation kettle, wherein the extraction pressure is 25-40 MPa, the extraction temperature is 53-62 ℃, and the extraction time is 2-3 h; the pressure of the separation column is 18-26 MPa, and the temperature is 40-60 ℃; the conditions of the two separation kettles were: the pressure is 10-15 MPa, the temperature is 48-55 ℃, the pressure is 5-6 MPa, and the temperature is 30-40 DEG C

Further, said CO₂The extraction pressure of the supercritical extraction is 30MPa, the extraction temperature is 55 ℃, and the extraction time is 2.5 h; the pressure of the separation column is 20MPa, and the temperature is 45 ℃; the conditions of the two separation kettles are respectively as follows: the pressure is 11MPa, the temperature is 50 ℃, the pressure is 5.6MPa, and the temperature is 35 ℃.

Compared with the prior art, the production process for extracting diosgenin has the following advantages:

(1) the invention solves the problem of environmental pollution of the prior acid hydrolysis process by establishing a scale production process for extracting the diosgenin in an environment-friendly way, fully utilizes rich yam medicinal resources to produce the diosgenin, and provides raw materials for synthesizing various steroid hormones and steroid contraceptives;

(2) the production process of diosgenin can improve the extraction rate and purity of diosgenin, can recycle waste materials, and has the effects of protecting environment and fully recycling resources;

(3) compared with gasoline method, the production process of diosgenin uses supercritical CO₂The diosgenin is extracted by the extraction technology, so that the quality is higher, the production period is greatly shortened, and the product yield is obviously improved under the condition that the production cost is almost the same.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention, are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:

fig. 1 is a schematic view of an enzymatic hydrolysis stirring device according to the present invention.

Description of reference numerals:

1. the enzymolysis system comprises an enzymolysis stirring tank, 11, a first enzymolysis stirring tank, 111, a tank body, 112, a material inlet, 113, an enzyme inlet, 114, a first stirring shaft, 115, a discharge pipeline, 116, a heating device, 117, a crushing device, 12, a second enzymolysis stirring tank, 13, a third enzymolysis stirring tank, 14, a fourth enzymolysis stirring tank, 2, a total enzymolysis stirring tank, 21, a second stirring shaft and 22, and a discharge port.

Detailed Description

The invention will be further illustrated with reference to specific embodiments. It should be noted at first that the data in the experimental examples described below are obtained by the inventors through a large number of experiments, limited to the space, only a part of which is shown in the specification, and those skilled in the art can understand and implement the present invention under the data. These examples are provided only for illustrating the present invention and are not intended to limit the scope of the present invention. Furthermore, it should be understood that various changes or modifications to the invention may be made by those skilled in the art after reading the disclosure of the present invention, and these changes or modifications also fall within the scope of the protection of the present application.

The main idea of the process for extracting the diosgenin is to extract the diosgenin from the dioscorea by solvent extraction and combining ultrasonic and microwave effects, obtain the diosgenin by enzymatic hydrolysis of the diosgenin, and then extract and purify the diosgenin.

Specifically, the production process for extracting diosgenin comprises the following steps:

s1, pretreatment of raw materials: removing hair roots of fresh yam plants, cleaning to remove silt, cutting into sections (the sections are cut into sections with the thickness of 0.1-1 cm), cleaning with water, and separating starch from yam residues, wherein the starch can be comprehensively utilized;

s2, solvent extraction: collecting the dioscorea opposita residue in the step S1, and extracting the dioscorea opposita residue by using a solvent to obtain dioscin;

s3, carrying out enzymolysis on the diosgenin to obtain diosgenin;

s4, extracting, purifying and recrystallizing the diosgenin in the step S3.

Specifically, in step S2, in order to extract dioscin from the dioscorea opposita, the dioscin can be directly extracted by a solvent extraction method under the presence of an organic solvent in combination with the action of microwaves and ultrasound.

