Production method of high-particle-strength needle coke

Abstract

The invention discloses a high particle strength needle coke production method, which comprises: heating raw material oil, introducing the heated raw material oil into a coke tower, carrying out coke charging, switching coke drawing raw materials after the coke charging is completed, and carrying out coke drawing treatment, wherein the coke drawing raw materials comprise at least two types, and the two types are respectively recorded as a raw material A and a raw material B, the 5% distillation point temperature of the raw material A is 300-380 DEG C, and the distillation point temperature of the raw material B is 300-380 DEG C; the temperature of the 95% point distillation point is 400-520 DEG C, preferably 410-460 DEG C, and the temperature of the 95% point distillation point is 400-520 DEG C; the 5% distillation point temperature of the raw material B is 250-350 DEG C, preferably 250-300 DEG C, the 95% distillation point temperature of the raw material B is 350-450 DEG C, preferably 350-400 DEG C, and the raw material A and the raw material B are subjected to coke drawing in sequence. The method can be used for preparing the high-particle-strength needle coke.

Description

Technical Field

[0001] The invention relates to a method for producing high-particle strength needle coke, in particular to a method for producing high-particle strength needle coke by using petroleum-based or coal-based raw materials. Background Art

[0002] Needle coke is an excellent carbon product with a streamlined texture. Due to its good electrical conductivity, orientation and thermal conductivity, it has become the main raw material for manufacturing ultra-high power graphite electrodes for steelmaking. The use of ultra-high power electrodes in steelmaking can shorten the smelting time by about 2 / 3 and reduce power consumption by about 50%, with obvious economic benefits.

[0003] CN202011305509.9 discloses a method and process system for producing needle coke from heavy oil, comprising: a component cutting process, taking heavy oil as raw material, cutting it into light fraction oil, heavy fraction oil and tailings; a hydrogenation process, hydrogenating the heavy fraction oil to obtain a hydrogenated heavy fraction; a mixing process, mixing the hydrogenated heavy fraction with the light fraction oil to obtain a mixed oil; and a delayed coking process, subjecting the mixed oil to delayed coking to obtain needle coke.

[0004] US4894144 discloses a method for simultaneously preparing needle coke and high-sulfur petroleum coke, which uses a hydrogenation process to pretreat straight-run heavy oil, and the hydrogenated residual oil is divided into two parts, which are coked and then calcined to obtain needle coke and high-sulfur petroleum coke.

[0005] US5286371 also discloses a straight-run residue oil hydrotreating process, with a hydrogenation reaction temperature of 379-480°C and a reaction pressure of 6.8MPa-34.4MPa. The treated heavy residue oil is mixed with catalytic cracking clarified oil and enters a solvent deasphalting device, and the logistics after deasphalting is used as a raw material for needle coke.

[0006] US4178229 discloses a method for producing high-quality petroleum coke from straight-run vacuum residue oil, wherein the vacuum residue oil is first converted into distillate oil and asphalt, and then the asphalt and hydrogen donor are further cracked to produce raw materials for high-quality coke.

[0007] CN202010439340.X discloses a method for preparing needle coke for ultra-high power electrodes from heavy oil. The method comprises taking heavy oil as raw material, adopting a size exclusion separation method, and using polystyrene as a separation column filler to separate components with a specific molecular volume of a relative molecular mass distribution of 400-1000; removing the acidic and alkaline components therein through ion exchange chromatography to obtain a neutral raw material; and preparing needle coke from the treated raw material through two continuous carbonization processes.

[0008] Needle coke is used as graphite electrode aggregate to produce HP and UHP graphite electrodes. The main goal is to have a lower coefficient of thermal expansion (CTE). In order to obtain needle coke products with a lower CTE value, the coking process must follow the liquid phase carbonization theory, that is, the raw material coking process must be slow from low temperature to high temperature, forming a sufficient wide-area intermediate phase structure before solidifying into coke. However, in actual production, although a low coefficient of thermal expansion is obtained, the particle strength is generally low. Summary of the invention

[0009] The inventors have found through in-depth research that the thermal reaction time and thermal reaction temperature of the raw materials entering the coke tower at different stages of the coking process are different, causing some raw materials to be coked at high temperature without following the liquid phase carbonization, resulting in low needle coke particle strength, affecting the application performance of needle coke. In view of the shortcomings of the prior art, the present invention provides a production method of high particle strength needle coke

