Separation and purification system of phytosterol ester

Abstract

The utility model relates to a separation and purification system of phytosterol ester, which comprises a pre-mixing module, an extraction module, a saponification module, a liquid separation module, an adsorption module, an evaporator and a dryer, the pre-mixing module is used for mixing and heating an extraction liquid A and an extraction liquid B, the extraction liquid A is insoluble in water and can dissolve the phytosterol ester, and the extraction module is used for extracting the phytosterol ester. The pre-mixing module is provided with an extraction liquid B, the extraction liquid B is dissolved in water and can dissolve phytosterol, a crude product to be separated and purified is added into the extraction module, a weak base solution is added into the saponification module, the adsorption module is filled with activated carbon, and the pre-mixing module, the extraction module, the saponification module and the adsorption module are micro-channel continuous flow modules. The device disclosed by the utility model has the beneficial effects that esterification crude products of fatty acid and phytosterol are separated by utilizing a modularized micro-channel continuous flow extraction technology, and the problem that sterol, fatty acid and sterol ester in the crude products coexist and are difficult to separate is solved, so that high-purity phytosterol ester is obtained.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of phytosterol ester extraction, and particularly relates to a separation and purification system for phytosterol ester. BACKGROUND

[0002] Phytosterol ester (PSE) is a derivative of phytosterol (PS), has good fat solubility and the dual effects of phytosterol and fatty acid without changing the biological effects of phytosterol. Phytosterol ester is generally prepared by enzymatic synthesis or chemical synthesis. Whether by enzymatic synthesis or chemical synthesis, the obtained product after reaction is a crude esterification product. In the crude product, phytosterol, fatty acid and phytosterol ester coexist. Common separation methods for the crude phytosterol ester product include extraction and recrystallization. However, the solubility of alcohol, acid and ester in some organic solvents is not significantly different, which often leads to the inability to achieve both purity and yield during separation.

[0003] Although the recrystallization method is simple to operate, widely applicable and requires low equipment, it has a large solvent consumption and the crystallization effect is affected by multiple factors and sensitive to operating conditions. For some substances with small solubility difference, the recrystallization efficiency is low and multiple recrystallizations are often required to improve the purification effect. The recrystallization method usually consists of a dissolving kettle, a conveying pipeline, a crystallizer, a separation device and a drying device. From the perspective of operation continuity, it is difficult to achieve continuous and automatic operation and is not suitable for large-scale processing. The extraction method has a wide application range, high selectivity, can effectively extract and separate target substances, is relatively simple to operate and easy to realize continuous production. However, the extraction method has a large solvent consumption and low extraction efficiency for substances with small solubility difference. Therefore, appropriate solvents and extraction conditions need to be selected, otherwise the purification effect may be affected.

[0004] Traditional extraction technology often uses tank extraction. In tank extraction, the raw material liquid and the extractant are placed in a stirred tank or a mixing tank, and the two are mixed by stirring to allow the solute to be distributed between the two solvents. After a certain extraction balance is reached, the mixed liquid enters a separator such as a settling tank or a centrifugal separator to separate the extraction phase and the raffinate phase. The advantage of tank extraction is that the operation is relatively simple and the equipment requirement is not high. However, the stirring intensity of tank extraction is low, the mass transfer efficiency is not high, and it is difficult to achieve the extraction effect. For extraction operations that require heating, the heat transfer efficiency of tank extraction is also not high. Tank extraction usually requires a long mixing time, and when the amount of solution to be treated is large, the efficiency and separation effect of tank extraction may also be affected. Therefore, the overall efficiency of tank extraction is low and the energy consumption is high. SUMMARY

[0005] The utility model discloses a plant phytosterol ester's separation and purification system, utilize the modularization's microchannel continuous extraction technology separation fatty acid, the esterification crude product of phytosterol, solve the problem that the crude product is difficult to separate in the coexistence of sterol, fatty acid, sterol ester, to obtain the high purity phytosterol ester.

[0006] The utility model discloses a plant phytosterol ester's separation and purification system, utilize the modularization's microchannel continuous extraction technology separation fatty acid, the esterification crude product of phytosterol, solve the problem that the crude product is difficult to separate in the coexistence of sterol, fatty acid, sterol ester, to obtain the high purity phytosterol ester.

