Plant enzymolysis replacement decoction extraction method and extraction system thereof

Abstract

The invention discloses a plant enzymolysis replacement decoction extraction method and system, and the method comprises the following steps: putting a concentrate into an extraction tank, then adding an extracting solution containing xylanase to carry out enzymolysis on the concentrate, replacing the previous extracting solution after the enzymolysis is completed, then carrying out negative pressure decoction, replacing the previous liquid after the negative pressure decoction is completed, and carrying out enzymolysis on the concentrate after the negative pressure decoction is completed. Performing positive-pressure and negative-pressure decoction, and performing material-liquid separation after decoction is completed; according to the invention, the problems of mass reduction and extraction rate reduction of the extract caused by decomposition and loss of effective medicine components such as volatile substances under a high-temperature condition are avoided; according to the method, the steam consumption can be effectively reduced by more than 40% through replacement decoction and negative pressure decoction, and the water consumption is saved and the energy consumption is reduced by replacing decoction with clear water once; after secondary extraction, the coarse slurry is used for pulping, and the separated waste liquid is recycled, so that the wastewater discharge is effectively reduced, the sewage treatment cost is saved, and the environment is protected; the utilization rate of coarse slurry is improved; meanwhile, the equipment is simple to operate.

Description

Technical Field

[0001] The present invention relates to the technical field of plant extraction, and more particularly to a plant enzymatic hydrolysis, displacement, and decoction extraction method and an extraction system thereof. Background Art

[0002] Plants such as mulberry, bamboo, and paper mulberry have a wide range of uses. They are not only high-quality fiber raw materials, but also Chinese medicinal materials. After their internal components are extracted and used as raw materials in the fields of medicine or cosmetics, the remaining solid fibers can also be used in processes such as papermaking. Currently, traditional extraction processes mainly include: decoction method, reflux method, percolation method, etc. These methods use multiple extraction tanks for multiple intermittent extractions, which have the problems of large solvent consumption, low effective ingredient transfer rate, and many extraction times. They also greatly increase the processing time of subsequent processes, are not energy-saving, have low utilization rate of the extract, have low utilization value of residual materials, and are not environmentally friendly.

[0003] CN215538582U discloses a horizontal, straight-cylinder, outer-disc, half-tube extraction tank. This tank can be used for extracting plants such as mulberry, bamboo, and paper mulberry. It also uses multiple extraction tanks for multiple, intermittent extractions, but suffers from high solvent consumption, low extract utilization, low effective ingredient transfer rate, and a high number of extractions. 201911307366.2 discloses a method and application for producing bamboo pulp fiber and bamboo extract from bamboo. The bamboo extract is produced by steam-decoction of bamboo fibers. However, direct steam decoction results in high temperatures, which can easily decompose and lose the effective ingredients in the bamboo, reducing the useful ingredients in the extract. 201810095380.X discloses a method and application for separating bark and stem from mulberry branches. The branches undergo preparation and decoction, and the separated extract (waste) liquid—the decoction liquid—is directly concentrated in an evaporator. After concentration, it is dried in a dryer to produce a mulberry branch extract. However, this method suffers from high energy consumption and low extraction rates of medicinal ingredients due to the two water extraction steps. In particular, substances requiring low-temperature extraction are susceptible to decomposition and volatilization at high temperatures. Furthermore, substances requiring high-temperature extraction cannot achieve the desired effects of extracting active ingredients, softening fibers, and lignin at low temperatures. Producing pulp fiber from residual materials is costly and does not fully utilize the resource value of the raw materials. Summary of the Invention

[0004] The present invention overcomes the shortcomings of the prior art and provides a plant enzymatic hydrolysis replacement decoction extraction method and an implementation scheme of its extraction system, in the hope of solving the problems of low extraction efficiency, large water consumption, high energy consumption and environmental pollution in the prior art during plant extraction.

[0005] The present invention provides a plant enzymatic hydrolysis, displacement, decoction and extraction method, comprising the following steps:

[0006] (1) Material preparation: Cut and wash the raw materials to obtain the concentrate, and prepare the extraction solution in the No. 1 replacement liquid storage tank: add xylanase to the extraction solution at a weight ratio of absolute dry concentrate to xylanase of 1000:1-5;

[0007] (2) Enzymatic extraction: the concentrate obtained in step (1) is placed in an extraction tank, and then the extracted stock solution obtained in step (1) is pumped into the extraction tank, heated and enzymatically hydrolyzed, and the weight ratio of the absolute dry concentrate to the extracted stock solution is 1:5-15;

[0008] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank is pumped into the bottom of the extraction tank through the No. 1 liquid pump at a weight ratio of absolute dry concentrate to liquid of 1:4-12, and the liquid in the extraction tank is replaced into the decoction liquid storage tank through the No. 4 pipeline;

[0009] (3) Negative pressure decoction: After the replacement in step (2) is completed, the vacuum system is turned on to adjust the pressure in the extraction tank to -0.01 to -0.09 MPa for negative pressure decoction, and the decoction time is 0.5-2 hours;

[0010] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:3-10, and the prepared liquid is pumped into the bottom of the extraction tank through the No. 2 liquid pump. During the pumping process, the liquid in the extraction tank is replaced into the No. 1 replacement liquid storage tank through the No. 2 pipe, and is used as the liquid for preparing the extraction solution in step (1) (when the next tank is extracted);

[0011] (4) Decoction under positive and negative pressure conditions: After the replacement in step (3) is completed, the pressure of the extraction tank is increased to 0.1 to 0.27 MPa, and the pressure is maintained for positive pressure decoction, and the decoction time is 0.5-1 h; then the exhaust valve is opened to exhaust steam to the condenser (water in the fresh solvent storage tank is used as condenser cooling water to recover heat). When the exhaust is completed, the vacuum system is opened to make the pressure in the extraction tank -0.01 to -0.09 MPa and maintained, and negative pressure decoction is performed, and the decoction time is 0.5-1 h;

[0012] After the decoction is completed, the material and liquid are separated. When the material and liquid are separated, the liquid in the extraction tank is pumped into the No. 2 replacement liquid storage tank by the No. 1 liquid pump, and used as the solution for the extraction in step (3) (when the next tank is extracted). After the material and liquid separation is completed, the extraction tank is opened to take out the decoction material.

[0013] Furthermore, in step (1), acid is added to the preparation of the extraction solution to adjust the pH value of the extraction solution so that the pH value of the extraction solution is 4.5-6.5.

[0014] Furthermore, in step (2), the enzymatic hydrolysis temperature of the extraction tank is 40-60° C., and the enzymatic hydrolysis is carried out for 4.5-8 hours. During the enzymatic hydrolysis process in step (2), the extracted raw liquid is circulated once every hour by the No. 4 liquid pump until the enzymatic hydrolysis is completed.

[0015] Furthermore, the method further includes processing the decoction obtained in step (4), and the specific steps are as follows:

[0016] (5) Peeling the cooked material to separate the core material and the skin material;

[0017] (6) The core rod material obtained by separation in step (5) is sent to a tearing machine and a thread rolling machine for refinement treatment. The treated coarse material is sent to a desubmersible tank, and a clear liquid is added to adjust the coarse material concentration to 8-12% (the concentration here refers to the weight content of solid matter). At the same time, the desubmersible tank is heated to a temperature of 60-100°C in the desubmersible tank, and stirred continuously for 0.5-1h. After stirring, the vacuum system is turned on to make the pressure in the desubmersible tank -0.01 to -0.08MPa and maintain it for negative pressure desubmersible treatment, and the treatment time is 0.5-1h; after the treatment is completed, the material is pumped into the extruder with a slurry pump for material-liquid separation to obtain an extract and a coarse slurry;

[0018] (7) Prepare a mixed liquid by taking water in a weight ratio of 1:3.8-4.2 between the absolute dry coarse pulp and water, then add 5-20% potassium hydroxide, 0.5-2% sodium silicate, 0.2-1% magnesium sulfate, 2-6% hydrogen peroxide, and 0.1-0.5% ethylenediaminetetraacetic acid (EDTA) (all by weight) to the water and mix them evenly to form a mixed liquid; send the mixed liquid and the coarse pulp into a mixer and mix them evenly, and then send them into a twin-screw pulping machine for treatment: the fine pulp obtained after treatment is sent to a de-submersible tank for de-submersible treatment, the de-submersible pulp is pumped to a high-consistency pulping machine for treatment, and then enters a washing machine for washing, and finally a concentrator for dehydration treatment. The dehydrated pulp is sent to a dryer for drying, and after drying, pulp fiber is obtained. The black liquor produced during the twin-screw pulping process is sent to a dryer for drying, and after drying, a raw material for potash fertilizer is obtained.

