A high-efficiency separation type oil deacidification refining method

Abstract

The application discloses a high-efficiency separation type oil deacidification refining method and belongs to the technical field of oil processing. The method comprises the steps of raw material pretreatment, deacidification reaction, separation and post-treatment, and is characterized in that the method specifically comprises the following steps: S1, raw material pretreatment; S2, micro-flow field selective complexation reaction; S3, two-stage gradient ceramic membrane cross-flow separation; S4, refining post-treatment; and S5, degreasing agent regeneration and by-product recovery. The high-efficiency separation type oil deacidification refining method solves the technical problems of large oil loss, high energy consumption, more three-waste emissions and poor thermal sensitivity adaptability in the traditional deacidification process, and realizes low-temperature, high-efficiency and green continuous oil deacidification.

Description

Technical Field

[0001] This invention relates to the field of oil processing technology, and in particular to a highly efficient separation-type deacidification and refining method for oils. Background Technology

[0002] In existing technologies, oil deacidification is the core process for removing free fatty acids from crude oil, directly determining the quality, yield, and processing cost of the finished oil. Currently, the mainstream industrial deacidification technologies are as follows: Alkali refining method: This method neutralizes free fatty acids with alkali to produce soapstock, which is then removed by sedimentation. This process results in a neutral oil saponification loss rate of 3%–8%, and the soapstock carries a large amount of neutral oil. It also generates high-COD wastewater and hazardous soapstock waste, placing significant pressure on environmental treatment. Furthermore, it is economically inefficient for high-acid-value oils due to high alkali consumption.

[0003] Physical distillation deacidification: This method relies on high-temperature (240-260℃) and high-vacuum steam distillation to remove free fatty acids. This process is energy-intensive, easily leads to the oxidation and polymerization of unsaturated oils, the formation of trans fatty acids, and the destruction of natural active substances such as vitamin E and phytosterols. It is not suitable for highly unsaturated heat-sensitive oils such as flaxseed oil and fish oil.

[0004] Single membrane separation deacidification: This method uses the difference in membrane pore size to separate fatty acids and neutral oils. However, it generally suffers from problems such as rapid membrane flux decay, severe oil phase contamination, limited separation accuracy, and difficulty in long-term continuous operation, which limits its industrial application.

[0005] While existing technologies have attempted to combine complexing agents with membrane separation, they generally employ an integrated reaction-separation design, resulting in low mass transfer efficiency, incomplete separation, and poor selectivity of complexing agents for free fatty acids, leading to neutral oil entrainment losses. Consequently, they cannot simultaneously achieve the multiple objectives of high acidity, low oil loss, and green and low-carbon development. Summary of the Invention

[0006] The purpose of this invention is to provide a highly efficient separation-type deacidification and refining method for oils and fats, which solves the technical problems of large oil loss, high energy consumption, large emissions of waste gas, wastewater, and poor heat sensitivity adaptability in traditional deacidification processes, and achieves low-temperature, high-efficiency, green and continuous deacidification of oils and fats.

[0007] To achieve the above objectives, the present invention provides a highly efficient separation-based deacidification and refining method for oils, comprising raw material pretreatment, deacidification reaction, separation, and post-treatment steps, characterized by the following specific steps: S1. Raw material pretreatment: Filter the crude oil to be deacidified to remove mechanical impurities and preheat it to 30~55℃; S2. Microfluidic selective complexation reaction: The preheated oil and amino-modified β-cyclodextrin deacidifying agent aqueous solution are continuously fed into the microfluidic reactor at a mass ratio of 100:8~20. The complexation reaction is carried out under normal pressure and 30~55℃ conditions, with a hydraulic residence time of 5~60s, to obtain a mixture of oil phase and loaded fatty acid deacidifying agent phase. S3. Two-stage gradient ceramic membrane cross-flow separation: The mixture obtained in step S2 is fed into a two-stage gradient pore size ceramic membrane cross-flow separation system for continuous separation. The primary coarse separation uses a zirconia ceramic membrane with a pore size of 50~100nm, an operating pressure of 0.2~0.4MPa, and a cross-flow velocity of 3~5m / s. The permeated deacidifying agent-rich phase is collected, and the retained concentrated oil phase is returned to the microflow reactor for recycling. The secondary deep separation uses an alumina ceramic membrane with a pore size of 5~20nm, an operating pressure of 0.3~0.5MPa, and a cross-flow velocity of 2~4m / s to perform deep separation on the primary concentrated oil phase to remove trace amounts of deacidifying agent. The secondary permeate is incorporated into the primary deacidifying agent-rich phase, and the secondary concentrate is the deacidified crude oil product. S4. Refining and post-processing: After precision filtration, the deacidified crude oil is vacuum dried to remove trace amounts of moisture, resulting in refined deacidified oil. S5. Degreasing agent regeneration and by-product recovery: The deacidifying agent rich phase obtained in step S3 is sent to a vacuum desorption tank and stripped under vacuum at 65~80℃ and 8~15kPa absolute pressure. Free fatty acids escape with water vapor and are condensed to obtain crude fatty acid by-products. The desorbed deacidifying agent solution is decolorized by adsorption of granular activated carbon and then returned to the deacidifying agent storage tank of step S2 for recycling.