[0007] A kind of plant phytosterol ester's separation and purification system, it is characterized by comprising:

[0008] Premixing unit, premixing unit includes premixing module, premixing module is used to mix and heat extraction liquid A and extraction liquid B, extraction liquid A is insoluble in water and can dissolve phytosterol ester, extraction liquid B is dissolved in water and can dissolve phytosterol, the mixed heating temperature of extraction liquid A and extraction liquid B is less than the boiling point of extraction liquid A and extraction liquid B;

[0009] Extraction unit, extraction unit includes extraction module and saponification module, the outlet of premixing module is connected to the inlet of extraction module by pipeline, the outlet of extraction module is connected to the inlet of saponification module by pipeline, the crude product to be separated and purified is added in extraction module, and weak base solution is added in saponification module;

[0010] Liquid separation unit, liquid separation unit includes liquid separation module, the outlet of saponification module is connected to the inlet of liquid separation module by pipeline;

[0011] Adsorption unit, adsorption unit includes adsorption module, the outlet of liquid separation module is connected to the inlet of adsorption module by pipeline, and activated carbon is filled in adsorption module;

[0012] Drying unit, drying unit includes evaporator and dryer, the outlet of adsorption module is connected to the inlet of evaporator by pipeline, and the outlet of evaporator is connected to the inlet of dryer by pipeline;

[0013] Premixing module, extraction module, saponification module and adsorption module are all microchannel continuous flow modules.

[0014] Further, the premixing unit further includes a first liquid storage device and a second liquid storage device, the outlet of the first liquid storage device and the outlet of the second liquid storage device are both connected to the inlet of the premixing module by pipelines, a first valve, a first feed pump and a first flow meter are sequentially arranged on the connecting pipeline between the first liquid storage device and the premixing module, a second valve, a second feed pump and a second flow meter are sequentially arranged on the connecting pipeline between the second liquid storage device and the premixing module, the first liquid storage device stores the extraction liquid A, and the second liquid storage device stores the extraction liquid B.

[0015] Further, the extraction liquid A comprises n-hexane, cyclohexane, n-heptane, isooctane or petroleum ether, and the extraction liquid B comprises ethanol, n-butanol, isopropyl alcohol, ethyl acetate or acetone.

[0016] Further, the extraction unit further comprises a third storage device and a fourth storage device, the outlet of the third storage device is connected to the inlet of the extraction module through a pipeline, a third valve, a third feed pump and a third flow meter are sequentially arranged on the connecting pipeline between the third storage device and the extraction module, the outlet of the fourth storage device is connected to the inlet of the saponification module through a pipeline, a fourth valve, a fourth feed pump and a fourth flow meter are sequentially arranged on the connecting pipeline between the fourth storage device and the saponification module, the third storage device stores the crude product, and the fourth storage device stores a weak alkali solution, wherein the weak alkali solution comprises a sodium bicarbonate solution or a potassium bicarbonate solution.

[0017] Further, the extraction unit further comprises a third storage device and a fourth storage device, the outlet of the third storage device is connected to the inlet of the extraction module through a pipeline, a third valve, a third feed pump and a third flow meter are sequentially arranged on the connecting pipeline between the third storage device and the extraction module, the outlet of the fourth storage device is connected to the inlet of the saponification module through a pipeline, a fourth valve, a fourth feed pump and a fourth flow meter are sequentially arranged on the connecting pipeline between the fourth storage device and the saponification module, the third storage device stores the crude product, and the fourth storage device stores a weak alkali solution, wherein the weak alkali solution comprises a sodium bicarbonate solution or a potassium bicarbonate solution.

[0018] Further, the sixth feed pump is arranged on the connecting pipeline between the sixth storage device and the adsorption module, and the seventh feed pump is arranged on the connecting pipeline between the evaporator and the dryer.

[0019] Further, the first temperature control device is arranged outside the third storage device.

[0020] Further, the second temperature control device is arranged outside the premixing module, the extraction module and the saponification module.