As the solvent used in the extraction process, an organic solvent with high solubility to dioscin and low solubility to impurities is selected. The organic solvent passes through the cell wall of the dioscorea opposita and permeates into the interior of the cell, so that the dioscin is dissolved. The dioscin has a certain concentration difference inside and outside cells, the extraction solvent with higher concentration diffuses outwards and takes away a part of dioscin, and the organic solvent outside the cells continuously enters the cells and is circulated to extract dioscin as much as possible. In view of economy and toxicity of organic solvents, ethanol may be selected as the extraction solvent. Since dioscin has a complex composition and has a long or short sugar chain and thus a large polarity or a small polarity, an aqueous solution of ethanol may be used as an extraction solvent. In order to increase the penetrating power of the solvent, accelerate the in and out of the solvent, destroy cell walls and release dioscin as much as possible, microwave and ultrasonic assisted modes can be adopted.

According to the method in the article 'extraction of steroid saponin in dioscorea zingiberensis and diosgenin green preparation process research', the applicant adopts 70% ethanol solution as extraction solvent, and the weight of dioscorea zingiberensis is 1g to the volume ratio of ethanol: 15ml, the microwave power is 500W, and the ultrasonic and microwave synergistic treatment time is 420 s. However, the method is not economical because a large amount of ethanol is needed and the ethanol is not easy to recover. In a fortuitous experiment, the applicant finds that when the weight-to-ethanol volume ratio of the yam residue is continuously increased and the microwave power of different processing time is changed, the yield of the dioscin is not changed, but the extraction time can be shortened. In addition, because the ethanol is added in an excessive amount, the ethanol can be favorably recycled at the end of the reaction and used for the next production. A large number of experiments also prove that the quality of the recovered ethanol has no influence and can be used as an extraction solvent. Can really realize the green low-cost process. Specific data are shown in table 1.

TABLE 1

As can be seen from table 1, when the amount of ethanol added is excessive, the ratio of the weight of the yam residue to the volume of ethanol is 1 g: 40 ml-1 g: when the volume is 55ml, the microwave power of different treatment time is changed, the microwave power is 450-500W within 0-60 s, the microwave power is 400-450W within 60-150 s, and the microwave power is 600W within 150-300 s, so that the treatment time can be shortened under the condition that the saponin yield is unchanged and higher, and the recovery rate is up to 89-95% because the added ethanol is excessive and is convenient to recover. The recovered ethanol can be used continuously.

Specifically, in step S3, diosgenin can be obtained by adding glycosidase to hydrolyze the dioscin extracted from the dioscorea plant. Specifically, the application adopts an enzymolysis agitating unit, as shown in fig. 1. The enzymolysis agitating unit is including dividing enzymolysis agitator tank 1 and total enzymolysis agitator tank 2. The enzymolysis agitator tank 1 is connected in parallel with a plurality of agitator tanks, and is connected with the total enzymolysis agitator tank 2. In this experimental example 1, divide enzymolysis agitator tank 1 to set up four, be first enzymolysis agitator tank 11, second enzymolysis agitator tank 12, third enzymolysis agitator tank 13 and fourth enzymolysis agitator tank 14 respectively, four enzymolysis agitator tanks structure is the same, and the difference place lies in throwing into different glycosidases.

