Apparatus for separating and preparing scyllitol

Abstract

The utility model discloses a kind of preparation devices of separating of shark muscle inositol, it is related to shark muscle inositol production technical field, the outlet of shark muscle inositol conversion liquid tank is communicated with flocculation tank, the inlet of flocculation tank is communicated with glacial acetic acid tank, the outlet of flocculation tank is communicated with ceramic membrane device, the clear liquid outlet of ceramic membrane device is communicated with ultrafiltration membrane device, the clear liquid outlet of ultrafiltration membrane device is communicated with cation exchange resin column, the outlet of cation exchange resin column is communicated with anion exchange resin column, the outlet of anion exchange resin column is communicated with concentration tank, the outlet of concentration tank is communicated with first crystallization tank, the inlet of first crystallization tank is communicated with seed tank, the outlet of first crystallization tank is communicated with first filter, the solid phase outlet of first filter is communicated with flushing tank, the inlet of flushing tank is communicated with first purified water tank, the outlet of flushing tank is communicated with crude product tank. Simple process, product purity is high, and it is friendly to environment.

Description

Technical Field

[0001] This utility model relates to the field of squalinosin production technology, specifically to a squalinosin separation and preparation apparatus. Background Technology

[0002] Inositol is a cyclohexanol compound widely found in living organisms. One of its isomers, L-chiro-inositol, has shown significant application value in the pharmaceutical and health product fields in recent years. Studies have shown that L-chiro-inositol has significant effects in improving insulin resistance, regulating glucose metabolism, and treating polycystic ovary syndrome (PCOS), leading to increasing market demand.

[0003] Currently, the industrial production of squalene mainly relies on extraction from plants or chemical conversion of inexpensive myoinositol. However, both extraction and conversion methods yield a mixture of squalene and other isomers such as myoinositol. Because squalene and myoinositol have extremely similar physicochemical properties, especially their similar solubility in water, efficiently and with high purity, separating squalene from the mixture remains a major technical challenge in this field.

[0004] Traditional separation and purification processes commonly employ the boric acid complexation method. This method utilizes the fact that squalinositol can form a stable complex with boric acid and crystallize out, while myosinositol has a weaker complexing ability. Although this method was used for a period of time, boric acid is a toxic compound to humans, exhibiting reproductive and developmental toxicity. The use of boric acid may lead to the risk of boric acid residues in the final product, raising consumer concerns about product safety and making it difficult to meet increasingly stringent food and drug regulations. Furthermore, this process is lengthy, requiring multiple steps such as complexation, acid hydrolysis, and boron removal, resulting in long production cycles, high energy consumption, and increased equipment investment and plant space requirements. Simultaneously, the lengthy process also leads to a loss of target product yield. Summary of the Invention

[0005] The technical problem to be solved by this utility model is to provide a separation and preparation device for squalene, which is simple in process, produces high-purity products, and is environmentally friendly, in order to address the shortcomings of the existing technology.

[0006] To solve the above-mentioned technical problems, the technical solution of this utility model is as follows:

[0007] A squalene separation and preparation apparatus includes a squalene conversion liquid tank. The outlet of the squalene conversion liquid tank is connected to a flocculation tank via a pipeline. The inlet of the flocculation tank is connected to a glacial acetic acid tank via a pipeline. The outlet of the flocculation tank is connected to a ceramic membrane device via a pipeline. The clear liquid outlet of the ceramic membrane device is connected to an ultrafiltration membrane device via a pipeline. The clear liquid outlet of the ultrafiltration membrane device is connected to a cation exchange resin column via a pipeline. The outlet of the cation exchange resin column is connected to an anion exchange resin column via a pipeline. The outlet of the anion exchange resin column is connected to a concentration tank via a pipeline. The outlet of the concentration tank is connected to a first crystallization tank via a pipeline. The inlet of the first crystallization tank is connected to a seed crystal tank via a pipeline. The outlet of the first crystallization tank is connected to a first filter via a pipeline. The solid phase outlet of the first filter is connected to a rinsing tank via a pipeline. The inlet of the rinsing tank is connected to a first purified water tank via a pipeline. The outlet of the rinsing tank is connected to a crude product tank via a pipeline.

[0008] As an improved technical solution, the inlet of the flocculation tank is connected to a polyaspartic acid salt tank via a pipeline.

