阅读说明：本技术 一种从空心莲子草中提取黄酮类化合物的方法 (Method for extracting flavonoid compounds from alternanthera philoxeroides ) 是由 王辛 于 2020-12-22 设计创作，主要内容包括：本发明公开了一种从空心莲子草中提取黄酮类化合物的方法,具体涉及天然产物生物分离领域,该方法包括空心莲子草的采集和清洗、压榨、榨汁除杂、浓缩、醇浸提、醇提液除醇、催化水解、浓缩结晶等步骤,还可以包括压榨后水洗、低温气爆、萃取等步骤,催化水解还可以采用相应的生物酶。采用该方法能够从空心莲子草新鲜植株中提取纯度较高黄酮类物质。既消除空心莲子草对自然环境的危害,又能得到具有抗肿瘤活性、抗病毒、抑菌和抗氧化等能力的黄酮类物质,克服了现有技术中只能从干燥植株中提取黄酮类物质和黄酮苷类物质的混合物,黄酮类物质纯度不高、品质不高的缺陷,一举两得。(The invention discloses a method for extracting flavonoid compounds from alternanthera philoxeroides, and particularly relates to the field of bioseparation of natural products. The method can be used for extracting flavonoids with higher purity from fresh plants of alternanthera philoxeroides. The method not only eliminates the harm of the alternanthera philoxeroides to the natural environment, but also can obtain flavonoids with the capabilities of antitumor activity, virus resistance, bacteriostasis, oxidation resistance and the like, overcomes the defects that the prior art can only extract a mixture of flavonoids and flavonoid glycosides from dry plants, and the flavonoids have low purity and low quality, and achieves two purposes at one time.)

1. A method for extracting flavonoid compounds from alternanthera philoxeroides comprises the following steps:

step 1) collecting and cleaning alternanthera philoxeroides: collecting fresh alternanthera philoxeroides plants from a natural protection area, washing away impurities such as silt and the like by using water, and removing surface water;

step 2) squeezing: squeezing the cleaned fresh alternanthera philoxeroides plant obtained in the step 1) in a squeezing device to obtain juice and solid residues;

step 3), juicing and impurity removing: microfiltering and filtering the juice obtained in the step 2) to obtain juice filtrate, removing chlorophyll impurities in the juice filtrate by using a petroleum ether extraction method, and removing impurities such as polysaccharide and the like in the juice filtrate by using an alcohol precipitation method to obtain purified juice filtrate;

step 4), juicing and concentrating: pumping the purified juicing filtrate obtained in the step 3) into a rotary evaporation device, and removing alcohol and redundant water in the juicing filtrate to obtain a juicing concentrated solution;

step 5) alcohol leaching: putting the solid residue obtained in the step 2) into 80-90% ethanol solution, and performing alcohol leaching to obtain alcohol extract;

step 6) removing alcohol from the alcohol extract: adding the alcohol extract obtained in the step 5) into deionized water with the same volume, and pumping the mixture into a rotary evaporation device to remove ethanol in the rotary evaporation device to obtain an alcohol extract solution;

step 7) catalytic hydrolysis: mixing the juice concentrate obtained in the step 4) and the alcohol extract solution obtained in the step 6), and adding solid acid into the mixture to hydrolyze flavonoid glycoside substances into flavonoid substances to obtain catalytic hydrolysate;

step 8) concentration and crystallization: and (3) placing the catalytic hydrolysate obtained in the step 7) in a rotary evaporation device, concentrating under reduced pressure to crystallize out flavonoid substances in the catalytic hydrolysate, and carrying out solid-liquid separation to obtain the flavonoid substances.

2. The method for extracting flavonoids from alternanthera philoxeroides as claimed in claim 1, wherein the squeezing device in step 2) comprises a commercially available double-roll squeezer, the diameter of the squeezing roll is 10-20 cm, the pressure between the rolls is 30-60N/cm, and the squeezing temperature is 12-23 ℃.