[0010] A method for producing high-particle strength needle coke comprises the following contents: raw material oil is heated and then introduced into a coke drum for coking; after coking, the coke-drawing raw material is switched for coke-drawing treatment; the coke-drawing raw materials are at least two kinds, which are respectively recorded as raw material A and raw material B; the 5% distillation point temperature of raw material A is 300-380°C, preferably 340-360°C, and the 95% distillation point temperature is 400-520°C, preferably 410-460°C; the 5% distillation point temperature of raw material B is 250-350°C, preferably 250-300°C, and the 95% distillation point temperature is 350-450°C, preferably 350-400°C; raw material A and raw material B are coked in order.

[0011] In the method of the present invention, the conditions for coking raw material A are as follows: the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the coking time is 10-24h, preferably 12-18h; the coke tower pressure is 0.1-1.0MPa, preferably 0.2-0.8MPa, and more preferably 0.3-0.6MPa.

[0012] In the method of the present invention, the conditions for coking raw material B are as follows: the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 1-15h, preferably 2-10h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.1-0.3MPa.

[0013] In the method of the present invention, the solid content of the raw oil is 0-500 μg / g, preferably 0-200 μg / g, and more preferably 0-100 μg / g; the 5% distillation point temperature is 350°C-450°C, preferably 370°C-410°C, and the 95% distillation temperature is 450°C-550°C, preferably 480°C-500°C; the sulfur content is 0-1.0%, preferably 0-0.5%, and more preferably 0-0.4%.

[0014] In the method of the present invention, the conditions for coking the crude oil are as follows: the outlet temperature of the heating furnace is 400°C-580°C, preferably 450°C-550°C, and more preferably 480°C-520°C; the charging time is 4-30h, preferably 15-25h; and the coke tower pressure is 0.1-1.5MPa, preferably 0.3-1.0MPa, and more preferably 0.4-0.8MPa.

[0015] In the method of the present invention, the mass ratio of the raw material oil, the coke-pulling raw material A and the coke-pulling raw material B to the single coke tower charge is 1:0.2-2.0:0.1-2.0.

[0016] A method for producing high particle strength needle coke, specifically comprising the following contents:

[0017] (6) The fresh raw material passes through the hydrotreating unit and enters the hydrodistillation tower to separate at least the hydrotreated distillate oil;

[0018] (7) The hydrogenated distillate oil is heated in a heating furnace and then fed into a coke drum for charging. The oil and gas generated by the reaction are discharged from the top of the coke drum and fed into a coking fractionation tower to separate at least a coking heavy wax oil fraction and a coking light wax oil fraction;

[0019] (8) The hydrogenated distillate oil in step (2) is switched to the coking heavy distillate oil in step (2) to continue charging the coke drum;

[0020] (9) the coking heavy wax oil fraction in step (3) is switched to the coking light wax oil fraction in step (2) to continue charging the coke drum;

[0021] (10) After the coking of the coke drum with the coking light wax oil in step (4) is completed, the coke drum is subjected to small blowing, large blowing, decoking and other operations, and the needle coke product is discharged from the bottom of the drum;

[0022] In the above method, the fresh raw material in step (1) 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 residue;

[0023] In the above method, the solid content of the fresh raw material in step (1) is 0-500 μg / g, preferably 0-200 μg / g, more preferably 0-100 μg / g;

