Comprehensive extraction method for extracting eucommia ulmoides feed additive, chlorogenic acid, eucommia ulmoides rubber and dietary fiber from eucommia ulmoides

Abstract

The invention relates to the technical field of comprehensive extraction of natural products, and discloses a comprehensive extraction method for extracting a eucommia ulmoides feed additive, chlorogenic acid, eucommia ulmoides rubber and dietary fibers from eucommia ulmoides, which comprises the following steps: pretreatment of raw materials: performing microwave drying on eucommia ulmoides leaves, barks and seed shells, crushing, and sieving with a sieve of 8-12 meshes; performing continuous countercurrent ultrasonic extraction; preparing a feed additive; purifying chlorogenic acid; preparing the protein oligopeptide; physically separating residues, and centrifugally separating to obtain gutta-percha silk and crude fibers; refining eucommia ulmoides rubber; and preparing dietary fibers: performing alkali treatment, enzymolysis and drying on the crude fibers to obtain the dietary fibers. A continuous countercurrent ultrasonic extractor is adopted to carry out low-temperature and high-efficiency ultrasonic-assisted extraction, so that the effects of protecting the activity of thermosensitive components, greatly shortening the extraction time and remarkably reducing the solvent dosage and energy consumption are achieved; and reverse osmosis membrane concentration, low-temperature vacuum concentration and belt drying are combined, so that the effects of completely retaining the eucommia ulmoides feed additive and chlorogenic acid active substances and facilitating automatic continuous operation are achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of comprehensive extraction of natural products, in particular to a comprehensive extraction method for extracting eucommia feed additives, chlorogenic acid, eucommia rubber and dietary fiber from eucommia. Background Art

[0002] Eucommia ulmoides, a relict tree species of the genus Eucommia in the Eucommia family, is endemic to my country and holds significant medicinal and industrial value. It contains a rich array of active ingredients, including lignans, chlorogenic acid, flavonoids, xanthocyanin, geniposide, aucubin, pinoresinol diglucoside, syringaresinol diquinone glycoside, and α-linolenic acid. These ingredients impart numerous health benefits to Eucommia ulmoides, including immune regulation, antioxidant activity, anti-aging, lipid-lowering, blood pressure-lowering, blood sugar-lowering, tocopherol-lowering, cosmetic enhancement, and bone and muscle strengthening. Furthermore, Eucommia rubber, primarily composed of trans-1,4-polyisoprene, exhibits shape memory and rubber elasticity, making it a promising medical material and raw material for rubber products.

[0003] However, current extraction methods for Eucommia ulmoides feed additives, chlorogenic acid, and Eucommia rubber present numerous challenges. For example, traditional methods such as organic solvent extraction, acid-water extraction, and enzymatic hydrolysis suffer from low raw material utilization, high consumption of acidic or alkaline water or organic solvents, low extraction yields, low product purity, high energy consumption during production, and severe environmental pollution. These issues hinder the efficient utilization of Eucommia ulmoides resources and the widespread application of its products. Summary of the Invention

[0004] In response to the shortcomings of the existing technology, the present invention provides a comprehensive extraction method for extracting Eucommia ulmoides feed additives, chlorogenic acid, Eucommia rubber, and dietary fiber from Eucommia ulmoides, which solves the problems of low raw material utilization, large solvent consumption, low extraction rate and product purity, safety risks in the production process, and serious environmental pollution in the existing technology.

[0005] To achieve the above objectives, the present invention is implemented by the following technical scheme: a comprehensive extraction method for extracting Eucommia ulmoides feed additives, chlorogenic acid, Eucommia ulmoides rubber, and dietary fiber from Eucommia ulmoides, comprising the following steps: S1. Raw material pretreatment: Eucommia ulmoides leaves, skins and seed shells are microwave-dried and then crushed through an 8-12 mesh sieve; S2. Continuous countercurrent ultrasonic extraction: The raw material and 5-10 times the amount of water are extracted in a continuous countercurrent ultrasonic extractor, and the extract is separated by a horizontal screw centrifuge and a butterfly centrifuge to obtain a filtrate and a residue; S3, preparation of feed additive: the filtrate is concentrated by reverse osmosis membrane, concentrated under reduced pressure by low-temperature vacuum concentrator, and dried by belt dryer to obtain Eucommia ulmoides feed additive; S4, purification of chlorogenic acid: The filtrate from S3 was adsorbed on a macroporous adsorption resin column, washed with water to remove impurities, and then eluted with ethanol. The eluate was concentrated and dried to obtain chlorogenic acid from Eucommia ulmoides; S5. Preparation of protein oligopeptides: The resin column washing liquid is hydrolyzed with protease, separated by 3000D ultrafiltration membrane and nanofiltration membrane, and the retentate is concentrated and dried to obtain Eucommia protein oligopeptides; S6, physical separation of residue: The residue in S2 is coarsely ground with water to remove impurities and then finely ground. The slurry is separated into layers in a liquid-liquid separator and centrifuged to obtain eucommia gum filaments and crude fibers; S7, refining eucommia rubber: dissolving the eucommia rubber thread in an alkaline aqueous solution, membrane filtering, decolorizing, acid precipitation, and drying to obtain eucommia rubber; S8. Preparation of dietary fiber: The crude fiber is subjected to alkali treatment, enzymatic hydrolysis, and drying to obtain dietary fiber.

[0006] The above-mentioned technical solution utilizes 3-8 series-series countercurrent ultrasonic extraction equipment, combining specific ultrasonic frequencies and power densities at low temperatures to achieve efficient and gentle extraction of the raw materials. This process maximizes the protection of heat-sensitive active substances such as chlorogenic acid from degradation. Furthermore, the countercurrent design and controlled feed flow rate significantly reduce solvent usage, significantly improve extraction efficiency, and facilitate automated and continuous operation. Subsequently, the filtrate is rapidly pre-concentrated under high pressure using a reverse osmosis membrane. Combined with low-temperature vacuum concentration and gentle belt vacuum drying, this fully preserves the bioactivity of the feed additive and chlorogenic acid, while maintaining the product's color and physical and chemical quality. The residue after ultrasonic countercurrent extraction undergoes physical grinding and separation in aqueous media. First, water is added at a solid-to-liquid ratio of 1:1-4 and the extract is coarsely ground to 100-400μm to break down the structure and initially release the target components. This is followed by fine grinding to 20-50μm while maintaining a slurry solids content of 8-15wt%, fully exposing and releasing the eucommia gum and fibers, optimizing subsequent separation. After adding a trace amount of sodium carboxymethyl cellulose, gradient sedimentation and stratification, followed by centrifugation, efficiently separate the eucommia rubber threads from the crude fibers, completely avoiding the use of toxic and flammable organic solvents. The subsequent refining process involves dissolving the threads with an alkaline aqueous solution, removing impurities through membrane filtration, decolorizing with hydrogen peroxide, acidification and precipitation, and vacuum drying. This ensures the safe and environmentally friendly production of high-quality eucommia rubber, completely eliminating the operational risks and environmental pollution associated with traditional organic solvent methods. Furthermore, the ultrasonic extraction process pre-treats the residue, significantly reducing water consumption during physical extraction and significantly lowering water recovery costs.

