A complete set of equipment for continuously preparing peanut protein

Abstract

The utility model relates to a kind of peanut protein processing complete equipment of continuous preparation, including leaching device, desolventizing vessel, evaporation unit, condenser, turnover tank, first heat exchanger and second heat exchanger;The wet meal output end of leaching device is connected with the input end of desolventizing vessel;Desolventizing vessel's desolventizing tail gas end is sequentially connected with turnover tank through first heat exchanger, condenser;The mixed oil output end of leaching device is connected with the input end of evaporation unit pipeline;Evaporation unit's evaporation tail gas end is sequentially connected with turnover tank through second heat exchanger and condenser;The output end of turnover tank is sequentially connected with the leaching liquid input end of leaching device through first heat exchanger and second heat exchanger, so that the low-temperature leaching liquid exported by turnover tank sequentially flows through first heat exchanger and second heat exchanger, realizes double-stage preheating, fully absorbs tail gas heat, can reduce the heating load of evaporation unit and desolventizing vessel, reduce the refrigeration load of condenser simultaneously, save energy consumption.

Description

Technical Field

[0001] This utility model relates to the field of peanut protein processing technology, specifically to a complete set of equipment for continuous peanut protein processing. Background Technology

[0002] In peanut protein processing, organic solvents (such as n-hexane) are often used for leaching to extract oil from peanuts and obtain defatted peanut meal. References can be made to existing technologies such as 200810007828.4, "A Preparation Process of High-Activity Fully Defatted Peanut Protein Powder," and CN 103820220 B, "A Method for Simultaneous and Continuous Stable Production of Soybean Wet Meal from High-Temperature and Low-Temperature Desolventizing on Two Different Production Lines." This process generally includes leaching, desolventizing, evaporation, condensation, and solvent circulation. In the leaching unit, the solvent comes into full contact with the peanut raw material, generating a mixed oil and wet meal. The wet meal enters the desolventizing unit, where residual solvent is removed through heating and stripping. The mixed oil enters the evaporation unit, where the solvent is recovered through stepwise evaporation to obtain crude oil.

[0003] In the evaporator and desolventizing units, the solvent is heated and vaporized to form gaseous leachate. This exhaust gas needs to be condensed into liquid solvent by a condenser and returned to a storage tank for recycling. The liquid leachate in the storage tank is usually at a low temperature (20–40°C) and needs to be heated to the operating temperature of the extractor (40–60°C). In addition, the mixed oil and wet meal often require secondary heating in the evaporator or desolventizing unit to reach their operating temperatures for evaporation and desolventizing (around 80°C for low-temperature desolventizing to ensure the peanuts do not denature). This results in high heating energy consumption, and the subsequent condenser also has high operating energy consumption, requiring a large amount of electricity and cooling water for heat dissipation.

[0004] Therefore, it is necessary to study a complete set of equipment for continuous peanut protein production. Utility Model Content

[0005] Therefore, the purpose of this utility model is to provide a complete set of equipment for continuous peanut protein preparation, which can effectively solve the problem of high energy consumption in the evaporation, desolvation and condensation stages of the existing peanut protein preparation process.

[0006] To achieve the above objectives, the technical solution adopted by this utility model is as follows: A complete set of equipment for continuous peanut protein production includes an extractor, a solvent remover, an evaporator, a condenser, a transfer tank, a first heat exchanger, and a second heat exchanger. The wet meal output end of the leachate is connected to the input end of the desolventizer; The desolvent exhaust gas end of the desolventizer is connected to the first heat exchanger, the condenser and the transfer tank in sequence. The mixed oil output end of the leaching unit is connected to the input end of the evaporator unit; The evaporation exhaust gas end of the evaporator unit is connected to the transfer tank via a second heat exchanger and a condenser in sequence. The output end of the transfer tank is connected to the leachate input end of the leachate extractor via a first heat exchanger and a second heat exchanger.

[0007] Furthermore, it also includes a third heat exchanger, through which the mixed oil output end of the leaching unit is connected to the input end of the evaporator unit; The desolvent exhaust gas from the desolventizer is connected to the second heat exchanger after passing through the third heat exchanger.

[0008] Furthermore, the evaporator unit includes a first-effect evaporator separator, a second-effect evaporator separator, and a stripping tower connected in sequence. The gaseous output ends of the first-effect evaporator separator, the second-effect evaporator separator, and the stripping tower are all connected to a steam conveying pipe and then connected to the first heat exchanger through the steam conveying pipe.