[0021] Further, the first sampling port is arranged on the pipeline between the fifth valve and the separation module, the second sampling port is arranged on the pipeline between the fifth feed pump and the separation module, and the first exhaust port is arranged on the top of the separation module.

[0022] Further, the outlet of the evaporator is further connected with a first heat exchanger through a pipeline, the outlet of the first heat exchanger is connected with a seventh storage device through a pipeline, the outlet of the dryer is connected with a second heat exchanger through a pipeline, the outlet of the second heat exchanger is connected to the inlet of the seventh storage device through a pipeline, the outlet of the seventh storage device is connected to the inlet of the first storage device through a pipeline, and an eighth feed pump and a sixth valve are sequentially arranged on the connecting pipeline between the seventh storage device and the first storage device.

[0023] Compared with the prior art, the utility model has the advantages of:

[0024] 1. The utility model discloses a modular microchannel continuous extraction technology, through the solvent of continuous circulation flow, can fully contact the material to be extracted, compared with the traditional kettle batch extraction method, continuous extraction can better utilize the solvent, reduce the waste of solvent, and its balance time is less than the traditional extraction process several orders of magnitude, and the extraction efficiency is higher, in addition, continuous extraction has better scalability and flexibility, can adjust the production capacity according to the need, and realizes the continuous and stable production, and then adapts to different scale and demand industrial production.

[0025] 2. The utility model discloses a modular microchannel continuous extraction technology, has the characteristics of high specific surface area, high heat transfer mass transfer rate, can realize the accurate control of heat transfer, mass transfer, and the separation factor beta of target material in the microchannel continuous extraction process is much higher than the traditional kettle extraction process, has higher selectivity, and thus has the advantages of high yield, high selectivity, smaller residence time distribution, faster system response, smaller equipment volume, etc., significantly improves the extraction efficiency and process controllability. BRIEF DESCRIPTION OF DRAWINGS

[0026] Figure 1 It is the structure schematic drawing of premixing unit in the utility model;

[0027] Figure 2 It is the structure schematic drawing of extraction unit in the utility model;

[0028] Figure 3 It is the structure schematic drawing of liquid separation unit and adsorption unit in the utility model;

[0029] Figure 4 It is the structure schematic drawing of drying unit in the utility model.

[0030] In the drawing: 1, premixing module; 2, extraction module; 3, saponification module; 4, liquid separation module; 5, adsorption module; 6, evaporator; 7, dryer; 8, first liquid storage device; 9, second liquid storage device; 10, first valve; 11, first feed pump; 12, first flow meter; 13, second valve; 14, second feed pump; 15, second flow meter; 16, third liquid storage device; 17, fourth liquid storage device; 18, third valve; 19, third feed pump; 20, third flow meter; 21, fourth valve; 22, fourth feed pump; 23, fourth flow meter; 24, fifth liquid storage device; 25, sixth liquid storage device; 26, fifth valve; 27, fifth feed pump; 28, sixth feed pump; 29, seventh feed pump; 30, first temperature control device; 31, first sampling port; 32, second sampling port; 33, first exhaust port; 34, first heat exchanger; 35, seventh liquid storage device; 36, second heat exchanger; 37, eighth feed pump; 38, sixth valve; 39, second temperature control device. DETAILED DESCRIPTION

[0031] The utility model is further described below in combination with the drawings, but the protection scope of the utility model is not limited to the following.

[0032] As shown in the figure, a phytosterol ester separation and purification system for separating esterification crude products of fatty acids and phytosterols comprises a premixing unit, an extraction unit, a liquid separation unit, an adsorption unit and a drying unit. Figures 1-4 The premixing unit comprises a premixing module 1, the extraction unit comprises an extraction module 2 and a saponification module 3, the liquid separation unit comprises a liquid separation module 4, the adsorption unit comprises an adsorption module 5, and the drying unit comprises an evaporator 6 and a dryer 7. The outlet of the premixing module 1 is connected to the inlet of the extraction module 2 through a pipeline, the outlet of the extraction module 2 is connected to the inlet of the saponification module 3 through a pipeline, the outlet of the saponification module 3 is connected to the inlet of the liquid separation module 4 through a pipeline, the outlet of the liquid separation module 4 is connected to the inlet of the adsorption module 5 through a pipeline, the outlet of the adsorption module 5 is connected to the inlet of the evaporator 6 through a pipeline, and the outlet of the evaporator 6 is connected to the inlet of the dryer 7 through a pipeline.

