Cottonseed dephenolated protein concentration extraction apparatus and method

Abstract

The application belongs to the technical field of chemical industry, and particularly relates to a cottonseed dephenolized concentrated protein extraction equipment and method, which comprises pretreatment unit, extraction unit, post-treatment unit, evaporation and concentration unit and solvent recovery unit connected in sequence. The pretreatment unit comprises double roller embryo press, bulking machine and turnover plate cooler. The extraction unit comprises extractor A for removing oil and fat by n-hexane extraction and extractor B for removing gossypol by methanol extraction. The post-treatment unit comprises horizontal screw conveyor dryer A and horizontal screw conveyor dryer B for drying and desolventizing the extracted cottonseed meal to obtain cottonseed dephenolized concentrated protein. The evaporation and concentration unit is used for evaporating and concentrating the mixed oil and mixed liquid after extraction. The solvent recovery unit comprises multiple condensers connected with the evaporation and concentration unit. The application can realize low-temperature and high-efficiency extraction. The protein content of the extracted product cottonseed dephenolized concentrated protein is as high as 72.7-76.2%, the gossypol content is as low as 230-290 ppm, the residual solvent in the protein is as low as 280-340 ppm, and the product quality is high.

Description

Technical Field

[0001] This invention belongs to the field of chemical technology, specifically relating to a cottonseed dephenolization and concentrated protein extraction device and method. Background Technology

[0002] China is one of the world's largest cotton producers, and cotton is a major economic crop. Cottonseed is a byproduct of cotton ginning, and extracting protein and oil from it improves the overall economic benefits of cotton cultivation. However, cottonseed contains toxic gossypol, and traditional oil extraction processes result in cottonseed meal with high gossypol content, limiting its application in the feed and food industries.

[0003] The dephenolization technology has significantly increased the economic value of cottonseed. Existing cottonseed dephenolization protein extraction processes typically include pretreatment, oil leaching, methanol dephenolization, drying and desolventizing.

[0004] Currently, most oil leaching processes use drag chain leaching machines, where the material is pushed by scrapers inside the tank and comes into countercurrent contact with n-hexane. However, this equipment has the following problems: the material is easily compacted during the conveying process, and the upper material does not come into sufficient contact with the solvent, forming "channels" and "dead zones", resulting in low extraction efficiency, high residual oil in the extracted meal, and long extraction time.

[0005] The methanol dephenolization process often uses immersion extraction, but in existing equipment, the material is mostly in a static or slow-moving state, with limited contact area with the solvent, low mass transfer efficiency, and requires a long extraction time to meet the dephenolization requirements. In addition, the wet meal after dephenolization has a high solubility, which increases the subsequent drying load.

[0006] The drying and desolventizing process usually uses a horizontal ribbon dryer, but conventional equipment has the following drawbacks: First, a dry shell is easily formed on the surface of the material during the drying process, and the internal solvent is difficult to evaporate. High temperature (100~110℃) is required to meet the residual solvent requirements, which leads to protein thermal denaturation and reduces product quality. Second, the material is prone to agglomeration and adhesion, which affects continuous operation, requires a long drying time, and has high energy consumption.

[0007] To address the aforementioned issues, there is an urgent need to design a cottonseed dephenolization and concentration protein extraction device and method that can achieve low-temperature and high-efficiency extraction, protect protein activity, improve product quality, and reduce energy consumption. Summary of the Invention

[0008] The purpose of this invention is to overcome the shortcomings of the prior art and to provide a cottonseed dephenolization and concentrated protein extraction device and method.

[0009] To achieve the above objectives, the technical solution adopted by the present invention is as follows: A cottonseed dephenolization and concentrated protein extraction device includes a pretreatment unit, an extraction unit, a posttreatment unit, an evaporation and concentration unit, and a solvent recovery unit connected in sequence. The pretreatment unit includes a twin-roller pressing machine, an extruder, and a flip-plate cooler; The extraction unit includes extractor A and extractor B. Extractor A is used for hexane extraction to remove oils and fats, and extractor B is used for methanol extraction to remove gossypol. The post-processing unit includes a horizontal ribbon dryer A and a horizontal ribbon dryer B, which are used to dry and desolventize the extracted meal to obtain cottonseed dephenolized concentrated protein. The evaporation and concentration unit includes a first evaporation component and a second evaporation component. The first evaporation component includes a first-effect evaporator, a second-effect evaporator, and a stripping tower, which are used to evaporate and concentrate the mixed oil extracted by extractor A to obtain crude oil. The second evaporation component includes a distillation tower, a first-effect evaporator, and a thin-film evaporator, which are used to evaporate and concentrate the mixed liquid extracted by extractor B to obtain cottonseed sugar concentrate. The solvent recovery unit includes multiple condensers connected to a first-effect evaporator, a second-effect evaporator, a stripping column, a distillation column, and a thin-film evaporator.

[0010] Preferably, the twin-roller extruder is connected to the puffing machine via a screw conveyor; Extractor A and extractor B, extractor B and horizontal ribbon dryer A, and horizontal ribbon dryer A and horizontal ribbon dryer B are all connected by elevators.

[0011] Preferably, the extractor A includes a housing, a sprocket mechanism, a spraying mechanism, a rake mechanism, a liquid collection hopper, and a jacket A; The sprocket mechanism is installed inside the housing, and scrapers are installed on the sprocket mechanism at equal intervals. The spraying mechanism includes a liquid delivery pipe, and multiple spray pipes are installed at equal intervals at the lower part of the liquid delivery pipe. Each spray pipe penetrates the upper side wall of the box and extends into the box. Each spray pipe has a spray nozzle installed at its lower end, and the spraying area of ​​each spray nozzle corresponds to an extraction zone. The raking mechanism includes a drive motor A, a rotating shaft and multiple raking shafts. The output end of the drive motor A is fixedly connected to the upper end of the rotating shaft, and the lower end of the rotating shaft is rotatably connected to the upper side wall of the box. The rotating shaft is connected to multiple raking shafts through a transmission assembly. The raking shafts extend vertically and are rotatably connected to the upper side wall of the box, and raking teeth are fixedly connected to their lower parts. The raking shafts are spaced apart from the spray pipes. The lower part of the chamber is equipped with a draining grid plate, and multiple liquid collection hoppers are fixed to the lower side wall of the chamber. Each liquid collection hopper is located below the corresponding extraction zone, and each liquid collection hopper is connected to the spray pipe of the corresponding extraction zone through a reflux pipe and a circulation pump. The upper left side and lower left side of the box are respectively provided with a material inlet A and a material outlet A; The front and rear sides of the box are fixedly connected to a jacket A, and the lower left side and upper right side of the jacket A are respectively provided with a steam inlet A and a steam outlet A.

