WO2020199858A1 - 一种大豆浓缩蛋白制取*** - Google Patents

一种大豆浓缩蛋白制取*** Download PDF

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Publication number
WO2020199858A1
WO2020199858A1 PCT/CN2020/078566 CN2020078566W WO2020199858A1 WO 2020199858 A1 WO2020199858 A1 WO 2020199858A1 CN 2020078566 W CN2020078566 W CN 2020078566W WO 2020199858 A1 WO2020199858 A1 WO 2020199858A1
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Prior art keywords
inlet
outlet
extractor
spiral
tank
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PCT/CN2020/078566
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English (en)
French (fr)
Inventor
尹越峰
张玉琛
梁椿松
袁媛
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迈安德集团有限公司
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Application filed by 迈安德集团有限公司 filed Critical 迈安德集团有限公司
Priority to EA202191376A priority Critical patent/EA202191376A1/ru
Publication of WO2020199858A1 publication Critical patent/WO2020199858A1/zh

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    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J3/00—Working-up of proteins for foodstuffs
    • A23J3/14—Vegetable proteins
    • A23J3/16—Vegetable proteins from soybean
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
    • C07K1/14—Extraction; Separation; Purification
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
    • C07K1/14—Extraction; Separation; Purification
    • C07K1/34—Extraction; Separation; Purification by filtration, ultrafiltration or reverse osmosis

Definitions

  • the invention relates to an extraction system, in particular to a soybean protein concentrate preparation system, which can be used for dynamic extraction in food, environmental protection, chemical and other industries, and belongs to the technical field of extraction equipment.
  • the raw material of soy protein concentrate is low-denaturation puffed soybean meal or white soybean flakes desolved at low temperature.
  • the preparation process starts from the daily warehouse, which stores raw materials for about one day, which can ensure the stable operation of the extraction workshop; the materials are first quantitatively output by the daily warehouse discharge frequency conversion scraper, and then enter the grading sieve (20 mesh) through the elevator, and then on the sieve. The material enters the weighing scale for measurement, and then is sent to the temporary storage tank in the extraction workshop through a hoist and a flat scraper.
  • the temporary storage tank in the leaching workshop plays the role of material sealing and ensuring the stability of the leaching supply.
  • the temporary storage box is fed with a variable frequency feed air shutoff device to feed the prepreg quantitatively.
  • the raw materials are fully contacted with the mixed solvent to complete the expansion process, so that the prepreg soybean meal has good permeability in the extractor; the prepreg expanded raw materials enter the extractor, and the soluble sugars and soluble sugars are fully extracted in the extractor.
  • Other small amounts of soluble substances while ensuring that the protein is dissolved as little as possible, so as to achieve the process of increasing the protein content of the raw material, and become a wet-based protein concentrate.
  • the existing soy protein concentrate preparation system has the following defects: 1.
  • the low utilization rate of raw materials leads to a decline in economic benefits.
  • the soy protein concentrate raw materials are processed, transported, and upgraded through multiple processes. Some raw materials inevitably turn into powder from flakes and granules. After sieving, the sieve (passing a 20-mesh sieve or 30-mesh sieve) becomes powdery white beans. Flake or powder low-denaturation puffed soybean meal accounts for 8-10% of the total raw materials, and this part of the material must be stored separately. Among them, the powdered white bean flakes can only process soy protein isolate. If there is a related protein isolate production line, it can still be used with value.
  • the raw material is low-denaturation puffed soybean meal, this part of high-protein mixed raw soybean meal can only be mixed into the high-temperature meal production line, and can be used as animal feed after maturation, which has low economic value.
  • a pre-soaking process must be set up: the raw materials must be pre-soaked before leaching, so that the protein tissue will fully expand after absorbing water, so that the volume of the wet material will increase by about 15-20% compared to the dry material, otherwise the raw material will swell and compact after absorbing moisture and is completely impermeable.
  • the raw material that is saturated with water and ethanol has poor strength, and the porosity under the self-weight pressure after the formation of the material layer is low, and the permeability is poor.
  • the only way to reduce the thickness of the material layer is to control the thickness of the material layer to 350mm (conventional soybean extract material layer is 1000-2800mm), which leads to a huge size of the alcohol washing extractor, but the production capacity is very low.
  • the capacity of an extractor of the same size is only one tenth of that of conventional leaching. As a result, the investment in the extractor is huge, and the related production workshop, civil engineering, steel structure and floor space are very large.
  • the extractor needs to be equipped with a multi-stage solvent circulation pump and a grid backwash system: the solvent circulation spray system is usually no less than a 12-stage circulation pump, which consumes a lot of electricity and has many pump valve leakage points.
  • the concentrated extract obtained by the soy protein concentrate production system contains many powder particles, which will cause the valve of the outlet pipe to be blocked when flowing into the subsequent pipeline, and it must be filtered by a filter screen or a grid. The clogging of the filter or grid will cause the extraction or washing process to be reduced or unsustainable, and must be cleaned and maintained frequently; the grid backwash system is complex in structure, enclosed in an explosive solvent environment (full of ethanol vapor), and frequently malfunctions, affecting the chemical industry The unit runs continuously.
  • the purpose of the present invention is to overcome the problems existing in the prior art and provide a soy protein concentrate preparation system, which can omit screening, prepreg equipment, solvent circulation spraying and grid backwashing systems, so that all powder leftovers can be obtained. Utilization greatly improves economic efficiency.
  • a soybean protein concentrate preparation system of the present invention includes a raw material temporary storage bin, a quantitative auger, a powder extractor and a wet meal conveyor, the outlet of the raw material temporary storage bin and the inlet of the quantitative auger
  • the outlet of the quantitative auger is connected with the solid material inlet of the extractor
  • the wet meal outlet of the extractor is connected with the inlet of the wet meal conveyor
  • the inlet of the new solvent pump is connected with the fresh solvent pipe
  • the outlet of the new solvent pump is connected with the fresh solvent of the extractor.
  • the inlet is connected, the concentrate outlet of the extractor is connected with the inlet of the concentrate extraction pump, the outlet of the concentrate extraction pump is connected to the inlet of the first-stage hydrocyclone through the mixed liquid delivery pipe, and the light phase of the first-stage hydrocyclone
  • the outlet is connected with the inlet of the secondary hydrocyclone, the light phase outlet of the secondary hydrocyclone is connected with the inlet of the solution temporary storage tank, and the primary cyclonic separator, the secondary hydrocyclone and the solution temporary storage tank
  • the bottom outlets are all connected with the return port of the powder extractor; the lower outlet of the solution temporary storage tank is connected with the inlet of the temporary storage tank transfer pump, and the outlet of the temporary storage tank transfer pump is connected to the concentrated extraction of the extraction liquid evaporation recovery system
  • the liquid inlet is connected.
  • the present invention has achieved the following beneficial effects: white soybean flakes or low-denatured soybean meal enter the quantitative auger from the raw material temporary storage bin, and the quantitative auger sends the white soybean flakes directly into the extractor solid material of the powder extractor At the inlet, the powder extractor adopts "one-pot stew" extraction, and the extracted wet-based protein concentrate is discharged from the wet meal outlet of the extractor and sent out by the wet meal conveyor.
  • the new solvent pump sends the new solvent to the freshly dissolved inlet of the extractor.
  • the concentrated solution containing certain powder particles is drawn by the concentrated extracting liquid pump, it is sent to the first-stage hydrocyclone through the mixed liquid delivery pipe for separation, and the solution is removed for the first time
  • the solid particles in the solution are removed again by the secondary hydrocyclone, they enter the solution temporary storage tank for storage.
  • the separated solid particles flow will be extracted from the soaking tank of the leaching device, and the concentrated solution after precipitation will be temporarily removed from the solution.
  • the outlet of the storage tank is sent to the concentrated extraction liquid inlet of the extraction liquid evaporation recovery system through the temporary storage tank transfer pump. This system omits the screening and prepreg process, saves the investment and installation site of screening, storage, and prepreg equipment, and eliminates the complicated and tedious solvent circulation spray system and grid backwashing system.
  • the equipment has good airtightness. The hidden dangers such as running and dripping are eliminated, and the operating cost is low.
  • Greatly improve the utilization rate of raw materials increase the utilization rate of raw materials from 90% to 100%. After deducting sugar quality loss and processing costs, its economic value can be increased by 1800-2000 yuan per ton, and additional storage and transportation costs are eliminated.
  • Increasing the utilization rate of powder materials can greatly increase the profitability of concentrated protein enterprises.
  • the extraction system can be standardized, the investment is low, the plant is built quickly, and the expansion is convenient and quick. It is expected to break the bottleneck of the development of soybean protein concentrate and realize the great development of the industry.
  • the outlet of the temporary storage tank transfer pump is also connected to the return port of the solution temporary storage tank through the temporary storage tank return pipe, and the outlet of the wet meal conveyor is connected to the inlet of the double screw squeezer.
  • the outlet is connected, the liquid phase outlet of the double screw squeezer is connected with the inlet of the squeezing liquid transfer pump, and the outlet of the squeezing liquid transfer pump is also connected with the concentrated extract inlet of the extraction liquid evaporation recovery system; the extraction liquid is evaporated and recovered
  • the ethanol condensate outlet of the system is connected with the ethanol condensate output pipe, and the ethanol condensate output pipe is connected with the extraction liquid supplement pipe and then connected with the fresh solvent pipe.
  • the outlet solution of the temporary storage tank transfer pump can also return to the solution temporary storage tank through the temporary storage tank return pipe.
  • the wet-based concentrated protein sent from the wet meal conveyor enters the double-screw squeezer for mechanical squeezing and desolventization.
  • the separated concentrated extract is sent to the concentrated extract inlet of the extract evaporation recovery system by the squeezed liquid delivery pump.
  • the liquid evaporation recovery system evaporates, the concentrated oligosaccharide slurry obtained by evaporation is discharged from the concentrated oligosaccharide slurry outlet, and the 60-65% (wt) ethanol condensate obtained by evaporation is discharged from the ethanol condensate outlet and enters the ethanol condensate output pipe. It is mixed with 95% (wt) ethanol from the extracting solution replenishing pipe to form 70% (wt) ethanol, which is recycled into the fresh solvent pipe.
  • the discharge port of the double screw squeezing dryer is connected with the feed port of the horizontal disc dryer, and the discharge port of the horizontal disc dryer is connected to the inlet of the hot meal scraper conveyor
  • the outlet of the hot meal scraper conveyor is connected with the inlet of the distribution auger, and the outlet of the distribution auger is connected with the inlet of each vertical disc dryer, and the outlet of each vertical disc dryer is respectively It is connected to the feed inlet of Shakron through the protein air pipe, the exhaust outlet of Shakron is connected to the inlet of the induced draft fan, and the bottom of the Shakron is equipped with a rotary discharge valve; horizontal disc dryer and vertical
  • the gas-phase discharge ports of the disc dryer are respectively connected with the reused heat medium inlet of the extraction liquid evaporation recovery system through the reused heat medium pipe.
  • the wet-based protein after being extruded and desolventized by the double screw squeezer first enters the horizontal disc dryer for pre-drying.
  • the moisture content of the pre-dried protein decreases, the temperature rises, and the material becomes divergent, which is scraped by the hot meal
  • the plate conveyor is sent to the entrance of the distribution auger, and the distribution auger distributes the hot meal into each vertical disc dryer for drying, and obtains concentrated protein particles with a moisture content of less than 7%, which are sent to the Shakelong through the protein air pipe After centrifugal separation, it is discharged from the rotary discharge valve at the bottom of the Shakelong, and then enters the crushing section for crushing to obtain 95% powdered protein concentrate with 100 meshes.
