A process for the processing of a high acid heavy crude oil

Abstract

The application discloses a processing method of high-acid heavy crude oil, and the method comprises the following steps: pretreating the high-acid heavy crude oil; contacting the pretreated material with alkali metal to perform reaction; and obtaining liquid phase material by removing solid from the reacted material to obtain the final product. The method can efficiently remove impurities such as petroleum acid and heavy metal in the high-acid heavy crude oil, improve the yield of the liquid phase product, thereby providing high-quality raw materials for downstream devices, and realizing efficient utilization of crude oil resources and long-period operation of subsequent processing devices.

Description

Technical Field

[0001] This invention relates to a processing method for high-acid heavy crude oil, and more specifically to a method for deacidifying and demetallizing high-acid heavy crude oil. Background Technology

[0002] With the increasing trend of crude oil resources becoming heavier and of lower quality, the production and proportion of high-acid crude oil are constantly increasing. The acidic components in crude oil mainly exist in the form of naphthenic acids, accounting for approximately 95% of the total acid content. During petroleum refining, naphthenic acids can react directly with metallic iron under certain temperature conditions, and can also damage the iron sulfide protective film on the surface of equipment, causing severe corrosion of processing units. Furthermore, high-acid crude oil is a medium-heavy crude oil, not only with a high total acid value but also with high levels of impurities such as heavy metals, sulfur, and nitrogen. Therefore, the processing of high-acid crude oil has become a pressing technical challenge for the petrochemical industry.

[0003] Currently, the main processing methods for high-acid crude oil include blending with low-acid crude oil, thermal deacidification, and hydrodeacidification. However, due to the increasing production of high-acid crude oil year by year, blending with low-acid crude oil cannot fundamentally solve the processing problem of high-acid crude oil.

[0004] Thermal deacidification utilizes the poor thermal stability of petroleum acids to decompose them into non-corrosive petroleum hydrocarbons and carbon dioxide under high-temperature conditions. Patent CN114106874A discloses a method and apparatus for thermal deacidification of high-acid crude oil or high-acid residue oil. This method includes the following steps: heating the feedstock and feeding it into a gas-liquid separator to separate water and light gas oil; the feedstock containing water and light gas oil flows out from the bottom of the gas-liquid separator and enters from the bottom to the top of a shallow thermal cracking reaction tower, where it is rapidly cooled to obtain the shallow thermal cracking product, i.e., the deacidified product. This method cannot completely avoid the corrosive temperature range of naphthenic acids and also suffers from problems such as excessive cracking of light components and low yield of liquid phase products.

[0005] Hydroacidification removes acidic components by altering the structure of petroleum acids through hydrogenation. Patent CN102443417A discloses a method for hydrotreating high-acid hydrocarbon oils. This method involves mixing high-acid crude oil with hydrogen and then feeding it into a fixed-bed reactor equipped with a heat storage medium for hydrogenation. The reaction product exits the reactor as a product with a qualified total acid number. Although hydrotreating effectively removes petroleum acids and improves oil quality, it suffers from high investment and operating costs; catalyst pores are easily clogged by metallic impurities, making long-term operation difficult; and the hydrogenation process damages the structure of naphthenic acids, making their recovery impossible.

[0006] In summary, existing technologies generally present difficulties in processing high-acid heavy crude oil, making the development of efficient processing methods for high-acid heavy crude oil of great significance. Summary of the Invention

[0007] To address the shortcomings of existing technologies, this invention provides a processing method for high-acid heavy crude oil. This method efficiently removes petroleum acids and heavy metals from high-acid heavy crude oil, increasing the yield of liquid-phase products and thus providing high-quality feedstock for downstream equipment. This enables efficient utilization of crude oil resources and long-term operation of subsequent processing units.

[0008] A method for processing high-acid heavy crude oil, the method comprising: pretreating the high-acid heavy crude oil; reacting the pretreated material with an alkali metal; and obtaining a liquid phase material as the final product after desolidification of the reacted material.

[0009] In the method of this invention, the pretreated material is controlled to have the following properties: total acid value less than 0.05 mg KOH / g, water content less than 0.08 wt.%, salt content less than 8 mg / L, metal content 50-350 μg / g, and sulfur content 0.2-5.0 wt.%; preferably, the total acid value is less than 0.02 mg KOH / g, water content less than 0.05 wt.%, salt content less than 5 mg / L, metal content 80-320 μg / g, and sulfur content 0.5-4.5 wt.%.

