System for producing transparent soybean concentrated phospholipid with soybean oil foot as raw material

Abstract

The utility model discloses a system for producing transparent soybean concentrated phospholipid with soybean oil foot as raw material, soybean oil foot and hydrogen peroxide enter first static mixer, and the mixed discharge is into phospholipid storage tank through oil foot conditioning tank, the tube of first phospholipid dryer, first phospholipid temporary storage tank, first phospholipid pump, first phospholipid cooler, the outlet of phospholipid storage tank and n-hexane pipe is connected to second static mixer, and the outlet of second static mixer is connected with washing tank and settling tank, the light phase outlet of settling tank is connected with light phase pump, clear liquid tank, second mixed liquid pump and the top inlet of falling film evaporator, and the bottom outlet of falling film evaporator is connected with the tube inlet of second phospholipid dryer, the tube outlet of second phospholipid dryer is connected with stripping tank through second phospholipid temporary storage tank, fourth phospholipid pump, second phospholipid cooler, and the bottom outlet of stripping tank is connected with transparent phospholipid output pipe. The concentrated phospholipid obtained by the system has high transparency and light color, and the utilization value of soybean oil foot is greatly improved.

Description

Technical Field

[0001] This utility model relates to a system for producing transparent soybean concentrated phospholipids, and more particularly to a system for producing transparent soybean concentrated phospholipids using soybean oil residue as raw material, belonging to the field of resource comprehensive utilization technology. Background Technology

[0002] Phospholipids are a class of lipid compounds with a unique amphiphilic structure, whose molecules consist of hydrophilic phosphate groups and hydrophobic fatty acid chains. As a core component of biological membranes, phospholipids play a crucial role in life activities and industrial applications. Adults need to ingest 3-5g of phospholipids daily. Phospholipid deficiency can lead to decreased membrane fluidity, delayed nerve conduction, and lipid metabolism disorders.

[0003] Soybean oil residue is an important byproduct of soybean oil processing. Most domestic processes for processing soybean oil residue involve: mixing and conditioning with vegetable oil, dehydrating under negative pressure in a thin-film evaporator, and cooling with a heat exchanger. The crude phospholipids obtained from this process are dark in color and have poor transparency, generally used as feed-grade phospholipids. When used as food-grade phospholipids, the product has poor sensory qualities, significantly reducing the value of soybean oil residue.

[0004] To improve the transparency of concentrated phospholipids, Chinese patent application CN108003187A discloses "a method for preparing transparent membrane concentrated soybean phospholipids". This technical solution uses feed-grade concentrated soybean phospholipids as raw materials, dissolves them with non-polar substances, and produces highly transparent concentrated soybean phospholipids through steps such as centrifugation for pre-removal of impurities, filter cake layer filtration, further centrifugation separation, and solvent removal. This process has many steps and the cost of industrial production is relatively high.

[0005] Chinese patent application CN111892623A discloses "a transparent phospholipid and its preparation method." The method involves mixing phospholipids with vegetable oil and then using a specialized filtration system—either a gravity filter, vacuum filter, pressure filter, or precision filter—in single or combined filtration units to produce a clear and transparent phospholipid product. This process uses vegetable oil as the solution, rather than a non-polar solvent, effectively avoiding solvent residue in the phospholipids and improving product safety. However, the use of filter aids can lead to the removal of some phospholipids and vegetable oil, resulting in low yields of concentrated phospholipids and low vegetable oil recovery rates.

[0006] Chinese patent CN115850325A discloses "a method for preparing high-quality transparent soybean lecithin", which is a process for preparing transparent soybean concentrated lecithin using a non-polar / polar dual solvent system. The soybean concentrated lecithin obtained by this process has a light color and good transparency, but it has the problems of the small difference between the boiling points of n-hexane and ethanol, which makes it easy to azeotropically react and the low purity of the recovered solvent.

[0007] Chinese patent CN114605467A discloses a method for preparing transparent phospholipids, which involves treatment with protease and glucosylamylase, solvent dissolution, protein adsorption, and centrifugal concentration to obtain transparent soybean concentrated phospholipids. This process can greatly improve the transparency of concentrated phospholipids, but the enzyme preparations are expensive and difficult to reuse multiple times. Therefore, this process is generally applicable to the pharmaceutical field. Utility Model Content

[0008] The purpose of this section is to outline some aspects of embodiments of the present invention and to briefly describe some preferred embodiments. Simplifications or omissions may be made in this section, as well as in the abstract and title of this application, and such simplifications or omissions should not be construed as limiting the scope of the present invention.