  • the thin syrup of the concentrated extract in the solution temporary storage tank enters the extract evaporation recovery system for concentration.
  • the extract evaporation recovery system includes a preheater, a first evaporator, a second evaporator, and a third evaporator.
  • the thin syrup first preheater For preheating, the preheater uses the secondary steam generated by the horizontal disc dryer and the vertical disc dryer as the heat source.
  • the preheated thin syrup enters the first evaporator, and the first evaporator uses raw steam As the heat source, the first evaporator is micro-negative pressure evaporation, the evaporated second steam is used as the heat source of the second steam, and the second steam is the negative pressure evaporation.
  • the thin syrup After the first steam, the thin syrup enters the second steam for negative pressure evaporation; then enters the third In the evaporator, the three steaming is negative pressure evaporation, and the secondary steam of the horizontal disc dryer and the vertical disc dryer is used as the heat source to realize the utilization of the waste heat in this system; the syrup after the three steaming is from the outlet of the concentrated oligosaccharide slurry Discharge, enter the syrup temporary storage tank, and then quantitatively enter the thin film evaporator for concentration, and finally form a thick syrup with a concentration of ⁇ 55%.
  • the powder extractor includes a rectangular box, and a plurality of parallel tank partitions are connected between the front and rear wall panels of the tank, and each tank partition divides the cavity of the tank into multiple There are two soaking tanks.
  • the upper part of each tank partition is provided with overflow ports.
  • the overflow ports on the adjacent tank partitions are staggered in the front and rear directions, and the height of each overflow port gradually decreases from right to left.
  • the discharge end of the immersion tank on the right is connected with the fresh dissolving inlet of the extractor, and the feed end of the leftmost immersion tank is connected with the concentrate outlet of the extractor; the solid material inlet of the extractor is located at the feed end of the leftmost immersion tank Above, the discharge end of each tank partition is respectively provided with a guide groove for lifting and turning the material to the right.
  • the discharge end of the right wall panel of the box body is equipped with a discharge groove extending upward and right.
  • the extractor is wet.
  • the meal outlet is located at the upper end of the discharging trough; the bottom of each soaking trough is arc-shaped and is equipped with soaking trough spirals, and the spiral directions of the adjacent soaking troughs are opposite; each of the guide troughs is respectively installed with a scraper to lift A scraper discharging mechanism is installed in the discharging trough.
  • the material falls from the solid material inlet of the extractor into the feed end of the leftmost soaking tank, and the new solvent pump sends the new solvent into the new melt inlet of the extractor, into the rightmost soaking tank.
  • the soaking and extraction process is completed in the soaking tank.
  • each soaking tank When the material is pushed to the discharge end of each soaking tank, it is pulled up along the guide tank, and after leaving the liquid surface, it is drained briefly and falls into the lower-level soaking tank on the right.
  • the advancing direction of the materials in adjacent soaking tanks is opposite, so that the solid materials move forward in an S-shaped zigzag.
  • the solid material enters the final soaking tank, it is fully immersed and mixed with the new solution, and then removed from the discharge end of the rightmost soaking tank along the discharge tank and discharged from the wet meal outlet of the extractor, and then passes through the wet meal conveyor Send out.
  • the solid material and the solution always keep reverse flow, the material with the highest content is in contact with the concentrated solution, and the material with the lower content is in contact with the dilute solution, which can always maintain a good osmotic pressure, which further improves the mass transfer efficiency.
  • the solid material advances horizontally along the soaking tank alternately, and after a period of lateral advancement, it is taken out and dropped into the next-stage soaking tank in the vertical direction.
  • the material and solution are stirred repeatedly, and the material and solution are in a turbulent state without laminar flow, even if the porosity is small.
  • the powder can also be fully saturated by the solution.
  • the adjacent overflow ports are staggered in the front and rear directions, and the solvent also flows in an S-shaped zigzag direction opposite to the forward direction of the solid material, flows through the full length of each immersion tank, and then uses the offset overflow to enter the next immersion tank and flow back through
  • the full length of the soaking tank greatly extends the extraction stroke of the solid material and the solution, and can achieve full extraction, thereby achieving efficient extraction.
  • the concentrated extract that reaches the leftmost soaking tank is discharged from the concentrated liquid outlet of the extractor.
  • the soaking liquid level is slightly higher than the solid phase, the solid-liquid mixing is sufficient, the solvent consumption is low, the obtained mixed liquid concentration is high, and the evaporation and separation energy consumption is low.
  • the bottom of the soaking tank is arc-shaped and coincides with the soaking tank spiral, which can avoid dead space at the bottom of the tank; the soaking tank spiral is responsible for the transportation of solid materials in the soaking tank and completes the soaking extraction.
  • the forced stirring of the spiral blade avoids the simple soaking process.
  • the spiral directions of adjacent soaking tanks are opposite to make the materials advance in an S shape.
  • the scraper lifting mechanism is used to lift, drain, and transport the soaked solid materials for solid-liquid separation and solid phase lifting; the scraper discharging mechanism is used to lift, drain and transport the solid materials after extraction. discharge.
  • the screw plus scraper not only plays the role of conveying solid materials, but also can strongly stir the solid materials.
  • the height of the material layer in the soaking box can reach 800mm, which is 50-80% higher than the traditional 350mm material layer;
  • the extraction liquid is naturally permeated from top to bottom, changed to spiral mechanical stirring, solid-liquid direct mixing and leaching, extraction power is large, and extraction efficiency is high; the amount of solvent involved in the circulation of the traditional leaching system is 5 times that of the solid material.
  • the liquid volume ratio is about 1.2-1.5 times, and the initial dosage is only one-fourth to one-third of the original amount, which greatly saves a lot of solvents and capital.
  • each immersion tank is provided with at least one baffle plate extending in the left and right direction, and the lower end of each baffle plate is clamped above the spiral of the immersion tank through the concave arc of the baffle plate.
  • the baffle can prevent the surface solution from short-circuiting out if it is not in full contact with the solid material.
  • the concave arc of the baffle is stuck above the spiral of the soaking tank, which provides a channel for material transportation and forcing the solution from the gap of the concave arc of the baffle.
  • the solid material and the extraction liquid are in agitation and mixing contact, and the two phases are fully contacted in a turbulent state, which further improves the infiltration effect of the material and the solution; the solid and liquid are in turbulent contact under stirring, and the liquid phase is in turbulent contact.
  • Multiple baffles make the solvent flow in an S-shaped upward and downward directions in each immersion tank, preventing short circuit of the solvent, significantly increasing the extraction power and high extraction efficiency.
  • the discharging end of the spiral shaft of each soaking trough is equipped with a hollow large sprocket
  • the lower end of the lifting drive chain of the corresponding scraper lifting mechanism is engaged with the hollow large sprocket
  • the lifting drive chain is evenly provided Multiple lifting scrapers.
  • Part of the material can enter the discharge end of the soaking tank through the hollow of the large hollow sprocket, so that the receiving area of the lifting scraper is enlarged and the conveying capacity of the lifting scraper is increased.
  • the soaking tank spiral and the scraper lifting mechanism rotate synchronously.
  • the lifting scraper picks up and lifts the pushed material from the solution, and then falls into the next soaking tank.
  • the conveying capacity of the lifting scraper is greater than the soaking tank spiral, which can ensure that it does not cause blockage. material.
  • each lifting drive chain is meshed with the small lifting sprocket, each small lifting sprocket is respectively installed on the drive shaft, and each drive shaft is also respectively installed with a linkage sprocket, two adjacent drive
  • the shaft is a group and the two linkage sprockets are connected by a linkage chain; the shaft end of one of the drive shafts is equipped with a lifting sprocket, and the lifting sprocket is connected to the main sprocket of the drive reducer through the main chain.
  • the main sprocket of the drive reducer drives the large sprocket to rotate through the main chain, and the large sprocket drives the small sprocket and the linkage sprocket through the drive shaft to rotate, and the linkage chain drives the other drive shaft and the small sprocket to rotate synchronously ,
  • the two small hoisting sprockets drive the hoisting scraper and the spiral rotation of the soaking trough through the hoisting drive chain respectively to realize a drive reducer that drives the two soaking trough spirals to push the solid materials to the left and right at the same time.
  • Two scraper hoisting mechanisms simultaneously catch, drain and lift solid materials.
  • each spiral bearing seat is fixed in the center of the circular sealing plate, and each circular sealing plate covers and is fixed in the immersion tank.
  • the outside of the screw mounting holes at both ends. Remove the circular sealing plate and the spiral bearing seat to extract the immersion tank spiral from the screw mounting hole.
  • each immersion tank spiral includes a spiral shaft and a main spiral piece wound around the outer circumference of the spiral shaft.
  • a filter cartridge is installed at the feed end of the spiral shaft below the solid material inlet of the extractor, and the filter cartridge faces the main The port on one side of the spiral piece is closed and the other side is open.
  • the concentrate outlet of the extractor is inserted into the inner cavity of the filter cartridge.
  • a plurality of grate bars extending in the axial direction are evenly distributed on the circumference of the filter cartridge , The gap between adjacent grate bars is narrow outside and wide inside.
  • the powder is trapped on the outer surface of the filter cartridge to reduce the content of powdery solids in the concentrated extract as much as possible to provide guarantee for the subsequent hydrocyclone separation and evaporation; the concentration of solid-liquid mixed media
  • the extract After the extract is continuously and stably filtered out, it enters the concentrated liquid outlet of the extractor and flows out.
  • the filtered concentrated extract can be stably and continuously filtered out and transported without clogging the outlet pipe valve, so that it can enter the hydrocyclone separation system for precision. filter.
  • the powder Once the powder passes through the outermost gap of the filter cartridge, it can smoothly fall into the bottom of the filter cartridge and be pushed out by the spiral belt in the filter cartridge to self-clean; prevent powder particles from getting stuck in the gap between adjacent grate bars and affect the filtering capacity.
  • the outer circumference of the filter cartridge is wrapped with a filter cartridge outer spiral belt, and the rotation direction of the filter cartridge outer spiral belt is the same as the coaxial main spiral; the inner wall of the filter cartridge is provided with a filter cartridge The inner spiral belt, the spiral direction of the inner spiral belt in the filter cartridge is opposite to the coaxial main spiral piece.
  • the outer spiral belt of the filter cartridge can push the solid materials flowing with the liquid to the side where the main spiral is located, avoiding excessive material accumulation outside the filter cartridge. A small amount of solid powder will enter the filter cartridge with the extraction liquid and settle on the lower part of the inner wall of the filter cartridge.
  • the spiral belt in the filter cartridge that rotates in the opposite direction of the main spiral will push the sediment out of the filter cartridge from the open end, and then be outside the filter cartridge.
  • the spiral belt pushes out the filter section to complete the self-cleaning process of the filter cartridge. In this way, stable and reliable continuous filtration is realized, the process of the soybean protein concentrate preparation system is complete, the problem of separation of high-powder material and liquid is solved, and the soybean protein concentrate preparation system has a wide range of adaptability to various oils.
  • Figure 1 is the first flow chart of the soybean protein concentrate preparation system of the present invention.
  • FIG. 2 is the second flow chart of the soybean protein concentrate preparation system of the present invention.
  • Figure 3 is a front view of the first embodiment of the powder extractor of the present invention.
  • Fig. 4 is a cross-sectional view along A-A in Fig. 3.
  • Fig. 5 is a sectional view taken along B-B in Fig. 3.
  • Fig. 6 is a cross-sectional view along C-C in Fig. 3.
  • Figure 7 is a schematic diagram of Figure 3 with the front wall panel removed.