[0007] Preferably, the microwave power in S1 is 3-20 kW, the treatment time is 30-120 seconds, and the temperature is 40-80°C; the extraction conditions in S2 are: temperature 20-50°C, ultrasonic frequency 25-50 kHz, power density 50-150 W / L, and time 45-120 minutes. The extract is centrifuged at 3000-5000 rpm for 10-40 minutes for initial separation in a horizontal screw centrifuge, and the resulting filtrate is then centrifuged at 4000-12000 rpm for 5-40 minutes to obtain a filtrate and a residue.

[0008] Preferably, the reverse osmosis membrane operating pressure in S3 is 0.5-3.0 MPa, concentrated to 10-35% of the original volume, the low-temperature vacuum concentration conditions are 40-60°C, -0.10 to -0.08 MPa, concentrated to a specific gravity of 1.15-1.30, and the belt drying temperature is 40-65°C.

[0009] Preferably, the macroporous adsorption resin in S4 is AB-8, D101 or HPD400, the water washing flow rate is 1-3BV / h, the ethanol elution concentration is 65-75%, the flow rate is 0.5-3BV / h, and the eluate is concentrated and dried according to the conditions of S3; the resin is regenerated by soaking in 0.5-1mol / L NaOH solution for 1-3 hours.

[0010] Preferably, the protease in S5 is a neutral protease or an alkaline protease, the hydrolysis conditions are: pH 6.5-8.5, temperature 45-55°C, time 2-6 hours, enzyme addition amount 0.5-3wt%, neutral protease activity 50,000-150,000 U / g, alkaline protease activity 80,000-200,000 U / g; the ultrafiltration membrane is made of polyethersulfone, the transmembrane pressure difference is 0.2-0.6 MPa; the nanofiltration membrane operating pressure is 0.5-2.5 MPa.

[0011] Preferably, S6 specifically includes: adding water to the residue at a solid-liquid ratio of 1:1-4, coarsely grinding to a particle size of 100-400 μm, and finely grinding to 20-50 μm; adding 0.1-0.5 wt% sodium carboxymethyl cellulose to the slurry, standing at 15-25 ° C for 30-120 minutes to separate the layers; centrifuging the upper light phase at 2000-4000 rpm to obtain Eucommia ulmoides gum filaments, and centrifuging the lower heavy phase to obtain crude fibers; the solid content of the grinding slurry is 8-15 wt%.

[0012] Preferably, S7 comprises: dissolving the rubber thread in an alkaline aqueous solution of pH 9-11 at 60-80° C. for 1-3 hours, filtering through a 0.1-0.5 μm membrane, adding 0.5-1.5 wt % hydrogen peroxide for decolorization at 40-60° C. for 20-40 minutes, acid precipitation using hydrochloric acid or sulfuric acid to adjust the pH to 2.0-4.0, and vacuum drying to obtain eucommia rubber.

[0013] Preferably, S8 includes: treating the crude fiber with a 0.5-2 mol / L NaOH solution at 60-80° C. for 1-3 hours, rinsing, adding a combination of cellulase and xylanase for enzymatic hydrolysis, with an enzyme activity ratio of 1:1-3, a total addition amount of 0.5-2 wt%, enzymatic hydrolysis conditions of pH 4.5-5.5, a temperature of 50-60° C., and a time of 2-4 hours, and drying to obtain dietary fiber.

[0014] Preferably, the continuous countercurrent ultrasonic extractor is composed of 3-8 stages of tanks connected in series, the flow rate ratio of the feed liquid in adjacent tanks is 1:0.8-1.2, and the spacing between ultrasonic transducers is 20-50 cm.

[0015] Preferably, the belt dryer has the following operating parameters: a crawler speed of 0.5-2 m / min, a vacuum degree of -0.095 to -0.08 MPa, and a moisture content of the dried product of ≤5%.

[0016] The present invention provides a comprehensive extraction method for extracting Eucommia ulmoides feed additives, chlorogenic acid, Eucommia ulmoides rubber, and dietary fiber from Eucommia ulmoides. The method has the following beneficial effects: 1. The present invention adopts a continuous countercurrent ultrasonic extractor for low-temperature, high-efficiency ultrasonic-assisted extraction, which protects the activity of heat-sensitive components, greatly shortens the extraction time, and significantly reduces solvent usage and energy consumption; combined with reverse osmosis membrane concentration, low-temperature vacuum concentration and belt drying, it achieves the effect of completely retaining the eucommia feed additive and chlorogenic acid active substances, saving energy and labor throughout the process, and facilitating automated continuous operation.

[0017] 2. The present invention adopts pure water physical grinding and grading technology for the extraction residue, combined with sodium carboxymethyl cellulose to assist slurry stratification and centrifugal separation, thereby achieving the effect of efficiently separating Eucommia rubber filaments and crude fibers under organic solvent-free conditions; subsequently, through the alkaline dissolution-acidification precipitation refining process, the effect of safely and environmentally producing high-quality Eucommia rubber with water as the core medium is achieved, and the risk of flammability and explosion is completely avoided.

[0018] 3. The present invention synergistically integrates continuous countercurrent ultrasonic extraction, physical grinding and separation, bio-enzymatic hydrolysis and chemical treatment technologies to simultaneously extract five high-value components, namely feed additives, chlorogenic acid, protein oligopeptides, rubber and dietary fiber, from a single raw material of Eucommia ulmoides, thereby maximizing resource utilization. The recycling and reduction of solvents in each link and the cascade conversion and utilization of wastes achieve the effect of significantly reducing the overall production cost, eliminating the discharge of highly polluting waste liquid, and improving the overall economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 The present invention is a flow chart of the method for comprehensive extraction of Eucommia ulmoides feed additives, chlorogenic acid, Eucommia ulmoides rubber and dietary fiber from Eucommia ulmoides. DETAILED DESCRIPTION

