CN209797825U - System is prepared to soybean protein concentrate - Google Patents

Abstract

The utility model relates to a system is prepared to soybean protein concentrate, the export in the raw materials temporary storage storehouse links to each other with the solid material entry of leacher through the ration auger, the export of leacher wet dregs of meal export links to each other with the entry of wet dregs of meal conveyer, the entry of new solvent pump links to each other with fresh solvent pipe, the export of new solvent pump links to each other with the new mouth that dissolves of leacher, the concentrated solution export of leacher links to each other with the entry of concentrated extract extraction pump, the export of concentrated extract extraction pump links to each other with the entry of one-level hydrocyclone through mixed liquid conveyer pipe, the light phase export of one-level hydrocyclone links to each other with the entry of second grade hydrocyclone, the light phase export of second grade hydrocyclone links to each other with the entry of solution temporary storage tank, the bottom of one-level hydrocyclone and solution temporary storage tank links to; the lower outlet of the solution temporary storage tank is connected with an extraction liquid evaporation and recovery system through a temporary storage tank delivery pump. The soybean protein concentrate preparation system has the advantages of saving equipment investment, fully utilizing powder leftovers and greatly improving economic benefit.

Description

System is prepared to soybean protein concentrate

Technical Field

The utility model relates to an extraction system especially relates to a system is prepared to soybean protein concentrate, can be used to the dynamic extraction of trades such as food, environmental protection and chemical industry, belongs to extraction equipment technical field.

Background

The soybean protein concentrate is low-denaturation puffed soybean meal or low-temperature desolventized soybean flakes. The preparation process starts from a daily warehouse, and the raw materials are stored in the daily warehouse for about one day, so that the stable operation of a leaching workshop can be ensured; the material is firstly quantitatively output by a daily bin discharging variable frequency scraper, enters a classifying screen (20 meshes) through a lifting machine, and oversize materials enter a metering scale for metering and then are conveyed to a temporary storage tank of a leaching workshop through the lifting machine and a flat scraper. The temporary storage tank of the leaching workshop plays a role in material sealing and ensuring the stability of leaching and feeding, and is provided with a material level detection device; and (4) a down-conversion feeding air seal machine of the temporary storage box quantitatively feeds materials to the pre-soaking device. The raw materials are fully contacted with the mixed solvent in the pre-soaking device to complete the swelling process, so that the pre-soaked bean pulp has good permeability in the leaching device; the presoaked and expanded raw materials enter an extractor, soluble sugar and other small amount of soluble substances are fully extracted from the extractor, and simultaneously, the protein is dissolved out as little as possible, so that the process of improving the protein content of the raw materials is realized, and the raw materials are changed into wet-based concentrated protein.

The prior soybean protein concentrate preparation system has the following defects: 1. the low utilization rate of raw materials leads to the reduction of economic benefits. The soybean protein concentrate raw material is processed, conveyed and lifted through a plurality of processes, part of the raw material is inevitably made into powder from flakes and granules, and after screening, undersize (passing through a 20-mesh sieve or a 30-mesh sieve) is powdery white bean flakes or powdery low-denaturation expanded bean pulp which accounts for 8-10% of the total amount of the raw material, and the part of the raw material needs to be stored separately. Wherein, the powdery white bean slices can only process soybean protein isolate, and can be used for value preservation if a related protein isolate production line is established. If no related production line exists, the product can be sold at low price, and the economic benefit is seriously influenced. If the raw material is low-denaturation expanded soybean meal, the high-protein intergrown soybean meal can only be mixed into a high-temperature meal production line, and can be used as animal feed after being aged, so that the economic value is low.

2. A screening process must be provided: because the original leacher can not process high-powder raw materials, only can process flaky or granular materials.

3. A pre-soaking process must be set: the raw materials are pre-soaked before leaching, so that the protein tissue is fully expanded after absorbing water, the volume of a wet material is increased by about 15-20% compared with that of a dry material, otherwise, the raw materials are expanded and hardened after absorbing water and are completely impermeable.

4. An oversized leacher must be provided: the raw materials which absorb water and ethanol are poor in strength, and the voidage is low and the permeability is poor under the self-weight pressure after a material layer is formed. To ensure the permeability of the bed, only the bed thickness was reduced, typically controlled at 350mm (1000-2800 mm for conventional soy leach), resulting in a large size alcohol-wash extractor, but with very low capacity, plus long extraction times, the same size extractor can only produce one tenth of the capacity of conventional leaching. Leading to huge investment of the leacher and very large related production workshops, civil engineering, steel structures and occupied areas.

5. The existing leacher is that solids are naturally accumulated into a stable material bed or a stable material bed is forcibly formed, extraction liquid or washing liquid is poured into the leacher from the upper part of the material bed, and liquid permeates the material layer to finish the mass transfer process. The granularity of the solid materials is required, the solid materials are in bulk or in a sheet shape, and certain gaps are formed among the stacked particles to facilitate the permeation of the extraction liquid or the washing liquid. When the powder level in the solid material is too high, resulting in insufficient bed voidage, the permeation rate may be reduced or not.

6. The leacher needs to be equipped with a multi-stage solvent circulation pump and a grid plate backwash system: the solvent circulating spraying system is usually not lower than a 12-stage circulating pump, the power consumption is high during operation, and the leakage points of a pump valve are more. The concentrated extract liquid extracted by the soybean protein concentrate preparation system contains a plurality of powder particles, and the thick extract liquid flows into a subsequent pipeline to cause the blockage of a liquid outlet pipe valve, so that the thick extract liquid needs to be filtered by a filter screen or a grid plate. The blockage of the filter screen or the grid plate can cause the effect of the extraction or washing process to be reduced or not continuous, and the filter screen or the grid plate needs to be cleaned and maintained frequently; the grid plate backwashing system is complex in structure, is sealed in an explosive solvent environment (full of ethanol steam), and has multiple faults, so that continuous operation of a chemical unit is influenced.

7. In the working process of the existing leacher, most of solid materials are in laminar flow contact with extraction liquid, and are not fully mixed with the extraction liquid; the extract liquid flows automatically through the fall, the light phase is positioned at the upper part of the liquid layer, and the short circuit is easy to occur in the new solution, so that the extraction power is insufficient, and the extraction efficiency is low; the extraction path appears to be longer, but the utilization of the upper screen surface of each group of leaching units is low. The leacher is long, the length of a workshop is determined according to the length of equipment, the requirement on the site is high, the leacher is specially designed in a non-standard way, and the yield is increased or the leacher is difficult to modify and upgrade.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to overcome the problem that exists among the prior art, provide a system is prepared to soybean protein concentrate, can omit screening, preimpregnation equipment, solvent circulation and spray and grid tray back flush system, the powder leftover bits and pieces are whole to be utilized, improves economic benefits greatly.

