Process for processing crude oil in a non-hydroprocess, system for processing crude oil in a non-hydroprocess

Abstract

The present application relates to the technical field of petroleum refining, and discloses a method for processing crude oil in a non-hydrogen process and a system for processing crude oil in a non-hydrogen process. The method comprises the following steps: (1) sequentially performing heating treatment and electric desalting treatment on crude oil to obtain intermediate I; and (2) performing separation treatment on the intermediate I to obtain catalytic cracking raw material and / or catalytic cracking raw material. The content of sulfur in the crude oil is less than or equal to 1.2 wt%, the content of nitrogen is less than or equal to 0.30 wt%, and the content of vanadium is less than or equal to 20 mg / kg. The method provided by the present application can broaden the types of crude oil processing, reduce the cost of crude oil procurement, and greatly reduce the cost of crude oil processing. The system for processing crude oil in a non-hydrogen process provided by the present application has the advantages of low investment, small land occupation, simplicity, practicality, good production flexibility, large operation flexibility and low energy consumption.

Description

Technical Field

[0001] This invention relates to the field of petroleum refining technology, specifically to a method and system for processing crude oil using non-hydrogenation processes. Background Technology

[0002] The feedstocks processed by the catalytic cracking unit of the refinery are mostly hydrotreated feedstocks, mainly including hydrotreated heavy oil produced from the residue of the atmospheric and vacuum distillation unit after hydrotreating the residue, and refined wax oil produced from the heavy wax oil, coking wax oil, and solvent deasphalted oil produced from the heavy wax oil, coking wax oil, and solvent deasphalted oil produced from the wax oil after hydrotreating the heavy wax oil, coking wax oil, and solvent deasphalted oil produced from the heavy wax oil, coking wax oil, and solvent deasphalted oil produced from the heavy wax oil of the heavy wax oil and the wax oil produced from the heavy wax oil of the heavy wax oil. The remainder are mainly straight-run wax oil (such as atmospheric fourth-run wax oil and vacuum wax oil) and residue oil (including atmospheric residue oil or vacuum residue oil) produced from the heavy wax oil of the heavy wax oil and the vacuum distillation unit after processing low-sulfur crude oil (including low-sulfur paraffin-based crude oil and low-sulfur high-acid crude oil).

[0003] The feedstock for catalytic cracking is directly supplied by the traditional atmospheric and vacuum distillation unit. Suitable crude oil needs to be selected. The crude oil undergoes crude oil desalting and primary distillation tower to separate primary top naphtha. The primary bottom oil is heated by an atmospheric furnace and enters an atmospheric distillation tower for atmospheric distillation to separate atmospheric naphtha, aviation kerosene feedstock (Atmospheric Line 1), diesel fraction (Atmospheric Lines 2 and 3), heavy wax oil (Atmospheric Line 4), and atmospheric residue oil.

[0004] Multi-product solutions also require the use of a vacuum system. Atmospheric residue oil is heated by a vacuum furnace and enters a vacuum tower for vacuum distillation, separating vacuum wax oil (generally vacuum line 1, vacuum line 2, vacuum line 3, etc.) and vacuum residue oil.

[0005] The aforementioned non-hydrogen-dependent process for producing catalytic cracking feedstock has a long processing flow, high energy consumption, limited types of crude oil to be processed, and complex production operations. In particular, when processing high-acid crude oil, naphthenic acids are enriched in the 280-400℃ fraction, posing a risk of high-temperature naphthenic acid corrosion, leakage, and fire. This requires material upgrades and the addition of high-temperature corrosion inhibitors, increasing construction investment and operating costs.

[0006] With the rapid development of new energy products, the market demand for refined oil products has declined. Against the backdrop of the transformation and development of refining and chemical enterprises by reducing oil and chemical production, there is an urgent need for a new method for producing catalytic cracking or catalytic pyrolysis feedstocks through an ultra-short process without hydrogenation. This is of great significance for refining and chemical enterprises to broaden the types of crude oil they process, reduce crude oil processing costs, and save energy and reduce consumption. Summary of the Invention

[0007] The purpose of this invention is to overcome the problems of existing technologies, such as long processing flow, high energy consumption, limited types of crude oil processing, high crude oil procurement costs, and easy corrosion and leakage of crude oil processing equipment, which are common in non-hydrogen-dependent catalytic cracking or catalytic pyrolysis feedstock production.

