Method and system for preparing high-quality petroleum coke raw material from catalytic slurry oil and ethylene tar

Abstract

The invention discloses a method and system for preparing a high-quality petroleum coke raw material from catalytic slurry oil and ethylene tar, and relates to the field of petrochemical engineering. The method comprises the following steps: mixing catalytic slurry oil and ethylene tar to obtain raw oil, conveying the raw oil into a riser reactor for hydrogen transfer reaction, and separating a mixed material obtained by the hydrogen transfer reaction; conveying the separated hydrogen transfer catalyst to a catalyst regenerator, and returning the high-temperature hydrogen transfer catalyst regenerated by the catalyst regenerator to the riser reactor; the separated oil gas is fractionated by a fractionating tower to obtain a wax oil fraction capable of producing the high-quality petroleum coke, the pretreatment on the catalytic slurry oil is reduced in the process of preparing the high-quality petroleum coke raw material, and the comprehensive utilization efficiency of the ethylene tar and the catalytic slurry oil is improved.

Description

Technical Field

[0001] The present invention relates to the field of petrochemical industry, and specifically to a method and system for preparing high-quality petroleum coke raw materials from catalytic slurry and ethylene tar. Background Art

[0002] High-quality petroleum coke generally refers to petroleum coke with a coke content of more than 95%, an ash content of less than 0.5%, and a volatile content of less than 0.5%. As a scarce product, in the future, it is an inevitable trend for its price to be at a high level. In China, the amount of low-sulfur slurry resources for producing high-quality petroleum coke raw materials is small, and the proportion of catalytic slurry with a sulfur content within 0.5 is less than 10%. With the accumulation of time, the reserve of light crude oil resources in China will continue to decrease. Coupled with the continuous expansion of the national new energy market, the market demand for high-quality petroleum coke will gradually increase, which will bring huge economic benefits to enterprises producing high-quality petroleum coke.

[0003] Ethylene tar is a product of high-temperature condensation during the steam cracking of ethylene cracking raw materials, and it is also a by-product of ethylene cracking units, with a yield accounting for about 10%-20% (mass fraction) of ethylene production. The main component of ethylene tar is aromatic compounds, rich in polycyclic aromatic hydrocarbons (C8-C15) with more than two rings, the aromatic mass fraction exceeds 80%, and it contains a small amount of heterocyclic compounds such as sulfur, nitrogen, and oxygen. It has the characteristics of short side chains, high carbon-hydrogen ratio, high mass fraction of gum and asphaltene, low mass fraction of ash, and low mass fraction of heavy metals, and is an excellent raw material or blending raw material for producing high-quality petroleum coke.

[0004] Using the processing method of blending ethylene tar in a delayed coking unit will bring a series of problems. The main reason is that the compatibility of ethylene tar and vacuum residue is poor, which is easy to damage the colloid system of vacuum residue and easily cause the precipitation of asphaltene. In addition, ethylene tar contains a certain amount of olefins, and olefins are prone to coke condensation in the furnace tubes of the heating furnace, resulting in a shortened operation cycle of the furnace tubes of the delayed coking heating furnace and affecting the long-term operation of the delayed coking unit.

[0005] Catalytic slurry is a by-product of a catalytic cracking unit, composed of saturated hydrocarbons, aromatic hydrocarbons, gum, and a small amount of asphaltene. Catalytic slurry is rich in 3-5 ring aromatic hydrocarbons and is an ideal raw material for preparing high-quality petroleum coke. However, due to the large amount of catalyst solid particles in catalytic slurry, and the high content of impurities such as asphaltene, sulfur, nitrogen, and metals, it is necessary to perform pretreatment on it to obtain the raw material for preparing high-quality petroleum coke.

[0006] The prior art's pretreatment of catalytic slurry oil generally refers to feeding catalytic slurry oil into a hydrogenation reactor for hydrotreating, and reacting under the condition of the presence of a hydrogenation catalyst to obtain a raw material for preparing high-quality petroleum coke. As a commonly used device in the petroleum refining industry, the riser reactor, however, there are few reports on the scheme of treating catalytic slurry oil in the riser reactor to prepare high-quality petroleum coke raw materials. Summary of the Invention

[0007] The present invention aims to provide a method and system for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar. The riser reactor is used to provide a reaction site for catalytic slurry oil and ethylene tar, reducing the pretreatment of catalytic slurry oil in the process of preparing high-quality petroleum coke raw materials and improving the comprehensive utilization efficiency of ethylene tar and catalytic slurry oil.