[0024] In the above method, the hydrotreating device in step (1) can be any hydrotreating technology applicable to the present invention, such as fixed bed residue hydrotreating technology, suspended bed residue hydrotreating technology, fluidized bed residue hydrotreating technology, mobile bed residue hydrotreating technology, etc. Taking the current more mature fixed bed hydrotreating technology in industry as an example, the hydrotreating catalyst used refers to a single catalyst or a combination catalyst having functions such as hydrodemetallization, hydrodesulfurization, hydrodenitrogenation and hydrocracking. These catalysts are generally based on porous refractory inorganic oxides such as alumina as carriers, oxides of VIB group and / or VIII group metals such as W, Mo, Co, Ni, etc. as active components, and selectively add various other additives such as P, Si, F, B and other elements of the catalyst, such as CEN, FZC, ZTN, ZTS series residue hydrotreating catalysts produced by the Catalyst Branch of Sinopec, and ZTN and ZTS series catalysts produced by the First Fertilizer Plant of Qilu Petrochemical Company belong to this type of catalyst. At present, in fixed bed hydrogenation technology, multiple catalysts are often used in combination, including protective agents, hydrodemetallization catalysts, hydrodesulfurization catalysts, and hydrodenitrogenation catalysts. The loading order is generally to make the feed oil contact with the protective agent, hydrodemetallization, hydrodesulfurization, and hydrodenitrogenation catalysts in turn. Of course, there is also a technology for mixing these catalysts. Hydroprocessing generally sets up multiple reactors to increase the processing volume. It is usually operated at an absolute pressure of 1MPa-35MPa, preferably 2MPa-6MPa, and a reaction temperature of 250℃-500℃, preferably 250℃-350℃. The liquid hourly volume space velocity and hydrogen partial pressure are selected according to the characteristics of the material to be treated and the required conversion rate and refining depth. The liquid hourly volume space velocity is generally 0.1h -1 -5.0h -1 , preferably 0.15h -1 -2.0h -1 In the range of, the total hydrogen to oil volume ratio is 100-5000, preferably 300-3000.

[0025] In the above method, the 5% distillation point temperature of the hydrogenated distillate oil in step (1) is 350°C-450°C, preferably 370°C-410°C, and the 95% distillation temperature is 450°C-550°C, preferably 480°C-500°C.

[0026] In the above method, the sulfur content of the hydrogenated distillate oil in step (1) is 0-1.0%, preferably 0-0.5%, and more preferably 0-0.4%.

[0027] In the above method, the hydrogenated distillate oil in step (2) passes through a heating furnace, and the furnace outlet temperature is 400°C-580°C, preferably 450°C-550°C, and more preferably 480°C-520°C.

[0028] In the above method, the charging time of the hydrogenated distillate oil to the coke drum in step (2) is 4-30 hours, preferably 15-25 hours, and the pressure of the coke drum is 0.1-1.5 MPa, preferably 0.3-1.0 MPa, and more preferably 0.4-0.8 MPa;

[0029] In the above method, the 5% distillation point temperature of the coking heavy wax oil fraction in step (3) is 300°C-380°C, preferably 340°C-360°C, and the 95% distillation point temperature is 400°C-520°C, preferably 410°C-460°C.

[0030] In the above method, in the charging process of the coking heavy wax oil fraction in step (3), the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 10-24h, preferably 12-18h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.2-0.8MPa, and more preferably 0.3-0.6MPa.

[0031] In the above method, the 5% distillation point temperature of the coker light wax oil fraction in step (4) is 250°C-350°C, preferably 250°C-300°C, and the 95% distillation point temperature is 350°C-450°C, preferably 350°C-400°C.

[0032] In the above method, in the charging process of the coking light wax oil fraction in step (4), the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 1-15h, preferably 2-10h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.1-0.3MPa.

[0033] In the above method, the mass ratio of the hydrogenated distillate oil, the coking heavy wax oil fraction, and the coking light wax oil to the single coke tower charge is 1:0.2-2.0:0.1-2.0.

[0034] The inventors have found through experiments that the strength of needle coke is closely related to the medium and operating conditions of the coke drawing process, especially in the later stage of coke drawing, when the main product of needle coke has been solidified and formed, and the coke drawing medium continues to react into coke, and the strength of the formed petroleum coke is very low. The present invention adopts coking light wax oil and heavy wax oil to respectively carry out the coke drawing process of needle coke. The main function of coke drawing with heavy wax oil is to raise the temperature of the system and solidify it, while the main function of coke drawing with light wax oil is to further provide heat to the solidified needle coke product to enhance the product strength, while greatly reducing the low-strength needle coke produced by the coke drawing medium. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] Figure 1The present invention is a flow chart of a method for preparing needle coke by a combined process, wherein 1 is a fresh raw material, 2 is a hydrotreating device, 3 is a hydrogenation product pipeline, 4 is a fractionation tower, 5 is a hydrogenation gas product pipeline, 6 is a pipeline for fractions below light diesel oil, 7 is hydrogenation distillate oil, 8 is a coking heating furnace, 9 is a coke tower, 10 is a coking product pipeline, 11 is a coking fractionation tower, 12 is coking gas, 13 is coking gasoline, 14 is coking diesel, 15 is a coking heavy wax oil fraction, and 16 is a coking light wax oil fraction. DETAILED DESCRIPTION

