A method and system for treating heavy crude oil

Abstract

The present disclosure relates to a method and system for treating heavy crude oil, which includes: subjecting the crude oil, catalyst and hydrogen supply agent to hydrogenation reaction, separating the hydrogenation reaction product to obtain high-fraction oil; subjecting the high-fraction oil to stripping treatment, subjecting the obtained stripping tower bottom oil to atmospheric distillation to obtain the hydrogen supply agent after hydrogenation and the atmospheric tower bottom oil; subjecting the atmospheric tower bottom oil to vacuum distillation to obtain heavy oil products and unconverted oil containing catalyst; returning part of the unconverted oil to the slurry bed reactor for further reaction; subjecting the hydrogen supply agent and hydrogen to hydrogenation regeneration treatment to obtain regenerated hydrogen supply agent; returning part of the regenerated hydrogen supply agent to the slurry bed reactor for recycling. The method disclosed in the present disclosure can realize the recycling of hydrogen supply agent, catalyst and unconverted oil, improve the reaction conversion rate, and also enable the hydrogenation reaction to be carried out under safer conditions.

Description

Technical Field

[0001] The present disclosure relates to the field of petrochemical engineering, and in particular, to a method and system for processing heavy crude oil. Background Art

[0002] Today, as the whole society calls for sustainable development and green environmental protection, oil refining companies are facing the competitive pressure of rising crude oil prices, deteriorating crude oil properties, rising demand for light oil products, and stricter fuel and environmental standards. At present, there are four types of residue oil hydrogenation processes in the world, namely fixed bed, fluidized bed, moving bed and slurry bed residue oil hydrogenation. The advantage of slurry bed hydrogenation technology is that it can process the worst residue oil, even coal, but its reaction system pressure is high, chemical hydrogen consumption is higher than that of fixed bed, fluidized bed and moving bed, and equipment investment is high. Therefore, reducing the pressure of the reaction system is of vital importance to energy saving and consumption reduction of the entire device.

[0003] In the slurry bed residue oil hydrogenation, the reaction system is under high pressure and in the presence of hydrogen. The raw oil has poor properties and severe coking. In addition, due to the low molecular weight of hydrogen, it is easy to escape and leak, causing great safety risks. At the same time, the device is under high pressure conditions, the equipment investment is high, and the safety risk is high. These have brought great troubles to the stable, safe and long-term operation of the slurry bed residue oil hydrogenation device using the existing technology. Summary of the invention

[0004] The purpose of the present disclosure is to provide a method and system for processing heavy crude oil, so that a slurry bed reaction can be carried out under low pressure and non-hydrogen conditions.

[0005] In order to achieve the above-mentioned purpose, the first aspect of the present disclosure provides a method for treating heavy crude oil, which comprises: contacting the crude oil, a catalyst and a hydrogen donor in a slurry bed reactor for a hydrogenation reaction to obtain a hydrogenation reaction product; subjecting the hydrogenation reaction product to hot high-pressure separation and cold high-pressure separation to obtain a first gas phase and a high-fraction oil; subjecting the high-fraction oil to a stripping treatment to obtain a second gas phase and a stripper bottom oil; subjecting the stripper bottom oil to atmospheric distillation to obtain a third gas phase, a hydrogen donor after hydrogenation, a light oil product and atmospheric bottom oil; subjecting the atmospheric bottom oil to reduced pressure distillation to obtain a fourth gas phase, a heavy oil product and an unconverted oil containing a catalyst; returning part of the unconverted oil to the slurry bed reactor for further reaction; sending the hydrogen donor after hydrogenation and hydrogen to a hydrogen donor regeneration unit for hydrogenation regeneration treatment to obtain a regenerated hydrogen donor; returning part of the regenerated hydrogen donor to the slurry bed reactor for recycling, and sending another part of the regenerated hydrogen donor out of the system as a light fraction.

[0006] Optionally, the feedstock oil is selected from one or more of atmospheric residue oil, vacuum residue oil, vacuum wax oil, coker wax oil, deasphalted oil and coal tar; the hydrogen donor is selected from one or more of cyclohexane, methylcyclohexane, decahydronaphthalene and cyclohexadiene; and the catalyst is an oil-soluble organic homogeneous molybdenum-based catalyst and / or a supported nickel-molybdenum-based ultrafine powder catalyst.