  • Fig. 8 is a perspective view of Fig. 3.
  • Fig. 9 is a perspective view of the box body of the powder extractor in Fig. 3 with the top cover removed.
  • Fig. 10 is a perspective view of two adjacent soaking tanks in Fig. 3.
  • Fig. 11 is a perspective view of the leftmost soaking tank in Fig. 3.
  • Fig. 12 is a perspective view of the filter cartridge in Fig. 11.
  • Figure 13 is a partial enlarged view of the filter cartridge.
  • Figure 14 is a schematic diagram of the working state of the second embodiment of the powder extractor of the present invention.
  • Fig. 15 is a top view of Fig. 14.
  • Extractor wet meal outlet 1c. Spiral mounting hole; 1d. Round sealing plate; 1e. Vent hole; 2. Tank partition; 2a. Overflow port; 2b. Guide Feed trough; 2c. Discharge trough; 3. Baffle plate; 3a. Concave arc on the baffle plate; 4. Soaking groove spiral; 4a. Spiral shaft; 4b. Main spiral; 4c. Hollow out large sprocket; 4d. Screw bearing seat; 4e. Right push screw; 4f. Left push screw; 5. Scraper lifting mechanism; 5a. Lifting drive chain; 5b. Lifting scraper; 6. Lifting small sprocket; 7. Drive shaft; 8. Linkage Sprocket; 9. Linkage chain; 10. Lifting large sprocket; 11.
  • the terms “upper”, “lower”, “front”, “rear”, “left”, “right”, “inner”, “outer”, etc. indicate the orientation or positional relationship based on the attached
  • the orientation or position relationship shown in the figure is only for the convenience of describing the present invention and simplifying the description, and does not mean that the device must have a specific orientation.
  • the soybean protein concentrate preparation system of the present invention includes a raw material temporary storage warehouse E3, a quantitative auger E4, a powder extractor E5 and a wet meal conveyor E6, and the exit of the raw material temporary storage warehouse E3 is connected to
  • the inlet of the quantitative auger E4 is connected, the outlet of the quantitative auger E4 is connected to the solid material inlet of the extractor, the wet meal outlet of the extractor is connected to the inlet of the wet meal conveyor E6, and the outlet of the wet meal conveyor E6 is connected to the double screw squeezer.
  • the feed port of E12 is connected, the liquid phase outlet of the double screw squeezer E12 is connected to the inlet of the squeezing liquid transfer pump B4, and the outlet of the squeezing liquid transfer pump B4 is also connected to the concentrated extract inlet E11a of the extract evaporation recovery system E11 Connected; the ethanol condensate outlet E11b of the extract evaporation recovery system E11 is connected to the ethanol condensate output pipe G5, and the ethanol condensate output pipe G5 is connected to the extract replenishment pipe G6 and then connected to the fresh solvent pipe G1.
  • the discharge port of the double screw squeezing dryer E12 is connected to the feed port of the horizontal disc dryer E13, and the discharge port of the horizontal disc dryer E13 is connected to the inlet of the hot meal scraper conveyor E14.
  • the outlet of the plate conveyor E14 is connected to the inlet of the distribution auger E15, and the outlet of the distribution auger E15 is connected to the inlet of each vertical disc dryer E16, and the outlet of each vertical disc dryer E16 is respectively Connected to the inlet of Shakelong E17 through the protein air supply pipe G7, the exhaust port of Shakelong E17 is connected to the inlet of the induced draft fan E18, and the bottom of the Shakelong E17 is installed with a rotary discharge valve E17a; horizontal round
  • the gas-phase discharge ports of the disk dryer E13 and the vertical disk dryer E16 are respectively connected to the reuse heat medium inlet E11e of the extraction liquid evaporation recovery system E11 through the reuse heat medium pipe G8.
  • the inlet of the new solvent pump B1 is connected to the fresh solvent pipe G1
  • the outlet of the new solvent pump B1 is connected to the fresh dissolving inlet 15 of the extractor
  • the concentrated liquid outlet 16 of the extractor is connected to the inlet of the concentrated extract extraction pump B2
  • the concentrated extract extraction pump The outlet of B2 is connected to the inlet of the first hydrocyclone E7 through the mixed liquid delivery pipe G2
  • the light phase outlet of the first hydrocyclone E7 is connected to the inlet of the second hydrocyclone E8, the second hydrocyclone
  • the light phase outlet of E8 is connected to the inlet of the solution temporary storage tank E9
  • the bottom outlets of the first-level hydrocyclone E7, the second-level hydrocyclone E8 and the solution temporary storage tank E9 are all connected to the return port of the powder extractor E5 .
  • the white soybean flakes or low-denaturation soybean meal are raised to the high position by the bucket elevator E1, they are sent to the raw material temporary storage warehouse E3 by the horizontal conveyor E2E2 for storage, and enter the quantitative auger E4 from the raw material temporary storage warehouse E3, and the quantitative auger E4
  • the white soybean flakes are directly sent to the solid material inlet of the extractor of powder extractor E5, and the "one-pot stew" extraction is adopted in the powder extractor E5, and the extracted wet-based concentrated protein is discharged from the wet meal outlet of the extractor. It is sent out by the wet meal conveyor E6.
  • the wet-based concentrated protein sent by the wet meal conveyor E6 enters the double screw squeezer E12 for mechanical extrusion and desolventization.
  • the separated concentrated extract is sent to the concentrated extract of the extract evaporation recovery system E11 by the squeeze liquid transfer pump B4
  • the squeeze liquid transfer pump B4 At the inlet E11a, evaporation is carried out in the extract evaporation recovery system E11, the concentrated oligosaccharide slurry obtained by evaporation is discharged from the concentrated oligosaccharide slurry outlet E11c, and the 60-65% (wt) ethanol condensate obtained by evaporation is discharged from the ethanol condensate outlet E11b.
  • enter the ethanol condensate output pipe G5 mix with 95% (wt) ethanol from the extraction solution supplement pipe G6 into 70% (wt) ethanol, and enter the fresh solvent pipe G1 for recycling.
  • the new solvent pump B1 sends the new solvent into the new dissolving inlet 15 of the extractor, and the white soybean flakes or low-denaturation soybean meal contact the solvent in the powder extractor E5 to complete the extraction.
  • a fresh solvent flow meter Q1 is installed on the outlet pipe of the new solvent pump B1.
  • the outlet of the solution temporary storage tank E9 is connected to the inlet of the temporary storage tank transfer pump B3 through the temporary storage tank output pipe G4, and the outlet of the temporary storage tank transfer pump B3 passes through
  • the concentrated solution flow meter Q2 and the temporary storage tank output pipe G4 are connected to the extraction liquid evaporation recovery system E11, and the outlet of the temporary storage tank transfer pump B3 is also connected to the return port of the solution temporary storage tank E9 through the temporary storage tank return pipe G3.
  • the concentrated solution after precipitation is discharged from the outlet of the solution temporary storage tank E9 through the temporary storage tank output pipe G4, and the temporary storage tank transfer pump B3 sends it to the first-stage evaporator.
  • the temporary storage tank transfer pump B3 The outlet solution can also be returned to the solution temporary storage tank E9 through the temporary storage tank return pipe G3.
  • the fresh solvent flow meter Q1 can monitor the flow of the fresh solvent
  • the concentrated solution flow meter Q2 can monitor the flow of the output concentrated solution.
  • the concentrated solution containing certain powder particles is drawn by the concentrated extract liquid extraction pump B2, it is sent to the first-stage hydrocyclone E7 through the mixed liquid delivery pipe G2 for separation.
  • the solid particles in the solution are removed for the first time, and then separated by the second-stage hydrocyclone.
  • the separated solid particles will flow into the soaking tank of the powder extractor E5 and can enter the second soaking tank from the left to reduce the concentration of the extractor. Particle concentration at outlet 16.
  • the concentrated solution after precipitation is sent from the outlet of the solution temporary storage tank E9 via the temporary storage tank transfer pump to the concentrated extract inlet E11a of the extract evaporation recovery system E11.
  • the wet-based protein after being extruded and desolvated by the double screw squeezer E12 first enters the horizontal disc dryer E13 for pre-drying. After the pre-drying, the moisture content of the protein decreases, the temperature rises, and the material becomes divergent.
  • the meal scraper conveyor E14 is sent to the entrance of the distribution auger E15, and the distribution auger E15 distributes the hot meal into each vertical disc dryer E16 for drying to obtain concentrated protein particles with a moisture content of less than 7%, which are sent by the protein air
  • the pipeline G7 is sent to the Shakelong E17 for centrifugal separation, and after being discharged from the rotary discharge valve E17a at the bottom of the Shakelong E17, it enters the crushing section and is crushed to obtain 95% powdery protein concentrate with 100 meshes.
  • the thin syrup of the concentrated extract in the solution temporary storage tank E9 enters the extract evaporation recovery system E11 for concentration.
  • the extract evaporation recovery system E11 includes a preheater, a first evaporator, a second evaporator, and a third evaporator.
  • the preheater performs preheating.
  • the preheater uses the secondary steam produced by the horizontal disc dryer E13 and the vertical disc dryer E16 as the heat source.
  • the preheated thin syrup enters the first evaporator.
  • the evaporator uses 10bar saturated raw steam entering from the raw steam inlet E11d as the heat source.
  • the first evaporator is micro-negative pressure evaporation, and the evaporated second steam is used as the heat source of the second steam.
  • the second steam is the negative pressure evaporation, and the thin syrup passes through the first steam.
  • the third steam is negative pressure evaporation, using the secondary steam of the horizontal disc dryer E13 and the vertical disc dryer E16 as the heat source to realize the waste heat
  • the system uses; the syrup after three steaming is discharged from the concentrated oligosaccharide slurry outlet E11c, enters the syrup temporary storage tank, and then quantitatively enters the thin film evaporator for concentration, and finally forms a concentrated syrup with a concentration of ⁇ 55%.
  • the powder extractor E5 includes a rectangular box.
  • the top of the box is provided with an exhaust hole 1e and a manhole.
  • the exhaust hole 1e and the exhaust port of the solution temporary storage tank E9 are all connected with the exhaust gas.
  • the condenser E10 is connected, and the exhaust steam outlet E11f of the extraction liquid evaporation recovery system E11 is also connected with the tail gas condenser E10, and the ethanol gas is condensed and recovered for recycling.
  • a number of parallel tank partitions 2 are connected between the front and rear wall panels of the box. Each tank partition 2 divides the inner cavity of the tank into a plurality of soaking tanks 1.
  • each tank partition 2 is respectively provided Overflow port 2a, the overflow ports 2a on the adjacent tank partitions 2 are staggered in the front and rear direction, and the height of each overflow port 2a gradually decreases from right to left, and the discharge end of the rightmost soaking tank is connected with
  • the fresh dissolving inlet 15 of the extractor the feed end of the leftmost soaking tank is connected with the extractor concentrate outlet 16;
  • the leftmost soaking tank is provided with a solid material inlet 1a of the extractor above the feed end of the soaking tank, and each tank is divided
  • the discharge ends of 2 are respectively provided with a guide groove 2b for lifting and turning to the right, and the discharge end of the right wall panel of the box body is equipped with a discharge groove 2c extending upward and right.
  • each soaking tank 1 is arc-shaped and is respectively installed with soaking tank spirals 4, the spirals 4 of adjacent soaking tanks are rotated in opposite directions, starting from the solid material inlet 1a of the solid material extractor, the odd-numbered tank is the left push screw 4f, Push the solid material toward the front side wall of the powder extractor; in the even-numbered grooves, the right push screw 4e pushes the solid material toward the back side wall of the powder extractor.