3. The method for extracting flavonoids from alternanthera philoxeroides as claimed in claim 1, wherein the microfiltration operation in step 3) adopts a cellulose acetate microfiltration membrane with a pore size of 0.45 micron, the oil-water ratio of the chlorophyll extracted by petroleum ether is 1: 3-2: 3, the temperature is 20-32 ℃, the stirring speed is 100-300 r/min, the extraction time is 40-60 min, the mass percentage concentration of ethanol for removing polysaccharides by an alcohol precipitation method is 76% -79%, 10-20 r/min, the stirring is 8-10 min, and then the precipitate is removed by filtration.

4. The method for extracting flavonoids from alternanthera philoxeroides as claimed in claim 1, wherein the juicing and concentrating operation of step 4) is divided into three stages, the first stage: the vacuum degree is-50 to-63 kPa, the temperature is 45 to 56 ℃, and the time is 1 to 1.5 hours; and a second stage: the vacuum degree is-70 to-79 kPa, the temperature is 53 to 64 ℃, and the time is 1.6 to 2.1 h; and a third stage: the vacuum degree is-78 to-92 kPa, and the temperature is 74 to 87 ℃.

5. The method for extracting flavonoids from alternanthera philoxeroides according to claim 1, wherein the solid-liquid ratio of alcohol leaching in the step 5) is 1: 7-1: 16, the temperature is 70-82 ℃, and the time is 24-48 h.

6. The method for extracting flavonoids compounds from alternanthera philoxeroides according to claim 1, wherein the alcohol removal in the step 6) is performed under the vacuum degree of-56 to-68 kPa at the temperature of 48 to 59 ℃, so that the ethanol in the alcohol is removed to be less than 0.9 mass percent.

7. The method for extracting flavonoids from alternanthera philoxeroides according to claim 1, wherein the solid acid in step 7) comprises an H-type macroporous strong-acid cation exchange resin.

8. The method for extracting flavonoids compounds from alternanthera philoxeroides according to claim 1, wherein the addition amount of the solid acid in the step 7) is 10% -24% of the mass of the liquid to be catalyzed, the temperature is 80-86 ℃, the stirring speed is 28-33 r/min, and the catalysis time is 4-8 h.

9. The method for extracting flavonoids from alternanthera philoxeroides according to claim 1, wherein the vacuum degree of the reduced pressure concentration in the step 8) is-81 to-93 kPa, the evaporation temperature is 72 to 83 ℃, and the concentration multiple is 8 to 19 times.

Technical Field

The invention relates to the field of biological separation of natural products, in particular to a method for extracting flavonoid compounds from alternanthera philoxeroides.

Background

Alternanthera philoxeroides is a perennial root herbaceous plant of the genus Alternanthera, Amaranthaceae, also named Amaranthus hypochondriacus, Alternanthera philoxeroides, Arachis hypogaea, etc. Native to Brazil, and after being introduced in China, the wild vegetable is changed into wild vegetable and widely grows in ponds and ditches. The plant has strong reproductive capacity, can become a dominant plant in a certain area of subtropical and temperate zones, harms the biodiversity of the area, and is listed as a preliminary list of foreign invasive species in China by the department of ecological environmental protection.

The alligator alternanthera can be used as a medicine by using the whole herb and has the effects of resisting virus, resisting bacteria, protecting liver and the like. The extract contains high concentration flavonoids and their glycoside derivatives. Research shows that the compound has stronger antiviral effect, such as respiratory syncytial virus, hepatitis B virus, influenza virus, hantavirus, herpes virus and the like, and also has anticancer, bacteriostatic, antioxidant and other effects.

At present, the method for extracting flavonoids from alternanthera philoxeroides is to put alternanthera philoxeroides hay into a certain amount of polar solvent such as ethanol and the like, and reflux-extract the alternanthera philoxeroides hay at a certain temperature. It has the following disadvantages: the hay is used as a raw material, and the fresh grass is not suitable for the method; the extraction period is long, and the extraction period often needs tens of hours; the extracted flavonoids include flavones and glycoside derivatives thereof, the purity is low, and the quality stability is difficult to guarantee.

Therefore, it is required to develop a method for extracting flavonoids from fresh grass plants, which has a short extraction period and can obtain relatively pure flavonoids.