[0009] As an improved technical solution, the outlet of the ultrafiltration membrane clear liquid is connected to a nanofiltration membrane device via a pipeline, and the clear liquid outlet of the nanofiltration membrane device is connected to the cation exchange resin column via a pipeline.

[0010] As an improved technical solution, the nanofiltration membrane device has a molecular weight cutoff of 200-300 Da.

[0011] As an improved technical solution, the filter size of the ceramic membrane device is 20-50 nm, and the molecular weight cutoff of the ultrafiltration membrane device is 800-1000 Da.

[0012] As an improved technical solution, the outlet of the cation exchange resin column is connected to a macroporous adsorption resin column via a pipeline, and the outlet of the macroporous adsorption resin column is connected to the anion exchange resin column via a pipeline.

[0013] As a preferred technical solution, the liquid phase outlet of the first filter is connected to a coarse crystallization mother liquor tank via a pipeline, and the outlet of the coarse crystallization mother liquor tank is connected to the flocculation tank via a pipeline.

[0014] As a preferred technical solution, the outlet of the crude product tank is connected to a dissolving tank via a pipeline, the inlet of the dissolving tank is connected to a second purified water tank via a pipeline, the outlet of the dissolving tank is connected to a second filter via a pipeline, the outlet of the second filter is connected to a second crystallization tank via a pipeline, the inlet of the second crystallization tank is connected to a solvent tank via a pipeline, the outlet of the second crystallization tank is connected to a third filter via a pipeline, the solid phase outlet of the third filter is connected to a dryer via a pipeline, and the outlet of the dryer is connected to a squalene pure product tank via a pipeline.

[0015] As a preferred technical solution, the inlet of the dissolving tank is connected to an activated carbon tank via a pipe.

[0016] As a preferred technical solution, the liquid phase outlet of the third filter is connected to a refined mother liquor tank via a pipeline, and the outlet of the refined mother liquor tank is connected to the dissolving tank via a pipeline.

[0017] Due to the adoption of the above technical solution, the beneficial effects of this utility model are:

[0018] This utility model discloses a squalene separation and preparation apparatus, comprising a squalene conversion liquid tank, an outlet of which is connected to a flocculation tank via a pipeline, an inlet of which is connected to a glacial acetic acid tank via a pipeline, an outlet of which is connected to a ceramic membrane device via a pipeline, a clear liquid outlet of which is connected to an ultrafiltration membrane device via a pipeline, a clear liquid outlet of which is connected to a cation exchange resin column via a pipeline, an outlet of which is connected to an anion exchange resin column via a pipeline, an outlet of which is connected to a concentration tank via a pipeline, an outlet of which is connected to a first crystallization tank via a pipeline, an inlet of which is connected to a seed crystal tank via a pipeline, an outlet of which is connected to a first filter via a pipeline, a solid phase outlet of which is connected to a rinsing tank via a pipeline, an inlet of which is connected to a first purified water tank via a pipeline, and an outlet of which is connected to a crude product tank via a pipeline. Through a multi-step synergistic operation involving flocculation, membrane filtration, ion exchange, crystallization, and filtration rinsing, impurities in the conversion solution are gradually removed and squalene is initially enriched. This provides a stable and systematic process route for obtaining crude squalene, ensuring the orderliness and effectiveness of the initial separation and preparation. This separation and preparation process does not use highly hazardous boric acid, shortens the preparation process, does not form squalene-boric acid complex salts in the intermediate process, and does not require subsequent acid hydrolysis of the complex salts. While shortening the process, it increases the yield and saves production and equipment costs. The finished product has no boric acid residue, making it safer and more acceptable to consumers. The preparation process is also safer and more friendly to human health and the ecological environment. It eliminates the need to treat boron-containing mother liquor, resulting in less investment in environmental protection facilities.

[0019] The inlet of the flocculation tank of this invention is connected to a polyaspartic acid (PAA) tank via a pipeline. PAA, as a highly efficient flocculant, can form larger and more stable flocs with suspended impurities and colloidal particles in the conversion liquid. Compared to using glacial acetic acid alone, it can significantly improve the flocculation effect, accelerate the sedimentation rate of impurities, reduce flocculation time, and simultaneously reduce the filtration load of the subsequent ceramic membrane device, preventing membrane pore blockage, extending the service life of the ceramic membrane, and improving the overall separation efficiency.

