CN107033952B

CN107033952B - Heavy oil processing method

Info

Publication number: CN107033952B
Application number: CN201610076818.0A
Authority: CN
Inventors: 许志明; 周嘉文; 孟祥海; 段爱军; 赵锁奇; 徐春明; 苑少军; 王栋; 吴青
Original assignee: China University of Petroleum Beijing; China National Offshore Oil Corp CNOOC; CNOOC Oil and Petrochemicals Co Ltd; CNOOC Huizhou Petrochemicals Co Ltd
Current assignee: China University of Petroleum Beijing; China National Offshore Oil Corp CNOOC; CNOOC Oil and Petrochemicals Co Ltd; CNOOC Huizhou Petrochemicals Co Ltd
Priority date: 2016-02-03
Filing date: 2016-02-03
Publication date: 2020-04-03
Anticipated expiration: 2036-02-03
Also published as: CN107033952A

Abstract

The invention relates to the field of petroleum refining and discloses a heavy oil processing method, which comprises the following steps: (1) carrying out reduced pressure distillation treatment on the heavy oil to obtain reduced pressure wax oil and reduced pressure residual oil; (2) carrying out solvent directional separation treatment on the vacuum residue to obtain light deasphalted oil, heavy deasphalted oil and deoiled asphalt; (3) subjecting the heavy deasphalted oil and the deoiled asphalt to delayed coking treatment; (4) subjecting a portion of the vacuum wax oil and a portion of the light deasphalted oil to a hydrocracking treatment; (5) and carrying out catalytic cracking treatment on the residual vacuum wax oil, the residual light deasphalted oil, the hydrocracking tail oil generated in the hydrocracking treatment process and the coking wax oil generated in the delayed coking treatment process. The method provided by the invention can improve the yield and quality of light oil and increase the added value of products.

Description

Heavy oil processing method

Technical Field

The invention relates to the field of petroleum refining, in particular to a heavy oil processing method.

Background

In recent years, as the yield of heavy crude oil is increased, the content of residual oil in crude oil is high and the content of light oil is low, and part of foreign high-sulfur crude oil is introduced, the lightening of residual oil becomes one of the main problems of petroleum processing in various countries in the world at present. Therefore, how to select a reasonable method to process heavy oil becomes an important strategic target for improving the economic benefit of the oil refinery.

Although the investment cost and the operation cost are low and the adaptability to crude oil is strong, the yield of light oil is low, the coke with low additional value is high, the quality of delayed coking products is poor, and particularly the coking products of sulfur-containing raw materials need secondary processing. The catalytic cracking of heavy oil is also an important method for processing vacuum residue, and the application of the method is mainly limited by the content of impurities in the raw oil, metals in the residue can be deposited on a catalyst to cause the permanent deactivation of the catalyst, and only part of the vacuum residue can be blended in the vacuum wax oil generally. If the property of the vacuum residue is poor or the blending ratio is improved, the vacuum residue needs to be subjected to hydrogenation pretreatment. Although the residual oil hydrogenation technology develops rapidly in recent years, the high investment and operation cost is the bottleneck limiting the development. In order to fully utilize precious heavy oil resources to produce more light oil products, refineries often adopt a heavy oil combined processing scheme.