[0019] The current pulping methods mainly include the sulfate method and the caustic soda method. These methods have the following problems: low pulping yield; poor pulp strength; difficulty in black liquor treatment and high industrial production costs. The present invention solves these problems in the pulping process because the alkali used in the pulping fiber process is potassium hydroxide, and the pulping black liquor contains rich potassium and can be used as a raw material for potassium fertilizer.

[0020] Furthermore, the method further comprises mixing the extract obtained in step (6) with the extract obtained in step (2), sending the mixture to a membrane separation device for separation treatment, and vacuum concentrating the separated concentrated liquid to obtain a finished product - an extract.

[0021] Furthermore: it also includes leather processing, specifically as follows: the leather obtained in step (5) is sent to a tree bast separation device to separate the surface bark and bast, the separated bast is sent to a dryer for drying, and after drying, it is sent to an opener and a carding machine for processing to obtain a finished product - a bast fiber product, and the separated surface bark is sent to a dryer for drying to obtain a finished product - a surface bark product.

[0022] Further: the pH value of the clear solution in step (6) is adjusted by alkali to a pH value of 7.5-9.5.

[0023] Furthermore: the xylanase in step (1) is food grade xylanase.

[0024] The boiling temperature of the extraction tank is provided by steam. A steam valve is set on the spiral heating coil to control the steam supply and disconnection. The extraction tank is equipped with an exhaust valve for exhausting and extracting steam. The exhaust and extraction pipes are connected to the vacuum system.

[0025] During the enzymatic hydrolysis, displacement, and decoction extraction process, the plant material needs to be converted to an absolute dry concentrate to facilitate accurate calculation of the raw material dosage. This can be achieved by drying the plant material sample in a dryer until the weight remains constant, calculating the weight loss rate to obtain the moisture content of the plant material sample, and then calculating the absolute dry weight after removing the water from the plant material. Other methods can also be used to convert the plant material to an absolute dry concentrate.

[0026] The "replacement" referred to in the present invention means that a container such as a tank is originally filled with raw materials and liquid, and then new liquid is pumped into the container from the bottom, so that the liquid components and liquid contained in the original raw materials in the tank are forced to be discharged from the top of the tank. By pumping in the new liquid, a considerable volume of the original liquid is forced to be discharged out of the tank.

[0027] The "clear liquid" referred to in the present invention refers to the extract obtained after the plant raw material is extracted. The extract is subjected to membrane separation, and the concentrated substance obtained is used to make the extract. The large amount of liquid obtained is recycled as the "clear liquid" in the process.

[0028] The present invention also provides a plant branch enzymatic hydrolysis, replacement, and decoction extraction system, comprising an extraction tank, a No. 1 replacement liquid storage tank, a No. 2 replacement liquid storage tank, a fresh solvent liquid storage tank, and a decoction liquid tank; the bottoms of the No. 1 replacement liquid storage tank and the No. 2 replacement liquid storage tank are both connected to the bottom of the extraction tank through a No. 1 pipe, a No. 1 liquid pump is provided on the No. 1 pipe, the top of the extraction tank is connected to the top of the No. 1 replacement liquid storage tank through a No. 2 pipe, the bottom of the fresh solvent liquid storage tank is connected to the bottom of the extraction tank through a No. 3 pipe, a No. 2 liquid pump is also provided on the No. 3 pipe, the top of the decoction liquid tank is connected to the top of the extraction tank through a No. 4 pipe, the bottom of the extraction tank is connected to the top of the No. 2 replacement liquid storage tank through a No. 6 pipe, a No. 4 liquid pump is also provided on the No. 6 pipe, and a valve is provided on each pipe.

[0029] The outside of the extraction tank body is wrapped with a spiral heating coil, which contains a heating medium (steam). The extraction tank is heated by circulating heating through the spiral heating coil (the pressure in the closed extraction tank will rise during the heating process); the No. 1 displacement liquid storage tank and the No. 2 displacement liquid storage tank both have an insulation layer so that the displaced liquid can be kept warm. When the displaced liquid is used for the next tank of plant branch enzymatic hydrolysis, displacement, and decoction extraction, the extraction tank can use the heat energy retained by the displaced liquid, thereby reducing the amount of steam used. In the low-temperature enzymatic hydrolysis extraction process of the present invention, the liquid in the No. 1 displacement liquid storage tank is used, and the liquid temperature is maintained at around 60°C, which meets the temperature required for enzymatic hydrolysis. When extracting under negative pressure conditions, the liquid in the No. 2 displacement liquid storage tank is used, and the liquid temperature is around 70°C. Only a small amount of steam heating is required to heat and maintain the temperature. The clean water in the fresh solvent tank used for subsequent positive and negative pressure extractions is first used as cooling water for the condenser. After absorbing heat, the cooling water temperature is increased and then enters the fresh solvent tank for standby use. Since the clean water in the fresh solvent tank is hotter than water at room temperature, the amount of steam used for decoction heating is reduced. The decoction process of the prior art uses room temperature clean water for two extractions, both of which are heated to a certain temperature by steam. However, in the present invention, only one of the three extractions in each tank is used for extraction, and the clean water temperature is higher than room temperature. The other two extractions use a displacement fluid at a certain temperature.

[0030] The purpose of negative pressure decoction: the extraction tank is connected to the condenser, the condenser is connected to the vacuum pump, and the vacuum system is turned on for vacuum treatment to form a low-temperature negative pressure decoction environment in the extraction tank, thereby reducing the boiling point of the liquid. The volatile substances are cooled by the condenser and turned into liquid and flow into the condenser collection box for recycling and reuse. At the same time, cavitation bubbles are generated in the extraction tank to obtain cavitation effect and vibration, which breaks the cell wall of the raw material and accelerates the release of effective ingredients and intracellular substances.

[0031] Compared with the prior art, the present invention has at least the following beneficial effects:

[0032] 1. The present invention can extract different components of plants under different temperature, acid and alkaline conditions, with high extraction rate and better quality. The same set of process methods solves the problem of extracting different components contained in the same plant raw material, achieving the purpose of both extracting medicinal materials and producing pulp fiber. By performing a primary enzymatic extraction under low temperature and acidic conditions and a secondary extraction under alkaline conditions, the water-soluble medicinal components are dissolved first, avoiding the decomposition and loss of effective medicinal components such as volatile substances under high temperature conditions, which leads to reduced extract quality and extraction rate.

[0033] 2. This invention reduces energy consumption through displacement decoction and negative pressure decoction, effectively reducing heat energy usage by over 40%. By using clean water for displacement decoction and membrane separation, and recycling cooling water and separated waste liquid, it saves over 70% of water, effectively reducing wastewater discharge, saving sewage treatment costs, lowering production costs, and protecting the environment.

[0034] 3. This process can be used to process the cooking material to produce pulp, bast fiber, surface leather and other products, further improving the utilization rate of the cooking material. At the same time, the equipment is simple and easy to operate, which is conducive to large-scale industrial production.

[0035] 4. The pulping black liquor of the present invention contains plant nutrient elements such as potassium and plant growth regulators such as lignin, which can be used as high-quality fertilizer raw materials, thereby achieving "zero discharge" of pulping black liquor and turning waste into treasure.

[0036] 5. The present invention adopts cross-industry development and utilization and fully utilizes and transforms waste resources. The utilization rate, conversion rate and output rate of raw materials are high, and it realizes the full utilization of agricultural waste - mulberry branches, mulberry branches, bamboo and other plant branches, improves the ecological environment, and helps achieve the "carbon neutrality" goal, which is of great significance.

[0037] 6. The present invention can realize the integrated modern resource high-value comprehensive utilization green ecological industry of "agriculture (mulberry leaves for silkworm farming, pulping waste liquid as fertilizer), forestry (mulberry branches replacing wood, reducing deforestation and improving the environment), paper (mulberry branch bast fiber, core fiber pulping and papermaking), and medicine (mulberry branch extract as medicinal material)", bringing significant economic, social and environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 Schematic diagram of the extraction system of the present invention;

[0039] Figure 2 This is a cross-sectional view of the extraction tank of the present invention;

[0040] Figure 3 It is a schematic cross-sectional view of the cage of the present invention;

[0041] Figure 4 This is a schematic cross-sectional view of the extraction tank of the present invention;

[0042] Figure 5 A photo of the layout of the extraction tanks in the plant of the present invention;

[0043] Figure 6 This is a photo of the extract packed in barrels.