[0008] To achieve the above objectives, a first aspect of the present invention provides a method for processing crude oil using a non-hydrogenation process, the method comprising:

[0009] (1) The crude oil was subjected to heat treatment and electro-desalting treatment in sequence to obtain intermediate I;

[0010] The heat treatment temperature is 130-180℃, and the heating time is 30-60s;

[0011] (2) The intermediate I is separated to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock;

[0012] The crude oil contains ≤1.2wt% sulfur, ≤0.30wt% nitrogen, and ≤20mg / kg vanadium.

[0013] A second aspect of the present invention provides a system for processing crude oil using a non-hydrogenation process, the system comprising: a crude oil storage unit, a crude oil transportation unit, a crude oil heating unit, a crude oil electrostatic desalting unit, and an oil separation unit;

[0014] The crude oil storage unit includes a crude oil storage tank; the bottom of the crude oil storage tank is provided with an inlet and an outlet; the inlet is used to introduce crude oil material.

[0015] The crude oil conveying unit includes a crude oil pump; the crude oil pump has an oil pump inlet and an oil pump outlet; the oil pump inlet is connected to the discharge port of the crude oil storage tank; the crude oil pump is used to convey crude oil from the crude oil storage tank to the crude oil heating unit.

[0016] The crude oil heating unit includes a crude oil heater; the inlet of the crude oil heater is connected to the oil pump outlet of the crude oil pump;

[0017] The crude oil desalting unit includes a crude oil desalting tank, the inlet of which is connected to the outlet of the crude oil heater.

[0018] The oil separation unit includes a primary distillation column, the inlet of which is connected to the outlet of the crude oil desalting tank.

[0019] Through the above technical solutions, the method and system for processing crude oil using non-hydrogenation processes provided by the present invention have the following advantages:

[0020] (1) The method provided by the present invention can broaden the types of crude oil processing, has strong adaptability to crude oil, and can reduce crude oil procurement costs;

[0021] (2) The non-hydrogen-dependent crude oil processing system provided by the present invention has low investment, small footprint, is simple and practical, has good production flexibility and high operational flexibility, can shorten the crude oil processing process, and significantly reduce crude oil processing costs and overall energy consumption.

[0022] (3) The non-hydrogen-dependent crude oil processing system provided by the present invention can avoid the risk of equipment pipeline corrosion, leakage and fire caused by processing high acid crude oil, which is conducive to safe production. Attached Figure Description

[0023] Figure 1 This is a system and process flow diagram of a non-hydrogen-dependent process for processing crude oil, provided by a specific embodiment of the present invention.

[0024] Explanation of reference numerals in the attached figures

[0025] 11. Crude oil storage tank 12. Crude oil pump

[0026] 13. Crude oil heater; 14. Crude oil electric desalting tank

[0027] 15. Primary distillation column 16. Top cooler

[0028] 17. Top reflux tank 18. Top reflux pump

[0029] 19. Aviation kerosene stripping tower; 20. Aviation kerosene transfer pump

[0030] 21. Initial oil pump Detailed Implementation

[0031] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0032] As previously stated, a first aspect of the present invention provides a method for processing crude oil using a non-hydrogenation process, the method comprising:

[0033] (1) The crude oil was subjected to heat treatment and electro-desalting treatment in sequence to obtain intermediate I;

[0034] The heat treatment temperature is 130-180℃, and the heating time is 30-60s;

[0035] (2) The intermediate I is separated to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock;

[0036] The crude oil contains ≤1.2wt% sulfur, ≤0.30wt% nitrogen, and ≤20mg / kg vanadium.

[0037] The present invention does not have special requirements for the conditions of the electro-desalting treatment. It is only necessary to ensure that the intermediate I after the electro-desalting treatment meets the requirements of the downstream production equipment. Those skilled in the art can make selections based on the conditions known in the art.

