A catalytic conversion process for producing light aromatics

Abstract

The application provides a catalytic conversion method for producing light aromatic hydrocarbons, which comprises the following steps: feeding light raw oil into a first reactor to contact with a first catalyst for first catalytic conversion, so as to obtain first catalyst to be stripped and first upward oil gas product; the first catalyst to be stripped is subjected to first stripping, so as to obtain first spent catalyst and first stripping product; the first reactor is a bubbling fluidized bed reactor or a turbulent fluidized bed reactor; the first upward oil gas product and the first stripping product are fed into a riser reactor to contact with a second catalyst, and then contact with heavy raw oil for second catalytic conversion, so as to obtain second catalytically converted material; the second catalytically converted material is subjected to gas-solid separation and stripping, so as to obtain second oil gas product and second spent catalyst. Through the technical scheme, the conversion rate and selectivity of catalytic conversion for producing light aromatic hydrocarbons are effectively improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of petroleum chemical industry, in particular to a catalytic conversion method for producing light aromatic hydrocarbons. BACKGROUND

[0002] Benzene, toluene and xylene are collectively referred to as BTX, which are important raw materials for producing chemical products such as polyester fibers. The demand for light aromatic hydrocarbons in the market is increasing and is still in short supply.

[0003] In the process of petroleum refining, in addition to gasoline and diesel fuel products for vehicles, a large amount of by-products such as heavy oil, heavy gasoline, heavy naphtha, etc. will be produced. These products have less direct demand in the market. These products are rich in polycyclic aromatic hydrocarbons and other components, which can be used to produce light aromatic hydrocarbons after catalytic conversion.

[0004] ZL98101765.7 discloses a method for simultaneously producing low-carbon olefins and high-aromatic gasoline. The heavy petroleum hydrocarbon and water vapor are contacted with a zeolite-containing catalyst in the lower part of the lifting pipe of a composite reactor composed of a lifting pipe and a dense phase fluidized bed, and the light petroleum hydrocarbon is contacted with the zeolite-containing catalyst from the lifting pipe at the bottom of the dense phase fluidized bed of the upper part of the composite reactor.

[0005] However, the conversion rate and selectivity of the existing catalytic cracking method for producing light aromatic hydrocarbons still need to be further improved. SUMMARY

[0006] The purpose of the present application is to further improve the conversion rate and selectivity of catalytic cracking for producing light aromatic hydrocarbons.

[0007] In order to achieve the above purpose, the present application provides a catalytic conversion method for producing light aromatic hydrocarbons, which comprises: feeding a light raw oil into a first reactor to contact with a first catalyst for carrying out a first catalytic conversion, to obtain a first catalyst to be stripped and a first upward oil gas product; the first reactor is a bubbling fluidized bed reactor or a turbulent fluidized bed reactor; feeding the first upward oil gas product and the first stripping product into a lifting pipe reactor to contact with a second catalyst, and then contacting with a heavy raw oil to carry out a second catalytic conversion, to obtain a second catalytic conversion material; carrying out gas-solid separation and stripping on the second catalytic conversion material to obtain a second oil gas product and a second spent catalyst; carrying out first regeneration and second regeneration on the first spent catalyst and the second spent catalyst respectively to obtain a first regenerated catalyst and a second regenerated catalyst respectively, and returning to participate in the first catalytic conversion and the second catalytic conversion respectively.

[0008] Through the above technical solution, the present invention realizes the directional and zoned conversion of two different reactions in a set of reaction devices, and the reaction products of the light raw oil improve the product distribution of the heavy raw oil, thereby increasing the catalytic conversion rate of heavy aromatics in the raw oil and the yield of target product light aromatics, saving device investment and energy consumption.

[0009] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0010] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the following detailed description, they are used to explain the present invention but do not constitute a limitation of the present invention. In the accompanying drawings:

[0011] Figure 1 This is a schematic diagram of the system structure in a preferred embodiment of the present invention.