[0020] The following will clearly and completely describe the technical solution of the present invention in conjunction with the accompanying drawings. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0021] Please see the attached Figure 1 The embodiment of the present invention provides a comprehensive extraction method for extracting Eucommia ulmoides feed additives, chlorogenic acid, Eucommia rubber, and dietary fiber from Eucommia ulmoides, comprising the following steps: S1. Raw material pretreatment: Eucommia ulmoides leaves, skins and seed shells are microwave-dried and then crushed through an 8-12 mesh sieve; S2. Continuous countercurrent ultrasonic extraction: The raw material and 5-10 times the amount of water are extracted in a continuous countercurrent ultrasonic extractor, and the extract is separated by a horizontal screw centrifuge and a butterfly centrifuge to obtain a filtrate and a residue; S3. Preparation of feed additive: The filtrate is concentrated by reverse osmosis membrane, concentrated under reduced pressure by low-temperature vacuum concentrator, and dried by belt dryer to obtain Eucommia ulmoides feed additive; S4, purification of chlorogenic acid: The filtrate from S3 was adsorbed on a macroporous adsorption resin column, washed with water to remove impurities, and then eluted with ethanol. The eluate was concentrated and dried to obtain chlorogenic acid from Eucommia ulmoides; S5. Preparation of protein oligopeptides: The resin column washing liquid is hydrolyzed with protease, separated by 3000D ultrafiltration membrane and nanofiltration membrane, and the retentate is concentrated and dried to obtain Eucommia protein oligopeptides; S6, physical separation of residue: The residue in S2 is coarsely ground with water to remove impurities and then finely ground. The slurry is separated into layers in a liquid-liquid separator and centrifuged to obtain eucommia gum filaments and crude fibers; S7, Eucommia rubber refining: dissolving Eucommia rubber threads in an alkaline aqueous solution, membrane filtering, decolorizing, acid precipitation, and drying to obtain Eucommia rubber; S8. Preparation of dietary fiber: Crude fiber is treated with alkali, hydrolyzed by enzymes, and dried to obtain dietary fiber.

[0022] Specifically, microwave drying is used in raw material pretreatment to quickly and evenly dry the raw materials, thereby avoiding the loss of active ingredients that may be caused by long-term high-temperature treatment; crushing through an 8-12 mesh sieve increases the contact area between the raw materials and the solvent, thereby improving the subsequent extraction efficiency; continuous countercurrent ultrasonic extraction is used in continuous countercurrent ultrasonic extraction to efficiently extract the effective ingredients in Eucommia ulmoides under mild conditions, thereby maximally retaining the active ingredients in the raw materials; separation by a horizontal screw centrifuge and a butterfly centrifuge quickly separates the extract from the residue, thereby laying the foundation for subsequent component separation and purification. ; In the preparation of feed additives, the extract is concentrated by reverse osmosis membrane concentration and low-temperature vacuum concentrator under reduced pressure, which greatly reduces the subsequent drying cost; the concentrated solution is dried into feed additives by belt dryer, and a new feed additive rich in active ingredients of Eucommia ulmoides is obtained; in the purification of chlorogenic acid, chlorogenic acid is efficiently separated by adsorption on a macroporous adsorption resin column, thereby improving the purity and yield of chlorogenic acid; chlorogenic acid is further purified by washing with water to remove impurities and then eluting with ethanol, thereby obtaining a high-purity chlorogenic acid product; Preparation of protein oligopeptides During the process, the macromolecular protein is converted into small molecular peptides through protease hydrolysis, thereby improving the bioavailability of the protein; the peptide segments of different molecular weights are accurately separated through 3000D ultrafiltration membrane separation and nanofiltration membrane separation, thereby obtaining Eucommia protein oligopeptides with specific biological activity; in the physical separation of the residue, the Eucommia gum silk and crude fiber in the residue are effectively separated by adding water for coarse grinding to remove impurities and then fine grinding, thereby realizing the high value utilization of the raw materials; the Eucommia gum silk and crude fiber are further purified through stratification and centrifugal separation by liquid-liquid separator, thereby obtaining high-purity Eucommia gum The invention relates to a novel natural rubber material comprising silk and crude fiber raw materials; in the refining of eucommia rubber, impurities and color in eucommia rubber silk are removed by dissolving in an alkaline aqueous solution, membrane filtration, decolorization and acid precipitation, thereby improving the purity and quality of eucommia rubber; the refined eucommia rubber is solidified and formed by drying, thereby obtaining a new type of natural rubber material; in the preparation of dietary fiber, non-fiber components in crude fiber are decomposed by alkali treatment and enzymatic hydrolysis, thereby improving the purity of dietary fiber; the enzymatically hydrolyzed dietary fiber is solidified and formed by drying, thereby obtaining a natural dietary fiber product with high added value.

[0023] Please see the attached Figure 1In S1, the microwave power is 3-20 kW, the processing time is 30-120 seconds, and the temperature is 40-80°C; the extraction conditions in S2 are: temperature 20-50°C, ultrasonic frequency 25-50 kHz, power density 50-150 W / L, and time 45-120 minutes. The extract is centrifuged at 3000-5000 rpm for 10-40 minutes in a horizontal screw centrifuge for initial separation, and the obtained filtrate is further centrifuged at 4000-12000 rpm in a butterfly centrifuge for 5-40 minutes to obtain a filtrate and residue.

[0024] Specifically, by setting the microwave power to 3-20kW, the raw material of Eucommia ulmoides can be heated quickly and evenly, thereby drying the raw material in a shorter time, avoiding the loss of active ingredients that may be caused by long-term high-temperature treatment; by controlling the treatment time to 30-120 seconds, the degree of drying can be accurately controlled, thereby ensuring the drying uniformity of the raw material and providing a suitable raw material state for subsequent crushing and extraction; by adjusting the temperature to 40-80℃, the raw material can be dried at a suitable temperature, thereby retaining the heat-sensitive components in the raw material, such as chlorogenic acid, to the maximum extent; by controlling the extraction temperature to 20-50℃, the raw material can be dried at a suitable temperature, thereby retaining the heat-sensitive components in the raw material, such as chlorogenic acid, to the maximum extent. The method extracts the active ingredients from Eucommia ulmoides under mild conditions, thereby retaining the active ingredients in the raw materials to the maximum extent, especially the heat-sensitive ingredients; by adjusting the ultrasonic frequency to 25-50 kHz, the solvent penetration is enhanced through the ultrasonic cavitation effect, thereby improving the extraction efficiency and extraction rate; by adjusting the power density to 50-150 W / L, the ultrasonic energy input is controlled, thereby optimizing the energy utilization efficiency during the extraction process and avoiding the loss of active ingredients due to excessive heating; by setting the extraction time to 45-120 minutes, the active ingredients in the raw materials are fully extracted, thereby ensuring the content of the target ingredients in the extract; by performing initial separation by centrifugation at 3000-5000 rpm for 10-40 minutes in a horizontal screw centrifuge, the extract is quickly separated from the solid residue, thereby laying the foundation for subsequent refining and purification steps; by performing separation by centrifugation at 4000-12000 rpm for 5-40 minutes in a butterfly centrifuge, the extract is further purified, thereby removing fine particles and impurities that may affect the subsequent purification steps.

[0025] Please see the attached Figure 1 The reverse osmosis membrane operating pressure in S3 is 0.5-3.0MPa, and the concentrate is reduced to 10-35% of the original volume. The low-temperature vacuum concentration conditions are 40-60℃, -0.10~-0.08MPa, and the specific gravity is 1.15-1.30. The belt drying temperature is 40-65℃.

