阅读说明：本技术 一种混合溶剂提取大豆有效成分的装置及其工艺 (Device and process for extracting soybean effective components by using mixed solvent ) 是由 林凤岩 武象 王国栋 李肖 薛亚南 李鹏 于 2020-03-30 设计创作，主要内容包括：本发明公开一种混合溶剂提取大豆有效成分的装置及其工艺,包括前处理装置、浸出装置、脱溶装置、粉碎包装装置、混合油蒸发装置、混合液蒸发装置和气体冷凝回收装置；所述前处理装置与所述浸出装置连接,所述脱溶装置与所述浸出装置连接；所述粉碎包装装置与所述脱溶装置连接,所述混合油蒸发装置和混合液蒸发装置通过分液器与所述浸出装置连接；所述气体冷凝回收装置用于回收上述装置产生的不凝气体；本发明降低湿蛋白中含湿率,减少湿蛋白烘干所需能源,降低生产运行成本,减少设备和基建总投资,为企业带来更大的经济效益。(The invention discloses a device for extracting soybean active ingredients by using a mixed solvent and a process thereof, wherein the device comprises a pretreatment device, a leaching device, a desolventizing device, a crushing and packaging device, a mixed oil evaporation device, a mixed liquid evaporation device and a gas condensation and recovery device; the pretreatment device is connected with the leaching device, and the desolventizing device is connected with the leaching device; the crushing and packaging device is connected with the desolventizing device, and the mixed oil evaporation device and the mixed liquid evaporation device are connected with the leaching device through a liquid distributor; the gas condensation and recovery device is used for recovering the non-condensable gas generated by the device; the invention reduces the moisture content in wet protein, reduces the energy required by drying wet protein, reduces the production and operation cost, reduces the total investment of equipment and capital construction, and brings greater economic benefit for enterprises.)

1. A device for extracting soybean active ingredients by using a mixed solvent is characterized by comprising a pretreatment device, a leaching device, a desolventizing device, a crushing and packaging device, a mixed oil evaporation device, a mixed liquid evaporation device and a gas condensation and recovery device; the pretreatment device is connected with the leaching device, and the desolventizing device is connected with the leaching device; the crushing and packaging device is connected with the desolventizing device, and the mixed oil evaporation device and the mixed liquid evaporation device are connected with the leaching device through a liquid distributor; the gas condensation recovery device is used for recovering the non-condensable gas generated by the device.

2. The apparatus for extracting soybean active ingredient with mixed solvent as claimed in claim 1, wherein the leaching apparatus comprises a submerged swelling leacher and a tank chain leacher; one end of the immersed swelling leacher is connected with the pretreatment device, and the other end of the immersed swelling leacher is connected with the box chain type leacher; the box chain type leacher is connected with the desolventizing device.

3. The apparatus for extracting soybean active ingredient with mixed solvent according to claim 2, wherein the desolventizing apparatus comprises a screw extruder, a horizontal desolventizing machine and a vertical desolventizing machine; one end of the screw extruder is connected with the box chain type leacher, the other end of the screw extruder is connected with the horizontal desolventizing machine, and the vertical desolventizing machine is respectively connected with the horizontal desolventizing machine and the crushing and packaging device.

4. The mixed solvent soybean active ingredient extraction apparatus as set forth in claim 3, wherein the pulverization packaging means comprises a pulverizer and a packaging machine; one end of the pulverizer is connected with the vertical desolventizing machine, and the other end of the pulverizer is connected with the packaging machine.

5. The device for extracting soybean active ingredients with mixed solvent according to claim 4, wherein the mixed oil evaporation device comprises a first mixed oil evaporation unit, a second mixed oil evaporation unit and a third mixed oil evaporation unit; the mixed oil evaporation first evaporation unit adopts an MVR evaporation process, and the mixed oil evaporation second evaporation unit adopts a climbing film evaporator; the third evaporation unit for evaporating the mixed oil adopts a plate-type stripping tower; the mixed liquid evaporation device comprises a mixed liquid evaporation first evaporation unit, a mixed liquid evaporation second evaporation unit, a mixed liquid evaporation third evaporation unit and a mixed liquid evaporation fourth evaporation unit; the mixed liquid evaporation first evaporation unit takes secondary steam generated in a wet protein drying process as a heat source, the mixed liquid evaporation second evaporation unit takes secondary steam generated in the mixed liquid evaporation first evaporation unit as a heat source, the mixed liquid evaporation third evaporation unit adopts an MVR evaporation process, the generated secondary steam is pressurized and heated by a mechanical compressor and then serves as a mixed liquid evaporation third evaporation unit heat source, and the mixed liquid evaporation fourth evaporation unit takes water vapor as a heat source.

6. A process for extracting soybean active ingredients by using a mixed solvent is characterized by comprising the following steps:

s1, conveying the raw material soybeans into a pretreatment device by conveying equipment;

s2, conveying the prepreg into a leaching device by conveying equipment;

s3, conveying the wet protein into a desolventizing device by conveying equipment;

s4, conveying the protein particles into a crushing and packaging device by conveying equipment;

s5, conveying the leachate to a liquid distributor through conveying equipment after the leachate overflows from the immersed swelling leacher; standing the leachate in a liquid separator for 30-50 minutes, layering the mixed oil and the mixed liquid, and allowing the layered mixed oil and the layered mixed liquid to flow out from respective channels to form mixed oil containing 20-35% of soybean oil and mixed liquid containing 5-15% of oligosaccharide, wherein the mixed oil enters a mixed oil evaporation device, and the mixed liquid enters a mixed liquid evaporation device;

and S6, after the secondary steam generated by the devices in the steps S1-S5 is respectively used for waste heat, the generated non-condensable gas enters a gas condensation and recovery device.

7. The process for extracting soybean active ingredients from mixed solvents according to claim 6, wherein in step S1, the soybeans are first cleaned by cleaning equipment to remove impurities, and the content of solid impurities is reduced to below 0.5%; heating the soybean subjected to impurity removal to 40-60 ℃ by heating equipment, and cracking the surface of the soybean; removing soybean hulls from the soybeans with cracked skins by using a huller, wherein the content of the soybean hulls is reduced to be below 0.5%; heating the peeled soybeans to 60-70 ℃ in heating equipment, and keeping for hardening and tempering for 40-60 minutes; and extruding the soybean processed and tempered soybean into a soybean blank by a soybean processing and rolling machine, wherein the thickness of the soybean blank is 0.25-0.35 mm.