[0009] In view of the problems existing in the above and / or prior art, this utility model is proposed.

[0010] The purpose of this invention is to solve the problem that the concentrated phospholipids produced from soybean oil residue in the current market are dark in color, have poor transparency, and poor sensory quality. The invention provides a system for producing transparent soybean concentrated phospholipids from soybean oil residue. The process is simple, and the resulting concentrated phospholipids have high transparency, light color, and high sensory quality, which greatly improves the utilization value of soybean oil residue.

[0011] To solve the above technical problems, this utility model provides a system for producing transparent soybean concentrated phospholipids using soybean oil residue as raw material. The system includes a soybean oil residue feeding pipe, which, along with a hydrogen peroxide pipe, is connected to the inlet of a first static mixer. The outlet of the first static mixer is connected to the tube-side inlet of a first phospholipid dryer via an oil residue conditioning tank. The tube-side outlet of the first phospholipid dryer is sequentially connected to the inlet of a phospholipid storage tank via a first phospholipid temporary storage tank, a first phospholipid pump, and a first phospholipid cooler. The outlets of the phospholipid storage tank and the n-hexane pipe are both connected to a second static mixer. The inlet and outlet of the second static mixer are connected sequentially to the inlet of the settling tank via a washing tank and a first mixing pump. The light phase outlet of the settling tank is connected sequentially to the top inlet of the falling film evaporator via a light phase pump, a clear liquid tank, and a second mixing pump. The bottom outlet of the falling film evaporator is connected to the tube-side inlet of the second phospholipid dryer via a third phospholipid pump. The tube-side outlet of the second phospholipid dryer is connected sequentially to the upper inlet of the stripping tank via a second phospholipid storage tank, a fourth phospholipid pump, and a second phospholipid cooler. The bottom outlet of the stripping tank is connected to the transparent phospholipid output pipe.

[0012] Furthermore, the heavy phase outlet of the settling tank is connected to the inlet of the heavy phase pump, the outlet of the heavy phase pump is connected to the inlet of the heavy phase tank, and the bottom outlet of the heavy phase tank is connected to the hexane insoluble matter output pipe.

[0013] Furthermore, the outlet of the hexane insoluble matter output pipe is connected to the head end of the leachate extractor.

[0014] Furthermore, the vacuum port of the falling film evaporator is connected to the vacuum tube; the gas phase outlet of the first phospholipid dryer is connected to the middle inlet of the first liquid-liquid separator, and the bottom outlet of the first liquid-liquid separator is connected to the feed port of the oil foot conditioning tank through the first liquid-liquid receiving tank and the phospholipid return pipe.

[0015] Furthermore, the top exhaust port of the first liquid separator is connected to the shell-side inlet of the vacuum condenser, the tube side of the vacuum condenser is connected to the cooling water pipe, and the shell-side exhaust port of the vacuum condenser is connected to the vacuum pumping pipe.

[0016] Furthermore, the gas phase outlet of the second phospholipid dryer is connected to the middle inlet of the second liquid foam separator, the bottom outlet of the second liquid foam separator is connected to the inlet of the second liquid foam receiving tank, and the outlet of the second liquid foam receiving tank is connected to the feed port of the oil foot conditioning tank through the phospholipid reflux pipe; the top exhaust port of the second liquid foam separator is connected to the vacuum pipe.

[0017] Furthermore, the nitrogen inlet at the conical bottom of the stripping tank is connected to the outlet of the nitrogen pipe; the top exhaust port of the stripping tank is connected to the middle inlet of the third liquid foam separator; the bottom outlet of the third liquid foam separator is connected to the top reflux port of the stripping tank; and the top outlet of the third liquid foam separator is connected to the vacuum pipe.

[0018] Furthermore, the oil residue conditioning tank, washing tank, and stripping tank are all equipped with hot water coils, with the inlet of the hot water coil connected to the hot water inlet pipe and the outlet connected to the hot water outlet pipe.

[0019] Furthermore, the shell-side inlets of the first phospholipid dryer, the falling film evaporator, and the second phospholipid dryer are connected to a steam pipe, and the shell-side condensate outlet is connected to a condensate discharge pipe.

