A method for producing needle coke in a combined process

Abstract

The application discloses a method for producing needle coke by a combined process, which comprises the following steps: (1) subjecting raw oil to a hydroprocessing device and then performing fractionation to obtain at least light fraction oil and heavy fraction oil; (2) introducing the light fraction oil and the heavy fraction oil into a coke drum for coke charging after being heated by a heating furnace, preferably simultaneously; the residence time of the light fraction oil and the heavy fraction oil in the heating furnace is 1-60 min, preferably 5-30 min, and further preferably 10-20 min; (3) introducing coking raw material (preferably coking wax oil) into the coke drum for coking after the coke charging in step (2) is completed; and (4) obtaining needle coke products by coke removal after the coking in step (3) is completed. The needle coke prepared by the method has preferably improved indexes such as thermal expansion coefficient, volatile matter, tap density and particle strength coefficient, and can be used for preparing high-quality artificial graphite negative electrode materials.

Description

TECHNICAL FIELD

[0001] The present application relates to a method for producing needle coke by a combined process, in particular to a method for producing high-quality needle coke by a combined process using petroleum or coal-based raw materials. BACKGROUND

[0002] Needle coke is an excellent carbon product, which has obvious streamline texture structure from its appearance. Due to its good electrical conductivity, orientation and thermal conductivity, it becomes the main raw material for manufacturing ultra-high power graphite electrodes for steelmaking. Using ultra-high power electrodes for steelmaking, the smelting time can be shortened by about 2 / 3, and the power consumption can be reduced by about 50%, which has very obvious economic benefits.

[0003] US5286371 also discloses a straight-run residual oil hydroprocessing process, the hydrogenation reaction temperature is 379-480℃, the reaction pressure is 6.8MPa-34.4MPa, the treated heavy residual oil is mixed with catalytic cracking clarified oil into a solvent deasphalting device, and the stream after removing asphalt is used as the raw material for needle coke.

[0004] US4178229 discloses a method for producing high-quality petroleum coke from straight-run vacuum residue, which first converts the vacuum residue into distillate oil and asphalt, and then further cracks the asphalt and hydrogen donor to produce high-quality coke raw material.

[0005] US4894144 discloses a method for simultaneously producing needle coke and high-sulfur petroleum coke, which uses a hydroprocessing process to pretreat straight-run heavy oil, and the hydrogenated residual oil is divided into two parts to produce needle coke and high-sulfur petroleum coke after coking and baking.

[0006] CN202010439340.X discloses a method for preparing needle coke for ultra-high power electrode from heavy oil, which uses volume exclusion separation method, and polystyrene as separation column filler to separate components with specific molecular volume and relative molecular mass distribution of 400-1000; through ion exchange chromatography, the acidic and basic components are removed respectively to obtain neutral raw material; the treated raw material is subjected to two-stage continuous carbonization process to prepare needle coke.

[0007] CN202011305509.9 discloses a method and process system for producing needle coke from heavy oil, which includes: a group of component cutting processes, using heavy oil as raw material to cut into light distillate oil, heavy distillate oil and tail residue; a hydrogenation process, the heavy distillate oil is subjected to hydroprocessing to obtain hydrogenated heavy distillate; a mixing process, the hydrogenated heavy distillate is mixed with the light distillate oil to obtain mixed oil; a delayed coking process, the mixed oil is subjected to delayed coking treatment to obtain needle coke.

[0008] In recent years, with the rapid development of new energy vehicles, the demand for power batteries has also increased significantly. The negative electrode material of lithium battery is divided into carbon material and non-carbon material, and the main graphite material in carbon material is mainly graphite material. The production of artificial graphite negative electrode material by needle coke has attracted widespread attention, but the performance of needle coke for producing artificial graphite negative electrode material in the prior art, such as thermal expansion coefficient, volatile matter, tap density, particle strength coefficient and other indicators, still needs to be further improved. SUMMARY

[0009] In view of the deficiencies of the prior art, a method for producing needle coke by a combined process is disclosed. The needle coke prepared by the method has an optimized thermal expansion coefficient, volatile matter, tap density, particle strength coefficient and other indicators, and can be used to prepare high-quality artificial graphite negative electrode material.