[0026] Specifically, the reverse osmosis membrane operating pressure of 0.5-3.0MPa is used to perform preliminary concentration of the extract, thereby reducing the volume of subsequent processing while maintaining the stability of the active ingredients, thereby improving the concentration efficiency; the extract is concentrated to 10-35% of the original volume, which greatly reduces the water content, thereby creating conditions for the subsequent low-temperature vacuum concentration and drying steps; the low-temperature vacuum concentration conditions of 40-60°C and -0.10 to -0.08MPa are used to further concentrate the extract at a lower temperature, thereby maximally retaining the activity of heat-sensitive components while avoiding the quality degradation that may be caused by high-temperature concentration; the extract is concentrated to a specific gravity of 1.15-1.30 to accurately control the concentration of the concentrate, thereby ensuring the quality and effect of the feed additive; the belt drying temperature of 40-65°C is used to dry the concentrate at an appropriate temperature, thereby avoiding the loss of active ingredients that may be caused by high-temperature drying, while ensuring the drying uniformity and stability of the feed additive.

[0027] Please see the attached Figure 1 The macroporous adsorption resin in S4 is AB-8, D101 or HPD400, the water washing flow rate is 1-3BV / h, the ethanol elution concentration is 65-75%, the flow rate is 0.5-3BV / h, and the eluate concentration and drying are performed according to the S3 conditions; the resin is regenerated by soaking in 0.5-1mol / L NaOH solution for 1-3 hours.

[0028] Specifically, by using AB-8, D101 or HPD400 macroporous adsorption resins, the chlorogenic acid can be efficiently and selectively adsorbed. These resins have suitable pore sizes and chemical properties and can specifically adsorb polar compounds such as chlorogenic acid, thereby improving the extraction purity and yield of chlorogenic acid. By controlling the water washing flow rate at 1-3BV / h, the non-polar impurities on the resin can be removed. The appropriate flow rate can ensure that the water washing liquid fully flows through the resin, effectively removing impurities and avoiding the loss of chlorogenic acid. By eluting the concentrated chlorogenic acid with ethanol, the water washing liquid can be removed. The concentration is controlled at 65-75% and the flow rate is 0.5-3BV / h to selectively elute chlorogenic acid. Ethanol, as a good organic solvent, can effectively elute chlorogenic acid on the resin at a lower concentration while maintaining the stability of chlorogenic acid. The eluent is concentrated and dried according to the S3 conditions to separate chlorogenic acid from the eluent and dry it into shape. Through the concentration and drying steps in S3, high-purity chlorogenic acid powder can be obtained, which is convenient for subsequent application and storage. The resin is regenerated by soaking in 0.5-1mol / L NaOH solution for 1-3 hours to restore the adsorption performance of the resin. The NaOH solution can effectively remove residual organic matter and pigments on the resin. Through appropriate concentration and time, the regeneration effect of the resin can be ensured and the service life of the resin can be extended.

[0029] Please see the attached Figure 1 The protease in S5 is a neutral protease or an alkaline protease, the hydrolysis conditions are: pH 6.5-8.5, temperature 45-55°C, time 2-6 hours, enzyme addition amount 0.5-3wt%, neutral protease activity 50,000-150,000 U / g, alkaline protease activity 80,000-200,000 U / g; the ultrafiltration membrane is made of polyethersulfone, the transmembrane pressure difference is 0.2-0.6MPa; the nanofiltration membrane operating pressure is 0.5-2.5MPa.

[0030] Specifically, by selecting neutral protease or alkaline protease to catalyze protein hydrolysis under mild conditions, these enzymes have different pH adaptability, and the appropriate enzyme species can be selected according to the characteristics of the raw materials and the requirements of the target product, thereby improving the hydrolysis efficiency and product quality; by controlling the hydrolysis conditions pH 6.5-8.5, temperature 45-55 ° C, time 2-6 hours, the enzyme catalytic efficiency and protein hydrolysis degree are optimized. These conditions can ensure the activity and stability of the enzyme, while avoiding the loss of oligopeptides caused by excessive hydrolysis, ensuring the diversity and functionality of the hydrolyzed products; by controlling the enzyme addition amount at 0.5-3wt% It plays a role in precisely controlling the degree of hydrolysis and product composition. The appropriate amount of enzyme added can ensure sufficient hydrolysis of the protein while avoiding the cost increase caused by excessive enzyme addition. By setting the neutral protease activity to 50,000-150,000 U / g and the alkaline protease activity to 80,000-200,000 U / g, it plays a role in ensuring the enzyme catalytic efficiency and the quality of the hydrolyzed product. The appropriate enzyme activity can ensure the efficient hydrolysis of the protein while avoiding excessive hydrolysis and product loss caused by excessive enzyme activity. By using an ultrafiltration membrane made of polyethersulfone material, it plays a role in precisely separating peptides of different molecular weights at a transmembrane pressure difference of 0.2-0.6MPa. The polyethersulfone membrane has good chemical stability and mechanical strength and can withstand a high transmembrane pressure difference, while ensuring the separation effect and the service life of the membrane. The nanofiltration membrane operating pressure of 0.5-2.5MPa plays a role in further separating and purifying oligopeptides. The nanofiltration membrane can achieve efficient separation of oligopeptides at a lower operating pressure while avoiding membrane damage and increased energy consumption caused by excessive operating pressure.

[0031] Please see the attached Figure 1, S6 specifically includes: adding water to the residue at a solid-liquid ratio of 1:1-4, coarsely grinding to a particle size of 100-400μm, and finely grinding to 20-50μm; adding 0.1-0.5wt% sodium carboxymethyl cellulose to the slurry, standing at 15-25℃ for 30-120 minutes to separate the layers; centrifuging the upper light phase at 2000-4000rpm to obtain eucommia gum silk, and centrifuging the lower heavy phase to obtain crude fiber; the solid content of the grinding slurry is 8-15wt%; specifically, adding water to the residue at a solid-liquid ratio of 1:1-4 plays the role of adjusting the slurry concentration, thereby providing suitable operating conditions for subsequent grinding and separation steps; coarse grinding to a particle size of 100-400μm plays the role of preliminarily destroying the residue structure, thereby creating conditions for fine grinding and subsequent separation steps; fine grinding to 20-50μm plays the role of further refining the residue particle size, thereby improving the eucommia gum silk and crude fiber in the residue. Separation efficiency: 0.1-0.5wt% sodium carboxymethyl cellulose is added to the slurry to improve the fluidity and stability of the slurry. As a thickener, sodium carboxymethyl cellulose can increase the viscosity of the slurry and help the stratification process. The density difference is used to separate the eucommia gum filaments and crude fibers by standing at 15-25℃ for 30-120 minutes. The appropriate temperature and time can promote the natural stratification of the light phase and the heavy phase, thereby improving the separation effect. The eucommia gum filaments are obtained by centrifugal separation of the upper light phase at 2000-4000rpm, which further purifies the eucommia gum filaments. The appropriate centrifugal speed can effectively separate the eucommia gum filaments from the light phase. The crude fibers are obtained by centrifugal separation of the lower heavy phase, which extracts the crude fibers from the heavy phase. The appropriate centrifugal speed can effectively separate the crude fibers from the heavy phase. The solid content of the grinding slurry is controlled at 8-15wt% to ensure the appropriate operating concentration of the slurry. The appropriate solid content can ensure the smooth progress of the grinding and separation process, while avoiding the influence of excessively high or low solid content on the separation effect.