[0020] The outlet of the ultrafiltration membrane clarified solution is connected to a nanofiltration membrane device via a pipeline, and the clarified solution outlet of the nanofiltration membrane device is connected to the cation exchange resin column via a pipeline. In addition to ultrafiltration removing large molecular impurities, adding a nanofiltration membrane device can further retain substances in the ultrafiltration clarified solution with molecular weights between small molecular impurities and squalene (such as some oligosaccharides, small molecular polymers, etc.), achieving further purification of squalene, reducing the processing pressure on the subsequent cation exchange resin column, increasing the purity of the feed solution entering the ion exchange stage, and laying a better foundation for subsequent purification.

[0021] The nanofiltration membrane device has a molecular weight cutoff of 200-300 Da, effectively retaining some polysaccharide fragments and large organic molecules, while ensuring the smooth passage of squalinosin. Under the premise of ensuring the removal of impurities, it minimizes the loss of squalinosin and improves the recovery rate and product purity of squalinosin.

[0022] The ceramic membrane device has a filter size of 20-50 nm, and the ultrafiltration membrane device has a molecular weight cutoff of 800-1000 Da. This filter size of the ceramic membrane can efficiently remove larger flocs, suspended particles, and some microorganisms from the conversion solution after flocculation, preventing clogging of the subsequent ultrafiltration membrane. The molecular weight cutoff of the ultrafiltration membrane can effectively retain large protein molecules, colloids, polysaccharides, and other impurities. The two-step membrane filtration process is clearly defined and works synergistically to gradually refine the particle size of impurities, providing a higher purity feed solution for the subsequent ion exchange stage and improving the adsorption selectivity and treatment efficiency of the ion exchange resin.

[0023] The outlet of the cation exchange resin column is connected to a macroporous adsorption resin column via a pipeline, and the outlet of the macroporous adsorption resin column is connected to the anion exchange resin column via a pipeline. After cation exchange removes cationic impurities, the macroporous adsorption resin column can further remove pigments and some organic impurities in the feed solution through physical adsorption, compensating for the insufficient removal capacity of the cation exchange resin for these impurities, improving the color and purity of the feed solution, reducing impurity interference from the subsequent anion exchange resin column, and improving the overall separation and purification effect.

[0024] The liquid phase outlet of the first filter is connected to a coarse crystallization mother liquor tank via a pipeline, and the outlet of the coarse crystallization mother liquor tank is connected to the flocculation tank via a pipeline. This achieves the recycling of the coarse crystallization mother liquor. The coarse crystallization mother liquor still contains a certain amount of squalene, which is returned to the flocculation tank to participate in the separation process again. This can effectively improve the total recovery rate of squalene, reduce raw material waste, and at the same time reduce the environmental pressure and resource consumption caused by mother liquor discharge, thereby improving the economic efficiency and environmental friendliness of the equipment.

[0025] The outlet of the crude product tank is connected to a dissolving tank via a pipeline. The inlet of the dissolving tank is connected to a second purified water tank via a pipeline. The outlet of the dissolving tank is connected to a second filter via a pipeline. The outlet of the second filter is connected to a second crystallization tank via a pipeline. The inlet of the second crystallization tank is connected to a solvent tank via a pipeline. The outlet of the second crystallization tank is connected to a third filter via a pipeline. The solid phase outlet of the third filter is connected to a dryer via a pipeline. The outlet of the dryer is connected to a squalene pure product tank via a pipeline. Through steps such as dissolving in purified water, filtering to remove impurities, adding ethanol for crystallization, and filtering and drying again, residual impurities (such as small amounts of salt and fine impurity particles) in the crude product are deeply removed, significantly improving the purity of the squalene product and meeting the production requirements of high-purity squalene.

[0026] The inlet of the dissolving tank is connected to an activated carbon tank via a pipe. Activated carbon has a strong adsorption capacity, which can effectively adsorb pigments, odor substances and some organic impurities in the crude product solution after dissolution, further improving the color and purity of the solution, avoiding these impurities from affecting the subsequent crystallization effect and the quality of the final product, so that the refined squalene product has a greater advantage in appearance and purity.