The above information disclosed in this background section is only for enhancement of understanding of the background of the disclosure and therefore it may contain information that does not constitute prior art that is already known to a person of ordinary skill in the art.

Disclosure of Invention

The invention aims to provide a method for extracting flavonoids from alternanthera philoxeroides.

In order to solve the technical problems, the invention provides a method for extracting flavonoid compounds from alternanthera philoxeroides, which comprises the following steps:

step 1) collecting and cleaning alternanthera philoxeroides: collecting fresh alternanthera philoxeroides plants from a natural protection area, washing away impurities such as silt and the like by using water, and removing surface water;

step 2) squeezing: squeezing the cleaned fresh alternanthera philoxeroides plant obtained in the step 1) in a squeezing device to obtain juice and solid residues;

step 3), juicing and impurity removing: microfiltering and filtering the juice obtained in the step 2) to obtain juice filtrate, removing chlorophyll impurities in the juice filtrate by using a petroleum ether extraction method, and removing impurities such as polysaccharide and the like in the juice filtrate by using an alcohol precipitation method to obtain purified juice filtrate;

step 4), juicing and concentrating: pumping the purified juicing filtrate obtained in the step 3) into a rotary evaporation device, and removing alcohol and redundant water in the juicing filtrate to obtain a juicing concentrated solution;

step 5) alcohol leaching: putting the solid residue obtained in the step 2) into 80-90% ethanol solution, and performing alcohol leaching to obtain alcohol extract;

step 6) removing alcohol from the alcohol extract: adding the alcohol extract obtained in the step 5) into deionized water with the same volume, and pumping the mixture into a rotary evaporation device to remove ethanol in the rotary evaporation device to obtain an alcohol extract solution;

step 7) catalytic hydrolysis: mixing the juice concentrate obtained in the step 4) and the alcohol extract solution obtained in the step 6), and adding solid acid into the mixture to hydrolyze flavonoid glycoside substances into flavonoid substances to obtain catalytic hydrolysate;

step 8) concentration and crystallization: and (3) placing the catalytic hydrolysate obtained in the step 7) in a rotary evaporation device, concentrating under reduced pressure to crystallize out flavonoid substances in the catalytic hydrolysate, and carrying out solid-liquid separation to obtain the flavonoid substances.

The squeezing device in the step 2) comprises a commercial double-roll squeezer, the diameter of each squeezing roll is 10-20 cm, the pressure between the rolls is 30-60N/cm, and the squeezing temperature is 12-23 ℃. Squeezing fresh alternanthera philoxeroides, and separating most of water from plants, so that flavonoids can be extracted from the fresh alternanthera philoxeroides plants, the plant drying step is omitted, and the drying energy consumption is saved; the water leaching effect can be still realized after the water leaching step is omitted, and the water-soluble flavonoid glycoside substances in the water are extracted, so that the water consumption and the energy consumption of the water leaching are saved; the structure of each tissue of the alternanthera philoxeroides plant can be furthest destroyed, and the leaching speed in the subsequent extraction step is favorably accelerated.

Preferably, the pressing step is performed under an inert gas blanket. For example, the squeezing device is disposed in a closed space, the closed space is filled with inert gas (such as nitrogen), and the closed space is kept at a slight positive pressure, which means that the gas pressure is 1000Pa to 2000Pa greater than the atmospheric pressure, to prevent oxygen in the outside air from entering the closed space. Further preferably, before the fresh alternanthera philoxeroides plant enters the closed space where the squeezing device is located, inert gas is used for blowing the fresh alternanthera philoxeroides plant, so that the possibility that oxygen in the air enters the closed space is reduced.

The squeezing is carried out under the protection of inert gas, so that the oxidation reaction of hydroxyl in the flavonoid can be greatly reduced, the oxidation resistance of the flavonoid can be kept at a higher level, and the quality of the flavonoid can be improved.