[0044] The serial numbers in the figure are as follows: 1. Extraction tank; 2. No. 1 replacement liquid storage tank; 3. No. 2 replacement liquid storage tank; 4. Fresh solvent storage tank; 5. Decoction liquid storage tank; 6. No. 1 pipeline; 7. No. 1 liquid pump; 8. No. 2 pipeline; 9. No. 3 pipeline; 10. No. 2 liquid pump; 11. No. 4 pipeline; 12. No. 5 pipeline; 13. No. 3 liquid pump; 14. Internal liquid circulation pipeline; 15. No. 4 liquid pump; 16. Spare pipeline; 17. Cage; 18. Tank cover; 19. Spiral heating coil; 20. Condensate outlet; 21. Pressure gauge; 22. Slide rail; 23. Pulley groove; 24. Traction device; 25. Safety valve; 26. No. 6 pipeline; 27. Extraction tank interface. DETAILED DESCRIPTION

[0045] In order to make the purpose, technical solutions and advantages of the present invention more clear, the present invention is further described in detail below with reference to the embodiments.

[0046] Example 1

[0047] The method for extracting mulberry branches by enzymatic hydrolysis, replacement and decoction comprises the following steps:

[0048] 1. Material preparation: Cut the mulberry branches into short stalks of 80-100mm in length and send them to a washing machine for washing to remove dust and dirt on the surface of the raw materials that may affect the quality of the extract, thereby obtaining the raw branch concentrate (hereinafter referred to as concentrate);

[0049] The concentrate was converted into 200 kg of absolute dry concentrate, and the extraction stock solution was prepared in the No. 1 replacement liquid storage tank 2: the absolute dry concentrate and the extraction stock solution were prepared in a weight ratio of 1:7, hydrochloric acid was added to the extraction stock solution, the pH value of the extraction stock solution was adjusted to 4.5, and then 0.8 kg of food-grade xylanase was added to obtain the extraction stock solution.

[0050] 2. Enzymatic extraction: The concentrate obtained in step 1 is placed in the extraction tank 1; the extracted stock solution obtained in step 1 is then mixed evenly and pumped into the extraction tank 1 by the No. 1 liquid pump 7. The concentrate is subjected to low-temperature enzymatic hydrolysis of the extract stock solution at a temperature of 45°C and an enzymatic hydrolysis time of 5 hours. During the enzymatic hydrolysis process, the extracted stock solution is circulated once every 1 hour by the No. 4 liquid pump 15;

[0051] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared according to the weight ratio of absolute dry concentrate to liquid of 1:6, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced into the decoction liquid storage tank 5 through the No. 4 pipeline 11. The extract in the decoction liquid storage tank 5 is allowed to stand, and then the supernatant is filtered to obtain 1200 kg of extract A, which is sent to the next process for standby.

[0052] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure inside the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure inside the extraction tank 1 rises to -0.06MPa, maintain the current pressure for decoction. The decoction time is 1 hour.

[0053] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:5, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8, and used as the liquid for preparing the extraction stock solution in step 1 of the next tank.

[0054] IV. Decoction under Positive and Negative Pressure: After the replacement in step 3 is completed, the pressure in extraction tank 1 is raised to 0.25 MPa and maintained for positive pressure decoction for 0.6 hours. The exhaust valve is then opened to exhaust steam to the condenser. When the exhaust is complete, the vacuum system is activated to reduce the pressure in extraction tank 1 to -0.06 MPa and maintain this pressure for negative pressure decoction for 0.7 hours. After decoction, the liquid in extraction tank 1 is separated: the liquid in extraction tank 1 is pumped into displacement tank 3 (No. 2) via liquid pump 7 to serve as the prepared solution for the next extraction in step 3. After the separation is complete, extraction tank 1 is opened and 382 kg of decoction material (49% moisture content) is removed.

[0055] 5. Peeling of cooking material: The cooking material is sent to the peeling machine for peeling, and 288kg of core rod material and 94kg of skin material are obtained, with a skin and core rod separation rate of 98.4%.

[0056] 6. Secondary extraction: The core rod material separated in step 5 is sent to a tearing machine and a thread rolling machine for refinement treatment. The treated coarse material is sent to a de-submersible tank, and then clear liquid is added. The clear liquid is adjusted to a pH value of 9 with food-grade alkali. The clear liquid is added to the de-submersible tank to slurry the coarse material, and the slurry concentration is adjusted to 8%. The de-submersible tank is then heated to a tank temperature of 80°C and stirred for 0.7h. The vacuum system is then turned on to make the pressure in the de-submersible tank -0.06MPa and maintained for negative pressure de-submersible treatment for 0.5h. After the treatment is completed, the slurry is pumped into an extruder with a slurry pump for material-liquid separation, and 1336kg of extract B and 495kg of coarse slurry (water content 71%) are separated.

[0057] 7. Pulping: The coarse pulp separated in step 6 is converted into an absolute dry material, and water is taken according to the material:liquid weight ratio of 1:3.9. 10% potassium hydroxide, 1.5% sodium silicate, 0.8% magnesium sulfate, 5% hydrogen peroxide, and 0.3% ethylenediaminetetraacetic acid are added to the water and mixed evenly, all calculated by weight to form a mixed liquid. The mixed liquid and the coarse pulp are sent to a mixer for mixing, and then sent to a twin-screw pulping machine for processing to obtain fine pulp and black liquor;

[0058] De-latency treatment of fine pulp: send the fine pulp into the de-latency tank, add water to adjust the pulp concentration to 8%, raise the temperature to 80℃, and de-latency treatment time is 0.7h. The pulp after de-latency treatment is pumped to the high-consistency refiner for treatment with a pulp pump, and then enters the washing machine for washing and the concentrator for dehydration. The dehydrated pulp is sent to the dryer. After drying, the finished product is obtained - 126.5kg of mulberry branch pulp, and the pulp yield is 88.1%.

[0059] 62kg of black liquor produced by the twin-screw pulping machine is sent to the dryer. After drying, the residue is the finished product - 16kg of potash fertilizer raw material.

[0060] 8. Preparation of mulberry branch extract: 1336 kg of extract B separated in step 6 was pumped into an extract tank and mixed with 1200 kg of extract A extracted in step 2. The mixture was then pumped to a membrane separation device for separation. The separated concentrated liquid was vacuum concentrated to obtain the finished product - 17.5 kg of mulberry branch extract (concentration 48.5%). The separated clear liquid was reused.

[0061] IX. Hide Processing: The hide separated in step 5 is conveyed to a bast separation device for separation of the surface bark and bast. The separation rate of surface bark and bast is 97.5%. The separated bast is sent to a dryer for drying. After drying, it is sent to an opener and carding machine to produce a finished product - 25 kg of bast fiber product. The separated surface bark is sent to a dryer for drying to produce a finished product - 22.9 kg of surface bark product.

[0062] Example 2

[0063] Another embodiment of the method for extracting mulberry branches by enzymatic hydrolysis, displacement and decoction comprises the following steps:

[0064] 1. Material preparation: Prepare concentrate according to the method of Example 1;

[0065] Preparation of extraction stock solution: convert the concentrate into 200 kg of absolute dry concentrate, and prepare the extraction stock solution in the No. 1 replacement liquid storage tank 2: prepare it according to the weight ratio of absolute dry concentrate and extraction stock solution of 1:8, then add hydrochloric acid to the extraction stock solution, adjust the pH value of the extraction stock solution to 5, and then add 0.6 kg of xylanase to obtain the extraction stock solution.

[0066] 2. Enzymatic extraction: The concentrate obtained in step 1 is placed in the extraction tank 1, and then the extract obtained in step 1 is mixed evenly and pumped into the extraction tank 1 by the No. 1 liquid pump 7 to perform low-temperature enzymolysis on the concentrate. The enzymatic hydrolysis temperature is 50°C and the enzymatic hydrolysis time is 5.5h. During the enzymatic hydrolysis process, the extract is circulated once every 1h by the No. 4 liquid pump 15;

[0067] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared into a liquid according to the weight ratio of absolute dry concentrate to liquid of 1:7, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced into the decoction liquid storage tank 5 through the No. 4 pipeline 11. The extract in the decoction liquid storage tank 5 is allowed to stand, and the supernatant is filtered. The liquid constitutes 1400 kg of extract A, and the extract A is sent to the next process for standby.