[0012] Description of Reference Numerals

[0013] 100. First reactor; 200. Second reactor; 300. First stripper; 400. First regenerator; 500. Second regenerator; 600. Second stripper

[0014] 101. First fluidizing medium inlet; 102. Light crude oil and atomizing medium inlet; 103. Sloping pipe for stripping; 104. Gas distribution plate

[0015] 201. Heavy feedstock oil and atomizing medium inlet; 202. Second waiting inclined pipe; 203. Reaction oil and gas outlet; 204. First stripping product inlet

[0016] 301. First stripping medium inlet; 302. First waiting inclined pipe; 303. First supplement inclined pipe;

[0017] 401. First regeneration medium inlet; 402. First regeneration inclined tube; 403. First regeneration flue gas;

[0018] 501. Second regeneration medium inlet; 502. Second regeneration inclined tube; 503. Second regeneration flue gas;

[0019] 601. Second stripping medium inlet DETAILED DESCRIPTION

[0020] The following is a detailed description of the specific embodiments of the present invention. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention and are not intended to limit the present invention.

[0021] The present invention provides a catalytic conversion method for producing light aromatic hydrocarbons, which comprises: feeding light raw oil into a first reactor, contacting the first catalyst with the first catalyst, performing a first catalytic conversion, obtaining a first catalyst to be stripped and a first rising oil and gas product, performing a first stripping on the first catalyst to be stripped, obtaining a first catalyst to be regenerated and a first stripping product; the first reactor is a bubbling fluidized bed reactor or a turbulent fluidized bed reactor; feeding the first rising oil and gas product and the first stripping product into a riser reactor, contacting the first catalyst with a second catalyst, and then contacting the first stripping product with a heavy raw oil, performing a second catalytic conversion, obtaining a material after the second catalytic conversion, performing gas-solid separation and stripping on the material after the second catalytic conversion, obtaining a second oil and gas product and a second catalyst to be regenerated; performing a first regeneration and a second regeneration on the first catalyst to be regenerated and the second catalyst to be regenerated, respectively, obtaining a first regenerated catalyst and a second regenerated catalyst, and returning them to participate in the first catalytic conversion and the second catalytic conversion, respectively.

[0022] The inventors of the present invention have discovered that using different catalysts for zoned conversion of light feedstock and heavy feedstock, and using the conversion products of light feedstock oil to participate in the conversion of heavy feedstock oil, can effectively improve product distribution, increase the catalytic conversion rate of heavy aromatics in the feedstock oil and the yield of target product light aromatics.

[0023] Optionally, the method further includes: fractionating the second oil and gas product to obtain a recycled fraction, and then returning at least a portion of the recycled fraction to the first reactor to participate in the first catalytic conversion; the starting point temperature of the distillation range of the recycled fraction is any value between 80-110°C and the end point temperature is any value between 200-280°C.

[0024] Among them, optionally, a first stripping product inlet, a second catalyst inlet and a heavy raw oil inlet are arranged in sequence from bottom to top at the lower part of the riser reactor, so that the first rising oil and gas product and the first stripping product contact the second catalyst for catalytic conversion before the heavy raw oil.

[0025] Among them, optionally, the conditions for the first catalytic conversion include: the first catalyst is in a bubbling fluidization state or a turbulent fluidization state from bottom to top, and the light feedstock oil contacts the first catalyst from bottom to top in downstream; the relative apparent average linear velocity of oil and gas is 0.05-3 m / s, preferably 0.1-2 m / s; the weight hourly space velocity of oil and gas is 1-6 h -1 , preferably 2-4h -1 The reaction temperature is 300-700°C, preferably 350-500°C, the agent-oil weight ratio is 1-20, preferably 2-10, the reaction pressure is 0.1-1.0MPa, preferably 0.1-0.5MPa, and the reaction time is 1-30 seconds, preferably 5-20 seconds.

[0026] Optionally, the first catalyst is a spherical catalyst or a non-spherical catalyst, preferably a spherical catalyst; the average particle size of the first catalyst is 0.2-7 mm, preferably 0.35-3.5 mm; the particle density of the first catalyst is 1.4-2 g / cm 3 , preferably 1.5-1.8g / cm 3 ; The first catalyst contains ZSM molecular sieve and / or Beta molecular sieve; The first catalyst is loaded with 0.1-3 weight% of a first metal, and the first metal is at least one of Fe, Mo, Re, Pt or Pd.

[0027] Among them, optionally, the conditions for the second catalytic conversion include: the second catalyst particles are in a transport fluidized state, the oil and gas apparent average linear velocity is 2-20 m / s, preferably 3-10 m / s; the oil and gas weight hourly space velocity is 4-20h -1 , preferably 6-12h -1 ; The reaction temperature is 400-700°C, preferably 500-650°C; the agent-oil weight ratio is 3-20, preferably 4-12, the reaction pressure is 0.1-0.4MPa, preferably 0.1-0.3MPa, and the reaction time is 1-10 seconds, preferably 1-5 seconds.