[0020] Furthermore, the shell-side inlets of the first and second phospholipid coolers are connected to the cooling water inlet pipe, and the shell-side outlets of the first and second phospholipid coolers are connected to the cooling water outlet pipe.

[0021] Compared with the prior art, the advantages or beneficial effects of this utility model include at least the following: 1. The price of phospholipids obtained from soybean oil residue processed using traditional methods is 10,000 yuan / ton, while the price of transparent phospholipids obtained using this system is 20,000 yuan / ton. Based on a transparent phospholipid plant with a production capacity of 20 TPD and 300 processing days per year, the annual additional revenue is 1 * 20 * 300 = 60 million yuan.

[0022] 2. The transparent phospholipids produced by this process have high light transmittance, a light amber color, and high sensory quality, making them suitable for high-end foods. Attached Figure Description

[0023] To more clearly illustrate the technical solutions of the embodiments of this utility model, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. The drawings are provided for reference and illustration only and are not intended to limit this utility model. Wherein: Figure 1 This invention provides a systematic process for producing transparent soybean concentrated phospholipids from soybean oil residue. Figure 1 ; Figure 2 This invention provides a systematic process for producing transparent soybean concentrated phospholipids from soybean oil residue. Figure 2 ; Figure reference numerals: First static mixer E1; Oil foot conditioning tank E2; First phospholipid dryer E3; Second static mixer E4; Washing tank E5; Falling film evaporator E6; Second phospholipid dryer E7; Stripping tank E8; Hydrogen peroxide tank T1; First phospholipid temporary storage tank T2; First liquid separator T3; First liquid receiving tank T4; Phospholipid storage tank T5; First settling tank T6; Second settling tank T7; Heavy phase tank T8; Clear liquid tank T9; Second phospholipid temporary storage tank T10; Second liquid separator T11; Second liquid receiving tank T12; Third liquid separator T13; First phospholipid cooler H1; Vacuum condenser H2; Second phospholipid cooler H3; Oil foot feed pump P1.; First phospholipid pump P2.; Second phospholipid pump P3.; First mixed liquid pump P4.; Heavy phase pump P5.; Light phase pump P6.; Second mixed liquid pump P7.; Third phospholipid pump P8.; Fourth phospholipid pump P9.; Transparent phospholipid transfer pump P10.; Hydrogen peroxide pump P11. Soybean oil feed pipe G1; Hot water inlet pipe G2; Hot water outlet pipe G3; Steam pipe G4; Condensate discharge pipe G5; Cooling water inlet pipe G6; Cooling water outlet pipe G7; Phospholipid return pipe G8; Vacuum pipe G9; Hexane pipe G10; Nitrogen pipe G11; Transparent phospholipid output pipe G12; Hexane insoluble matter output pipe G13. Detailed Implementation

[0024] In the following description of this utility model, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this utility model and simplifying the description, and do not mean that the device must have a specific orientation.

[0025] To make the technical means, creative features, achieved objectives and effects of this utility model easier to understand, the present utility model will be further described below with reference to specific illustrations. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments.

[0026] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

[0027] like Figure 1 , Figure 2 As shown, the system for producing transparent soybean concentrated phospholipids from soybean oil residue according to this invention includes a first static mixer E1, an oil residue conditioning tank E2, a first phospholipid dryer E3, a second static mixer E4, a washing tank E5, a falling film evaporator E6, a second phospholipid dryer E7, and a stripping tank E8. The outlet of hydrogen peroxide tank T1 is connected to the inlet of hydrogen peroxide pump P11. The outlet of hydrogen peroxide pump P11 and the outlet of soybean oil residue feeding pipe G1 are both connected to the inlet of the first static mixer E1. The outlet of the first static mixer E1 is connected to the inlet of the oil residue conditioning tank E2. The oil residue conditioning tank E2 is equipped with a hot water tracing coil. The lower inlet of the hot water tracing coil is connected to the hot water inlet pipe G2, and the upper outlet of the hot water tracing coil is connected to the hot water outlet pipe G3.