CN1546613A discloses a combined process for heavy oil processing, which utilizes a combined process of fluidized decarbonization of heavy oil, hydrotreatment of residual oil and catalytic cracking of residual oil to produce light fuel oil from heavy oil, and organically combines decarbonization and hydrogenation. CN1844325A discloses a combined process for processing heavy oil, wherein heavy oil is subjected to solvent deasphalting treatment to obtain deasphalted oil and deasphalted asphalt after being used alone or mixed with catalytic cracking clarified oil; the deoiled asphalt is subjected to coking treatment independently or after being mixed with the other part of heavy oil, and the obtained coking heavy oil returns to a solvent deasphalting device or enters a heavy oil hydrotreating device, a catalytic cracking device and a hydrocracking device; the deasphalted oil is subjected to hydrotreating alone or after being mixed with one or more of vacuum wax oil, atmospheric residue oil, vacuum residue oil, catalytic cracking cycle oil and coking heavy oil, so that the feeding property of a heavy oil hydrotreating device is improved, and the operating conditions of the heavy oil hydrotreating device are alleviated. CN101050383A relates to a heavy oil processing combination process, vacuum residue is subjected to butane deasphalting treatment to obtain two components of deasphalted oil and deoiled hard asphalt; mixing deasphalted oil with one or more of other catalytic cracking raw materials of atmospheric residue and vacuum wax oil to be used as a raw material of a catalytic cracking device, and treating catalytic cracking slurry oil which is difficult to crack by a vacuum fractionation process to be divided into two components of light slurry oil and topped heavy slurry oil; mixing the light oil slurry with part of deoiled hard asphalt produced by a solvent deasphalting device to be used as a raw material of a visbreaking device to produce No. 7 commercial fuel oil; the topped heavy slurry oil and the other part of deoiled hard asphalt are fully mixed to produce the high-grade road petroleum asphalt. The related published patents also comprise CN101892074A, CN102234536A and CN102234529A, and the solvent deasphalting process, the catalytic cracking slurry topping process and the asphalt blending process are organically combined, so that the mutual supply and optimization of raw materials among the processes are realized, and the rationality, flexibility and overall economic benefit of heavy oil processing are improved. In the combined processing technology of heavy oil containing solvent deasphalting reported in literature, deasphalted oil is generally used as a raw material for catalytic cracking to be processed, the yield of light oil is not high enough, and the quality of catalytic cracking gasoline and diesel oil is poor, so that subsequent processing treatment is still needed.

Disclosure of Invention

The invention aims to overcome the defects of low light oil yield and poor quality of catalytic cracking gasoline and diesel oil in the heavy oil processing process in the prior art, and provides a heavy oil processing method.

In order to achieve the above object, the present invention provides a heavy oil processing method, wherein the method comprises the steps of:

(1) carrying out reduced pressure distillation treatment on the heavy oil to obtain reduced pressure wax oil and reduced pressure residual oil;

(2) carrying out solvent directional separation treatment on the vacuum residue to obtain light deasphalted oil, heavy deasphalted oil and deoiled asphalt;

(3) subjecting the heavy deasphalted oil and the deoiled asphalt to delayed coking treatment;

(4) subjecting a portion of the vacuum wax oil and a portion of the light deasphalted oil to a hydrocracking treatment;

(5) and carrying out catalytic cracking treatment on the residual vacuum wax oil, the residual light deasphalted oil, the hydrocracking tail oil generated in the hydrocracking treatment process and the coking wax oil generated in the delayed coking treatment process.

In the heavy oil processing method, the vacuum residue is subjected to solvent directional separation to obtain light deasphalted oil, heavy deasphalted oil and deoiled asphalt, the light deasphalted oil is far superior to the vacuum residue in property, the content of carbon residue is less than 6%, the content of Ni + V is less than 15 mu g/g, the content of carbon residue and metal is far lower than that of the vacuum residue, corresponding hydrocracking and catalytic cracking can be selected in a targeted manner for subsequent processing, the deep conversion of part of high-quality resources in the heavy oil is realized, the yield and quality of light oil are improved, and the additional value of products is increased.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic diagram of one embodiment of the process provided by the present invention.

Description of the reference numerals

1-a reduced pressure distillation device; 2-a solvent directional separation device; 3-a delayed coker; 4-a hydrocracking unit; 5-catalytic cracking unit.

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

The invention provides a heavy oil processing method, which comprises the following steps:

According to the present invention, in the step (1), the vacuum distillation treatment may be carried out in various conventional manners, for example, in a vacuum distillation column. The principle of the reduced pressure distillation treatment is as follows: according to the principle that the boiling point of oil product is reduced along with the reduction of system pressure, the method of reducing pressure of distillation tower is adopted to distill heavy distillate oil (vacuum wax oil) whose boiling point is 350-500 deg.C under normal pressure at lower temp. In the present invention, the conditions of the vacuum distillation treatment are not particularly limited.

According to the present invention, in the step (2), the solvent-directing separation process may be performed in various conventional manners, for example, in a solvent-directing separation apparatus. The principle of the solvent directional separation treatment is as follows: heating the vacuum residue obtained in the vacuum distillation treatment process, mixing the heated vacuum residue with a solvent from a solvent heating furnace according to a preset proportion, feeding the mixture into a first-stage extractor, separating the settled deoiled asphalt from deasphalted oil, and discharging the deasphalted asphalt from the bottom of the first-stage extractor; and the deasphalted oil enters a second-stage heating furnace from the top of the first-stage extractor, enters a second-stage separation tower after being heated to a preset temperature, heavy components in the deasphalted oil are further separated out from the solvent, and enter a buffer tank from the bottom of the second-stage separation tower in the form of heavy deasphalted oil, so that the solvent in the heavy deasphalted oil is recovered. And the light deasphalted oil led out from the top of the second-stage separation tower enters a solvent separator after pressure reduction, the solvent is heated and volatilized and returns to a solvent tank after cooling, and the light deasphalted oil is obtained from the bottom of the second-stage separation tower.