[0010] A method for producing needle coke by a combined process, the method comprising the following steps:

[0011] (1) The raw oil is treated by a hydrogenation treatment device and then fractionated to obtain at least light fraction oil and heavy fraction oil;

[0012] (2) The light fraction oil and the heavy fraction oil are heated by a heating furnace and then introduced into a coke tower for charging, preferably simultaneously, the residence time of the light fraction oil and the heavy fraction oil in the heating furnace is 1-60 min, preferably 5-30 min, and further preferably 10-20 min;

[0013] (3) After the charging in step (2) is completed, a coke drawing raw material (preferably coking wax oil) is introduced for coke drawing;

[0014] (4) After the coke drawing in step (3) is completed, needle coke products are obtained by coke removal.

[0015] In the method of the present application, the raw oil is at least one selected from coal-based raw materials and petroleum-based raw materials, preferably at least one selected from coal tar, coal tar pitch, petroleum heavy oil, ethylene tar, catalytic cracking slurry or thermal cracking residual oil, and has a solid content of 0-500 μg / g, preferably 0-200 μg / g, and more preferably 0-100 μg / g.

[0016] In the method of the present application, the raw oil can be directly fractionated or first treated by hydrogenation and then fractionated according to the specific properties of the raw oil, such as sulfur content.

[0017] In the process of the present application, the hydrogen treatment device can be any hydrogen treatment technology suitable for the present application, such as fixed-bed residual oil hydrogen treatment technology, suspended-bed residual oil hydrogen treatment technology, boiling-bed residual oil hydrogen treatment technology, moving-bed residual oil hydrogen treatment technology, etc. Taking the fixed-bed hydrogen treatment technology which is relatively mature in the industry as an example, the hydrogen treatment catalyst used refers to a single catalyst or a combined catalyst having the functions of hydrodemetallization, hydrodesulfurization, hydrodenitrogenation and hydrocracking, etc. These catalysts are generally porous refractory inorganic oxides such as alumina as the carrier, oxides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc. as the active component, and optionally adding other various additives such as P, Si, F, B, etc. elements, for example, the CEN, FZC, ZTN, ZTS series of residual oil hydrogen catalysts produced by the Catalyst Branch of China Petroleum Chemical Corporation, and the ZTN, ZTS series of catalysts produced by the First Chemical Fertilizer Factory of Qilu Petrochemical Company, which belong to this type of catalyst. At present, in the fixed-bed hydrogenation technology, multiple catalysts are often used in combination, including protective agents, hydrodemetallization catalysts, hydrodesulfurization catalysts, and hydrodenitrogenation catalysts, and the loading sequence is generally such that the raw oil is sequentially contacted with the protective agent, the hydrodemetallization catalyst, the hydrodesulfurization catalyst, and the hydrodenitrogenation catalyst. Of course, there is also a technology of mixing and loading these catalysts. Hydrogen treatment is generally provided with multiple reactors to increase the processing capacity. Generally, it is operated at an absolute pressure of 1 MPa-35 MPa, preferably 2 MPa-6 MPa, and a reaction temperature of 250℃-500℃, preferably 250℃-350℃. The liquid hourly space velocity and the hydrogen partial pressure are selected according to the characteristics of the material to be treated and the required conversion rate and refining depth, and the liquid hourly space velocity is generally in the range of 0.1h -1 -5.0h -1 , preferably 0.15 h-1 -2.0h -1 , and the total hydrogen oil volume ratio is 100-5000, preferably 300-3000.

[0018] In the process of the present application, the light distillate oil has a 5% distillation point temperature of 320℃-420℃, preferably 360℃-400℃, and a 95% distillation point temperature of 400℃-480℃, preferably 430℃-460℃.

[0019] In the process of the present application, the heavy distillate oil has a 5% distillation point temperature of 380℃-460℃, preferably 400℃-440℃, and a 95% distillation point temperature of 460℃-550℃, preferably 480℃-530℃.

[0020] In the process of the present application, the light distillate oil and the heavy distillate oil are heated by heating furnace I and heating furnace II, respectively, and then introduced into the coke tower for coking at the same time.

[0021] In the method, the residence time of the light fraction oil in heating furnace I is longer than that of the heavy fraction oil in heating furnace II, generally 5-60 minutes, preferably 20-30 minutes.