In order to solve the technical problems, the utility model relates to a soybean protein concentrate preparation system, which comprises a raw material temporary storage bin and a quantitative auger, the device comprises a powder leacher and a wet meal conveyor, wherein an outlet of a raw material temporary storage bin is connected with an inlet of a quantitative packing auger, an outlet of the quantitative packing auger is connected with a solid material inlet of the leacher, a wet meal outlet of the leacher is connected with an inlet of the wet meal conveyor, an inlet of a new solvent pump is connected with a fresh solvent pipe, an outlet of the new solvent pump is connected with a new dissolution inlet of the leacher, a concentrated solution outlet of the leacher is connected with an inlet of a concentrated solution extraction pump, an outlet of the concentrated solution extraction pump is connected with an inlet of a primary hydrocyclone separator through a mixed solution conveying pipe, a light phase outlet of the primary hydrocyclone separator is connected with an inlet of a secondary hydrocyclone separator, a light phase outlet of the secondary hydrocyclone separator is connected with an inlet of a solution temporary storage tank, and outlets at the bottoms of the primary hydrocyclone separator, the secondary hydrocyclone separator and the; the lower part export of solution jar of keeping in links to each other with the entry of keeping in jar delivery pump, the export of keeping in jar delivery pump links to each other with the concentrated extract liquid entry of extraction liquid evaporation recovery system.

Compared with the prior art, the utility model discloses following beneficial effect has been obtained: white bean flakes or low denatured bean pulp enter a quantitative auger from a raw material temporary storage bin, the quantitative auger directly sends the white bean flakes into a solid material inlet of an extractor of a powder extractor, one-pot stewing extraction is adopted in the powder extractor, and extracted wet-based concentrated protein is discharged from a wet pulp outlet of the extractor and is sent out by a wet pulp conveyor. The new solvent pump sends new solvent into the new import of dissolving of leacher, after the concentrated solution that contains certain powder particle is taken out by concentrated extract extraction pump, send to one-level hydrocyclone separation through mixed liquid conveyer pipe and separate, get rid of the solid particle in the solution for the first time, get into the solution and keep in storage after the solid particle in the solution is got rid of again through second grade hydrocyclone separation, the solid particle stream that separates can leach the soaking groove of ware, concentrated solution after the sediment is from the export of solution keep in storage tank through keeping in storage tank conveyer pump and send it to the concentrated extract entry of extraction liquid evaporation recovery system. The system omits screening and presoaking procedures, saves investment and installation sites of screening, storage and presoaking equipment, omits a complex and fussy solvent circulating spray system and a grid plate backwashing system, has good equipment tightness, eliminates potential safety hazards such as running, falling, dripping and leaking and the like, and has low operating cost. Greatly improves the utilization rate of raw materials, improves the utilization rate of the raw materials of 90 percent to 100 percent, deducts the mass loss of sugar and the processing cost, can improve the economic value by 1800 plus 2000 yuan per ton, and simultaneously eliminates the additional storage and transportation cost. The utilization rate of the powder is improved, and the profit level of the concentrated protein enterprises can be greatly improved. The method has the advantages of standardization of a leaching system, investment conservation, quick factory building, and convenient and quick capacity expansion, is expected to break through the development bottleneck of the soybean protein concentrate, and realizes the large development of the industry.

As an improvement of the utility model, the outlet of the temporary storage tank delivery pump is connected with the reflux port of the solution temporary storage tank through a temporary storage tank reflux pipe, the outlet of the wet meal conveyor is connected with the feed inlet of the double-screw wringing machine, the liquid phase outlet of the double-screw wringing machine is connected with the inlet of the wringing liquid delivery pump, and the outlet of the wringing liquid delivery pump is also connected with the concentrated extraction liquid inlet of the extraction liquid evaporation and recovery system; an ethanol condensate outlet of the extraction liquid evaporation and recovery system is connected with an ethanol condensate output pipe, and the ethanol condensate output pipe is connected with the extraction liquid replenishing pipe and then connected with the fresh solvent pipe. At the initial stage of system operation, the outlet solution of the temporary storage tank delivery pump can also return to the solution temporary storage tank through a temporary storage tank return pipe. And (2) enabling wet-based concentrated protein sent out by the wet meal conveyor to enter a double-screw extruding machine for mechanical extrusion desolventizing, conveying separated concentrated extract liquid into a concentrated extract liquid inlet of an extract liquid evaporation and recovery system by an extruding and drying liquid conveying pump, evaporating in the extract liquid evaporation and recovery system, discharging concentrated oligosaccharide syrup obtained by evaporation from a concentrated oligosaccharide syrup outlet, discharging 60-65% (wt) ethanol condensate obtained by evaporation from an ethanol condensate outlet, enabling the ethanol condensate to enter an ethanol condensate output pipe, mixing the ethanol condensate with 95% (wt) ethanol from an extract liquid supplementing pipe to form 70% (wt) ethanol, and enabling the ethanol to enter a fresh solvent pipe for recycling.

As a further improvement of the utility model, the discharge port of the double-helix squeezing dryer is connected with the feed inlet of the horizontal disc dryer, the discharge port of the horizontal disc dryer is connected with the inlet of the hot meal scraper conveyer, the outlet of the hot meal scraper conveyer is connected with the inlet of the distribution auger, the outlet of the distribution auger is respectively connected with the feed inlets of the vertical disc dryers, the discharge port of each vertical disc dryer is respectively connected with the feed inlet of the cyclone through a protein air conveying pipeline, the air outlet of the cyclone is connected with the inlet of the draught fan, and the bottom of the cyclone is provided with a rotary discharge valve; the gas phase discharge ports of the horizontal disc dryer and the vertical disc dryer are respectively connected with the recycling heat medium inlet of the extraction liquid evaporation and recovery system through recycling heat medium pipes. Wet base protein extruded and desolventized by a double-screw extruding dryer firstly enters a horizontal disc dryer for pre-drying, the moisture content of the pre-dried protein is reduced, the temperature is increased, the material becomes diffused, the hot meal is conveyed to an inlet of a distribution auger by a hot meal scraper conveyor, the distribution auger distributes the hot meal to enter each vertical disc dryer for drying to obtain concentrated protein particles with the moisture content of less than 7%, the concentrated protein particles are conveyed to a cyclone for centrifugal separation by a protein air conveying pipeline, and the concentrated protein particles are discharged from a rotary discharge valve at the bottom of the cyclone and then enter a crushing section for crushing to obtain 100-mesh 95% powdered concentrated protein. Dilute syrup of concentrated extract in the solution temporary storage tank enters an extract evaporation and recovery system for concentration, the extract evaporation and recovery system comprises a preheater, a first evaporator, a second evaporator and a third evaporator, the dilute syrup is preheated by the preheater, secondary steam generated by a horizontal disc dryer and a vertical disc dryer is used as a heat source for the preheater, the preheated dilute syrup enters the first evaporator, raw steam is used as the heat source for the first evaporator, the first evaporator is micro-negative pressure evaporation, the evaporated secondary steam is used as a heat source for second evaporation, the second evaporation is negative pressure evaporation, the dilute syrup enters the second evaporation after the first evaporation, and the negative pressure evaporation is carried out; then the waste heat enters a third evaporator, the third evaporation is negative pressure evaporation, and secondary steam of a horizontal disc dryer and a vertical disc dryer is used as a heat source to realize the utilization of the waste heat of the system; discharging the syrup subjected to the third steaming from a concentrated low-polymer syrup outlet, allowing the syrup to enter a syrup temporary storage tank, quantitatively allowing the syrup to enter a thin film evaporator for concentration, and finally forming concentrated syrup with the concentration of more than or equal to 55%.