The first enzymatic agitation tank 11 is taken as an example for detailed description. The first enzymolysis agitator tank 11 comprises a tank body 111, a material inlet 112, an enzyme inlet 113, a first agitator shaft 114, a discharge pipeline 115 and a heating device 116. The material inlet 112 and the enzyme inlet 113 are located at the top of the tank body 111, the discharge pipeline 115 is located at the bottom of the tank body 111, one end of the discharge pipeline is connected with the first enzymolysis stirring tank 11, and the other end of the discharge pipeline is connected with the total enzymolysis stirring tank 2. The material inlet 112 is used for throwing the yam plant residues, and the enzyme inlet 113 is used for throwing glycosidase. The dioscorea opposita residue and the glycosidase are fully mixed and hydrolyzed in the tank body 111, and the hydrolyzed mixture enters the total enzymatic hydrolysis stirring tank 2 through the discharge pipeline 115. The first stirring shaft 114 is located in the tank 111, and is driven by a stirrer to fully stir and mix the dioscorea opposita residue and the glycosidase entering the tank 111. Further, a plurality of crushing devices 117 are uniformly or non-uniformly arranged on the first stirring shaft 114, and the crushing devices 117 may be blades. The crushing device 117 extends from the direction of the first stirring shaft 114 to the side wall direction of the tank 111, and can divide the tank 111 into a plurality of small spaces which are communicated with each other. In this application, the yam plant is simply cut into pieces and not ground or ground to fine particles. If the dioscorea opposita is crushed into fine particles and then placed into the enzymolysis stirring tank 1 for hydrolysis treatment, the particles are easy to agglomerate due to the fact that the particle size is too small, glycosidase can only contact the outer surfaces of the agglomerated particles and cannot contact the inner surfaces of the agglomerated particles, the contact area of the dioscorea opposita and the glycosidase is reduced, hydrolysis efficiency is reduced, and the extraction effect of the diosgenin is reduced. After the yam plant residue and the glycosidase are thrown down from the top of the tank 111, they are sufficiently mixed by the stirring action of the first stirring shaft 114, and at the same time, they continuously contact and collide with the crushing device 117. The yam plant residue is crushed and cut into smaller grain sizes by the crushing device 117 while being mixed and contacted with glycosidase, so that the contact area is increased, and the phenomena of easy adhesion and agglomeration caused by too small grain sizes of yam plants are reduced. In addition, because the tank 111 can be divided into a plurality of spaces by the crushing device 117, the dioscorea opposita can be continuously overturned under the driving of the first stirring shaft 114 and collide and extrude with the inner wall of the tank 111 and the crushing device 117, so that the adhesion and agglomeration among the dioscorea opposita particles are reduced, the multi-space and multi-stage continuous hydrolysis is realized, and the hydrolysis effect is improved. Since the enzymatic hydrolysis process usually requires a specific temperature, a heating device 116 is installed on the sidewall of the tank 111 to heat the whole tank to provide a suitable temperature for hydrolysis.

The total enzymolysis agitator tank 2 comprises a second agitating shaft 21 and a discharge port 22. Second (mixing) shaft 21 sets up in total enzymolysis agitator tank 2, and the material after a plurality of branch enzymolysis agitator tanks 1 that set up in parallel accomplished the hydrolysis collects total enzymolysis agitator tank 2 through discharge conduit 115 in, fully mixes under the stirring effect of second (mixing) shaft 21, then discharges through discharge gate 22.

Diosgenin can be generated from saponin in dioscorea plants by hydrolysis of glycosidase. The applicant has made a lot of attempts and improvements in the experimental process, and found that the effect of using the compound glycosidase is better than that of using a single glycosidase, and the content of the prepared diosgenin is higher. The addition amount of each glycosidase is 0.4-0.6% of the weight of the yam residue. In the present application, the glycosidase used is selected from the group consisting of alpha-glucosidase, beta-glucosidase, rhamnosidase, phlorizin hydrolase, glucuronidase, acetylglucosaminidase. Since each glycosidase has the optimum hydrolysis condition, if the complex glycosidase and the yam plant are directly mixed for reaction, the optimum hydrolysis effect cannot be achieved due to the difference of the optimum hydrolysis conditions of each glycosidase. Meanwhile, various interference factors exist due to the simultaneous hydrolysis of various glycosidases, and the respective effects are influenced. Through a plurality of branch enzymolysis agitator tanks 1 that set up in parallel to throw in different glycosidases and dioscorea plant at every branch enzymolysis agitator tank 1 and react, can diversely give full play to the effect of compound glycosidase comprehensively, and adjust according to the optimum hydrolysis temperature and the reaction pH of each glycosidase to ensure the best hydrolysis condition. After respective hydrolysis, the mixture enters a total enzymolysis stirring tank 1 for mixing, and then the obtained material is discharged for the next operation.