[0022] In the method, the outlet temperature of the light fraction oil in heating furnace I is higher than that of the heavy fraction oil in heating furnace II, generally 5-30℃, preferably 10-20℃.

[0023] In the method, the operation conditions of heating furnace I for the light fraction oil are as follows: the outlet temperature of the furnace is 450-550℃, preferably 470-520℃; the residence time of the light fraction oil in the furnace tube of heating furnace I is 5-60 minutes, preferably 20-30 minutes.

[0024] In the method, the operation conditions of heating furnace II for the heavy fraction oil are as follows: the outlet temperature of heating furnace II is 450-520℃, preferably 460-510℃; the residence time of the hydrogenated heavy fraction oil in the furnace tube of heating furnace II is 1-50 minutes, preferably 10-20 minutes.

[0025] In the method, the coking time of a single coke tower for the light fraction oil and the heavy fraction oil is 15-45 hours, preferably 20-30 hours; the pressure of the coke tower is 0.3-1.5 MPa, preferably 0.4-0.8 MPa.

[0026] In the method, the coking wax oil can be self-produced coking wax oil or coking wax oil introduced from other devices.

[0027] In the method, the 5% distillation point temperature of the coking wax oil is 300-430℃, preferably 350-400℃; the sulfur content is ≯1.0%, preferably ≯0.6%.

[0028] In the method, the coking process of the coking wax oil can use a separate heating furnace, which is heating furnace III, or use heating furnace I or heating furnace II, preferably use a separate heating furnace, and the specific operation conditions are as follows: the outlet temperature of the heating furnace is 450-550℃, preferably 480-530℃; the pressure of the coke tower is 0.1-1.5 MPa, preferably 0.1-0.8 MPa.

[0029] In the method, the total time of the coking of the light fraction oil and the heavy fraction oil and the coking of the coking wax oil is T, and the coking time of the coking wax oil accounts for 30%-80% of the total time, preferably 40-60%.

[0030] In the method, the light oil, the heavy oil and the coking wax oil are introduced into the single coke tower, and the mass ratio of the light oil, the heavy oil and the coking wax oil is 1:0.5-1.5:0.8-3.0, preferably 1:0.8-1.2:0.8-2.5.

[0031] In the method, the coke tower can be provided as multiple, and switching is used, for example, a three-furnace two-tower process can be provided with two heating furnaces and three coke towers.

[0032] Compared with the prior art, the method for producing needle coke by the combined process has the following beneficial effects:

[0033] (1) The delayed coking reaction is to delay the heavy oil thermal cracking-condensation reaction to be performed to the coke tower downstream of the heating furnace, so that the oil in the furnace tube generally requires a short residence time, and the residence time is usually not more than 30s. The inventor finds through in-depth research that by prolonging the residence time of the distillate oil in the furnace tube of the heating furnace, a certain degree of cracking and polymerization reaction of the distillate oil in the furnace tube of the heating furnace is achieved, the content of the ideal component of the three-ring and four-ring short side chain aromatic hydrocarbon in the raw material is increased, and the quality of the needle coke product is improved through optimization of the raw material.

[0034] (2) The reaction time and reaction temperature of the light oil, the hydrogenated heavy oil in the heating furnace tube to the ideal component of the three-ring and four-ring short side chain aromatic hydrocarbon are different, the hydrogenated light oil heating furnace and the hydrogenated heavy oil heating furnace are provided in the method, the heat treatment conditions are set according to the characteristics of the heating furnace feed, and the optimization of the needle coke raw material is further ensured, and the quality of the needle coke product is further improved. BRIEF DESCRIPTION OF DRAWINGS

[0035] Figure 1 A flow chart of the method for preparing needle coke by the combined process is shown in the figure, wherein 1 is a fresh raw material, 2 is a hydrogenation treatment device, 3 is a hydrogenation product pipeline, 4 is a hydrogenation fractionating tower, 5 is a hydrogenated light diesel oil, 6 is a hydrogenated light oil, 7 is a hydrogenated heavy oil, 8 is a heating furnace I, 9 is a heating furnace II, 10 is a coking coke tower, 11 is a coking fractionating tower, 12 is a coking gas, 13 is a coking gasoline, 14 is a coking diesel oil, 15 is a coking wax oil, and 16 is a coking wax oil heating furnace. DETAILED DESCRIPTION

[0036] The specific embodiments of the present application are described in detail below, but it should be pointed out that the protection scope of the present application is not limited by these specific embodiments, but is determined by the claims in the appendix.