[0007] Optionally, the reaction conditions of the hydrogenation reaction include: reaction temperature of 150-450° C., reaction pressure of 5-70 bar, reaction time of 0.5-10 h, and a mass ratio of hydrogen donor to feedstock oil of less than 2; preferably less than 1.

[0008] Optionally, the method further comprises, before entering the slurry bed reactor, increasing the pressure of the mixed raw material obtained by mixing the raw oil, the catalyst and the hydrogen donor to 0.5-7 MPa, exchanging heat with the hydrogenation reaction product, and then increasing the temperature to 150-450° C.;

[0009] Optionally, the stripping medium of the stripping treatment is water vapor.

[0010] Optionally, the temperature cut-off point between the third gas phase and the hydrogen supply agent after hydrogen supply is 40-80°C, the temperature cut-off point between the hydrogen supply agent after hydrogen supply and the light oil product is 130-160°C, and the temperature cut-off point between the light oil product and the atmospheric tower bottom oil is 300-360°C; the temperature cut-off point between the fourth gas phase and the heavy oil product is 300-360°C, and the temperature cut-off point between the heavy oil product and the unconverted oil is 480-540°C.

[0011] Optionally, the ratio of the part of the unconverted oil returned to the slurry bed reactor to the total weight of the unconverted oil is less than 1, preferably less than 0.8; the ratio of the part of the regenerated hydrogen supply agent returned to the slurry bed reactor to the total weight of the regenerated hydrogen supply agent is 0.2-1, preferably 0.8-1.

[0012] Optionally, the conditions of the hydrogenation regeneration treatment include: a reaction temperature of 150 to 250° C., a reaction pressure of 0.5 to 5 MPa, a reaction time of 0.1 to 1 h, and a volume ratio of the hydrogen gas to the hydrogen supply agent after hydrogen supply of 10 to 300:1.

[0013] The second aspect of the present disclosure provides a system for treating heavy crude oil, which includes a hydrogenation reaction unit, a high-pressure separation unit, a stripping unit, an atmospheric distillation unit, a vacuum distillation unit and a hydrogen supply agent regeneration unit; the hydrogenation reaction unit includes a slurry bed reactor, a crude oil inlet, a catalyst inlet, a hydrogen supply agent inlet and a hydrogenation reaction product outlet; the high-pressure separation unit includes a hydrogenation reaction product inlet, a first gas phase outlet and a high-fraction oil outlet; the stripping unit includes a high-fraction oil inlet, a stripping medium inlet, a second gas phase outlet and a stripping tower bottom oil outlet; the atmospheric distillation unit includes an atmospheric distillation tower; the atmospheric distillation tower includes a stripping tower bottom oil inlet, a third gas phase outlet, a hydrogen supply agent outlet after hydrogen supply, a light oil product outlet and an atmospheric tower bottom oil outlet; the vacuum distillation unit includes a vacuum distillation tower; the vacuum distillation tower includes an atmospheric tower bottom oil inlet, a fourth gas phase outlet, a heavy oil product outlet and an unconverted oil outlet; The hydrogen supplier regeneration unit comprises a hydrogenation reactor; the hydrogenation reactor comprises a hydrogen supplier inlet after hydrogenation, a hydrogen inlet and a regenerated hydrogen supplier outlet; wherein, the hydrogenation reaction product outlet of the hydrogenation reaction unit is connected with the hydrogenation reaction product inlet of the high-pressure separation unit through a hydrogenation reaction product pipeline; the high-fraction oil outlet of the high-pressure separation unit is connected with the high-fraction oil inlet of the stripping unit; the stripping tower bottom oil outlet of the stripping unit is connected with the stripping tower bottom oil inlet of the atmospheric distillation tower; the atmospheric tower bottom oil outlet of the atmospheric distillation tower is connected with the atmospheric tower bottom oil inlet of the vacuum distillation tower; the unconverted oil outlet of the vacuum distillation tower is connected with the raw oil inlet of the hydrogenation reaction unit; the hydrogen supplier outlet after hydrogenation of the atmospheric distillation tower is connected with the hydrogen supplier inlet after hydrogenation of the hydrogen supplier regeneration unit; the regenerated hydrogen supplier outlet of the hydrogen supplier regeneration unit is connected with the hydrogen supplier inlet of the hydrogenation reaction unit.