According to the present invention, the solvent in the process of the solvent-directed separation treatment may be a solvent used in a solvent-directed separation process conventional in the art, and preferably, the solvent is butane or a butane and pentane mixture. When the solvent is butane, the preferred conditions for the directional separation of the solvent include: the pressure is 3-6MPa, and the temperature is 90-130 ℃; when the solvent is a butane and pentane mixture, the conditions of the solvent directional separation treatment preferably comprise: the pressure is 3-6MPa, and the temperature is 110-170 ℃.

In the present invention, when the solvent is a mixture of butane and pentane, the amounts of the butane and the pentane to be used are not particularly limited.

In the present invention, there is no particular limitation on the selection of the butane and the pentane, the butane may be at least one of n-butane and isobutane, and the pentane may be at least one of n-pentane, isopentane and neopentane.

In the present invention, there is no particular limitation on the weight ratio of the solvent to the vacuum residue, so long as the solvent is used in an amount sufficient to separate the light deasphalted oil, the heavy deasphalted oil and the deoiled asphalt in the vacuum residue. Preferably, the weight ratio of the solvent to the vacuum residue is 1-10: 1, preferably 3 to 5: 1, more preferably 4 to 5: 1.

according to the present invention, in the step (3), the process of the delayed coking treatment may be carried out in various conventional manners, for example, may be carried out in a delayed coking unit. The main purpose of the delayed coking treatment is to convert the residual oil with high carbon residue value into light oil, and the device can be operated circularly, namely, the heavier fraction in the coking distillate oil of the heavy oil is used as circulating oil, and the residence time in the device is longer. In the present invention, the conditions of the vacuum distillation treatment are not particularly limited, but in order to obtain a high yield of light oil, the conditions of the delayed coking treatment preferably include: the reaction temperature is 440 ℃ and 510 ℃, the pressure is 0.15-0.4MPa, and the circulation ratio is 0.1-0.3.

According to the present invention, in the step (4), the hydrocracking treatment process may be carried out in various conventional manners, for example, may be carried out in a hydrocracking apparatus. Preferably, the hydrocracking treatment conditions include: the temperature is 390-420 ℃, the pressure is 9-14MPa, the volume ratio of hydrogen to oil is 800-1400, and the liquid hourly space velocity is 1-2.5h^-1(ii) a More preferably, the hydrocracking treatment conditions include: the temperature is 400-420 ℃, the pressure is 9-10MPa, the volume ratio of hydrogen to oil is 1000-1400, and the liquid hourly space velocity is 1-1.5h^-1. According to the present invention, the light deasphalted oil is used in an amount of 5 to 30 parts by weight, preferably 5 to 25 parts by weight, more preferably 10 to 25 parts by weight, and still more preferably 10 to 20 parts by weight, based on 100 parts by weight of the total of the partial vacuum wax oil and the partial light deasphalted oil in the hydrocracking treatment.

According to the present invention, in the step (5), the process of the catalytic cracking treatment may be carried out in various conventional manners, for example, may be carried out in a catalytic cracking unit. The catalytic cracking treatment refers to a process of converting heavy petroleum fractions into cracked gas, gasoline, diesel oil and the like through a cracking reaction under the action of a catalyst at a high temperature. Preferably, the conditions of the catalytic cracking treatment include: the temperature is 480 ℃ and 530 ℃, and the liquid hourly space velocity is 10-30h^-1The mass ratio of the agent to the oil is 4-8, and the mass ratio of the water to the oil is 0.04-0.12; more preferably, the conditions of the catalytic cracking treatment include: the temperature is 480 ℃ and 500 ℃, and the liquid hourly space velocity is 15-25h^-1The mass ratio of the agent to the oil is 5-7, and the mass ratio of the water to the oil is 0.08-0.1.