[0027] The liquid outlet of the third filter is connected to a refining mother liquor tank via a pipeline, and the outlet of the refining mother liquor tank is connected to the dissolving tank via a pipeline. This enables the recycling of the refining mother liquor. The refining mother liquor still contains incompletely crystallized squalene; returning it to the dissolving tank to participate in the refining process further improves the squalene recovery rate, reduces product loss during refining, lowers mother liquor emissions, enhances the resource utilization and environmental performance of the equipment, and reduces production costs. Attached Figure Description

[0028] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0029] Figure 1 This is a structural schematic diagram of an embodiment of the present utility model;

[0030] The components include: 1. Squalene conversion solution tank; 2. Flocculation tank; 3. Glacial acetic acid tank; 4. Ceramic membrane device; 5. Ultrafiltration membrane device; 6. Cation exchange resin column; 7. Anion exchange resin column; 8. Concentration tank; 9. First crystallization tank; 10. Seed crystal tank; 11. First filter; 12. Washing tank; 13. First purified water tank; 14. Crude product tank; 15. Polyaspartic acid salt tank; 16. Nanofiltration membrane device; 17. Macroporous adsorption resin column; 18. Crude crystallization mother liquor tank; 19. Dissolving tank; 20. Second purified water tank; 21. Second filter; 22. Second crystallization tank; 23. Solvent tank; 24. Third filter; 25. Dryer; 26. Squalene pure product tank; 27. Activated carbon tank; 28. Refined mother liquor tank. Detailed Implementation

[0031] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0032] like Figure 1 As shown, an apparatus for separating and preparing squalene includes a squalene conversion liquid tank 1. The outlet of the squalene conversion liquid tank 1 is connected to a flocculation tank 2 via a pipeline. The inlet of the flocculation tank 2 is connected to a glacial acetic acid tank 3 via a pipeline. The outlet of the flocculation tank 2 is connected to a ceramic membrane device 4 via a pipeline. The clear liquid outlet of the ceramic membrane device 4 is connected to an ultrafiltration membrane device 5 via a pipeline. The clear liquid outlet of the ultrafiltration membrane device 5 is connected to a cation exchange resin column 6 via a pipeline. The outlet of the cation exchange resin column 6 is connected to an anion exchange resin column 7 via a pipeline. The outlet of the anion exchange resin column 7 is connected to a concentration tank 8 via a pipeline. The outlet of the concentration tank 8 is connected to a first crystallization tank 9 via a pipeline. The inlet of the first crystallization tank 9 is connected to a seed crystal tank 10 via a pipeline. The outlet of the first crystallization tank 9 is connected to a first filter 11 via a pipeline. The solid phase outlet of the first filter 11 is connected to a rinsing tank 12 via a pipeline. The inlet of the rinsing tank 12 is connected to a first purified water tank 13 via a pipeline. The outlet of the rinsing tank 12 is connected to a crude product tank 14 via a pipeline. Through a multi-step synergistic operation involving flocculation, membrane filtration, ion exchange, crystallization, and filtration rinsing, impurities in the conversion solution are gradually removed and squalene is initially enriched. This provides a stable and systematic process route for obtaining crude squalene, ensuring the orderliness and effectiveness of the initial separation and preparation. This separation and preparation process does not use highly hazardous boric acid, shortens the preparation process, does not form squalene-boric acid complex salts in the intermediate process, and does not require subsequent acid hydrolysis of the complex salts. While shortening the process, it increases the yield and saves production and equipment costs. The finished product has no boric acid residue, making it safer and more acceptable to consumers. The preparation process is also safer and more friendly to human health and the ecological environment. It eliminates the need to treat boron-containing mother liquor, resulting in less investment in environmental protection facilities.

[0033] The inlet of flocculation tank 2 is connected to polyaspartic acid tank 15 via a pipeline. As a highly efficient flocculant, polyaspartic acid can form larger and more stable flocs with suspended impurities and colloidal particles in the conversion liquid. Compared with using glacial acetic acid alone, it can significantly improve the flocculation effect, accelerate the sedimentation rate of impurities, reduce flocculation time, and at the same time reduce the filtration load of the subsequent ceramic membrane device 4, avoid membrane pore blockage, extend the service life of the ceramic membrane, and improve the overall separation efficiency.