[0028] Wherein, optionally, the second catalyst contains 10-60 wt% of a molecular sieve, 1-40 wt% of a binder and 1-90 wt% of a carrier; the molecular sieve contains or does not contain rare earth and is a ZSM molecular sieve, a Y molecular sieve, a HY molecular sieve, a USY molecular sieve and a Beta molecular sieve; the binder is selected from a silica binder and / or an alumina binder; the carrier is selected from one or more of silica, kaolin, montmorillonite, diatomaceous earth, halloysite, saponite, rectorite, sepiolite, attapulgite, hydrotalcite and bentonite; the rare earth is one or more of La, Ce, Pr and Nd; the average particle size of the second catalyst is 50-100 μm, preferably 60-80 μm, and the particle density of the second catalyst is 1.3-1.5 g / cm 3 .

[0029] Wherein, optionally, the diameter of the first reactor is 1.1-30 times, preferably 2-20 times, the diameter of the riser reactor, and the first reactor is connected in series at the lower part of the riser reactor; one or more gas distribution plates are provided at the connection between the two reactors; the ratio of the average particle size of the first catalyst and the second catalyst particles is 3-30:1, preferably 5-15:1, and the ratio of the particle density is 1.1-1.2:1.

[0030] Among them, optionally, the starting point temperature of the distillation range of the light feedstock oil is any value between 80-110°C and the end point temperature is any value between 200-280°C and contains 1-99 weight% of C9 aromatics and 1-99 weight% of toluene; preferably, the light feedstock oil contains 10-90 weight% of C9 aromatics and 10-90 weight% of toluene; more preferably, the light feedstock oil contains 20-80 weight% of C9 aromatics and 20-80 weight% of toluene; further preferably, the light feedstock oil contains 40-60 weight% of C9 aromatics and 40-60 weight% of toluene; the starting point temperature of the distillation range of the heavy feedstock oil is any value between 150-250°C and the end point temperature is any value between 300-550°C.

[0031] Among them, optionally, the light feedstock oil contains at least one of naphtha fraction, gasoline fraction, FCC light cycle oil light fraction, hydrotreated diesel light fraction and aromatic mixture; the heavy feedstock oil contains at least one of hydrotreated diesel (HLCO), straight-run diesel, straight-run wax oil, coker wax oil, hydrotreated wax oil, deasphalted oil, hydrorefined oil, hydrocracking tail oil, vacuum residue and atmospheric residue.

[0032] Optionally, the first regeneration uses a fluidized bed coking tank for complete regeneration, and the second regeneration uses a riser reactor for regeneration.

[0033] refer to Figure 1As a relatively preferred embodiment of the present invention, the light feedstock oil is preheated and enters the first reactor 100 together with the light feedstock oil atomizing medium through the light feedstock oil inlet 102 for a first catalytic conversion to obtain a first catalyst to be stripped and a first rising oil and gas product. The first rising oil and gas product enters the riser reactor 200 under the action of the fluidizing medium entering from the inlet 101. The heavy feedstock oil is preheated and enters the riser reactor 200 together with the heavy feedstock oil atomizing medium through the heavy feedstock oil inlet 201 for a second catalytic conversion. The heavy feedstock oil inlet 201 is located above the outlet of the second regeneration inclined tube 502. It is stripped by the second stripping medium in the second stripper 600 (entering the stripping medium inlet 601) to obtain a second oil and gas product and a second catalyst to be regenerated. The second oil and gas product enters the separation equipment through the oil and gas outlet 203. After reaction in the first reactor 100, the first catalyst to be stripped enters the first stripper 300 via the stripping transfer inclined pipe 103 for stripping, producing a first spent catalyst and a first stripping product. The first stripping product enters the riser reactor 200 via the first stripping product inlet 204, which is located below the outlet of the second regeneration inclined pipe 502. A portion of the first spent catalyst stripped in the first stripper is recycled back to the first reactor 100 via the first supplementary inclined pipe 303, while a portion enters the first regenerator 400 via the first regeneration inclined pipe 302 for first regeneration. After the first regeneration, the first regenerated catalyst is returned to the lower portion of the first reactor 100 via the first regeneration inclined pipe 402. The first regenerator utilizes a fluidized bed for complete regeneration. After reaction in the riser reactor 200, the second spent catalyst enters the second regenerator 500 via the second regeneration inclined pipe 202 for regeneration. After regeneration, the catalyst returns to the lower portion of the riser reactor via the second regeneration inclined pipe 502.