  • a scraper lifting mechanism 5 is installed in each guide groove 2b, and a scraper discharging mechanism 14 is installed in the discharging groove 2c.
  • the material enters the feed end of the leftmost soaking tank from the solid material inlet 1a of the extractor, and the new solvent enters the rightmost soaking tank.
  • the soaking and extraction process is completed in the soaking tank 1.
  • the material is pushed by the soaking tank spiral 4 to the discharge end of each soaking tank 1, it is lifted up by the scraper lifting mechanism 5 along the guide tank 2b. Drain and drop into the lower soaking tank on the right.
  • the advancing direction of the materials in adjacent soaking tanks is opposite, so that the solid materials move forward in an S-shaped zigzag.
  • the solid material When the solid material enters the final soaking tank, it is fully immersed and mixed with the new solution, and is taken out from the discharge end of the rightmost soaking tank along the discharge tank 2c by the scraper discharge mechanism 14 and from the wet meal outlet 1b of the extractor Exhaust from the machine.
  • the solid material and the solution always keep reverse flow, the material with the highest content is in contact with the concentrated solution, and the material with the lower content is in contact with the dilute solution, which can always maintain a good osmotic pressure, which further improves the mass transfer efficiency.
  • the solid material alternately advances horizontally along the immersion tank 1, and after a period of horizontal advancement, it is taken out and dropped into the next vertical immersion tank. It is repeatedly stirred.
  • the material and the solution are in a turbulent state, and there will be no laminar flow, even if the porosity is very high. Small powders can also be fully saturated by the solution.
  • the adjacent overflow ports 2a are staggered in the front and rear directions, and the solvent also flows in an S-shaped zigzag direction opposite to the forward direction of the solid material, flows through the full length of each immersion tank 1, and then uses the offset overflow to enter the next immersion tank and turn back
  • the full length of the soaking tank is extended to greatly extend the extraction stroke of the solid material and the solution, and can achieve full extraction, thereby achieving efficient extraction.
  • the concentrated extraction liquid reaching the leftmost soaking tank is discharged from the concentrated liquid outlet 16 of the extractor.
  • the soaking liquid level is slightly higher than the solid phase, the solid-liquid mixing is sufficient, the solvent consumption is low, the obtained mixed liquid concentration is high, and the evaporation and separation energy consumption is low.
  • the bottom of the soaking tank 1 is arc-shaped and coincides with the soaking tank spiral 4, which can avoid the dead zone at the bottom of the tank; the soaking tank spiral 4 is responsible for the transportation of solid materials in the soaking tank 1 and completes the soaking and extraction.
  • the forced stirring of the spiral blade avoids In the simple soaking process, the material and the solvent are insufficiently transferred.
  • the spiral 4 of the adjacent soaking tank rotates in opposite directions so that the material advances in an S shape.
  • the scraper lifting mechanism 5 is used to lift, drain, and transport the soaked solid materials for solid-liquid separation and solid phase lifting; the scraper discharge mechanism 14 is used to lift and drain the solid materials after extraction. Dry and drain.
  • the spiral scraper not only plays the role of conveying solid materials, but also can strongly stir solid materials.
  • each soaking tank 1 is provided with at least one baffle 3 extending in the left-right direction, and the lower end of each baffle 3 is clamped above the spiral of the soaking tank through the concave arc 3a of the baffle.
  • the baffle 3 can prevent the surface solution from flowing out in a short-circuit if it is not in full contact with the solid material.
  • the concave arc 3a of the baffle is stuck on the top of the spiral 4 of the soaking tank to provide a channel for material transportation and forcing the solution to sink from the baffle.
  • the solid material and the extraction liquid Passing through the gap of arc 3a, the solid material and the extraction liquid are in agitation and mixing contact, and the two phases are fully contacted in turbulent state, which further improves the infiltration effect of the material and the solution; the solid and liquid are in turbulent contact under the action of stirring, and the liquid phase is in turbulent contact, the same
  • the phase density is consistent.
  • the multiple baffles 3 make the solvent flow in an S-shaped upward and downward directions in each immersion tank 1 to prevent the short circuit of the solvent, the extraction power is significantly increased, and the extraction efficiency is high.
  • the discharge end of the screw shaft of each immersion tank spiral 4 is respectively equipped with a hollow large sprocket 4c, and the lower end of the lifting drive chain 5a of the corresponding scraper lifting mechanism 5 engages with the hollow large sprocket 4c to lift the drive chain
  • a plurality of lifting scrapers 5b are uniformly provided on 5a. Part of the material can enter the discharge end of the soaking tank through the hollow of the hollow large sprocket 4c, so that the material receiving area of the lifting scraper 5b is enlarged, and the conveying capacity of the lifting scraper 5b is increased.
  • the soaking tank spiral 4 rotates synchronously with the scraper lifting mechanism 5.
  • the lifting scraper 5b picks up and lifts the pushed material from the solution and drops it into the next soaking tank.
  • the conveying capacity of the lifting scraper 5b is greater than that of the soaking tank spiral 4. It can ensure that there is no blockage.
  • each lifting drive chain 5a is meshed with the small lifting sprocket 6.
  • Each small lifting sprocket 6 is respectively installed on the drive shaft 7, and each drive shaft 7 is also equipped with a linkage sprocket 8 respectively.
  • Two adjacent drive shafts 7 is a group and two linkage sprockets 8 are connected by linkage chain 9; one of the drive shafts 7 is equipped with a lifting sprocket 10 at the shaft end, and the lifting sprocket 10 passes through the main chain 11 and the main drive of the reducer 12
  • the sprocket 12a is connected in transmission.
  • the main sprocket 12a of the drive reducer 12 drives the large lifting sprocket 10 to rotate through the main chain 11, the large lifting sprocket 10 drives the small lifting sprocket 6 and the linkage sprocket 8 to rotate through the drive shaft 7, and the linkage chain 9 drives the other
  • the drive shaft 7 and the small lifting sprocket 6 rotate synchronously.
  • the two small lifting sprockets 6 respectively drive the lifting scraper 5b through the lifting drive chain 5a and the rotation of the soaking trough spiral 4 to realize a drive reducer 12 to drive two at the same time
  • the soaking tank screw 4 pushes the solid materials to the left and right, and simultaneously drives the two scraper lifting mechanisms 5 to synchronously scoop, drain and lift the solid materials.
  • each screw bearing housing 4d is respectively fixed in the center of the circular sealing plate 1d, and each circular sealing plate 1d is covered and fixed to the two immersion tanks.
  • the outer side of the screw mounting hole 1c Remove the circular sealing plate 1d and the spiral bearing seat 4d to extract the immersion tank spiral 4 from the screw mounting hole 1c.
  • the lower end of the discharging drive chain 14a of the scraper discharging mechanism 14 is engaged with the hollow large sprocket 4c, and a plurality of discharging scrapers 14b are evenly provided on the discharging drive chain 14a.
  • Part of the material can enter the discharge end of the rightmost soaking tank through the hollow of the large hollow sprocket 4c, so that the receiving area of the discharge scraper 14b is enlarged, and the conveying capacity of the discharge scraper 14b is improved.
  • the soaking tank spiral 4 rotates synchronously with the scraper discharging mechanism 14.
  • the discharging scraper 14b picks up the pushed material from the solution, lifts and discharges the powder extractor.
  • the conveying capacity of the discharging scraper 14b is greater than that of the soaking tank spiral 4. It can ensure that there is no blockage.
  • each immersion tank spiral 4 includes a spiral shaft 4a and a main spiral piece 4b wound around the outer circumference of the spiral shaft.
  • the feed end of the leftmost spiral shaft below the solid material inlet 1a of the extractor is installed with Filter cartridge 13, the port on one side of the filter cartridge 13 facing the main spiral piece 4b is closed and the other side is open, the extractor concentrate outlet 16 is inserted into the inner cavity of the filter cartridge 13, and there are multiple evenly distributed on the circumference of the filter cartridge 13
  • the gap between the adjacent grate bars 13a is narrow outside and wide inside.
  • the powder is trapped on the outer surface of the filter cartridge 13, reducing the powdery solid content in the concentrated extract as much as possible, providing guarantee for the subsequent hydrocyclone separation and evaporation; solid-liquid mixed media
  • the concentrated extract After the concentrated extract is continuously and stably filtered out, it enters the concentrated liquid outlet 16 of the extractor and flows out.
  • the filtered concentrated extract can be stably and continuously filtered out and transported without causing blockage of the outlet pipe valve to facilitate the separation of the liquid
  • the system performs fine filtration.
  • the powder Once the powder passes through the outermost gap of the filter cartridge 13, it can smoothly fall into the bottom of the filter cartridge 13 and be pushed out by the spiral belt 13c in the filter cartridge to self-clean; avoid the powder particles from getting stuck in the gap between adjacent grate bars 13a, Affect filtration capacity.
  • the outer circumference of the filter cartridge 13 is wound with a filter cartridge outer spiral belt 13b, and the rotation direction of the filter cartridge outer spiral belt 13b is the same as the coaxial main spiral piece 4b.
  • the outer spiral belt 13b of the filter cartridge can push the solid material flowing with the liquid to the side where the main spiral piece 4b is located, so as to avoid excessive accumulation of material outside the filter cartridge 13.
  • the inner wall of the filter cartridge 13 is provided with a filter cartridge inner spiral belt 13c, and the spiral direction of the filter cartridge inner spiral belt 13c is opposite to the coaxial main spiral piece 4b.
  • a small amount of solid powder will enter the filter cartridge 13 with the extract and settle on the lower part of the inner wall of the filter cartridge 13.
  • the spiral belt 13c in the filter cartridge which rotates opposite to the main spiral 4b, pushes the sediment out of the filter cartridge 13 from the open end. Then the filter cartridge is pushed out of the filter section by the outer spiral belt 13b of the filter cartridge, thereby completing the self-cleaning process of the filter cartridge 13.
  • stable and reliable continuous filtration is realized, the process of the soybean protein concentrate preparation system is complete, the problem of separation of high-powder material and liquid is solved, and the soybean protein concentrate preparation system has a wide range of adaptability to various oils.
  • the solid material inlet 1a of the extractor can be located at the left part of the top cover of the box, and a feed diversion tube 1a1 is connected below the solid material inlet 1a of the extractor to divert the new solid material to the filter cartridge. 13 front side.
  • the solid material inlet 1a of the extractor can also be provided on the upper part of the left side wall of the box body, and the position in the front-rear direction is also located on the front side of the filter cartridge 13.
  • the immersion tank on the far right has the highest level and overflows to the left one by one.
  • the big arrow in Figure 15 is the direction of the solid material, and the small arrow is the flow direction of the solution, which flows in the reverse direction.
  • the invention adopts "one-pot stew” type leaching, which is efficient and reliable, and can be used for leaching powdery materials and high-powder materials. It can solve the bottleneck in the preparation of soy protein concentrate and cottonseed protein concentrate, overcome the problems of poor material permeability, easy dissolution of protein and sugar and blocking the grid, shallow leaching material, large equipment investment, low production efficiency, and high system failure rate. For powdery leftovers that cannot be processed in the traditional extraction process, such as high-powder white soybean flakes and semi-denatured puffed powder, the soybean protein concentrate preparation system of the present invention can be used to extract and process such materials into concentrated Protein can greatly increase the economic value of such materials, and enhance the economic efficiency and market competitiveness of enterprises.