[0010] A specific method for processing high-acid heavy crude oil, the method comprising the following steps:

[0011] (1) Initial pretreatment of high-acid heavy crude oil;

[0012] (2) The material obtained in step (1) after initial pretreatment is subjected to deacidification treatment;

[0013] (3) The material obtained in step (2) reacts with an alkali metal;

[0014] (4) The liquid phase material obtained by solid-liquid separation of the material after reaction in step (3) is the final product.

[0015] In step (1) of the method of the present invention, the properties of the high-acid heavy crude oil are as follows: total acid value 1.0-30.0 mgKOH / g, water content 0.1-50.0 wt.%, salt content 1-500 mg / L, metal content 5-350 μg / g, sulfur content 0.1-5.0 wt.%, preferably total acid value 1.0-25.0 mgKOH / g, water content 0.1-20.0 wt.%, salt content 1-400 mg / L, metal content 50-350 μg / g, sulfur content 0.2-5.0 wt.%.

[0016] In step (1) of the method of the present invention, the initial pretreatment is one or more of deacidification treatment, desalination treatment, and dehydration treatment. The deacidification treatment, desalination treatment or dehydration treatment can all adopt existing technologies. The specific method adopted depends on the specific properties of the high acid heavy crude oil.

[0017] In step (2) of the method of the present invention, the total acid value of the material after the initial pretreatment is 1.0-5.0 mgKOH / g, preferably 1.5-3.5 mgKOH / g.

[0018] In step (2) of the method of the present invention, the material after the initial pretreatment has a water content of less than 0.08 wt.%, a salt content of less than 8 mg / L, a metal content of 50-350 μg / g, and a sulfur content of 0.2-5.0 wt.%; preferably, the water content is less than 0.05 wt.%, the salt content is less than 5 mg / L, the metal content is 80-320 μg / g, and the sulfur content is 0.5-4.5 wt.%.

[0019] In step (2) of the method of the present invention, the deacidification treatment is carried out by contacting the material after the initial pretreatment obtained in step (1) with the organic alkaline material. The organic alkaline material includes amino compounds and amine compounds, preferably amine compounds, and the amine compounds are one or more of monoethanolamine, alkoxyamine, and tertiary amine ethoxylates.

[0020] In step (2) of the method of the present invention, the mass ratio of the organic alkaline material to the material after initial pretreatment obtained in step (1) is 0.1:100-2.0:100, preferably 0.2:100-1.2:100.

[0021] In step (2) of the method of the present invention, the deacidification treatment is carried out in a reactor, which includes various types of reactors that can realize liquid phase reaction, such as batch reactor, tubular reactor, and jet reactor; the deacidification treatment reaction operation conditions are: reaction temperature 60-150℃, reaction time or residence time 5-120min; the preferred operation conditions are: reaction temperature 80-120℃, reaction time or residence time 5-60min.

[0022] In step (3) of the method of the present invention, the material obtained in step (2) has a total acid value of less than 0.05 mg KOH / g, a water content of less than 0.08 wt.%, a salt content of less than 8 mg / L, a metal content of 50-350 μg / g, and a sulfur content of 0.2-5.0 wt.%; preferably, the total acid value is less than 0.02 mg KOH / g, the water content is less than 0.05 wt.%, the salt content is less than 5 mg / L, the metal content is 80-320 μg / g, and the sulfur content is 0.5-4.5 wt.%.

[0023] In step (3) of the method of the present invention, the alkali metal includes one or more of lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs) and francium (Fr), preferably one or more of lithium (Li), sodium (Na) and potassium (K), and more preferably sodium (Na).

[0024] In step (3) of the method of the present invention, the material obtained in step (2) reacts with an alkali metal in the presence of hydrogen. The reaction involves demetallization, desulfurization, denitrification and so on.

[0025] In step (3) of the method of the present invention, the material obtained in step (2) reacts with the alkali metal in a reactor. The reactor is a stirred tank reactor with a stirring rate of 300-1600 r / min, preferably 500-1200 r / min.

[0026] In step (3) of the method of the present invention, the reaction conditions for the material obtained in step (2) to react with the alkali metal are as follows: reaction temperature 150-300℃, hydrogen partial pressure 1.0-18.0MPa, alkali metal to raw material mass ratio 0.1-5.0wt.%, hydrogen-to-oil volume ratio 100-1000Nm. 3 / m 3 The preferred operating conditions are: reaction temperature 180-280℃, hydrogen partial pressure 3.0-16.0 MPa, alkali metal to feedstock mass ratio 0.5-3.0 wt.%, and hydrogen-to-oil volume ratio 300-800 Nm³. 3 / m 3 .