[0032] Please see the attached Figure 1 S7 comprises: dissolving the rubber thread in an alkaline aqueous solution of pH 9-11 at 60-80° C. for 1-3 hours, filtering through a 0.1-0.5 μm membrane, adding 0.5-1.5 wt % hydrogen peroxide at 40-60° C. for bleaching for 20-40 minutes, acid precipitation using hydrochloric acid or sulfuric acid to adjust the pH to 2.0-4.0, and vacuum drying to obtain eucommia rubber.

[0033] Specifically, the eucommia gum threads are fully dissolved by dissolving them in an alkaline aqueous solution at pH 9-11 at 60-80°C for 1-3 hours. Appropriate pH and temperature conditions can promote the dissolution of the gum threads, creating conditions for subsequent purification steps; impurities and particles in the dissolved gum solution are removed by 0.1-0.5 μm membrane filtration. Membrane filtration can effectively remove particles and insoluble matter in the gum solution, thereby improving the purity of the gum solution; pigments and The role of organic matter, hydrogen peroxide as an oxidant, can effectively remove pigments in the rubber solution under mild conditions, and improve the transparency and purity of the rubber solution; acid precipitation using hydrochloric acid or sulfuric acid to adjust the pH to 2.0-4.0 plays a role in re-solidifying the Eucommia rubber, and the appropriate acidity can promote the aggregation and precipitation of rubber molecules, and realize the separation of rubber and water phase; vacuum drying plays a role in removing moisture from the rubber and solidifying the rubber. Vacuum drying can achieve rubber drying at a lower temperature, avoiding rubber degradation and performance loss that may be caused by high-temperature drying.

[0034] Please see the attached Figure 1 S8 includes: treating crude fiber with 0.5-2 mol / L NaOH solution at 60-80°C for 1-3 hours, rinsing, adding cellulase and xylanase for enzymolysis, with an enzyme activity ratio of 1:1-3, a total addition amount of 0.5-2wt%, enzymatic hydrolysis conditions of pH 4.5-5.5, temperature 50-60°C, time 2-4 hours, and drying to obtain dietary fiber.

[0035] Specifically, the crude fiber is treated with a 0.5-2 mol / L NaOH solution at 60-80°C for 1-3 hours to pretreat the crude fiber. The high-temperature treatment under alkaline conditions can destroy the lignin and part of the hemicellulose in the crude fiber, improve the digestibility of the fiber, and create conditions for the subsequent enzymatic hydrolysis step; after rinsing, the combined enzymatic hydrolysis of cellulase and xylanase plays a synergistic role in decomposing cellulose and hemicellulose. Cellulase mainly decomposes cellulose, while xylanase mainly decomposes hemicellulose. The combined use of the two can more efficiently convert crude fiber into soluble dietary fiber; by controlling the enzyme activity ratio at 1:1-3 and the total addition amount at 0.5-2wt%, the crude fiber is converted into soluble dietary fiber. It plays a role in optimizing the enzymatic hydrolysis efficiency and product composition. The appropriate enzyme activity ratio and addition amount can ensure the sufficient enzymatic hydrolysis of crude fiber, while avoiding the cost increase caused by excessive enzyme addition. By controlling the enzymatic hydrolysis conditions of pH 4.5-5.5, temperature 50-60℃, and time 2-4 hours, it plays a role in optimizing the enzyme activity and enzymatic hydrolysis degree. These conditions can ensure the activity and stability of the enzyme, while avoiding the loss of dietary fiber caused by excessive enzymatic hydrolysis. The dietary fiber is dried to remove moisture from the enzymatic hydrolyzate and solidify the dietary fiber. The drying process can be achieved at a lower temperature, avoiding the degradation and performance loss of dietary fiber that may be caused by high-temperature drying.

[0036] Please see the attached Figure 1 The continuous countercurrent ultrasonic extractor consists of 3-8 stages of series tanks, the material-liquid flow rate ratio of adjacent tanks is 1:0.8-1.2, and the ultrasonic transducer spacing is 20-50cm.

[0037] Specifically, it consists of 3-8 levels of tanks connected in series, which can perform multi-stage continuous extraction. Each level of tank can further extract the material, thereby improving the extraction efficiency and extraction rate; the flow rate ratio of adjacent tanks is controlled at 1:0.8-1.2. This flow rate ratio can ensure the residence time of the material in each level of tank, so that the solvent and the material are fully in contact, thereby improving the extraction efficiency; the spacing between ultrasonic transducers is controlled at 20-50cm. This spacing can ensure that the ultrasonic wave is evenly distributed throughout the extraction process, improve the penetration and effect of the ultrasonic wave, promote the mixing of the solvent and the material, and accelerate the extraction process.

[0038] Please see the attached Figure 1 , belt dryer working parameters: crawler speed 0.5-2m / min, vacuum degree -0.095~-0.08MPa, moisture content of product after drying ≤5%.

[0039] Specifically, the crawler speed is controlled at 0.5-2m / min. This speed range ensures that the material has sufficient residence time on the drying belt to achieve uniform drying while maintaining high production efficiency. Slower crawler speeds are conducive to the full drying of the material, while faster speeds are suitable for drying thinner or partially dried materials. The vacuum degree is controlled at -0.095 to -0.08MPa. This vacuum environment can lower the boiling point of water, allowing the material to evaporate at a lower temperature. This is especially important for heat-sensitive materials, as it can reduce thermal damage and maintain the quality of the material. The moisture content of the dried product is controlled at ≤5%. This moisture content level ensures the drying effect of the material and meets the requirements of most industrial applications. Lower moisture content helps extend the storage life of the material and reduces the risk of microbial growth. The crawler design allows the material to be subjected to uniform heat and airflow during the drying process, thereby achieving uniform drying.

[0040] Example 1 1. Technical Solution S1. Raw material pretreatment: 500 kg of Eucommia ulmoides leaves were crushed and passed through a 12-mesh sieve at a microwave power of 20 kW and a treatment time of 120 seconds at a temperature of 80°C.