[0034] The outlet of the ultrafiltration membrane clarified solution is connected to a nanofiltration membrane device 16 via a pipeline, and the clarified solution outlet of the nanofiltration membrane device 16 is connected to the cation exchange resin column 6 via a pipeline. In addition to ultrafiltration removing large molecular impurities, the addition of the nanofiltration membrane device 16 can further retain substances in the ultrafiltration clarified solution with molecular weights between small molecular impurities and squalene (such as some oligosaccharides, small molecular polymers, etc.), achieving further purification of squalene, reducing the processing pressure on the subsequent cation exchange resin column 6, increasing the purity of the feed solution entering the ion exchange stage, and laying a better foundation for subsequent purification.

[0035] The nanofiltration membrane device 16 has a molecular weight cutoff of 200-300 Da, effectively retaining some polysaccharide fragments, large organic molecules, etc., while ensuring that squalene passes through smoothly. Under the premise of ensuring the removal of impurities, it minimizes the loss of squalene and improves the recovery rate and product purity of squalene.

[0036] The ceramic membrane device 4 has a filter size of 20-50 nm, and the ultrafiltration membrane device 5 has a molecular weight cutoff of 800-1000 Da. This filter size of the ceramic membrane can efficiently remove larger flocs, suspended particles, and some microorganisms from the conversion solution after flocculation, preventing clogging of the subsequent ultrafiltration membrane. The molecular weight cutoff of the ultrafiltration membrane can effectively retain large protein molecules, colloids, polysaccharides, and other impurities. The two-step membrane filtration has a clear division of labor and works synergistically to gradually refine the particle size of impurities, providing a higher purity feed solution for the subsequent ion exchange stage and improving the adsorption selectivity and treatment efficiency of the ion exchange resin.

[0037] The outlet of the cation exchange resin column 6 is connected to a macroporous adsorption resin column 17 via a pipe, and the outlet of the macroporous adsorption resin column 17 is connected to the anion exchange resin column 7 via a pipe. After cation exchange removes cationic impurities, the macroporous adsorption resin column 17 can further remove pigments and some organic impurities in the feed solution through physical adsorption, compensating for the insufficient removal capacity of the cation exchange resin for these impurities, improving the color and purity of the feed solution, reducing impurity interference from the subsequent anion exchange resin column 7, and improving the overall separation and purification effect.

[0038] The liquid phase outlet of the first filter 11 is connected to a coarse crystallization mother liquor tank 18 via a pipeline, and the outlet of the coarse crystallization mother liquor tank 18 is connected to the flocculation tank 2 via a pipeline. This achieves the recycling of the coarse crystallization mother liquor. The coarse crystallization mother liquor still contains a certain amount of squalene, which is returned to the flocculation tank 2 to participate in the separation process again. This can effectively improve the total recovery rate of squalene, reduce raw material waste, and at the same time reduce the environmental pressure and resource consumption caused by mother liquor discharge, thereby improving the economic efficiency and environmental friendliness of the equipment.

[0039] The outlet of the crude product tank 14 is connected to a dissolving tank 19 via a pipeline. The inlet of the dissolving tank 19 is connected to a second purified water tank 20 via a pipeline. The outlet of the dissolving tank 19 is connected to a second filter 21 via a pipeline. The outlet of the second filter 21 is connected to a second crystallization tank 22 via a pipeline. The inlet of the second crystallization tank 22 is connected to a solvent tank 23 via a pipeline. The outlet of the second crystallization tank 22 is connected to a third filter 24 via a pipeline. The solid phase outlet of the third filter 24 is connected to a dryer 25 via a pipeline. The outlet of the dryer 25 is connected to a squalene pure product tank 26 via a pipeline. Through steps such as dissolving in purified water, filtering to remove impurities, adding solvent ethanol for crystallization, and filtering and drying again, residual impurities (such as small amounts of salt and fine impurity particles) in the crude product are deeply removed, significantly improving the purity of the squalene product and meeting the production requirements of high-purity squalene.

[0040] The inlet of the dissolving tank 19 is connected to the activated carbon tank 27 via a pipe. Activated carbon has a strong adsorption capacity and can effectively adsorb pigments, odor substances and some organic impurities in the crude product solution after dissolution, further improving the color and purity of the solution, avoiding these impurities from affecting the subsequent crystallization effect and the quality of the final product, so that the refined squalene product has a greater advantage in appearance and purity.