[0028] The outlet of the oil residue conditioning tank E2 is connected to the inlet of the oil residue feed pump P1. The outlet of the oil residue feed pump P1 is connected to the upper inlet of the tube side of the first phospholipid dryer E3. The shell side inlet of the first phospholipid dryer E3 is connected to the steam pipe G4. The shell side condensate outlet of the first phospholipid dryer E3 is connected to the condensate discharge pipe G5. The lower inlet of the tube side of the first phospholipid dryer E3 is connected to the inlet of the first phospholipid storage tank T2. The outlet of the first phospholipid storage tank T2 is connected to the inlet of the first phospholipid pump P2. The outlet of the first phospholipid pump P2 is connected to the tube side inlet of the first phospholipid cooler H1. The shell side inlet of the first phospholipid cooler H1 is connected to the cooling water inlet pipe G6. The shell side outlet of the first phospholipid cooler H1 is connected to the cooling water outlet pipe G7. The tube side outlet of the first phospholipid cooler H1 is connected to the inlet of the phospholipid storage tank T5. The outlet of the first mixing tank is connected to the inlet of the second phospholipid pump P3. The outlet of the second phospholipid pump P3 and the outlet of the n-hexane pipe G10 are both connected to the inlet of the second static mixer E4. The outlet of the second static mixer E4 is connected to the upper inlet of the washing tank E5. The washing tank E5 is equipped with a hot water coil. The lower inlet of the hot water coil is connected to the hot water inlet pipe G2, and the upper outlet of the hot water coil is connected to the hot water outlet pipe G3. The bottom outlet of the washing tank E5 is connected to the inlet of the first mixing pump P4. The outlet of the first mixing pump P4 is connected to the inlets of the first settling tank T6 and the second settling tank T7. The heavy phase outlets of the first settling tank T6 and the second settling tank T7 are both connected to the inlet of the heavy phase pump P5. The outlet of the heavy phase pump P5 is connected to the inlet of the heavy phase tank T8. The bottom outlet of the heavy phase tank T8 is connected to the head end of the leachate through the hexane insoluble matter output pipe G13.

[0029] The light phase outlets of the first settling tank T6 and the second settling tank T7 are both connected to the inlet of the light phase pump P6. The outlet of the light phase pump P6 is connected to the inlet of the clear liquid tank T9. The outlet of the clear liquid tank T9 is connected to the inlet of the second mixed liquid pump P7. The outlet of the second mixed liquid pump P7 is connected to the top inlet of the falling film evaporator E6. The shell-side inlet of the falling film evaporator E6 is connected to the steam pipe G4. The shell-side condensate outlet of the falling film evaporator E6 is connected to the condensate discharge pipe G5.

[0030] The bottom outlet of the falling film evaporator E6 is connected to the inlet of the third phospholipid pump P8. The outlet of the third phospholipid pump P8 is connected to the upper inlet of the tube side of the second phospholipid dryer E7. The shell-side inlet of the second phospholipid dryer E7 is connected to the steam pipe G4. The shell-side condensate outlet of the second phospholipid dryer E7 is connected to the condensate discharge pipe G5. The lower outlet of the tube side of the second phospholipid dryer E7 is connected to the inlet of the second phospholipid storage tank T10. The outlet of the second phospholipid storage tank T10 is connected to the inlet of the fourth phospholipid pump P9. The outlet of the fourth phospholipid pump P9 is connected to the tube-side inlet of the second phospholipid cooler H3. The shell-side inlet of the second phospholipid cooler H3 is connected to the upper inlet of the tube side of the second phospholipid dryer E7. The shell-side outlet of the second phospholipid cooler H3 is connected to the cooling water inlet pipe G6, and the shell-side outlet of the second phospholipid cooler H3 is connected to the cooling water outlet pipe G7. The tube-side outlet of the second phospholipid cooler H3 is connected to the upper inlet of the stripping tank E8. The stripping tank E8 is equipped with a hot water heating coil. The lower inlet of the hot water heating coil is connected to the hot water inlet pipe G2, and the upper outlet of the hot water heating coil is connected to the hot water outlet pipe G3. The cone-bottom nitrogen inlet of the stripping tank E8 is connected to the outlet of the nitrogen pipe G11, and the bottom outlet of the stripping tank E8 is connected to the inlet of the transparent phospholipid transfer pump P10. The outlet of the transparent phospholipid transfer pump P10 is connected to the transparent phospholipid output pipe G12.

[0031] The upper gas phase outlet of the first phospholipid dryer E3 is connected to the middle inlet of the first liquid foam separator T3, the bottom outlet of the first liquid foam separator T3 is connected to the inlet of the first liquid foam receiving tank T4, and the bottom outlet of the first liquid foam receiving tank T4 is connected to the feed port of the oil foot conditioning tank E2 through the phospholipid reflux pipe G8.