[0008] Preferably, the aqueous solution of the amino-modified β-cyclodextrin deacidifying agent in step S2 is composed of the following components by mass fraction: 15%~25% mono-6-amino-β-cyclodextrin, 5%~10% propylene glycol, and the balance being deionized water.

[0009] Preferably, the reaction temperature of the microfluidic reactor in step S2 is the same as the preheating temperature in step S1, and the hydraulic residence time is 20~50s.

[0010] Preferably, the operating temperature of the two-stage ceramic membrane separation process in step S3 is the same as the reaction temperature in step S2.

[0011] Preferably, the zirconia ceramic membrane used for primary coarse separation in step S3 has a pore size of 60~80nm, an operating pressure of 0.25~0.45MPa, and a cross-flow velocity of 3.5~4.5m / s.

[0012] Preferably, the zirconia ceramic membrane used for secondary deep separation in step S3 has a pore size of 8~15nm, an operating pressure of 0.35~0.45MPa, and a cross-flow velocity of 2.5~3.5m / s.

[0013] Preferably, the filtration accuracy of the precision filter in step S4 is 1 μm; the conditions for vacuum drying are: temperature 45~60℃, absolute pressure 5~10 kPa.

[0014] Preferably, the crude fatty acid is purified by short-path distillation to obtain industrial-grade free fatty acids with a purity of ≥95%.

[0015] Preferably, the crude oil to be deacidified in step S1 has an acid value of 5~35 mgKOH / g, including any one of rice bran oil, rapeseed oil, palm oil, flaxseed oil, fish oil or waste recycled oil.

[0016] Preferably, the adsorption and decolorization temperature of the granular activated carbon in step S5 is 40~60℃, the amount of activated carbon added is 0.5%~2% of the mass of the deacidifying agent solution, and the adsorption time is 20~40min.

[0017] Therefore, the present invention employs the above-mentioned highly efficient separation-type oil deacidification and refining method, and the technical effects are as follows: 1) High deacidification precision and extremely low neutral oil loss: For oils with an acid value of 5~35mgKOH / g, the deacidification rate is ≥98.5% and the neutral oil loss rate is ≤0.8%, which is far superior to the oil loss level of 3%~8% in the traditional alkali refining method, greatly improving the oil yield and economic benefits.

[0018] 2) Gentle process to protect oil quality: The maximum temperature throughout the process does not exceed 80℃, avoiding oil oxidation and polymerization and the formation of trans fatty acids caused by high temperature, and fully preserving natural active ingredients such as vitamin E and phytosterols, especially suitable for highly unsaturated heat-sensitive oils.

[0019] 3) The efficiency of the split architecture is significantly improved: the reaction unit adopts micro-flow field to enhance mass transfer, and the reaction time is shortened from tens of minutes to tens of seconds, with an efficiency improvement of more than 10 times; the separation unit adopts gradient cross-flow membrane separation, which can operate continuously and has a separation efficiency far higher than that of traditional sedimentation separation, without the problem of soap residue entrainment.

[0020] 4) Green and low-carbon, with less waste discharge: No soap residue hazardous waste is generated, and wastewater discharge is reduced by more than 90% compared with the traditional alkali refining method; the deacidifying agent has a recycling rate of ≥98%, resulting in low operating costs. At the same time, high-value-added fatty acid by-products can be recovered, improving overall benefits.