As a further improvement of the utility model, the powder leaching device comprises a rectangular box body, a plurality of parallel groove body clapboards are connected between the front wall board and the rear wall board of the box body, each groove body clapboard divides the inner cavity of the box body into a plurality of leaching tanks, the upper parts of each groove body clapboard are respectively provided with an overflow port, the overflow ports on the adjacent groove body clapboards are arranged in a staggered way in the front and rear direction, the height of each overflow port is gradually reduced from right to left, the discharge end of the right side leaching tank is connected with a leaching device new solution inlet, and the feed end of the left side leaching tank is connected with a leaching device concentrated solution outlet; the solid material inlet of the leacher is positioned above the feeding end of the leftmost soaking tank, the discharging end of each tank body partition plate is respectively provided with a guide chute for lifting and turning materials to the right side, the discharging end of the right wall plate of the tank body is provided with a discharging chute extending upwards and rightwards, and the wet meal outlet of the leacher is positioned at the upper end of the discharging chute; the bottom of each soaking groove is arc-shaped and is respectively provided with a soaking groove spiral, and the spiral directions of adjacent soaking grooves are opposite; and each guide chute is internally provided with a scraper lifting mechanism, and the discharge chute is internally provided with a scraper discharging mechanism. The material falls into the feed end of the leftmost soaking tank from the solid material inlet of the leacher, and the new solvent is sent into the new solvent inlet of the leacher by the new solvent pump and enters the rightmost soaking tank. The soaking and extracting processes are finished in the soaking tanks, and when the materials are pushed to the discharge ends of the soaking tanks, the materials are upwards fished out along the guide grooves, separated from the liquid level, and then drained by short drip to fall into the lower soaking tank on the right side. The advancing directions of the materials in the adjacent soaking tanks are opposite, so that the solid materials advance in an S-shaped zigzag manner. When the solid material enters the final stage soaking tank, the solid material is fully soaked and mixed with the new solution, and then the solid material is fished out from the discharge end of the rightmost soaking tank along the discharge tank, discharged from a wet meal outlet of the leacher and sent out by a wet meal conveyor. The solid material and the solution always keep reverse flow, the material with the highest content contacts with the concentrated solution, the material with the lower content contacts with the dilute solution, the good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid material transversely advances along soaking the groove in turn, transversely advances after a section and is fished out and fall into fore-and-aft next-level soaking groove, obtains the stirring repeatedly, and material and solution all are the torrent state, can not appear laminar flow state, even the very little powder of void fraction also can be fully soaked by solution. The adjacent overflow ports are arranged in a staggered manner in the front and back directions, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the full length of each soaking tank, then flows into the next soaking tank by using potential difference overflow and turns back to flow through the full length of the soaking tank, the extraction stroke of the solid material and the solution is greatly prolonged, full extraction can be realized, and high-efficiency extraction is realized. The concentrated extract reaching the leftmost leaching tank is discharged from the concentrated liquor outlet of the leacher. The soaking liquid level is slightly higher than the solid phase, the solid and the liquid are mixed fully, the solvent consumption is low, the concentration of the obtained mixed liquid is high, and the energy consumption of evaporation separation is low. The bottom of the soaking groove is arc-shaped and is matched with the spiral of the soaking groove, so that dead zones at the bottom of the soaking groove can be avoided; the spiral of the soaking tank is responsible for conveying solid materials in the soaking tank and completing soaking extraction, the defect of insufficient mass transfer of the materials and the solvent in the simple soaking process is overcome through forced stirring of the spiral blades, and the spiral direction of the adjacent soaking tanks is opposite to make the materials advance in an S shape. The scraper lifting mechanism is used for fishing, draining and lifting the soaked solid materials for solid-liquid separation and solid-phase lifting; the scraper plate discharging mechanism is used for scooping up, draining and discharging the extracted solid materials. The spiral scraper can not only transport solid materials, but also stir the solid materials with strong force, the height of the material layer in the soaking box can reach 800mm, and the productivity is improved by 50-80% in unit area compared with the traditional 350mm material layer; the extraction liquid naturally permeates from top to bottom, and is changed into spiral mechanical stirring, solid-liquid direct mixing immersion cleaning, the extraction power is large, and the extraction efficiency is high; the solvent amount that traditional leaching system participated in the circulation is 5 times of solid material, the utility model discloses well solid-liquid volume ratio is about 1.2-1.5 times, and initial throw solvent amount only has original quarter to third, saves a large amount of solvents greatly and the fund occupies.

As a further improvement of the utility model, at least one baffle plate extending along the left and right directions is respectively arranged in each soaking groove, and the lower end of each baffle plate is respectively clamped above the spiral of the soaking groove through the upper concave arc of the baffle plate. The baffle plate can prevent the short-circuit outflow of the surface solution without fully contacting with the solid material, the upper concave arc of the baffle plate is clamped above the spiral of the soaking tank to convey and provide a channel for the material, the solution is forced to pass through the notch of the upper concave arc of the baffle plate, the solid material and the extraction liquid are stirred, mixed and contacted, the two phases are fully contacted in a turbulent flow state, and the soaking effect of the material and the solution is further improved; the solid and the liquid are in turbulent contact under the stirring action, the liquid phase has no chromatography, and the concentrations of the same phases are consistent. The plurality of baffle plates enable the solvent to flow in an S shape in the vertical direction in each soaking tank, so that the short circuit phenomenon of the solvent is avoided, the extraction power is obviously increased, and the extraction efficiency is high.