[0008] To solve the above technical problems, the specific solution adopted by the present invention is as follows: A method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar, mixing catalytic slurry oil and ethylene tar into a raw material oil and transporting it into the riser reactor for hydrogen transfer reaction, and then separating the mixed material obtained from the hydrogen transfer reaction; the hydrogen transfer catalyst separated is transported to the catalyst regenerator, and the high-temperature hydrogen transfer catalyst regenerated by the catalyst regenerator returns to the riser reactor; the separated oil and gas are fractionated by a fractionating tower to obtain a wax oil fraction capable of producing high-quality petroleum coke.

[0009] As a further optimization of the above technical solution, the mass of ethylene tar accounts for 20% - 75% of the mass of the raw material oil.

[0010] As a further optimization of the above technical solution, the aromatic hydrocarbon content in the catalytic slurry oil exceeds 50%, the saturated fraction content does not exceed 40%, and the sulfur content is 0.5% - 2.0%; the olefin content in the ethylene tar does not exceed 30%, the aromatic hydrocarbon content is greater than 50%, and the gum and asphaltene content does not exceed 30%.

[0011] As a further optimization of the above technical solution, the reaction temperature in the riser reactor is 350 - 450°C, the reaction pressure is 0.1 - 0.3 MPa, and the reaction time is 0.5 - 5 s.

[0012] As a further optimization of the above technical solution, the hydrogen transfer catalyst is a molecular sieve catalyst with hydrogen transfer function, and the catalyst-oil ratio is 15:1 - 25:1.

[0013] As a further optimization of the above technical solution, the mass ratio of steam to raw material oil feed in the riser reactor is 0.05:1 - 1:1.

[0014] As a further optimization of the above technical solution, the regeneration temperature in the catalyst regenerator is 500 - 550 °C, the regeneration pressure is 0.20 - 0.40 MPa, and the regeneration time is 5 - 20 min.

[0015] A system for preparing high-quality petroleum coke raw materials from catalytic slurry and ethylene tar includes a raw material oil mixing tank, a riser reactor, and a fractionating tower that are connected in sequence. A catalyst regenerator is connected to the riser reactor;

[0016] The riser reactor includes a vertically arranged riser body. A stripping steam pipe is provided at the lower end of the riser body, and the upper end passes through a stripper and extends into a settler. The settler is connected to the fractionating tower through an oil and gas outlet pipe provided thereon;

[0017] The settler is connected to the stripper, and steam escape holes are provided on the riser body located in the stripper;

[0018] A riser regeneration inclined pipe is provided at the lower part of the riser body, and a settler conveying inclined pipe is provided at the lower part of the stripper. The discharge port of the settler conveying inclined pipe is connected to the feed port of the catalyst regenerator, and the discharge port of the catalyst regenerator is communicated with the feed port of the riser regeneration inclined pipe;

[0019] The raw material oil mixing tank is connected to the lower part of the riser body and is located above the riser regeneration inclined pipe.

[0020] As a further optimization of the above technical solution, a first cyclone separator is provided in the settler, and a second cyclone separator is provided in the catalyst regenerator.

[0021] As a further optimization of the above technical solution, the catalyst regenerator is a fluidized bed regenerator, and the regenerant is air or a mixture of air and steam.

[0022] Beneficial effects:

[0023] The riser reactor of the present invention provides a place for the reaction of ethylene tar and catalytic slurry. In the riser reactor, the catalytic slurry and ethylene tar react with the high-temperature regenerated catalyst in a water vapor atmosphere. The temperature of the hydrogen transfer catalyst after regeneration in the catalyst regenerator is relatively high. These high-temperature hydrogen transfer catalysts return to the riser reactor to participate in the catalytic reaction in a cycle, which can provide heat for the riser reactor and save resources.

[0024] The present invention uses inexpensive and abundant ethylene tar and catalytic slurry as raw materials to produce high-quality petroleum coke raw materials, increasing the added value of catalytic slurry and ethylene tar. Through the hydrogen transfer reaction between ethylene tar and catalytic slurry, on the one hand, the catalytic slurry no longer needs to be hydrotreated, reducing the pretreatment cost of the catalytic slurry; on the other hand, the hydrogen transfer catalyst has a certain desulfurization effect. By blending between low-sulfur ethylene tar and high-sulfur catalytic slurry, the sulfur content in the raw materials is reduced, improving the quality of the prepared high-quality petroleum coke raw materials.