[0021] 5) Wide range of compatibility and easy industrialization: It is compatible with low acid value refined semi-finished products and high acid value acidified oil and waste oil. All the equipment involved are mature industrial equipment, which is easy to scale up and modify existing production lines.

[0022] The technical solution of the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. Attached Figure Description

[0023] Figure 1 This is a flowchart of an embodiment of an efficient separation-type oil deacidification and refining method according to the present invention. Detailed Implementation

[0024] The technical solution of the present invention will be further described below with reference to the accompanying drawings and embodiments.

[0025] Unless otherwise defined, the technical or scientific terms used in this invention shall have the ordinary meaning understood by one of ordinary skill in the art to which this invention pertains. The terms "first," "second," and similar terms used in this invention do not indicate any order, quantity, or importance, but are merely used to distinguish different components. Terms such as "comprising" or "including" mean that the element or object preceding the word encompasses the elements or objects listed following the word and their equivalents, without excluding other elements or objects. Terms such as "connected" or "linked" are not limited to physical or mechanical connections, but can include electrical connections, whether direct or indirect. Terms such as "upper," "lower," "left," and "right" are used only to indicate relative positional relationships; when the absolute position of the described object changes, the relative positional relationship may also change accordingly.

[0026] Example 1 For deacidification and refining of rice bran oil with medium acid value, the raw material is crude rice bran oil with an acid value of 18.6 mg KOH / g, a moisture content of 0.25%, and impurities of 0.08%.

[0027] like Figure 1 As shown, this invention provides a highly efficient separation-based deacidification and refining method for oils, including raw material pretreatment, deacidification reaction, separation, and post-treatment processes; the specific process steps are as follows: S1. Raw material pretreatment: Crude rice bran oil is filtered through a plate and frame filter press to remove mechanical impurities, preheated to 45°C through a plate heat exchanger, and then temporarily stored in a raw material buffer tank.

[0028] S2. Microfluidic Selective Complexation Reaction: Prepare an aqueous solution of deacidifying agent, by mass fraction: 20% mono-6-amino-β-cyclodextrin, 8% propylene glycol, and the remainder deionized water. The preheated oil and the deacidifying agent aqueous solution are continuously fed into a microfluidic reactor at a mass ratio of 100:12. The complexation reaction is carried out at atmospheric pressure and 45°C with a hydraulic residence time of 30 s. After the reaction is complete, a mixture of the oil phase and the phase loaded with fatty acid deacidifying agent is obtained.

[0029] S3, Two-stage gradient ceramic membrane cross-flow separation: The mixture is fed into a two-stage ceramic membrane cross-flow separation system, with the operating temperature maintained at 45℃ throughout the process. Primary coarse separation: A zirconia ceramic membrane with a pore size of 70 nm is used, the operating pressure is 0.3 MPa, and the cross-flow velocity is 4 m / s; the deacidifying agent-rich phase is collected on the permeate side, and the retained concentrated oil phase is returned to the inlet of the microflow reactor for recycling reaction, thereby enhancing the deacidification depth.

[0030] Secondary deep separation: Alumina ceramic membrane with a pore size of 10nm is used, with an operating pressure of 0.4MPa and a cross-flow velocity of 3m / s; the primary concentrated oil phase is deeply separated to remove trace amounts of deacidifying agent entrained in the oil phase, and the secondary permeate is incorporated into the primary deacidifying agent-rich phase. The secondary concentrate is the deacidified crude oil product.

[0031] S4. Refining and post-processing: The deacidified crude oil is filtered with a precision of 1μm to remove trace particulate matter, and then sent to a vacuum thin-film dryer to remove trace moisture under conditions of 55℃ and 8kPa absolute pressure to obtain the finished refined deacidified rice bran oil.

[0032] S5. Deacidifying agent regeneration and by-product recovery: The deacidifying agent rich phase obtained from the two-stage membrane separation is sent to a vacuum desorption tank. Under the conditions of 70℃ and 10kPa absolute pressure, vacuum stripping decomplexes the free fatty acids, which escape with water vapor. After condensation, crude fatty acid by-products are obtained. 1% of granular activated carbon is added to the desorbed deacidifying agent solution, and adsorption and decolorization are carried out at 50℃ for 30 minutes. After filtration, the solution is returned to the deacidifying agent storage tank of step S2 for recycling. The crude fatty acids are further purified by short-path distillation to obtain industrial-grade free fatty acids.