As the utility model discloses a further improvement, the big sprocket of fretwork is installed respectively to the screw axis discharge end of each soaking groove spiral, and corresponding scraper blade hoist mechanism's promotion drive chain lower extreme meshing evenly is equipped with a plurality of promotion scraper blades on the promotion drive chain on the big sprocket of fretwork. Partial materials can enter the discharge end of the soaking groove through the hollow part of the hollow large chain wheel, so that the material receiving area of the lifting scraper is increased, and the conveying capacity of the lifting scraper is increased. Soak groove spiral and scraper blade hoist mechanism synchronous revolution, promote the material that the scraper blade will push and come and drag for, promote from the solution, fall into next soaking groove, promote the conveying capacity of scraper blade and be greater than soaking groove spiral, can ensure not to cause the putty.

As a further improvement of the utility model, the upper end of each lifting driving chain is engaged on a small lifting chain wheel, each small lifting chain wheel is respectively arranged on a driving shaft, each driving shaft is also respectively provided with a linkage chain wheel, two adjacent driving shafts form a group, and the two linkage chain wheels are connected by the linkage chain; and a lifting large chain wheel is arranged at the shaft end of one driving shaft and is in transmission connection with a main chain wheel of a driving speed reducer through a main chain. The main chain wheel of the driving speed reducer drives the lifting large chain wheel to rotate through the main chain, the lifting large chain wheel drives the lifting small chain wheel and the linkage chain wheel to rotate through the driving shaft, the linkage chain drives the other driving shaft and the lifting small chain wheel to synchronously rotate, the two lifting small chain wheels drive the lifting scraper to operate and the soaking groove to spirally rotate through the lifting driving chain respectively, one driving speed reducer simultaneously drives the two soaking groove spirals to push solid materials leftwards and rightwards, and simultaneously drives the two scraper lifting mechanisms to synchronously drag for the materials, drain and lift the solid materials.

As a further improvement, the spiral shaft of each soaking groove spiral is supported at both ends respectively in the spiral shaft bearing, and each spiral shaft bearing is fixed respectively at the center of circular shrouding, and each circular shrouding covers respectively and fixes in the outside of soaking groove both ends spiral mounting hole. Tear circular shrouding and spiral bearing frame open and can will soak the whole spiral of groove and take out from the spiral mounting hole, will soak the groove spiral and penetrate from the spiral mounting hole earlier during the installation, then cover circular shrouding and pass through the bolt fastening, install spiral bearing frame again and fix.

Drawings

The invention will be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.

FIG. 1 is a first flow chart of the soy protein concentrate preparation system of the present invention.

FIG. 2 is a second flow chart of the soy protein concentrate preparation system of the present invention.

FIG. 3 is a front view of the first embodiment of the powder extractor of the present invention.

Fig. 4 is a cross-sectional view taken along a-a in fig. 3.

Fig. 5 is a cross-sectional view taken along line B-B of fig. 3.

Fig. 6 is a cross-sectional view taken along line C-C of fig. 3.

Fig. 7 is a schematic view of fig. 3 with the front wall panel removed.

Fig. 8 is a perspective view of fig. 3.

Fig. 9 is a perspective view of the powder extractor box of fig. 3 with the top cover removed.

Fig. 10 is a perspective view of two adjacent steeping tanks of fig. 3.

Figure 11 is a perspective view of the leftmost infusion tank of figure 3.

Figure 12 is a perspective view of the filter cartridge of figure 11.

Fig. 13 is an enlarged view of a portion of the filter cartridge.

FIG. 14 is a schematic view of the operation state of the second embodiment of the powder extractor of the present invention.

Fig. 15 is a top view of fig. 14.

In the figure: E1. a bucket elevator; E2. a horizontal conveyor; E3. temporarily storing the raw materials in a bin; E4. a quantitative auger; E5. a powder extractor; E6. a wet meal conveyor; E7. a primary hydrocyclone separator; E8. a secondary hydrocyclone separator; E9. a solution temporary storage tank; E10. a tail gas condenser; E11. an extract evaporation recovery system; e11a. a concentrated extract inlet; e11b. an ethanol condensate outlet; e11c. outlet for concentrated oligosaccharide syrup; an E11d. raw steam inlet; e11e. a recycling heating medium inlet; e11f. exhaust steam outlet; E12. a double helix wringer; E13. a horizontal disc dryer; E14. a hot meal scraper conveyor; E15. distributing the packing auger; E16. a vertical disc dryer; E17. a saxolone; e17a. rotating the bleeder valve; E18. an induced draft fan; B1. a new solvent pump; B2. a concentrated extract liquid pump; B3. a temporary storage tank delivery pump; B4. a squeeze liquid delivery pump; G1. a fresh solvent tube; G2. a mixed liquid conveying pipe; G3. a temporary storage tank return pipe; G4. a temporary storage tank output pipe; G5. an ethanol condensate output pipe; G6. an extract liquid replenishing pipe; G7. a protein air supply pipeline; G8. recycling the heating medium pipe; q1. fresh solvent flow meter; q2. a thick solution flow meter; 1. a soaking tank; 1a, a solid material inlet of a leacher; 1a1. feed flow guide pipe; 1b, a wet dreg outlet of the leacher; 1c, a spiral mounting hole; 1d, a circular sealing plate; 1e, exhausting holes; 2. a tank body clapboard; 2a, an overflow port; 2b, a material guide groove; 2c, discharging a trough; 3. a baffle plate; 3a, a concave arc is arranged on the baffle plate; 4. the soaking groove is spiral; 4a screw shaft; 4b, main spiral sheets; 4c, hollowing out the large chain wheel; 4d, a spiral bearing seat; 4e, pushing the spiral right; 4f, left-pushing the helix; 5. a squeegee elevation mechanism; 5a, lifting a driving chain; 5b, lifting the scraper; 6. lifting the small chain wheel; 7. a drive shaft; 8. a link sprocket; 9. a linkage chain; 10. lifting the large chain wheel; 11. a main chain; 12. driving a speed reducer; 12a. a main sprocket; 13. a filter cartridge; grate bars; 13b, a filter cylinder outer helical band; 13c, a filter cartridge inner helical band; 14. a scraper plate discharging mechanism; 14a. a discharge drive chain; 14b, a discharge scraper; 15. a new solution inlet of the leacher; 16. and a concentrated solution outlet of the leacher.

Detailed Description

In the following description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, and do not mean that the device must have a specific orientation.

As shown in fig. 1 and 2, the soybean protein concentrate preparation system of the present invention comprises a raw material temporary storage bin E3, a quantitative packing auger E4, a powder extractor E5 and a wet meal conveyor E6, wherein an outlet of the raw material temporary storage bin E3 is connected with an inlet of the quantitative packing auger E4, an outlet of the quantitative packing auger E4 is connected with a solid material inlet of the extractor, a wet meal outlet of the extractor is connected with an inlet of the wet meal conveyor E6, an outlet of the wet meal conveyor E6 is connected with a feed inlet of a double-helix squeezer E12, a liquid phase outlet of the double-helix squeezer E12 is connected with an inlet of a squeezing liquid conveying pump B4, and an outlet of the squeezing liquid conveying pump B4 is also connected with an extract inlet E11a of an extract evaporation recovery system E11; an ethanol condensate outlet E11b of the extraction liquid evaporation and recovery system E11 is connected with an ethanol condensate output pipe G5, and an ethanol condensate output pipe G5 is connected with an extraction liquid supplement pipe G6 and then is connected with a fresh solvent pipe G1.