Specifically, in step S4, the dioscorea opposita after glycosidase hydrolysis needs to be extracted and purified. Drying hydrolysate hydrolyzed by glycosidase, and adding CO₂Extracting diosgenin by supercritical extraction. After extraction, recrystallization was carried out with ethanol. In the presence of CO₂In the supercritical extraction technology, ethanol is required to be selected as an entrainer. In particular, CO₂The specification of equipment used for supercritical extraction is 2000L multiplied by 3/35MPa, and the equipment comprises: 3 extraction kettles, the single kettle volume of 2000L, 1 separation column, 2 separation kettles and the single kettle volume of 1000L. The extraction pressure is 25-40 MPa, the extraction temperature is 53-62 ℃, and the extraction time is 2-3 h; the pressure of the separation column is 18-26 MPa, and the temperature is 40-60 ℃; the conditions of the two separation kettles are respectively as follows: the pressure is 10-15 MPa, the temperature is 48-55 ℃, the pressure is 5-6 MPa, and the temperature is 30-40 ℃.

To further illustrate CO₂The supercritical extraction and the gasoline extraction have the extraction effect that the extraction pressure is 30MPa, the extraction temperature is 55 ℃, and the extraction time is 2.5 h. The pressure of the separation column is 20MPa, the temperature is 45 ℃, and the conditions of the two separation kettles are as follows: extracting diosgenin at 11MPa, 50 deg.C, 5.6MPa and 35 deg.C. The extracted dregs can be fermented by enzyme to prepare alcohol, or organic fertilizer or animal feed can be produced. Table 2 shows the gasoline process and CO₂Performing supercritical extraction on various indexes of diosgenin.

TABLE 2

Item	CO2Supercritical extraction (based on hydrolysate)	Gasoline method (based on hydrolysate)
			Product yield (%)	5.26	2.27
Purity of the product	96％	94％
			Production cycle (h)	12	30
Production cost (Yuan/kg)	551	563

As can be seen from Table 2, the use of CO₂The supercritical extraction technology has high yield and purity of hydrolysate and can shorten production period under the condition of almost the same production cost.

Example 1

Taking 1kg of fresh yellow ginger, cleaning, cutting into small sections with the thickness of 0.1-1 cm, cleaning with water, and separating starch from yellow ginger residues; adding the turmeric residue into a 70% ethanol solution, wherein the volume of the ethanol solution is 50L, then performing ultrasonic microwave synergistic treatment for 300s, wherein the microwave power is 450W when 0-60 s, 400W when 60-150 s and 150-30W when 60-150 sThe microwave power is 600W at 0 s; after the reaction is finished, dividing the obtained substances into four parts, respectively putting the four parts into a first enzymolysis stirring tank, a second enzymolysis stirring tank, a third enzymolysis stirring tank and a fourth enzymolysis stirring tank through material inlets, simultaneously adding 4g of alpha-glucosidase into the first enzymolysis stirring tank, adjusting the pH to 5.3 and the temperature to 55 ℃, adding 4g of rhamnosidase into the second enzymolysis stirring tank, adjusting the pH to 4.1 and the temperature to 35 ℃, adding 6g of glucuronidase into the third enzymolysis stirring tank, adjusting the pH to 6.5 and the temperature to 55 ℃, adding 5g of beta-glucosidase into the fourth enzymolysis stirring tank, adjusting the pH to 4.5 and the temperature to 60 ℃; drying the hydrolysate after hydrolysis, and adding CO₂Extracting and separating by supercritical extraction technology to obtain diosgenin, and recrystallizing with ethanol to obtain colorless needle crystal pure product. By HPLC analysis, the extraction rate of the dry weight of the raw material is 2.3%, and the purity is 96.6%. .

Example 2

Taking 1kg of fresh peltate yam, cleaning, cutting into small sections with the thickness of 0.1-1 cm, cleaning with water, and separating starch from peltate yam residue; adding the peltate yam rhizome residues into a 70% ethanol solution, wherein the volume of the ethanol solution is 55L, and then performing ultrasonic microwave synergistic treatment for 300s, wherein the microwave power is 480W when 0-60 s, 430W when 60-150 s and 600W when 150-300 s; after the reaction is finished, dividing the obtained substances into four parts, respectively putting the four parts into a first enzymolysis stirring tank, a second enzymolysis stirring tank, a third enzymolysis stirring tank and a fourth enzymolysis stirring tank through material inlets, simultaneously adding 4.5g of alpha-glucosidase into the first enzymolysis stirring tank, adjusting the pH to 5.0 and the temperature to 51 ℃, adding 4.8g of glucuronidase into the second enzymolysis stirring tank, adjusting the pH to 7.0 and the temperature to 56 ℃, adding 5.2g of rhamnosidase into the third enzymolysis stirring tank, adjusting the pH to 4.5 and the temperature to 42 ℃, adding 5.5g of phlorizin hydrolase into the fourth enzymolysis stirring tank, adjusting the pH to 5.5 and the temperature to 60 ℃; drying the hydrolysate after hydrolysis, and adding CO₂Extracting and separating by supercritical extraction technology to obtain diosgenin, and recrystallizing with ethanol to obtain colorless needle crystal pure product. By HPLC analysis, onThe extraction rate of the dry weight of the raw material is 2.2 percent, and the purity is 96.8 percent.