[0033] Test results: The finished product acid value was 0.26 mg KOH / g, the deacidification rate was 98.6%; the neutral oil loss rate was 0.72%; the vitamin E retention rate was 92.7%; no trans fatty acids were detected; and the deacidifying agent recycling rate was 98.3%.

[0034] Example 2 For deacidification of high-acid-value palm oil, the raw material is palm oil with an acid value of 32.4 mg KOH / g, moisture content of 0.32%, and impurities of 0.12%. Specific process steps are as follows: S1. Raw material pretreatment: The palm acidified oil is filtered through a plate and frame filter press to remove mechanical impurities, preheated to 50°C, and then sent to the raw material buffer tank.

[0035] S2. Microfluidic Selective Complexation Reaction: Prepare an aqueous solution of deacidifying agent, by mass fraction: 25% mono-6-amino-β-cyclodextrin, 10% propylene glycol, and the remainder deionized water. The oil and the deacidifying agent aqueous solution are continuously fed into a microfluidic reactor at a mass ratio of 100:18. The reaction is carried out at atmospheric pressure and 50°C with a hydraulic residence time of 50 s, yielding a mixture of the oil phase and the phase loaded with fatty acid deacidifying agent.

[0036] S3, Two-stage gradient ceramic membrane cross-flow separation: Operating temperature maintained at 50℃ throughout: Primary coarse separation: A zirconia ceramic membrane with an 80 nm pore size is used, the operating pressure is 0.35 MPa, and the cross-flow velocity is 4.5 m / s; the retained concentrated oil phase is recycled back to the microflow reactor.

[0037] Secondary deep separation: Alumina ceramic membrane with a pore size of 15nm is used, the operating pressure is 0.45MPa, and the cross-flow velocity is 3.5m / s; the secondary permeate is incorporated into the primary deacidifying agent enrichment phase, and the secondary concentrate is the deacidified crude oil.

[0038] S4. Refining and post-processing: After the deacidified crude oil is filtered through a 1μm precision filter, it is vacuum dried at 60℃ and 7kPa absolute pressure to obtain the finished deacidified oil.

[0039] S5. Deacidifying agent regeneration and by-product recovery: The deacidifying agent is fed into a vacuum desorption tank and stripped under reduced pressure at 75℃ and 10kPa absolute pressure to decomposite it. Crude fatty acids are recovered by condensation. 1.5% of granular activated carbon is added to the desorbed deacidifying agent solution. The solution is adsorbed and decolorized at 55℃ for 35 minutes. After filtration, it is recycled. The crude fatty acids are purified by short-path distillation to obtain high-purity fatty acids.

[0040] Test results: The acid value of the finished product was 0.48 mg KOH / g, the deacidification rate was 98.5%; the neutral oil loss rate was 0.78%; the purity of the recovered crude fatty acid was 92%, and the purity reached 95.8% after short-path distillation; the recycling rate of the deacidifying agent was 98.1%.

[0041] Example 3 For low-temperature deacidification of cold-pressed flaxseed oil (a heat-sensitive oil), the raw material is cold-pressed flaxseed oil with an acid value of 6.2 mg KOH / g, moisture content of 0.18%, impurities of 0.05%, and α-linolenic acid content of 57.2%. Specific processing steps are as follows: S1. Raw material pretreatment: Cold-pressed flaxseed oil is filtered to remove mechanical impurities, preheated to 35°C, and then sent to the raw material buffer tank.

[0042] S2. Microfluidic Selective Complexation Reaction: Prepare an aqueous solution of deacidifying agent, by mass fraction: 15% mono-6-amino-β-cyclodextrin, 5% propylene glycol, and the remainder is deionized water. The oil and the deacidifying agent aqueous solution are continuously fed into a microfluidic reactor at a mass ratio of 100:10. The reaction is carried out at atmospheric pressure and 35°C with a hydraulic residence time of 20 s to obtain a mixed solution.