[0036] The specific embodiments of the present invention are described in detail below, but it should be pointed out that the protection scope of the present invention 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 incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings conventionally understood by those skilled in the art. In the event of a conflict, the definitions in this specification shall prevail.

[0038] When this specification uses the prefix "well-known to those skilled in the art", "prior art" or similar terms to introduce materials, substances, methods, steps, devices or components, etc., the objects introduced by the prefix cover those commonly used in the art when this application is filed, but also include those that are not commonly used at present but will become recognized in the art as being suitable for similar purposes.

[0039] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight, unless the weight basis does not conform to the common understanding of those skilled in the art.

[0040] In the context of this specification, any two or more embodiments of the present invention may be arbitrarily combined, and the technical solutions thus formed belong to part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0041] According to one embodiment of the present invention, there is no particular limitation on the type of the separation tower, and any separation device that can separate the material transported to the separation tower into multiple components according to predetermined requirements can be used, such as a distillation tower, a flash tower, an evaporation tower or a fractionation tower, etc., preferably a fractionation tower.

[0042] In the context of the present invention, including in the embodiments and comparative examples, the coefficient of thermal expansion is determined in accordance with the international standard GB / T3074.4 "Determination method for coefficient of thermal expansion (CTE) of graphite electrode", the particle strength coefficient is determined in accordance with T / ZGTS002-2019, the volatile matter is determined in accordance with the petrochemical standard SH / T0313 "Petroleum coke inspection method", the true density is determined in accordance with the international standard GB / T32158, and the sulfur content is determined in accordance with GB / T24256.

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

[0044] like Figure 1 As shown: fresh feedstock 1 passes through hydrogenation device 2, and the hydrogenation product enters hydrogenation fractionation tower 4 through pipeline 3 to separate gas, fractions below light diesel oil and hydrogenated distillate oil. Gas and fractions below light diesel oil are discharged from the device through pipelines 5 and 6 respectively. Hydrogenated distillate oil passes through heating furnace 8 from pipeline 7 and enters coke 9 through a four-way valve. The oil and gas generated by coking enters coking fractionation tower 11 from the top of the coke tower through pipeline 10 to separate coking gas 12, coking gasoline 13, coking diesel 14, coking heavy wax oil fraction 15 and coking light wax oil fraction 16. Among them, the coking heavy wax oil fraction 15 and the coking light wax oil fraction 16 enter the coke tower through the heating furnace 8 in sequence to charge coke and flush materials, and the produced needle coke product is discharged from the bottom of the coke tower.

[0045] Example 1

[0046] The analysis of the raw material properties provided by a refinery is shown in Table 1. The catalyst of the hydroprocessing unit adopts CEN, FZC, ZTN, and ZTS series residual oil hydrogenation catalysts produced by the Catalyst Branch of Sinopec, which specifically include protective agents, demetallization catalysts, desulfurization catalysts, denitrogenation catalysts, etc. The loading order is generally to make the raw oil contact with protective agents, hydrodemetallization, hydrodesulfurization, and hydrodenitrogenation catalysts in turn. Of course, there is also a technology for mixing and loading these catalysts. The above catalyst loading technology is a technical content well known to those skilled in the art. The hydroprocessing process conditions are shown in Table 2.