[0034] The present invention is further described in detail below by way of examples. Unless otherwise specified, the raw materials used in the examples can be obtained from commercial sources.

[0035] The catalysts used in the examples and comparative examples include: the first catalyst is a spherical catalyst with an average particle size of 1 mm and a particle density of 1.7 g / cm 3 The first catalyst is composed of a beta molecular sieve loaded with 2 wt% Mo and 0.2 wt% Fe, with a minimum fluidization velocity of 0.4 m / s; the second catalyst is purchased from SLA-1, with an average particle size of 70 mm and a particle density of 1.47 g / cm 3 The second catalyst contains 30% by weight of Y molecular sieve, 20% by weight of silica binder and 50% of kaolin, and the minimum fluidization velocity is 0.0022m / s.

[0036] The properties of the light crude oil and heavy crude oil used in the examples and comparative examples are shown in Tables 1 and 2.

[0037] Table 1

[0038]

[0039] Table 2

[0040] Feedstock oil name Heavy feedstock oil Feedstock oil origin HLCO <![CDATA[密度(20℃),千克 / 米 3 ]]> 912.1 Freezing point, °C <-50 Aniline point, °C <25 Average molecular weight 183 Hydrocarbon group mass composition, wt% 100 Paraffins 8.8 Naphthenes 14.4 Aromatics 76.8 Monocyclic aromatics 63.8 Bicyclic aromatics 11.8 Other aromatics 1.2 Distillation range, °C 156.8～338.2 Carbon and hydrogen content, wt% 100 Carbon content 89.05 Hydrogen content 10.95 Refraction index (20°C) 1.51

[0041] Example 1

[0042] refer to Figure 1 The first reactor is a bubbling bed reactor, the riser reactor is a constant diameter riser reactor, and the ratio of the inner diameter of the first reactor to that of the riser reactor is 10:1.

[0043] The light feedstock oil is a simulated feedstock oil mixed with C9 heavy aromatics and toluene in a mass ratio of 65.8:34.2. After preheating, it is fed into the first reactor at a feed rate of 30g / min together with the atomizing medium nitrogen from the oil and gas inlet at the lower part of the first reactor. The temperature is 400℃, the feedstock mass ratio is 3, and the weight hourly space velocity is 3h -1 Under the conditions of countercurrent contact reaction with the first catalyst, the reaction product is carried by the fluidizing medium nitrogen into the riser reactor, and the heavy crude oil HLCO is preheated and enters the riser reactor together with the atomizing medium water vapor. At a temperature of 580 ° C, a catalyst-oil mass ratio of 9, and a weight hourly space velocity of 10h -1 The reaction was carried out under the following conditions, and the stripped reaction oil and gas entered the separation equipment. The catalyst after the reaction in the first reactor entered the first stripper through the lower catalyst outlet for stripping. The stripping medium was nitrogen. The stripped oil and gas entered the riser reactor through the first stripping product inlet. Part of the stripped first catalyst was recycled back to the catalyst replenishment port at the top of the first reactor, and part was regenerated in the first regenerator. The regenerated first regenerator returned to the bottom of the first reactor. The first regenerator used a fluidized bed for complete regeneration. After the second catalytic conversion reaction in the riser reactor, the second catalyst was stripped and regenerated in the second regenerator. The regenerated second regenerator returned to the riser reactor. The operating parameters and product compositions are shown in Tables 3 and 4. The simulated feedstock and HLCO feed weights were equal per unit time.

[0044] Comparative Example 1

[0045] A conventional riser reactor was used, i.e., only the riser reactor in Example 1 was used. The feedstock oil was a mixture of simulated feedstock oil and HLCO in a mass ratio of 1:1. The mixed feedstock oil was preheated and fed into the riser reactor at a feed rate of 30 g / min together with the atomizing medium water vapor. The temperature was 560°C, the feedstock-oil mass ratio was 8, and the space velocity was 10 h. -1The reaction was carried out under the following conditions. The stripped reaction oil and gas were then fed into the separation equipment. The catalyst was stripped and then regenerated in the regenerator. The regenerated catalyst was then returned to the riser reactor. The operating parameters and product compositions are shown in Tables 3 and 4.