[0012] Preferably, the transmission assembly includes a driving sprocket, a driven sprocket, and a chain; The driving sprocket is fixed to the rotating shaft, and the driven sprocket is fixed to the rake shaft. The driving sprocket and the driven sprocket are connected by a chain.

[0013] Preferably, the extractor B includes a housing, a stirring mechanism, and a jacket B; The stirring mechanism includes a drive motor B and a stirring shaft. The output end of the drive motor B is fixedly connected to the right end of the stirring shaft, and the left end of the stirring shaft is rotatably connected to the inner wall of the left side of the box. A spiral stirring blade is fixedly connected to the stirring shaft. The upper right side of the box is provided with a feed inlet B and a liquid outlet, and the lower left side of the box is provided with a discharge outlet B and a liquid inlet. A jacket B is fixedly connected to the middle of the outer side of the box body. A steam inlet B and a steam outlet B are respectively provided on the lower right side and upper left side of the jacket B.

[0014] Preferably, the horizontal ribbon dryer A includes a housing, a crushing mechanism, and a first jacket; The crushing mechanism includes a first drive motor and a crushing shaft. The output shaft of the first drive motor is fixedly connected to the right end of the crushing shaft, and the left end of the crushing shaft is rotatably connected to the inner wall of the left side of the housing. Crushing teeth and a first spiral ribbon are fixedly connected to the crushing shaft, and the crushing teeth and the first spiral ribbon are distributed at intervals along the axial direction of the crushing shaft. The upper right side and lower left side of the box are respectively provided with a first inlet and a first outlet; A first jacket is fixedly connected to the middle of the outer side of the box body. A first steam inlet and a first steam outlet are respectively provided on the lower left and upper right sides of the first jacket.

[0015] Preferably, the horizontal ribbon dryer B includes a housing, an extrusion mechanism, and a second jacket; The extrusion mechanism includes two drive motors and two extrusion shafts arranged in parallel front and rear and rotating in opposite directions. The right end of the extrusion shaft is fixedly connected to the output end of the corresponding drive motor, and the left end of the extrusion shaft is rotatably connected to the inner wall of the left side of the box. A second spiral ribbon distributed along the axial direction is fixedly connected to the extrusion shaft. The second spiral ribbon includes at least two sections, the diameter of the second spiral ribbon in different sections gradually increases along the material conveying direction, and the pitch of the second spiral ribbon in different sections gradually decreases along the material conveying direction; The upper right side and lower left side of the box are respectively provided with a second inlet and a second outlet; A second jacket is fixedly connected to the middle of the outer side of the box body. The lower left and upper right sides of the second jacket are respectively provided with a second steam inlet and a second steam outlet.

[0016] This invention also discloses a method for extracting concentrated protein from cottonseed after dephenolization, using the aforementioned cottonseed dephenolized protein extraction equipment, specifically including the following steps: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cottonseed hulls are obtained. The obtained cottonseed kernels are fed into a two-roller press for pressing to obtain embryo sheets with a thickness of 0.3~0.4 mm. The obtained embryo sheets are fed into an extruder for extrusion treatment to obtain extruded material. The extruded material is fed into a flip-plate cooler for cooling to obtain pretreated material. Step S2, Extraction The pretreated material is extracted with hexane by extractor A to remove oil, and then the extract meal obtained by extractor A is extracted with methanol by extractor B to remove gossypol. Step S3: Drying and desolventizing The extract obtained after extraction in extractor B is subjected to two-stage drying and desolventizing by using horizontal ribbon dryer A and horizontal ribbon dryer B in sequence to obtain cottonseed dephenolized concentrated protein. Step S4, Evaporation and Cooling The mixed oil extracted from extractor A is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil; the mixed liquid extracted from extractor B is sequentially fed into a distillation tower, a first-effect evaporator, and a thin-film evaporator to obtain cottonseed sugar concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0017] Preferably, in step S1, the temperature inside the twin-roll press is 65~70℃, and the moisture content of the wafer is 8~10%. The temperature inside the extruder is 120~150℃, and the extrusion time is 3~8 min; The discharge temperature of the flap cooler is 30~35℃.

[0018] Preferably, in step S2, the weight ratio of n-hexane to pretreated material in extractor A is 0.8~1.0:1, the extraction temperature is 50~55℃, and the extraction time is 90~100 min; the weight ratio of methanol to extract meal obtained from extractor A in extractor B is 0.7~0.8:1, the extraction temperature is 50~55℃, and the extraction time is 90~100 min.

[0019] Preferably, in step S3, the temperature inside the horizontal ribbon dryer A is 85~90℃, and the drying time is 8~10 min; the temperature inside the horizontal ribbon dryer B is 80~85℃, and the drying time is 8~10 min.

[0020] Compared with the prior art, the beneficial effects of the present invention are: 1. This invention uses extractor A to extract hexane from pretreated cottonseed to remove oil. A rake mechanism is set in the upper layer of extractor A to stir and turn the material, break the diffusion boundary layer, make the hexane solvent evenly distributed, avoid the formation of "channels" and "dead zones", improve extraction efficiency, and reduce the amount of hexane used and extraction time.

[0021] 2. In this invention, the extract meal extracted by extractor A is subjected to methanol extraction by extractor B to remove gossypol. A spiral stirring mechanism is set in extractor B to ensure that the material is in full contact with methanol, thereby reducing the amount of methanol used and the extraction time, and improving the phenol removal effect.

[0022] 3. This invention uses a horizontal ribbon dryer A and a horizontal ribbon dryer B to perform two-stage drying and solvent removal on the extracted meal. The horizontal ribbon dryer A is equipped with pulverizing teeth that shear and crush the material, achieving dynamic renewal of the material surface, effectively eliminating mass transfer resistance, improving the primary drying effect and efficiency, and reducing the burden on the secondary drying. The horizontal ribbon dryer B is equipped with an extrusion mechanism, on which a variable-diameter, variable-pitch ribbon is installed to form a progressive extrusion action, achieving deep solvent removal at low temperatures and reducing solvent residue.