[0047] Fresh raw materials are passed through a hydrogenation unit to obtain hydrogenated distillate oil, the properties of which are as follows: 5% distillation point temperature is 380°C, 95% distillation temperature is 500°C, sulfur content is 0.32%, and the charging process conditions of the hydrogenated distillate oil to the coke tower are as follows: the outlet temperature of the heating furnace is 480°C, the charging time is 15h, and the coke tower pressure is 0.7MPa; the 5% distillation point temperature of the coking heavy wax oil fraction is preferably 355°C, and the 95% distillation point temperature is preferably The temperature of the coking heavy wax oil fraction is 455℃, and the charging process conditions of the coking heavy wax oil fraction to the coking tower are as follows: the outlet temperature of the heating furnace is 495℃, the charging time is 12h, and the coking tower pressure is 0.6MPa; the 5% distillation point temperature of the coking light wax oil fraction is 295℃, the 95% distillation point temperature is 385℃, and the charging process conditions of the coking light wax oil fraction to the coking tower are as follows: the outlet temperature of the heating furnace is 480℃, the charging time is 4h, and the coking tower pressure is 0.2MPa. The mass ratio of hydrogenated distillate oil, coking heavy wax oil fraction, and coking light wax oil to a single coking tower charge is 1:1:0.5, and the properties of the needle coke product obtained are shown in Table 3.

[0048] Comparative Example 1

[0049] The coking process of coking light wax oil to charge the coke drum was cancelled, and the coking light wax oil in Example 1 was completed by replacing the coking light wax oil with coking heavy wax oil. The other conditions were exactly the same as those in Example 1. The properties of the needle coke product obtained are shown in Table 3.

[0050] Comparative Example 2

[0051] The coking process of coking heavy wax oil to charge the coke drum was cancelled, and the coking heavy wax oil in Example 1 was completed by replacing the coking heavy wax oil with coking light wax oil. The other conditions were exactly the same as those in Example 1. The properties of the needle coke product obtained are shown in Table 3.

[0052] Table 1 Raw material properties

[0053] Analyze Project Fresh ingredients <![CDATA[Density g / cm 3 > 1.0325 Ash % 0.01 C%(w) 90.05 H%(w) 7.86 S%(w) 1.98 N%(w) 0.11 Four components % (w) Saturated 18.62 Aroma 76.80 Gel 4.26 Asphaltene 0.32

[0054] Table 2 Hydrotreating process conditions

[0055] project Operating conditions raw material Fresh ingredients Hydrogen partial pressure, MPa 5.0 Reaction temperature, °C 310 <![CDATA[Space velocity, h -1 > 1.0 Hydrogen to Oil Ratio 800

[0056] Table 3 Properties of needle coke produced in Examples and Comparative Examples

[0057]

[0058]

[0059] Example 2

[0060] The analysis of the raw material properties provided by a refinery is shown in Table 4. The catalyst of the hydroprocessing unit adopts CEN, FZC, ZTN, and ZTS series residual oil hydrogenation catalysts produced by the Catalyst Branch of Sinopec, which specifically include protective agents, demetallization catalysts, desulfurization catalysts, denitrogenation catalysts, etc. The loading order is generally to make the raw oil contact with protective agents, hydrodemetallization, hydrodesulfurization, and hydrodenitrogenation catalysts in turn. Of course, there is also a technology for mixing and loading these catalysts. The above catalyst loading technology is a technical content well known to those skilled in the art. The hydroprocessing process conditions are shown in Table 5.

[0061] Fresh raw materials are passed through a hydrogenation unit to obtain hydrogenated distillate oil, the properties of which are as follows: 5% distillation point temperature is 410°C, 95% distillation temperature is 490°C, and sulfur content is 0.26%; the conditions for charging the coke tower with hydrogenated distillate oil are as follows: the outlet temperature of the heating furnace is 495°C, the charging time is 24h, and the coke tower pressure is 0.5MPa; the 5% distillation point temperature of the coking heavy wax oil fraction is 345°C, the 95% distillation point temperature is 415°C,

[0062] The charging process conditions of coking heavy wax oil fraction to coke tower are as follows: the outlet temperature of heating furnace is 510℃, the charging time is 15h, and the pressure of coke tower is 0.5MPa; the 5% distillation point temperature of coking light wax oil fraction is 260℃, and the 95% distillation point temperature is 385℃. The charging process conditions of coking light wax oil fraction to coke tower are as follows: the outlet temperature of heating furnace is 500℃, the charging time is 8h, and the pressure of coke tower is 0.3MPa. The mass ratio of hydrogenated distillate oil, coking heavy wax oil fraction, and coking light wax oil to single coke tower charging is 1:0.8:0.6, and the properties of the obtained needle coke product are shown in Table 6.