[0033] The utility model adopts a composite extractant composed of extraction liquid A and extraction liquid B for extraction washing, wherein the extraction liquid A is insoluble in water and can dissolve phytosterol ester, and the extraction liquid B is soluble in water and can dissolve phytosterol. In the process of separating and purifying the crude product of phytosterol ester, the extraction liquid A and the extraction liquid B are mixed and heated by the premixing module 1 to improve the solubility of the crude product, and the mixed heating temperature of the extraction liquid A and the extraction liquid B is less than the boiling point of the extraction liquid A and the extraction liquid B. The crude product to be separated and purified is added into the extraction module 2, and a weak alkali solution is added into the saponification module 3. The heated composite extractant and the crude product are fully mixed in the extraction module 2 to obtain a mixed liquid, and then the mixed liquid is sent into the saponification module 3. In the weak alkali environment, the unreacted fatty acid undergoes saponification reaction to generate fatty acid salt which can be dissolved in the water phase. Since the solubility of the extraction liquid B in the water phase is greater, the water phase contains a mixture of the extraction liquid B, phytosterol and fatty acid salt, and the extraction liquid A is insoluble in water, so the extraction liquid A and the phytosterol ester are separated out. The extracted mixed liquid is sent into the liquid separation module 4 for static layering, and then the water phase (containing the mixture of the extraction liquid B, phytosterol and fatty acid salt) is discharged and treated, the mixed sample of the extraction liquid A and the phytosterol ester is discharged and sent into the adsorption module 5, and the adsorption module 5 is filled with activated carbon. The sample is adsorbed and faded by the activated carbon, so that the color of the sample changes from light yellow to colorless. The faded sample is first sent into the evaporator 6 for concentration, and then the concentrated sample is sent into the dryer 7 for drying treatment, and finally the purified phytosterol ester is obtained.

[0034]

[0035] ​The above separation and purification process is continuous as a whole, and the pre-mixing module 1, the extraction module 2, the saponification module 3 and the adsorption module 5 all adopt micro-channel continuous flow modules, thereby forming a modular micro-channel continuous flow extraction technology for separating and purifying phytosterol esters. Compared with the traditional kettle batch extraction method, the micro-channel continuous extraction process has higher selectivity for target substances, which can greatly reduce the waste of solvents; secondly, the characteristics of high specific surface area and high heat and mass transfer rate can realize precise control of the heat and mass transfer process; in addition, the smaller residence time distribution significantly improves the extraction efficiency; at the same time, continuous extraction has better scalability and flexibility, which can adjust the production capacity according to needs and realize continuous and stable production, thereby adapting to different scales and needs of industrial production.

[0036] In the present embodiment, the extraction liquid A includes n-hexane, cyclohexane, n-heptane, isooctane or petroleum ether, and the extraction liquid B includes ethanol, n-butanol, isopropyl alcohol, ethyl acetate or acetone.

[0037] As shown in Figure 1 The pre-mixing unit further includes a first liquid storage device 8 and a second liquid storage device 9. The outlet of the first liquid storage device 8 and the outlet of the second liquid storage device 9 are both connected to the inlet of the pre-mixing module 1 through pipelines, and a first valve 10, a first feed pump 11 and a first flow meter 12 are sequentially installed on the connecting pipeline between the first liquid storage device 8 and the pre-mixing module 1, and a second valve 13, a second feed pump 14 and a second flow meter 15 are sequentially installed on the connecting pipeline between the second liquid storage device 9 and the pre-mixing module 1. The first liquid storage device 8 stores the extraction liquid A, and the second liquid storage device 9 stores the extraction liquid B. After the first valve 10 and the second valve 13 are opened, the extraction liquid A and the extraction liquid B are pumped into the pre-mixing module 1 through the first feed pump 11 and the second feed pump 14 respectively, and the first flow meter 12 and the second flow meter 15 are used for accurately measuring the pump-in amount of the extraction liquid.