[0014] Optionally, according to the flow direction of the raw materials, the hydrogenation reaction unit further includes a feed pipeline, a feed pump, a feed heat exchanger and a reaction feed heating furnace which are connected in sequence; the feed pipeline is provided with the feed oil inlet, the catalyst inlet and the hydrogen supply agent inlet, the outlet of the feed pump is connected to the cold medium side inlet of the feed heat exchanger, the cold medium side outlet of the feed heat exchanger is connected to the inlet of the reaction feed heating furnace, and the outlet of the reaction feed heating furnace is connected to the raw material inlet of the slurry bed reactor;

[0015] Optionally, the hot medium side of the feed heat exchanger is connected to the hydrogenation reaction product pipeline.

[0016] Optionally, the unconverted oil outlet pipeline of the vacuum distillation tower is divided into two branches, one of which is connected to the feed oil inlet of the slurry bed reactor, and the other is sent out of the system; the regenerated hydrogen agent outlet pipeline of the hydrogen agent regeneration unit is divided into two branches, one of which is connected to the hydrogen agent inlet of the slurry bed reactor, and the other is sent out of the system.

[0017] Through the above technical scheme, the method disclosed in the present invention is adopted to perform hydrogenation regeneration treatment on the hydrogen supplying agent after hydrogen supply, and return part of the regenerated hydrogen supplying agent to the slurry bed reactor for further reaction, so as to realize the recycling of the hydrogen supplying agent; the unconverted oil containing the catalyst obtained by further separating the atmospheric tower bottom oil is returned to the slurry bed reactor, so as to realize the recycling of the catalyst and the unconverted oil, reduce the use amount of the catalyst, and improve the reaction conversion rate; the method disclosed in the present invention can reduce the consumption of the hydrogen supplying agent, and the product is easy to separate, and the hydrogenation operation pressure of the hydrogen supplying agent is low, so that the hydrogenation reaction can be carried out under safer conditions.

[0018] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0020] Figure 1 The present invention discloses a process flow chart of a method for treating heavy crude oil in an embodiment.

[0021] Description of Reference Numerals

[0022] P1, feed pump; E, feed heat exchanger; F1, reaction feed heating furnace; R1, slurry bed reactor; D1, cold / hot high pressure separator; T1, stripping tower; T2, atmospheric distillation tower; T3, vacuum distillation tower; F2, reaction feed heating furnace; R2, hydrogenation reactor; 1, crude oil; 2, hydrogen donor; 3, catalyst; 4, mixed material; 5, heat exchange mixed material; 6, preheated mixed material; 7, hydrogenation reaction product; 8, exchange Post-heat hydrogenation reaction product; 9. First gas phase; 10. High-fraction oil; 11. Second gas phase; 12. Stripping tower bottom oil; 13. Third gas phase; 14. Hydrogen; 15. Hydrogen donor after hydrogen supply; 16. Light oil product; 17. Pipeline; 18. External hydrogen donor; 19. Regenerated hydrogen donor; 20. Atmospheric tower bottom oil; 21. Fourth gas phase; 22. Heavy oil product; 23. Unconverted oil containing catalyst; 24. External unconverted oil containing catalyst. DETAILED DESCRIPTION

[0023] The specific implementation of the present disclosure is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described herein is only used to illustrate and explain the present disclosure, and is not used to limit the present disclosure.