[0009] Furthermore, it also includes a pretreatment unit, which comprises a cleaning unit, a peeling unit, and a pulverizing unit connected in sequence.

[0010] Furthermore, the cleaning unit includes a primary cleaning screen, a destoner, and a magnetic separator connected in sequence.

[0011] Furthermore, the peeling unit includes a modulator, a red garment peeling machine, a red garment screening machine, and a red garment buffer chamber connected in sequence, with the input end of the modulator connected to the output end of the magnetic separator.

[0012] Furthermore, the pulverizing unit includes a crusher and a cold press connected in sequence. The cold-pressed peanut cake output end of the cold press is connected to the extractor; the input end of the crusher is connected to the peanut kernel output end of the red skin peeling machine.

[0013] The beneficial effects of the above technical solution are: (1) Before entering the condenser, the high-temperature exhaust gas of the solvent extractor of this utility model exchanges heat with the low-temperature liquid leachate from the turnover tank through the first heat exchanger to recover the waste heat of the exhaust gas, thereby achieving the first preheating of the leachate and the precooling of the solvent extractor exhaust gas; before entering the condenser, the high-temperature exhaust gas of the evaporator exchanges heat with the liquid leachate from the turnover tank through the second heat exchanger to achieve the second preheating of the leachate and the precooling of the evaporator exhaust gas; thus, the low-temperature leachate output from the turnover tank flows through the first heat exchanger and the second heat exchanger in sequence to achieve double-stage preheating, fully absorb the heat of the exhaust gas, reduce the heating load of the evaporator and the solvent extractor, and at the same time reduce the cooling load of the condenser, thus saving energy.

[0014] (2) By setting a third heat exchanger, the mixed oil output from the extractor exchanges heat with the tail gas of the desolvent before entering the evaporator unit, and uses the residual heat of the tail gas to preheat the mixed oil, thereby reducing the heating load of the evaporator unit. Attached Figure Description

[0015] Figure 1 This is a schematic diagram of the leaching and desolventizing process of this utility model; Figure 2 This is a schematic diagram of the pretreatment unit.

[0016] Attached reference numerals: 1. Leacher; 2. Solvent remover; 3. Evaporator; 4. Condenser; 5. Transfer tank; 6. First heat exchanger; 7. Second heat exchanger; 8. Third heat exchanger; 9. Primary cleaning screen; 10. Destoner; 11. Magnetic separator; 12. Regulator; 13. Red skin peeling machine; 14. Red skin screening machine; 15. Red skin buffer silo; 16. Crusher; 17. Cold press; 18. Chiller; 301. First-effect evaporator separator; 302. Second-effect evaporator separator; 303. Stripping tower; 304. Steam conveying pipe. Detailed Implementation

[0017] The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments: This embodiment aims to provide a complete set of equipment for continuous peanut protein preparation, which is mainly used for low-temperature preparation of peanut protein, and addresses the problem of high energy consumption in the evaporation, desolvation and condensation stages of existing peanut protein preparation processes.

[0018] A complete set of equipment for continuous peanut protein production, such as Figure 1 It includes an extractor 1, a solvent remover 2, an evaporator 3, a condenser 4, a transfer tank 5, a first heat exchanger 6, and a second heat exchanger 7.

[0019] The extractor 1 is a continuous low-temperature leaching device. Cold-pressed peanut cake is continuously fed into the extractor 1 via an inlet scraper conveyor and a sealed auger to remove the oil from the peanut cake, so that the oil content in the peanut cake is less than 1% and the nitrogen solubility index is greater than 50%. The leaching temperature is controlled at 50°C, and the leaching solution is n-hexane with a boiling point of 60°C.