The discharge port of a double-helix squeezing dryer E12 is connected with the feed port of a horizontal disc dryer E13, the discharge port of a horizontal disc dryer E13 is connected with the inlet of a hot meal scraper conveyor E14, the outlet of the hot meal scraper conveyor E14 is connected with the inlet of a distribution packing auger E15, the outlet of the distribution packing auger E15 is respectively connected with the feed ports of the vertical disc dryers E16, the discharge port of each vertical disc dryer E16 is respectively connected with the feed port of a cyclone E17 through a protein air supply pipeline G7, the exhaust port of the cyclone E17 is connected with the inlet of a draught fan E18, and the bottom of the cyclone E17 is provided with a rotary discharge valve E17 a; the gas phase discharge ports of the horizontal disc dryer E13 and the vertical disc dryer E16 are respectively connected with a recycled heat medium inlet E11E of an extract evaporation recovery system E11 through a recycled heat medium pipe G8.

The inlet of a new solvent pump B1 is connected with a fresh solvent pipe G1, the outlet of a new solvent pump B1 is connected with a new dissolution inlet 15 of the leacher, the concentrated solution outlet 16 of the leacher is connected with the inlet of a concentrated solution extraction pump B2, the outlet of the concentrated solution extraction pump B2 is connected with the inlet of a primary hydrocyclone E7 through a mixed solution conveying pipe G2, the light phase outlet of the primary hydrocyclone E7 is connected with the inlet of a secondary hydrocyclone E8, the light phase outlet of the secondary hydrocyclone E8 is connected with the inlet of a solution temporary storage tank E9, and the bottom outlets of the primary hydrocyclone E7, the secondary hydrocyclone E8 and the temporary storage tank E9 are connected with the reflux port of a powder leacher E5.

After the white bean flakes or the low denatured bean pulp are lifted to a high position by a bucket elevator E1, the white bean flakes or the low denatured bean pulp are conveyed into a raw material temporary storage bin E3 by a horizontal conveyor E2E2 to be stored, the white bean flakes enter a quantitative auger E4 from the raw material temporary storage bin E3, the white bean flakes are directly conveyed into a solid material inlet of a leacher of a powder leacher E5 by the quantitative auger E4, the powder leacher E5 is extracted in a one-pot stewing way, and extracted wet-based concentrated protein is discharged from a wet pulp outlet of the leacher and is conveyed out by a wet pulp conveyor E6.

Wet-based concentrated protein sent out by a wet meal conveyor E6 enters a double-screw wringing machine E12 for mechanical squeezing and desolventizing, separated concentrated extract is sent into a concentrated extract inlet E11a of an extract evaporation and recovery system E11 by a wringing liquid conveying pump B4 and is evaporated in an extract evaporation and recovery system E11, concentrated oligosaccharide syrup obtained by evaporation is discharged from a concentrated oligosaccharide syrup outlet E11c, 60-65% (wt) ethanol condensate obtained by evaporation is discharged from an ethanol condensate outlet E11B and enters an ethanol condensate output pipe G5, is mixed with 95% (wt) ethanol from an extract supplementing pipe G6 to form 70% (wt) ethanol, and enters a fresh solvent pipe G1 for recycling.

And (3) sending a new solvent into a new dissolution inlet 15 of the leacher by a new solvent pump B1, and contacting the white bean flakes or the low denatured bean pulp with the solvent in a powder leacher E5 to finish extraction. The outlet pipeline of the new solvent pump B1 is provided with a fresh solvent flow meter Q1, the outlet of the solution temporary storage tank E9 is connected with the inlet of a temporary storage tank delivery pump B3 through a temporary storage tank output pipe G4, the outlet of the temporary storage tank delivery pump B3 is connected with an extract evaporation recovery system E11 through a concentrated solution flow meter Q2 and a temporary storage tank output pipe G4, and the outlet of the temporary storage tank delivery pump B3 is also connected with the return port of the solution temporary storage tank E9 through a temporary storage tank return pipe G3. The concentrated solution after precipitation is discharged from the outlet of the solution temporary storage tank E9 through a temporary storage tank output pipe G4, the temporary storage tank delivery pump B3 sends the concentrated solution to the first-stage evaporator, and in the initial operation stage of the system, the outlet solution of the temporary storage tank delivery pump B3 can also return to the solution temporary storage tank E9 through a temporary storage tank return pipe G3. A fresh solvent flow meter Q1 may monitor the flow rate of fresh solvent and a rich solution flow meter Q2 may monitor the flow rate of the output rich solution.

Concentrated solution containing certain powder particles is pumped by a concentrated extract pump B2, and then is sent to a primary hydrocyclone E7 for separation through a mixed solution conveying pipe G2, solid particles in the solution are removed for the first time, and then are removed again through a secondary hydrocyclone E8, and then enter a solution temporary storage tank E9 for storage, the separated solid particle flow can enter a soaking tank of a powder leacher E5, and can enter a left second soaking tank, so that the particle concentration at a concentrated solution outlet 16 of the leacher is reduced. The precipitated concentrated solution is sent to a concentrated extract liquid inlet E11a of an extract liquid evaporation and recovery system E11 from an outlet of a solution temporary storage tank E9 through a temporary storage tank conveying pump.