[0068] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure in the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure in the extraction tank 1 rises to -0.05MPa, maintain the current pressure for decoction. The decoction time is 1.5h.

[0069] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:6, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced by positive pressure through the No. 2 pipeline 8 into the No. 1 replacement liquid storage tank 2. This liquid is used as the liquid for preparing the extraction stock solution in the next tank in step 1.

[0070] IV. Decoction under positive and negative pressure conditions: After the replacement in step 3 is completed, the pressure in extraction tank 1 is raised to 0.21 MPa and maintained for positive pressure decoction for 0.7 hours. The exhaust valve is then opened to exhaust steam to the condenser. When the exhaust is complete, the vacuum system is activated to reduce the pressure in extraction tank 1 to -0.05 MPa and maintain this pressure for negative pressure decoction for 0.6 hours. After decoction, the liquid in extraction tank 1 is separated: the liquid in extraction tank 1 is pumped into displacement liquid storage tank 3 (No. 2) via liquid pump 7 to serve as the prepared solution for extraction in step 3. After the separation is complete, the extraction tank is opened and 385 g of decoction material (moisture content 49.6%) is removed.

[0071] 5. Peeling of the cooking material: After the separation of the material and liquid is completed, the cooking material is sent to the peeling machine for peeling, and 290kg of core rod material and 95kg of skin material are obtained, and the skin and core rod separation rate is 98.5%.

[0072] 6. Secondary extraction: The core rod material separated in step 5 is sent to a tearing machine and a thread rolling machine for refinement treatment. The treated coarse material is sent to a de-submersible tank, and then clear liquid is added. The clear liquid is first adjusted to a pH value of 8.5 by food-grade alkali. The clear liquid is added to the de-submersible tank to slurry the coarse material, and the slurry concentration is adjusted to 9%. Then, the temperature is raised to 70°C in the de-submersible tank, stirred for 0.8h, and the vacuum system is turned on to make the pressure in the de-submersible tank -0.07MPa and maintained for negative pressure de-submersible treatment. The treatment time is 0.6h. After the treatment is completed, the material is pumped into the extruder with a slurry pump for material-liquid separation, and 1143kg of extract B and 477kg of coarse slurry (water content 70%) are separated.

[0073] 7. Pulping: The coarse pulp separated in step 6 is converted into an absolute dry material, water is taken at a material-liquid weight ratio of 1:4, 14% potassium hydroxide, 1.2% sodium silicate, 0.6% magnesium sulfate, 4% hydrogen peroxide, and 0.2% ethylenediaminetetraacetic acid are added to the water and mixed evenly to form a mixed liquid, the mixed liquid and the coarse pulp are sent to a mixer for mixing, and then sent to a twin-screw pulping machine for processing to obtain fine pulp and black liquor.

[0074] De-latching treatment of fine pulp: send the fine pulp into the de-latching tank, add water to adjust the concentration to 9%, raise the temperature to 70℃, and de-latching treatment time is 0.8h. The pulp after de-latching treatment is pumped to the high-consistency refiner with a pulp pump, and then enters the washing machine for washing and the concentrator for dehydration. The dehydrated pulp is sent to the dryer. After drying, the finished product is obtained - 122kg mulberry branch pulp, with a pulp yield of 85.3%.

[0075] 76 kg of black liquor produced during the processing of the twin-screw pulping machine is sent to the dryer. After drying, the residue is the finished product - 19 kg of potash fertilizer raw material.

[0076] 8. Preparation of mulberry branch extract: 1143 kg of extract B separated in step 6 was pumped into an extract tank and mixed with 1400 kg of extract A extracted in step 2. The mixture was pumped to a membrane separation device for separation. The separated concentrated liquid was vacuum concentrated to obtain 19 kg of mulberry branch extract (concentration 48%). The separated clear liquid was reused.

[0077] IX. Hide Processing: The hide separated in step 5 was conveyed to a bast separation device for separation of the surface bark and bast. The separation rate of surface bark and bast was 98%. The separated bast was sent to a dryer for drying. After drying, it was sent to an opener and carding machine to produce a finished product - 24.9 kg of bast fiber product. The separated surface bark was sent to a dryer for drying to produce a finished product - 23 kg of surface bark product.

[0078] Example 3

[0079] The enzymatic hydrolysis, replacement, and decoction extraction method of paper mulberry branches comprises the following steps:

[0080] 1. Material preparation: Prepare concentrate according to the method of Example 1;

[0081] Preparation of extraction stock solution: convert the obtained concentrate into 200 kg of absolute dry concentrate, and prepare the extraction stock solution in the No. 1 replacement liquid storage tank 2: prepare it according to the weight ratio of absolute dry concentrate and extraction stock solution of 1:6, add hydrochloric acid to the extraction stock solution, adjust the pH value of the extraction stock solution to 6, add 0.4 kg of xylanase, and obtain the extraction stock solution.

[0082] 2. Enzymatic extraction: The concentrate obtained in step 1 is placed in the extraction tank 1. The extract obtained in step 1 is mixed evenly and then pumped into the extraction tank 1 by the No. 1 liquid pump 7 to perform low-temperature enzymolysis on the concentrate. The enzymatic hydrolysis temperature is 55°C and the enzymatic hydrolysis time is 6 hours. During the enzymatic hydrolysis process, the extract is circulated once every 1 hour by the No. 4 liquid pump 15.

[0083] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared according to the weight ratio of absolute dry concentrate to liquid of 1:5, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced into the decoction liquid storage tank 5 through the No. 4 pipeline 11. The extract in the decoction liquid storage tank 5 is allowed to stand, and the supernatant is filtered. The liquid constitutes 1000 kg of extract A, and the extract A is sent to the next process for standby.

[0084] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure in the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure in the extraction tank 1 rises to -0.05MPa, maintain the current pressure for decoction. The decoction time is 1h.

[0085] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:4, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8. This liquid is used as the liquid for preparing the extraction stock solution in the next step one.

[0086] 4. Decoction under positive and negative pressure conditions: After the replacement in step 3 is completed, the pressure of the extraction tank 1 is increased to 0.22 MPa, and the pressure is maintained for positive pressure decoction, and the decoction time is 0.7 h; then the exhaust valve is opened to exhaust steam to the condenser. When the exhaust is completed, the vacuum system is opened to reduce the pressure in the extraction tank 1 to -0.06 MPa and maintain it for negative pressure decoction, and the decoction time is 0.8 h; after the decoction is completed, the material-liquid separation is carried out: the liquid in the extraction tank 1 is pumped into the No. 2 replacement liquid storage tank 3 by the No. 1 liquid pump 7, as the prepared solution for the next extraction in step 3; after the material-liquid separation is completed, the extraction tank 1 is opened to take out 378 kg of decoction material (the moisture content of the decoction material is 48.5%).

[0087] 5. Peeling of cooking material: The cooking material is sent to the peeling machine for peeling, and 284 kg of core rod material and 94 kg of skin material are obtained, and the separation rate of skin and core rod is 99%.

[0088] 6. Secondary extraction: the core rod material separated in step 5 is sent to a tearing machine and a thread rolling machine for refinement treatment, and the coarse material after treatment is sent to a de-submersible tank, and then a clear liquid is added, and the pH value of the clear liquid is adjusted to 8 with food-grade alkali, and the clear liquid is added to the de-submersible tank to adjust the coarse material to a slurry, and the slurry concentration is adjusted to 10%. The temperature is heated to 85°C in the de-submersible tank and stirred for 0.6h. The vacuum system is then turned on to make the pressure in the de-submersible tank -0.05MPa and maintained for negative pressure de-submersible treatment, and the treatment time is 0.7h. After the treatment is completed, the material is pumped into the extruder with a slurry pump for material-liquid separation, and 1002kg of extract is separated, and 458kg of coarse slurry is separated (water content 69%).

[0089] 7. Pulping: The coarse pulp separated in step 6 is converted into absolute dryness, water is taken at a material-liquid weight ratio of 1:4.1, 16% potassium hydroxide, 1% sodium silicate, 0.4% magnesium sulfate, 3% hydrogen peroxide, and 0.1% ethylenediaminetetraacetic acid are added to the water and mixed evenly to form a mixed liquid, the mixed liquid and the coarse pulp are sent to a mixer for mixing, and then sent to a twin-screw pulping machine for processing to obtain fine pulp and black liquor.