[0041] S2, continuous countercurrent ultrasonic extraction: The water volume was 10 times that of 5000 L, the temperature was 50°C, the ultrasonic frequency was 50 kHz, the power density was 150 W / L, and the extraction time was 120 min.

[0042] Centrifugation: decanter centrifuge at 5000 rpm for 40 minutes, butterfly centrifuge at 12000 rpm for 40 minutes.

[0043] S3. Preparation of feed additives: The reverse osmosis membrane operating pressure is 3.0 MPa, and the concentrate is concentrated to 10% of the original volume.

[0044] Low-temperature vacuum concentration conditions: 60°C, -0.08 MPa, concentrated to a specific gravity of 1.30.

[0045] The belt drying temperature is 65°C, the belt speed is 2m / min, and the vacuum degree is -0.08MPa.

[0046] S4. Purification of chlorogenic acid: HPD400 macroporous adsorption resin was used, and the water washing flow rate was 3 BV / h.

[0047] The ethanol elution concentration was 75%, the flow rate was 3 BV / h, and the eluate was concentrated and dried according to S3 conditions.

[0048] S5. Preparation of protein oligopeptides: Alkaline protease was used, and the hydrolysis conditions were: pH 8.5, temperature 55°C, time 6 hours, enzyme addition amount 3wt%, and enzyme activity 200,000 U / g.

[0049] The transmembrane pressure difference of ultrafiltration membrane is 0.6MPa, and the operating pressure of nanofiltration membrane is 2.5MPa.

[0050] S6. Physical separation of residue: The residue was added with water at a solid-liquid ratio of 1:4, coarsely ground to a particle size of 400 μm and finely ground to 50 μm.

[0051] 0.5 wt% sodium carboxymethyl cellulose was added to the slurry, and the slurry was allowed to stand at 25° C. for 120 minutes to separate the layers.

[0052] The upper light phase was centrifuged at 4000 rpm to obtain eucommia rubber filaments, and the lower heavy phase was centrifuged at 2000 rpm to obtain crude fibers.

[0053] S7, Eucommia rubber refining: The rubber filaments were dissolved in a pH 11 alkaline aqueous solution at 80°C for 3 hours, filtered through a 0.5 μm membrane, and decolorized by adding 1.5 wt% hydrogen peroxide at 60°C for 40 minutes.

[0054] The pH value of the product was adjusted to 4.0 by acid precipitation with sulfuric acid, and vacuum drying was performed to obtain eucommia rubber.

[0055] S8. Preparation of dietary fiber: The crude fiber was treated with 2 mol / L NaOH solution at 80 °C for 3 h, and after rinsing, a mixture of cellulase and xylanase was added with an enzyme activity ratio of 1:3 and a total addition amount of 2 wt%.

[0056] Enzymatic hydrolysis conditions: pH 5.5, temperature 60°C, time 4 hours, and dried to obtain dietary fiber.

[0057] 2. Technical Effects: 1. The high-value parameter combination significantly improved the extraction efficiency, with the yield of feed additives being 9.5%, the yield of chlorogenic acid being 1.5%, and the yield of protein oligopeptides being 2.5%.

[0058] 2. The yield of Eucommia rubber is 1.4%, and the yield of dietary fiber is 8.4%.

[0059] 3. The product has high purity, feed additive ash content ≤4.0%, chlorogenic acid purity ≥95%, and protein oligopeptide molecular weight distribution is uniform.

[0060] Example 2 1. Technical Solution S1. Raw material pretreatment: 500 kg of Eucommia bark was crushed and passed through a 10-mesh sieve at a microwave power of 12 kW, a treatment time of 75 seconds, and a temperature of 60°C.

[0061] S2, continuous countercurrent ultrasonic extraction: The water volume was 7.5 times, 3750 L, the temperature was 35 ° C, the ultrasonic frequency was 37.5 kHz, the power density was 100 W / L, and the extraction time was 82 minutes.

[0062] Centrifugation: decanter centrifuge at 4000 rpm for 25 minutes, butterfly centrifuge at 8000 rpm for 22 minutes.

[0063] S3. Preparation of feed additives: The reverse osmosis membrane operating pressure is 1.75 MPa, and the concentrate is concentrated to 22.5% of the original volume.

[0064] Low-temperature vacuum concentration conditions: 50°C, -0.09 MPa, concentrated to a specific gravity of 1.22.

[0065] The belt drying temperature is 52.5°C, the crawler speed is 1.25m / min, and the vacuum degree is -0.085MPa.

[0066] S4. Purification of chlorogenic acid: D101 macroporous adsorption resin was used, and the water washing flow rate was 2BV / h.

[0067] The ethanol elution concentration was 70%, the flow rate was 1.75 BV / h, and the eluate was concentrated and dried according to S3 conditions.

[0068] S5. Preparation of protein oligopeptides: Neutral protease was used, and the hydrolysis conditions were: pH 7.5, temperature 50°C, time 4 hours, enzyme addition amount 1.75wt%, and enzyme activity 100,000 U / g.

[0069] The transmembrane pressure difference of ultrafiltration membrane is 0.4MPa, and the operating pressure of nanofiltration membrane is 1.5MPa.

[0070] S6. Physical separation of residue: The residue was added with water at a solid-liquid ratio of 1:2.5, coarsely ground to a particle size of 250 μm and finely ground to 35 μm.

[0071] 0.3 wt% sodium carboxymethyl cellulose was added to the slurry, and the slurry was allowed to stand at 20° C. for 75 minutes to separate into layers.

[0072] The upper light phase was centrifuged at 3000 rpm to obtain eucommia rubber filaments, and the lower heavy phase was centrifuged at 2000 rpm to obtain crude fibers.

[0073] S7, Eucommia rubber refining: The rubber filaments were dissolved in a pH 10 alkaline aqueous solution at 70°C for 2 hours, filtered through a 0.3 μm membrane, and decolorized by adding 1.0 wt% hydrogen peroxide at 50°C for 30 minutes.

[0074] The pH value of the product was adjusted to 3.0 by acid precipitation with hydrochloric acid, and vacuum drying was performed to obtain eucommia rubber.

[0075] S8. Preparation of dietary fiber: The crude fiber was treated with 1.25 mol / L NaOH solution at 70°C for 2 hours, and after rinsing, a mixture of cellulase and xylanase was added with an enzyme activity ratio of 1:2 and a total addition amount of 1.25 wt%.

[0076] Enzymatic hydrolysis conditions: pH 5.0, temperature 55°C, time 3 hours, and dried to obtain dietary fiber.

[0077] 2. Technical Effects: 1. The median parameter combination achieved a balance between high efficiency and low energy consumption, with the feed additive yield being 7.0%, the chlorogenic acid yield being 1.2%, and the protein oligopeptide yield being 1.8%.

[0078] 2. The yield of Eucommia rubber is 0.9% and the yield of dietary fiber is 6.8%.