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Abstract

一种大豆浓缩蛋白制取***，包括原料暂存仓（E3）、定量绞龙（E4）、粉料浸出器（E5）、湿粕输送机（E6）等部件，其中原料暂存仓（E3）的出口经定量绞龙（E4）与浸出器（E5）固料入口相连，浸出器湿粕出口与湿粕输送机（E6）的入口相连，新溶剂泵（B1）的入口与新鲜溶剂管（G1）相连，新溶剂泵（B1）的出口与浸出器新溶进口相连，浸出器浓液出口与浓萃液抽出泵（B2）的入口相连，浓萃液抽出泵（B2）的出口通过混合液输送管（G2）与一级旋液分离器（E7）的入口相连，一级旋液分离器（E7）的轻相出口与二级旋液分离器（E8）的入口相连，二级旋液分离器（E8）的轻相出口与溶液暂存罐（E9）的入口相连，一级、二级旋液分离器及溶液暂存罐的底部与粉料浸出器的回流口相连；溶液暂存罐的下部出口经暂存罐输送泵（B3）与萃取液蒸发回收***（E11）相连。该大豆浓缩蛋白制取***，设备投资省，粉末下脚料全部得以利用，大大提高经济效益。

Description

一种大豆浓缩蛋白制取*** 技术领域
本发明涉及一种萃取***，尤其涉及一种大豆浓缩蛋白制取***，可用于食品、环保及化工等行业的动态萃取，属于萃取设备技术领域。
背景技术
大豆浓缩蛋白原料为低变性膨化大豆粕或经低温脱溶的白豆片。制取工艺从日仓开始，日仓储存一天左右的原料，能保证浸出车间的稳定运行；物料首先由日仓出料变频刮板定量输出，经过提升机进入分级筛(20目)，筛上物进入计量秤进行计量，然后通过提升机及平刮板送到浸出车间暂存罐。浸出车间暂存罐起到料封和保证浸出供料稳定的作用，装有料位检测装置；暂存箱下变频喂料关风器，定量向预浸器喂料。在预浸器内原料与混合溶剂充分接触，完成膨胀的过程，使预浸豆粕在浸出器内具有良好的渗透性；经过预浸膨胀的原料进入浸出器，在浸出器内充分提取可溶性糖分及其他少量可溶物质，同时保证蛋白尽量少的溶出，从而实现原料蛋白含量提高的过程，变成湿基浓缩蛋白。
现有的大豆浓缩蛋白制取***存在如下缺陷：1.原料利用率低导致经济效益下降。大豆浓缩蛋白原料经多道工序加工和输送、提升，部分原料不可避免的由片状、颗粒状成为粉末，经筛分后筛下物(过20目筛或30目筛)为粉状白豆片或粉状低变性膨化豆粕，占原料总量的8-10％，此部分物料须单独存放。其中，粉状白豆片只可加工大豆分离蛋白，如建有相关分离蛋白生产线，尚可保值使用。若没有相关生产线，只能***，严重影响经济效益。若原料为低变性膨化豆粕，则此部分高蛋白夹生豆粕只能掺入高温粕生产线，经熟化后方可作为动物饲料，经济价值低。
2.必须设置有筛分工序：因为原浸出器不能处理高粉末度原料，只能处理片状或颗粒状物料。
3.必须设置预浸泡工序：原料在浸出前须预浸泡，让蛋白组织吸水后充分膨胀，使湿料比干料体积增大约15-20％，否则原料吸湿后膨胀板结，完全不渗透。
4.须配备尺寸超大的浸出器：吸饱水和乙醇的原料强度差，形成料层后在自重压力下空隙率低，渗透性差。为保证料层的渗透性，只有降低料层厚度，通常将料层厚度控制在350mm(常规大豆浸出料层在1000-2800mm)，导致醇洗浸出器尺寸巨大，但产能很低，加上萃取时间长，同样尺寸的浸出器产能只有常规浸出的十分之一。导致浸出器投资巨大，相关生产车间、土建、钢结构以及占地面积都非常大。
5.现有浸出器是固体自然堆积成稳定料床或强制形成稳定料床，萃取液或洗涤液从料床上方淋入，液体渗透料层完成传质过程。对固体物料的粒度有要求，固体物料应为散装或片状，堆积后颗粒间有一定间隙，以利于萃取液或洗涤液渗透。当固体物料中粉末度过大，导致料床空隙率不足，渗透速率会下降或不渗透。
6.浸出器需配有多级溶剂循环泵和栅板反冲洗***：溶剂循环喷淋***通常不低于12级循环泵，运行电耗大、泵阀泄漏点多。大豆浓缩蛋白制取***萃取得到的浓萃取液中含有很多粉料颗粒，流入后续管道会导致出液管阀堵塞，必须利用滤网或栅板进行过滤。过滤网或栅板堵塞会导致萃取或洗涤过程的效果下降或不可持续，须经常清理维护；栅板反冲洗***结构复杂，封闭在***性溶剂环境(充满乙醇蒸汽)中，且多发故障，影响化工单元连续运行。
7.现有的浸出器在工作过程中，大部分固体物料与萃取液之间的接触为层流式接触，与萃取液混合不充分；萃取液通过落差自流，轻相位于液层上部，新溶易发生短路，导致萃取动力不足，萃取效率低下；萃取路径貌似较长，但每组浸出单元上层筛面利用率很低。浸出器为细长状，车间长度依据设备长度定，对场地要求高，且为专门非标设计，提产或改造升级困难。
发明内容
本发明的目的在于，克服现有技术中存在的问题，提供一种大豆浓缩蛋白制取***，可省略筛分、预浸设备、溶剂循环喷淋和栅板反冲洗***，粉末下脚料全部得以利用，大大提高经济效益。
为解决以上技术问题，本发明的一种大豆浓缩蛋白制取***，包括原料暂存仓、定量绞龙、粉料浸出器和湿粕输送机，原料暂存仓的出口与定量绞龙的入口相连，定量绞龙的出口与浸出器固料入口相连，浸出器湿粕出口与湿粕输送机的入口相连，新溶剂泵的入口与新鲜溶剂管相连，新溶剂泵的出口与浸出器新溶进口相连，浸出器浓液出口与浓萃液抽出泵的入口相连，浓萃液抽出泵的出口通过混合液输送管与一级旋液分离器的入口相连，一级旋液分离器的轻相出口与二级旋液分离器的入口相连，二级旋液分离器的轻相出口与溶液暂存罐的入口相连，一级旋液分离器、二级旋液分离器及溶液暂存罐的底部出口均与粉料浸出器的回流口相连；所述溶液暂存罐的下部出口与暂存罐输送泵的入口相连，所述暂存罐输送泵的出口与萃取液蒸发回收***的浓萃取液入口相连。
相对于现有技术，本发明取得了以下有益效果：白豆片或低变性豆粕从原料暂存仓进入定量绞龙，定量绞龙将白豆片直接送入粉料浸出器的浸出器固料入口，在粉料浸出 器中采用“一锅炖”式萃取，萃取后的湿基浓缩蛋白从浸出器湿粕出口排出，由湿粕输送机送出。新溶剂泵将新溶剂送入浸出器新溶进口，含有一定粉末颗粒的浓溶液被浓萃液抽出泵抽出后，通过混合液输送管送往一级旋液分离器进行分离，初次去除溶液中的固体颗粒，再经二级旋液分离器再次去除溶液中的固体颗粒后，进入溶液暂存罐储存，分离出来的固体颗粒流会浸出器的浸泡槽，经过沉淀后的浓溶液从溶液暂存罐的出口经暂存罐输送泵将其送往萃取液蒸发回收***的浓萃取液入口。本***省略了筛分和预浸工序，节省了筛分、存储、预浸设备的投资和安装场地，省去了复杂繁琐的溶剂循环喷淋***和栅板反冲洗***，设备密闭性好，消除了跑冒滴漏等安全隐患，运行费用低。大大提高原料利用率，将原90％的原料利用率提高到100％，扣除糖分质量损失和加工成本，其经济价值每吨可提升1800-2000元，同时消除了额外的存储、转运费用。提高粉料利用率可极大提高浓缩蛋白企业盈利水平。可以将浸出***标准化，投资省、建厂快，扩容方便快捷，有望突破大豆浓缩蛋白的发展瓶颈，实现行业大发展。
作为本发明的改进，所述暂存罐输送泵的出口还通过暂存罐回流管与所述溶液暂存罐的回流口相连，所述湿粕输送机的出口与双螺旋挤干机的进料口相连，所述双螺旋挤干机的液相出口与挤干液输送泵的入口相连，挤干液输送泵的出口也与萃取液蒸发回收***的浓萃取液入口相连；萃取液蒸发回收***的乙醇冷凝液出口与乙醇冷凝液输出管相连，乙醇冷凝液输出管与萃取液补充管相连后与所述新鲜溶剂管相连。在***运行初期，暂存罐输送泵的出口溶液还可以通过暂存罐回流管回到溶液暂存罐。湿粕输送机送出的湿基浓缩蛋白进入双螺旋挤干机进行机械挤压脱溶，分离出来的浓萃取液由挤干液输送泵送入萃取液蒸发回收***的浓萃取液入口，在萃取液蒸发回收***进行蒸发，蒸发得到的浓缩低聚糖浆从浓缩低聚糖浆出口排出，蒸发得到的60-65％(wt)乙醇冷凝液从乙醇冷凝液出口排出，并进入乙醇冷凝液输出管，与来自萃取液补充管的95％(wt)乙醇混合成70％(wt)乙醇，进入新鲜溶剂管循环利用。
作为本发明的进一步改进，所述双螺旋挤干机的出料口与卧式圆盘干燥机的进料口相连，卧式圆盘干燥机的出料口与热粕刮板输送机的入口相连，热粕刮板输送机的出口与分配绞龙的入口相连，分配绞龙的出口分别与各立式圆盘干燥机的进料口相连，各立式圆盘干燥机的出料口分别通过蛋白风送管道与沙克龙的进料口相连，沙克龙的排风口与引风机的入口相连，沙克龙的底部安装有旋转出料阀；卧式圆盘干燥机与立式圆盘干燥机的气相排放口分别通过回用热媒管与萃取液蒸发回收***的回用热媒入口相连。经双螺旋挤干机挤压脱溶后的湿基蛋白先进入卧式圆盘干燥机进行预干燥，预干燥后的蛋白含湿量降 低，温度升高，物料变得发散，由热粕刮板输送机送入分配绞龙的入口，分配绞龙将热粕分配进入各立式圆盘干燥机进行干燥，得到水分含量小于7％的浓缩蛋白颗粒，通过蛋白风送管道送入沙克龙离心分离，从沙克龙底部的旋转出料阀排出后，进入粉碎工段粉碎，得到100目过95％的粉状浓缩蛋白。溶液暂存罐中浓萃取液的稀糖浆进入萃取液蒸发回收***浓缩，萃取液蒸发回收***包括预热器、第一蒸发器、第二蒸发器和第三蒸发器，稀糖浆先预热器进行预热，预热器采用卧式圆盘干燥机与立式圆盘干燥机产生的二次蒸汽作为热源，经过预热后的稀糖浆在进入第一蒸发器，第一蒸发器采用生蒸汽作为热源，第一蒸发器为微负压蒸发，蒸发的二次蒸汽作为二蒸的热源，二蒸为负压蒸发，稀糖浆经过一蒸后进入二蒸，进行负压蒸发；然后进入第三蒸发器，三蒸为负压蒸发，采用卧式圆盘干燥机与立式圆盘干燥机的二次蒸汽作为热源，实现余热的本***利用；经过三蒸后的糖浆从浓缩低聚糖浆出口排出，进入糖浆暂存罐，然后定量进入薄膜蒸发器进行浓缩，最终形成浓度≥55％的浓糖浆。