[0037] All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the same meaning as is commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control. In addition, the materials, methods, and examples are illustrative only and not intended to be limiting.

[0038] When the specification states that a material, substance, composition, process, step, apparatus or component etc. is "known to those of ordinary skill in the art", it is intended that the disclosure be interpreted to cover those items which are currently known as well as those which become known in the future.

[0039] Unless otherwise indicated, all percentages, parts, ratios, etc. in the specification are based on weight, unless their use would imply a different basis.

[0040] In the context of the present specification, any two or more embodiments of the present application can be combined to form further embodiments of the present application, and the technical solutions thus formed are part of the original disclosure of the present specification and also fall within the scope of protection of the present application.

[0041] According to one embodiment of the present application, the type of the separation column is not particularly limited, and any separation device that can separate the material delivered to the separation column into multiple components according to predetermined requirements can be used, such as a rectifying column, a flash column, an evaporation column, or a fractionating column, preferably a fractionating column.

[0042] In the context of the present application, including in the examples and comparative examples, the coefficient of thermal expansion is determined according to the international standard GB / T3074.4 "Determination of coefficient of thermal expansion (CTE) of graphite electrode", the volatile matter is determined according to the petrochemical standard SH / T0313 "Test method of petroleum coke", the true density is determined according to the international standard GB / T6155 "Determination of true density of carbon materials", the resistivity is determined according to GB24525-2009 "Determination of resistivity of carbon materials", and the appearance of the needle coke is directly evaluated by the naked eye.

[0043] The present application will be further described in detail by the following examples and comparative examples, but the present application is not limited to the following examples.

[0044] As Figure 1As shown: fresh feed 1 enters the hydrotreating unit 2, the hydrogenation product enters the hydrogenation fractionating column 4 through pipeline 3, the hydrogenation light diesel below fraction, hydrogenation light fraction oil and hydrogenation heavy fraction oil are separated, the hydrogenation light diesel below fraction is discharged from the unit through pipeline 5, the hydrogenation light fraction oil enters the light heating furnace 8 through pipeline 6 and then enters the coke tower 10 through the four-way valve, the hydrogenation heavy fraction oil enters the heating furnace 9 through pipeline 7 and then enters the coke tower 10 through the four-way valve, the oil gas generated by coking is introduced into the coking fractionating column 11 from the top of the coke tower through the large oil gas pipeline, and the coking gas, coking gasoline, coking diesel and coking wax oil fraction are separated, wherein the coking gas, coking gasoline and coking diesel fraction are discharged from the unit through pipelines 12, 13 and 14 respectively, the coking wax oil enters the heating furnace 16 through pipeline 15 and then enters the coke tower 10 through the four-way valve, and the needle coke produced is discharged from the unit from the bottom of the coke tower.

[0045] Example 1

[0046] The properties of the feedstock provided by a certain refinery are shown in Table 1, the hydrotreating catalysts of the hydrotreating unit are CEN, FZC, ZTN and ZTS series residual oil hydrogenation catalysts produced by China Petroleum Chemical Co., Ltd. Catalyst Branch, which specifically include protective agents, metal removal catalysts, desulfurization catalysts, denitrification catalysts and the like, and the loading sequence is generally such that the feedstock oil is sequentially contacted with the protective agent, the hydrogenation metal removal catalyst, the hydrogenation desulfurization catalyst and the hydrogenation denitrification catalyst, and of course there is also a technology of mixing and loading these catalysts. The above-mentioned catalyst loading technology is well known to those skilled in the art. The hydrotreating process conditions are shown in Table 2.