In the present invention, the catalyst used in the catalytic cracking treatment is not particularly limited and may be a catalyst conventionally used in the art. In the present invention, the amount of the catalyst is also not particularly limited as long as the catalyst can be used in an amount sufficient for catalytic cracking reaction. The feedstock comprises the remaining vacuum wax oil, the remaining light deasphalted oil, the hydrocracked tail oil and the coker wax oil of step (5).

According to the invention, the weight distribution ratio of the vacuum wax oil in the hydrocracking treatment process and the catalytic cracking treatment process is 1-7: 1, preferably 2 to 4: 1.

in the present invention, the heavy oil is at least one of atmospheric residue and vacuum residue, and is preferably atmospheric residue.

In the present invention, the pressure refers to an absolute pressure unless otherwise specified.

The present invention will be described in further detail below by way of specific examples.

The following examples were carried out using the embodiment shown in FIG. 1. The implementation mode is as follows: carrying out reduced pressure distillation treatment on the heavy oil through a reduced pressure distillation device 1 to obtain reduced pressure wax oil and reduced pressure residual oil; then the vacuum residue is subjected to solvent directional separation treatment by a solvent directional separation device 2 to obtain light deasphalted oil, heavy deasphalted oil and deoiled asphalt; carrying out delayed coking treatment on the heavy deasphalted oil and the deoiled asphalt through a delayed coking device 3 to obtain dry gas, liquefied gas, gasoline, diesel oil, coking wax oil and petroleum coke; performing hydrocracking treatment on part of the vacuum wax oil and part of the light deasphalted oil through a hydrocracking device 4 to obtain dry gas, liquefied gas, gasoline, diesel oil and hydrocracking tail oil; and carrying out catalytic cracking treatment on the residual vacuum wax oil, the residual light deasphalted oil, the hydrocracking tail oil generated in the hydrocracking process and the coking wax oil generated in the delayed coking process through a catalytic cracking device 5 to obtain dry gas, liquefied gas, gasoline, diesel oil and slurry oil.

For ease of understanding, the various components in the following examples are designated by letters, respectively, including: vacuum wax oil (VGO), vacuum residue oil (VR), light deasphalted oil (LDAO), heavy deasphalted oil (HDAO), deoiled asphalt (DOA).

The following examples and comparative examples were prepared by subjecting crude oils Penglai and Darlia, which were mainly processed by Heizhou oil refining company, Zhonghai petroleum, to a real-boiling-point distillation to obtain atmospheric residue oils, i.e., heavy oils, which are referred to as PZ and DZ, respectively. The true boiling point distillation data for both atmospheric residues are shown in table 1.

TABLE 1

Distillation range, deg.C	PZ，wt％	DZ，wt％
			Initial boiling point-500	42.67	44.59
Greater than 500	55.93	54.19
			Loss of power	1.40	1.22
Total up to	100	100

Example 1

This example is intended to illustrate a process for processing heavy oil using PZ as a raw material.

The PZ is subjected to reduced pressure distillation treatment by a reduced pressure distillation device 1 to obtain VGO₁And VR₁，VGO₁And VR₁The specific properties of (a) are shown in table 2;

using isobutane as solvent, adding 20 weight portions of VR₁And 80 parts by weight of isobutane, and carrying out solvent directional separation treatment by using a solvent directional separation device 2 under the conditions that the temperature is 90 ℃ and the pressure is 4MPa to obtain LDAO₁、HDAO₁And DAO₁，LDAO₁、HDAO₁And DAO₁The yield of (D) is as shown in Table 3, LDAO₁The properties of (A) are shown in Table 4;

HDAO₁And DAO₁Carrying out delayed coking treatment by a delayed coking device 3 under the conditions of 500 ℃ of temperature, 0.2MPa of pressure and 0.2 of circulation ratio to obtain dry gas, liquefied gas, gasoline, diesel oil, coking wax oil and petroleum coke;

90 parts by weight of VGO₁(VGO₁The weight distribution ratio in the hydrocracking treatment process and the catalytic cracking treatment process is 3.07: 1) and 10 parts by weight of LDAO₁At 400 ℃, 9MPa of pressure, 1000 of hydrogen-oil volume ratio and 1h of liquid hourly space velocity^-1Carrying out hydrocracking treatment by a hydrocracking device 4 under the condition of (1) to obtain dry gas, liquefied gas, gasoline, diesel oil and hydrocracking tail oil;

residual VGO₁Remaining LDAO₁Mixing the hydrocracking tail oil and the coking wax oil at 480 ℃ and a liquid hourly space velocity of 15h^-1The catalytic cracking treatment is carried out by a catalytic cracking device 5 under the conditions that the agent-oil mass ratio is 6 and the water-oil mass ratio is 0.08, so as to obtain dry gas, liquefied gas, gasoline, diesel oil and oil slurry.