[0038] Preferably, in step (2), the separation process includes:

[0039] The overhead oil and gas at the top of the primary distillation column are condensed and cooled to obtain the liquid product as primary overhead naphtha.

[0040] Of which, 60wt%-70wt% of the primary top naphtha is refluxed to the top of the primary distillation column to control the top temperature of the primary distillation column, so that the final boiling point of the primary top naphtha is ≤175℃.

[0041] In a preferred embodiment, the conditions for the condensation cooling process include a temperature of 35-45°C.

[0042] In a preferred embodiment, in step (2), the separation process includes: extracting the jet fuel fraction from the side of the primary distillation column. The inventors of this invention have discovered that, in this preferred embodiment, good economic benefits can be achieved with lower energy consumption.

[0043] Preferably, the method further includes: after the separation treatment, pressurizing the initial bottom oil to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock;

[0044] The conditions for pressurization include: a temperature of 130-180℃ and a pressure of 0.8-1.5 MPa.

[0045] As mentioned above, a second aspect of the present invention provides a system for processing crude oil using a non-hydrogenation process, the system comprising: a crude oil storage unit, a crude oil transportation unit, a crude oil heating unit, a crude oil electrostatic desalting unit, and an oil separation unit;

[0046] The crude oil storage unit includes a crude oil storage tank 11; the bottom of the crude oil storage tank 11 is provided with an inlet and an outlet; the inlet is used to introduce crude oil material.

[0047] The crude oil conveying unit includes a crude oil pump 12; the crude oil pump 12 is provided with an oil pump inlet and an oil pump outlet; the oil pump inlet is connected to the discharge port of the crude oil storage tank 11; the crude oil pump 12 is used to convey the crude oil in the crude oil storage tank 11 to the crude oil heating unit;

[0048] The crude oil heating unit includes a crude oil heater 13; the inlet of the crude oil heater 13 is connected to the oil pump outlet of the crude oil pump 12;

[0049] The crude oil desalting unit includes a crude oil desalting tank 14, the inlet of which is connected to the outlet of the crude oil heater 13.

[0050] The oil separation unit includes a primary distillation column 15, the inlet of which is connected to the outlet of the crude oil electrostatic desalting tank 14.

[0051] In a preferred embodiment, the crude oil heater 13 is a steam heater or a crude oil heat exchanger.

[0052] The present invention does not have any particular requirements on the types of the steam heater and the crude oil heat exchanger, and those skilled in the art can make selections in conjunction with known technologies in the field.

[0053] It should be noted that there are no particular limitations on the types and quantities of equipment used in the crude oil electrostatic desalting unit in this invention. Those skilled in the art can select equipment based on known technologies in the field. For example, the crude oil electrostatic desalting unit may also be equipped with facilities for water injection, demulsifier injection, and decalcification agent injection, depending on the properties of the crude oil. These will not be described in detail here, and those skilled in the art should not construe this as a limitation of the invention.

[0054] Preferably, the crude oil electro-desalting unit contains 2-3 crude oil electro-desalting tanks 14 connected in series to achieve two-stage or three-stage electro-desalting of crude oil.

[0055] It should be noted that various control valves known to those skilled in the art can be installed in the circulation path of the non-hydrogen-exposed crude oil processing system of the present invention to control the flow of fluids such as crude oil, primary top naphtha, primary bottom oil, and jet fuel fraction.

[0056] It should be noted that all pressure vessels (e.g., primary distillation towers, crude oil desalting tanks) in the non-hydrogen-process crude oil processing system of the present invention can be equipped with independent vent valves, and can also be equipped with pressure gauges and temperature gauges to display the pressure and temperature inside the device.

[0057] In order to enable catalytic cracking feedstock or catalytic pyrolysis feedstock to flow into crude oil storage tanks as catalysts, the various devices in the apparatus of the present invention can be matched or set up to each other according to specific needs.

[0058] Preferably, the oil separation unit further includes a top cooler 16 and a top reflux tank 17; the top oil and gas at the top of the primary distillation column 15 is condensed and cooled by the top cooler 16 and then enters the top reflux tank 17 to obtain the liquid product, primary top naphtha.