8. The process for extracting soybean active ingredients from mixed solvents according to claim 6, wherein in step S2, the prepreg is first put into an immersion swelling and leaching device, and the immersion swelling and leaching device is filled with the mixed solvent containing 20-35% of soybean oil, 5-15% of oligosaccharide and 40-60 ℃ to fill the swelling and leaching section of the swelling and leaching device; fully contacting the prepreg with a mixed solvent consisting of a vegetable oil extraction solvent, ethanol and water in a swelling and leaching section, and dissolving part of soybean oil in the prepreg in the vegetable oil extraction solvent to form mixed oil; swelling and leaching the prepreg in an immersed swelling and leaching device for 10-60 minutes; the leachate formed by the mixed oil and the mixed liquid flows into a liquid separator for separation; the swelled prepreg enters a box chain type leacher to leach soybean oil and oligosaccharide, the leachate carries out countercurrent continuous spray leaching on the prepreg, a mixed solvent with the soybean oil content of 20-35%, the oligosaccharide content of 5-15% and the temperature of 40-60 ℃ is adopted at the feed end of the box chain type leacher to leach, and a vegetable oil extraction solvent, ethanol and water are adopted at the discharge end of the box chain type leacher in a ratio of 1:2: 1; the swelling and leaching time of the prepreg in the box chain type is 150-300 minutes; the solid material of the leached mixed solvent forms wet protein and enters a desolventizing device.

9. The process for extracting soybean active ingredients from a mixed solvent according to claim 6, wherein in step S3, wet protein firstly enters a screw extruder, the moisture content of the wet protein is reduced from 65-70% to 55-58% through the extrusion and grinding of a screw, the extruded extrusion liquid is returned to a box-chain type extractor again, the extruded wet protein firstly enters a horizontal dryer, the desolventizing operation is carried out under the vacuum condition of-0.005-0.01 MPa, and the discharging temperature is 70-80 ℃; the moisture content is 35-40%; after being dried by a horizontal dryer, wet protein enters a vertical dryer, the wet protein is uniformly spread on the disc surface of the vertical dryer by a layer of 2 cm per month, and is continuously stirred, the temperature is increased to 80-90 ℃, desolventization and dehydration are carried out under the vacuum state of-0.005-0.01 MPa, protein particles with water content of 4-8% are formed after drying, and the protein particles enter a crushing and packaging device.

10. The process for extracting soybean active ingredients from a mixed solvent as claimed in claim 6, wherein in step S4, the protein particles are first cooled by wind and then sent to a crusher, and crushed into 100 mesh protein powder by the crusher, and the protein powder is packaged in a packaging scale to obtain the soybean protein concentrate product.

Technical Field

The invention relates to the technical field of vegetable oil processing, in particular to the technical field of simultaneously preparing soybean protein concentrate, soybean oil, soybean oligosaccharide and other products from soybeans, and particularly relates to a device and a process for extracting soybean active ingredients by using a mixed solvent.

Background

The process for preparing the products such as soybean protein concentrate, soybean oil, soybean oligosaccharide and the like by mainstream soybeans is carried out step by step; extracting oil from soybean by using a nonpolar solvent to generate soybean oil and soybean meal products, and extracting soluble oligosaccharide from the soybean meal by using a polar solvent to generate soybean oligosaccharide and soybean protein concentrate products; the main production device is composed of six devices, namely a pretreatment device, a leaching device, a desolventizing device, a crushing and packaging device, a mixed oil evaporation device, a gas condensation and recovery device and the like, wherein a nonpolar solvent adopted by the mainstream soybean production technology is mainly a vegetable oil extraction solvent (GB 1886.52 also called hexane solvent), the raw material soybean enters the pretreatment device to be subjected to a series of treatments, and a prepreg (bean blank or puffed material) suitable for the leaching device is formed; the prepreg enters a leaching device, and is soaked and sprayed by a non-polar solvent in a leaching device, so that the grease in the prepreg is dissolved in the non-polar solvent to form mixed oil; the leached wet soybean meal enters a desolventizing device, is dried and cooled by a vertical evaporator, and then enters a crushing and packaging device to be crushed and packaged into a soybean meal product; the leached mixed oil enters a mixed oil evaporation device to be subjected to three procedures of two times of negative pressure evaporation and steam stripping to form a soybean oil product, and gas generated in all the devices enters a gas condensation recovery device and is condensed into liquid by a condenser for recycling; in the mainstream process technology for preparing soybean protein concentrate and soybean oligosaccharide products, a main production device comprises a pretreatment device, a leaching device, a desolventizing device, a crushing and packaging device, a mixed liquid evaporation device, a gas condensation and recovery device and the like, soybean meal after soybean oil extraction enters the pretreatment device, 10-15% of soybean meal powder is removed through screening to form prepreg, the prepreg enters the leaching device, and soluble oligosaccharide in the prepreg is dissolved in a polar solvent to form mixed liquid through polar solvent soaking and spraying in a swelling device and a leaching device; the leached wet protein enters a desolventizing device, is extruded and dehydrated by a screw extruder, is dried by a horizontal dryer and a vertical dryer, and then enters a crushing and packaging device to be crushed and packaged into a soybean protein concentrate product; the leached mixed liquor enters a mixed liquor evaporation device to be subjected to multi-effect evaporation, MVR evaporation and wiped film evaporation to form a soybean oligosaccharide product, and gas generated in all the devices enters a gas condensation recovery device to be condensed into liquid through a condenser for recycling.

The water vapor consumption of the process for preparing the soybean protein concentrate, the soybean oil, the soybean oligosaccharide and other products by the mainstream soybeans step by step is 3500-3800 kg/t of protein, the power consumption is 350-400 wk.h/t of protein, and the concentrated protein yield is 40-45%, so that the energy consumption is high, and the concentrated protein yield is low.

From the above, the processing technology for preparing soybean protein concentrate, soybean oil and soybean oligosaccharide products from soybeans is long, the used devices are various, partial devices are overlapped, the occupied area is large, the raw material waste is more, the energy consumption of electric energy, water vapor and the like is higher, the investment of fixed assets of processing enterprises is huge, the production and operation cost is higher, and the profit margin of the enterprises is generally low.

Based on the problems, at present, scientific researchers carry out a series of targeted researches, wherein optimization of a process, leaching of a mixed solvent and energy conservation and consumption reduction of a device are main development directions, a plurality of patent and literature reports exist, and the published reports show that the technologies focus on being single and relatively comprehensive and cannot organically integrate related devices together to form a set of complete and optimized process technology for guiding production and operation of enterprises.

Disclosure of Invention

In order to overcome the problems that the prior art has single and unilateral emphasis and cannot organically integrate related devices, the invention provides the device for extracting the effective components of the soybeans by using the mixed solvent and the process thereof, which greatly optimize and shorten the process for preparing the products such as the soybean protein concentrate, the soybean oil, the soybean oligosaccharide and the like by using the soybeans, reduce the equipment quantity and reduce the water vapor consumption and the power consumption.

The invention is realized by the following technical scheme.