[0025] The present invention uses a hydrogen transfer catalyst to carry out a hydrogen transfer reaction between ethylene tar and catalytic slurry in a riser reactor. The naphthenes in the catalytic slurry convert olefins and diolefins in the ethylene tar into alkanes through the hydrogen transfer reaction, and the naphthenes in the catalytic slurry dehydrogenate to form aromatics. This can not only increase the aromatic content in the catalytic slurry but also hydrogenate and convert unstable components such as olefins and diolefins in the ethylene tar into alkanes, which is beneficial for the condensation and coking reaction of the product fractionated after the hydrogen transfer reaction as a high-quality petroleum coke raw material during the delayed coking reaction process, thereby increasing the yield of high-quality petroleum coke. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic diagram of the system for preparing high-quality petroleum coke raw materials of the present invention;

[0027] Figure 2 It is an optical picture of the needle coke prepared in Application Example 1 of the present invention;

[0028] Reference numerals: 1, ethylene tar raw material tank; 2, catalytic slurry raw material tank; 3, raw material oil mixing tank; 4, ethylene tar oil pump; 5, catalytic slurry pump; 6, mixed raw material feed pump; 7, riser body; 8, settler; 9, first cyclone separator; 10, riser regeneration inclined pipe; 11, settler conveying inclined pipe; 12, regeneration air pipe; 13, catalyst regenerator; 14, second cyclone separator; 15, stripper; 16, fractionating tower; 17, stripping steam pipe; 18, oil and gas outlet pipe; 19, regeneration flue gas pipe. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0029] The following further elaborates on the technical solution of the present invention in conjunction with the drawings and specific embodiments. For parts not detailedly recorded and disclosed in the following embodiments of the present invention, they should all be understood as the prior art known or should be known to those skilled in the art.

[0030] The present invention discloses a system for preparing high-quality petroleum coke raw materials from catalytic slurry and ethylene tar, including a raw material oil mixing tank 3, a riser reactor, and a fractionating tower 16 connected in sequence, and a catalyst regenerator 13 is connected to the riser reactor.

[0031] The pipeline on the raw material oil mixing tank 3 is connected to the ethylene tar raw material tank 1 and the catalytic slurry raw material tank 2. Specifically, an ethylene tar pump 4 is connected to the outlet pipeline of the ethylene tar raw material tank 1, and a catalytic slurry pump 5 is connected to the outlet pipeline of the catalytic slurry raw material tank 2. The ethylene tar pump 4 and the catalytic slurry pump 5 are respectively used to cooperate with the corresponding mixing tank and the outlet pipeline to transport ethylene tar and catalytic slurry into the raw material oil mixing tank 3. A mixed raw material feed pump 6 is connected to the outlet pipeline of the raw material oil mixing tank 3 to transport the mixed raw material oil into the riser reactor.

[0032] The riser reactor includes a vertically arranged riser body 7. A stripping steam pipe 17 is arranged at the lower end of the riser body 7, and the upper end passes through the stripper 15 and extends into the settler 8.

[0033] The riser body 7 is used to provide a reaction site for the reaction between the catalytic slurry and the ethylene tar, and the reaction carried out is a hydrogen transfer reaction. A first cyclone separator 9 is arranged in the settler 8 to carry out gas-solid separation of the products after the hydrogen transfer reaction and the hydrogen transfer catalyst. An oil and gas outlet pipe 18 is arranged above the settler 8, and the oil and gas outlet pipe 18 is communicated with the fractionating tower 16 to transport the separated oil and gas into the fractionating tower 16 for fractionation.

[0034] The settler 8 is communicated with the stripper 15, and steam escape holes are arranged on the riser body 7 located in the stripper 15. The water vapor in the riser body 7 can escape into the stripper 15 through the steam escape holes. The separated hydrogen transfer catalyst enters the stripper 15, and after being stripped by the water vapor in the stripper 15, it is then transported to the catalyst regenerator 13 for regeneration.