[0090] De-latching treatment of fine pulp: send the fine pulp into the de-latching tank, add water to adjust the concentration to 10%, raise the temperature to 80℃, and de-latching for 0.8h. The pulp after de-latching is pumped to the high-consistency refiner with a slurry pump, and then enters the washing machine for washing and the concentrator for dehydration. The dehydrated pulp is sent to the dryer. After drying, the finished product is obtained - 120kg of mulberry tree core fiber pulp, with a pulp yield of 84.5%.

[0091] 85kg of black liquor produced by the twin-screw pulping machine is sent to the dryer. After drying, the residue is the finished product - 20kg of potash fertilizer raw material.

[0092] 8. Extract Preparation: 1002 kg of the extract B separated in step 6 was pumped into an extract tank and mixed with 1000 kg of the extract A extracted in step 2. The mixture was then pumped to a membrane separation device for separation. The separated concentrated liquid was vacuum concentrated to obtain 21 kg of paper mulberry branch extract (concentration 44%). The separated clear liquid was reused.

[0093] IX. Hide Processing: The hide separated in step 5 is conveyed to a bast separation device via a conveyor to separate the surface bark from the bast. The separation rate of surface bark and bast is 98.5%. The separated bast is sent to a dryer for drying. After drying, it is sent to an opener and carding machine to produce a finished product - 25 kg of bast fiber product. The separated surface bark is sent to a dryer for drying to produce a finished product - 23.4 kg of surface bark product.

[0094] Example 4

[0095] Another embodiment of the method for extracting paper mulberry branches by enzymatic hydrolysis, displacement and decoction comprises the following steps:

[0096] 1. Material preparation: Prepare concentrate according to the method of Example 1;

[0097] Preparation of extraction stock solution: convert the above-obtained concentrate into 200 kg of absolute dry concentrate, and prepare the extraction stock solution in the No. 1 replacement liquid storage tank 2: prepare it according to the weight ratio of absolute dry concentrate and extraction stock solution of 1:7, then add hydrochloric acid to the extraction stock solution, adjust the pH value of the extraction stock solution to 6, add 0.6 kg of xylanase, and obtain the extraction stock solution.

[0098] 2. Enzymatic hydrolysis and extraction: The concentrate obtained in step 1 is placed in the extraction tank 1. The extracted stock solution obtained in step 1 is mixed evenly and then pumped into the extraction tank 1 by the No. 1 liquid pump 7 to perform low-temperature enzymatic hydrolysis on the concentrate. The enzymatic hydrolysis temperature is 50°C and the enzymatic hydrolysis time is 5.5 hours. During the enzymatic hydrolysis process, the extracted stock solution is circulated once every 1 hour by the No. 4 liquid pump 15.

[0099] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared into a liquid according to the weight ratio of absolute dry concentrate to liquid of 1:6, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced by positive pressure through the No. 4 pipeline 11 into the decoction liquid storage tank 5. The extract in the decoction liquid storage tank 5 is allowed to stand, and the supernatant is filtered. The liquid constitutes 1200 kg of extract A, and the extract A is sent to the next process for standby.

[0100] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure in the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure in the extraction tank 1 rises to -0.06MPa, maintain the current pressure for decoction. The decoction time is 1.5h.

[0101] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:5, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8. This liquid is used as the liquid for preparing the extraction stock solution in the next step one.

[0102] IV. Decoction under positive and negative pressure conditions: After the replacement in step 3 is completed, the pressure in extraction tank 1 is raised to 0.18 MPa and maintained for positive pressure decoction for 0.8 hours. The exhaust valve is then opened to exhaust steam to the condenser. When the exhaust is complete, the vacuum system is activated to reduce the pressure in extraction tank 1 to -0.05 MPa and maintain this pressure for negative pressure decoction for 0.7 hours. After decoction, the liquid in extraction tank 1 is separated: the liquid in extraction tank 1 is pumped into displacement tank 3 (No. 2) via liquid pump 7 to serve as the prepared solution for the next extraction in step 3. After the separation is complete, the decoction is removed from extraction tank 1, resulting in 383 kg of decoction (49% moisture content).

[0103] 5. Peeling of cooking material: The cooking material is sent to the peeling machine for peeling, and 288kg of core rod material and 96kg of skin material are obtained, and the skin and core rod separation rate is 99.5%.

[0104] 6. Secondary extraction: The core rod material separated in step 5 is sent to a tearing machine and a thread rolling machine for refinement treatment. The treated coarse material is sent to a desubmersible tank, and then a clear liquid is added. The clear liquid is adjusted to a pH value of 8 by using food-grade alkali. The clear liquid is added to the desubmersible tank to slurry the coarse material, and the slurry concentration is adjusted to 9%. The desubmersible tank is then heated to 90°C and stirred for 0.7 hours. The vacuum system is then turned on to make the pressure in the desubmersible tank -0.04MPa and maintained for negative pressure desubmersible treatment for 0.6 hours. After the treatment is completed, the material is pumped into an extruder with a slurry pump for material-liquid separation, and 1146kg of extract B and 481kg of coarse slurry are separated (water content 70.5%).

[0105] 7. Pulping: The coarse pulp separated in step 6 is converted into an absolute dry material, water is taken according to the material-liquid weight ratio of 1:4, 12% potassium hydroxide, 1% sodium silicate, 0.4% magnesium sulfate, 4% hydrogen peroxide, and 0.1% ethylenediaminetetraacetic acid are added to the water and mixed evenly to form a mixed liquid, the mixed liquid and the coarse pulp are sent to a mixer, mixed evenly, and then sent to a twin-screw pulping machine for processing to obtain a fine pulp.

[0106] De-latching treatment of fine pulp: send the fine pulp into the de-latching tank, add water to adjust the concentration to 8%, raise the temperature to 80℃, and de-latching treatment time is 0.7h. The pulp after de-latching treatment is pumped to the high-consistency refiner with a pulp pump, and then enters the washing machine for washing and the concentrator for dehydration. The dehydrated pulp is sent to the dryer. After drying, the finished product is obtained - 123kg of mulberry tree core fiber pulp, with a pulp yield of 86.7%.

[0107] 64kg of black liquor produced by the twin-screw pulping machine is sent to the dryer. After drying, the residue is the finished product - 18kg of potash fertilizer raw material.

[0108] 8. Extract preparation: 1146 kg of extract B separated in step 6 is pumped into an extract tank and mixed with 1200 kg of extract A extracted in step 2, and then pumped to a membrane separation device for separation. The separated concentrated liquid is vacuum concentrated to obtain a finished product - 19 kg of paper mulberry branch extract (concentration 48.5%). The separated clear liquid is reused.

[0109] IX. Hide Processing: The hide separated in step 5 is conveyed to a bast separation device via a conveyor to separate the surface bark from the bast. The separation rate of surface bark and bast is 97.5%. The separated bast is sent to a dryer for drying. After drying, it is sent to an opener and carding machine to produce a finished product - 25 kg of bast fiber product. The separated surface bark is sent to a dryer for drying to produce a finished product - 23 kg of surface bark product.

[0110] Example 5

[0111] Another embodiment of the fresh bamboo enzymatic hydrolysis, displacement, decoction and extraction method comprises the following steps:

[0112] 1. Material preparation: Prepare the concentrate according to the method of Example 1

[0113] Preparation of extraction stock solution: prepare the extraction stock solution in the No. 1 displacement storage tank 2, convert the above concentrate into 200 kg of absolute dry concentrate, prepare it according to the concentrate and extraction stock solution weight ratio of 1:6, and then add 0.3 kg of food-grade xylanase to obtain the extraction stock solution.

[0114] 2. Enzymatic extraction: The concentrate obtained in step 1 is placed in the extraction tank 1; the extracted stock solution obtained in step 1 is then mixed evenly and pumped into the extraction tank 1 by the No. 1 liquid pump 7 to perform low-temperature enzymatic hydrolysis on the concentrate. The enzymatic hydrolysis temperature is 45°C and the enzymatic hydrolysis time is 5 hours. During the enzymatic hydrolysis process, the extracted stock solution is circulated once every 1 hour by the No. 4 liquid pump 15;

[0115] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared into a liquid according to the weight ratio of absolute dry concentrate to liquid of 1:5, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced into the decoction liquid storage tank 5 through the No. 4 pipeline 11. The extract in the decoction liquid storage tank 5 is allowed to stand, and then the supernatant is filtered. The liquid constitutes 1000 kg of extract A, and the extract A is sent to the next process for standby.