A device for extracting soybean effective components with mixed solvent comprises a pretreatment device, a leaching device, a desolventizing device, a crushing and packaging device, a mixed oil evaporation device, a mixed liquid evaporation device and a gas condensation and recovery device; the pretreatment device is connected with the leaching device, and the desolventizing device is connected with the leaching device; the crushing and packaging device is connected with the desolventizing device, and the mixed oil evaporation device and the mixed liquid evaporation device are connected with the leaching device through a liquid distributor; the gas condensation and recovery device is used for recovering the non-condensable gas generated by the device; the wet protein drying device can reduce the moisture content in wet protein, reduce energy required by drying the wet protein, reduce the production and operation cost, reduce the total investment of equipment and capital construction, and bring greater economic benefit for enterprises.

As a further improvement of the technical scheme, the leaching device comprises an immersed swelling leacher and a box chain type leacher; one end of the immersed swelling leacher is connected with the pretreatment device, and the other end of the immersed swelling leacher is connected with the box chain type leacher; the box chain type leacher is connected with the desolventizing device.

As a further improvement of the technical scheme, the desolventizing device comprises a screw extruder, a horizontal desolventizing machine and a vertical desolventizing machine; one end of the screw extruder is connected with the box chain type leacher, the other end of the screw extruder is connected with the horizontal desolventizing machine, and the vertical desolventizing machine is respectively connected with the horizontal desolventizing machine and the crushing and packaging device.

As a further improvement of the above technical solution, the crushing and packaging device comprises a crusher and a packaging machine; one end of the pulverizer is connected with the vertical desolventizing machine, and the other end of the pulverizer is connected with the packaging machine.

As a further improvement of the above technical solution, the mixed oil evaporation device includes a mixed oil evaporation first evaporation unit, a mixed oil evaporation second evaporation unit, and a mixed oil evaporation third evaporation unit; the mixed oil evaporation first evaporation unit adopts an MVR evaporation process, and the mixed oil evaporation second evaporation unit adopts a climbing film evaporator; the third evaporation unit for evaporating the mixed oil adopts a plate-type stripping tower; the mixed liquid evaporation device comprises a mixed liquid evaporation first evaporation unit, a mixed liquid evaporation second evaporation unit, a mixed liquid evaporation third evaporation unit and a mixed liquid evaporation fourth evaporation unit; the mixed liquid evaporation first evaporation unit takes secondary steam generated in a wet protein drying process as a heat source, the mixed liquid evaporation second evaporation unit takes secondary steam generated in the mixed liquid evaporation first evaporation unit as a heat source, the mixed liquid evaporation third evaporation unit adopts an MVR evaporation process, the generated secondary steam is pressurized and heated by a mechanical compressor and then serves as a mixed liquid evaporation third evaporation unit heat source, and the mixed liquid evaporation fourth evaporation unit takes water vapor as a heat source.

The invention is realized by the following technical scheme.

A process for extracting soybean active ingredients by using a mixed solvent comprises the following steps:

s1, conveying the raw material soybeans into a pretreatment device by conveying equipment;

s2, conveying the prepreg into a leaching device by conveying equipment;

s3, conveying the wet protein into a desolventizing device by conveying equipment;

s4, conveying the protein particles into a crushing and packaging device by conveying equipment;

s5, conveying the leachate to a liquid distributor through conveying equipment after the leachate overflows from the immersed swelling leacher; standing the leachate in a liquid separator for 30-50 minutes, layering the mixed oil and the mixed liquid, and allowing the layered mixed oil and the layered mixed liquid to flow out from respective channels to form mixed oil containing 20-35% of soybean oil and mixed liquid containing 5-15% of oligosaccharide, wherein the mixed oil enters a mixed oil evaporation device, and the mixed liquid enters a mixed liquid evaporation device;

and S6, after the secondary steam generated by the devices in the steps S1-S5 is respectively used for waste heat, the generated non-condensable gas enters a gas condensation and recovery device.

As a further improvement of the above technical scheme, in step S1, the soybeans are first cleaned by a cleaning device to remove impurities, and the content of solid impurities is reduced to below 0.5%; heating the soybean subjected to impurity removal to 40-60 ℃ by heating equipment, and cracking the surface of the soybean; removing soybean hulls from the soybeans with cracked skins by using a huller, wherein the content of the soybean hulls is reduced to be below 0.5%; heating the peeled soybeans in heating equipment to 60-70 ℃, and keeping for hardening and tempering for 40-60 minutes; and extruding the soybean processed and tempered soybean into a soybean blank by a soybean processing and rolling machine, wherein the thickness of the soybean blank is 0.25-0.35 mm.

As a further improvement of the technical scheme, in step S2, the prepreg firstly enters an immersion type swelling and leaching device, and the immersion type swelling and leaching device is filled with a mixed solvent containing 20-35% of soybean oil, 5-15% of oligosaccharide and 40-60 ℃ to fill a swelling and leaching section of the swelling and leaching device; the prepreg is fully contacted with a mixed solvent consisting of a vegetable oil extraction solvent, ethanol and water in a swelling and leaching section, part of soybean oil in the prepreg is dissolved in the vegetable oil extraction solvent to form mixed oil, and protein in the prepreg is subjected to an alcohol change reaction when meeting ethanol, is changed from hydrophilicity to hydrophobicity, and absorbs water to swell; dissolving part of oligosaccharide in the prepreg in water to form a mixed solution; swelling and leaching the prepreg in an immersed swelling and leaching device for 10-60 minutes; the leachate formed by the mixed oil and the mixed liquid flows into a liquid separator for separation; the swelled prepreg enters a box chain type leacher to leach soybean oil and oligosaccharide, the leachate carries out countercurrent continuous spray leaching on the prepreg, a mixed solvent with the soybean oil content of 20-35%, the oligosaccharide content of 5-15% and the temperature of 40-60 ℃ is adopted at the feed end of the box chain type leacher to leach, and a fresh mixed solvent with the vegetable oil extraction solvent, ethanol and water in the ratio of 1:2:1 and the temperature of 40-60 ℃ is adopted at the discharge end of the box chain type leacher to carry out final leaching; the swelling and leaching time of the prepreg in the box chain type is 150-300 minutes; the leached solid material containing a certain mixed solvent forms wet protein and enters a desolventizing device.

As a further improvement of the technical scheme, in step S3, wet protein firstly enters a screw extruder, the moisture content of the wet protein is reduced from 65-70% to 55-58% through the extrusion and grinding action of a screw, the extruded extrusion liquid returns to a box-chain type leacher again, the extruded wet protein firstly enters a horizontal dryer, the desolventizing operation is carried out under the vacuum condition of-0.005-0.01 MPa, and the discharging temperature is about 70-80 ℃; the moisture content is 35-40%; after being dried by a horizontal dryer, wet protein enters a vertical dryer, the wet protein is uniformly spread on the disc surface of the vertical dryer by a layer of 2 cm per month, and is continuously stirred, the temperature is increased to 80-90 ℃, desolventization and dehydration are carried out under the vacuum state of-0.005-0.01 MPa, protein particles with water content of 4-8% are formed after drying, and the protein particles enter a crushing and packaging device.