作为本发明的进一步改进，所述粉料浸出器包括长方形箱体，箱体的前后墙板之间连接有多道相互平行的槽体隔板，各槽体隔板将箱体内腔分隔成多个浸泡槽，各槽体隔板的上部分别设有溢流口，相邻槽体隔板上的溢流口在前后方向交错设置，且各溢流口的高度自右向左逐渐降低，最右侧浸泡槽的出料端连接有浸出器新溶进口，最左侧浸泡槽的进料端连接有浸出器浓液出口；所述浸出器固料入口位于最左侧浸泡槽的进料端上方，每个槽体隔板的出料端分别设有向右侧提升翻料的导料槽，箱体右墙板的出料端安装有向右上延伸的出料槽，所述浸出器湿粕出口位于所述出料槽的上端；各浸泡槽的底部呈弧形且分别安装有浸泡槽螺旋，相邻浸泡槽螺旋的旋向相反；各所述导料槽中分别安装有刮板提升机构，所述出料槽中安装有刮板出料机构。物料从浸出器固料入口落入最左侧浸泡槽的进料端，新溶剂泵将新溶剂送入浸出器新溶进口，进入最右侧的浸泡槽。浸泡萃取过程在浸泡槽中完成，物料被推行至各浸泡槽的出料端时，沿导料槽被向上捞出，脱离液面后，经短促沥干，落入右侧的下级浸泡槽。相邻浸泡槽中物料的前进方向相反，使得固体物料呈S形曲折前进。当固体料进入末级浸泡槽时，与新溶充分浸泡混合后，从最右侧浸泡槽的出料端沿出料槽被捞出并从浸出器湿粕出口排出，再经湿粕输送机送出。固体料与溶液始终保持逆向流动，含量最高的物料与浓溶液接触，含量较低的物料与稀溶液接触，始终能保持很好的渗透压，进一步提高了传质效率。固体料交替沿浸泡槽横向前进，横向前进一段后被捞出落入纵向的下一级浸泡槽，反复得到搅拌，物料及溶液均呈湍流状态，不会出现层流状态，即使空隙率很小的粉料也能被溶液充分浸透。相邻溢流口在前后方向交 错设置，溶剂也呈S形曲折流动且与固体料前进方向相反，流经各浸泡槽的全长，然后利用位差溢流进入下个浸泡槽并折返流经该浸泡槽的全长，大大延长了固体料与溶液的萃取行程，可实现充分萃取，从而实现高效萃取。到达最左侧浸泡槽的浓萃取液从浸出器浓液出口排出。浸泡液面略高于固相，固液混合充分，溶剂消耗少，得到的混合液浓度高，蒸发分离能耗少。浸泡槽的底部呈弧形与浸泡槽螺旋相吻合，可避免槽底出现死区；浸泡槽螺旋负责浸泡槽中固体物料的输送并且完成浸泡萃取，通过螺旋叶片的强制搅拌，避免简单浸泡过程中物料和溶剂传质不充分的缺陷，相邻浸泡槽螺旋的旋向相反使物料呈S形前进。刮板提升机构用于将浸泡后的固体物料捞起、沥干和提升输送，用于固液分离和固相提升；刮板出料机构用于将萃取完成的固体物料捞起、沥干和排出。螺旋加刮板不仅起到输送固体料的作用，还可以对固体料进行强力搅拌，浸泡箱内物料料层高度可达到800mm，比之传统350mm料层，单位面积上产能提高50-80％；将萃取液自上至下自然渗透，改为螺旋机械搅拌，固液直混浸洗，萃取动力大，萃取效率高；传统浸出***参与循环的溶剂量为固体物料的5倍，本发明中固液容积比约为1.2-1.5倍，初始投溶量只有原来的四分之一至三分之一，大大节省大量溶剂和资金占用。
作为本发明的进一步改进，各浸泡槽中分别设有至少一道沿左右方向延伸的折流板，各折流板的下端分别通过折流板上凹弧卡在浸泡槽螺旋的上方。折流板可以防止表层溶液未与固体物料充分接触即短路流出，折流板上凹弧卡在浸泡槽螺旋的上方，为物料输送和提供通道，且强制溶液从折流板上凹弧的缺口中通过，固体物料与萃取液间为搅拌混合接触，两相间湍流状态充分接触，进一步提高物料与溶液的浸润效果；固液在搅拌作用下湍流接触，液相无层析，相同相位浓度一致。多道折流板使溶剂在各浸泡槽内作上下方向的S形流动，杜绝出现溶剂短路现象，萃取动力明显加大，萃取效率高。
作为本发明的进一步改进，各浸泡槽螺旋的螺旋轴出料端分别安装有镂空大链轮，相应刮板提升机构的提升驱动链条下端啮合在镂空大链轮上，提升驱动链条上均匀设有多个提升刮板。部分物料可经镂空大链轮的镂空处进入浸泡槽出料端，使提升刮板的受料面积加大，增大提升刮板的输送能力。浸泡槽螺旋与刮板提升机构同步旋转，提升刮板将推送过来的物料从溶液中捞起、提升，落入下一浸泡槽，提升刮板的输送能力大于浸泡槽螺旋，可确保不造成堵料。
作为本发明的进一步改进，各提升驱动链条的上端啮合在提升小链轮上，各提升小链轮分别安装在驱动轴上，各驱动轴上还分别安装有联动链轮，相邻两根驱动轴为一组且两联动链轮通过联动链条传动连接；其中一根驱动轴的轴端安装有提升大链轮，所述提 升大链轮通过主链条与驱动减速机的主链轮传动连接。驱动减速机的主链轮通过主链条带动提升大链轮转动，提升大链轮通过驱动轴带动提升小链轮和联动链轮转动，联动链条带动另一根驱动轴及提升小链轮同步转动，两提升小链轮分别通过提升驱动链条驱动提升刮板运行及浸泡槽螺旋的转动，实现了一台驱动减速机同时驱动两根浸泡槽螺旋将固体物料向左和向右推送，且同时驱动两台刮板提升机构同步捞料、沥干和提升固体物料。
作为本发明的进一步改进，各浸泡槽螺旋的螺旋轴两端分别支撑在螺旋轴承座中，各螺旋轴承座分别固定在圆形封板的中心，各圆形封板分别覆盖且固定在浸泡槽两端螺旋安装孔的外侧。拆掉圆形封板及螺旋轴承座即可将浸泡槽螺旋整体从螺旋安装孔中抽出，安装时先将浸泡槽螺旋从螺旋安装孔中穿入，然后覆盖上圆形封板并通过螺栓固定，再安装上螺旋轴承座并固定。
作为本发明的进一步改进，各浸泡槽螺旋包括螺旋轴及缠绕在螺旋轴外周的主螺旋片，位于浸出器固料入口下方的螺旋轴的进料端安装有滤筒，所述滤筒面向主螺旋片一侧的端口封闭且另一侧敞口，所述浸出器浓液出口***于所述滤筒的内腔，所述滤筒的圆周上均匀分布有多根沿轴向延伸的篦条，相邻篦条之间的缝隙外窄内宽。在流出之前经过滤筒的过滤，粉料被截留在滤筒的外表面，尽可能降低浓萃取液中粉状固体含量，为后续旋液分离和蒸发提供保障；固液互混介质中的浓萃取液被连续稳定滤出后，进入浸出器浓液出口流出，过滤后的浓萃取液可稳定连续滤出、输送，不会造成出液管阀的堵塞，以便于进入旋液分离***进行精滤。粉料一旦越过滤筒最外侧的缝隙，即可顺利落入滤筒底部，被滤筒内螺带推出自清；避免粉料颗粒卡在相邻篦条之间的缝隙中，影响过滤能力。
作为本发明的进一步改进，所述滤筒的外周缠绕有滤筒外螺带，所述滤筒外螺带的旋向与同轴的主螺旋片相同；所述滤筒的内壁设有滤筒内螺带，所述滤筒内螺带的旋向与同轴的主螺旋片相反。滤筒外螺带可将随液体流淌过来的固体物料向主螺旋片所在一侧推送出去，避免滤筒外淤积过多的物料。少量固体粉末会随萃取液进入滤筒内，沉降在滤筒内壁的下部，与主螺旋片旋向相反的滤筒内螺带将沉降物从敞口端推送出滤筒，再被滤筒外螺带推送出过滤段，从而完成滤筒的自清过程。从而实现稳定可靠的连续过滤，使大豆浓缩蛋白制取***工艺完备，解决了高粉末度物料与液体分离的难题，使大豆浓缩蛋白制取***对各种油料具有广泛的适应性。
附图说明
下面结合附图和具体实施方式对本发明作进一步详细的说明，附图仅提供参考与说明用，非用以限制本发明。
图1为本发明大豆浓缩蛋白制取***的流程图一。
图2为本发明大豆浓缩蛋白制取***的流程图二。
图3为本发明中粉料浸出器实施例一的主视图。
图4为图3中沿A-A的剖视图。
图5为图3中沿B-B的剖视图。
图6为图3中沿C-C的剖视图。
图7为图3去掉前墙板后的示意图。
图8为图3的立体图。
图9为图3中粉料浸出器箱体去掉顶盖后的立体图。
图10为图3中相邻两个浸泡槽的立体图。
图11为图3中最左侧浸泡槽的立体图。
图12为图11中滤筒的立体图。
图13为滤筒的局部放大图。
图14为本发明中粉料浸出器实施例二的工作状态示意图。
图15为图14的俯视图。
图中：E1.斗式提升机；E2.水平输送机；E3.原料暂存仓；E4.定量绞龙；E5.粉料浸出器；E6.湿粕输送机；E7.一级旋液分离器；E8.二级旋液分离器；E9.溶液暂存罐；E10.尾气冷凝器；E11.萃取液蒸发回收***；E11a.浓萃取液入口；E11b.乙醇冷凝液出口；E11c.浓缩低聚糖浆出口；E11d.生蒸汽入口；E11e.回用热媒入口；E11f.乏汽出口；E12.双螺旋挤干机；E13.卧式圆盘干燥机；E14.热粕刮板输送机；E15.分配绞龙；E16.立式圆盘干燥机；E17.沙克龙；E17a.旋转出料阀；E18.引风机；B1.新溶剂泵；B2.浓萃液抽出泵；B3.暂存罐输送泵；B4.挤干液输送泵；G1.新鲜溶剂管；G2.混合液输送管；G3.暂存罐回流管；G4.暂存罐输出管；G5.乙醇冷凝液输出管；G6.萃取液补充管；G7.蛋白风送管道；G8.回用热媒管；Q1.新鲜溶剂流量计；Q2.浓溶液流量计；1.浸泡槽；1a.浸出器固料入口；1a1.进料导流管；1b.浸出器湿粕出口；1c.螺旋安装孔；1d.圆形封板；1e.排气孔；2.槽体隔板；2a.溢流口；2b.导料槽；2c.出料槽；3.折流板；3a.折流板上凹弧；4.浸泡槽螺旋；4a.螺旋轴；4b.主螺旋片；4c.镂空大链轮；4d.螺旋轴承座；4e.右推螺旋；4f.左推螺旋；5.刮板提升机构；5a.提升驱动链条；5b.提升刮板；6.提升小链轮；7.驱动轴；8.联动链轮；9.联动链条；10.提升大链轮；11.主链条；12.驱动减速机；12a.主链轮；13.滤筒；13a.篦条；13b.滤筒外螺带；13c.滤筒内螺带；14.刮板出料机构；14a.出料驱动链条；14b.出料刮板；15. 浸出器新溶进口；16.浸出器浓液出口。
具体实施方式