[0063] Table 4 Raw material properties

[0064]

[0065]

[0066] Table 5 Hydrotreating process conditions

[0067] project Operating conditions raw material Fresh ingredients Hydrogen partial pressure, MPa 4.0 Reaction temperature, °C 300 <![CDATA[Space velocity, h -1 > 1.2 Hydrogen to Oil Ratio 1000

[0068] Example 3

[0069] The fresh raw material is passed through the hydrogenation unit to obtain hydrogenated distillate oil. The properties of the hydrogenated distillate oil are as follows: the 5% distillation point temperature is 375℃, the 95% distillation temperature is 495℃, and the sulfur content is 0.30%; the charging process conditions of the hydrogenated distillate oil to the coke tower are as follows: the outlet temperature of the heating furnace is 485℃, the charging time is 20h, and the coke tower pressure is 0.7MPa; the 5% distillation point temperature of the coking heavy wax oil fraction is 350℃, the 95% distillation point temperature is 4 30℃, the coking heavy wax oil fraction charging process conditions for the coking tower are as follows: the outlet temperature of the heating furnace is 495℃, the charging time is 14h, and the coking tower pressure is 0.7MPa; the 5% distillation point temperature of the coking light wax oil fraction is 260℃, and the 95% distillation point temperature is 360℃, and the coking light wax oil fraction charging process conditions for the coking tower are as follows: the outlet temperature of the heating furnace is 530℃, the charging time is 4h, and the coking tower pressure is 0.2MPa. The mass ratio of hydrogenated distillate oil, coking heavy wax oil fraction, and coking light wax oil to a single coking tower charge is 1:0.9:0.4, and the properties of the obtained needle coke product are shown in Table 6.

[0070] Table 6 Properties of needle coke in Example

[0071] project Example 2 Example 3 <![CDATA[Coefficient of thermal expansion, 10 -6 / °C]]> 0.97 0.98 Volatile matter, w% 5.36 5.64 Ash content, w% 0.02 0.01 Moisture, w% 0.54 0.59 Sulfur content, w% 0.32 0.33 <![CDATA[True density, g / cm 3 > 1.45 1.42 Particle strength coefficient, % 23.58 23.66

Claims

1. A method for producing high particle strength needle coke, characterized in that: The method comprises the following contents: after heating, the crude oil is introduced into a coke drum for coking; after the coking is completed, the coke-drawing raw material is switched for coke-drawing treatment; the coke-drawing raw materials are at least two kinds, which are respectively recorded as raw material A and raw material B; the 5% distillation point temperature of raw material A is 300°C-380°C, preferably 340°C-360°C, and the 95% distillation point temperature is 400°C-520°C, preferably 410°C-460°C; the 5% distillation point temperature of raw material B is 250°C-350°C, preferably 250°C-300°C, and the 95% distillation point temperature is 350°C-450°C, preferably 350°C-400°C; raw materials A and raw material B are coked in order.

2. The method according to claim 1, characterized in that: The conditions for coking raw material A are as follows: the outlet temperature of the heating furnace is 450-550°C, preferably 480-530°C; the coking time is 10-24h, preferably 12-18h; the coke tower pressure is 0.1-1.0MPa, preferably 0.2-0.8MPa, more preferably 0.3-0.6MPa.

3. The method according to claim 1, characterized in that: The conditions for coking raw material B are as follows: the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 1-15h, preferably 2-10h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.1-0.3MPa.

4. The method according to claim 1, characterized in that: The solid content of the raw oil is 0-500 μg / g, preferably 0-200 μg / g, and more preferably 0-100 μg / g; the 5% distillation point temperature is 350°C-450°C, preferably 370°C-410°C, and the 95% distillation temperature is 450°C-550°C, preferably 480°C-500°C; the sulfur content is 0-1.0%, preferably 0-0.5%, and more preferably 0-0.4%.

5. The method according to claim 1, characterized in that: The conditions for coking the crude oil are as follows: the outlet temperature of the heating furnace is 400°C-580°C, preferably 450°C-550°C, more preferably 480°C-520°C; the charging time is 4-30h, preferably 15-25h; the coke tower pressure is 0.1-1.5MPa, preferably 0.3-1.0MPa, more preferably 0.4-0.8MPa.