Further preferably, a water washing step can be added after squeezing to wash out the squeezed juice remained in the plant gaps, so that the yield is improved. And (3) washing with water at a solid-liquid ratio of 1: 3-1: 7 at a temperature of 16-28 ℃ for 20-50 min, filtering with 100-200 mesh nylon filter cloth, and extruding to remove water in solid gaps.

And 3) carrying out microfiltration operation by adopting a 0.45-micron-aperture cellulose acetate microfiltration membrane, extracting chlorophyll by adopting petroleum ether at a temperature of 20-32 ℃ and a stirring speed of 100-300 r/min for 40-60 min, removing polysaccharide by adopting an alcohol precipitation method, wherein the mass percentage concentration of ethanol is 76-79% and 10-20 r/min, stirring for 8-10 min, and then filtering to remove precipitate.

The juicing and concentrating operation in the step 4) is divided into three stages, namely a first stage: the vacuum degree is-50 to-63 kPa, the temperature is 45 to 56 ℃, and the time is 1 to 1.5 hours; and a second stage: the vacuum degree is-70 to-79 kPa, the temperature is 53 to 64 ℃, and the time is 1.6 to 2.1 h; and a third stage: the vacuum degree is-78 to-92 kPa, and the temperature is 74 to 87 ℃. Removing ethanol to below 1.3 percent by mass; concentrating to 0.1-0.2 times of the volume of the juice obtained in the step 2). The first stage has the main function of distilling the ethanol added in the alcohol precipitation step; the second stage has the main function of evaporating partial ethanol and water in the form of alcohol-water azeotrope; the main function of the third stage is to distill off excess water.

The solid-liquid ratio of alcohol leaching in the step 5) is 1: 7-1: 16, the temperature is 70-82 ℃, and the time is 24-48 h.

Preferably, a low-temperature steam explosion pretreatment step can be added before the step 5), the solid slag obtained in the step 2) is placed in a closed metal pressure-bearing container, compressed nitrogen is slowly introduced (in order to reduce the oxidation degree of flavonoids), so that the gas pressure in the container reaches more than 2.0MPa, the pressure rise time is more than 60s (in order to prevent the temperature from being too high), the pressure is maintained for more than 90s (in order to ensure that high-pressure gas can permeate into the alternanthera philoxeroides cells), the temperature is maintained at 60-80 ℃ (in order to provide enough energy for the gasification of water in the cells when the gas pressure is instantly reduced), and the gas pressure in the container is reduced to 101kPa within 0.1s (in order to destroy the complete structure of the cells and accelerate the alcohol leaching speed). The above process is circulated for more than 7 times.

The vacuum degree of the alcohol removal in the step 6) is-56 to-68 kPa, the temperature is 48 to 59 ℃, and the ethanol in the alcohol is removed to be less than 0.9 mass percent.

The solid acid in the step 7) comprises H-type macroporous strong-acid cation exchange resin, and the H-type macroporous strong-acid cation exchange resin comprises resin with the trade mark of D001.

The conditions for converting the macroporous strong-acid cation exchange resin into the H type are as follows: the resin completely pretreated according to the method in the prior art is immersed into a transformation solution with the sulfuric acid concentration of 1.5-2.0 mol/L and the zinc sulfate concentration of 0.001-0.002 mol/L, the volume of the solution is 2-4 times of the volume of the resin, the stirring speed is 20-30 r/min, the immersion time is 3-5H, then the resin is washed to be neutral by deionized water, and the circulation is carried out for more than 3 times, so that the resin is fully transformed into the H type.

The inventor finds that the addition of a trace amount of zinc sulfate in the transformation solution can accelerate the rate of catalytic conversion of flavonoid glycosides by solid acid.

The adding amount of the solid acid in the step 7) is 10-24% of the mass of the liquid to be catalyzed, the temperature is 80-86 ℃, the stirring speed is 28-33 r/min, and the catalysis time is 4-8 h.

Further preferably, the catalyst for catalyzing hydrolysis in step 7) may further comprise a glycosidase. The conditions for hydrolyzing the flavonoid glycoside substances into flavonoid substances and sugar by adopting the biological enzyme are as follows: a glucosidase: rhamnosidase is 2: 1-3: 1; the total enzyme addition amount is 1-2% of the liquid mass, the pH value is 4.8-5.3, the temperature is 56-63 ℃, and the enzyme hydrolysis time is 10-16 h. The biological enzyme is a commercial enzyme.