[0038] As shown in Figure 2As shown, the extraction unit further comprises a third storage device 16 and a fourth storage device 17. The outlet of the third storage device 16 is connected to the inlet of the extraction module 2 through a pipeline, and a third valve 18, a third feed pump 19 and a third flow meter 20 are sequentially arranged on the connecting pipeline between the third storage device 16 and the extraction module 2. The outlet of the fourth storage device 17 is connected to the inlet of the saponification module 3 through a pipeline, and a fourth valve 21, a fourth feed pump 22 and a fourth flow meter 23 are sequentially arranged on the connecting pipeline between the fourth storage device 17 and the saponification module 3. The third storage device 16 stores the crude product, and the fourth storage device 17 stores the weak base solution. After the third valve 18 and the fourth valve 21 are opened, the crude product is pumped into the extraction module 2 through the third feed pump 19, and the weak base solution is pumped into the saponification module 3 through the fourth feed pump 22. The third flow meter 20 and the fourth flow meter 23 are respectively used for accurately measuring the pump-in amount of the crude product and the weak base solution. In this embodiment, the weak base solution includes sodium bicarbonate solution or potassium bicarbonate solution.

[0039] As shown in FIG. 4, Figure 3 As shown, the separation unit further comprises a fifth storage device 24 and a sixth storage device 25. The outlet of the separation module 4 comprises an upper outlet and a lower outlet. The lower outlet of the separation module 4 is connected to the inlet of the fifth storage device 24 through a pipeline, and a fifth valve 26 is arranged on the connecting pipeline between the separation module 4 and the fifth storage device 24. The upper outlet of the separation module 4 is connected to the inlet of the sixth storage device 25 through a pipeline, and a fifth feed pump 27 is arranged on the connecting pipeline between the separation module 4 and the sixth storage device 25. The outlet of the sixth storage device 25 is connected to the inlet of the adsorption module 5 through a pipeline. After the fifth valve 26 is opened, the water phase containing the extraction liquid B, phytosterols and fatty acid salts after the separation can be discharged to the fifth storage device 24 for storage, so as to facilitate subsequent centralized treatment. The mixed sample of the extraction liquid A and phytosterol esters after the separation can be pumped into the sixth storage device 25 for storage through the fifth feed pump 27.

[0040] As shown in FIG. 4, Figure 3 、 Figure 4 As shown, a sixth feed pump 28 is arranged on the connecting pipeline between the sixth storage device 25 and the adsorption module 5, and a seventh feed pump 29 is arranged on the connecting pipeline between the evaporator 6 and the dryer 7. After the mixed sample in the sixth storage device 25 is pumped into the adsorption module 5 for adsorption and fading by the sixth feed pump 28, the faded sample is sent into the evaporator 6 for concentration, and then the concentrated sample is pumped into the dryer 7 for drying treatment by the seventh feed pump 29.

[0041] As shown in FIG. 4, Figure 2 、 Figure 3As shown, the third liquid storage device 16 is externally provided with a first temperature control device 30 for precise temperature control, and the pre-mixing module 1, the extraction module 2 and the saponification module 3 are externally provided with second temperature control devices 39 for precise temperature control; a first sampling port 31 is arranged on the pipeline between the fifth valve 26 and the liquid separation module 4, and a second sampling port 32 is arranged on the pipeline between the fifth feed pump 27 and the liquid separation module 4, so that sampling and analysis can be performed at any time through the first sampling port 31 and the second sampling port 32; and the liquid separation module 4 is provided with a first exhaust port 33 at the top for exhaust.

[0042] As shown in Figure 1 , Figure 4 In order to recycle the extractant A, improve the utilization rate of the solvent and reduce the waste of the solvent, the outlet of the evaporator 6 is further connected with a first heat exchanger 34 through a pipeline, the outlet of the first heat exchanger 34 is connected with a seventh liquid storage device 35 through a pipeline, the outlet of the dryer 7 is connected with a second heat exchanger 36 through a pipeline, the outlet of the second heat exchanger 36 is connected with the inlet of the seventh liquid storage device 35 through a pipeline, and the outlet of the seventh liquid storage device 35 is connected with the inlet of the first liquid storage device 8 through a pipeline. The eighth feed pump 37 and the sixth valve 38 are sequentially arranged on the connecting pipeline between the seventh liquid storage device 35 and the first liquid storage device 8. The extractant A evaporated from the evaporator 6 and the dryer 7 is condensed by the first heat exchanger 34 and the second heat exchanger 36 respectively and then sent to the seventh liquid storage device 35, and then the sixth valve 38 is opened and the eighth feed pump 37 is used to pump the extractant to the first liquid storage device 8 for recycling.