The product distribution of example 1 is shown in table 5.

Example 2

Heavy oil was processed as in example 1, except that 80 parts by weight of VGO₁And 20 parts by weight of LDAO₁And carrying out hydrocracking treatment.

The product distribution of example 2 is shown in table 5.

Example 3

Heavy oil was processed as in example 1, except that 70 parts by weight of VGO₁And 30 parts by weight of LDAO₁And carrying out hydrocracking treatment.

The product distribution of example 3 is shown in table 5.

Example 4

Heavy oil was processed as in example 1, except that isobutane and n-pentane were used as solvents and the weight ratio of isobutane to n-pentane was 4: 1.

the product distribution of example 4 is shown in table 5.

Example 5

This example illustrates a heavy oil processing method using DZ as a feedstock.

The heavy oil was processed as in example 1. Except that DZ is used as the raw material. Obtaining VGO₂And VR₂，VGO₂And VR₂The specific properties of (a) are shown in table 2; to obtain LDAO₂、HDAO₂And DAO₂，LDAO₂、HDAO₂And DAO₂The yield of (D) is shown in Table 3, LDAO₂The properties of (A) are shown in Table 4;

the product distribution of example 5 is shown in table 6.

Example 6

This example illustrates a heavy oil processing method using DZ as a feedstock.

The heavy oil was processed as in example 5. What is needed isExcept that 80 parts by weight of VGO₂And 20 parts by weight of LDAO₂And carrying out hydrocracking treatment.

The product distribution of example 6 is shown in table 6.

Comparative example 1

This comparative example is illustrative of a heavy oil processing process using PZ as a feedstock.

The heavy oil was processed as in example 1. Except that VR₁The solvent directional separation treatment is not carried out, and the delayed coking treatment is directly carried out.

The product distribution of comparative example 1 is shown in table 5.

Comparative example 2

This comparative example is illustrative of a heavy oil processing process using DZ as a feedstock.

The heavy oil was processed as in example 6. Except that VR₂The solvent directional separation treatment is not carried out, and the delayed coking treatment is directly carried out.

The product distribution of comparative example 2 is shown in table 6.

TABLE 2

Parameter(s)	VGO₁	VR₁	VGO₂	VR₂
					Density (50 ℃ C.), g.cm^-3	0.906	1.022	0.917	0.962
Viscosity (100 ℃ C.), mm²·s^-1	9.39	1339.79	6.58	447.03
					Carbon residue in wt%	0.03	15.68	0.14	14.12
C，wt％	86.81	86.18	87.06	86.76
					H，wt％	12.29	11.10	12.13	11.23
S，wt％	0.27	0.50	0.40	0.82
					N，wt％	0.15	1.09	0.08	0.70
Saturated fraction, wt%	68.48	27.28	71.41	30.06
					The fragrance is in wt%	22.35	34.16	23.03	37.77
Gum, wt%	7.38	37.13	5.37	28.94
					Asphaltenes, wt.%	1.79	2.28	0.19	3.22

TABLE 3

Component name	Yield, wt.%
		LDAO₁	54.21
HDAO₁	3.17
		DAO₁	42.62
LDAO₂	65.62
		HDAO₂	4.17
DAO₂	30.21

TABLE 4

Parameter(s)	LDAO₁	LDAO₂
			Density (50 ℃ C.), g.cm^-3	0.917	0.940
Viscosity (100 ℃ C.), mm²·s^-1	68.16	71.87
			Carbon residue in wt%	4.11	4.23
Ni+V，μg/g	8.5	9.2
			C，wt％	86.42	86.62
H，wt％	11.84	11.68
			S，wt％	0.38	0.69
N，wt％	0.72	<0.3
			Saturated fraction, wt%	35.93	42.17
The fragrance is in wt%	39.96	40.01
			Gum, wt%	24.11	17.78
Asphaltenes, wt.%	0	0