[0032] The top exhaust port of the first liquid separator T3 is connected to the shell-side air inlet of the vacuum condenser H2. The shell-side exhaust port of the vacuum condenser H2 is connected to the vacuum unit through the vacuum pumping pipe G9. The tube-side inlet of the vacuum condenser H2 is connected to the cooling water inlet pipe G6. The tube-side outlet of the vacuum condenser H2 is connected to the cooling water outlet pipe G7. The shell-side condensate outlet of the vacuum condenser H2 is connected to the condensate discharge pipe G5.

[0033] The vacuum port of the falling film evaporator E6 is connected to the vacuum unit through the vacuum pipe G9; the upper gas phase outlet of the second phospholipid dryer E7 is connected to the middle inlet of the second liquid mist separator T11, the bottom outlet of the second liquid mist separator T11 is connected to the inlet of the second liquid mist receiving tank T12, and the bottom outlet of the second liquid mist receiving tank T12 is connected to the feed port of the oil foot conditioning tank E2 through the phospholipid reflux pipe G8.

[0034] The top exhaust port of the stripping tank E8 is connected to the middle inlet of the third liquid foam separator T13, the bottom outlet of the third liquid foam separator T13 is connected to the top return port of the stripping tank E8, and the top outlet of the third liquid foam separator T13 is connected to the vacuum unit through the vacuum pipe G9.

[0035] Soybean oil residue enters the first static mixer E1 through the soybean oil residue feed pipe G1. Simultaneously, 30% hydrogen peroxide from the hydrogen peroxide tank T1 is also pumped into the first static mixer E1 by the hydrogen peroxide pump P11, with an addition ratio of 5-10% of the soybean oil residue. After the soybean oil residue and hydrogen peroxide are evenly mixed in the static mixer, they enter the oil residue conditioning tank E2. The conditioning tank E2 is equipped with hot water tracing; hot water enters through the hot water inlet pipe G2 and flows out through the hot water outlet pipe G3, ensuring the temperature of the conditioning tank E2 is around 50℃. Due to the oxidizing properties of hydrogen peroxide, the pigments in the soybean oil residue are oxidized and broken down, improving the product color. After conditioning, the residue is transported by the oil residue feed pump P1 to the first phospholipid dryer E3. The first phospholipid dryer E3 operates at a pressure of -0.05 MPaG. This negative pressure environment ensures water removal without causing the product color to darken due to excessive temperature.

[0036] The heating source for the first phospholipid dryer E3 is steam. Steam enters the shell side of the first phospholipid dryer E3 through steam pipe G4, and condensate flows out through condensate discharge pipe G5. In the first phospholipid dryer E3, the moisture content of soybean oil residue is reduced from 50% to 2-5%. The dried crude phospholipid has a temperature of 80-90℃ and enters the first phospholipid temporary storage tank T2 under gravity. It is then pumped by the first phospholipid pump P2 into the hot side (tube side) of the first phospholipid cooler H1. Cooling water enters the shell side of the first phospholipid cooler H1 through cooling water inlet pipe G6 and flows out through cooling water outlet pipe G7, reducing the temperature of the crude phospholipid to about 40℃. After being cooled by the first phospholipid cooler H1, the phospholipid enters the phospholipid storage tank T5 for buffering. The purpose of buffering is to avoid drastic fluctuations in the entire production line caused by unstable feeding. Crude phospholipids in phospholipid storage tank T5 are pumped into the second static mixer E4 via the second phospholipid pump P3. Simultaneously, n-hexane is also pumped into the second static mixer E4 via the n-hexane pipe G10. The addition ratio of n-hexane is 100% of the crude phospholipids. After thorough mixing, the crude phospholipids and n-hexane enter the washing tank E5. The washing tank E5 is equipped with hot water tracing; hot water enters through the hot water inlet pipe G2 and exits through the hot water outlet pipe G3, ensuring that the temperature of the washing tank E5 is maintained at approximately 40-50℃. In the washing tank E5, the phospholipids are fully dissolved in the n-hexane.