[0041] The liquid outlet of the third filter 24 is connected to a refining mother liquor tank 28 via a pipeline, and the outlet of the refining mother liquor tank 28 is connected to the dissolving tank 19 via a pipeline. This enables the recycling of the refining mother liquor. The refining mother liquor still contains incompletely crystallized squalene, which is returned to the dissolving tank 19 to participate in the refining process. This can further improve the recovery rate of squalene, reduce product loss during the refining process, reduce mother liquor discharge, improve the resource utilization and environmental performance of the equipment, and reduce production costs.

[0042] It should be understood that these embodiments are for illustrative purposes only and are not intended to limit the scope of the present invention. Furthermore, it should be understood that after reading the teachings of this invention, those skilled in the art can make various alterations or modifications to the invention, and these equivalent forms also fall within the scope defined by the appended claims.

Claims

1. A device for separating and preparing squalene, comprising a squalene conversion tank, characterized in that: The outlet of the squalene conversion tank is connected to a flocculation tank via a pipeline. The inlet of the flocculation tank is connected to a glacial acetic acid tank via a pipeline. The outlet of the flocculation tank is connected to a ceramic membrane device via a pipeline. The clear liquid outlet of the ceramic membrane device is connected to an ultrafiltration membrane device via a pipeline. The clear liquid outlet of the ultrafiltration membrane device is connected to a cation exchange resin column via a pipeline. The outlet of the cation exchange resin column is connected to an anion exchange resin column via a pipeline. The outlet of the anion exchange resin column is connected to a concentration tank via a pipeline. The outlet of the concentration tank is connected to a first crystallization tank via a pipeline. The inlet of the first crystallization tank is connected to a seed crystal tank via a pipeline. The outlet of the first crystallization tank is connected to a first filter via a pipeline. The solid phase outlet of the first filter is connected to a rinsing tank via a pipeline. The inlet of the rinsing tank is connected to a first purified water tank via a pipeline. The outlet of the rinsing tank is connected to a crude product tank via a pipeline.

2. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The inlet of the flocculation tank is connected to a polyaspartic acid salt tank via a pipe.

3. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The outlet of the ultrafiltration membrane supernatant is connected to a nanofiltration membrane device via a pipeline, and the supernatant outlet of the nanofiltration membrane device is connected to the cation exchange resin column via a pipeline.

4. The apparatus for separating and preparing squalene as described in claim 3, characterized in that: The nanofiltration membrane device has a molecular weight cutoff of 200-300 Da.

5. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The ceramic membrane device has a filter size of 20-50 nm, and the ultrafiltration membrane device has a molecular weight cutoff of 800-1000 Da.

6. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The outlet of the cation exchange resin column is connected to a macroporous adsorption resin column via a pipe, and the outlet of the macroporous adsorption resin column is connected to the anion exchange resin column via a pipe.

7. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The liquid phase outlet of the first filter is connected to a coarse crystallization mother liquor tank via a pipeline, and the outlet of the coarse crystallization mother liquor tank is connected to the flocculation tank via a pipeline.

8. The apparatus for separating and preparing squalene as described in claim 1, characterized in that: The outlet of the crude product tank is connected to a dissolving tank via a pipeline. The inlet of the dissolving tank is connected to a second purified water tank via a pipeline. The outlet of the dissolving tank is connected to a second filter via a pipeline. The outlet of the second filter is connected to a second crystallization tank via a pipeline. The inlet of the second crystallization tank is connected to a solvent tank via a pipeline. The outlet of the second crystallization tank is connected to a third filter via a pipeline. The solid phase outlet of the third filter is connected to a dryer via a pipeline. The outlet of the dryer is connected to a squalene pure product tank via a pipeline.

9. The apparatus for separating and preparing squalene as described in claim 8, characterized in that: The inlet of the dissolving tank is connected to an activated carbon tank via a pipe.

10. The apparatus for separating and preparing squalene as described in claim 8, characterized in that: The liquid phase outlet of the third filter is connected to a refined mother liquor tank via a pipeline, and the outlet of the refined mother liquor tank is connected to the dissolving tank via a pipeline.

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