[0046] Example 2

[0047] Catalytic conversion was carried out in the same manner as in Example 1, except that the light feedstock oil was replaced by the simulated feedstock oil as shown in Table 1. The operating parameters and product compositions are shown in Tables 3 and 4.

[0048] Comparative Example 2

[0049] Catalytic conversion was carried out in the same manner as in Comparative Example 1, except that the light feedstock oil was replaced by the simulated feedstock oil as shown in Table 1. The operating parameters and product compositions are shown in Tables 3 and 4.

[0050] Table 3

[0051]

[0052] Table 4

[0053] Example 1 Comparative Example 1 Example 2 Comparative Example 2 Product distribution, wt% Gasoline 67.88 63.01 61.04 57.85 Other 32.12 36.99 38.96 42.15 C6-C10 aromatics yield, wt% 64.25 59.37 57.41 46.88 Benzene 2.92 1.87 2.09 2.12 Toluene 16.20 28.70 11.55 21.04 Xylene 25.67 7.12 31.17 6.89 Ethylbenzene 0.83 0.95 4.26 1.09 C8 aromatics 26.50 8.07 35.43 7.98 C9 aromatics 14.13 18.37 5.17 9.20 C10 aromatics 4.50 2.36 3.17 6.54 BTX yield, wt% 44.79 37.69 44.81 30.05 C9 aromatics single pass conversion, wt% 52.89 38.76 33.13 25.22

[0054] As can be seen from Table 2, compared with Comparative Examples 1 and 2, the BTX yield and C9 aromatics conversion rate of Examples 1 and 2 are significantly improved.

[0055] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, and these simple modifications all fall within the scope of protection of the present invention.

[0056] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any appropriate manner without contradiction. To avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0057] In addition, the various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A catalytic conversion method for producing light aromatic hydrocarbons, characterized in that: The method comprises: feeding light crude oil into a first reactor to contact with a first catalyst for a first catalytic conversion to obtain a first catalyst to be stripped and a first rising oil and gas product; and performing a first stripping on the first catalyst to be stripped to obtain a first spent catalyst and a first stripping product; the first reactor is a bubbling fluidized bed reactor or a turbulent fluidized bed reactor; The first rising oil and gas product and the first stripping product are fed into a riser reactor and contacted with a second catalyst and then with heavy feedstock oil to undergo a second catalytic conversion to obtain a second catalytically converted material, and the second catalytically converted material is subjected to gas-solid separation and stripping to obtain a second oil and gas product and a second spent catalyst; Regenerating the first catalyst to be spent and the second catalyst to be spent respectively to obtain a first regenerated catalyst and a second regenerated catalyst, and returning the catalysts to participate in the first catalytic conversion and the second catalytic conversion respectively; The first catalyst contains ZSM molecular sieve and / or Beta molecular sieve; the first catalyst is loaded with 0.1-3 wt% of a first metal, and the first metal is at least one of Fe, Mo, Re, Pt or Pd; The light feedstock oil has a distillation range with a starting point temperature of any value between 80-110° C. and an end point temperature of any value between 200-280° C. and contains 1-99% by weight of C9 aromatics and 1-99% by weight of toluene; The second catalyst contains 10-60 wt% of a molecular sieve, 1-40 wt% of a binder and 1-90 wt% of a carrier; The diameter of the first reactor is 1.1 to 30 times the diameter of the riser reactor, and the first reactor is connected in series to the lower part of the riser reactor.

2. The method according to claim 1, wherein The method also includes: fractionating the second oil and gas product to obtain a recycled fraction, and then returning at least a portion of the recycled fraction to the first reactor to participate in the first catalytic conversion; the starting point temperature of the distillation range of the recycled fraction is any value between 80-110°C and the end point temperature is any value between 200-280°C; and a first stripping product inlet, a second catalyst inlet, and a heavy feedstock inlet are arranged in sequence from bottom to top at the lower part of the riser reactor.

3. The method according to claim 1 or 2, wherein: The conditions for the first catalytic conversion include: the first catalyst is in a bubbling fluidization state or a turbulent fluidization state from bottom to top, the light feedstock oil contacts the first catalyst from bottom to top in downstream flow; the relative apparent average linear velocity of the oil and gas is 0.05-3 m / s; the weight hourly space velocity of the oil and gas is 1-6 h -1 The reaction temperature is 300-700°C, the agent-oil weight ratio is 1-20, the reaction pressure is 0.1-1.0 MPa, and the reaction time is 1-30 seconds.