[0035] A settler conveying inclined pipe 11 is arranged at the lower part of the stripper 15. The discharge port of the settler conveying inclined pipe 11 is connected to the feed port of the catalyst regenerator 13 to transport the hydrogen transfer catalyst stripped by the water vapor in the stripper 15 into the catalyst regenerator 13. A riser regeneration inclined pipe 10 is arranged at the lower part of the riser body 7. The feed port of the riser regeneration inclined pipe 10 is communicated with the discharge port of the catalyst regenerator 13 to transport the regenerated high-temperature hydrogen transfer catalyst into the riser body 7.

[0036] The catalyst regenerator 13 is a fluidized bed regenerator, and the regenerant is a mixture of air and steam or air. A regenerated air pipe 12 is provided at the bottom of the catalyst regenerator 13, a regenerated flue gas pipe 19 is provided at the top, and a second cyclone separator 14 is arranged inside the catalyst regenerator 13. The second cyclone separator 14 is located in the upper middle part of the catalyst regenerator 13. After the hydrogen transfer catalyst stripped by the steam in the stripper 15 enters the catalyst regenerator 13, air (or oxygen-containing gas) is introduced into the regenerated air pipe 12 at the bottom of the catalyst regenerator 13 to burn the coked hydrogen transfer catalyst and remove the coke on the catalyst. After the regenerated flue gas is separated from the solid by the second cyclone separator 14, it enters the flue gas treatment system through the regenerated flue gas pipe 19, and the solid particles separated by the second cyclone separator 14 are returned to the dense phase bed area of the catalyst regenerator 13.

[0037] The feedstock oil mixing tank 3 is connected to the lower part of the riser reactor body 7, and the connection point between the feedstock oil mixing tank 3 and the riser reactor body 7 is located above the riser regenerator inclined pipe 10.

[0038] Both the first cyclone separator 9 and the second cyclone separator 14 are cyclone separators in the prior art, and are one or more combinations of horizontal cyclone separators and vertical cyclone separators.

[0039] The present invention also discloses a method for preparing high-quality petroleum coke raw materials by using catalytic slurry and ethylene coking. The catalytic slurry and ethylene tar are mixed into a feedstock oil and transported into a riser reactor for hydrogen transfer reaction, and then the mixed material obtained from the hydrogen transfer reaction is separated; the separated hydrogen transfer catalyst is transported to the catalyst regenerator, and the high-temperature hydrogen transfer catalyst regenerated by the catalyst regenerator is returned to the riser reactor, and the heat generated by the regenerated hydrogen transfer catalyst is used to provide heat for the reaction in the riser reactor; the separated oil and gas are fractionated in a fractionating tower to obtain a wax oil fraction capable of producing high-quality petroleum coke.

[0040] In the feedstock oil mixed by the catalytic slurry and ethylene tar, the mass ratio of ethylene tar in the feedstock oil is 20% - 75%, preferably 30% - 50%.

[0041] The catalytic slurry is a by-product of a catalytic cracking unit, mainly containing saturated components, aromatic components and resins. The aromatic hydrocarbon content in the catalytic slurry exceeds 50%, the saturated component content does not exceed 40%, the saturated component is mainly composed of naphthene structures, and the sulfur content is 0.5% - 2.0%.

[0042] The ethylene tar is a by-product of a steam cracking unit, which has the advantages of low content of impurities such as sulfur and ash and high aromatic hydrocarbon content. The olefin content in the ethylene tar does not exceed 30%, the aromatic hydrocarbon content is greater than 50%, and the sum of the resin and asphaltene contents does not exceed 30%.

[0043] The reaction temperature in the riser reactor is 350-450° C., preferably 380-420° C., the reaction pressure is 0.1-0.3 MPa, preferably 0.12-0.15 MPa, and the reaction time is 0.5-5 s, preferably 1.0-2.0 s.

[0044] The hydrogen transfer catalyst is a molecular sieve catalyst with hydrogen transfer function, such as Y-type molecular sieve, ZSM-5, etc. The catalyst-oil ratio is 15:1 to 25:1.

[0045] The mass ratio of water vapor to crude oil feed in the riser reactor is 0.05:1 to 1:1, preferably 0.1:1 to 0.2:1.