[0024] The first aspect of the present disclosure provides a method for treating heavy crude oil, which comprises: contacting the crude oil, a catalyst and a hydrogenation agent in a slurry bed reactor for a hydrogenation reaction to obtain a hydrogenation reaction product; subjecting the hydrogenation reaction product to hot high-pressure separation and cold high-pressure separation to obtain a first gas phase and a high-fraction oil; subjecting the high-fraction oil to a stripping treatment to obtain a second gas phase and a stripping tower bottom oil; subjecting the stripping tower bottom oil to atmospheric distillation to obtain a third gas phase, a hydrogenation agent after hydrogenation, a light oil product and atmospheric tower bottom oil; subjecting the atmospheric tower bottom oil to reduced pressure distillation to obtain a fourth gas phase, a heavy oil product and an unconverted oil containing a catalyst; returning part of the unconverted oil to the slurry bed reactor for further reaction; sending the hydrogenation agent after hydrogenation and hydrogen to a hydrogenation agent regeneration unit for hydrogenation regeneration treatment to obtain a regenerated hydrogenation agent; returning part of the regenerated hydrogenation agent to the slurry bed reactor for recycling, and sending another part of the regenerated hydrogenation agent out of the system as a light fraction.

[0025] Through the above technical scheme, the method disclosed in the present invention is adopted to perform hydrogenation regeneration treatment on the hydrogen supply agent after hydrogen supply, and return part of the regenerated hydrogen supply agent to the slurry bed reactor for further reaction, so as to realize the recycling of the hydrogen supply agent; the unconverted oil containing the catalyst obtained by further separating the atmospheric tower bottom oil is returned to the slurry bed reactor, so as to realize the recycling of the catalyst and the unconverted oil, reduce the use of the catalyst, and improve the reaction conversion rate; the method disclosed in the present invention can reduce the consumption of the hydrogen supply agent, the product is easy to separate, the hydrogenation operation pressure of the hydrogen supply agent is low, and the hydrogenation reaction can be carried out under safer conditions.

[0026] In one embodiment, the method disclosed herein can process many heavy crude oils with high viscosity and many impurities. For example, the crude oil can be selected from one or more of atmospheric residue oil, vacuum residue oil, vacuum wax oil, coker wax oil, deasphalted oil and coal tar.

[0027] In one embodiment, the flow ratio of the regenerated hydrogen donor returning to the slurry bed reactor to the fresh hydrogen donor is 0.1 to 99:1.

[0028] In one embodiment, the hydrogen donor is selected from one or more of cyclohexane, methylcyclohexane, decahydronaphthalene and cyclohexadiene. In the above embodiment, the use of a hydrogen donor to replace hydrogen in the prior art can reduce the pressure during the hydrogen transfer reaction and further enhance the safety of the reaction. At the same time, the effect of the hydrogenation reaction is not much different from that of the reaction using hydrogen.

[0029] In one embodiment, the mass ratio of the hydrogen donor to the feedstock oil is less than 2, preferably less than 1, and more preferably 0.3 to 1. In this embodiment, the mass ratio of the hydrogen donor to the feedstock oil is controlled at a certain ratio, which can save the amount of hydrogen donor added while ensuring a good hydrogenation reaction effect, thereby further reducing costs.

[0030] In one embodiment, the catalyst is an oil-soluble organic homogeneous molybdenum catalyst and / or a supported nickel-molybdenum ultrafine powder catalyst. The oil-soluble organic homogeneous molybdenum catalyst can also be used as a reaction raw material for continuous reaction in a slurry bed reactor. In this embodiment, the catalyst can play a catalytic role, thereby making the reaction more complete, and therefore, the efficiency and completion of the hydrogenation reaction can be further improved.

[0031] In one embodiment, the reaction conditions of the hydrogenation reaction include: a reaction temperature of 150 to 450° C., a reaction pressure of 5 to 70 bar, and a reaction time of 0.5 to 10 h.

[0032] In this embodiment, in order to improve the reaction effect of the hydrogenation reaction, the conditions of the hydrogenation reaction and the amount of reactants are selected; by further optimizing the relevant reaction conditions, the effect of the hydrogenation reaction can be further improved.

[0033] In one embodiment, the method further comprises, before entering the slurry bed reactor, increasing the pressure of the mixed raw material obtained by mixing the raw oil, the catalyst and the hydrogen supply agent to 0.5-7 MPa, and then introducing it into the tube side of the feed heat exchanger, exchanging heat with the hydrogenation reaction product flowing through the shell side of the feed heat exchanger, and then heating it to 150-450° C. through the reaction feed heating furnace. In this embodiment, the mixed raw material can quickly reach the reaction temperature when entering the slurry bed reactor, and then react.