Wet basic protein extruded and desolventized by a double-screw extruder E12 is firstly fed into a horizontal disc dryer E13 for pre-drying, the moisture content of the pre-dried protein is reduced, the temperature is increased, the material becomes diffused, the wet basic protein is fed into an inlet of a distribution auger E15 by a hot meal scraper conveyor E14, the hot meal is distributed by the distribution auger E15 to be fed into each vertical disc dryer E16 for drying, concentrated protein particles with the moisture content of less than 7 percent are obtained, the concentrated protein particles are fed into a cyclone E17 through a protein air feeding pipeline G7 for centrifugal separation, the concentrated protein particles are discharged from a rotary discharge valve E17a at the bottom of the cyclone E17 and then fed into a crushing working section for crushing, and powdery concentrated protein with 100 meshes and 95 percent is obtained. Dilute syrup of concentrated extract in a solution temporary storage tank E9 enters an extract evaporation and recovery system E11 for concentration, an extract evaporation and recovery system E11 comprises a preheater, a first evaporator, a second evaporator and a third evaporator, the dilute syrup is preheated by the preheater, the preheater adopts secondary steam generated by a horizontal disc dryer E13 and a vertical disc dryer E16 as a heat source, the preheated dilute syrup enters the first evaporator, the first evaporator adopts 10bar saturated raw steam entering from a raw steam inlet E11d as the heat source, the first evaporator adopts micro-negative pressure evaporation, the evaporated secondary steam serves as a heat source for secondary evaporation, the secondary evaporation is negative pressure evaporation, the dilute syrup enters the secondary evaporation after primary evaporation, and the negative pressure evaporation is carried out; then the waste heat enters a third evaporator, the third evaporation is negative pressure evaporation, and secondary steam of a horizontal disc dryer E13 and a vertical disc dryer E16 is used as a heat source, so that the system utilization of the waste heat is realized; and discharging the syrup subjected to the triple steaming from a concentrated oligosaccharide syrup outlet E11c, allowing the syrup to enter a syrup temporary storage tank, quantitatively allowing the syrup to enter a thin film evaporator for concentration, and finally forming concentrated syrup with the concentration of more than or equal to 55%.

As shown in fig. 1 to 15, 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 both connected to a tail gas condenser E10, the exhaust steam outlet E11f of the extract evaporation recovery system E11 is also connected to a tail gas condenser E10, and the ethanol gas is recycled after being condensed and recovered. A plurality of parallel tank body partition plates 2 are connected between the front wall plate and the rear wall plate of the tank body, the inner cavity of the tank body is divided into a plurality of soaking tanks 1 by each tank body partition plate 2, the upper parts of the tank body partition plates 2 are respectively provided with an overflow port 2a, the overflow ports 2a on the adjacent tank body partition plates 2 are arranged in a staggered manner in the front-rear direction, the heights of the overflow ports 2a are gradually reduced from right to left, the discharge end of the right soaking tank is connected with a new leaching device inlet 15, and the feed end of the left soaking tank is connected with a leaching device concentrated solution outlet 16; a solid material inlet 1a of the leacher is arranged above the feeding end of the leftmost soaking tank, a guide chute 2b for lifting and turning materials to the right side is respectively arranged at the discharging end of each tank body clapboard 2, and a discharging chute 2c extending upwards to the right side is arranged at the discharging end of the right wall plate of the box body.

The bottom of each soaking tank 1 is arc-shaped and is respectively provided with a soaking tank spiral 4, the rotating directions of the adjacent soaking tank spirals 4 are opposite, and a left push spiral 4f is arranged in an odd number of tanks from a solid material inlet 1a of the solid material leacher to push the solid material to the front side wall direction of the powder leacher; and a right pushing screw 4e is arranged in the even number of grooves and pushes the solid materials to the direction of the rear side wall of the powder extractor. Each guide chute 2b is provided with a scraper lifting mechanism 5, and the discharge chute 2c is provided with a scraper discharging mechanism 14.

The material enters the feed end of the leftmost soaking tank from the solid material inlet 1a of the leacher, and the new solvent enters the rightmost soaking tank. The soaking and extraction processes are completed in the soaking tanks 1, and when the materials are pushed to the discharge ends of the soaking tanks 1 by the soaking tank spiral 4, the materials are upwards fished out by the scraper lifting mechanism 5 along the guide groove 2b, separated from the liquid level, and then are drained by short drip to fall into the lower soaking tank on the right side. The advancing directions of the materials in the adjacent soaking tanks are opposite, so that the solid materials advance in an S-shaped zigzag manner. When the solid material enters the final stage soaking tank, the solid material is fully soaked and mixed with the new solution, and then the solid material is fished out from the discharge end of the rightmost soaking tank along the discharge groove 2c by the scraper discharge mechanism 14 and is discharged out of the machine from the wet pulp outlet 1b of the leacher. The solid material and the solution always keep reverse flow, the material with the highest content contacts with the concentrated solution, the material with the lower content contacts with the dilute solution, the good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid material transversely advances along soaking groove 1 in turn, transversely advances after a section and is fished out and fall into fore-and-aft next-level soaking groove, obtains the stirring repeatedly, and material and solution all are the torrent state, can not appear laminar flow state, even the very little powder of void fraction also can be fully soaked by solution. The adjacent overflow ports 2a are arranged in a staggered manner in the front and back directions, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the full length of each soaking tank 1, then flows into the next soaking tank by using potential difference overflow and turns back the full length of the soaking tank, the extraction stroke of the solid material and the solution is greatly prolonged, full extraction can be realized, and high-efficiency extraction is realized. The concentrate reaching the leftmost leach tank is discharged from the leach concentrate outlet 16. The soaking liquid level is slightly higher than the solid phase, the solid and the liquid are mixed fully, the solvent consumption is low, the concentration of the obtained mixed liquid is high, and the energy consumption of evaporation separation is low.

The bottom of the soaking tank 1 is arc-shaped and is matched with the spiral 4 of the soaking tank, so that dead zones at the bottom of the tank can be avoided; soaking groove spiral 4 is responsible for the transport of solid material in soaking groove 1 and accomplishes and soak the extraction, through helical blade 'S compulsory stirring, avoids simply soaking the insufficient defect of in-process material and solvent mass transfer, and adjacent soaking groove spiral 4' S the opposite direction of turning makes the material be the S-shaped and gos forward. The scraper lifting mechanism 5 is used for fishing, draining and lifting the soaked solid materials for solid-liquid separation and solid-phase lifting; the scraper discharge mechanism 14 is used for scooping up, draining and discharging the extracted solid materials. The spiral scraper not only can transport solid materials, but also can stir the solid materials strongly.

As shown in fig. 9, each immersion tank 1 is provided with at least one baffle plate 3 extending in the left-right direction, and the lower end of each baffle plate 3 is clamped above the spiral of the immersion tank by a baffle plate upper concave arc 3a. The baffle plate 3 can prevent the surface solution from short-circuit outflow without fully contacting with the solid material, the upper concave arc 3a of the baffle plate is clamped above the spiral 4 of the soaking tank to convey and provide a channel for the material, the solution is forced to pass through the gap of the upper concave arc 3a of the baffle plate, the solid material and the extraction liquid are stirred, mixed and contacted, the two phases are fully contacted in a turbulent state, and the soaking effect of the material and the solution is further improved; the solid and the liquid are in turbulent contact under the stirring action, the liquid phase has no chromatography, and the concentrations of the same phases are consistent. The plurality of baffle plates 3 enable the solvent to flow in an S shape in the vertical direction in each soaking tank 1, thereby avoiding the short circuit phenomenon of the solvent, obviously increasing the extraction power and having high extraction efficiency.