在本发明的以下描述中，术语“上”、“下”、“前”、“后”、“左”、“右”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指装置必须具有特定的方位。
如图1、图2所示，本发明的大豆浓缩蛋白制取***包括原料暂存仓E3、定量绞龙E4、粉料浸出器E5和湿粕输送机E6，原料暂存仓E3的出口与定量绞龙E4的入口相连，定量绞龙E4的出口与浸出器固料入口相连，浸出器湿粕出口与湿粕输送机E6的入口相连，湿粕输送机E6的出口与双螺旋挤干机E12的进料口相连，双螺旋挤干机E12的液相出口与挤干液输送泵B4的入口相连，挤干液输送泵B4的出口也与萃取液蒸发回收***E11的浓萃取液入口E11a相连；萃取液蒸发回收***E11的乙醇冷凝液出口E11b与乙醇冷凝液输出管G5相连，乙醇冷凝液输出管G5与萃取液补充管G6相连后与新鲜溶剂管G1相连。
双螺旋挤干机E12的出料口与卧式圆盘干燥机E13的进料口相连，卧式圆盘干燥机E13的出料口与热粕刮板输送机E14的入口相连，热粕刮板输送机E14的出口与分配绞龙E15的入口相连，分配绞龙E15的出口分别与各立式圆盘干燥机E16的进料口相连，各立式圆盘干燥机E16的出料口分别通过蛋白风送管道G7与沙克龙E17的进料口相连，沙克龙E17的排风口与引风机E18的入口相连，沙克龙E17的底部安装有旋转出料阀E17a；卧式圆盘干燥机E13与立式圆盘干燥机E16的气相排放口分别通过回用热媒管G8与萃取液蒸发回收***E11的回用热媒入口E11e相连。
新溶剂泵B1的入口与新鲜溶剂管G1相连，新溶剂泵B1的出口与浸出器新溶进口15相连，浸出器浓液出口16与浓萃液抽出泵B2的入口相连，浓萃液抽出泵B2的出口通过混合液输送管G2与一级旋液分离器E7的入口相连，一级旋液分离器E7的轻相出口与二级旋液分离器E8的入口相连，二级旋液分离器E8的轻相出口与溶液暂存罐E9的入口相连，一级旋液分离器E7、二级旋液分离器E8及溶液暂存罐E9的底部出口均与粉料浸出器E5的回流口相连。
白豆片或低变性豆粕由斗式提升机E1提升至高位后，再由水平输送机E2E2送入原料暂存仓E3中储存，从原料暂存仓E3进入定量绞龙E4，定量绞龙E4将白豆片直接送入粉料浸出器E5的浸出器固料入口，在粉料浸出器E5中采用“一锅炖”式萃取，萃取后的湿基浓缩蛋白从浸出器湿粕出口排出，由湿粕输送机E6送出。
湿粕输送机E6送出的湿基浓缩蛋白进入双螺旋挤干机E12进行机械挤压脱溶，分离出来的浓萃取液由挤干液输送泵B4送入萃取液蒸发回收***E11的浓萃取液入口E11a，在萃取液蒸发回收***E11进行蒸发，蒸发得到的浓缩低聚糖浆从浓缩低聚糖浆出口E11c排出，蒸发得到的60-65％(wt)乙醇冷凝液从乙醇冷凝液出口E11b排出，并进入乙醇冷凝液输出管G5，与来自萃取液补充管G6的95％(wt)乙醇混合成70％(wt)乙醇，进入新鲜溶剂管G1循环利用。
新溶剂泵B1将新溶剂送入浸出器新溶进口15，白豆片或低变性豆粕在粉料浸出器E5中与溶剂接触，完成萃取。新溶剂泵B1的出口管道上安装有新鲜溶剂流量计Q1，溶液暂存罐E9的出口通过暂存罐输出管G4与暂存罐输送泵B3的入口相连，暂存罐输送泵B3的出口通过浓溶液流量计Q2及暂存罐输出管G4与萃取液蒸发回收***E11相连，暂存罐输送泵B3的出口还通过暂存罐回流管G3与溶液暂存罐E9的回流口相连。经过沉淀后的浓溶液从溶液暂存罐E9的出口经过暂存罐输出管G4排出，暂存罐输送泵B3将其送往一级蒸发器，在***运行初期，暂存罐输送泵B3的出口溶液还可以通过暂存罐回流管G3回到溶液暂存罐E9。新鲜溶剂流量计Q1可以监控新鲜溶剂的流量，浓溶液流量计Q2可以监控输出浓溶液的流量。
含有一定粉末颗粒的浓溶液被浓萃液抽出泵B2抽出后，通过混合液输送管G2送往一级旋液分离器E7进行分离，初次去除溶液中的固体颗粒，再经二级旋液分离器E8再次去除溶液中的固体颗粒后，进入溶液暂存罐E9储存，分离出来的固体颗粒流会粉料浸出器E5的浸泡槽，可以进入左起第二道浸泡槽，减少浸出器浓液出口16处的颗粒浓度。经过沉淀后的浓溶液从溶液暂存罐E9的出口经暂存罐输送泵将其送往萃取液蒸发回收***E11的浓萃取液入口E11a。
经双螺旋挤干机E12挤压脱溶后的湿基蛋白先进入卧式圆盘干燥机E13进行预干燥，预干燥后的蛋白含湿量降低，温度升高，物料变得发散，由热粕刮板输送机E14送入分配绞龙E15的入口，分配绞龙E15将热粕分配进入各立式圆盘干燥机E16进行干燥，得到水分含量小于7％的浓缩蛋白颗粒，通过蛋白风送管道G7送入沙克龙E17离心分离，从沙克龙E17底部的旋转出料阀E17a排出后，进入粉碎工段粉碎，得到100目过95％的粉状浓缩蛋白。溶液暂存罐E9中浓萃取液的稀糖浆进入萃取液蒸发回收***E11浓缩，萃取液蒸发回收***E11包括预热器、第一蒸发器、第二蒸发器和第三蒸发器，稀糖浆先预热器进行预热，预热器采用卧式圆盘干燥机E13与立式圆盘干燥机E16产生的二次蒸汽作为热源，经过预热后的稀糖浆在进入第一蒸发器，第一蒸发器采用从生蒸汽入口 E11d进入的10bar饱和生蒸汽作为热源，第一蒸发器为微负压蒸发，蒸发的二次蒸汽作为二蒸的热源，二蒸为负压蒸发，稀糖浆经过一蒸后进入二蒸，进行负压蒸发；然后进入第三蒸发器，三蒸为负压蒸发，采用卧式圆盘干燥机E13与立式圆盘干燥机E16的二次蒸汽作为热源，实现余热的本***利用；经过三蒸后的糖浆从浓缩低聚糖浆出口E11c排出，进入糖浆暂存罐，然后定量进入薄膜蒸发器进行浓缩，最终形成浓度≥55％的浓糖浆。
如图1至图15所示，粉料浸出器E5包括长方形的箱体，箱体顶部设有排气孔1e和人孔，排气孔1e和溶液暂存罐E9的排气口均与尾气冷凝器E10相连，萃取液蒸发回收***E11的乏汽出口E11f也与尾气冷凝器E10相连，乙醇气体冷凝回收后循环利用。箱体的前后墙板之间连接有多道相互平行的槽体隔板2，各槽体隔板2将箱体内腔分隔成多个浸泡槽1，各槽体隔板2的上部分别设有溢流口2a，相邻槽体隔板2上的溢流口2a在前后方向交错设置，且各溢流口2a的高度自右向左逐渐降低，最右侧浸泡槽的出料端连接有浸出器新溶进口15，最左侧浸泡槽的进料端连接有浸出器浓液出口16；最左侧浸泡槽的进料端上方设有浸出器固料入口1a，每个槽体隔板2的出料端分别设有向右侧提升翻料的导料槽2b，箱体右墙板的出料端安装有向右上延伸的出料槽2c。
各浸泡槽1的底部呈弧形且分别安装有浸泡槽螺旋4，相邻浸泡槽螺旋4的旋向相反，从固体料的浸出器固料入口1a起，奇数槽中为左推螺旋4f，将固体料向粉料浸出器的前侧壁方向推进；偶数槽中为右推螺旋4e，将固体料向粉料浸出器的后侧壁方向推进。各导料槽2b中分别安装有刮板提升机构5，出料槽2c中安装有刮板出料机构14。
物料从浸出器固料入口1a进入最左侧浸泡槽的进料端，新溶剂进入最右侧的浸泡槽。浸泡萃取过程在浸泡槽1中完成，物料被浸泡槽螺旋4推行至各浸泡槽1的出料端时，沿导料槽2b被刮板提升机构5向上捞出，脱离液面后，经短促沥干，落入右侧的下级浸泡槽。相邻浸泡槽中物料的前进方向相反，使得固体物料呈S形曲折前进。当固体料进入末级浸泡槽时，与新溶充分浸泡混合后，从最右侧浸泡槽的出料端沿出料槽2c被刮板出料机构14捞出并从浸出器湿粕出口1b排出机外。固体料与溶液始终保持逆向流动，含量最高的物料与浓溶液接触，含量较低的物料与稀溶液接触，始终能保持很好的渗透压，进一步提高了传质效率。固体料交替沿浸泡槽1横向前进，横向前进一段后被捞出落入纵向的下一级浸泡槽，反复得到搅拌，物料及溶液均呈湍流状态，不会出现层流状态，即使空隙率很小的粉料也能被溶液充分浸透。相邻溢流口2a在前后方向交错设置，溶剂也呈S形曲折流动且与固体料前进方向相反，流经各浸泡槽1的全长，然后利用位差溢流进入下个浸泡槽并折返流经该浸泡槽的全长，大大延长了固体料与溶液的萃取行程，可实现充 分萃取，从而实现高效萃取。到达最左侧浸泡槽的浓萃取液从浸出器浓液出口16排出。浸泡液面略高于固相，固液混合充分，溶剂消耗少，得到的混合液浓度高，蒸发分离能耗少。
浸泡槽1的底部呈弧形与浸泡槽螺旋4相吻合，可避免槽底出现死区；浸泡槽螺旋4负责浸泡槽1中固体物料的输送并且完成浸泡萃取，通过螺旋叶片的强制搅拌，避免简单浸泡过程中物料和溶剂传质不充分的缺陷，相邻浸泡槽螺旋4的旋向相反使物料呈S形前进。刮板提升机构5用于将浸泡后的固体物料捞起、沥干和提升输送，用于固液分离和固相提升；刮板出料机构14用于将萃取完成的固体物料捞起、沥干和排出。螺旋加刮板不仅起到输送固体料的作用，还可以对固体料进行强力搅拌。
如图9所示，各浸泡槽1中分别设有至少一道沿左右方向延伸的折流板3，各折流板3的下端分别通过折流板上凹弧3a卡在浸泡槽螺旋的上方。折流板3可以防止表层溶液未与固体物料充分接触即短路流出，折流板上凹弧3a卡在浸泡槽螺旋4的上方，为物料输送和提供通道，且强制溶液从折流板上凹弧3a的缺口中通过，固体物料与萃取液间为搅拌混合接触，两相间湍流状态充分接触，进一步提高物料与溶液的浸润效果；固液在搅拌作用下湍流接触，液相无层析，相同相位浓度一致。多道折流板3使溶剂在各浸泡槽1内作上下方向的S形流动，杜绝出现溶剂短路现象，萃取动力明显加大，萃取效率高。
如图10所示，各浸泡槽螺旋4的螺旋轴出料端分别安装有镂空大链轮4c，相应刮板提升机构5的提升驱动链条5a下端啮合在镂空大链轮4c上，提升驱动链条5a上均匀设有多个提升刮板5b。部分物料可经镂空大链轮4c的镂空处进入浸泡槽出料端，使提升刮板5b的受料面积加大，增大提升刮板5b的输送能力。浸泡槽螺旋4与刮板提升机构5同步旋转，提升刮板5b将推送过来的物料从溶液中捞起、提升，落入下一浸泡槽，提升刮板5b的输送能力大于浸泡槽螺旋4，可确保不造成堵料。