As a further improvement of the technical scheme, in step S4, the protein particles are firstly cooled by wind and then sent to a crusher, the crushed protein particles are crushed into protein powder of 100 meshes by the crusher, the protein powder enters a packing scale to be packed, and finally the protein powder becomes a soybean protein concentrate product.

According to the technical scheme, the invention has the following advantages:

raw material soybeans enter a pretreatment device to be subjected to a series of treatments to form a prepreg (bean blank or puffed material) suitable for a leaching device; the prepreg enters a leaching device, the leached wet protein enters a desolventizing device to form protein particles, the leached oil and oligosaccharide leaching solution are separated by a liquid separator, and the vegetable oil extraction solvent containing the oil enters a mixed oil evaporation device to be subjected to MVR evaporation, negative pressure evaporation and steam stripping to form a soybean oil product; the ethanol water solution containing the oligosaccharide separated by the liquid separator enters a mixed solution evaporation device to be subjected to multi-effect evaporation, MVR evaporation and wiped film evaporation to obtain the soybean oligosaccharide product. The method has the advantages that the steam consumption and the power consumption are greatly reduced, the total steam consumption of the concentrated protein prepared from the soybeans is about 1300-1500 kg/t of protein, the power consumption is 280-320 wk.h/t of protein, the concentrated protein yield is 45-50%, compared with the total steam consumption of the concentrated protein prepared from the soybeans in the mainstream, the power consumption is reduced by 60%, and the concentrated protein yield is improved by 5-8%; the invention greatly optimizes and shortens the process for preparing the products such as soybean protein concentrate, soybean oil, soybean oligosaccharide and the like from soybeans, reduces the number of equipment, reduces the water vapor consumption and the power consumption, improves the product yield, saves the construction investment of equipment, land, factory buildings and the like, greatly reduces the production and operation cost of enterprises at the same time, and brings greater economic benefit for the enterprises.

Drawings

In order to more clearly illustrate the technical solution of the present invention, the drawings used in the description will be briefly introduced, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.

FIG. 1 is a schematic structural diagram of an embodiment of the present invention;

FIG. 2 is a schematic cross-sectional view of a submerged swelling extractor of the present invention;

FIG. 3 is a schematic plan view of a submerged swell extractor of the present invention;

FIG. 4 is a schematic cross-sectional view of the operation of the drive chain and the stripper plate of the present invention;

FIG. 5 is a schematic view of the plane of travel of the drive chain and the stripper plate of the present invention;

FIG. 6 is a schematic cross-sectional view of an overflow arrangement of the present invention;

FIG. 7 is a schematic diagram of the right-side view of the overflow device of the present invention;

FIG. 8 is a three-dimensional simulation of the drive chain of the present invention;

FIG. 9 is a three-dimensional simulation of a stripper plate of the present invention;

FIG. 10 is a three-dimensional simulation of the drive chain and material pushing plate combination of the present invention;

FIG. 11 is a three-dimensional simulation of the overflow arrangement of the present invention;

FIG. 12 is a schematic view of the evaporator of the present invention;

FIG. 13 is a three-dimensional simulated view of the evaporator of the present invention;

FIG. 14 is a three-dimensional simulation of the upper hose box of the present invention;

FIG. 15 is a three-dimensional simulation of an overflow weir-type distributor of the present invention;

FIG. 16 is a three-dimensional simulation of a porous flow pattern distributor of the present invention;

figure 17 is a schematic view of a tubular falling film evaporation apparatus of the present invention.

1. A feed pump; 2. a first heat exchanger; 3. a first evaporator A; 4. a first evaporator B; 5. a first flash box; 6, circulating the first pump; 7. a second heat exchanger; 8. a second evaporator A; 9. a second evaporator B; 10. a second flash tank; 11, a second circulating pump; 12. a third heat exchanger; 13. a heater; 14. a third evaporator A; 15. a third evaporator B; 16, a flash tank III; 17. a third circulating pump; 18. a mechanical compressor; 19. a wiped film evaporator; 20. a flash tank IV; a receiving tank; 22. a feed pump; 23. a circulation pipe; 24. a liquid inlet pipe; 25. a steam inlet pipe; 26. an evaporation tube; 27. a housing; 28. a lower tube plate; 29. a lower box body; 30. an upper box body; 31. an overflow weir-type distributor; 32. a porous flow pattern distributor; 33. an upper tube sheet; 34. a baffle plate; 35. a non-condensing tube; 36. a gas-liquid mixing pipe; 37. an arc-shaped plate; 38. a driven shaft; 39. a tail section; 40. a material pushing plate; 41. a drive chain; 42. a swelling extraction section; 43. a feed inlet; 44. a liquid inlet; 45. a curved section; 46. a draining section; 47. a nose section; 48. a transmission device; 49. a drive shaft; 50. a drive sprocket; 51. a discharge port; 52. an overflow device; 53. a partition plate; 54. a driven sprocket; 55, an upper cavity; 56. a vertical rib plate; 57. a housing; 58. a lower cavity; 59. filtering the plate; 60. an overflow port.

Detailed Description

In order to make the objects, features and advantages of the present invention more obvious and understandable, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings in the present embodiment, and it is apparent that the embodiments described below are only a part of embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the scope of protection of this patent.

Referring to fig. 1, in one aspect, the present invention provides an apparatus for extracting soybean active ingredients with a mixed solvent, comprising a pretreatment apparatus, a leaching apparatus, a desolventizing apparatus, a pulverizing and packaging apparatus, a mixed oil evaporation apparatus, a mixed liquid evaporation apparatus, and a gas condensation and recovery apparatus; the pretreatment device is connected with the leaching device, and the desolventizing device is connected with the leaching device; the crushing and packaging device is connected with the desolventizing device, and the mixed oil evaporation device and the mixed liquid evaporation device are connected with the leaching device through a liquid distributor; the gas condensation recovery device is used for recovering the non-condensable gas generated by the device. When in use, raw material soybeans enter a pretreatment device to be subjected to a series of treatments to form a prepreg (bean blank or puffed material) suitable for a leaching device; the prepreg enters a leaching device, the leached wet protein enters a desolventizing device to form protein particles, and the protein particles enter a crushing and packaging device to be crushed and packaged into a soybean protein concentrate product; separating the leached grease and oligosaccharide leaching solution by a liquid separator, wherein the vegetable oil extraction solvent containing the grease enters a mixed oil evaporation device to be subjected to MVR evaporation, negative pressure evaporation and steam stripping to obtain a soybean oil product; the ethanol water solution containing the oligosaccharide separated by the liquid separator enters a mixed solution evaporation device to be subjected to multi-effect evaporation, MVR evaporation and wiped film evaporation to obtain the soybean oligosaccharide product.