[0046] The regeneration temperature of the catalyst regenerator is 500-550°C, the regeneration pressure is 0.20-0.40MPa, the regeneration time is 5-20min, and the temperature of the high-temperature hydrogen transfer catalyst after regeneration by the catalyst regenerator is also 500-550°C.

[0047] The method of preparing high-quality petroleum coke raw materials by using catalytic slurry oil and ethylene coking of the present invention can adopt the system of preparing high-quality petroleum coke raw materials by using catalytic slurry oil and ethylene tar. The method is specifically as follows:

[0048] The ethylene tar in the ethylene tar raw material tank 1 and the catalytic slurry in the catalytic slurry raw material tank 2 are respectively transported to the raw material oil mixing tank 3 by the ethylene tar pump 4 and the catalytic slurry pump 5 for sufficient mixing, and the mass of the ethylene tar accounts for 30% to 50% of the mass of the raw material oil;

[0049] The mixed crude oil is pumped out through the mixed crude feed pump 6 and sent to the riser body 7. Water vapor enters the riser body 7 through the stripping steam pipe 17. The mass ratio of water vapor to crude oil feed is 0.1:1-0.2:1. The water vapor rising at high speed in the riser body 7 drives the hydrogen transfer catalyst from the riser regeneration inclined tube 10 to rise at high speed. The hydrogen transfer catalyst and the crude oil are mixed, heated and hydrogen transfer reacted in the riser body 7. The reaction temperature in the riser body 7 is 380-420°C, the reaction pressure is 0.12-0.15MPa, the reaction time is 1.0-2.0s, and the hydrogen transfer agent-oil ratio is 15-25.

[0050] The mixed material after the reaction (including the reaction product and the hydrogen transfer catalyst) enters the settler 8 and is separated from the gas by the first cyclone separator 9. The separated hydrogen transfer catalyst enters the stripper 15, and after being stripped by water vapor in the stripper 15, it is sent to the catalyst regenerator 13 through the settler conveying inclined pipe 11 for regeneration. The regeneration air pipe 12 at the bottom of the catalyst regenerator 13 is introduced with air (or oxygen-containing gas) to burn the coked catalyst to remove the coke on the catalyst. The regeneration temperature of the catalyst regenerator is 500-550°C, and the regeneration pressure is 0.20- 0.40MPa, the regeneration time is 5 to 20min, and the temperature of the high-temperature hydrogen transfer catalyst after regeneration in the catalyst regenerator is also 500 to 550°C; the regenerated flue gas formed after the catalyst is charred is separated from the solid by the second cyclone separator 14, and then enters the flue gas treatment system through the regeneration flue gas pipe 19, and the solid particles separated by the regenerator cyclone separator are returned to the dense phase bed area of ​​the regenerator, and the regenerated high-temperature hydrogen transfer catalyst is returned to the bottom of the riser reactor through the riser regeneration inclined pipe 10 for recirculation, so as to provide the riser reactor with the heat required for the reaction;

[0051] The separated reaction products enter the fractionation tower 16 through the oil and gas outlet pipe 18, and after fractionation, products such as gas and gasoline fractions, diesel fractions and wax oil fractions are obtained. The wax oil fraction can be used as a raw material for producing high-quality petroleum coke.

[0052] In the riser reactor, cycloalkanes, hydrogenated aromatics, etc. in the catalytic oil slurry are used as hydrogen donors to dehydrogenate and aromatize, and the removed hydrogen is transferred to diolefins, olefins, etc. in the ethylene tar, so that the olefins in the ethylene tar are reduced to stable components such as alkanes, thereby reducing the coking performance of the ethylene tar. Heavy components such as asphaltene in the catalytic oil slurry and ethylene tar undergo high-temperature condensation reaction on the hydrogen transfer catalyst to generate coke attached to the hydrogen transfer catalyst. The hydrogen transfer catalyst is regenerated by the catalyst regenerator 13. On the one hand, the coke on the hydrogen transfer catalyst is removed so that the catalyst can be recycled. On the other hand, the high temperature of the regenerated hydrogen transfer catalyst is used to provide the heat required for the reaction to the riser reactor, thereby saving energy.