[0116] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure in the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure in the extraction tank 1 rises to -0.06MPa, maintain the current pressure for decoction. The decoction time is 1.2h.

[0117] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:4, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8. This liquid is used as the liquid for preparing the extraction stock solution in step 1.

[0118] Fourth, decoction under positive and negative pressure conditions: After the replacement in step 3 is completed, the pressure in extraction tank 1 is increased to 0.2 MPa and maintained for positive pressure decoction for 0.8 hours. The exhaust valve is then opened to exhaust steam to the condenser. When the exhaust is complete, the vacuum system is activated to reduce the pressure in extraction tank 1 to -0.03 MPa and maintain this pressure for negative pressure decoction for 1 hour. After decoction, the liquid is separated: During the separation, the liquid in extraction tank 1 is pumped into replacement tank 3 (No. 2) via liquid pump 7 to serve as the preparation solution for the next extraction in step 3. After the separation, the decoction material in extraction tank 1 is removed, yielding 361 kg of decoction material with a moisture content of 49.5%.

[0119] 5. Secondary extraction: The decoction obtained in step 4 is sent to a wire rolling machine for refining treatment. After the wire rolling is completed, it is sent to a de-submersible tank, and then a clear liquid is added to adjust the concentration to 8%. The pH value of the clear liquid is adjusted to 7.5 by food-grade alkali; after adding the clear liquid, the de-submersible tank is heated to 80°C and stirred for 0.6h. After the stirring is completed, the vacuum system is turned on to make the pressure in the de-submersible tank -0.05MPa and maintain it for negative pressure de-submersible treatment for 0.6h; after the treatment is completed, the de-submersible is pumped to an extruder for material-liquid separation with a slurry pump. The 1693kg liquid after separation constitutes extract B, and the separated 580kg slurry constitutes a coarse slurry with a water content of 70%.

[0120] 6. Pulping: The coarse pulp obtained in step 5 is converted into an absolute dry material, and water is added at a weight ratio of 1:3.9 between the material and the liquid. 10% potassium hydroxide, 1.5% sodium silicate, 0.8% magnesium sulfate, 5% hydrogen peroxide, and 0.4% ethylenediaminetetraacetic acid are added to the water to form a mixed liquid. The mixed liquid and the coarse pulp are then sent to a mixer for uniform mixing, and then sent to a twin-screw pulping machine for processing to obtain fine pulp and black liquor;

[0121] Fine pulp latent removal treatment: The fine pulp is sent to a latent removal tank, where water is added to adjust the pulp concentration to 8%. The temperature is then raised to 80°C for 0.6 hours. After latent removal, the pulp is pumped to a refiner for refining, followed by washing in a washing machine and dehydration in a thickener. The dehydrated pulp is then sent to a dryer. After drying, the finished product is 153 kg of bamboo pulp, with a pulp yield of 87.9%.

[0122] 87 kg of black liquor produced during the processing of the twin-screw pulping machine was sent to the dryer for drying, and the residue was dried to obtain a finished product - 19.8 kg of potash fertilizer raw material.

[0123] VII. Extract Preparation: 1693 kg of Extract B from Step 5 was mixed with 1000 kg of Extract A from Step 2 and pumped to a membrane separation device. The separated concentrated solution was vacuum concentrated to obtain 52 kg of fresh bamboo extract with a concentration of 49.5%. The separated clear solution was reused.

[0124] Example 6

[0125] Another embodiment of the fresh bamboo enzymatic hydrolysis, displacement, decoction and extraction method comprises the following steps:

[0126] 1. Material preparation: Prepare the concentrate according to the method of Example 1, and convert it into 200 kg of absolute dry material;

[0127] Preparation of extraction stock solution: prepare the extraction stock solution in the No. 1 displacement storage tank 2: prepare it according to the weight ratio of the concentrate and the extraction stock solution of 1:7, and then add 0.4 kg of xylanase into the extraction stock solution to obtain the extraction stock solution.

[0128] 2. Enzymatic extraction: The concentrate obtained in step 1 is placed in the extraction tank 1. The extract obtained in step 1 is mixed evenly and then pumped into the extraction tank 1 by the No. 1 liquid pump 7 to perform low-temperature enzymolysis on the concentrate. The enzymolysis temperature is 50°C and the enzymolysis time is 5.5h. During the enzymolysis process, the extract is circulated once every 1 hour by the No. 4 liquid pump 15.

[0129] After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank 3 is prepared into a liquid according to the weight ratio of absolute dry concentrate to liquid of 1:6, and the liquid in the No. 2 replacement liquid storage tank 3 is pumped into the bottom of the extraction tank 1 through the No. 1 liquid pump 7. During the pumping process, the liquid in the extraction tank 1 is replaced into the decoction liquid storage tank 5 through the No. 4 pipeline 11. The extract in the decoction liquid storage tank 5 is allowed to stand, and the supernatant is filtered to obtain 1200 kg of extract A, which is sent to the next process for standby.

[0130] 3. Negative pressure decoction: Turn on the vacuum system to perform negative pressure decoction on the extraction tank 1. When the pressure inside the extraction tank 1 is -0.09MPa, open the steam valve to heat and increase the temperature. When the pressure inside the extraction tank 1 rises to -0.05MPa, maintain the current air pressure for decoction. The decoction time is 1 hour.

[0131] After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:5, and the prepared liquid is pumped into the bottom of the extraction tank 1 through the No. 2 liquid pump 10. During the pumping process, the liquid in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8. This liquid is used as the liquid for preparing the extraction stock solution in the next step one.

[0132] Fourth, decoction under positive and negative pressure conditions: After the replacement in step 3 is completed, the pressure in extraction tank 1 is raised to 0.15 MPa and maintained for positive pressure decoction for 1 hour. The exhaust valve is then opened to exhaust steam to the condenser. When the exhaust is complete, the vacuum system is activated to reduce the pressure in extraction tank 1 to -0.04 MPa and maintain this pressure for negative pressure decoction for 0.8 hour. After decoction, the liquid in extraction tank 1 is separated: the liquid in extraction tank 1 is pumped into replacement liquid storage tank 3 (No. 2) via liquid pump 7 to serve as the prepared solution for the next extraction in step 3. After the separation is complete, the extraction tank is opened and 368 kg of decoction material is removed, with a moisture content of 50.2%.

[0133] 5. Secondary extraction: The decoction obtained in step 4 is sent to a wire rolling machine for refining treatment. After the wire rolling is completed, it is sent to a desubstrate tank, and then a clear liquid is added to adjust the concentration to 9%. The pH value of the clear liquid is adjusted to 8 by food-grade alkali; after adding the clear liquid, the desubstrate tank is heated to 90°C and stirred for 0.6h. After the stirring is completed, the vacuum system is turned on to make the pressure in the desubstrate tank -0.04MPa and maintain it for negative pressure desubstrate treatment. The treatment time is 0.7h; after the treatment is completed, the desubstrate is pumped to an extruder for material-liquid separation. The 1446kg liquid after separation constitutes extract B, and the separated 586kg slurry constitutes a coarse slurry (water content 70.5%).

[0134] 6. Pulping: The coarse pulp obtained in step 5 is converted into an absolute dry material, and water is added according to a weight ratio of 1:4 between the material and the liquid. 12% potassium hydroxide, 1.2% sodium silicate, 0.6% magnesium sulfate, 4% hydrogen peroxide, and 0.3% ethylenediaminetetraacetic acid are added to the water to form a mixed liquid. The mixed liquid and the coarse pulp are sent to a mixer for uniform mixing, and then sent to a twin-screw pulping machine for processing to obtain fine pulp and black liquor;

[0135] Fine pulp latent removal treatment: The fine pulp is sent to a latent removal tank, where water is added to adjust the pulp concentration to 9%. The temperature is raised to 70°C and the latent removal treatment lasts for 0.7 hours. After the latent removal is completed, the pulp is pumped to a pulping machine for refining, followed by washing in a washing machine and dehydration in a thickener. The dehydrated pulp is sent to a dryer, where 151 kg of finished bamboo pulp is obtained, with a pulp yield of 87.3%.