[0020] The wet meal output end of the leachator 1 is connected to the input end of the desolventizer 2, allowing the wet meal (peanut cake and liquid leachate) continuously discharged from the leachator 1 to continuously enter the desolventizer 2. The desolventizer 2 uses an existing low-temperature desolventizer AB cylinder to remove the leachate from the cake. The leachate is condensed and recycled by the condenser 4. The defatted peanut meal has a protein content greater than 50% and a nitrogen solubility index greater than 50%. The desolventizing temperature is maintained at around 80°C to avoid high-temperature denaturation of peanut protein. The working principle and specific structure of the leachator 1 and the desolventizer 2 are based on existing technology and can be found in the documents cited in the background section; they will not be repeated here. The desolventizing tail gas end of the desolventizer 2 is connected to the first heat exchanger 6, the condenser 4, and the transfer tank 5 in sequence to cool and liquefy the gaseous leachate for recycling. The protein meal output end of the desolventizer 2 is used to output defatted protein meal, which then enters the pulverizing equipment to produce defatted low-denatured peanut protein powder. The pulverizing equipment specifically includes a pulverizer, a grading screen and auxiliary dust removal equipment to obtain defatted low-denatured peanut protein powder with a fineness (passing through a 0.154mm diameter screen) greater than 95%.

[0021] The output end of the mixed oil (peanut oil and liquid leachate) of the extractor 1 is connected to the input end of the evaporator unit 3. The evaporator unit 3 is mainly used to evaporate and separate the leachate from the mixed oil. The evaporator unit 3 includes a first-effect evaporator separator 301, a second-effect evaporator separator 302, and a stripping tower 303 connected in sequence. The gaseous output ends of the first-effect evaporator separator 301, the second-effect evaporator separator 302, and the stripping tower 303 are all connected to a steam conveying pipe 304, and then connected to a second heat exchanger 7 through the steam conveying pipe 304 to collect and uniformly transport the evaporation tail gas. The evaporator unit 3 can produce crude oil, and the residual solvent in the crude oil should be less than 100 ppm. Subsequently, the crude oil enters the refining equipment, specifically including a hydration tank, an alkali refining tank, a washing tank, a dehydration tank, a decolorization tank, a filter, and a deodorization tank to produce extracted peanut oil. The specific refining equipment uses existing technology and will not be described in detail here.

[0022] The evaporation exhaust gas from evaporator unit 3 is connected to transfer tank 5 via the second heat exchanger 7 and condenser 4. It should be noted that the desolvation exhaust gas and evaporation exhaust gas do not necessarily need to enter the same condenser 4 after confluence. Depending on the actual operating conditions, a separate condenser 4 can be selected. However, after passing through condenser 4, the gas should flow back to the same transfer tank 5, and the condensed liquid leachate should be maintained between 20–40 °C. A chiller 18 is connected to condenser 4 via a pipeline to provide chilled water.

[0023] The output end of the turnover tank 5 is connected to the leachate input end of the leachator 1 via the first heat exchanger 6 and the second heat exchanger 7 in sequence. The turnover tank 5 is used to store the leachate, and a replenishment port for new liquid input is provided on the turnover tank 5.

[0024] It also includes a third heat exchanger 8. The desolventizing tail gas of the desolventizer 2 is connected to the first heat exchanger 6 after passing through the third heat exchanger 8. The mixed oil output end of the extractor 1 is connected to the input end of the evaporator 3 through the third heat exchanger 8, so that the mixed oil output from the extractor 1 exchanges heat with the tail gas of the desolventizer 2 before entering the evaporator, and uses the waste heat of the tail gas to preheat the mixed oil, thereby reducing the heating load of the evaporator.

[0025] The heat exchangers in the first heat exchanger 6 are the desolventized tail gas that has passed through the third heat exchanger 8 and the liquid leachate at the outlet of the transfer tank 5. The first heat exchanger 6 is located near the outlet of the transfer tank 5 and is mainly used for the primary preheating of the leachate and the secondary precooling of the desolventized tail gas.

[0026] The heat exchangers in the second heat exchanger 7 are the evaporation exhaust gas and the liquid leachate that has passed through the first heat exchanger 6 and is about to enter the leachate 1. The second heat exchanger 7 is located close to the leachate 1 and is mainly used for secondary preheating of the leachate and precooling of the evaporation exhaust gas.

[0027] The third heat exchanger 8 exchanges heat with the desolventized tail gas and the mixed oil that is about to enter the evaporator unit. The third heat exchanger 8 is located near the input end of the desolventizer 2 and is mainly used for the primary preheating of the mixed oil and the primary precooling of the desolventized tail gas.