The leaching device comprises an immersed swelling leacher and a box chain type leacher; one end of the immersed swelling leacher is connected with the pretreatment device, and the other end of the immersed swelling leacher is connected with the box chain type leacher; the box chain type leacher is connected with the desolventizing device; when the device is used, the immersed swelling leacher is completely filled with the mixed solvent, the prepreg is completely immersed in the mixed solvent, the prepreg is fully contacted with the mixed solvent, meanwhile, part of soluble grease and oligosaccharide in the prepreg are dissolved in the mixed solvent, the leaching purpose is achieved (namely, protein, grease and oligosaccharide in the prepreg are simultaneously separated through mixed solvent immersion and spraying), and the leached wet protein enters a desolventizing device; the box-chain type leacher can improve the leaching rate and reduce the residue of effective components, and the leacher adopts a vacuum draining technology, so that the moisture content in wet protein is reduced, the energy required by drying the wet protein is reduced, the production and operation cost is reduced, the total investment of equipment and capital construction is reduced, and greater economic benefit is brought to enterprises.

Referring to fig. 2-11, the submerged swelling extractor comprises a machine head section 47, a draining section 46, a bending section 45, a swelling and extracting section 42, a closed space formed by a machine tail section 39, a transmission device 48 and a material pushing plate 40; the swelling and extracting section 42 is provided with a feed inlet 43 and a liquid inlet 44; a partition plate 53 is arranged in the swelling extraction section 42, and the swelling extraction section 42 and the draining section 46 are divided into an upper cavity 55 and a lower cavity 58; the material pushing plate 40 is arranged in the immersed swelling extractor and is driven by the transmission device 48, and the lower part of the draining section 46 is provided with a discharge hole 51. The immersed swelling extractor enters the lower cavity along the upper cavity in a closed space, so that the swelling time is prolonged; the swelling extraction section 42 and the tail section 39 are completely filled with ethanol water solution, the soybean meal is completely immersed in the ethanol water solution, the soybean meal is fully contacted with the ethanol water solution and is completely swelled, and meanwhile, part of soluble oligosaccharide in the soybean meal is dissolved in the ethanol water solution, so that the purpose of extraction is achieved.

The transmission device 48 comprises a driven shaft 38, a transmission chain 41, a driving shaft 49, a driving chain wheel 50 and a driven chain wheel 54; the driven shaft 38 and the driven chain wheel 54 are arranged on the tail section 39, and the driving shaft 49 and the driving chain wheel 50 are arranged on the head section 47; the driven sprocket 54 and the driving sprocket 50 are linked through the transmission chain 41, and the transmission chain 41 is connected with the material pushing plate 40; the driven shaft 38, the material pushing plate 40, the transmission chain 41, the driving shaft 49, the driving chain wheel 50 and the driven chain wheel 54 form a complete reciprocating operation system to push the bean pulp to move; the transmission chain 41 is connected with the material pushing plate 40 by the vertical rib plate 56, so that on one hand, the connection strength can be increased, and on the other hand, the material pushing plate 40 is convenient to disassemble and assemble.

The material pushing plate 40 is provided with a plurality of through holes, so that circulation of ethanol water is facilitated.

The curved section 45 is provided with an overflow device 52, which overflow device 52 is provided with a filter plate 59 and an overflow 60. When the device is used, after the ethanol water solution in the swelling and extracting section 42 is filled, the excessive ethanol water solution can be discharged from an overflow port 60 of the overflow device 52, and a filter plate 59 arranged on the overflow device 52 ensures that the overflowing liquid does not contain large particles, and is preferably detachable; meanwhile, a back washing device (not shown in the drawing) is arranged on the overflow pipe device to carry out back washing on the filter plates 59 periodically so as to ensure that the filter plates 59 are not blocked.

The inclination angle between the draining section 46 and the horizontal direction is 10-60 degrees, so that the ethanol water solution in the swelling extraction section 42 can not flow out from the discharge hole 51, and meanwhile, the free ethanol water solution in the bean pulp can be separated from the bean pulp under the action of gravity.

The tail section 39 is provided with an arc-shaped plate 37 to prevent the tail section 39 from storing materials.

The desolventizing device comprises a screw extruder, a horizontal desolventizing machine and a vertical desolventizing machine; one end of the screw extruder is connected with the box chain type leacher, the other end of the screw extruder is connected with the horizontal desolventizing machine, and the vertical desolventizing machine is respectively connected with the horizontal desolventizing machine and the crushing and packaging device; when the device is used, the liquid extruded by the screw extruder replaces part of the fresh mixed solvent to be sprayed into the leacher, the using amount of the fresh mixed solvent is reduced, energy is saved, the protein particles are formed by dehydrating the liquid by the screw extruder and drying the liquid by the horizontal dryer and the vertical dryer, and the protein particles enter the crushing and packaging device.

The crushing and packaging device comprises a crusher and a packaging machine; one end of the pulverizer is connected with the vertical desolventizing machine, the other end of the pulverizer is connected with the packaging machine, and the pulverizing and packaging device is pulverized and packaged into a soybean protein concentrate product.

The mixed oil evaporation device comprises a mixed oil evaporation first evaporation unit, a mixed oil evaporation second evaporation unit and a mixed oil evaporation third evaporation unit; the mixed oil evaporation first evaporation unit adopts an MVR evaporation process, secondary steam generated by the MVR evaporation first evaporation unit is used as a heat source of a mixed oil evaporation second evaporation unit after being pressurized and heated by a mechanical compressor, the mixed oil evaporation second evaporation unit adopts a climbing film evaporator, and water vapor is used as a heat source to evaporate under certain vacuum; the third evaporation unit for evaporating the mixed oil adopts a plate-type stripping tower, the steam partial pressure replaces the steam partial pressure of the vegetable oil extraction solvent under certain vacuum, the vegetable oil extraction solvent in the mixed oil is easier to evaporate, and the purpose of removing the residual vegetable oil extraction solvent in the soybean oil is achieved.

The mixed liquid evaporation device comprises a mixed liquid first evaporation unit, a mixed liquid second evaporation unit, a mixed liquid third evaporation unit and a mixed liquid fourth evaporation unit; the mixed liquor first evaporation unit takes secondary steam generated in a wet protein drying process as a heat source, the mixed liquor second evaporation unit takes secondary steam generated in the mixed liquor first evaporation unit as a heat source, the mixed liquor third evaporation unit adopts an MVR evaporation process, the generated secondary steam is pressurized and heated by a mechanical compressor to serve as a heat source of the mixed liquor third evaporation unit, and the mixed liquor fourth evaporation unit takes water vapor as a heat source; the evaporators of the mixed liquid first evaporation unit, the mixed liquid second evaporation unit and the mixed liquid third evaporation unit all adopt two-section tubular falling film evaporators; the mixed liquid evaporation device ensures that the mixed liquid and a high-temperature heat source exchange heat fully, and improves the heat efficiency; the temperature difference between the high-temperature heat source and the dilute syrup is small, the liquid distribution of the evaporation tube is uniform, and the syrup is not easy to be pasted and hung on the wall.