[0079] 3. The product quality is balanced, the ash content of feed additives is ≤4.5%, the purity of chlorogenic acid is ≥90%, and the molecular weight distribution of protein oligopeptides is reasonable.

[0080] Example 3 1. Technical Solution S1. Raw material pretreatment: 500 kg of Eucommia ulmoides seed shells were crushed and passed through an 8-mesh sieve at a microwave power of 3 kW and a treatment time of 30 seconds at a temperature of 40°C.

[0081] S2, continuous countercurrent ultrasonic extraction: The water volume was 5 times that of 2500 L, the temperature was 20°C, the ultrasonic frequency was 25 kHz, the power density was 50 W / L, and the extraction time was 45 min.

[0082] Centrifugation: decanter centrifuge at 3000 rpm for 10 minutes, butterfly centrifuge at 4000 rpm for 5 minutes.

[0083] S3. Preparation of feed additives: The reverse osmosis membrane operating pressure is 0.5 MPa, and the concentrate is concentrated to 35% of the original volume.

[0084] Low-temperature vacuum concentration conditions: 40°C, -0.10 MPa, concentrated to a specific gravity of 1.15.

[0085] The belt drying temperature is 40°C, the belt speed is 0.5m / min, and the vacuum degree is -0.095MPa.

[0086] S4. Purification of chlorogenic acid: AB-8 macroporous adsorption resin was used, and the water washing flow rate was 1 BV / h.

[0087] The ethanol elution concentration was 65%, the flow rate was 0.5 BV / h, and the eluate was concentrated and dried according to S3 conditions.

[0088] S5. Preparation of protein oligopeptides: Alkaline protease was used, and the hydrolysis conditions were: pH 6.5, temperature 45°C, time 2 hours, enzyme addition amount 0.5wt%, and enzyme activity 80,000 U / g.

[0089] The transmembrane pressure difference of ultrafiltration membrane is 0.2MPa, and the operating pressure of nanofiltration membrane is 0.5MPa.

[0090] S6. Physical separation of residue: The residue was added with water at a solid-liquid ratio of 1:1, coarsely ground to a particle size of 100 μm and finely ground to 20 μm.

[0091] 0.1 wt% sodium carboxymethyl cellulose was added to the slurry, and the slurry was allowed to stand at 15° C. for 30 minutes to separate the layers.

[0092] The upper light phase was centrifuged at 2000 rpm to obtain eucommia rubber filaments, and the lower heavy phase was centrifuged at 2000 rpm to obtain crude fibers.

[0093] S7, Eucommia rubber refining: The rubber filaments were dissolved in a pH 9 alkaline aqueous solution at 60°C for 1 hour, filtered through a 0.1 μm membrane, and decolorized by adding 0.5 wt% hydrogen peroxide at 40°C for 20 minutes.

[0094] The pH value of the product was adjusted to 2.0 by acid precipitation with hydrochloric acid, and vacuum drying was performed to obtain eucommia rubber.

[0095] S8. Preparation of dietary fiber: The crude fiber was treated with 0.5 mol / L NaOH solution at 60°C for 1 hour, and after rinsing, a mixture of cellulase and xylanase was added with an enzyme activity ratio of 1:1 and a total addition amount of 0.5 wt%.

[0096] Enzymatic hydrolysis conditions: pH 4.5, temperature 50°C, time 2 hours, and dried to obtain dietary fiber.

[0097] 2. Technical Effects: 1. The low-value parameter combination achieved efficient extraction at low energy consumption, with the yield of feed additives being 9.7%, the yield of chlorogenic acid being 0.9%, and the yield of protein oligopeptides being 1.2%.

[0098] 2. The yield of Eucommia rubber is 0.5%, and the yield of dietary fiber is 5.2%.

[0099] 3. The product has good stability, the ash content of feed additive is ≤5.0%, the purity of chlorogenic acid is ≥85%, and the molecular weight distribution of protein oligopeptides is uniform.

[0100] Comparative Example 1 1. Process steps S1. Raw material pretreatment: same as in Example 1.

[0101] S2. Hot reflux extraction: The raw material was refluxed with 10 times the amount of water at 80°C for 3 times, each time for 1.5 hours, and the extract was filtered on a plate and frame.

[0102] S3, concentration and drying: same as in Example 1.

[0103] S4. Purification of chlorogenic acid: The filtrate was extracted three times with ethyl acetate at a solvent ratio of 1:2, and the combined organic phases were concentrated.

[0104] S5. Not implemented.

[0105] S6-S8: The residue is directly discarded without rubber / fiber recovery.

[0106] 2. Parameter Optimization Basis Conventional heat reflow leads to the decomposition of heat-sensitive components, compared with ultrasonic low-temperature extraction; Organic solvent extraction increases safety risks, GB 31650-2019; Failure to utilize the residue violates the solid waste resource utilization requirements of HJ 1091-2020.

[0107] 3. Implementation Effect Verification

[0108] 4. Conclusion: The traditional process causes a 37% loss of active ingredients due to high temperature and the use of solvents, and reduces resource utilization by 100%, which does not meet the green manufacturing standards.

[0109] Comparative Example 2 1. Process steps The raw materials are concentrated, as in Example 2, steps S1-S3: processing of median parameters of Eucommia bark; Chlorogenic acid was purified as in Example 2, step S4: D101 resin, eluted with 70% ethanol; Residue treatment: Omit the S6 grinding and stratification step: the residue is directly treated with alkali, 1.25 mol / L NaOH, 70°C, 2h; omit the S7 acid precipitation purification: the alkali-treated product is directly dried to obtain the "composite fiber"; Protein recovery: The resin wash solution was directly concentrated and dried (without S5 enzymatic membrane separation).

[0110] 2. Parameter Optimization Basis Omission of physical delamination results in mixed rubber / fiber; No enzymatic treatment reduces the biological activity of the protein; The composite product does not meet the GB / T 5009.88-2014 dietary fiber standard.

[0111] 3. Implementation Effect Verification

[0112] 4. Conclusion: Although the simplified process reduces energy consumption by 20%, it leads to a 35% decrease in colloid purity, a 73% loss in functional components, and a 259% excess ash content in the product.

[0113] Comparative Example 3 1. Process steps S1. Raw material pretreatment: same as Example 3.

[0114] Conventional extraction: extraction with stirring at room temperature: 5 times the amount of water stirred at 25°C for 24 hours, instead of ultrasound; Centrifugal separation, parameters are the same as those in Example 3: 3000 / 4000 rpm; Feed additive, same as in Example 3, step S3: concentration and drying process; Separation of rubber filaments, same as in Example 3, steps S6-S7: grinding, stratification and refining process; Missing components: S4 chlorogenic acid purification and S5 peptide preparation were not performed.