The vacuum degree of the reduced pressure concentration in the step 8) is-81 to-93 kPa, the evaporation temperature is 72 to 83 ℃, and the concentration multiple is 8 to 19 times.

Further preferably, an extraction step can be added after the step 7) to extract out flavonoids substances generated by catalytic hydrolysis. The extracting agent is a mixture of ethanol and ethyl acetate, the mass ratio of the ethanol to the ethyl acetate is 1: 9-1: 12, the extraction temperature is 12-15 ℃, and the extraction time is 3.4-6.1 h. Standing for phase separation, and then distilling off the extractant in the extract liquor to obtain flavonoid substance powder.

The invention has the technical effects and advantages that:

the method for extracting the flavonoid compound from the alternanthera philoxeroides has the beneficial effects that: the method has the advantages that the fresh alligator alternanthera is used as the raw material, the flavonoid substances with biological activity are extracted, the harm of the alligator alternanthera to the ecological environment of plants is eliminated, the flavonoid substances with the capabilities of anti-tumor activity, anti-virus, bacteriostasis, antioxidation and the like can be obtained, the defects that the mixture of the flavonoid substances and the flavonoid glycoside substances can only be extracted from dry plants in the prior art, the purity of the flavonoid substances is low, and the quality is not high are overcome, and the method has two purposes.

Drawings

FIG. 1 is a schematic flow chart of the method for extracting flavonoids from Alternanthera philoxeroides according to the present invention;

FIG. 2 is a schematic flow chart of an embodiment of the method for extracting flavonoids from alternanthera philoxeroides according to the present invention.

Detailed Description

For a further understanding of the present invention, reference will now be made to the following descriptions taken in conjunction with the accompanying examples, and it is to be understood that the descriptions are intended to illustrate further features and advantages of the invention, rather than to limit the scope of the appended claims.

Examples 1 to 6

The method is adopted to extract flavonoid compounds from alternanthera philoxeroides:

step 1) collecting and cleaning alternanthera philoxeroides: collecting fresh alternanthera philoxeroides plants from a natural protection area, washing away impurities such as silt and the like by using water, and removing surface water;

step 2) squeezing: the cleaned fresh alligator alternanthera plants obtained in the step 1) are placed into a squeezing device to be squeezed to obtain squeezed juice and solid residues, the squeezing device in the step 2) comprises a commercial double-roll squeezer, and parameters such as straight warp of a squeezing roll, pressure between rolls, squeezing temperature and the like are shown in table 1;

step 3), juicing and impurity removing: microfiltering and filtering the juice obtained in the step 2) to obtain juice filtrate, removing chlorophyll impurities in the juice filtrate by using a petroleum ether extraction method, removing impurities such as polysaccharide and the like in the juice filtrate by using an alcohol precipitation method to obtain purified juice filtrate, wherein the parameters of the microfiltration membrane aperture, the extraction oil-water ratio, the extraction temperature, the stirring speed, the extraction time, the alcohol concentration of the alcohol precipitation, the rotating speed, the stirring time and the like are shown in tables 1 and 2;

step 4), juicing and concentrating: pumping the purified juicing filtrate obtained in the step 3) into a rotary evaporation device, removing alcohol and redundant water in the juicing filtrate to obtain a juicing concentrated solution, wherein the juicing concentration operation in the step 4) is divided into three stages, and parameters such as vacuum degree, temperature, time and the like of the three stages are shown in tables 3 and 4;

step 5) alcohol leaching: putting the solid residue obtained in the step 2) into 80-90% ethanol solution, and carrying out alcohol leaching to obtain alcohol extract, wherein the parameters of alcohol-to-solid ratio, temperature, time and the like are shown in table 5;