[0043] In this embodiment, the self-made crude stigmasterin oleate is taken as an example, and the crude stigmasterin oleate is separated and purified by the separation and purification system. The extractant A is n-hexane, the extractant B is anhydrous ethanol, the flow rate of the n-hexane is 10 ml / min, the flow rate of the anhydrous ethanol is 15-25 ml / min, the volume ratio of the n-hexane to the anhydrous ethanol is 1:1.5-2.5, and the crude stigmasterin oleate:n-hexane is 1:5-20 (m:v). The weak alkali solution is a 0.5 mol / L sodium bicarbonate solution. The temperature of the third liquid storage device 16 is controlled at 30°C, and the temperatures of the pre-mixing module 1, the extraction module 2 and the saponification module 3 are all controlled at 50°C. Similarly, the self-made crude stigmasterin oleate is taken as an example, and the crude stigmasterin oleate is separated and purified by the kettle extraction technology for comparison. The comparison results are shown in Table 1. The crude product before separation is light yellow and contains oleic acid, stigmasterin, stigmasterin ester and other substances. The product after separation is white.

[0044] Table 1: Comparison table of micro-channel continuous flow extraction and kettle extraction purification results

[0045]

[0046]

[0047] As can be seen from table 1, compared with kettle extraction technology, the balance time of micro-channel continuous flow extraction technology is less by several orders of magnitude, and the extraction efficiency is higher, wherein the purity of stigmasterol ester separated by micro-channel continuous flow extraction technology can reach 99.32%.

[0048] The separation and purification system of the utility model combines modular micro-channel continuous extraction technology, can fully contact the material to be extracted through the continuously circulating solvent, has better scalability and flexibility, can adjust the production capacity according to the needs, and realizes the continuous and stable production, and further adapts to different scale and demand of industrial production.

[0049] Finally, although the above description has shown and described the embodiments of the utility model, it can be understood by those skilled in the art that various changes, modifications, replacements and variations can be made to these embodiments without departing from the principles and spirits of the utility model, and the scope of the utility model is defined by the appended claims and their equivalents.

Claims

1. A system for separating and purifying phytosterol esters, characterized in that, The application relates to a plant sterol extraction and purification device. The pre-mixing unit comprises a pre-mixing module (1) for mixing and heating extractant A and extractant B, wherein extractant A is insoluble in water and soluble in plant sterol ester, extractant B is soluble in water and soluble in plant sterol, and the mixing and heating temperature of extractant A and extractant B is less than the boiling point of extractant A and extractant B. The extraction unit comprises an extraction module (2) and a saponification module (3), the outlet of the pre-mixing module (1) is connected to the inlet of the extraction module (2) through a pipeline, the outlet of the extraction module (2) is connected to the inlet of the saponification module (3) through a pipeline, the extraction module (2) is filled with crude products to be separated and purified, and the saponification module (3) is filled with a weak alkali solution. The separation unit comprises a separation module (4), and the outlet of the saponification module (3) is connected to the inlet of the separation module (4) through a pipeline. The adsorption unit comprises an adsorption module (5), and the outlet of the separation module (4) is connected to the inlet of the adsorption module (5) through a pipeline, and the adsorption module (5) is filled with activated carbon. The drying unit comprises an evaporator (6) and a dryer (7), and the outlet of the adsorption module (5) is connected to the inlet of the evaporator (6) through a pipeline, and the outlet of the evaporator (6) is connected to the inlet of the dryer (7) through a pipeline. The pre-mixing module (1), the extraction module (2), the saponification module (3) and the adsorption module (5) are all micro-channel continuous flow modules.