TABLE 5

TABLE 6

Product, wt%	Example 5	Example 6	Comparative example 2
				Dry gas	3.16	2.93	5.94
Liquefied gas	11.69	10.65	9.06
				Gasoline (gasoline)	47.90	48.34	48.89
Diesel oil	22.40	24.28	19.33
				Oil slurry	2.88	2.63	1.58
Petroleum coke	8.36	8.36	14.22
				Coke	4.84	4.39	2.48
Light oil	70.30	72.62	68.22
				Liquid recovery	81.99	83.27	77.28
Light oil increment	2.09	4.40	—
				Liquid gain	4.72	5.99	—

As can be seen from the data in Table 4, VR in the method of the invention₁And VR₂LDAO obtained after directional separation treatment of solvent₁And LDAO₂The carbon residue value of less than 6 percent and the Ni + V content of less than 15 mu g/g.

As can be seen from the data in tables 5 and 6, the yield of light oil obtained by processing heavy oil according to the method of the present invention is significantly higher than that obtained by the conventional method, and the total liquid yield is also significantly increased, i.e., the added value of the product is increased.

The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.

It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. The invention is not described in detail in order to avoid unnecessary repetition.

In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.

Claims

1. A method of processing heavy oil, comprising the steps of:

(5) carrying out catalytic cracking treatment on the residual vacuum wax oil, the residual light deasphalted oil, the hydrocracking tail oil generated in the hydrocracking treatment process and the coking wax oil generated in the delayed coking treatment process;

wherein the weight distribution ratio of the vacuum wax oil in the hydrocracking treatment process and the catalytic cracking treatment process is 1-7: 1.

2. a heavy oil processing method according to claim 1, wherein the weight ratio of the solvent to the vacuum residue used during the solvent directional separation treatment is 1-10: 1.

3. a heavy oil processing method according to claim 2, wherein the weight ratio of the solvent to the vacuum residue used during the solvent directional separation treatment is 3-5: 1.

4. a heavy oil processing method according to any one of claims 1-3, wherein during the solvent directional separation treatment, the solvent is butane or a mixture of butane and pentane.

5. The heavy oil processing method of claim 4, wherein when the solvent is butane, the conditions of the solvent directional separation process comprise: the pressure is 3-6MPa, and the temperature is 90-130 ℃;

when the solvent is a butane and pentane mixture, the conditions of the solvent directional separation treatment comprise: the pressure is 3-6MPa, and the temperature is 110-170 ℃.

6. The heavy oil processing method of claim 1, wherein the conditions of the delayed coking process comprise: the reaction temperature is 440 ℃ and 510 ℃, the pressure is 0.15-0.4MPa, and the circulation ratio is 0.1-0.3.

7. The heavy oil processing method of claim 1, wherein the weight distribution ratio of the vacuum wax oil during the hydrocracking treatment and the catalytic cracking treatment is 2-4: 1.

8. the heavy oil processing method according to claim 1, wherein the light deasphalted oil is used in an amount of 5 to 30 parts by weight based on 100 parts by weight of the total amount of the vacuum wax oil and the light deasphalted oil used in the hydrocracking treatment.

9. The heavy oil processing method of claim 1, wherein the hydrocracking treatment conditions comprise: the temperature is 390-420 ℃, the pressure is 9-14MPa, the volume ratio of hydrogen to oil is 800-1400, and the liquid hourly space velocity is 1-2.5h^-1。

10. The heavy oil processing method of claim 9, the hydrocracking treatment conditions comprising: the temperature is 400-420 ℃, the pressure is 9-10MPa, the volume ratio of hydrogen to oil is 1000-1400, and the liquid hourly space velocity is 1-1.5h^-1。

11. The heavy oil processing method of claim 1, wherein the conditions of the catalytic cracking treatment comprise: the temperature is 480 ℃ and 530 ℃, and the liquid hourly space velocity is 10-30h^-1The mass ratio of the agent to the oil is 4-8, and the mass ratio of the water to the oil is 0.04-0.12.

12. The heavy oil processing method of claim 11, the conditions of the catalytic cracking treatment comprising: the temperature is 480 ℃ and 500 ℃, and the liquid hourly space velocity is 15-25h^-1The mass ratio of the agent to the oil is 5-7, and the mass ratio of the water to the oil is 0.08-0.1.

13. The heavy oil processing method of claim 1, wherein the heavy oil is at least one of atmospheric residue and vacuum residue.

14. A heavy oil processing method according to claim 13, wherein the heavy oil is an atmospheric residuum.