[0059] Preferably, a nitrogen pressurization line is also provided at the top of the top reflux tank 17 to maintain the stability of the operating pressure of the top reflux tank 17.

[0060] In a preferred embodiment, the oil separation unit further includes a top reflux pump 18, which is used to transport the primary top naphtha, so that 60wt%-70wt% of the primary top naphtha is refluxed back to the top of the primary distillation column, and is used to control the top temperature of the primary distillation column so that the final boiling point of the primary top naphtha is ≯175℃, and 30wt%-40wt% of the primary top naphtha is sent out of the oil separation unit as a product.

[0061] Preferably, the oil separation unit further includes a jet fuel stripping tower 19, which is connected to the side of the primary distillation tower 15 for extracting jet fuel fraction from the side of the primary distillation tower 15.

[0062] In this invention, the jet fuel fraction refers to the fraction with a distillation range of 140-250℃.

[0063] In a preferred embodiment, the initial distillation column has 1-2 extraction ports on its side, and the number of trays between the extraction ports is 1-3. The inventors of this invention have discovered that, in this preferred embodiment, good economic benefits can be achieved with low energy consumption.

[0064] In a preferred embodiment, the oil separation unit further includes a jet fuel transfer pump 20, the inlet of which is connected to the outlet of the jet fuel stripping tower 19 to deliver jet fuel fraction.

[0065] Preferably, the oil separation unit further includes introducing stripping steam into the side of the jet fuel stripping tower 19, so that the stripping steam and the light components in the jet fuel enter the primary distillation tower through the oil-gas return line, thereby ensuring that the jet fuel meets the flash point requirements.

[0066] Preferably, the bottom of the primary distillation column 15 is provided with a primary bottom oil pump 21, which is used to pressurize the primary bottom oil to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock.

[0067] The method and system for processing crude oil using a non-hydrogenation process provided by the present invention will be described in detail below with reference to the accompanying drawings.

[0068] Figure 1 A system and process flow diagram for non-hydrogen-dependent crude oil processing according to a specific embodiment of the present invention are provided below:

[0069] from Figure 1 As can be seen from the above, the system for processing crude oil using the non-hydrogenation process includes a crude oil storage unit, a crude oil transportation unit, a crude oil heating unit, a crude oil electrostatic desalting unit, and an oil separation unit. The method for processing crude oil using the non-hydrogenation process is carried out in the above system and includes:

[0070] Crude oil from crude oil storage tank 11 is pumped by crude oil pump 12 to crude oil heater 13 for heating treatment, and then undergoes electro-desalting treatment in crude oil electro-desalting tank 14. The intermediate I obtained from electro-desalting is then separated by an oil separation unit. Specifically, the separation process includes: condensing and cooling the overhead oil and gas at the top of the primary distillation column 15 in the overhead cooler 16 (at a temperature of 40°C) before entering the overhead reflux tank 17 (a nitrogen pressurization line is located at the top of the overhead reflux tank 17 to maintain the stability of the operating pressure of the primary distillation column 15). The resulting liquid product is primary overhead naphtha, which is then pumped by overhead reflux pump 18 to ensure that the primary overhead naphtha is 60wt%-70wt% concentrated. Naphtha is refluxed to the top of the primary distillation column to control the top temperature of the column, ensuring that the final boiling point of the naphtha is ≤175℃. 30wt%-40wt% of the naphtha is sent out of the oil separation unit as a product. Aviation kerosene fraction is extracted from the side of the primary distillation column 15 via the aviation kerosene stripping column 19 (stripping steam (not shown in the figure) is introduced into the side of the aviation kerosene stripping column 19 so that the stripping steam and the light components in the aviation kerosene enter the primary distillation column 15 through the oil-gas return line (not shown in the figure) to ensure that the flash point of the aviation kerosene meets the requirements), and then transported out by the aviation kerosene transfer pump. The bottom oil is pressurized by the bottom oil pump 21 at the bottom of the primary distillation column 15 to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock.

[0071] The present invention will be described in detail below through examples.

[0072] In the following examples, unless otherwise specified, all raw materials used are either purchased or processed in-house.

[0073] Crude oil I: Sulfur content 0.9wt%, nitrogen content 0.3wt%, vanadium content 10mg / kg.