[0043] S3, Two-stage gradient ceramic membrane cross-flow separation: Operating temperature maintained at 35℃ throughout: Primary coarse separation: A zirconia ceramic membrane with a pore size of 60 nm is used, the operating pressure is 0.25 MPa, and the cross-flow velocity is 3 m / s; the concentrated oil phase is recycled back to the reactor.

[0044] Secondary deep separation: using an alumina ceramic membrane with an 8nm pore size, operating pressure of 0.35MPa, and cross-flow velocity of 2.5m / s; the secondary concentrate is deacidified crude oil.

[0045] S4. Refining and post-processing: After the deacidified crude oil is filtered through a 1μm precision filter, it is vacuum dried at 45℃ and 9kPa absolute pressure to obtain the finished deacidified flaxseed oil.

[0046] S5. Deacidifying agent regeneration and by-product recovery: The deacidifying agent is fed into a vacuum desorption tank and stripped under reduced pressure at 65℃ and 12kPa to decomposite and recover crude fatty acids; 0.8% of granular activated carbon is added to the desorbed deacidifying agent solution, and adsorption and decolorization are carried out at 45℃ for 25 minutes. After filtration, it is recycled.

[0047] Test results: The finished product acid value was 0.09 mg KOH / g, the deacidification rate was 98.5%; the neutral oil loss rate was 0.65%; the α-linolenic acid retention rate was 95.1%; the vitamin E retention rate was 94.2%; and no trans fatty acids were detected.

[0048] Comparative Example 1: The same batch of rice bran oil was treated using the traditional alkali refining method; Raw material: crude rice bran oil from the same batch as in the example, with an acid value of 18.6 mg KOH / g.

[0049] Process: The traditional intermittent alkali refining method is adopted. The alkali solution is 12°Bé sodium hydroxide solution, the excess alkali is 0.3%, the neutralization temperature is 65℃, the neutralization stirring time is 30min, and the soap residue is separated by standing and settling for 4h. The oil phase is washed with hot water and vacuum dried to obtain the finished product.

[0050] Test results: The acid value of the finished product was 0.32 mg KOH / g, the deacidification rate was 98.3%, the neutral oil loss rate was 4.2%, the vitamin E retention rate was 78.5%, the dry basis weight of the soap stubble was 6.8% of the raw oil, and the COD concentration of the washing wastewater was 12500 mg / L.

[0051] Comparative Example 2: Direct separation and deacidification using a single ceramic membrane. Raw material: crude rice bran oil from the same batch as in Example 1, with an acid value of 18.6 mg KOH / g.

[0052] Process: The crude oil is preheated to 45°C and directly introduced into a zirconia ceramic membrane with a pore size of 50nm for cross-flow separation. The operating pressure is 0.3MPa, the cross-flow velocity is 4m / s, and the process is carried out continuously for 4 hours.

[0053] Test results: The finished product acid value was 2.1 mg KOH / g, the deacidification rate was 88.7%, the neutral oil loss rate was 1.5%, and the membrane flux decreased by 38% after 4 hours of continuous operation, making it impossible to maintain stable separation accuracy.

[0054] A comparison of the examples and comparative examples shows that: The deacidification rate of this invention is comparable to that of the traditional alkali refining method, but the neutral oil loss rate is only 1 / 5 to 1 / 6 of that of the traditional alkali refining method, which greatly improves the oil yield. The entire process operates at low temperatures, resulting in a 15% or higher retention rate of heat-sensitive active ingredients compared to traditional processes. No trans fatty acids are generated, significantly improving the quality of the oil. The two-stage gradient membrane + cyclic reaction design solves the problems of low deacidification accuracy and rapid flux decay of single membrane separation, and can achieve long-term continuous and stable operation. It generates no soap residue hazardous waste, significantly reduces wastewater discharge, and allows for the recycling of deacidifying agents, thus combining economic and environmental benefits. It possesses outstanding substantive characteristics and remarkable technological advancements.

[0055] Therefore, the present invention adopts the above-mentioned efficient separation-type oil deacidification and refining method to solve the technical problems of large oil loss, high energy consumption, large amount of waste discharge, and poor heat sensitivity adaptability in traditional deacidification processes, and realizes low-temperature, high-efficiency, green and continuous oil deacidification.