As shown in fig. 10, a hollow large chain wheel 4c is respectively installed at the discharge end of the screw shaft of each soaking tank screw 4, the lower end of the lifting drive chain 5a of the corresponding scraper lifting mechanism 5 is engaged with the hollow large chain wheel 4c, and a plurality of lifting scrapers 5b are uniformly arranged on the lifting drive chain 5a. Partial materials can enter the discharge end of the soaking groove through the hollow part of the hollow large chain wheel 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. Soak groove spiral 4 and 5 synchronous revolutions of scraper blade hoist mechanism, promote material that scraper blade 5b comes with the propelling movement and drag for from solution, promote, fall into next and soak the groove, promote scraper blade 5 b's conveying capacity and be greater than and soak groove spiral 4, can ensure not to cause the putty.

The upper end of each lifting driving chain 5a is meshed with a small lifting chain wheel 6, each small lifting chain wheel 6 is respectively arranged on a driving shaft 7, each driving shaft 7 is also respectively provided with a linkage chain wheel 8, two adjacent driving shafts 7 form a group, and the two linkage chain wheels 8 are in transmission connection through a linkage chain 9; the shaft end of one of the driving shafts 7 is provided with a lifting large chain wheel 10, and the lifting large chain wheel 10 is in transmission connection with a main chain wheel 12a of a driving speed reducer 12 through a main chain 11. The main chain wheel 12a of the driving speed reducer 12 drives the lifting large chain wheel 10 to rotate through the main chain 11, the lifting large chain wheel 10 drives the lifting small chain wheel 6 and the linkage chain wheel 8 to rotate through the driving shaft 7, the linkage chain 9 drives the other driving shaft 7 and the lifting small chain wheel 6 to synchronously rotate, the two lifting small chain wheels 6 drive the lifting scraper 5b to operate and the dipping groove screw 4 to rotate through the lifting driving chain 5a respectively, the driving speed reducer 12 simultaneously drives the two dipping groove screws 4 to push solid materials leftwards and rightwards, and simultaneously drives the two scraper lifting mechanisms 5 to synchronously drag the materials, drain and lift the solid materials.

Both ends of a spiral shaft 4a of each soaking groove spiral 4 are respectively supported in spiral shaft bearing blocks 4d, each spiral shaft bearing block 4d is respectively fixed at the center of a circular sealing plate 1d, and each circular sealing plate 1d is respectively covered and fixed at the outer sides of spiral mounting holes 1c at both ends of the soaking groove. Tear circular shrouding 1d and screw bearing 4d down and can take out soaking groove spiral 4 is whole from spiral mounting hole 1c, during the installation earlier penetrates soaking groove spiral 4 from spiral mounting hole 1c, then covers circular shrouding 1d and passes through the bolt fastening, installs screw bearing 4d again and fixes.

The lower end of a discharge driving chain 14a of the scraper discharge mechanism 14 is meshed with the large hollow chain wheel 4c, and a plurality of discharge scrapers 14b are uniformly arranged on the discharge driving chain 14a. Partial materials can enter the discharge end of the rightmost soaking groove through the hollow part of the hollow large chain wheel 4c, so that the receiving area of the discharge scraper 14b is enlarged, and the conveying capacity of the discharge scraper 14b is improved. Soak groove spiral 4 and scraper blade discharge mechanism 14 synchronous revolution, ejection of compact scraper blade 14b with the material that the propelling movement was come drag for from solution, promote and discharge powder leaches the ware, ejection of compact scraper blade 14 b's transport capacity is greater than soak groove spiral 4, can ensure not to cause the putty.

As shown in fig. 11 to 13, each immersion groove screw 4 comprises a screw shaft 4a and a main screw plate 4b wound on the periphery of the screw shaft, a filter cartridge 13 is installed at the feed end of the leftmost screw shaft below the solid material inlet 1a of the extractor, the port of one side of the filter cartridge 13 facing the main screw plate 4b is closed, the other side of the filter cartridge 13 is open, the concentrated solution outlet 16 of the extractor is inserted into the inner cavity of the filter cartridge 13, a plurality of axially extending grid bars 13a are uniformly distributed on the circumference of the filter cartridge 13, and the gap between the adjacent grid bars 13a is narrow outside and wide inside. The powder is filtered by the filter cylinder 13 before flowing out, and the powder is retained on the outer surface of the filter cylinder 13, so that the content of powdery solid in the concentrated extract is reduced as much as possible, and the subsequent separation and evaporation of the rotary liquid are guaranteed; the concentrated extract liquid in the solid-liquid intermixing medium enters the concentrated liquid outlet 16 of the leacher to flow out after being continuously and stably filtered, and the filtered concentrated extract liquid can be stably and continuously filtered and conveyed without causing the blockage of a liquid outlet pipe valve so as to enter a rotary liquid separation system for fine filtration. Once the powder material crosses the gap at the outermost side of the filter cylinder 13, the powder material can smoothly fall into the bottom of the filter cylinder 13 and is pushed out by a spiral belt 13c in the filter cylinder for self-cleaning; avoiding the powder particles from being blocked in the gaps between the adjacent grate bars 13a and influencing the filtering capacity.

The outer periphery of the bowl 13 is wound with a bowl outer helical band 13b, and the direction of rotation of the bowl outer helical band 13b is the same as that of the coaxial main helical blade 4b. The filter cylinder outer spiral belt 13b can push out the solid materials flowing along with the liquid to one side where the main spiral sheet 4b is located, so that excessive materials are prevented from being deposited outside the filter cylinder 13.

The inner wall of the filter cylinder 13 is provided with a filter cylinder inner spiral belt 13c, and the spiral direction of the filter cylinder inner spiral belt 13c is opposite to the coaxial main spiral sheet 4b. A small amount of solid powder enters the filter cylinder 13 along with the extraction liquid and settles on the lower part of the inner wall of the filter cylinder 13, and the inner spiral belt 13c which is opposite to the rotation direction of the main spiral plate 4b pushes the settled matters out of the filter cylinder 13 from the open end and then out of the filter section by the outer spiral belt 13b of the filter cylinder, thereby completing the self-cleaning process of the filter cylinder 13. Therefore, 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 materials and liquid is solved, and the soybean protein concentrate preparation system has wide adaptability to various oil materials.

As shown in fig. 3 and 8, the solid inlet 1a of the extractor may be disposed at the left portion of the top cover of the tank, and a feeding guide pipe 1a1 is connected below the solid inlet 1a of the extractor to guide the fresh solid to the front side of the filter cartridge 13.

As shown in fig. 14 and 15, the extractor solid inlet 1a may be provided at the upper portion of the left side wall of the housing, and may be located at the front side of the filter cartridge 13 at a position in the front-rear direction. The right side of the soaking tank has the highest liquid level and overflows to the left side in sequence. In FIG. 15, the large arrows indicate the direction of solid materials, the small arrows indicate the direction of solution flow, and the whole process is in a reverse direction.