[0074] Crude Oil II: Sulfur content 1.2wt%, Nitrogen content 0.3wt%, Vanadium content 20mg / kg.

[0075] Crude Oil III: Sulfur content 1.2wt%, Nitrogen content 0.3wt%, Vanadium content 20mg / kg.

[0076] Unless otherwise specified, the following examples in this invention all adopt the following methods. Figure 1 The system shown is a non-hydrogen-dependent process for processing crude oil.

[0077] Example 1

[0078] The primary bottom oil obtained in this embodiment is directly used as a feedstock for catalytic cracking or catalytic pyrolysis.

[0079] The methods for processing crude oil using non-hydrogenation processes are as follows:

[0080] Crude oil from crude oil storage tank 11 is pumped by crude oil pump 12 to crude oil heater 13 for heating treatment, and then flows through crude oil electric desalting tank 14 (three crude oil electric desalting tanks are connected in series). Figure 1 (Not shown in the image) undergoes electro-desalting; the intermediate I obtained from the electro-desalting is then separated by an oil separation unit. Specifically, the separation process includes: condensing the overhead oil and gas from the top of the primary distillation column 15 via the overhead cooler 16 and then introducing it into the overhead reflux tank 17 (a nitrogen pressurization line is located at the top of the overhead reflux tank 17 to maintain the stability of the operating pressure of the primary distillation column 15). The resulting liquid product is primary overhead naphtha, which is then pumped by the overhead reflux pump 18 to remove 65 wt% of the primary overhead naphtha. Naphtha is refluxed to the top of the primary distillation column to control the top temperature of the column (approximately 85°C), ensuring that the final boiling point of the primary top naphtha is ≤175°C. 35 wt% of the primary top naphtha is sent out of the separation unit as product. Aviation kerosene fraction is extracted from the side of the primary distillation column 15 via the aviation kerosene stripping column 19, and then transported out via the aviation kerosene transfer pump. The primary bottom oil is pressurized by the primary bottom oil pump 21 at the bottom of the primary distillation column 15 to obtain catalytic cracking feedstock or catalytic pyrolysis feedstock. Specific parameters are shown in Table 1.

[0081] Example 2

[0082] In this embodiment, the primary bottom oil obtained from processing is mixed with the hydrotreated heavy oil from residue hydrotreating at a mass ratio of 1:1, and then used as feedstock for catalytic cracking or catalytic pyrolysis.

[0083] This embodiment follows a similar process to Embodiment 1. The difference is that the crude oil to be processed in this embodiment is crude oil II. All other parameters are the same as in Embodiment 1. Specific parameters are shown in Table 1.

[0084] Example 3

[0085] In this embodiment, the primary bottom oil obtained from processing and the refined wax oil obtained from the hydrogenation of wax oil are mixed at a mass ratio of 1:1 and used as feedstock for catalytic cracking or catalytic pyrolysis.

[0086] This embodiment follows a similar process to Embodiment 1. The difference is that the crude oil to be processed in this embodiment is crude oil III. All other parameters are the same as in Embodiment 1. Specific parameters are shown in Table 1.

[0087] Comparative Example 1

[0088] This comparative example uses a similar process to Example 1, except that the type of crude oil processed and the processing conditions are different, as shown in Table 1.

[0089] Table 1

[0090] Example 1 Example 2 Example 3 Comparative Example 1 crude type Crude Oil I Crude Oil II Crude Oil III Crude Oil II Mass flow rate, t / h 130 70 70 70 Heat treatment Temperature / °C 180 180 180 200 Time / second 30 30 30 30 Pressurization Temperature / °C 170 170 170 190 Pressure / MPa 1.0 1.0 1.0 1.0

[0091] The system operation results of the above embodiments and comparative examples are shown in Table 2.