[0028] The first heat exchanger 6, the second heat exchanger 7, and the third heat exchanger 8 are all gas-liquid heat exchangers and can utilize existing shell-and-tube heat exchangers to fully absorb the heat from the exhaust gas. This reduces the heating load on the evaporator and the solvent extractor 2, while also reducing the cooling load on the condenser 4, thus saving energy. It should be emphasized that this embodiment focuses on the connection of key equipment. In actual use, conventional components such as pumps, check valves, and filters can be selected according to the operating conditions to ensure that leachate from different phases can smoothly enter the next device and form a cycle.

[0029] Furthermore, such as Figure 2 It also includes a pretreatment unit, which comprises a cleaning unit, a peeling unit, and a pulverizing unit connected in sequence.

[0030] Specifically, the cleaning unit includes a primary cleaning screen 9, a destoner 10, and a magnetic separator 11 connected in sequence to remove soil, sand, gravel, and ironware from the material. The sand content is controlled below 0.02%, and the ash content is less than 6%, in order to meet the physical and chemical indicators such as sand content and ash content required for food-grade products. The pulverizing unit includes a crusher 16 and a cold press 17 connected in sequence. The cold-pressed peanut cake output end of the cold press 17 is connected to the extractor 1. The pulverizing unit, combined with the cold press 17, can effectively extract approximately 90% of the oil from peanut kernels at low temperatures, yielding cold-pressed peanut oil and cold-pressed peanut cake. The cold-pressed peanut cake at this stage is a semi-defatted peanut cake with low protein denaturation and an oil content of approximately 10%.

[0031] The peanut peeling unit includes a modulator 12, a red skin peeler 13, a red skin sieve 14, and a red skin buffer chamber 15 connected in sequence. The input end of the red skin peeler 13 is connected to the input end of the magnetic separator 11, and the peanut kernel output end of the red skin peeler 13 is connected to the input end of the crusher 16. After cleaning, the peanut kernels are effectively regulated by the modulator 12 to facilitate the removal of the peanut red skin in the red skin peeler 13, so as not to affect the ash content, crude fiber content, etc. of the final product. The peanut red skin is collected centrally in the red skin buffer chamber 15 and can be used as an additional by-product.

Claims

1. A complete set of equipment for continuous peanut protein production, characterized in that: It includes a leachator, a solvent remover, an evaporator, a condenser, a transfer tank, a first heat exchanger, and a second heat exchanger; The wet meal output end of the leachate is connected to the input end of the desolventizer; The desolvent exhaust gas end of the desolventizer is connected to the first heat exchanger, the condenser and the transfer tank in sequence. The mixed oil output end of the leaching unit is connected to the input end of the evaporator unit; The evaporation exhaust gas end of the evaporator unit is connected to the transfer tank via a second heat exchanger and a condenser in sequence. The output end of the transfer tank is connected to the leachate input end of the leachate extractor via a first heat exchanger and a second heat exchanger.

2. The complete set of equipment for continuous peanut protein preparation according to claim 1, characterized in that: It also includes a third heat exchanger, through which the mixed oil output end of the leaching unit is connected to the input end of the evaporator unit; The desolvent exhaust gas from the desolventizer is connected to the second heat exchanger after passing through the third heat exchanger.

3. The complete set of equipment for continuous peanut protein preparation according to claim 1, characterized in that: The evaporator unit includes a first-effect evaporator separator, a second-effect evaporator separator, and a stripping tower connected in sequence. The gaseous output ends of the first-effect evaporator separator, the second-effect evaporator separator, and the stripping tower are all connected to a steam conveying pipe and then connected to the first heat exchanger through the steam conveying pipe.

4. A complete set of equipment for continuous peanut protein production according to any one of claims 1-3, characterized in that: It also includes a pretreatment unit, which comprises a cleaning unit, a peeling unit, and a pulverizing unit connected in sequence.

5. The complete set of equipment for continuous peanut protein preparation according to claim 4, characterized in that: The cleaning unit includes a primary cleaning screen, a destoner, and a magnetic separator connected in sequence.

6. The complete set of equipment for continuous peanut protein preparation according to claim 5, characterized in that: The peeling unit includes a modulator, a red garment peeling machine, a red garment screening machine, and a red garment buffer chamber connected in sequence. The input end of the modulator is connected to the output end of the magnetic separator.

7. The complete set of equipment for continuous peanut protein preparation according to claim 6, characterized in that: The crushing unit includes a crusher and a cold press connected in sequence. The cold press peanut cake output end is connected to the extractor; the input end of the crusher is connected to the peanut kernel output end of the red skin peeling machine.

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