[0136] 83 kg of black liquor produced during the twin-screw pulping process was sent to the dryer for drying, and the dry residue constituted 20 kg of finished potash fertilizer raw material.

[0137] 7. Extract Preparation: 1446 kg of Extract B obtained in step 5 and 1200 kg of Extract A obtained in step 2 were mixed and pumped into a membrane separation device. The separated concentrated liquid was vacuum concentrated to obtain a finished product - 57 kg of fresh bamboo extract (concentration 47.5%). The separated clear liquid was reused.

[0138] Example 7

[0139] like Figure 1 As shown: A plant branch enzymatic hydrolysis, replacement, and decoction extraction system includes an extraction tank 1, a No. 1 replacement liquid storage tank 2, a No. 2 replacement liquid storage tank 3, a fresh solvent liquid storage tank 4, and a decoction liquid storage tank 5. The No. 1 replacement liquid storage tank 2, the No. 2 replacement liquid storage tank 3, the fresh solvent liquid storage tank 4, and the decoction liquid storage tank 5 are connected to the extraction tank 1 through various pipes and liquid pumps. Each pipe is equipped with a control valve to control the opening and closing of the pipe. The extraction tank 1 serves as an extraction container to perform enzymatic hydrolysis and component extraction on the plant branch. The No. 1 replacement liquid storage tank 2, the No. 2 replacement liquid storage tank 3, and the fresh solvent liquid storage tank 4 store the extract during replacement. The decoction liquid storage tank 5 allows the extract replaced in the decoction liquid storage tank 5 to stand and separate, so that the active ingredients extracted from the plant branch can enter the next process (the next process can be used to make an extract), thereby completing the extraction of the required ingredients.

[0140] There is only one extraction tank 1 , and a No. 1 replacement liquid storage tank 2 , a No. 2 replacement liquid storage tank 3 , and a fresh solvent liquid storage tank 4 are all connected to the extraction tank 1 .

[0141] More specifically, the bottoms of the No. 1 replacement storage tank 2 and the No. 2 replacement storage tank 3 are connected to the bottom of the extraction tank 1 through the No. 1 pipe 6, and the No. 1 liquid pump 7 is provided on the No. 1 pipe 6, and the extracted liquid in the No. 1 replacement storage tank 2 and the No. 2 replacement storage tank 3 is sucked into the extraction tank 1 through the No. 1 liquid pump 7, and the No. 1 replacement storage tank 2 and the No. 2 replacement storage tank 3 can be controlled by a valve to respectively feed liquid into the extraction tank 1; the top of the extraction tank 1 is connected to the top of the No. 1 replacement storage tank 2 through the No. 2 pipe 8, so that the extracted liquid in the extraction tank 1 is replaced by the No. 1 replacement storage tank 2 through the No. 2 pipe 8. Here, "replacement" means that when the liquid is pumped into the extraction tank 1 from the bottom of the extraction tank 1 by the positive pressure of the pump, the original liquid in the extraction tank 1 is discharged from the top of the extraction tank 1; the bottom of the extraction tank 1 is connected to the top of the No. 2 replacement storage tank 3 through the No. 6 pipe 26, and the No. 6 pipe 26 is also provided with a No. 4 liquid pump 15, which is connected to the No. 4 replacement storage tank 2 through the No. The liquid extraction pump 15 pumps the extract in the extraction tank 1 into the No. 2 replacement liquid storage tank 3; the bottom of the fresh solvent storage tank 4 is connected to the bottom of the extraction tank 1 through the No. 3 pipe 9, and the No. 3 pipe 9 is also provided with a No. 2 liquid extraction pump 10, which pumps the fresh solvent (such as water) in the fresh solvent storage tank 4 into the extraction tank 1 through the No. 2 liquid extraction pump 10, and the branches in the extraction tank 1 are supplemented with solvent and then boiled and extracted; the top of the decoction storage tank 5 is connected to the top of the extraction tank 1. The extracting tank 1 is connected to the decoction liquid storage tank 5 via the No. 4 pipe 11. During the process of replacing the extract in the extraction tank 1, the extract is displaced into the decoction liquid storage tank 5 by positive pressure. The decoction liquid storage tank 5 allows the extract to rest, and then removes the supernatant, which constitutes the extract. The extract is then sent to the next process for standby. The decoction liquid storage tank 5 is connected to the subsequent process via the No. 5 pipe 12. The No. 3 liquid pump 13 is also installed on the No. 5 pipe 12, and the supernatant is pumped by the No. 3 liquid pump 13. The extraction tank 1 is also provided with an internal liquid circulation pipe 14. The internal liquid circulation pipe 14 is arranged outside the extraction tank 1, with one end connected to the bottom of the extraction tank 1 and the other end connected to the top of the extraction tank. The internal liquid circulation pipe 14 is connected to the No. 4 liquid pump 15, and the No. 4 liquid pump 15 realizes the internal circulation of the extract, further improving the extraction efficiency and shortening the extraction time. According to one embodiment of the present invention, the two ends of the internal liquid circulation pipe 14 are respectively connected to the two ends of the extraction tank 1. A valve is installed on each pipeline to control the opening and closing of the pipeline.

[0142] Before extraction, the plant branches are cut, dusted and removed, and loaded into a material cage, which is then loaded into the extraction tank 1. The No. 1 replacement liquid storage tank 2 contains the extract replaced (second replacement) during the previous extraction, and the extract is added with xylanase; the No. 2 replacement liquid storage tank 3 contains the extract pumped out during the previous extraction, and the fresh solvent storage tank 4 contains fresh solvent (such as water). The decoction liquid storage tank 5 receives the extract replaced (first replacement) during the previous extraction, processes it, and enters the next process; during extraction, the extract in the No. 1 replacement liquid storage tank 2 is pumped into the extraction tank 1 from the bottom through the No. 1 pumping pump 7 and the No. 1 pipeline 6 to perform enzymatic hydrolysis on the plant branches. During the enzymatic hydrolysis process, the No. 4 pumping pump 15 is used to circulate the extract in the extraction tank 1 through the internal liquid circulation pipeline 14 once every 1 hour until the enzymatic hydrolysis is completed. During the circulation process, the valve on the No. 6 pipeline 26 should be closed. After the enzymatic hydrolysis is completed, the No. 1 liquid pump 7 extracts the extract in the No. 2 replacement liquid storage tank 3 and pumps it into the extraction tank 1 from the bottom of the extraction tank 1 through the No. 1 pipe 6, and the extract obtained after the enzymatic hydrolysis is replaced into the decoction liquid storage tank 5 through the No. 4 pipe 11 by positive pressure (the first replacement of this tank), and the decoction liquid storage tank 5 allows the extract to stand; after the replacement is completed, the extraction tank 1 is heated and the vacuum system is turned on to perform negative pressure decoction (pressure is less than atmospheric pressure) until the negative pressure decoction process is completed; after the decoction is completed, the No. 2 liquid pump 10 pumps the fresh solvent in the fresh solvent storage tank 4 into the extraction tank 1 through the No. 3 pipe 9. The extract in the extraction tank 1 is replaced into the No. 1 replacement liquid storage tank 2 through the No. 2 pipeline 8 by positive pressure (the second replacement of this tank); after the replacement is completed, the extraction tank 1 is first heated and heated for positive pressure decoction, and then negative pressure decoction is performed. When the decoction is completed, the material and liquid are separated; when the material and liquid are separated, the No. 4 liquid pump 15 sucks the extract in the extraction tank 1 into the No. 2 replacement liquid storage tank 3 through the No. 6 pipeline 26. After one batch of extraction is completed, the plant branch decoction in the extraction tank 1 is taken out and enters the next process, and new branches to be extracted are replaced to carry out the above-mentioned sequence of operations. The plant branch decoction after extraction can be used as a fiber raw material.