step 6) removing alcohol from the alcohol extract: adding the alcohol extract obtained in the step 5) into deionized water with the same volume, pumping into a rotary evaporation device, removing ethanol to obtain an alcohol extract solution, wherein the parameters of the alcohol removal vacuum degree, the temperature, the alcohol removal effect and the like are shown in table 6;

step 7) catalytic hydrolysis: mixing the concentrated juice obtained in the step 4) and the obtained alcohol extract solution obtained in the step 6), adding solid acid into the mixed solution to hydrolyze flavonoid glycoside substances into flavonoid substances, and obtaining catalytic hydrolysate, wherein the parameters of the solid acid type, the sulfuric acid concentration of the transformation solution, the zinc sulfate concentration, the volume of the transformation solution, the stirring speed, the time and the like are shown in table 7;

step 8) concentration and crystallization: placing the catalytic hydrolysate obtained in the step 7) in a rotary evaporation device, concentrating under reduced pressure to crystallize out flavonoid substances, and carrying out solid-liquid separation to obtain the flavonoid substances, wherein the parameters of vacuum degree, temperature, concentration multiple and the like of the reduced pressure concentration are shown in Table 8.

Table 1 main operating parameters of the process for extracting flavonoids according to the example of the invention

Table 2 main operating parameters of the process for extracting flavonoids according to the example of the invention (ii)

Table 3 main operating parameters (three) of the process for extracting flavonoids according to the example of the invention

Table 4 main operating parameters of the process for extracting flavonoids according to the example of the invention (iv)

Table 5 main operating parameters of the process for extracting flavonoids according to the example of the invention (v)

Table 6 main operating parameters (six) of the process for extracting flavonoids according to the example of the invention

Example number	Degree of vacuum (kPa) for alcohol removal	Temperature (. degree.C.)	Concentration after alcohol removal (%)
				1	-56～-58	50	0.9％
2	-59～-62	59	0.8％
				3	-63～-65	56	0.7％
4	-64～-66	48	0.78％
				5	-65～-67	52	0.84％
6	-66～-68	54	0.72％

Table 7 main operating parameters (seven) of the method for extracting flavonoids according to the example of the invention

Table 8 main operating parameters (eight) of the process for extracting flavonoids according to the example of the invention

The method of the above example was used to obtain flavonoids from alternanthera philoxeroides, the yield and purity of flavonoids and the content of flavonoid glycosides therein are shown in table 9, and the yield of flavonoids was based on all flavonoids contained in alternanthera philoxeroides.

TABLE 9 technical Effect (I) obtained by the embodiments of the present invention

Examples 7 to 8

The basic operating parameters used in examples 7 to 8 were the same as in example 5.

Examples 7 to 8 the pressing step in step 2) was carried out under the protection of an inert gas, nitrogen, and the pressing device was disposed in an enclosed space, which was filled with an inert gas and kept at a slight positive pressure to prevent oxygen in the outside air from entering the enclosed space.

The gas pressure in the enclosed space of example 7 was 1000Pa greater than atmospheric pressure. Because the oxidation degree of the flavonoid compound is reduced, the purity of the extracted flavonoid compound reaches 88.7 percent, which is 5.3 percent higher than that of the result in example 5.

Before the fresh alternanthera philoxeroides plants in the embodiment 8 enter the closed space where the squeezing device is located, inert gas is used for blowing the plants, and the gas pressure in the closed space is 2000Pa higher than the atmospheric pressure. Because the oxidation degree of the flavonoid compound is further reduced, the purity of the extracted flavonoid compound reaches 91.5 percent, which is 8.1 percent higher than that of the result in example 5.

Examples 8 to 9

The basic operating parameters used in examples 8 to 9 were the same as in example 3.

The step 2) of the examples 8-9 is followed by a water washing step to wash out the juice remaining in the plant spaces and improve the yield.

The solid-liquid ratio of the water washing of the embodiment 8 is 1:3, the temperature is 28 ℃, the water washing soaking time is 20min, after the completion, the water in solid gaps is removed by filtering through a 200-mesh nylon filter cloth and squeezing. Because the water-soluble flavonoid glycoside substances in the plant gaps are recovered, the yield of the extracted flavonoid compounds reaches 81.1 percent, which is 6.2 percent higher than the result of the example 3.