[0037] The phospholipid-n-hexane mixture is pumped by the first mixture pump P4 into the first settling tank T6 and the second settling tank T7. Hexane-insoluble matter settles at the bottom of the tanks under gravity. After natural settling for 2-5 hours, the heavy phase is pumped by the heavy phase pump P5 into the heavy phase tank T8. The hexane-insoluble matter in the heavy phase tank T8 is discharged from the bottom and enters the leachate extractor through the hexane-insoluble matter outlet pipe G13 for reuse. The light phase from the first settling tank T6 and the second settling tank T7 is pumped by the light phase pump P6 into the clear liquid tank T9, and then by the second mixture pump P7 into the falling film evaporator E6. The falling film evaporator E6 operates at a pressure of -0.05 MPaG, removing most of the n-hexane under negative pressure. The heating source for the falling film evaporator E6 is steam, which enters the shell side of the evaporator E6 through the steam pipe G4. The condensate exits through the condensate outlet pipe G5.

[0038] After solvent extraction and concentration, the phospholipid-n-hexane mixture is pumped into the second phospholipid dryer E7 by the third phospholipid pump P8. The second phospholipid dryer E7 operates at a pressure of -0.05 MPaG, removing any remaining n-hexane under negative pressure. The heating source for the second phospholipid dryer E7 is steam, which enters the shell side of the dryer through steam pipe G4. The condensate flows out through condensate discharge pipe G5. The dried phospholipids, at approximately 90°C, enter the second phospholipid storage tank T10 under gravity. Then, they pass through the fourth phospholipid pump P9 into the tube side of the second phospholipid cooler H3. Cooling water enters the shell side of the second phospholipid cooler H3 through the cooling water inlet pipe G6 and exits through the cooling water outlet pipe G7, ensuring the phospholipid temperature is reduced to approximately 80°C. The cooled phospholipids then enter the stripping tank E8. Nitrogen gas is blown in from the bottom of the stripping tank E8 through the nitrogen pipe G11, and hot water enters through the hot water inlet pipe G2 and exits through the hot water outlet pipe G3. Through nitrogen blowing and heating, residual solvent is reduced to below 50 mg / kg. The concentrated phospholipids exiting the stripping tank E8 have a transparency of approximately 88-90% (550 nm), exhibiting good sensory quality and reaching food-grade standards. They are then delivered to the client's tank area via the transparent phospholipid transfer pump P10 and the transparent phospholipid output pipe G12.

[0039] The gas phase generated by the first phospholipid dryer E3 enters the first liquid separator T3. The separated phospholipid enters the phospholipid receiving tank T4, and then returns to the oil foot conditioning tank E2 through the phospholipid return pipe G8. The separated gas phase enters the shell side of the vacuum condenser H2. Cooling water enters the tube side of the vacuum condenser H2 through the cooling water inlet pipe G6, and flows out through the cooling water outlet pipe G7, ensuring that all water vapor in the gas phase is condensed. The condensed water is discharged into the drain, and the non-condensable gas enters the vacuum system through the vacuum pipe G9.

[0040] The solvent vapor generated by the second phospholipid dryer E7 enters the second liquid-liquid separator T11. The separated phospholipid enters the phospholipid receiving tank T12, and then returns to the oil foot conditioning tank E2 through the phospholipid return pipe G8. The separated vapor enters the vacuum system through the vacuum pipe G9.

[0041] The gas phase generated in stripping tank E8 enters the third liquid foam separator T13. The separated phospholipids return to stripping tank E8, and the separated gas phase enters the vacuum system through vacuum tube G9.

[0042] The above description is merely a preferred embodiment of the present utility model, showing and describing the basic principles, main features, and advantages of the present utility model. It is not intended to limit the scope of patent protection of the present utility model. Those skilled in the art should understand that the present utility model is not limited to the above embodiments. In addition to the above embodiments, the present utility model may have other implementations without departing from the spirit and scope of the present utility model. Various changes and improvements to the present utility model are also possible. All technical solutions formed by equivalent substitutions or equivalent transformations fall within the scope of protection claimed by the present utility model. The scope of protection claimed by the present utility model is defined by the appended claims and their equivalents. Technical features not described in the present utility model can be implemented by or using existing technology, and will not be elaborated here.