[0047] Table 1 Properties of feedstock

[0048] Analysis item Fresh raw material Density g / cm 3 ]] 1.0254 Ash content 0.01 C% (w) 91.44 H% (w) 7.02 S% (w) 1.26 N ppm 0.28 Four component % (w) Saturates 12.36 Aromatics 82.12 Gel 5.12 Asphaltene 0.40

[0049] Table 2 Hydrotreating process conditions

[0050] Item Operating condition Raw material Fresh raw material Hydrogen partial pressure, MPa 4.5 Reaction temperature, °C 320 volume space velocity, h -1 ]] 1.2 Hydrogen / oil ratio 900

[0051] The fresh raw material is subjected to a hydrogenation device to obtain hydrogenated light fraction oil and hydrogenated heavy fraction oil. The 5% distillation point temperature of the hydrogenated light fraction oil is 350°C, and the 95% distillation temperature is 420°C. The hydrogenated fraction oil is introduced into a coke tower through heating furnace I. The outlet temperature of the heating furnace I is 490°C, and the residence time of the hydrogenated light fraction oil in the heating furnace I is 20 min. The 5% distillation point temperature of the hydrogenated heavy fraction oil is 410°C, and the 95% distillation temperature is 480°C. The hydrogenated fraction oil is introduced into the coke tower through heating furnace II. The outlet temperature of the heating furnace II is 480°C, and the residence time of the hydrogenated light fraction oil in the heating furnace II is 10 min. The hydrogenated light fraction oil and the hydrogenated heavy fraction oil are charged into the single coke tower for 20 h. The pressure of the coke tower is 0.6 MPa. After the charging process of the hydrogenated light fraction oil and the hydrogenated heavy fraction oil into the coke tower is completed, the charging of coking wax oil produced by the device into the coke tower is continued. The 5% distillation point temperature of the coking wax oil is 330°C, and the sulfur content is 0.42%. The operating conditions of the coking wax oil charging process are as follows: the outlet temperature of the heating furnace III is 520°C, the pressure of the coke tower is 0.6 MPa, and the duration of the coking wax oil charging process into the single coke tower is 25 h. The mass ratio of the hydrogenated light fraction oil, the hydrogenated heavy fraction oil, and the coking wax oil in the coking process of the single coke tower is 1:1.2:2.0. The properties of the needle coke product obtained are shown in Table 3.

[0052] Example 1-1

[0053] The same raw material as in Example 1 is used. The residence time of the hydrogenated light fraction oil in the heating furnace I and the residence time of the hydrogenated heavy fraction oil in the heating furnace II are both 30 s. The other conditions are the same as in Example 1. The properties of the needle coke product obtained are shown in Table 3.

[0054] Example 2

[0055] The same raw material and process as in Example 1 were used, the 5% distillation point temperature of the hydrogenated light fraction oil was 380°C, the 95% distillation point temperature was 450°C, the hydrogenated fraction oil was introduced into the coke tower through heating furnace I, the outlet temperature of heating furnace I was 500°C, the residence time of the hydrogenated light fraction oil in the heating furnace I was 25 min; the 5% distillation point temperature of the hydrogenated heavy fraction oil was 430°C, the 95% distillation point temperature was 500°C, the hydrogenated fraction oil was introduced into the coke tower through heating furnace II, the outlet temperature of heating furnace II was 510°C, the residence time of the hydrogenated light fraction oil in the heating furnace II was 15 min, the hydrogenated light fraction oil and the hydrogenated heavy fraction oil were charged into the single coke tower for 25 h, and the pressure of the coke tower was 0.8 MPa. After the charging process of the hydrogenated light fraction oil and the hydrogenated heavy fraction oil into the coke tower was completed, the self-produced coking wax oil of the device was switched to continue charging into the coke tower, the 5% distillation point temperature of the coking wax oil was 360°C, the sulfur content was 0.30%, and the charging process of the coking wax oil into the single coke tower was operated under the following conditions: the outlet temperature of heating furnace III was 500°C, the pressure of the coke tower was 0.7 MPa, the duration of the coking wax oil charging process into the single coke tower was 28 h, the mass ratio of the hydrogenated light fraction oil, the hydrogenated heavy fraction oil, and the coking wax oil in the charging process into the single coke tower was 1:0.8:1.8, and the properties of the needle coke product obtained were shown in Table 3.