[0056] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit them. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can still be made to the technical solutions of the present invention, and these modifications or equivalent substitutions cannot cause the modified technical solutions to deviate from the spirit and scope of the technical solutions of the present invention.

Claims

1. A highly efficient separation-based deacidification and refining method for oils, comprising raw material pretreatment, deacidification reaction, separation, and post-treatment steps, characterized in that, Specifically, the steps include the following: S1. Raw material pretreatment: Filter the crude oil to be deacidified to remove mechanical impurities and preheat it to 30~55℃; S2. Microfluidic selective complexation reaction: The preheated oil and amino-modified β-cyclodextrin deacidifying agent aqueous solution are continuously fed into the microfluidic reactor at a mass ratio of 100:8~20. The complexation reaction is carried out under normal pressure and 30~55℃ conditions, with a hydraulic residence time of 5~60s, to obtain a mixture of oil phase and loaded fatty acid deacidifying agent phase. S3. Two-stage gradient ceramic membrane cross-flow separation: The mixture obtained in step S2 is fed into a two-stage gradient pore size ceramic membrane cross-flow separation system for continuous separation. The primary coarse separation uses a zirconia ceramic membrane with a pore size of 50~100nm, an operating pressure of 0.2~0.4MPa, and a cross-flow velocity of 3~5m / s. The permeated deacidifying agent-rich phase is collected, and the retained concentrated oil phase is returned to the microflow reactor for recycling. The secondary deep separation uses an alumina ceramic membrane with a pore size of 5~20nm, an operating pressure of 0.3~0.5MPa, and a cross-flow velocity of 2~4m / s to perform deep separation on the primary concentrated oil phase to remove trace amounts of deacidifying agent. The secondary permeate is incorporated into the primary deacidifying agent-rich phase, and the secondary concentrate is the deacidified crude oil product. S4. Refining and post-processing: After precision filtration, the deacidified crude oil is vacuum dried to remove trace amounts of moisture, resulting in refined deacidified oil. S5. Degreasing agent regeneration and by-product recovery: The deacidifying agent rich phase obtained in step S3 is sent to a vacuum desorption tank and stripped under vacuum at 65~80℃ and 8~15kPa absolute pressure. Free fatty acids escape with water vapor and are condensed to obtain crude fatty acid by-products. The desorbed deacidifying agent solution is decolorized by adsorption of granular activated carbon and then returned to the deacidifying agent storage tank of step S2 for recycling.

2. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The aqueous solution of the amino-modified β-cyclodextrin deacidifying agent mentioned in step S2 consists of the following components by mass fraction: 15%~25% mono-6-amino-β-cyclodextrin, 5%~10% propylene glycol, and the balance being deionized water.

3. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The reaction temperature of the microfluidic reactor in step S2 is the same as the preheating temperature in step S1, and the hydraulic residence time is 20~50s.

4. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The operating temperature of the two-stage ceramic membrane separation process in step S3 is the same as the reaction temperature in step S2.

5. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The zirconia ceramic membrane used for primary coarse separation in step S3 has a pore size of 60~80nm, an operating pressure of 0.25~0.45MPa, and a cross-flow velocity of 3.5~4.5m / s.

6. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The zirconia ceramic membrane used for secondary deep separation in step S3 has a pore size of 8~15nm, an operating pressure of 0.35~0.45MPa, and a cross-flow velocity of 2.5~3.5m / s.

7. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The filtration accuracy of the precision filter in step S4 is 1 μm; the conditions for vacuum drying are: temperature 45~60℃, absolute pressure 5~10 kPa.

8. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The crude fatty acids were purified by short-path distillation to obtain industrial-grade free fatty acids with a purity of ≥95%.

9. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: The crude oil to be deacidified in step S1 has an acid value of 5~35 mgKOH / g, including any one of rice bran oil, rapeseed oil, palm oil, flaxseed oil, fish oil or waste recycled oil.

10. The efficient separation-type deacidification and refining method for oils and fats according to claim 1, characterized in that: In step S5, the temperature for adsorption and decolorization of the granular activated carbon is 40~60℃, the amount of activated carbon added is 0.5%~2% of the mass of the deacidifying agent solution, and the adsorption time is 20~40min.

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