[0034] Optionally, the high-fraction oil separated from the hydrogenation reaction product is subjected to a stripping treatment; the stripping treatment is carried out in a stripping tower, and the stripping medium is water vapor.

[0035] In one embodiment, the hot high-pressure separation and the cold high-pressure separation are performed in a cold / hot high-pressure separator, and the first gas phase and the high-fraction oil are separated by flash evaporation.

[0036] In one embodiment, the atmospheric distillation is carried out in an atmospheric distillation tower, the temperature cut point between the third gas phase and the hydrogen donor after hydrogen supply is 40-80°C, the temperature cut point between the hydrogen donor after hydrogen supply and the light oil product is 130-160°C, and the temperature cut point between the light oil product and the atmospheric tower bottom oil is 300-360°C. The fraction range of the hydrogen donor after hydrogen supply obtained by atmospheric distillation is 40-195°C, preferably 45-75°C;

[0037] In one embodiment, the vacuum distillation is carried out in a vacuum distillation tower, the temperature cut point between the fourth gas phase and the heavy oil product is 300-360° C., and the temperature cut point between the heavy oil product and the unconverted oil is 480-540° C. The distillation range of the unconverted oil containing the catalyst is 400-1000° C., preferably 520-1000° C.

[0038] In the above embodiment, the first gas phase, the second gas phase, the third gas phase and the fourth gas phase are light hydrocarbons, wherein the first gas phase, the second gas phase, the third gas phase and the fourth gas phase are led out of the system.

[0039] In one embodiment, the ratio of the weight of the portion of unconverted oil returned to the slurry bed reactor to the total weight of the unconverted oil is less than 1, preferably less than 0.8.

[0040] In one embodiment, the weight ratio of the part of the regenerated hydrogen donor returned to the slurry bed reactor to the total weight of the regenerated hydrogen donor is 0.2-1, preferably 0.8-1.

[0041] In one embodiment, after the hydrogen supply agent to be generated is mixed with hydrogen, it is first heated by a reaction feed heating furnace and then enters a hydrogenation reactor for a hydrogenation regeneration reaction; the conditions of the hydrogenation regeneration reaction include: a reaction temperature of 150-250°C, preferably 180-220°C; a reaction pressure of 0.5-5MPa, preferably 2.5-3.5MPa; a reaction time of 0.1-1h, and a volume ratio of hydrogen to the hydrogen supply agent to be generated of 10-300:1.