[0143] like Figure 2-4As shown: the extraction tank 1 includes a tank body and a material cage 17, and the feeding end and the discharging end of the extraction tank 1 are respectively provided with a tank cover 18, and the tank cover 18 and the tank body of the extraction tank 1 can be locked with a self-locking structure, such as a wedge gearing structure; a spiral heating coil 19 is wrapped around the outside of the tank body, and one end of the spiral heating coil 19 has a heat source inlet and is connected to the heat source, and the other end of the spiral heating coil 19 has a condensation outlet and is connected to a heat source recovery device, and a heating medium (steam) is contained in the spiral heating coil 19, and the extraction tank 1 is heated by circulating heating through the spiral heating coil 19; the extraction tank 1 is also provided with a condensate outlet 20 for discharging the condensate formed in the spiral heating coil 19; a plurality of extraction tank interfaces 27 connected to the inside of the extraction tank are provided on the extraction tank 1, and the extraction tank interfaces 27 are connected to Figure 1 The various pipes shown are connected to the condenser (not shown in the figure), and the number of interfaces can be set as needed. The vacuum system includes a condenser and a vacuum pump (not shown in the figure), the vacuum pump is connected to the condenser, and the condenser is connected to the extraction tank 1. A pressure gauge 21 is also provided on the top of the extraction tank 1. The detection end of the pressure gauge 21 is placed in the extraction tank 1, and the internal pressure of the extraction tank 1 is detected by the pressure gauge 21; the material cage 17 is a mesh material cage, and its external dimensions match the internal dimensions of the extraction tank 1 (the material cage 17 can be loaded into the extraction tank 1 and make full use of the internal space of the extraction tank 1); the bottom of the tank body in the extraction tank 1 is paved with a slide rail 22 from the feed end to the discharge end, and the bottom of the material cage 17 is provided with a pulley groove 23 matching the slide rail 22, so as to facilitate the entry and exit of the material cage 17; a traction device 24 is provided at the bottom of the discharge end of the extraction tank 1, and the traction device 24 can be a winch. When the material cage 17 is heavy, the material cage 17 can be pulled by the traction device 24 to achieve the purpose of saving effort; a safety valve 25 is also provided on the top of the extraction tank 1, and the safety valve 25 is used to release the pressure when the positive pressure in the extraction tank 1 exceeds the safety limit to avoid safety accidents.

Claims

1. A plant enzymatic hydrolysis, displacement, decoction and extraction method comprising the following steps: (1) Material preparation: Cut and wash the raw materials to obtain the concentrate, and prepare the extraction solution in the No. 1 replacement liquid storage tank: add xylanase to the extraction solution at a weight ratio of absolute dry concentrate to xylanase of 1000:1-5; (2) Enzymatic extraction: the concentrate obtained in step (1) is placed in an extraction tank, and then the extracted stock solution obtained in step (1) is pumped into the extraction tank, heated and enzymatically hydrolyzed, and the weight ratio of the absolute dry concentrate to the extracted stock solution is 1:5-15; After the enzymatic hydrolysis is completed, the liquid in the No. 2 replacement liquid storage tank is pumped into the bottom of the extraction tank through the No. 1 liquid pump at a weight ratio of absolute dry concentrate to liquid of 1:4-12, and the liquid in the extraction tank is replaced into the decoction liquid storage tank through the No. 4 pipeline; (3) Negative pressure decoction: After the replacement in step (2) is completed, the vacuum system is turned on to make the pressure value in the extraction tank between -0.01 and -0.09 MPa for negative pressure decoction, and the decoction time is 0.5-2 hours; After the decoction is completed, the liquid in the fresh solvent storage tank is prepared into a liquid according to the weight ratio of absolute dry material to liquid of 1:3-10, and the prepared liquid is pumped into the bottom of the extraction tank through the No. 2 liquid pump. During the pumping process, the liquid in the extraction tank is replaced into the No. 1 replacement liquid storage tank through the No. 2 pipe, which serves as the liquid for preparing the extraction solution in step (1); (4) Decoction under positive and negative pressure conditions: After the replacement in step (3) is completed, the pressure of the extraction tank is increased to 0.1 to 0.27 MPa, and the pressure is maintained for positive pressure decoction, and the decoction time is 0.5-1 h; then the exhaust valve is opened to exhaust steam to the condenser. When the exhaust is completed, the vacuum system is opened to reduce the pressure in the extraction tank to -0.01 to -0.09 MPa and maintain it, and negative pressure decoction is performed, and the decoction time is 0.5-1 h; After the decoction is completed, the material and liquid are separated. During the separation, the liquid in the extraction tank is pumped into the No. 2 replacement liquid storage tank by the No. 1 liquid pump, and used as the solution for the extraction in step (3). After the separation of the material and liquid is completed, the extraction tank is opened to take out the decoction material.

2. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 1, characterized in that: When preparing the extraction solution in step (1), acid is added to adjust the pH value of the extraction solution so that the pH value of the extraction solution is 4.5-6.

5.

3. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 1, characterized in that: The enzymatic hydrolysis temperature of the extraction tank in step (2) is 40-60°C, and the enzymatic hydrolysis time is 4.5-8h.

4. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 1, wherein: During the enzymatic hydrolysis process in step (2), the extracted stock solution is circulated once every hour through the No. 4 liquid pump until the enzymatic hydrolysis is completed.

5. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 1, characterized in that: The method further includes processing the decoction obtained in step (4), and the specific steps are as follows: (5) Peeling the cooked material to separate the core material and the skin material; (6) The core rod material obtained by separation in step (5) is sent to a tearing machine and a thread rolling machine for refinement treatment. The treated coarse material is sent to a desubmersible tank, a clear liquid is added, the desubmersible tank is heated and continuously stirred, and the vacuum system is turned on to make the pressure in the desubmersible tank be -0.01 to -0.08 MPa and maintained for negative pressure desubmersible treatment. The treatment time is 0.5-1 h. After the treatment is completed, the material is pumped into an extruder with a slurry pump for material-liquid separation to obtain an extract and a coarse slurry; (7) Prepare a mixed liquid. Take water according to the weight ratio of absolute dry coarse pulp to water of 1:3.8-4.2, then add 5-20wt% of potassium hydroxide, 0.5-2wt% of sodium silicate, 0.2-1wt% of magnesium sulfate, 2-6wt% of hydrogen peroxide, and 0.1-0.5wt% of ethylenediaminetetraacetic acid into the water and mix them evenly to form a mixed liquid. Send the mixed liquid and the coarse pulp into a mixer and mix them evenly. Then send them into a twin-screw pulping machine for treatment. The fine pulp obtained after treatment is sent to a de-submersible tank for de-submersible treatment. The pulp after de-submersible treatment is pumped to a high-concentration pulping machine for pulping treatment, then enters a washing machine for washing, and finally enters a concentrator for dehydration treatment. The dehydrated pulp is sent to a dryer for drying. After drying, paper pulp is obtained. The black liquor produced after the twin-screw pulping machine is sent to a dryer for drying. After drying, potash fertilizer raw material is obtained.

6. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 5, characterized in that: The method further comprises mixing the extracts obtained in step (6) and step (2), sending the mixture to a membrane separation device for separation treatment, and vacuum concentrating the separated concentrated liquid to obtain an extract.

7. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 6, characterized in that: The method also includes leather processing, which is as follows: the leather obtained in step (5) is sent to a tree bast separation device to separate the surface bark and bast, the separated bast is sent to a dryer for drying, and after drying, it is sent to an opener and a carding machine for processing to obtain a finished bast fiber product, and the separated surface bark is sent to a dryer for drying to obtain a finished surface bark product.

8. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 5, characterized in that: The pH value of the clear solution in step (6) is adjusted by alkali to a pH value of 7.5-9.

5.

9. The plant enzymatic hydrolysis, displacement, decoction and extraction method according to claim 1, characterized in that: The xylanase in step (1) is food grade xylanase.

10. A plant branch enzymatic hydrolysis, displacement, decoction and extraction system, characterized by: It includes an extraction tank, a No. 1 replacement liquid storage tank, a No. 2 replacement liquid storage tank, a fresh solvent liquid storage tank, and a decoction liquid tank; the bottoms of the No. 1 replacement liquid storage tank and the No. 2 replacement liquid storage tank are connected to the bottom of the extraction tank through the No. 1 pipe, and the No. 1 pipe is provided with a No. 1 liquid extraction pump. The top of the extraction tank is connected to the top of the No. 1 replacement liquid storage tank through the No. 2 pipe, and the bottom of the fresh solvent liquid storage tank is connected to the bottom of the extraction tank through the No. 3 pipe, and the No. 3 pipe is also provided with a No. 2 liquid extraction pump. The top of the decoction liquid tank is connected to the top of the extraction tank through the No. 4 pipe, and the bottom of the extraction tank is connected to the top of the No. 2 replacement liquid storage tank through the No. 6 pipe, and the No. 6 pipe is also provided with a No. 4 liquid extraction pump. Valves are set on each pipe.

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