2. The separation and purification system of plant sterol esters according to claim 1, characterized by: The pre-mixing unit further comprises a first liquid storage device (8) and a second liquid storage device (9), the outlet of the first liquid storage device (8) and the outlet of the second liquid storage device (9) are both connected to the inlet of the pre-mixing module (1) through pipelines, a first valve (10), a first feeding pump (11) and a first flow meter (12) are sequentially arranged on the connecting pipeline between the first liquid storage device (8) and the pre-mixing module (1), a second valve (13), a second feeding pump (14) and a second flow meter (15) are sequentially arranged on the connecting pipeline between the second liquid storage device (9) and the pre-mixing module (1), and the first liquid storage device (8) is used for storing extractant A, and the second liquid storage device (9) is used for storing extractant B.

3. The separation and purification system of plant sterol esters according to claim 2, characterized by: The extractant A comprises n-hexane, cyclohexane, n-heptane, isooctane or petroleum ether, and the extractant B comprises ethanol, n-butanol, isopropyl alcohol, ethyl acetate or acetone.

4. The separation and purification system of plant sterol esters according to claim 1, characterized by: The extraction unit further comprises a third storage device (16) and a fourth storage device (17), the outlet of the third storage device (16) is connected to the inlet of the extraction module (2) through a pipeline, and a third valve (18), a third feed pump (19) and a third flow meter (20) are sequentially arranged on the connecting pipeline between the third storage device (16) and the extraction module (2), the outlet of the fourth storage device (17) is connected to the inlet of the saponification module (3) through a pipeline, and a fourth valve (21), a fourth feed pump (22) and a fourth flow meter (23) are sequentially arranged on the connecting pipeline between the fourth storage device (17) and the saponification module (3), the third storage device (16) stores a crude product, and the fourth storage device (17) stores a weak alkali solution, and the weak alkali solution comprises a sodium bicarbonate solution or a potassium bicarbonate solution.

5. The separation and purification system of plant sterol esters according to claim 1, characterized by: The separation unit further comprises a fifth storage device (24) and a sixth storage device (25), the outlet of the separation module (4) comprises an upper outlet and a lower outlet, the lower outlet of the separation module (4) is connected to the inlet of the fifth storage device (24) through a pipeline, and a fifth valve (26) is arranged on the connecting pipeline between the separation module (4) and the fifth storage device (24), the upper outlet of the separation module (4) is connected to the inlet of the sixth storage device (25) through a pipeline, and a fifth feed pump (27) is arranged on the connecting pipeline between the separation module (4) and the sixth storage device (25), and the outlet of the sixth storage device (25) is connected to the inlet of the adsorption module (5) through a pipeline.

6. The separation and purification system of plant sterol esters according to claim 5, characterized in that: A sixth feed pump (28) is arranged on the connecting pipeline between the sixth storage device (25) and the adsorption module (5), and a seventh feed pump (29) is arranged on the connecting pipeline between the evaporator (6) and the dryer (7).

7. The separation and purification system of plant sterol esters according to claim 4, characterized by: A first temperature control device (30) is arranged outside the third storage device (16).

8. The separation and purification system of plant sterol esters according to claim 1, characterized by: Second temperature control devices (39) are arranged outside the premixing module (1), the extraction module (2) and the saponification module (3).

9. The separation and purification system of plant sterol esters according to claim 5, characterized by: A first sampling port (31) is arranged on the pipeline between the fifth valve (26) and the separation module (4), a second sampling port (32) is arranged on the pipeline between the fifth feed pump (27) and the separation module (4), and a first exhaust port (33) is arranged on the top of the separation module (4).

10. The separation and purification system of plant sterol esters according to claim 1, characterized by: The outlet of the evaporator (6) is further connected to a first heat exchanger (34) through a pipeline, the outlet of the first heat exchanger (34) is connected to a seventh storage device (35) through a pipeline, the outlet of the dryer (7) is connected to a second heat exchanger (36) through a pipeline, the outlet of the second heat exchanger (36) is connected to the inlet of the seventh storage device (35) through a pipeline, the outlet of the seventh storage device (35) is connected to the inlet of the first storage device (8) through a pipeline, and an eighth feed pump (37) and a sixth valve (38) are sequentially arranged on the connecting pipeline between the seventh storage device (35) and the first storage device (8).

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