[0023] 4. This invention uses a solvent recovery unit to condense and recover the solvent vapor generated by the evaporation and concentration unit. The resulting condensed solvent is recycled to the extraction step for reuse, which is energy-saving, environmentally friendly, and has significant economic and social benefits.

[0024] 5. The cottonseed dephenolized concentrated protein obtained by the extraction method of the present invention has a protein content as high as 72.7~76.2%, a gossypol content as low as 230~290 ppm, and a residual solubility in the protein as low as 280~340 ppm, which significantly improves the product quality. Attached Figure Description

[0025] Figure 1 This is a partial structural schematic diagram of the cottonseed dephenolization and concentrated protein extraction device of the present invention; Figure 2 This is a front sectional view of extractor A; Figure 3 This is the front view of extractor A; Figure 4 This is a top view of the transmission assembly; Figure 5 This is a front sectional view of extractor B; Figure 6 This is a front sectional view of horizontal ribbon dryer A; Figure 7 This is a front sectional view of the horizontal ribbon dryer B. Figure 8 This is a top sectional view of the horizontal ribbon dryer B. Figure 9 This is a schematic diagram of the process for extracting concentrated protein from cottonseed after dephenolization according to the present invention.

[0026] In the diagram: 1-Double roller extruder, 2-Expander, 3-Tilting plate cooler; 4-Extractor A, 401-Inlet A, 402-Sprocket Mechanism, 403-Scraper, 404-Spray Mechanism, 4041-Liquid Delivery Pipe, 4042-Spray Pipe, 405-Rake Mechanism, 4051-Drive Motor A, 4052-Rotating Shaft, 4053-Driven Sprocket, 4054-Driven Sprocket, 4055-Rake Shaft, 4056-Rake Teeth, 4057-Chain; 406-Liquid Collection Hopper, 407-Return Pipe, 408-Outlet A, 409-Draining Grate, 410-Jacket A, 411-Steam Inlet A, 412-Steam Outlet A; 5-Extractor B, 501-Stirring mechanism, 5011-Drive motor B, 5012-Stirring shaft, 5013-Spiral agitator, 502-Jacket B, 5021-Steam inlet B, 5022-Steam outlet B, 503-Feed inlet B, 504-Discharge outlet B, 505-Liquid inlet, 506-Liquid outlet; 6-Horizontal ribbon dryer A, 601-Pulverizing mechanism, 6011-First drive motor, 6012-Pulverizing shaft, 6013-Pulverizing teeth, 6014-First ribbon, 602-First feed inlet, 603-First discharge outlet, 604-First jacket, 6041-First steam inlet, 6042-First steam outlet; 7-Horizontal ribbon dryer B, 701-Extrusion mechanism, 7011-Second drive motor, 7012-Extrusion shaft, 7013-Second ribbon, 702-Second feed inlet, 703-Second discharge outlet, 704-Second jacket, 7041-Second steam inlet, 7042-Second steam outlet; 8-Screw conveyor, 9-Elevator. Detailed Implementation

[0027] The present invention will now be described in more detail with reference to the accompanying drawings and specific embodiments.

[0028] Example 1 This embodiment provides a cottonseed dephenolization and concentrated protein extraction device, which includes a pretreatment unit, an extraction unit, a posttreatment unit, an evaporation and concentration unit, and a solvent recovery unit connected in sequence.

[0029] See Figure 1 The pretreatment unit includes a twin-roller press 1, an extruder 2, and a flip-plate cooler 3. The twin-roller press 1 is connected to the extruder 2 via a screw conveyor 8. The extraction unit includes extractor A4 and extractor B5, which are connected by a hoist 9. Extractor A4 includes a housing, a sprocket mechanism 402, a spraying mechanism 404, a rake mechanism 405, a liquid collection hopper 406, and a jacket A410. (See Figure 2 and...) Figure 3 The upper left and lower left sides of the box are respectively provided with an inlet A401 and an outlet A408. The pre-treated material enters the box through the inlet A401. A sprocket mechanism 402 is installed inside the box, and the material is conveyed through the sprocket mechanism 402. Scrapers 403 are installed at equal intervals on the sprocket mechanism 402. The scrapers 403 are provided with multiple seepage holes to allow liquid flow. The spraying mechanism 404 includes a liquid delivery pipe 4041. Multiple spray pipes 4042 are installed at equal intervals at the lower part of the liquid delivery pipe 4041. Each spray pipe 4042... All pipes 4042 penetrate the upper side wall of the box and extend into the box. Each spray pipe 4042 is equipped with a solenoid valve and a spray nozzle is installed at the lower end of each spray pipe 4042. The spray area of ​​each spray nozzle corresponds to an extraction zone. Hexane is delivered to multiple spray pipes 4042 through the liquid delivery pipe 4041. Hexane solvent is sprayed into each extraction zone using multiple spray nozzles to extract the pretreated material with hexane and remove oil. The extracted meal enters the extractor B5 through the discharge port A408 and the elevator 9. See Figures 2-4The raking mechanism 405 includes a drive motor A4051, a rotating shaft 4052, and multiple raking shafts 4055. The output end of the drive motor A4051 is fixedly connected to the upper end of the rotating shaft 4052, and the lower end of the rotating shaft 4052 is rotatably connected to the upper side wall of the housing. The rotating shaft 4052 is connected to the multiple raking shafts 4055 through a transmission assembly. The transmission assembly includes a drive sprocket 4053, a driven sprocket 4054, and a chain 4057. The drive sprocket 4053 is fixedly connected to the rotating shaft 4052, and the driven sprocket 4054 is fixedly connected to the raking shafts 4055. The drive sprocket 4053 and the driven sprocket 4054 are connected by the chain 4057. The multiple raking shafts 4055 are driven by the drive motor A4051, the rotating shaft 4052, and the transmission assembly. 5. The rake shaft 4055 extends vertically and is rotatably connected to the upper side wall of the box, and the lower part of the rake shaft 4055 is fixedly connected to the rake teeth 4056. The rake teeth 4056 are located above the scraper 403. The rake shaft 4055 and the spray pipe 4042 are distributed at intervals. The height of the material is higher than the height of the scraper 403. During the material conveying process, the material located in the lower part of the material layer is stirred and pushed by the scraper 403 moving with the sprocket mechanism 402. At the same time, the material located in the upper part of the material layer is stirred by multiple sets of rake teeth 4056 arranged at intervals above the scraper 403. Through this synergistic effect of upper and lower layered stirring, the uniform turning of the entire material layer is achieved, which effectively destroys the diffusion boundary layer and strengthens the extraction mass transfer process. See Figure 2 and Figure 3 The lower part of the box is equipped with a drain grid plate 409, and multiple liquid collection hoppers 406 are fixed to the lower side wall of the box. The multiple liquid collection hoppers 406 are arranged along the material conveying direction and are respectively located directly below each extraction zone. They are used to collect the mixed oil that seeps down after spraying in the extraction zone. Each liquid collection hopper 406 is connected to the spray pipe 4042 of the corresponding extraction zone through an independent return pipe 407 and a circulation pump. The circulation pump transports the mixed oil to the spray pipe 4042 above the same extraction zone, thereby constructing an independent internal circulation system of solvent spraying-collection-re-spraying in each extraction zone, so that the n-hexane solvent can be recycled. See Figure 3The front and rear sides of the chamber are fixedly connected to jackets A410. Steam inlet A411 and steam outlet A412 are respectively set on the lower left and upper right sides of jacket A410, i.e., diagonally arranged, for introducing heating steam to heat the chamber. A temperature sensor (not shown in the figure) is also installed inside the chamber to monitor the temperature inside the extractor A4. The flow direction of the heating steam in jacket A410 is opposite to the conveying direction of the material in the chamber, forming countercurrent heating. This diagonal arrangement combined with the countercurrent heat exchange method makes the heating steam form an oblique countercurrent flow in jacket A410, which not only ensures the uniformity of temperature distribution in jacket A410, but also ensures that the material is heated steadily during the conveying process, ensuring the uniformity and stability of the extraction temperature, thereby improving the extraction effect and efficiency.