Example 3

Taking 1kg of fresh yam, cleaning, cutting into small sections with the thickness of 0.1-1 cm, cleaning with water, and separating starch from yam residues; adding the yam rhizome residues into a 70% ethanol solution, wherein the volume of the ethanol solution is 48L, and then performing ultrasonic microwave synergistic treatment for 300s, wherein the microwave power is 460W when 0-60 s, 420W when 60-150 s and 600W when 150-300 s; dividing the obtained substance into four parts after the reaction is finished, respectively putting the four parts into a first enzymolysis stirring tank, a second enzymolysis stirring tank, a third enzymolysis stirring tank and a fourth enzymolysis stirring tank through material inlets, simultaneously adding 4g of beta-glucosidase into the first enzymolysis stirring tank, adjusting the pH to be 4.2 and the temperature to be 62 ℃, adding 5.4g of rhamnosidase into the second enzymolysis stirring tank, adjusting the pH to be 4.3 and the temperature to be 50 ℃, adding 5.8g of glucuronidase into the third enzymolysis stirring tank, adjusting the pH to be 6.5 and the temperature to be 50 ℃, adding 5g of alpha-glucosidase into the fourth enzymolysis stirring tank, adjusting the pH to be 5.0 and the temperature to be 52 ℃; drying the hydrolysate after hydrolysis, and adding CO₂Extracting and separating by supercritical extraction technology to obtain diosgenin, and recrystallizing with ethanol to obtain colorless needle crystal pure product. By HPLC analysis, the extraction rate of the dry weight of the raw materials is 2.6%, and the purity is 97.7%.

Comparative example 1

According to the method of example 1 in CN101857855B, 1kg of yam is pretreated, hydrolyzed by the type i complex enzyme preparation for the first hydrolysis, hydrolyzed by the type ii complex enzyme preparation for the second hydrolysis, and extracted and purified to obtain the dioscin aglycone pure product, wherein the extraction rate of the dry weight of the raw material is 1.4%, and the purity is 90.5%.

Comparative example 2

The preparation method of comparative example 2 is different from that of example 1 in that the ultrasonic microwave synergistic treatment time is 420s and the microwave power is always maintained at 500W during the solvent extraction process. HPLC analysis of the diosgenin finally obtained shows that the extraction rate of the dry weight of the raw materials is 1.8%, and the purity is 95.7%.

The diosgenin is extracted from the dioscorea plants by the method, so that strong acid and petroleum are avoided, the cost is reduced, and the purpose of clean production of the diosgenin is achieved. The starch in the dioscorea plants is exposed by pretreating the raw materials, so that the starch can be recycled, the coating of the starch on the target product is reduced, and the target product is released as much as possible. Then combining solvent extraction, glycosidase hydrolysis and CO₂The method of supercritical extraction technology improves the extraction rate and purity of the prepared diosgenin, and the produced diosgenin raw material drug meets the international standard. The diosgenin of the embodiments 1 to 3 has the extraction rate of 2.2 to 2.6 percent and the purity of 96.6 to 97.7 percent. While comparative example 1 had an extraction rate of 1.4% and a purity of 90.5%, comparative example 2 had an extraction rate of only 1.8% and a purity of 95.7% by constant microwave power treatment in the solvent extraction step. Therefore, the extraction process disclosed by the application plays the unique role of various glycosidases, can better react with dioscorea plants, and improves the extraction rate and the purity of diosgenin through the process improvement of each step.

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.