6. The method according to claim 1, characterized in that: The mass ratio of the raw material oil, coke-pulling raw material A and coke-pulling raw material B to the single coke tower charge is 1:0.2-2.0:0.1-2.

0.

7. The method according to claim 1, characterized in that: The specific production method of high particle strength needle coke includes the following contents: (1) The fresh raw material passes through the hydrotreating unit and enters the hydrodistillation tower to separate at least the hydrotreated distillate oil; (2) The hydrogenated distillate oil is heated in a heating furnace and then fed into a coke drum for charging. The oil and gas generated by the reaction are discharged from the top of the coke drum and fed into a coking fractionation tower to separate at least a coking heavy wax oil fraction and a coking light wax oil fraction; (3) the hydrogenated distillate oil in step (2) is switched to the coking heavy distillate oil in step (2) to continue charging the coke drum; (4) the coking heavy wax oil fraction in step (3) is switched to the coking light wax oil fraction in step (2) to continue charging the coke drum; (5) After the coking of the coke drum with the coking light wax oil in step (4) is completed, the coke drum is subjected to small blowing, large blowing, decoking and other operations, and the needle coke product is discharged from the bottom of the drum.

8. The method according to claim 7, characterized in that: The fresh raw material described in step (1) 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.

9. The method according to claim 7, characterized in that: The solid content of the fresh raw material in step (1) is 0-500 μg / g, preferably 0-200 μg / g, and more preferably 0-100 μg / g.

10. The method according to claim 7, characterized in that: The hydroprocessing device in step (1) is one of the following: fixed bed residue oil hydroprocessing technology, suspended bed residue oil hydroprocessing technology, fluidized bed residue oil hydroprocessing technology, and moving bed residue oil hydroprocessing technology.

11. The method according to claim 7, characterized in that: The 5% distillation point temperature of the hydrogenated distillate oil in step (1) is 350°C-450°C, preferably 370°C-410°C, and the 95% distillation temperature is 450°C-550°C, preferably 480°C-500°C.

12. The method according to claim 7, characterized in that: The sulfur content of the hydrogenated distillate oil in step (1) is 0-1.0%, preferably 0-0.5%, more preferably 0-0.4%.

13. The method according to claim 7, characterized in that: The hydrogenated distillate oil in step (2) passes through a heating furnace, and the furnace outlet temperature is 400°C-580°C, preferably 450°C-550°C, and more preferably 480°C-520°C.

14. The method according to claim 7, characterized in that: The charging time of the hydrogenated distillate oil to the coke tower in step (2) is 4-30 hours, preferably 15-25 hours, and the pressure of the coke tower is 0.1-1.5 MPa, preferably 0.3-1.0 MPa, and more preferably 0.4-0.8 MPa.

15. The method according to claim 7, characterized in that: The 5% distillation point temperature of the coking heavy wax oil fraction in step (3) is 300°C-380°C, preferably 340°C-360°C, and the 95% distillation point temperature is 400°C-520°C, preferably 410°C-460°C.

16. The method according to claim 7, characterized in that: In the charging process of the coking heavy wax oil fraction in step (3), the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 10-24h, preferably 12-18h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.2-0.8MPa, and more preferably 0.3-0.6MPa.

17. The method according to claim 7, characterized in that: The 5% distillation point temperature of the coker light wax oil fraction in step (4) is 250°C-350°C, preferably 250°C-300°C, and the 95% distillation point temperature is 350°C-450°C, preferably 350°C-400°C.

18. The method according to claim 7, characterized in that: In the charging process of the coking light wax oil fraction in step (4), the outlet temperature of the heating furnace is 450°C-550°C, preferably 480°C-530°C; the charging time is 1-15h, preferably 2-10h; and the coke tower pressure is 0.1-1.0MPa, preferably 0.1-0.3MPa.

19. The method according to claim 7, characterized in that: The mass ratio of the hydrogenated distillate oil, the coking heavy wax oil fraction and the coking light wax oil to the single coke tower charge is 1:0.2-2.0:0.1-2.0.

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