Claims

1. A system for producing transparent soybean concentrated phospholipids from soybean oil residue, comprising a soybean oil residue feeding pipe (G1), characterized in that: The soybean oil residue feeding pipe (G1) and hydrogen peroxide pipe are both connected to the inlet of the first static mixer (E1). The outlet of the first static mixer (E1) is connected to the tube-side inlet of the first phospholipid dryer (E3) via the oil residue conditioning tank (E2). The tube-side outlet of the first phospholipid dryer (E3) is connected to the inlet of the phospholipid storage tank (T5) via the first phospholipid temporary storage tank (T2), the first phospholipid pump (P2), and the first phospholipid cooler (H1). The outlets of the phospholipid storage tank (T5) and the n-hexane pipe (G10) are both connected to the inlet of the second static mixer (E4). The outlet of the second static mixer (E4) is connected to the washing tank (E5) and the first mixed liquid via the first mixed liquid. Pump (P4) is connected to the inlet of the settling tank. The light phase outlet of the settling tank is connected to the top inlet of the falling film evaporator (E6) via the light phase pump (P6), the clear liquid tank (T9), and the second mixed liquid pump (P7). The bottom outlet of the falling film evaporator (E6) is connected to the tube-side inlet of the second phospholipid dryer (E7) via the third phospholipid pump (P8). The tube-side outlet of the second phospholipid dryer (E7) is connected to the upper inlet of the stripping tank (E8) via the second phospholipid storage tank (T10), the fourth phospholipid pump (P9), and the second phospholipid cooler (H3). The bottom outlet of the stripping tank (E8) is connected to the transparent phospholipid output pipe (G12).

2. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The heavy phase outlet of the settling tank is connected to the inlet of the heavy phase pump (P5), the outlet of the heavy phase pump (P5) is connected to the inlet of the heavy phase tank (T8), and the bottom outlet of the heavy phase tank (T8) is connected to the hexane insoluble matter output pipe (G13).

3. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 2, characterized in that: The outlet of the hexane insolubles outlet pipe (G13) is connected to the head end of the leachate.

4. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The vacuum port of the falling film evaporator (E6) is connected to the vacuum tube (G9); the gas phase outlet of the first phospholipid dryer (E3) is connected to the middle inlet of the first liquid foam separator (T3), and the bottom outlet of the first liquid foam separator (T3) is connected to the feed port of the oil foot conditioning tank (E2) through the first liquid foam receiving tank (T4) and the phospholipid reflux pipe (G8).

5. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 4, characterized in that: The top exhaust port of the first liquid foam separator (T3) is connected to the shell-side inlet of the vacuum condenser (H2), the tube side of the vacuum condenser (H2) is connected to the cooling water pipe, and the shell-side exhaust port of the vacuum condenser (H2) is connected to the vacuum pumping pipe (G9).

6. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The gas phase outlet of the second phospholipid dryer (E7) is connected to the middle inlet of the second liquid foam separator (T11), the bottom outlet of the second liquid foam separator (T11) is connected to the inlet of the second liquid foam receiving tank (T12), and the outlet of the second liquid foam receiving tank (T12) is connected to the feed port of the oil foot conditioning tank (E2) through the phospholipid reflux pipe (G8); the top exhaust port of the second liquid foam separator (T11) is connected to the vacuum pipe (G9).

7. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The conical bottom nitrogen inlet of the stripping tank (E8) is connected to the outlet of the nitrogen pipe (G11); the top exhaust port of the stripping tank (E8) is connected to the middle inlet of the third liquid foam separator (T13); the bottom outlet of the third liquid foam separator (T13) is connected to the top reflux port of the stripping tank (E8); and the top outlet of the third liquid foam separator (T13) is connected to the vacuum pipe (G9).

8. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The oil residue conditioning tank (E2), washing tank (E5) and stripping tank (E8) are all equipped with hot water coils. The inlet of the hot water coil is connected to the hot water inlet pipe (G2), and the outlet is connected to the hot water outlet pipe (G3).

9. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The shell-side inlet of the first phospholipid dryer (E3), the falling film evaporator (E6), and the second phospholipid dryer (E7) is connected to the steam pipe (G4), and the shell-side condensate outlet is connected to the condensate discharge pipe (G5).

10. The system for producing transparent soybean concentrated phospholipids from soybean oil residue according to claim 1, characterized in that: The shell-side inlets of the first phospholipid cooler (H1) and the second phospholipid cooler (H3) are connected to the cooling water inlet pipe (G6), and the shell-side outlets of the first phospholipid cooler (H1) and the second phospholipid cooler (H3) are connected to the cooling water outlet pipe (G7).

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