[0030] See Figure 5 Extractor B5 includes a housing, a stirring mechanism 501, and a jacket B502. The upper right side of the housing has a feed inlet B503 and a liquid outlet 506, while the lower left side has a discharge outlet B504 and a liquid inlet 505. The stirring mechanism 501 includes a drive motor B5011 and a stirring shaft 5012. The output end of the drive motor B5011 is fixedly connected to the right end of the stirring shaft 5012, and the left end of the stirring shaft 5012 is rotatably connected to the inner wall of the left side of the housing. A spiral stirring paddle 5013 is fixedly connected to the stirring shaft 5012. The extracted meal after extraction by extractor A4 enters the housing through the feed inlet B503, and the methanol solvent enters the housing through the liquid inlet 505. The mixture is stirred... The mixing mechanism 501 stirs and mixes the materials and solvents to improve the extraction effect. The flow direction of the methanol solvent is opposite to the flow direction of the extracted meal, which can further improve the extraction effect. A jacket B502 is fixedly connected to the middle of the outer side of the box. Steam inlet B5021 and steam outlet B5022 are respectively set on the lower right and upper left of the jacket B502, which are diagonally arranged to introduce heating steam to heat the box. This diagonal arrangement ensures the uniformity of temperature distribution in the jacket B502. A temperature sensor (not shown in the figure) is also installed in the box to monitor the temperature in the extractor B5. The extractor B5 extracts methanol from the extracted meal to remove gossypol.

[0031] See Figure 1 The post-processing unit includes a horizontal ribbon dryer A6 and a horizontal ribbon dryer B7, which are used to dry and desolventize the extracted meal to obtain cottonseed dephenolized concentrated protein. The horizontal ribbon dryer A6 includes a housing, a pulverizing mechanism 601, and a first jacket 604. (See attached image.) Figure 6The upper right side and lower left side of the housing are respectively provided with a first feed inlet 602 and a first discharge outlet 603. The crushing mechanism 601 includes a first drive motor 6011 and a crushing shaft 6012. The output shaft of the first drive motor 6011 is fixedly connected to the right end of the crushing shaft 6012. The left end of the crushing shaft 6012 is rotatably connected to the inner wall of the left side of the housing. Crushing teeth 6013 and a first screw ribbon 6014 are fixedly connected to the crushing shaft 6012. The crushing teeth 6013 and the first screw ribbon 6014 are distributed at intervals along the axial direction of the crushing shaft 6012. A first jacket 604 is fixedly connected to the middle of the outer side of the housing. The lower left side and upper right side of the first jacket 604 are respectively provided with a first feed inlet 602 and a first discharge outlet 603. A steam inlet 6041 and a first steam outlet 6042 introduce heating steam into the first jacket 604. A temperature sensor (not shown in the figure) is also installed inside the chamber to monitor the temperature inside the horizontal ribbon dryer A6. The extracted meal after two extractions by extractor A4 and extractor B5 enters the chamber through the first feed inlet 602. The heating steam in the first jacket 604 exchanges heat with the extracted meal inside the chamber, raising the temperature of the material and evaporating and removing moisture and residual solvent, thus achieving drying and desolventizing of the extracted meal. During the drying process, the crushing teeth 6013 crush and turn the material to prevent it from clumping and improve drying efficiency.

[0032] See Figure 7 and Figure 8 The horizontal ribbon dryer B7 includes a housing, an extrusion mechanism 701, and a second jacket 704. A second feed inlet 702 and a second discharge outlet 703 are respectively located on the upper right and lower left sides of the housing. The second jacket 704 is fixedly connected to the middle of the outer side of the housing. A second steam inlet 7041 and a second steam outlet 7042 are respectively located on the lower left and upper right sides of the second jacket 704. The extracted meal, after being dried and desolventized by the horizontal ribbon dryer A6, enters the housing through the second feed inlet 702. After further drying and desolventization within the housing, it is discharged through the second discharge outlet 703. The heating steam inside the second jacket 704 exchanges heat with the extracted meal inside the housing, raising the material temperature and further evaporating and removing moisture and residual solvents, thus achieving further drying and desolventization of the extracted meal. Furthermore, the heating steam inside the jacket flows counter-currently to the material conveying direction, ensuring uniform heating.