[0027] In step (4) of the method of the present invention, the separation device used for solid-liquid separation includes various types of equipment that can realize solid-liquid separation, such as filter separators, horizontal screw centrifuges, disc separators, hydrocyclones, etc.

[0028] In step (4) of the method of the present invention, the total acid value of the liquid phase material is controlled to be less than 0.05 mg KOH / g, the metal content is less than 50 μg / g, the sulfur content is less than 0.6 wt.%, and the solid content is less than 300 μg / g. Preferably, the total acid value is less than 0.03 mg KOH / g, the metal content is less than 25 μg / g, the sulfur content is less than 0.4 wt.%, and the solid content is less than 150 μg / g.

[0029] In step (4) of the method of the present invention, the solid-liquid separation process is a two-stage separation. A solid-liquid material A and a liquid-liquid material A are obtained through a single solid-liquid separation. The liquid-liquid material A is divided into two streams: a first liquid-liquid material A and a second liquid-liquid material A. The first liquid-liquid material A is recycled back to the reactor to mix with the alkali metal. The second liquid-liquid material A undergoes a second solid-liquid separation to obtain solid material B and liquid material B. The mass ratio of the first liquid-liquid material A to the second liquid-liquid material A is 5:100-50:100, preferably 10:100-35:100. The total acid value of liquid phase material A is controlled to be less than 0.05 mg KOH / g, the metal content is less than 50 μg / g, the sulfur content is less than 0.6 wt.%, and the solid content is 1500-5000 μg / g, preferably less than 0.03 mg KOH / g, the metal content is less than 25 μg / g, the sulfur content is less than 0.4 wt.%, and the solid content is 1800-3000 μg / g; the total acid value of liquid phase material B obtained after secondary solid-liquid separation is controlled to be less than 0.05 mg KOH / g, the metal content is less than 50 μg / g, the sulfur content is less than 0.6 wt.%, and the solid content is less than 300 μg / g, preferably less than 0.03 mg KOH / g, the metal content is less than 25 μg / g, the sulfur content is less than 0.4 wt.%, and the solid content is less than 150 μg / g.

[0030] In step (4) of the method of the present invention, the material after the reaction in step (3) is separated into liquid and solid phases. The solid phase contains naphthenic acid derivatives, alkali metal sulfides, alkali metal nitrides, and heavy metals. The solid phase is further processed to separate the naphthenic acid derivatives and heavy metals, which are then withdrawn from the device. The alkali metal sulfides and alkali metal nitrides are then regenerated in a regeneration device to obtain alkali metals, elemental sulfur, and nitrogen. The alkali metals are returned to the reaction zone, while the elemental sulfur and nitrogen are withdrawn from the device. The regeneration device can be any type of device / process capable of regenerating alkali metals, such as the alkali metal electrolytic regeneration process technology developed by Ceramatec Inc., Salt Lake City, Utah.

[0031] After initial pretreatment, high-acid heavy crude oil is contacted with organic alkaline materials under mild conditions for a deacidification reaction. The reaction products are a mixture of liquid and solid phases, meaning that the materials contain a certain amount of suspended particulate matter. When the reaction products are mixed with alkali metals for reaction, the presence of a certain amount of suspended particulate matter can inhibit the aggregation of liquid alkali metals, improve the dispersion of alkali metals in the reaction system, and thus enhance the reaction rate and the impurity removal effect. On the other hand, the solid products in the demetallization and desulfurization reaction products adhere to the suspended particulate matter, promoting the size growth of the solid particles and facilitating solid-liquid separation of the reaction products.

[0032] Furthermore, the material obtained in step (1) and the alkali metal are mixed and fed into the reactor for reaction. The reaction effluent undergoes a solid-liquid separation to obtain solid material A and liquid material A. The liquid material A is divided into two streams: first liquid material A and second liquid material A. The first liquid material A is recycled back to the reactor to mix with the alkali metal. The first liquid material A has a certain temperature and can act as a carrier to heat the alkali metal to a molten state, promoting the dispersion of the alkali metal in a liquid form. Moreover, by utilizing the high temperature characteristics of the first liquid material A, the overall temperature of the mixture stream can be significantly increased, thereby reducing the viscosity of the mixture stream and improving the dispersion effect of the alkali metal in the oil phase. In addition, the first liquid material A still contains a certain amount of solid particles, which can inhibit the aggregation of liquid alkali metal, further improving the dispersion of the alkali metal in the reaction system, thereby increasing the reaction rate and the impurity removal effect.