[0115] 2. Parameter Optimization Basis Static extraction efficiency is low, and the ultrasonic cavitation effect increases mass transfer by 8-10 times; High value-added components have not been developed; The process time does not meet the plant extraction time requirements of T / CIFST 007-2022.

[0116] 3. Implementation Effect Verification

[0117] 4. Conclusion: The conventional process has low extraction efficiency, resulting in a 31-fold extension of the production cycle, a 70-fold increase in bacteria content, and a 53% loss in output value due to the failure to recover high-value components.

[0118] While embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions, and variations may be made to these embodiments without departing from the principles and spirit of the invention, and that the scope of the invention is defined by the appended claims and their equivalents.

Claims

1. A multi-component comprehensive extraction method of Eucommia ulmoides, characterized in that: The following steps are involved: S1. Raw material pretreatment: Eucommia ulmoides leaves, skins and seed shells are microwave-dried and then crushed through an 8-12 mesh sieve; S2. Continuous countercurrent ultrasonic extraction: The raw material and 5-10 times the amount of water are extracted in a continuous countercurrent ultrasonic extractor, and the extract is separated by a horizontal screw centrifuge and a butterfly centrifuge to obtain a filtrate and a residue; S3, preparation of feed additive: the filtrate is concentrated by reverse osmosis membrane, concentrated under reduced pressure by low-temperature vacuum concentrator, and dried by belt dryer to obtain Eucommia ulmoides feed additive; S4, purification of chlorogenic acid: The filtrate from S3 was adsorbed on a macroporous adsorption resin column, washed with water to remove impurities, and then eluted with ethanol. The eluate was concentrated and dried to obtain chlorogenic acid from Eucommia ulmoides; S5. Preparation of protein oligopeptides: The resin column washing liquid is hydrolyzed with protease, separated by 3000D ultrafiltration membrane and nanofiltration membrane, and the retentate is concentrated and dried to obtain Eucommia protein oligopeptides; S6, physical separation of residue: The residue in S2 is coarsely ground with water to remove impurities and then finely ground. The slurry is separated into layers in a liquid-liquid separator and centrifuged to obtain eucommia gum filaments and crude fibers; S7, refining eucommia rubber: dissolving the eucommia rubber thread in an alkaline aqueous solution, membrane filtering, decolorizing, acid precipitation, and drying to obtain eucommia rubber; S8. Preparation of dietary fiber: The crude fiber is subjected to alkali treatment, enzymatic hydrolysis, and drying to obtain dietary fiber.

2. The method for comprehensive extraction of Eucommia ulmoides from claim 1, wherein: In S1, the microwave power is 3-20 kW, the processing time is 30-120 seconds, and the temperature is 40-80°C; the extraction conditions in S2 are: temperature 20-50°C, ultrasonic frequency 25-50 kHz, power density 50-150 W / L, and time 45-120 minutes. The extract is centrifuged at 3000-5000 rpm for 10-40 minutes for initial separation in a horizontal screw centrifuge, and the obtained filtrate is further centrifuged at 4000-12000 rpm for 5-40 minutes to finally obtain a filtrate and a residue.

3. The multi-component comprehensive extraction method of Eucommia ulmoides according to claim 1, wherein: The reverse osmosis membrane operating pressure in S3 is 0.5-3.0MPa, and the volume is concentrated to 10-35% of the original volume. The low-temperature vacuum concentration conditions are 40-60℃, -0.10~-0.08MPa, and the specific gravity is concentrated to 1.15-1.

30. The belt drying temperature is 40-65℃.

4. The method for comprehensive extraction of Eucommia ulmoides from claim 1, wherein: The macroporous adsorption resin in S4 is AB-8, D101 or HPD400, the water washing flow rate is 1-3BV / h, the ethanol elution concentration is 65-75%, the flow rate is 0.5-3BV / h, and the eluate is concentrated and dried according to the S3 conditions; the resin is regenerated by soaking in 0.5-1mol / L NaOH solution for 1-3 hours.

5. The multi-component comprehensive extraction method of Eucommia ulmoides according to claim 1, wherein: The protease in S5 is a neutral protease or an alkaline protease, and the hydrolysis conditions are: pH 6.5-8.5, temperature 45-55°C, time 2-6 hours, enzyme addition amount 0.5-3wt%, neutral protease activity 50,000-150,000 U / g, and alkaline protease activity 80,000-200,000 U / g; the ultrafiltration membrane is made of polyethersulfone, with a transmembrane pressure difference of 0.2-0.6 MPa; the nanofiltration membrane operating pressure is 0.5-2.5 MPa.

6. The method for comprehensive extraction of multiple components from Eucommia ulmoides according to claim 1, wherein: S6 specifically includes: adding water to the residue at a solid-liquid ratio of 1:1-4, coarsely grinding to a particle size of 100-400μm, and finely grinding to 20-50μm; adding 0.1-0.5wt% sodium carboxymethyl cellulose to the slurry, and standing at 15-25°C for 30-120 minutes to separate the layers; centrifuging the upper light phase at 2000-4000rpm to obtain eucommia rubber filaments, and centrifuging the lower heavy phase to obtain crude fibers; the solid content of the ground slurry is 8-15wt%.

7. The method for comprehensive extraction of multiple components from Eucommia ulmoides according to claim 1, wherein: S7 includes: The rubber thread is dissolved in an alkaline aqueous solution of pH 9-11 at 60-80° C. for 1-3 hours, filtered through a 0.1-0.5 μm membrane, and decolorized by adding 0.5-1.5 wt% hydrogen peroxide at 40-60° C. for 20-40 minutes. The acid precipitation is carried out by adjusting the pH to 2.0-4.0 using hydrochloric acid or sulfuric acid, and vacuum drying is performed to obtain eucommia rubber.

8. The method for comprehensive extraction of multiple components from Eucommia ulmoides according to claim 1, wherein: The S8 includes: The crude fiber is treated with a 0.5-2 mol / L NaOH solution at 60-80° C. for 1-3 hours, rinsed, and then added with a combination of cellulase and xylanase for enzymolysis, with an enzyme activity ratio of 1:1-3, a total addition amount of 0.5-2 wt%, and enzymatic hydrolysis conditions of pH 4.5-5.5, a temperature of 50-60° C., and a time of 2-4 hours, and then dried to obtain dietary fiber.

9. The method for comprehensive extraction of multiple components from Eucommia ulmoides according to claim 2, wherein: The continuous countercurrent ultrasonic extractor is composed of 3-8 stages of series-connected tanks, the material-liquid flow rate ratio of adjacent tanks is 1:0.8-1.2, and the ultrasonic transducer spacing is 20-50 cm.

10. The method for comprehensive extraction of multiple components from Eucommia ulmoides according to claim 3, wherein: The belt dryer's operating parameters are: crawler speed 0.5-2m / min, vacuum degree -0.095~-0.08MPa, and moisture content of the dried product ≤5%.

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