[0033] See Figure 8The extrusion mechanism 701 includes two drive motors and two extrusion shafts 7012 arranged in parallel front and rear and rotating in opposite directions. The right end of the extrusion shaft 7012 is fixedly connected to the output end of the corresponding drive motor, and the left end of the extrusion shaft 7012 is rotatably connected to the inner wall of the left side of the housing. A second screw ribbon 7013 distributed axially is fixedly connected to the extrusion shaft 7012 for extruding and pushing the material. The second screw ribbon 7013 includes three sections. The diameter of the second screw ribbon 7013 in each section gradually increases along the material conveying direction, and the pitch of the second screw ribbon 7013 in each section gradually decreases along the material conveying direction. This variable diameter and variable pitch setting of the second screw ribbon 7013 makes the material subject to gradual extrusion during the conveying process. It is rapidly advanced in the feeding section and slowly extruded in the discharging section, which is beneficial to the removal of residual solvent inside.

[0034] The evaporation and concentration unit includes a first evaporation component and a second evaporation component, see [link / reference]. Figure 9 The first evaporation assembly includes a first-effect evaporator, a second-effect evaporator, and a stripping tower, used to evaporate and concentrate the mixed oil extracted by extractor A4 to obtain crude oil; the second evaporation assembly includes a distillation tower, a first-effect evaporator, and a thin-film evaporator, used to evaporate and concentrate the mixed liquid extracted by extractor B5 to obtain cottonseed sugar concentrate.

[0035] The solvent recovery unit includes multiple condensers connected to the first-effect evaporator, second-effect evaporator, stripping column, distillation column, and thin-film evaporator, respectively. See [link to relevant documentation]. Figure 9 The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the obtained condensed solvent is recycled to the extraction step for reuse.

[0036] Example 2 This embodiment provides a method for extracting concentrated protein from cottonseed after dephenolization. The method uses the cottonseed concentrated protein extraction equipment from Example 1, and the specific extraction steps are as follows: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cotton hulls are obtained. The obtained cottonseed kernels are fed into a double-roller press 1 at 65℃ for pressing to obtain embryo sheets with a moisture content of 10% and a thickness of 0.4 mm. The obtained embryo sheets are fed into an extruder 2 at 120℃ for extrusion treatment. After extrusion for 8 minutes, the extruded material is obtained. The extruded material is fed into a flip-plate cooler 3 for cooling to obtain pre-treated material with an outlet temperature of 30℃.

[0037] Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 0.8:1, the extraction temperature was 50℃, and the extraction time was 100 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.7:1, the extraction temperature was 50℃, and the extraction time was 100 min.

[0038] Step S3: Drying and desolventizing First, the extract meal obtained after extraction in extractor B5 was subjected to primary drying and desolventizing for 10 min using a horizontal ribbon dryer A6 at 85℃. Then, the extract meal was subjected to secondary drying and desolventizing for 8 min using a horizontal ribbon dryer B7 at 85℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was tested to be 72.7%, the gossypol content was 290 ppm, and the residual solubility in the protein was 340 ppm.

[0039] Step S4, Evaporation and Cooling The mixed oil extracted from extractor A4 is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil. The mixture extracted from extractor B5 sequentially enters a distillation column, a first-effect evaporator, and a thin-film evaporator to obtain raffinose concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0040] Example 3 This embodiment provides a method for extracting concentrated protein from cottonseed after dephenolization. The method uses the cottonseed concentrated protein extraction equipment from Example 1, and the specific extraction steps are as follows: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cotton hulls are obtained. The obtained cottonseed kernels are fed into a double-roller press 1 at 65℃ for pressing to obtain embryo sheets with a moisture content of 10% and a thickness of 0.4 mm. The obtained embryo sheets are fed into an extruder 2 at 135℃ for extrusion treatment. After extrusion for 5 minutes, the extruded material is obtained. The extruded material is fed into a flip-plate cooler 3 for cooling to obtain pre-treated material with an outlet temperature of 32℃.

[0041] Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 0.8:1, the extraction temperature was 52℃, and the extraction time was 95 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.7:1, the extraction temperature was 52℃, and the extraction time was 95 min.

[0042] Step S3: Drying and desolventizing First, the extract meal obtained after extraction in extractor B5 was subjected to primary drying and desolventizing for 10 min using a horizontal ribbon dryer A6 at 85℃. Then, the extract meal was subjected to secondary drying and desolventizing for 10 min using a horizontal ribbon dryer B7 at 80℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was tested to be 74.3%, the gossypol content was 270 ppm, and the residual solubility in the protein was 330 ppm.

[0043] Step S4, Evaporation and Cooling The mixed oil extracted from extractor A4 is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil. The mixture extracted from extractor B5 sequentially enters a distillation column, a first-effect evaporator, and a thin-film evaporator to obtain raffinose concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0044] Example 4 This embodiment provides a method for extracting concentrated protein from cottonseed after dephenolization. The method uses the cottonseed concentrated protein extraction equipment from Example 1, and the specific extraction steps are as follows: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cotton hulls are obtained. The obtained cottonseed kernels are fed into a double-roller press 1 at 68℃ for pressing to obtain embryo sheets with a moisture content of 9% and a thickness of 0.33 mm. The obtained embryo sheets are fed into an extruder 2 at 135℃ for extrusion treatment. After extrusion for 5 minutes, the extruded material is obtained. The extruded material is fed into a flip-plate cooler 3 for cooling to obtain pre-treated material with an outlet temperature of 32℃.

[0045] Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 0.9:1, the extraction temperature was 52℃, and the extraction time was 95 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.75:1, the extraction temperature was 52℃, and the extraction time was 95 min.

[0046] Step S3: Drying and desolventizing The extract meal obtained after extraction in extractor B5 was first subjected to primary drying and desolventizing for 9 min using a horizontal ribbon dryer A6 at 88℃. Then, the extract meal was subjected to secondary drying and desolventizing for 9 min using a horizontal ribbon dryer B7 at 82℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was tested to be 76.2%, the gossypol content was 230 ppm, and the residual solubility in the protein was 280 ppm.