[0056] Example 3

[0057] The same raw material and process as in Example 1 were used, the 5% distillation point temperature of the hydrogenated light fraction oil was 370°C, the 95% distillation point temperature was 450°C, the hydrogenated fraction oil was introduced into the coke tower through heating furnace I, the outlet temperature of heating furnace I was 470°C, the residence time of the hydrogenated light fraction oil in the heating furnace I was 30 min; the 5% distillation point temperature of the hydrogenated heavy fraction oil was 450°C, the 95% distillation point temperature was 495°C, the hydrogenated fraction oil was introduced into the coke tower through heating furnace II, the outlet temperature of heating furnace II was 480°C, the residence time of the hydrogenated heavy fraction oil in the heating furnace II was 19 min, the hydrogenated light fraction oil and the hydrogenated heavy fraction oil were charged into the single coke tower for 18 h, and the pressure of the coke tower was 0.6 MPa. After the charging process of the hydrogenated light fraction oil and the hydrogenated heavy fraction oil into the coke tower was completed, the self-produced coking wax oil of the device was switched to continue charging into the coke tower, the 5% distillation point temperature of the coking wax oil was 380°C, the sulfur content was 0.32%, and the charging process of the coking wax oil into the single coke tower was operated under the following conditions: the outlet temperature of heating furnace III was 515°C, the pressure of the coke tower was 0.5 MPa, the duration of the coking wax oil charging process into the single coke tower was 24 h, the mass ratio of the hydrogenated light fraction oil, the hydrogenated heavy fraction oil, and the coking wax oil in the charging process into the single coke tower was 1:0.6:1.5, and the properties of the needle coke product obtained were shown in Table 3.

[0058] Comparative Example 1

[0059] The same raw materials as in Example 1 were used, the hydroprocessing unit was not fractionated into light and heavy hydroprocessed distillate oils, the hydroprocessed mixed distillate oil was directly passed into the coke drum through the heating furnace, the temperature at the furnace outlet was 490°C, the residence time of the hydroprocessed distillate oil in the heating furnace was 25 min, and the other conditions were exactly the same as in Example 1. The properties of the needle coke product obtained are shown in Table 3.

[0060] Table 3 Properties of needle coke produced in Examples and Comparative Examples

[0061] Analysis item Example 1 Example 1-1 Example 2 Example 3 Comparative example 1 coefficient of thermal expansion, 10 -6 / °C 0.96 1.06 1.02 0.98 1.21 Sulfur content, w% 0.31 0.33 0.32 0.31 0.31 Volatile matter, w% 5.0 12.0 5.1 5.3 9.0 Ash content, w% 0.01 0.01 0.01 0.01 0.01 True density, g / cm 3 ]] 2.15 2.11 2.14 2.14 2.11 Tap density, g / cm 3 ]] 0.89 0.75 0.88 0.89 0.72 Particle strength coefficient, % 20.6 19.6 21.1 20.5 15.6

Claims

1. A method of producing needle coke in a combined process, characterized by: The method comprises the following steps: (1) The raw oil is directly subjected to fractionation treatment or is subjected to fractionation treatment after being subjected to hydrotreatment, and at least light fraction oil and heavy fraction oil are fractionated out; (2) The light fraction oil and the heavy fraction oil are heated by a heating furnace I and a heating furnace II respectively and are introduced into a coke tower to charge coke in sequence or simultaneously, and the residence time of the light fraction oil and the heavy fraction oil in the heating furnace is 1-60 min; (3) After the charging in step (2) is completed, a coking raw material is introduced to coking; (4) After the coking in step (3) is completed, needle coke products are obtained through decoking; The 5% distillation point temperature of the light fraction oil is 320-420 DEG C, and the 95% distillation point temperature is 400-480 DEG C; The 5% distillation point temperature of the heavy fraction oil is 380-460 DEG C, and the 95% distillation point temperature is 460-550 DEG C; The residence time of the light fraction oil in the heating furnace I is 5-60 min longer than that of the heavy fraction oil in the heating furnace II; The outlet temperature of the light fraction oil in the heating furnace I is 5-30 DEG C higher than that of the heavy fraction oil in the heating furnace II; The operating conditions of the light fraction oil in the heating furnace I are as follows: the outlet temperature of the furnace is 450-550 DEG C, and the residence time of the light fraction oil in the furnace tube of the heating furnace I is 5-60 min; The operating conditions of the heavy fraction oil in the heating furnace II are as follows: the outlet temperature of the heating furnace II is 450-520 DEG C, and the residence time of the heavy fraction oil in the furnace tube of the heating furnace II is 1-50 min.

2. The method of claim 1, wherein: The residence time of the light fraction oil and the heavy fraction oil in the heating furnace is 5-30 min.

3. The method of claim 1, wherein: The residence time of the light fraction oil and the heavy fraction oil in the heating furnace is 10-20 min.