[0053] Example 1

[0054] The ethylene tar in the ethylene tar feed tank 1 and the catalytic oil slurry in the catalytic oil slurry feed tank 2 are respectively transported to the feed oil mixing tank 3 by the ethylene tar pump 4 and the catalytic oil slurry pump 5 for sufficient mixing. The mass of ethylene tar accounts for 50% of the mass of the feed oil, that is, the feed oil is prepared by mixing ethylene tar and catalytic oil slurry in equal amounts. The feed rate of catalytic oil slurry in the lifting pipe body 7 is 2.0 kg / h, and the feed rate of ethylene tar is 2.0 kg / h.

[0055] The mixed feedstock oil is pumped out by the mixed feedstock feed pump 6 and sent into the riser reactor body 7. Steam enters the riser reactor body 7 through the stripping steam pipe 17. The mass ratio of steam to the feedstock oil is 0.1:1. The high-speed upward steam in the riser reactor body 7 drives the hydrogen transfer catalyst from the riser regenerator inclined pipe 10 to move upward at high speed. The hydrogen transfer catalyst and the feedstock oil are mixed, heated and undergo hydrogen transfer reaction in the riser reactor body 7. The reaction temperature in the riser reactor body 7 is 380 °C, the reaction pressure is 0.12 MPa, the reaction time is 1.0 s, and the hydrogen transfer agent-oil ratio is 10.

[0056] The reacted mixture (including reaction products and hydrogen transfer catalyst) enters the settler 8 and undergoes gas-solid separation by the first cyclone separator 9. The separated hydrogen transfer catalyst enters the stripper 15, and after being stripped by the steam in the stripper 15, it is sent to the catalyst regenerator 13 through the settler transfer inclined pipe 11 for regeneration. The regeneration air pipe 12 at the bottom of the catalyst regenerator 13 introduces air (or oxygen-containing gas) to burn the coked catalyst to remove the coke on the catalyst. The regeneration temperature of the catalyst regenerator is 500 °C, the regeneration pressure is 0.20 MPa, and the regeneration time is 10 min. The temperature of the high-temperature hydrogen transfer catalyst after regeneration in the catalyst regenerator 13 is also 500 °C. After the regeneration flue gas formed by burning the catalyst coke is separated from solids by the second cyclone separator 14, it enters the flue gas treatment system through the regeneration flue gas pipe 19. The solid particles separated by the regenerator cyclone separator are returned to the dense phase bed area of the regenerator, and the regenerated high-temperature hydrogen transfer catalyst is returned to the bottom of the riser reactor through the riser regenerator inclined pipe 10 for recycling to provide the heat required for the reaction in the riser reactor; among them, the catalyst regenerator 13 is a fluidized bed regenerator, and the regenerating agent is air.

[0057] The separated reaction products enter the fractionating tower 16 through the oil-gas outlet pipe 18, and products such as gas, gasoline fraction, diesel fraction and wax oil fraction are obtained after fractionation. The wax oil fraction can be used as a raw material for producing high-quality petroleum coke. The yield and main physical properties of the prepared wax oil fraction are shown in Table 3.

[0058] The main physical properties of the catalytic slurry and ethylene tar used in this example are shown in Table 1: Table 1 Main properties of catalytic slurry and ethylene tar

[0059] Examples 2 - 6

[0060] The operation steps of Examples 2 - 6 are basically the same as those of Example 1, except that the main operating parameters in Examples 2 - 6 are as shown in Table 2 below: Table 2 Main operating parameters

[0061] The yields and main physical properties of the wax oil fractions prepared in Examples 1-6 are shown in Table 3 as follows: Table 3 Yields and Main Physical Properties of Wax Oil Fractions

[0062] As can be seen from Table 3, high wax oil yields can be obtained in the examples of this application.

[0063] Application Example 1

[0064] As a high-quality petroleum coke, the wax oil fraction used as the raw material for preparing high-quality petroleum coke in the present invention can be used to prepare needle coke and has good performance in the preparation of needle coke.