[0033] This invention utilizes alkali metals to treat high-acid heavy crude oil without the need for a catalyst. Due to the high reactivity of alkali metals, the reaction is less demanding, removing metal and other impurities from high-acid heavy crude oil under mild conditions.

[0034] Compared with the prior art, the present invention provides a method for processing high-acid heavy crude oil, which has the following advantages:

[0035] (1) This invention can remove acidic substances from high-acid heavy crude oil, and utilizes the properties of alkali metals to efficiently remove metal and other impurities from high-acid heavy crude oil under mild conditions, providing high-quality raw materials for downstream equipment.

[0036] (2) After the initial pretreatment, the high acid heavy crude oil reacts with organic alkaline substances. The reaction effluent contains a certain amount of suspended particulate matter, which can inhibit the aggregation of molten alkali metals and improve the dispersion of alkali metals in the reaction system, thereby increasing the reaction rate and the impurity removal effect. On the other hand, the solid products in the demetallization and desulfurization reaction products are attached to the suspended particulate matter, which promotes the size growth of the solid particulate matter and is conducive to the solid-liquid separation of the reaction products.

[0037] (3) In this invention, the first liquid phase material A obtained by solid-liquid separation of the material obtained by alkali metal treatment is recycled back to the reactor and mixed with alkali metal. The first liquid phase material A has a certain temperature and can be used as a carrier to heat the alkali metal to a liquid state, thereby promoting the dispersion of alkali metal in liquid form. Moreover, by utilizing the high temperature characteristics of the first liquid phase material A, the overall temperature of the mixture flow can be greatly increased, thereby reducing the viscosity of the mixture flow and improving the dispersion effect of alkali metal in the oil phase. In addition, the first liquid phase material A still contains a certain amount of solid particles, which can inhibit the aggregation of liquid alkali metal, further improve the dispersion of alkali metal in the reaction system, and thus improve the reaction rate and the impurity removal effect.

[0038] (4) The method of treating high-acid heavy crude oil with alkali metals in this invention has a low reaction temperature, which can effectively avoid excessive cracking of light components and maximize the yield of liquid phase products.

[0039] (5) The method of treating high-acid heavy crude oil with alkali metals in this invention has low reaction severity, does not require catalysts, and has low pollutant emissions, which can effectively reduce equipment investment and operating costs. Attached Figure Description

[0040] The attached figure is a schematic diagram of the process flow of a high-acid heavy crude oil processing method provided by the present invention.

[0041] Wherein: 1 is the initial pretreatment process, 2 is the deacidification reactor, 3 is the alkali metal treatment reactor, 4 is the separation device, 5 is the separation device, 6 is the high-acid heavy crude oil, 7 is the material after the initial pretreatment, 8 is the organic alkaline substance, 8 is the alkali metal, 10 is hydrogen, 11 is the effluent from the deacidification reaction, 12 is the effluent from the alkali metal treatment reaction, 13 is the second liquid phase material A, 14 is the solid phase material A, 15 is the first liquid phase material A, 16 is the liquid phase material B, and 17 is the solid phase material B. Detailed Implementation

[0042] The method provided by the present invention will now be described with reference to the accompanying drawings.

[0043] High-acid heavy crude oil from pipeline 6 enters reactor 1 for initial pretreatment. The pretreated material is then mixed with organic alkaline substances from pipeline 8 via pipeline 7 and enters deacidification reactor 2 for reaction. The reaction product is mixed with alkali metal from pipeline 9, second liquid phase material A from pipeline 15, and hydrogen from pipeline 10 via pipeline 11 and enters alkali metal treatment reactor 3 for further reaction. The reaction product enters separation device 4 via pipeline 12 for primary solid-liquid separation to obtain liquid phase material A and solid phase material A. Solid phase material A is extracted via pipeline 14. Liquid phase material A is divided into two streams: first liquid phase material A and second liquid phase material A. The first liquid phase material A is recycled back to the reactor via pipeline 15 to mix with the alkali metal. The second liquid phase material A enters separation device 5 via pipeline 13 for secondary solid-liquid separation to obtain liquid phase material B and solid phase material B. Liquid phase material B and solid phase material B are extracted via pipelines 16 and 17, respectively.

[0044] The following embodiments will further illustrate the method provided by the present invention, but do not limit the present invention.