Referring to fig. 12-17, in the above embodiment, the two-stage tube type falling film evaporator includes a shell 27, and a liquid inlet tube 24, an air inlet tube 25, an evaporation tube 26, a lower tube plate 28, a lower tank 29, an upper tank 30, a liquid distributor, an upper tube plate 33, a baffle plate 34, a noncondensable gas tube 35, and a gas-liquid mixing tube 36 provided on the shell 27; the liquid inlet pipe 24 is arranged on one side of the upper part of the shell 27 and is communicated with the upper box body 30, and the liquid distributor is arranged on the lower part of the upper box body 30 and is positioned on the upper part of the upper tube plate 33; the gas inlet pipe 14 is arranged at one side of the shell 27 and located at the lower part of the upper tube plate 33, the lower tube plate 28 is arranged at the lower part of the shell 27, the lower box body 29 is arranged at the bottom of the shell 27 and located at the lower part of the lower tube plate 28, the baffle plates 34 are provided in a plurality of numbers, the baffle plates 34 are uniformly distributed between the upper tube plate 33 and the lower tube plate 28, the noncondensable gas pipe 35 is arranged at one side of the shell 27 and located at the upper part of the lower tube plate 28, the gas-liquid mixing pipe 36 is arranged at one side of the shell 27 and connected with the lower box body 29, the upper part of the evaporation pipe 26 is connected with the upper tube plate 33, and the lower part of the evaporation pipe 26 is connected with the lower; the top of the shell 27 is also provided with a circulating pipe 23, and the circulating pipe 23 is connected with the upper tank 30.

In the above embodiment, the liquid distributor includes the weir-type distributor 31 and the porous flow-type distributor 32; the overflow weir type distributor 31 is disposed at the lower portion of the upper tank 30, the perforated flow type distributor 32 is disposed at the lower portion of the overflow weir type distributor 31, and the upper tube plate 33 is disposed at the lower portion of the perforated flow type distributor 32.

When the tubular falling-film evaporator is used, dilute syrup as a raw material enters an upper box body 30 of the evaporator from a liquid inlet pipe 24, the dilute syrup is firstly distributed by an overflow weir-type distributor 31, then falls into a porous flow-type distributor 32 for distribution again, finally falls onto an upper tube plate 33 of the evaporation tube, and uniformly flows into the inner surface of the evaporation tube 26 for evaporation; the dilute syrup on the inner surface of the evaporation tube 26 and a high-temperature heat source entering the evaporator shell 27 from the steam inlet tube 25 of the evaporator carry out partition wall heat exchange, and the ethanol and the water in the dilute syrup are vaporized by heat absorption to form steam; the vapor-liquid mixture formed by evaporation enters the next process from the vapor-liquid mixing pipe 36 of the evaporator lower box body 29; the lower box 29 can temporarily store part of the syrup, and the circulating pump 11 sends part of the syrup to the upper box 30 of the evaporator through the circulating pipe 23 to perform forced circulation evaporation; the high-temperature heat source entering the evaporator shell 27 is discharged from the non-condensable gas pipe 24 after fully exchanging heat with the thin syrup in the evaporation pipe 26 through the plurality of baffle plates 34 in the shell 27, and the gas enters the next process, so that the liquid of the evaporation pipe 26 is uniformly distributed, the thin syrup and the high-temperature heat source fully exchange heat, the heat efficiency is improved, and the syrup is not easy to be pasted and hung on the wall.

In the above embodiment, the first evaporation unit includes the feed pump 1, the heat exchanger one 2, the first evaporator a3, the first evaporator B4, the flash tank one 5, the circulation pump one 6; the feed pump 1 is connected with the first heat exchanger 2, the shell of the first evaporator A3 is communicated with the shell of the first evaporator B4 through an intermediate connecting pipe and forms a series structure, and the tube side of the first evaporator A3 is communicated with the tube side of the first evaporator B4 through an intermediate connecting pipe and forms a series structure; in order to realize the purpose that the first evaporator A3 and the first evaporator B4 share one flash box I5 and make the layout more compact, the tube side of the first evaporator B4 is communicated with the flash box I5 through an intermediate connecting pipe to form a series structure; the shell of the first heat exchanger 2 is communicated with the shell of the first evaporator B4 through a middle connecting pipe to form a series structure, so that non-condensable gas of the evaporator is heated by dilute syrup before evaporation; one side of the first circulation pump 6 is communicated with the first evaporator B4, and the other side of the first circulation pump 6 is respectively connected with the first evaporator A3 and the second evaporation unit.

The second evaporation unit comprises a second heat exchanger 7, a second evaporator A8, a second evaporator B9, a second flash tank 10 and a second circulating pump 11; one side of the second heat exchanger 7 is connected with the first circulation pump 6, the other side of the second heat exchanger 7 is connected with the second evaporator A8, the shell of the second evaporator A8 is communicated with the shell of the second evaporator B9 through an intermediate connecting pipe to form a series structure, and the tube side of the second evaporator A8 is communicated with the tube side of the second evaporator B9 through an intermediate connecting pipe to form a series structure; in order to realize the purpose that two evaporators of the second evaporator A8 and the second evaporator B9 share the second flash box 10, the layout of the second flash box is more compact, and the tube side of the second evaporator B9 is communicated with the second flash box 10 through an intermediate connecting pipe to form a series structure; the shell of the second heat exchanger 7 is communicated with the shell of the second evaporator B9 through a middle connecting pipe to form a series structure, so that the non-condensable gas of the evaporator is heated by the dilute syrup before evaporation; one side of the second circulating pump 11 is communicated with the second evaporator B9, and the other side of the second circulating pump 11 is respectively connected with the second evaporator A8 and the third evaporation unit.

The third evaporation unit comprises a heat exchanger III 12, a heater 13, a third evaporator A14, a third evaporator B15, a flash tank III 16, a circulating pump III 17 and a mechanical compressor 18; one side of the heat exchanger III 12 is connected with the circulating pump II 11, the other side of the heat exchanger III 12 is connected with the heater 13, the heater 13 is connected with the third evaporator A14, the shell of the third evaporator A14 is communicated with the shell of the third evaporator B15 through an intermediate connecting pipe and forms a series structure, and the tube side of the third evaporator A14 is communicated with the tube side of the third evaporator B15 through an intermediate connecting pipe and forms a series structure; in order to realize the purpose that the third evaporator A14, the third evaporator B15 and two evaporators share one flash box III 16 and make the layout more compact, the tube side of the third evaporator B15 is communicated with the flash box III 16 through an intermediate connecting pipe and forms a series structure; the shell of the heat exchanger III 12 is communicated with the shell of the third evaporator B15 through a middle connecting pipe to form a series structure, so that the non-condensable gas of the evaporator is heated by the dilute syrup before evaporation; the mechanical compressor 18 is respectively connected with the third evaporator A14 and the flash tank III 16, one side of the circulating pump III 17 is communicated with the third evaporator B15, and the other side of the circulating pump III 11 is respectively connected with the third evaporator A14 and the fourth evaporation unit.