[0092] Table 2

[0093] Example 1 Example 2 Example 3 Comparative Example 1 The amount of standard fuel oil consumed per ton of crude oil processed / kg 3.0 3.0 3.0 3.5 The quality of primary naphtha produced qualified qualified qualified Unqualified Quality of the produced jet fuel fraction qualified qualified qualified Unqualified

[0094] The results above show that the non-hydrogen-dependent crude oil processing method and system provided by this invention can broaden the types of crude oil that can be processed, have strong adaptability to crude oil (the content of sulfur in crude oil is ≤1.2wt%, the content of nitrogen is ≤0.30wt%, and the content of vanadium is ≤20mg / kg), and can significantly reduce crude oil processing costs and overall energy consumption.

[0095] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for processing crude oil using a non-hydrogenation process, characterized in that, The method includes: (1) The crude oil was subjected to heat treatment and electro-desalting treatment in sequence to obtain intermediate I; The heat treatment temperature is 130-180℃, and the heating time is 30-60s; (2) The intermediate I is separated to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock; The crude oil contains ≤1.2wt% sulfur, ≤0.30wt% nitrogen, and ≤20mg / kg vanadium.

2. The method according to claim 1, wherein, In step (2), the separation process includes: The overhead oil and gas at the top of the primary distillation column are condensed and cooled to obtain the liquid product as primary overhead naphtha. Of which, 60wt%-70wt% of the primary top naphtha is refluxed to the top of the primary distillation column to control the top temperature of the primary distillation column, so that the final boiling point of the primary top naphtha is ≤175℃.

3. The method according to claim 1 or 2, wherein, In step (2), the separation process includes: extracting jet fuel fraction from the side of the primary distillation tower.

4. The method according to claim 1 or 2, wherein, The method further includes: after the separation treatment, pressurizing the initial bottom oil to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock; The conditions for pressurization include: a temperature of 130-180℃ and a pressure of 0.8-1.5 MPa.

5. A system for processing crude oil using a non-hydrogenation process, characterized in that, The system includes: a crude oil storage unit, a crude oil transportation unit, a crude oil heating unit, a crude oil electrostatic desalting unit, and an oil separation unit; The crude oil storage unit includes a crude oil storage tank (11); the bottom of the crude oil storage tank (11) is provided with an inlet and an outlet; the inlet is used to introduce crude oil material; The crude oil conveying unit includes a crude oil pump (12); the crude oil pump (12) is provided with an oil pump inlet and an oil pump outlet; the oil pump inlet is connected to the discharge port of the crude oil storage tank (11); the crude oil pump (12) is used to convey the crude oil in the crude oil storage tank (11) to the crude oil heating unit; The crude oil heating unit includes a crude oil heater (13); the inlet of the crude oil heater (13) is connected to the oil pump outlet of the crude oil pump (12); The crude oil desalting unit includes a crude oil desalting tank (14), the inlet of which is connected to the outlet of the crude oil heater (13); The oil separation unit includes a primary distillation column (15), the inlet of which is connected to the outlet of the crude oil desalting tank (14).

6. The system according to claim 5, wherein, The oil separation unit also includes a top cooler (16) and a top reflux tank (17); the top oil and gas at the top of the primary distillation column (15) is condensed and cooled by the top cooler (16) and then enters the top reflux tank (17) to obtain the liquid product primary naphtha.

7. The system according to claim 6, wherein, The oil separation unit also includes a top reflux pump (18), which is used to transport the primary top naphtha, so that 60wt%-70wt% of the primary top naphtha is refluxed back to the top of the primary distillation column, and is used to control the top temperature of the primary distillation column so that the final boiling point of the primary top naphtha is ≯175℃, and 30wt%-40wt% of the primary top naphtha is sent out of the oil separation unit as a product.

8. The system according to any one of claims 5-7, wherein, The oil separation unit also includes a jet fuel stripping tower (19), which is connected to the side of the primary distillation tower (15) for extracting jet fuel fraction from the side of the primary distillation tower (15).

9. The system according to claim 8, wherein, The oil separation unit also includes a jet fuel transfer pump (20), the inlet of which is connected to the outlet of the jet fuel stripping tower (19) to deliver jet fuel fraction.

10. The system according to any one of claims 5-9, wherein, The bottom of the primary distillation column (15) is equipped with a primary bottom oil pump (21), which is used to pressurize the primary bottom oil to obtain catalytic cracking feedstock and / or catalytic pyrolysis feedstock.

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