The utility model discloses a leaching of "a pot is stewed" formula, it is high-efficient and reliable, can be used to leaching of powdery material and high powder degree material. The method can solve the preparation bottleneck of the soybean concentrated protein and the cottonseed concentrated protein, and overcome the problems of poor material permeability, easy dissolution of protein and sugar to block a grid plate, shallow leaching material layer, high equipment investment, low production efficiency, high system failure rate and the like. To the likepowder leftover bits and pieces that can't handle in traditional leaching process, like high powder degree soybean white bean piece, the popped powder of semi-degeneration, can adopt the utility model discloses a system is prepared to soybean protein concentrate, processes into protein concentrate after extracting this type of property material, can promote the economic value of this type of material by a wide margin, promotes enterprise economic benefits and market competition.

The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All the technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope claimed by the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.

Claims (8)

1. The utility model provides a system is prepared to soybean protein concentrate, including raw materials temporary storage storehouse, the ration auger, powder leaches ware and wet dregs of a meal conveyer, the export in raw materials temporary storage storehouse links to each other with the entry of ration auger, the export of ration auger links to each other with the solid material entry of leacher, leacher wet dregs of a meal export links to each other with the entry of wet dregs of a meal conveyer, the entry and the fresh solvent pipe of new solvent pump link to each other, the export and the leacher of new solvent pump link to each other with the new inlet that dissolves, leacher concentrated solution export links to each other with the entry of concentrated extract extraction pump, its characterized in that: the outlet of the concentrated extract liquid extraction pump is connected with the inlet of the primary hydrocyclone separator through a mixed liquid conveying pipe, the light phase outlet of the primary hydrocyclone separator is connected with the inlet of the secondary hydrocyclone separator, the light phase outlet of the secondary hydrocyclone separator is connected with the inlet of the solution temporary storage tank, and the outlets at the bottoms of the primary hydrocyclone separator, the secondary hydrocyclone separator and the solution temporary storage tank are all connected with the reflux port of the powder leacher; the lower part export of solution jar of keeping in links to each other with the entry of keeping in jar delivery pump, the export of keeping in jar delivery pump links to each other with the concentrated extract liquid entry of extraction liquid evaporation recovery system.

2. The soy protein concentrate manufacturing system of claim 1, wherein: the outlet of the temporary storage tank delivery pump is also connected with the return port of the solution temporary storage tank through a temporary storage tank return pipe, the outlet of the wet meal conveyor is connected with the feed port of a double-screw wringing machine, the liquid phase outlet of the double-screw wringing machine is connected with the inlet of a wringing liquid delivery pump, and the outlet of the wringing liquid delivery pump is also connected with the concentrated extraction liquid inlet of an extraction liquid evaporation recovery system; an ethanol condensate outlet of the extraction liquid evaporation and recovery system is connected with an ethanol condensate output pipe, and the ethanol condensate output pipe is connected with the extraction liquid replenishing pipe and then connected with the fresh solvent pipe.

3. The soy protein concentrate production system of claim 2, wherein: the discharge port of the double-helix squeezing dryer is connected with the feed port of the horizontal disc dryer, the discharge port of the horizontal disc dryer is connected with the inlet of the hot meal scraper conveyer, the outlet of the hot meal scraper conveyer is connected with the inlet of the distribution auger, the outlet of the distribution auger is respectively connected with the feed ports of the vertical disc dryers, the discharge port of each vertical disc dryer is respectively connected with the feed port of the cyclone through a protein air conveying pipeline, the air outlet of the cyclone is connected with the inlet of the induced draft fan, and the bottom of the cyclone is provided with a rotary discharge valve; the gas phase discharge ports of the horizontal disc dryer and the vertical disc dryer are respectively connected with the recycling heat medium inlet of the extraction liquid evaporation and recovery system through recycling heat medium pipes.

4. The soy protein concentrate manufacturing system of claim 1, wherein: the powder leacher comprises a rectangular box body, wherein a plurality of parallel groove body partition plates are connected between the front wall plate and the rear wall plate of the box body, each groove body partition plate divides the inner cavity of the box body into a plurality of soaking grooves, the upper part of each groove body partition plate is respectively provided with an overflow port, the overflow ports on the adjacent groove body partition plates are staggered in the front-rear direction, the height of each overflow port is gradually reduced from right to left, the discharge end of the rightmost soaking groove is connected with a new leaching device dissolving inlet, and the feed end of the leftmost soaking groove is connected with a concentrated solution outlet of the leacher; the solid material inlet of the leacher is positioned above the feeding end of the leftmost soaking tank, the discharging end of each tank body partition plate is respectively provided with a guide chute for lifting and turning materials to the right side, the discharging end of the right wall plate of the tank body is provided with a discharging chute extending upwards and rightwards, and the wet meal outlet of the leacher is positioned at the upper end of the discharging chute; the bottom of each soaking groove is arc-shaped and is respectively provided with a soaking groove spiral, and the spiral directions of adjacent soaking grooves are opposite; and each guide chute is internally provided with a scraper lifting mechanism, and the discharge chute is internally provided with a scraper discharging mechanism.

5. The soy protein concentrate production system of claim 4, wherein: at least one baffle plate extending along the left and right directions is respectively arranged in each soaking groove, and the lower end of each baffle plate is respectively clamped above the spiral of the soaking groove through the upper concave arc of the baffle plate.

6. The soy protein concentrate production system of claim 4, wherein: the discharge ends of the spiral shafts of the soaking grooves are respectively provided with a hollow large chain wheel, the lower ends of the lifting drive chains of the corresponding scraper lifting mechanisms are meshed with the hollow large chain wheels, and a plurality of lifting scrapers are uniformly arranged on the lifting drive chains.

7. The soy protein concentrate production system of claim 6, wherein: the upper end of each lifting driving chain is meshed with a small lifting chain wheel, each small lifting chain wheel is respectively arranged on a driving shaft, each driving shaft is also respectively provided with a linkage chain wheel, two adjacent driving shafts form a group, and the two linkage chain wheels are in transmission connection through the linkage chain; and a lifting large chain wheel is arranged at the shaft end of one driving shaft and is in transmission connection with a main chain wheel of a driving speed reducer through a main chain.

8. The soy protein concentrate production system of claim 4, wherein: the two ends of the spiral shaft of each soaking groove spiral are respectively supported in the spiral shaft bearing seats, each spiral bearing seat is respectively fixed at the center of the circular sealing plate, and each circular sealing plate respectively covers and is fixed at the outer sides of the spiral mounting holes at the two ends of the soaking groove.