[0045] The experiments in the examples and comparative examples were conducted on a pilot-scale plant for processing high-acid, heavy crude oil, designed in-house. The separation device used was a microporous filter, the organic alkaline material used was monoethanolamine, and the alkali metal used was sodium metal.

[0046] The raw material used in the examples and comparative examples is a high-acid heavy crude oil A, the properties of which are shown in Table 1.

[0047] Example 1

[0048] (1) Pretreatment of high-acid heavy crude oil; the pretreatment methods are filtration desalting and dehydration and solvent extraction deacidification. The properties of the high-acid heavy crude oil after pretreatment are as follows: total acid value 0.006 mg KOH / g, water content 0.03 wt.%, salt content 4 mg / L, sulfur content 0.85 wt.%, metal content 111.4 μg / g;

[0049] (2) The material obtained in step (1) reacts with an alkali metal;

[0050] (3) The liquid phase material obtained by solid-liquid separation of the material after reaction in step (2) is the final product.

[0051] Example 2

[0052] (1) The high-acid heavy crude oil was subjected to primary pretreatment. The primary pretreatment method was desalting and dehydration by filtration and deacidification by solvent extraction. The properties of the high-acid heavy crude oil after primary pretreatment were as follows: total acid value 2.0 mg KOH / g, water content 0.03 wt.%, salt content 4 mg / L, sulfur content 0.85 wt.%, and metal content 111.4 μg / g.

[0053] (2) The material obtained in step (1) after initial pretreatment is subjected to deacidification treatment; the total acid value of the material after deacidification treatment is 0.019 mg KOH / g, and the other properties remain basically unchanged;

[0054] (3) The material obtained in step (2) reacts with an alkali metal;

[0055] (4) The liquid phase material obtained by solid-liquid separation of the material after reaction in step (3) is the final product.

[0056] Example 3

[0057] The process flow in this embodiment is the same as in Embodiment 2. The total acid value of the material after deacidification is 0.011 mg KOH / g, and the other properties remain basically unchanged.

[0058] Example 4

[0059] The process flow in this embodiment is the same as in Embodiment 2. The total acid value of the material after deacidification is 0.006 mg KOH / g, and the other properties remain basically unchanged.

[0060] Example 5

[0061] In this embodiment, steps (1), (2), and (3) of the process flow are the same as in Example 2. The total acid value of the material after deacidification is 0.006 mg KOH / g, and the other properties remain basically unchanged.

[0062] (4) After the reaction in step (3), the material enters the microporous filter for a first solid-liquid separation to obtain liquid material A. Liquid material A is divided into two streams: first liquid material A and second liquid material A, with a mass ratio of 15:100. The first liquid material A is recycled back to the reactor to mix with alkali metal, and the second liquid material A enters the microporous filter for a second solid-liquid separation to obtain liquid material B. Liquid material B is the final product.

[0063] Example 6

[0064] The process flow in this embodiment is the same as in Example 5. The total acid value of the material after deacidification is 0.006 mg KOH / g, and the other properties remain basically unchanged. Liquid phase material A is divided into two streams: first liquid phase material A and second liquid phase material A, with a mass ratio of 25:100.

[0065] The deacidification operation conditions are shown in Table 2, the alkali treatment operation conditions are shown in Table 3, the solid-liquid separation operation conditions are shown in Table 4, and the properties of the final product are shown in Table 5.

[0066] Table 1 Properties of Raw Materials

[0067]

[0068] Table 2 Deacidification Operating Conditions

[0069]

[0070] Table 3 Alkali Treatment Operating Conditions

[0071]

[0072] Table 4 Solid-liquid separation operating conditions

[0073]

[0074] Table 5 Properties of the Final Product

[0075]

Claims

1. A method for processing high-acid heavy crude oil, characterized in that: The method includes the following steps: (1) The high-acid heavy crude oil is subjected to initial pretreatment; the initial pretreatment includes deacidification treatment; the total acid value of the material after initial pretreatment is 1.0 mgKOH / g-5.0 mgKOH / g; (2) The material obtained in step (1) after initial pretreatment is subjected to deacidification treatment; the deacidification treatment is carried out by contacting the material obtained in step (1) after initial pretreatment with organic alkaline material. (3) The material obtained in step (2) reacts with an alkali metal; (4) The liquid phase material obtained by solid-liquid separation of the material after reaction in step (3) is the final product; In step (1), the properties of the high-acid heavy crude oil are as follows: total acid value 6.08-30.0 mg KOH / g, water content 0.1-50.0 wt.%, salt content 1-500 mg / L, metal content 5-350 μg / g, and sulfur content 0.1-5.0 wt.%. In step (2), the organic alkaline material is an amine compound, which is one or more of monoethanolamine, alkoxyamine, and tertiary amine ethoxylate; The mass ratio of the organic alkaline material to the material obtained in step (1) after initial pretreatment is 0.1:100-2.0:100; In step (3), the material obtained in step (2) and the alkali metal react in the presence of hydrogen, and the reaction involves demetallization, desulfurization and denitrification.