[0047] Step S4, Evaporation and Cooling The mixed oil extracted from extractor A4 is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil. The mixture extracted from extractor B5 sequentially enters a distillation column, a first-effect evaporator, and a thin-film evaporator to obtain raffinose concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0048] Example 5 This embodiment provides a method for extracting concentrated protein from cottonseed after dephenolization. The method uses the cottonseed concentrated protein extraction equipment from Example 1, and the specific extraction steps are as follows: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cotton hulls are obtained. The obtained cottonseed kernels are fed into a double-roller press 1 at 68℃ for pressing to obtain embryo sheets with a moisture content of 9% and a thickness of 0.33 mm. The obtained embryo sheets are fed into an extruder 2 at 150℃ for extrusion treatment. After extrusion for 3 minutes, the extruded material is obtained. The extruded material is fed into a flip-plate cooler 3 for cooling to obtain pre-treated material with an outlet temperature of 35℃.

[0049] Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 0.9:1, the extraction temperature was 55℃, and the extraction time was 90 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.75:1, the extraction temperature was 55℃, and the extraction time was 90 min.

[0050] Step S3: Drying and desolventizing The extract meal obtained after extraction in extractor B5 was first subjected to primary drying and desolventizing for 8 min using a horizontal ribbon dryer A6 at 90℃. Then, the extract meal was subjected to secondary drying and desolventizing for 9 min using a horizontal ribbon dryer B7 at 82℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was tested to be 75.1%, the gossypol content was 260 ppm, and the residual solubility in the protein was 300 ppm.

[0051] Step S4, Evaporation and Cooling The mixed oil extracted from extractor A4 is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil. The mixture extracted from extractor B5 sequentially enters a distillation column, a first-effect evaporator, and a thin-film evaporator to obtain raffinose concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0052] Example 6 This embodiment provides a method for extracting concentrated protein from cottonseed after dephenolization. The method uses the cottonseed concentrated protein extraction equipment from Example 1, and the specific extraction steps are as follows: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cotton hulls are obtained. The obtained cottonseed kernels are fed into a 70°C double-roller press 1 for pressing to obtain embryo sheets with a moisture content of 8% and a thickness of 0.3 mm. The obtained embryo sheets are fed into a 150°C extruder 2 for extrusion treatment. After extrusion for 3 minutes, the extruded material is obtained. The extruded material is fed into a flip-plate cooler 3 for cooling to obtain pre-treated material with an outlet temperature of 35°C.

[0053] Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 1:1. The extraction temperature was 55℃ and the extraction time was 90 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.8:1, the extraction temperature was 55℃, and the extraction time was 90 min.

[0054] Step S3: Drying and desolventizing The extract meal obtained after extraction in extractor B5 was first subjected to primary drying and desolventizing for 8 min using a horizontal ribbon dryer A6 at 90℃. Then, the extract meal was subjected to secondary drying and desolventizing for 8 min using a horizontal ribbon dryer B7 at 85℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was tested to be 73.8%, the gossypol content was 280 ppm, and the residual solubility in the protein was 310 ppm.

[0055] Step S4, Evaporation and Cooling The mixed oil extracted from extractor A4 is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil. The mixture extracted from extractor B5 sequentially enters a distillation column, a first-effect evaporator, and a thin-film evaporator to obtain raffinose concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

[0056] Comparative Example 1 The difference between Comparative Example 1 and Example 4 is that in step S2, the extractor A4 does not contain the rake mechanism 405, the amount of hexane used as solvent is different, and the extraction time using extractor A4 is different, as detailed below: The pretreated material was extracted with n-hexane using extractor A4 to remove oil, wherein the weight ratio of n-hexane to pretreated material was 1.2:1, and the extraction time was 120 min. The remaining steps were the same as in Example 4. After two-stage drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was 63.5%, the gossypol content was 460 ppm, and the residual solubility in the protein was 440 ppm.

[0057] Comparative Example 2 The difference between Comparative Example 2 and Example 4 is that in step S2, the extractor B5 does not contain a stirring mechanism 501, the amount of methanol used as solvent is different, and the extraction time using extractor B5 is different, as detailed below: The extract meal obtained from extractor A4 was subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.9:1, and the extraction time was 120 min. The remaining steps were the same as in Example 4. After two-stage drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was 65.8%, the gossypol content was 450 ppm, and the residual solubility in the protein was 430 ppm.

[0058] Comparative Example 3 The difference between Comparative Example 3 and Example 4 is that, in step S3, the pulverizing mechanism 601 of the horizontal ribbon dryer A6 does not include pulverizing teeth 6013, the temperature inside the horizontal ribbon dryer A6 is different, and the time for primary drying and desolvation using the horizontal ribbon dryer A6 is different, as detailed below: The horizontal ribbon dryer A6 includes a housing, a crushing mechanism 601, and a first jacket 604. The crushing mechanism 601 includes a first drive motor 6011 and a crushing shaft 6012. The output shaft of the first drive motor 6011 is fixedly connected to the right end of the crushing shaft 6012. The left end of the crushing shaft 6012 is rotatably connected to the inner wall of the left side of the housing. A first ribbon 6014 is fixedly connected to the crushing shaft 6012. A first feed inlet 602 and a first discharge outlet 603 are respectively provided on the upper right side and lower left side of the housing. A first jacket 604 is fixedly connected to the middle of the outer side of the housing. A first steam inlet 6041 and a first steam outlet 6042 are respectively provided on the lower left side and upper right side of the first jacket 604. First, the extract meal obtained after extraction in extractor B5 was subjected to primary drying and desolventizing for 10 min using a horizontal ribbon dryer A6 at 100℃. Then, the extract meal was subjected to secondary drying and desolventizing for 9 min using a horizontal ribbon dryer B7 at 82℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was found to be 62.1%, the gossypol content was 430 ppm, and the residual solubility in the protein was 500 ppm.

[0059] Comparative Example 4 The difference between Comparative Example 4 and Example 4 is that in step S3, the horizontal ribbon dryer B7 does not contain the extrusion mechanism 701, and its structure is the same as that of the horizontal ribbon dryer A6 in Comparative Example 3. The temperature inside the horizontal ribbon dryer B7 is different, and the time for secondary drying and desolvation using the horizontal ribbon dryer B7 is different, as detailed below: The extract meal obtained after extraction in extractor B5 was first subjected to primary drying and desolventizing for 9 min using a horizontal ribbon dryer A6 at 88℃. Then, the extract meal was subjected to secondary drying and desolventizing for 10 min using a horizontal ribbon dryer B7 at 110℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was found to be 61.8%, the gossypol content was 480 ppm, and the residual solubility in the protein was 520 ppm.