4. The method according to claim 3, wherein: The relative apparent average linear velocity of oil and gas is 0.1-2 m / s; the weight hourly space velocity of oil and gas is 2-4 h -1 The reaction temperature is 350-500°C, the agent-oil weight ratio is 2-10, the reaction pressure is 0.1-0.5 MPa, and the reaction time is 5-20 seconds.

5. The method according to claim 1 or 2, wherein: The first catalyst is a spherical catalyst or a non-spherical catalyst; the average particle size of the first catalyst is 0.2-7 mm; the particle density of the first catalyst is 1.4-2 g / cm 3 .

6. The method according to claim 5, wherein: The first catalyst is a spherical catalyst; the average particle size of the first catalyst is 0.35-3.5 mm; the particle density of the first catalyst is 1.5-1.8 g / cm 3 .

7. The method according to claim 1 or 2, wherein: The conditions for the second catalytic conversion include: the second catalyst particles are in a transport fluidized state, the oil and gas apparent average linear velocity is 2-20 m / s; the oil and gas weight hourly space velocity is 4-20 h -1 ; The reaction temperature is 400-700℃; the agent-oil weight ratio is 3-20, the reaction pressure is 0.1-0.4MPa, and the reaction time is 1-10 seconds.

8. The method according to claim 7, wherein: The conditions for the second catalytic conversion include: the average apparent linear velocity of oil and gas is 3-10 m / s; the weight hourly space velocity of oil and gas is 6-12 h -1 ; The reaction temperature is 500-650℃; the agent-oil weight ratio is 4-12, the reaction pressure is 0.1-0.3MPa, and the reaction time is 1-5 seconds.

9. The method according to claim 1 or 2, wherein: The molecular sieve in the second catalyst contains or does not contain rare earth and is ZSM molecular sieve, Y molecular sieve, HY molecular sieve, USY molecular sieve or Beta molecular sieve; the binder is selected from silica binder and / or alumina binder; the carrier is selected from one or more of silica, kaolin, montmorillonite, diatomaceous earth, halloysite, saponite, rectorite, sepiolite, attapulgite, hydrotalcite and bentonite; the rare earth is one or more of La, Ce, Pr and Nd; The average particle size of the second catalyst is 50-100 μm, and the particle density of the second catalyst is 1.3-1.5 g / cm 3 .

10. The method according to claim 9, wherein: The average particle size of the second catalyst is 60-80 μm.

11. The method according to claim 1 or 2, wherein: One or more gas distribution plates are provided at the connection between the first reactor and the riser reactor; The ratio of average particle diameters of the first catalyst and the second catalyst particles is 3-30:1, and the ratio of particle densities is 1.1-1.2:

1.

12. The method according to claim 11, wherein The diameter of the first reactor is 2-20 times the diameter of the riser reactor; the ratio of the average particle diameters of the first catalyst and the second catalyst particles is 5-15:

1.

13. The method according to claim 1 or 2, wherein: The light feedstock oil contains 10-90 wt% of C9 aromatics and 10-90 wt% of toluene; The starting point temperature of the distillation range of the heavy feedstock oil is any value between 150-250°C and the ending point temperature is any value between 300-550°C.

14. The method according to claim 13, wherein The light feedstock oil contains 20-80 wt % of C9 aromatics and 20-80 wt % of toluene.

15. The method according to claim 14, wherein The light feedstock oil contains 40-60 wt % of C9 aromatics and 40-60 wt % of toluene.

16. The method according to claim 13, wherein: The light feedstock oil contains at least one of naphtha fraction, gasoline fraction, FCC light cycle oil light fraction, hydrotreated diesel light fraction and aromatic hydrocarbon mixture; The heavy feedstock oil contains at least one of hydrogenated diesel, straight-run diesel, straight-run wax oil, coker wax oil, hydrotreated wax oil, deasphalted oil, hydrorefined oil, hydrocracking tail oil, vacuum residue oil and atmospheric residue oil.

17. The method according to claim 1, wherein The first regeneration is performed using a fluidized bed coke drum for complete regeneration, and the second regeneration is performed using a riser reactor for regeneration.

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