The fourth evaporation unit comprises a wiped film evaporator 19, a flash tank four 20, a receiving tank 21, a feed pump 22; one side of the wiped film evaporator 19 is connected with the third circulating pump 17, the flash tank IV 20 and the receiving tank 21 are respectively connected with the wiped film evaporator 19, and the feeding pump 22 is connected with the receiving tank 21.

The soybean extraction device with the mixed solvent ensures the sufficient heat exchange of a high-temperature heat source, and improves the heat efficiency; the liquid of the evaporation pipe is uniformly distributed, and is not easy to be pasted and hung on the wall.

The second aspect of the invention provides a process for extracting soybean active ingredients by using a mixed solvent, which comprises the following steps:

s1, conveying the raw material soybeans into a pretreatment device by conveying equipment; firstly, cleaning soybeans by cleaning equipment to remove impurities, and reducing the content of solid impurities to be below 0.5%; heating the soybean subjected to impurity removal to 40-60 ℃ by heating equipment, and cracking the surface of the soybean; removing soybean hulls from the soybeans with cracked skins by using a huller, wherein the content of the soybean hulls is reduced to be below 0.5%; heating the peeled soybeans in heating equipment to 60-70 ℃, and keeping for hardening and tempering for 40-60 minutes; extruding the soybean processed and tempered soybean into a soybean blank by a soybean processing and rolling machine, wherein the thickness of the soybean blank is 0.25-0.35 mm; according to different purposes of the soybean protein concentrate product, the bean blank can be expanded into a porous expanded material by an expander, and the bean blank or the expanded material is used as a prepreg and enters a subsequent leaching device for continuous processing;

s2, conveying the prepreg into a leaching device by conveying equipment; the method comprises the following steps of firstly, enabling prepreg to enter an immersed swelling and leaching device, and filling a mixed solvent with the soybean oil content of 20-35%, the oligosaccharide content of 5-15% and the temperature of 40-60 ℃ in the immersed swelling and leaching device to fill a swelling and leaching section of the swelling and leaching device; the prepreg is fully contacted with a mixed solvent consisting of a vegetable oil extraction solvent, ethanol and water in a swelling and leaching section, part of soybean oil in the prepreg is dissolved in the vegetable oil extraction solvent to form mixed oil, and protein in the prepreg is subjected to an alcohol change reaction when meeting ethanol, is changed from hydrophilicity to hydrophobicity and is simultaneously swollen by absorbing water; dissolving part of oligosaccharide in the prepreg in water to form a mixed solution; swelling and leaching the prepreg in an immersed swelling and leaching device for 10-60 minutes; the leachate formed by the mixed oil and the mixed liquid flows into a liquid separator for separation; the swelled prepreg enters a box chain type leacher to leach soybean oil and oligosaccharide, the leachate carries out countercurrent continuous spray leaching on the prepreg, a mixed solvent with the soybean oil content of 20-35% and the oligosaccharide content of 5-15% at the feed end of the box chain type leacher is used for leaching, and a fresh mixed solvent with the vegetable oil extraction solvent, ethanol and water being 1:2:1 at the temperature of 40-60 ℃ is used for final leaching at the discharge end of the box chain type leacher; the swelling and leaching time of the prepreg in the box chain type is 150-300 minutes; wet protein formed by the leached solid material containing a certain mixed solvent enters a desolventizing device;

s3, conveying the wet protein into a desolventizing device by conveying equipment; wet protein firstly enters a screw extruder, the moisture content of the wet protein is reduced from 65-70% to 55-58% through the extrusion and grinding effects of a screw, so that the load of subsequent drying equipment is reduced, the desolventizing time is shortened, the thermal denaturation of the protein is reduced, meanwhile, the wet protein is changed into small particles from flakes (expanded materials are formed into small particles from large particles), the surface area is increased, and the ethanol is conveniently removed; the extruded extrusion liquid returns to the box-chain type leacher again to replace part of fresh mixed solvent, so that energy is saved; the extruded wet protein firstly enters a horizontal dryer, the materials in the horizontal dryer are continuously tumbled, and the continuous short-time contact with a drying disc is realized, so that the problem of color change caused by long-time contact is avoided, and the drying and desolventizing effects are improved; the desolventizing operation is carried out under a vacuum condition (-0.005 to-0.01 MPa), so that the boiling point of the ethanol solution can be reduced, and the thermal denaturation of the protein can be reduced. Ethanol and water in the wet protein are effectively removed through the operations, and the discharging temperature is about 70-80 ℃; the moisture content is about 35-40%; after being dried by a horizontal dryer, wet protein enters a vertical dryer, the wet protein is uniformly spread on a layer of tray surface of the vertical dryer by 2 cm per month, and is continuously stirred, the temperature is raised to 80-90 ℃, desolventization and dehydration are carried out under the vacuum (-0.005-0.01 MPa) state, protein particles with water content of 4-8% are formed after drying, and the protein particles enter a crushing and packaging device; secondary steam generated by the horizontal dryer and the vertical dryer is all used for a high-temperature heat source of a first evaporation unit in the mixed liquid evaporation device, non-condensable gas after full utilization is sent to a condenser for condensation, and condensate is recycled;

s4, conveying the protein particles into a crushing and packaging device by conveying equipment; the method comprises the following steps of (1) conveying protein particles into an ultrafine grinder after air cooling, grinding the protein particles into protein powder of 100 meshes by the ultrafine grinder, and packing the protein powder into a package scale to obtain a soybean protein concentrate product;

s5, conveying the leachate to a liquid distributor through conveying equipment after the leachate overflows from the immersed swelling leacher; the leaching solution mainly comprises five liquids of a vegetable oil extraction solvent, soybean oil, ethanol, water, soybean oligosaccharide and the like, wherein the vegetable oil extraction solvent and the soybean oil are mutually dissolved to form mixed oil, the ethanol, the water and the soybean oligosaccharide are mutually dissolved to form mixed liquid, the mixed oil and the mixed liquid are layered due to different densities after standing for a period of time, and the liquid distributor is designed by utilizing the properties of the mixed oil and the mixed liquid; standing the leachate in a liquid separator for 30-50 minutes, layering the mixed oil and the mixed liquid, and allowing the layered mixed oil and the layered mixed liquid to flow out from respective channels to form mixed oil containing 20-35% of soybean oil and mixed liquid containing 5-15% of oligosaccharide, wherein the mixed oil enters a mixed oil evaporation device, and the mixed liquid enters a mixed liquid evaporation device;