[0060] Comparative Example 5 The differences between Comparative Example 4 and Example 4 are as follows: ① In step S2, extractor A4 does not contain a rake mechanism 405, the amount of hexane used as solvent is different, and the extraction time using extractor A4 is different; ② In step S2, extractor B5 does not contain a stirring mechanism 501, the amount of methanol used as solvent is different, and the extraction time using extractor B5 is different; ③ The pulverizing mechanism 601 of the horizontal ribbon dryer A6 does not include pulverizing teeth 6013, the temperature inside the horizontal ribbon dryer A6 is different, and the time for primary drying and desolventizing using the horizontal ribbon dryer A6 is different; ④ The horizontal ribbon dryer B7 does not contain an extrusion mechanism 701, and its structure is the same as that of the horizontal ribbon dryer A6 in Comparative Example 3. The temperature inside the horizontal ribbon dryer B7 is different, and the time for secondary drying and desolventizing using the horizontal ribbon dryer B7 is different, as detailed below: Step S2, Extraction The pretreated material was first extracted with hexane using extractor A4 to remove oil. The weight ratio of hexane to pretreated material was 1.2:1, the extraction temperature was 52℃, and the extraction time was 120 min. The extract meal obtained from extractor A4 was then subjected to methanol extraction via extractor B5 to remove gossypol. The weight ratio of methanol to extract meal was 0.9:1, the extraction temperature was 52℃, and the extraction time was 120 min.

[0061] Step S3: Drying and desolventizing First, the extract meal obtained after extraction in extractor B5 was subjected to primary drying and desolventizing for 10 min using a horizontal ribbon dryer A6 at 100℃. Then, the extract meal was subjected to secondary drying and desolventizing for 10 min using a horizontal ribbon dryer B7 at 110℃. After two stages of drying and desolventizing, cottonseed dephenolized concentrated protein was obtained. The protein content was found to be 60.2%, the gossypol content was 500 ppm, and the residual solubility in the protein was 550 ppm.

[0062] Therefore, it can be seen that the extraction method of Examples 2-6 of this invention (extractor A4 rake stirring, extractor B5 spiral stirring, horizontal ribbon dryer A6 crushing tooth stirring, horizontal ribbon dryer B7 variable diameter and variable pitch extrusion) yields cottonseed dephenolized concentrated protein with a protein content as high as 72.7-76.2%, a gossypol content as low as 230-290 ppm, and a residual solubility in the protein as low as 280-340 ppm. Its protein content is higher than that of Comparative Examples 1-5, while the gossypol content and residual solubility in the protein are lower than those of Comparative Examples 1-5. Furthermore, the amount of solvents n-hexane and methanol used, as well as the time for the two-stage extraction, are lower than those of Comparative Examples 1-5, and the temperature and time for the two-stage drying and desolvation are also lower than those of Comparative Examples 1-5.

[0063] In embodiments 2-6 of this invention, the rake stirring of extractor A4 enhances oil extraction, providing high-quality raw materials for subsequent phenol removal. The spiral stirring of extractor B5 enhances mass transfer, shortening the extraction time while ensuring the phenol removal effect. The crushing teeth 6013 of the horizontal ribbon dryer A6 shear and break the material, achieving dynamic renewal of the material surface, effectively eliminating mass transfer resistance, improving drying effect and efficiency, and reducing the burden on secondary drying. The variable diameter and variable pitch extrusion of the horizontal ribbon dryer B7 enables deep desolventizing at low temperatures. Through this progressive synergistic effect, the quality of cottonseed phenol-removed concentrated protein product is ultimately improved, effectively reducing the amount of extraction solvent, shortening the total extraction time and drying time, improving production efficiency, and effectively reducing the temperature of the two-stage drying, achieving energy saving and consumption reduction.

[0064] The above embodiments are merely illustrative of the present invention and are not intended to limit the invention. Any obvious modifications made by those skilled in the art without departing from the principles and spirit of the present invention should be considered to be included within the scope of protection of the claims of the present invention.

Claims

1. A cottonseed dephenolization and concentrated protein extraction device, characterized in that, It includes a pretreatment unit, an extraction unit, a posttreatment unit, an evaporation and concentration unit, and a solvent recovery unit connected in sequence; The pretreatment unit includes a twin-roller pressing machine, an extruder, and a flip-plate cooler; The extraction unit includes extractor A and extractor B. Extractor A is used for hexane extraction to remove oils and fats, and extractor B is used for methanol extraction to remove gossypol. The post-processing unit includes a horizontal ribbon dryer A and a horizontal ribbon dryer B, which are used to dry and desolventize the extracted meal to obtain cottonseed dephenolized concentrated protein. The evaporation and concentration unit includes a first evaporation component and a second evaporation component. The first evaporation component includes a first-effect evaporator, a second-effect evaporator, and a stripping tower, which are used to evaporate and concentrate the mixed oil extracted by extractor A to obtain crude oil. The second evaporation component includes a distillation tower, a first-effect evaporator, and a thin-film evaporator, which are used to evaporate and concentrate the mixed liquid extracted by extractor B to obtain cottonseed sugar concentrate. The solvent recovery unit includes multiple condensers connected to a first-effect evaporator, a second-effect evaporator, a stripping column, a distillation column, and a thin-film evaporator.

2. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 1, characterized in that, The twin-roller pressing machine is connected to the extruder via a screw conveyor; Extractor A and extractor B, extractor B and horizontal ribbon dryer A, and horizontal ribbon dryer A and horizontal ribbon dryer B are all connected by elevators.

3. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 1, characterized in that, The extractor A includes a housing, a sprocket mechanism, a spraying mechanism, a rake mechanism, a liquid collection hopper, and a jacket A; The sprocket mechanism is installed inside the housing, and scrapers are installed on the sprocket mechanism at equal intervals. The spraying mechanism includes a liquid delivery pipe, and multiple spray pipes are installed at equal intervals at the lower part of the liquid delivery pipe. Each spray pipe penetrates the upper side wall of the box and extends into the box. Each spray pipe has a spray nozzle installed at its lower end, and the spraying area of ​​each spray nozzle corresponds to an extraction zone. The raking mechanism includes a drive motor A, a rotating shaft and multiple raking shafts. The output end of the drive motor A is fixedly connected to the upper end of the rotating shaft, and the lower end of the rotating shaft is rotatably connected to the upper side wall of the box. The rotating shaft is connected to multiple raking shafts through a transmission assembly. The raking shafts extend vertically and are rotatably connected to the upper side wall of the box, and raking teeth are fixedly connected to their lower parts. The raking shafts are spaced apart from the spray pipes. The lower part of the chamber is equipped with a draining grid plate, and multiple liquid collection hoppers are fixed to the lower side wall of the chamber. Each liquid collection hopper is located below the corresponding extraction zone, and each liquid collection hopper is connected to the spray pipe of the corresponding extraction zone through a reflux pipe and a circulation pump. The upper left side and lower left side of the box are respectively provided with a material inlet A and a material outlet A; The front and rear sides of the box are fixedly connected to a jacket A, and the lower left side and upper right side of the jacket A are respectively provided with a steam inlet A and a steam outlet A.

4. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 3, characterized in that, The transmission assembly includes a driving sprocket, a driven sprocket, and a chain; The driving sprocket is fixed to the rotating shaft, and the driven sprocket is fixed to the rake shaft. The driving sprocket and the driven sprocket are connected by a chain.

5. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 2, characterized in that, The extractor B includes a housing, a stirring mechanism, and a jacket B; The stirring mechanism includes a drive motor B and a stirring shaft. The output end of the drive motor B is fixedly connected to the right end of the stirring shaft, and the left end of the stirring shaft is rotatably connected to the inner wall of the left side of the box. A spiral stirring blade is fixedly connected to the stirring shaft. The upper right side of the box is provided with a feed inlet B and a liquid outlet, and the lower left side of the box is provided with a discharge outlet B and a liquid inlet. A jacket B is fixedly connected to the middle of the outer side of the box body. A steam inlet B and a steam outlet B are respectively provided on the lower right side and upper left side of the jacket B.

6. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 2, characterized in that, The horizontal ribbon dryer A includes a housing, a crushing mechanism, and a first jacket; The crushing mechanism includes a first drive motor and a crushing shaft. The output shaft of the first drive motor is fixedly connected to the right end of the crushing shaft, and the left end of the crushing shaft is rotatably connected to the inner wall of the left side of the housing. Crushing teeth and a first spiral ribbon are fixedly connected to the crushing shaft, and the crushing teeth and the first spiral ribbon are distributed at intervals along the axial direction of the crushing shaft. The upper right side and lower left side of the box are respectively provided with a first inlet and a first outlet; A first jacket is fixedly connected to the middle of the outer side of the box body. A first steam inlet and a first steam outlet are respectively provided on the lower left and upper right sides of the first jacket.

7. The cottonseed dephenolization and concentrated protein extraction equipment as described in claim 2, characterized in that, The horizontal ribbon dryer B includes a housing, an extrusion mechanism, and a second jacket. The extrusion mechanism includes two drive motors and two extrusion shafts arranged in parallel front and rear and rotating in opposite directions. The right end of the extrusion shaft is fixedly connected to the output end of the corresponding drive motor, and the left end of the extrusion shaft is rotatably connected to the inner wall of the left side of the box. A second spiral ribbon distributed along the axial direction is fixedly connected to the extrusion shaft. The second spiral ribbon includes at least two sections, the diameter of the second spiral ribbon in different sections gradually increases along the material conveying direction, and the pitch of the second spiral ribbon in different sections gradually decreases along the material conveying direction; The upper right side and lower left side of the box are respectively provided with a second inlet and a second outlet; A second jacket is fixedly connected to the middle of the outer side of the box body. The lower left and upper right sides of the second jacket are respectively provided with a second steam inlet and a second steam outlet.

8. A method for extracting concentrated protein from cottonseed after dephenolization, using the cottonseed concentrated protein extraction equipment according to any one of claims 1 to 7, characterized in that, Includes the following steps: Step S1, Preprocessing After separating the cottonseed hull from the kernel, cottonseed kernels and cottonseed hulls are obtained. The obtained cottonseed kernels are fed into a two-roller press for pressing to obtain embryo sheets with a thickness of 0.3~0.4 mm. The obtained embryo sheets are fed into an extruder for extrusion treatment to obtain extruded material. The extruded material is fed into a flip-plate cooler for cooling to obtain pretreated material. Step S2, Extraction The pretreated material is extracted with hexane by extractor A to remove oil, and then the extract meal obtained by extractor A is extracted with methanol by extractor B to remove gossypol. Step S3: Drying and desolventizing The extract obtained after extraction in extractor B is subjected to two-stage drying and desolventizing by using horizontal ribbon dryer A and horizontal ribbon dryer B in sequence to obtain cottonseed dephenolized concentrated protein. Step S4, Evaporation and Cooling The mixed oil extracted from extractor A is sequentially fed into a first-effect evaporator, a second-effect evaporator, and a stripping tower for evaporation and concentration to obtain crude oil; the mixed liquid extracted from extractor B is sequentially fed into a distillation tower, a first-effect evaporator, and a thin-film evaporator to obtain cottonseed sugar concentrate. Step S5, Solvent Recovery The solvent vapor phase generated by each effect evaporator, stripping column, distillation column and thin film evaporator is condensed and recovered by their respective independent condensers, and the resulting condensed solvent is recycled to the extraction step for reuse.

9. The method for extracting concentrated protein from cottonseed after dephenolization as described in claim 8, characterized in that, in step S1, the temperature inside the double-roller pressing mill is 65~70℃, and the moisture content of the embryo is 8~10%; The temperature inside the extruder is 120~150℃, and the extrusion time is 3~8 min; The discharge temperature of the flap cooler is 30~35℃.

10. The method for extracting concentrated protein from cottonseed after dephenolization as described in claim 8, characterized in that, in step S2, the weight ratio of n-hexane to pretreated material in extractor A is 0.8~1.0:1, the extraction temperature is 50~55℃, and the extraction time is 90~100 min; the weight ratio of methanol to extracted meal obtained from extractor A in extractor B is 0.7~0.8:1, the extraction temperature is 50~55℃, and the extraction time is 90~100 min; In step S3, the temperature inside the horizontal ribbon dryer A is 85~90℃, and the drying time is 8~10 min; the temperature inside the horizontal ribbon dryer B is 80~85℃, and the drying time is 8~10 min.

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