4. The method of claim 1, wherein: The coking raw material is coking wax oil.

5. The method of claim 1, wherein: The raw oil is at least one selected from coal-based raw materials and petroleum-based raw materials.

6. The method of claim 5, wherein: The raw oil is at least one selected from coal tar, coal tar pitch, petroleum heavy oil, ethylene tar, catalytic cracking slurry oil or thermal cracking residual oil, and the solid content thereof is 0-500 µg / g.

7. The method of claim 6, wherein: The solid content of the raw oil is 0-200 µg / g.

8. The method of claim 6, wherein: The solid content of the raw oil is 0-100 µg / g.

9. The method of claim 1, wherein: The hydrotreatment is one of fixed bed residual oil hydrotreatment technology, suspended bed residual oil hydrotreatment technology, ebullated bed residual oil hydrotreatment technology and moving bed residual oil hydrotreatment technology.

10. The method of claim 1, wherein: The 5% distillation point temperature of the light fraction oil is 360-400 DEG C, and the 95% distillation point temperature is 430-460 DEG C.

11. The method of claim 1, wherein: The 5% distillation point temperature of the heavy fraction oil is 400-440 DEG C, and the 95% distillation point temperature is 480-530 DEG C.

12. The method of claim 1, wherein: The light fraction oil and the heavy fraction oil are heated by the heating furnace I and the heating furnace II respectively and are introduced into the coke tower to charge coke simultaneously.

13. The method of claim 1, wherein: The residence time of the light fraction oil in the heating furnace I is 20-30 min longer than that of the heavy fraction oil in the heating furnace II.

14. The method of claim 1, wherein: The outlet temperature of the light fraction oil in the heating furnace I is 10-20 DEG C higher than that of the heavy fraction oil in the heating furnace II.

15. The method of claim 1, wherein: The operating conditions of the light oil in heating furnace I are as follows: the furnace outlet temperature is 470-520 DEG C; the residence time of the light oil in the heating furnace I is 20-30 min.

16. The method of claim 1, wherein: The operating conditions of the heavy oil in heating furnace II are as follows: the heating furnace II outlet temperature is 460-510 DEG C; the residence time of the heavy oil in the heating furnace II is 10-20 min.

17. The method of claim 1, wherein: The single coke tower charging time of the light oil and the heavy oil is 15-45 h; the coke tower pressure is 0.3-1.5 MPa.

18. The method of claim 17, wherein: The single coke tower charging time of the light oil and the heavy oil is 20-30 h; the coke tower pressure is 0.4-0.8 MPa.

19. The method of claim 4, wherein: The coking gas oil is the self-produced coking gas oil of the device or the coking gas oil introduced from other devices.

20. The method of claim 19, wherein: The 5% distillation point temperature of the coking gas oil is 300-430 DEG C; the sulfur content is ≯1.0%.

21. The method of claim 20, wherein: The 5% distillation point temperature of the coking gas oil is 350-400 DEG C; the sulfur content is ≯0.6%.

22. The method of claim 19, wherein: The coking gas oil coking process uses a separate heating furnace III or the heating furnace I or the heating furnace II, and the specific operating conditions are as follows: the heating furnace outlet temperature is 450-550 DEG C; the coke tower pressure is 0.1-1.5 MPa.

23. The method of claim 22, wherein: The specific operating conditions are as follows: the heating furnace outlet temperature is 480-530 DEG C; the coke tower pressure is 0.1-0.8 MPa.

24. The method of claim 4, wherein: The total time of the light oil and the heavy oil charging and the coking gas oil coking is T, and the coking gas oil coking time accounts for 30-80% of the total time.

25. The method of claim 24, wherein: The coking gas oil coking time accounts for 40-60% of the total time.

26. The method of claim 4, wherein: The mass ratio of the light oil, the heavy oil and the coking gas oil is 1:0.5-1.5:0.8-3.

0.

27. The method of claim 26, wherein: The mass ratio of the light oil, the heavy oil and the coking gas oil is 1:0.8-1.2:0.8-2.

5.

28. The method of claim 1, wherein: The coke tower is set to be multiple and is switched.

29. The method of claim 28, wherein: The coke tower is set to two heating furnaces and three coke towers, and the two-furnace three-tower process is used.

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