feeding the mixed oil containing 20-35% of soybean oil and being at the temperature of 40-60 ℃ into a mixed oil evaporation device; the mixed oil firstly enters a mixed oil first evaporation unit for evaporation concentration, the starting heat source for evaporation is water vapor, once evaporation is stable, secondary vapor generated by evaporation is pressurized by a mechanical compressor and heated to 80-90 ℃, and then is sent to the shell pass of the mixed oil first evaporation unit to serve as the heat source of the mixed oil first evaporation unit to support the evaporation concentration of the mixed oil first evaporation unit; the evaporation temperature of the first evaporation unit of the mixed oil is 60-70 ℃, and the vacuum degree is 0.0-minus 0.02 MPa; the non-condensable gas of the mixed oil first evaporation unit is sent to a gas condensation recovery device for condensation recovery; after being concentrated by the first mixed oil evaporation unit, the mixed liquid with the concentration of 50-70% and the temperature of 70-80 ℃ enters the second mixed oil evaporation unit and is continuously concentrated; the mixed oil with the concentration of 50-70% and the temperature of 70-80 ℃ enters a second mixed oil evaporation unit for evaporation and concentration, and the evaporation heat source is water vapor; the evaporation temperature is 100-110 ℃, the vacuum degree is-0.04 to-0.06 MPa, and secondary steam generated by evaporation is sent to a gas condensation recovery device for condensation recovery; after concentration, the mixed oil with the concentration of 85-95% enters a third mixed oil evaporation unit, and concentration is continued; the mixed oil with the concentration of 95-98% and the temperature of 100-110 ℃ enters a third mixed oil evaporation unit for evaporation concentration; the vacuum degree of a third evaporation unit of the mixed oil is-0.06 to-0.08 MPa, the evaporation temperature is 110 to 120 ℃, a certain amount of water vapor is introduced into the mixed oil, the partial pressure of the vapor of the vegetable oil extraction solvent is replaced by the partial pressure of the water vapor, the vegetable oil extraction solvent in the mixed oil is easier to evaporate, and the purpose of removing the residual vegetable oil extraction solvent in the soybean oil is achieved; secondary steam generated by evaporation is removed to a gas condensation recovery device for condensation recovery; concentrating to obtain soybean oil with the concentration of 99.5-99.9%, wherein the soybean oil can be eaten after being refined;

s6, feeding the mixed solution containing 5-15% of oligosaccharide into a mixed solution evaporation device; the mixed solution is firstly sent into a first mixed solution evaporation unit for evaporation concentration, the evaporation heat source is 90-110 ℃ secondary steam generated in the wet protein drying process, the evaporation temperature is 70-80 ℃, the vacuum degree is 0-minus 0.03MPa, and the secondary steam generated by evaporation is used as a heat source of a second evaporation unit and enters the shell side of the second mixed solution evaporation unit; the mixed solution with the concentration of 12-15% and the temperature of 70-80 ℃ enters a second evaporation unit of the mixed solution and is continuously concentrated; the mixed solution enters a second mixed solution evaporation unit for evaporation and concentration, and an evaporation heat source is secondary steam of 70-80 ℃ generated by evaporation of the first mixed solution evaporation unit; the evaporation temperature is 45-55 ℃, the vacuum degree is-0.060-0.08 MPa, and secondary steam generated by evaporation is sent to a gas condensation recovery device for condensation recovery; the concentrated mixed solution with the concentration of 25-35% enters a third evaporation unit of the mixed solution, and concentration is continued; the mixed solution with the concentration of 25-35% enters a third mixed solution evaporation unit for evaporation concentration, the mixed solution is firstly heated to 70-80 ℃, then enters an evaporator for evaporation concentration, the starting heat source for evaporation is water vapor, once evaporation is stable, secondary vapor generated by evaporation is pressurized by a mechanical compressor and heated to 90-100 ℃, and then is sent to the shell side of the third mixed solution evaporation unit to serve as the heat source of the third mixed solution evaporation unit to support evaporation of the third mixed solution evaporation unit; the evaporation temperature of the third evaporation unit of the mixed solution is 70-80 ℃, the vacuum degree is 0.0-minus 0.02MPa, and the non-condensable gas generated by evaporation is sent to a gas condensation recovery device for condensation recovery; the concentrated mixed solution with the concentration of 45-55% enters a fourth evaporation unit of the mixed solution, and the concentration of syrup is adjusted; the mixed solution with the concentration of 45-55% and the temperature of 70-80 ℃ enters a fourth evaporation cost of the mixed solution for evaporation concentration, the heat source of evaporation is water vapor, the evaporation temperature is 55-65 ℃, the vacuum degree is-0.08-0.10 MPa, and the non-condensable gas generated by evaporation is sent to a gas condensation recovery device for condensation recovery; feeding the concentrated oligosaccharide with the concentration of 55-60% into an oligosaccharide storage tank to form an oligosaccharide product for long-term storage;

s7, after the secondary steam generated by all the devices in the steps S1-S6 is subjected to respective waste heat utilization, the generated non-condensable gas enters a gas condensation recovery device; the method comprises the following steps that non-condensable gas firstly enters shell passes of respective condensers, circulating cooling water with the temperature of 20-30 ℃ is introduced into the tube passes of the condensers, the non-condensable gas and the circulating cooling water are subjected to heat exchange through heat exchange tubes, and condensable parts in the non-condensable gas are condensed into liquid with the temperature of 40-50 ℃ for recycling;

the liquid at 40-50 ℃ generated in the step of S7 is a vegetable oil extraction solvent and an ethanol water solution respectively, and the optimal fresh mixed solvent ratio in production practice is that the vegetable oil extraction solvent is ethanol and water is 1:2: 1.

The method has the advantages that the steam consumption and the power consumption are greatly reduced, the total steam consumption of the concentrated protein prepared from the soybeans is about 1300-1500 kg/t of protein, the power consumption is 280-320 wk.h/t of protein, the concentrated protein yield is 45-50%, compared with the total steam consumption of the concentrated protein prepared from the soybeans in the mainstream, the power consumption is reduced by 60%, and the concentrated protein yield is improved by 5-8%; the invention greatly optimizes and shortens the process for preparing the products such as soybean protein concentrate, soybean oil, soybean oligosaccharide and the like from soybeans, reduces the number of equipment, reduces the water vapor consumption and the power consumption, improves the product yield, saves the construction investment of equipment, land, factory buildings and the like, greatly reduces the production and operation cost of enterprises, and brings greater economic benefit for the enterprises.

The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other.