各提升驱动链条5a的上端啮合在提升小链轮6上，各提升小链轮6分别安装在驱动轴7上，各驱动轴7上还分别安装有联动链轮8，相邻两根驱动轴7为一组且两联动链轮8通过联动链条9传动连接；其中一根驱动轴7的轴端安装有提升大链轮10，提升大链轮10通过主链条11与驱动减速机12的主链轮12a传动连接。驱动减速机12的主链轮12a通过主链条11带动提升大链轮10转动，提升大链轮10通过驱动轴7带动提升小链轮6和联动链轮8转动，联动链条9带动另一根驱动轴7及提升小链轮6同步转动，两提升小链轮6分别通过提升驱动链条5a驱动提升刮板5b运行及浸泡槽螺旋4的转动，实现了一台驱动减速机12同时驱动两根浸泡槽螺旋4将固体物料向左和向右推送，且同时驱 动两台刮板提升机构5同步捞料、沥干和提升固体物料。
各浸泡槽螺旋4的螺旋轴4a两端分别支撑在螺旋轴承座4d中，各螺旋轴承座4d分别固定在圆形封板1d的中心，各圆形封板1d分别覆盖且固定在浸泡槽两端螺旋安装孔1c的外侧。拆掉圆形封板1d及螺旋轴承座4d即可将浸泡槽螺旋4整体从螺旋安装孔1c中抽出，安装时先将浸泡槽螺旋4从螺旋安装孔1c中穿入，然后覆盖上圆形封板1d并通过螺栓固定，再安装上螺旋轴承座4d并固定。
刮板出料机构14的出料驱动链条14a下端啮合在镂空大链轮4c上，出料驱动链条14a上均匀设有多个出料刮板14b。部分物料可经镂空大链轮4c的镂空处进入最右侧浸泡槽的出料端，使出料刮板14b的受料面积加大，提升出料刮板14b的输送能力。浸泡槽螺旋4与刮板出料机构14同步旋转，出料刮板14b将推送过来的物料从溶液中捞起、提升并排出粉料浸出器，出料刮板14b的输送能力大于浸泡槽螺旋4，可确保不造成堵料。
如图11至图13所示，各浸泡槽螺旋4包括螺旋轴4a及缠绕在螺旋轴外周的主螺旋片4b，位于浸出器固料入口1a下方的最左侧螺旋轴的进料端安装有滤筒13，滤筒13面向主螺旋片4b一侧的端口封闭且另一侧敞口，浸出器浓液出口16***于滤筒13的内腔，滤筒13的圆周上均匀分布有多根沿轴向延伸的篦条13a，相邻篦条13a之间的缝隙外窄内宽。在流出之前经过滤筒13的过滤，粉料被截留在滤筒13的外表面，尽可能降低浓萃取液中粉状固体含量，为后续旋液分离和蒸发提供保障；固液互混介质中的浓萃取液被连续稳定滤出后，进入浸出器浓液出口16流出，过滤后的浓萃取液可稳定连续滤出、输送，不会造成出液管阀的堵塞，以便于进入旋液分离***进行精滤。粉料一旦越过滤筒13最外侧的缝隙，即可顺利落入滤筒13底部，被滤筒内螺带13c推出自清；避免粉料颗粒卡在相邻篦条13a之间的缝隙中，影响过滤能力。
滤筒13的外周缠绕有滤筒外螺带13b，滤筒外螺带13b的旋向与同轴的主螺旋片4b相同。滤筒外螺带13b可将随液体流淌过来的固体物料向主螺旋片4b所在一侧推送出去，避免滤筒13外淤积过多的物料。
滤筒13的内壁设有滤筒内螺带13c，滤筒内螺带13c的旋向与同轴的主螺旋片4b相反。少量固体粉末会随萃取液进入滤筒13内，沉降在滤筒13内壁的下部，与主螺旋片4b旋向相反的滤筒内螺带13c将沉降物从敞口端推送出滤筒13，再被滤筒外螺带13b推送出过滤段，从而完成滤筒13的自清过程。从而实现稳定可靠的连续过滤，使大豆浓缩蛋白制取***工艺完备，解决了高粉末度物料与液体分离的难题，使大豆浓缩蛋白制取***对各种油料具有广泛的适应性。
如图3及图8所示，浸出器固料入口1a可以设在箱体顶盖的左部，浸出器固料入口1a下方连接有进料导流管1a1将新固体料导流至滤筒13前侧。
如图14、图15所示，浸出器固料入口1a也可以设在箱体左侧壁的上部，在前后方向的位置也位于滤筒13前侧。最右侧的浸泡槽液位最高，依次向左侧溢流。图15中大箭头为固体料的走向，小箭头为溶液流向，全程逆向流动。
本发明采用“一锅炖”式的浸出，高效且可靠，可用于粉状物料和高粉末度物料的浸出。可以解决大豆浓缩蛋白、棉籽浓缩蛋白的制取瓶颈，克服物料渗透性差，蛋白、糖分易溶出堵塞栅板，浸出料层浅、设备投资大、生产效率低、***故障率高等问题。对于传统浸出工艺中无法处理的粉状下脚料，如高粉末度大豆白豆片、半变性膨化粉料，可以采用本发明的大豆浓缩蛋白制取***，将这类性状物料萃取后加工成浓缩蛋白，可大幅提升这类物料的经济价值，提升企业经济效益和市场竞争力。
以上所述仅为本发明之较佳可行实施例而已，非因此局限本发明的专利保护范围。除上述实施例外，本发明还可以有其他实施方式。凡采用等同替换或等效变换形成的技术方案，均落在本发明要求的保护范围内。本发明未经描述的技术特征可以通过或采用现有技术实现，在此不再赘述。

Claims (10)

  1. 一种大豆浓缩蛋白制取***，包括原料暂存仓、定量绞龙、粉料浸出器和湿粕输送机，原料暂存仓的出口与定量绞龙的入口相连，定量绞龙的出口与浸出器固料入口相连，浸出器湿粕出口与湿粕输送机的入口相连，新溶剂泵的入口与新鲜溶剂管相连，新溶剂泵的出口与浸出器新溶进口相连，浸出器浓液出口与浓萃液抽出泵的入口相连，其特征在于：浓萃液抽出泵的出口通过混合液输送管与一级旋液分离器的入口相连，一级旋液分离器的轻相出口与二级旋液分离器的入口相连，二级旋液分离器的轻相出口与溶液暂存罐的入口相连，一级旋液分离器、二级旋液分离器及溶液暂存罐的底部出口均与粉料浸出器的回流口相连；所述溶液暂存罐的下部出口与暂存罐输送泵的入口相连，所述暂存罐输送泵的出口与萃取液蒸发回收***的浓萃取液入口相连。
  2. 根据权利要求1所述的大豆浓缩蛋白制取***，其特征在于：所述暂存罐输送泵的出口还通过暂存罐回流管与所述溶液暂存罐的回流口相连，所述湿粕输送机的出口与双螺旋挤干机的进料口相连，所述双螺旋挤干机的液相出口与挤干液输送泵的入口相连，挤干液输送泵的出口也与萃取液蒸发回收***的浓萃取液入口相连；萃取液蒸发回收***的乙醇冷凝液出口与乙醇冷凝液输出管相连，乙醇冷凝液输出管与萃取液补充管相连后与所述新鲜溶剂管相连。
  3. 根据权利要求2所述的大豆浓缩蛋白制取***，其特征在于：所述双螺旋挤干机的出料口与卧式圆盘干燥机的进料口相连，卧式圆盘干燥机的出料口与热粕刮板输送机的入口相连，热粕刮板输送机的出口与分配绞龙的入口相连，分配绞龙的出口分别与各立式圆盘干燥机的进料口相连，各立式圆 盘干燥机的出料口分别通过蛋白风送管道与沙克龙的进料口相连，沙克龙的排风口与引风机的入口相连，沙克龙的底部安装有旋转出料阀；卧式圆盘干燥机与立式圆盘干燥机的气相排放口分别通过回用热媒管与萃取液蒸发回收***的回用热媒入口相连。
  4. 根据权利要求1所述的大豆浓缩蛋白制取***，其特征在于：所述粉料浸出器包括长方形箱体，箱体的前后墙板之间连接有多道相互平行的槽体隔板，各槽体隔板将箱体内腔分隔成多个浸泡槽，各槽体隔板的上部分别设有溢流口，相邻槽体隔板上的溢流口在前后方向交错设置，且各溢流口的高度自右向左逐渐降低，最右侧浸泡槽的出料端连接有浸出器新溶进口，最左侧浸泡槽的进料端连接有浸出器浓液出口；所述浸出器固料入口位于最左侧浸泡槽的进料端上方，每个槽体隔板的出料端分别设有向右侧提升翻料的导料槽，箱体右墙板的出料端安装有向右上延伸的出料槽，所述浸出器湿粕出口位于所述出料槽的上端；各浸泡槽的底部呈弧形且分别安装有浸泡槽螺旋，相邻浸泡槽螺旋的旋向相反；各所述导料槽中分别安装有刮板提升机构，所述出料槽中安装有刮板出料机构。
  5. 根据权利要求4所述的大豆浓缩蛋白制取***，其特征在于：各浸泡槽中分别设有至少一道沿左右方向延伸的折流板，各折流板的下端分别通过折流板上凹弧卡在浸泡槽螺旋的上方。
  6. 根据权利要求4所述的大豆浓缩蛋白制取***，其特征在于：各浸泡槽螺旋的螺旋轴出料端分别安装有镂空大链轮，相应刮板提升机构的提升驱动链条下端啮合在镂空大链轮上，提升驱动链条上均匀设有多个提升刮板。
  7. 根据权利要求6所述的大豆浓缩蛋白制取***，其特征在于：各提升驱动链条的上端啮合在提升小链轮上，各提升小链轮分别安装在驱动轴上， 各驱动轴上还分别安装有联动链轮，相邻两根驱动轴为一组且两联动链轮通过联动链条传动连接；其中一根驱动轴的轴端安装有提升大链轮，所述提升大链轮通过主链条与驱动减速机的主链轮传动连接。
  8. 根据权利要求4所述的大豆浓缩蛋白制取***，其特征在于：各浸泡槽螺旋的螺旋轴两端分别支撑在螺旋轴承座中，各螺旋轴承座分别固定在圆形封板的中心，各圆形封板分别覆盖且固定在浸泡槽两端螺旋安装孔的外侧。
  9. 根据权利要求4至8中任一项所述的大豆浓缩蛋白制取***，其特征在于：各浸泡槽螺旋包括螺旋轴及缠绕在螺旋轴外周的主螺旋片，位于浸出器固料入口下方的螺旋轴的进料端安装有滤筒，所述滤筒面向主螺旋片一侧的端口封闭且另一侧敞口，所述浸出器浓液出口***于所述滤筒的内腔，所述滤筒的圆周上均匀分布有多根沿轴向延伸的篦条，相邻篦条之间的缝隙外窄内宽。
  10. 根据权利要求9所述的大豆浓缩蛋白制取***，其特征在于：所述滤筒的外周缠绕有滤筒外螺带，所述滤筒外螺带的旋向与同轴的主螺旋片相同，所述滤筒的内壁设有滤筒内螺带，所述滤筒内螺带的旋向与同轴的主螺旋片相反。
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