[0065] Taking the wax oil fraction prepared in Example 4 above as the feedstock for delayed coking, a delayed coking test was carried out on a medium-scale delayed coking unit. The main operating conditions of the delayed coking pilot test are shown in Table 4, and the yields and physical properties of the needle coke obtained from the delayed coking are shown in Table 5. Table 4 Main Operating Conditions of Delayed Coking Pilot Test

[0066] Comparative Example 1

[0067] In this comparative example, the method of the prior art was used to prepare needle coke. Specifically, the method disclosed in the invention patent with the patent number CN113122329A and the patent name of a method and system for co-producing needle coke and low-sulfur petroleum coke was adopted. The yields and physical properties of the needle coke prepared by the method of the prior art are shown in Table 5. Table 5 Yields and Main Properties of Needle Coke

[0068] As Figure 2 shown is the optical photograph of the needle coke prepared in Application Example 1. Combining with Table 5 and Figure 2 it can be known that the wax oil fraction prepared in this application can be used as the raw material for producing needle coke. After being processed by the delayed coking unit using this wax oil fraction, a needle coke yield of 50.30% can be obtained. Compared with Comparative Example 1, the needle coke yield prepared by the present invention has been improved to a certain extent, and the optical properties of the needle coke prepared in this application example are good, the fiber structure is obvious, and it has good performance.

[0069] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar, characterized in that The catalytic slurry oil and ethylene tar are mixed as feedstock oil and transported into a riser reactor for hydrogen transfer reaction, and then the mixed materials obtained from the hydrogen transfer reaction are separated; The separated hydrogen transfer catalyst is transported to a catalyst regenerator, and the high-temperature hydrogen transfer catalyst after regeneration in the catalyst regenerator returns to the riser reactor; The separated oil and gas are fractionated in a fractionating tower to obtain a wax oil fraction that can be used to produce high-quality petroleum coke.

2. The method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 1, characterized in that, The mass of ethylene tar accounts for 20% - 75% of the mass of the feedstock oil.

3. The method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 1, characterized in that, The aromatic hydrocarbon content in the catalytic slurry oil exceeds 50%, the saturated fraction content does not exceed 40%, and the sulfur content is 0.5% - 2.0%; the olefin content in the ethylene tar does not exceed 30%, the aromatic hydrocarbon content is greater than 50%, and the gum and asphaltene content does not exceed 30%.

4. A method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 1, characterized in that The reaction temperature in the riser reactor is 350 - 450 °C, the reaction pressure is 0.1 - 0.3 MPa, and the reaction time is 0.5 - 5 s.

5. A method for preparing high-quality petroleum coke raw materials from catalytic oil slurry and ethylene tar according to claim 1, characterized in that, The hydrogen transfer catalyst is a molecular sieve catalyst with hydrogen transfer function, and the catalyst-oil ratio is 15:1 - 25:

1.

6. The method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 1, characterized in that, The mass ratio of steam to feedstock oil feed in the riser reactor is 0.05:1 - 1:

1.

7. A method for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 1, characterized in that, The regeneration temperature in the catalyst regenerator is 500 - 550 °C, the regeneration pressure is 0.20 - 0.40 MPa, and the regeneration time is 5 - 20 min.

8. A system for preparing high-quality petroleum coke raw materials from catalytic slurry and ethylene tar, characterized in that: It includes a feedstock oil mixing tank (3), a riser reactor, and a fractionating tower (16) connected in sequence, and a catalyst regenerator (13) is connected to the riser reactor; The riser reactor includes a vertically arranged riser body (7). The lower end of the riser body (7) is provided with a stripping steam pipe (17), and the upper end passes through a stripper (15) and extends into a settler (8). The settler (8) is connected to the fractionating tower (16) through an oil and gas outlet pipe (18) provided thereon; The settler (8) is connected to the stripper (15), and steam escape holes are provided on the riser body (7) located in the stripper (15); The lower part of the riser body (7) is provided with a riser regeneration inclined pipe (10), and the lower part of the stripper (15) is provided with a settler transfer inclined pipe (11). The discharge port of the settler transfer inclined pipe (11) is connected to the feed port of the catalyst regenerator (13), and the discharge port of the catalyst regenerator (13) is connected to the feed port of the riser regeneration inclined pipe (10); The feedstock oil mixing tank (3) is connected to the lower part of the riser body (7) and is located above the riser regeneration inclined pipe (10).

9. The system for preparing high-quality petroleum coke raw materials from catalytic slurry and ethylene tar according to claim 8, wherein: A first cyclone separator (9) is provided in the settler (8), and a second cyclone separator (14) is provided in the catalyst regenerator (13).

10. A system for preparing high-quality petroleum coke raw materials from catalytic slurry oil and ethylene tar according to claim 8, characterized in that, The catalyst regenerator (13) is a fluidized bed regenerator, and the regenerating agent is air or a mixture of air and steam.

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