2. The method according to claim 1, characterized in that: In step (1), the properties of the high-acid heavy crude oil are as follows: total acid value 6.08-25.0 mgKOH / g, water content 0.1-20.0 wt.%, salt content 1-400 mg / L, metal content 50-350 μg / g, and sulfur content 0.2-5.0 wt.%.

3. The method according to claim 1, characterized in that: In step (1), the initial pretreatment also includes one or more of the following: desalination treatment and dehydration treatment.

4. The method according to claim 1, characterized in that: In step (2), the total acid value of the material after the initial pretreatment is 1.5-3.5 mg KOH / g.

5. The method according to claim 1, characterized in that: The mass ratio of the organic alkaline material to the material obtained in step (1) after initial pretreatment is 0.2:100-1.2:

100.

6. The method according to claim 1, characterized in that: In step (2), the deacidification reaction conditions are: reaction temperature 60-150℃, reaction time or residence time 5-120min.

7. The method according to claim 1, characterized in that: In step (2), the deacidification reaction conditions are: reaction temperature 80-120℃, reaction time or residence time 5-60min.

8. The method according to claim 1, characterized in that: In step (3), the alkali metal includes one or more of lithium (Li), sodium (Na), potassium (K), rubidium (Rb) and cesium (Cs).

9. The method according to claim 8, characterized in that: In step (3), the alkali metal includes one or more of lithium (Li), sodium (Na) and potassium (K).

10. The method according to claim 8, characterized in that: In step (3), the alkali metal includes sodium (Na).

11. The method according to claim 1, characterized in that: In step (3), the material obtained in step (2) reacts with the alkali metal in a reactor. The reactor is a stirred tank reactor with a stirring rate of 300-1600 r / min.

12. The method according to claim 11, characterized in that: In step (3), the stirring rate is 500-1200 r / min.

13. The method according to claim 1, characterized in that: In step (3), the material obtained in step (2) is contacted with alkali metal under the following reaction conditions: reaction temperature 150-300°C, hydrogen partial pressure 1.0-18.0 MPa, mass ratio of alkali metal to raw material 0.1-5.0 wt.%, hydrogen / oil volume ratio 100-1000 Nm 3 / m 3 .

14. The method according to claim 13, characterized in that: In step (3), the reaction conditions for the material obtained in step (2) to react with the alkali metal are as follows: reaction temperature 180-280℃, hydrogen partial pressure 3.0-16.0MPa, alkali metal to raw material mass ratio 0.5-3.0wt.%, hydrogen-to-oil volume ratio 300-800Nm. 3 / m 3 .

15. The method according to claim 1, characterized in that: In step (4), the separation device used for solid-liquid separation is one of the following: filter separator, horizontal screw centrifuge, disc separator, and hydrocyclone.

16. The method according to claim 1, characterized in that: In step (4), the solid-liquid separation process is a two-stage separation. After a first solid-liquid separation, solid material A and liquid material A are obtained; after a second solid-liquid separation, liquid material A is obtained solid material B and liquid material B.

17. The method according to claim 16, characterized in that: In step (4), the liquid material A is divided into two streams: a first liquid material A and a second liquid material A. The first liquid material A is recycled back to the reactor and mixed with the alkali metal. The mass ratio of the first liquid material A to the second liquid material A is 5:100-50:

100.

18. The method according to claim 17, characterized in that: In step (4), the mass ratio of the first liquid phase material A and the second liquid phase material A is 10:100-35:

100.

19. The method according to claim 1, characterized in that: In step (4), the material after the reaction in step (3) is separated into liquid and solid phases. The solid phase is further processed to separate the naphthenic acid derivatives and heavy metals and extract them from the device. The alkali metal sulfides and alkali metal nitrides are regenerated in the regeneration device to obtain alkali metals, elemental sulfur and nitrogen. The alkali metals are returned to the reaction zone and the elemental sulfur and nitrogen are extracted from the device.

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