The solid-liquid ratio of the water washing of the example 9 is 1:7, the temperature is 16 ℃, the water washing soaking time is 50min, after the completion, the water in solid gaps is removed by filtering through a 100-mesh nylon filter cloth and squeezing. Because the water-soluble flavonoid glycoside substances in the plant gaps are recovered, the yield of the extracted flavonoid compounds reaches 82.3 percent, which is 7.4 percent higher than the result of the example 3.

Examples 10 to 11

The basic operating parameters used in this example are the same as in example 4.

In the embodiment 10-11, a low-temperature steam explosion pretreatment step is added before the step 5), the solid slag obtained in the step 2) is placed in a closed metal pressure-bearing container, compressed nitrogen is slowly introduced to enable the gas in the container to reach a certain pressure, a certain time is kept and a certain temperature is kept, then the gas pressure in the container is reduced to the normal pressure within a period of time, and the process is circulated for multiple times.

In example 10, the gas pressure was 2.0MPa or more, the pressure-increasing time was 60 seconds, the pressure was maintained for 90 seconds, the temperature was maintained at 60 ℃, the gas pressure in the vessel was reduced to 101kPa within 0.1 seconds, and the above process was circulated 7 times. Because the complete structure of plant tissues and cells is damaged, the extraction is facilitated, the alcohol leaching time is shortened to 30 hours and is shortened by over 31 percent, the yield of the flavonoid compounds obtained by extraction reaches 82.8 percent, and the yield is improved by 7.2 percent compared with the result of example 4.

In example 11, the gas pressure was 3.0MPa or more, the pressure-increasing time was 70 seconds, the pressure was maintained for 100 seconds, the temperature was maintained at 80 ℃ and the gas pressure in the vessel was reduced to 101kPa within 0.05 seconds, and the above process was repeated 9 times. Because the complete structure of plant tissues and cells is more effectively destroyed, the extraction is facilitated, the alcohol leaching time is shortened to 20 hours and is shortened by more than 54 percent, the yield of the extracted flavonoid compounds reaches 83.9 percent, and the yield is improved by 8.3 percent compared with the result of example 4.

Examples 12 to 13

The basic operating parameters used in this example are the same as in example 2.

Step 7) of examples 12-13 was replaced by bio-enzyme catalysis, with glycosidase hydrolyzing the flavonoid glycosides to flavonoids and sugars.

The enzyme catalysis conditions for example 12 were: a glucosidase: the adding amount of rhamnosidase is 1% of the liquid mass, the pH is 4.8, the temperature is 63 ℃, the enzyme hydrolysis time is 10h, and the biological enzyme is commercial enzyme. Because the enzyme catalysis effect is better, the content of flavonoid glycoside compounds in the extracted flavonoid compounds is reduced to 2.7 percent and reduced by 1.2 percent.

The enzyme catalysis conditions for example 13 were: a glucosidase: rhamnosidase is 3: 1; the total enzyme addition amount is 2 percent of the liquid mass, the pH value is 5.3, the temperature is 56 ℃, the enzyme hydrolysis time is 16h, and the biological enzyme is a commercial enzyme. Because the enzyme catalysis effect is better, the content of flavonoid glycoside compounds in the extracted flavonoid compounds is reduced to 2.1 percent and reduced by 1.8 percent.

Example 14

The basic operating parameters used in this example are the same as in example 6.

The step 7) of the embodiment 14 is added with an extraction step, the used extractant is a mixture of ethanol and ethyl acetate, the mass ratio of the mixture is 1:10, the extraction temperature is 14 ℃, the extraction time is 5.6h, the mixture is kept still for more than 8h for phase separation, and then the extractant in the extraction liquid is distilled out to obtain flavonoid powder. The purity of the extracted flavonoid compound is improved to 89.2 percent and is improved by 4.6 percent; wherein the content of the flavonoid glycoside compound is reduced to 2.3 percent and reduced by 1.7 percent.

The foregoing shows and describes the general principles and broad features of the present invention and advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.