[0042] The second aspect of the present disclosure provides a system for treating heavy crude oil, the system comprising a hydrogenation reaction unit, a high-pressure separation unit, a stripping unit, an atmospheric distillation unit, a vacuum distillation unit and a hydrogen supply agent regeneration unit; the hydrogenation reaction unit comprises a slurry bed reactor, a crude oil inlet, a catalyst inlet, a hydrogen supply agent inlet and a hydrogenation reaction product outlet; the high-pressure separation unit comprises a hydrogenation reaction product inlet, a first gas phase outlet and a high-separation oil outlet; the stripping unit comprises a high-separation oil inlet, a stripping medium inlet, a second gas phase outlet and a stripping tower bottom oil outlet; the atmospheric distillation unit comprises an atmospheric distillation tower; The atmospheric distillation tower comprises a stripping tower bottom oil inlet, a third gas phase outlet, a hydrogen supply agent outlet after hydrogen supply, a light oil product outlet and an atmospheric tower bottom oil outlet; the vacuum distillation unit comprises a vacuum distillation tower; the vacuum distillation tower comprises an atmospheric tower bottom oil inlet, a fourth gas phase outlet, a heavy oil product outlet and an unconverted oil outlet; the hydrogen supply agent regeneration unit comprises a hydrogenation reactor; the hydrogenation reactor comprises a hydrogen supply agent inlet after hydrogen supply, a hydrogen inlet and a regenerated hydrogen supply agent outlet; wherein the hydrogenation reaction product outlet of the hydrogenation reaction unit is connected to the hydrogenation reaction of the high-pressure separation unit through a hydrogenation reaction product pipeline. The product inlet is connected so that the hydrogenation reaction product produced by the hydrogenation reaction enters the high-pressure separation unit for separation; the high-fraction oil outlet of the high-pressure separation unit is connected with the high-fraction oil inlet of the stripping unit, so that the high-fraction oil obtained by the high-pressure separation unit enters the stripping unit for stripping treatment; the stripping tower bottom oil outlet of the stripping unit is connected with the stripping tower bottom oil inlet of the atmospheric distillation tower, so that the stripping tower bottom oil enters the atmospheric distillation tower for atmospheric distillation; the atmospheric distillation tower bottom oil outlet is connected with the atmospheric distillation tower bottom oil inlet of the vacuum distillation tower, so that the atmospheric distillation bottom oil obtained by atmospheric distillation The oil enters the vacuum distillation tower for vacuum distillation; the unconverted oil outlet of the vacuum distillation tower is connected with the feed oil inlet of the hydrogenation reaction unit, so that the unconverted oil in the vacuum distillation tower returns to the hydrogenation reaction unit for further reaction; the hydrogen supply agent outlet of the atmospheric distillation tower after hydrogen supply is connected with the hydrogen supply agent inlet of the hydrogen supply agent regeneration unit after hydrogen supply, so as to allow the hydrogen supply agent after hydrogen supply to enter the hydrogen supply agent regeneration unit for hydrogenation regeneration treatment; the regenerated hydrogen supply agent outlet of the hydrogen supply agent regeneration unit is connected with the hydrogen supply agent inlet of the hydrogenation reaction unit, so as to allow the regenerated hydrogen supply agent to return to the hydrogenation reaction unit for reaction.

[0043] In one embodiment, according to the flow direction of the raw materials, the hydrogenation reaction unit further includes a connected feed pipeline, a feed pump, a feed heat exchanger and a reaction feed heating furnace in sequence; the feed pipeline is provided with the raw oil inlet, the catalyst inlet and the hydrogen supply agent inlet, the outlet of the feed pump is connected to the cold medium side inlet of the feed heat exchanger, and is used to allow the mixed material to enter the heat exchanger for heat exchange; the cold medium side outlet of the feed heat exchanger is connected to the inlet of the reaction feed heating furnace, and is used to allow the mixed material after heat exchange to enter the reaction feed heating furnace for preheating; the outlet of the reaction feed heating furnace is connected to the raw material inlet of the slurry bed reactor, and is used to send the preheated mixed material into the slurry bed reactor for hydrogenation reaction.

[0044] Optionally, the heat medium side of the feed heat exchanger is connected to the hydrogenation reaction product pipeline, so as to allow the hydrogenation reaction product after the reaction to enter the feed heat exchanger for heat exchange with the mixed material.

[0045] In one embodiment, the unconverted oil outlet pipeline of the vacuum distillation tower is divided into two branches, one of which is connected to the feed oil inlet of the slurry bed reactor to return part of the unconverted oil to the slurry bed reactor for further reaction; and the other is sent out of the system;

[0046] In one embodiment, the regenerated hydrogen agent outlet pipeline of the hydrogen agent regeneration unit is divided into two branches, one of which is connected to the hydrogen agent inlet of the slurry bed reactor and is used to return the regenerated hydrogen agent to the slurry bed reactor to participate in the reaction; the other is sent out of the system.

[0047] In one embodiment, if Figure 1 As shown, the method for treating heavy crude oil includes:

[0048] The raw material oil 1, the hydrogen supply agent 2 and the catalyst 3 are mixed and pressurized by the feed pump P1, and then heated by the feed heat exchanger E and the reaction feed heating furnace F1, and then enter the slurry bed reactor R1 for hydrogenation reaction. The obtained hydrogenation reaction product 7 is heat-exchanged by the feed heat exchanger E, and then enters the cold / hot high-pressure separator D1 to separate the first gas phase 9 and the high-fraction oil 10. The high-fraction oil 10 enters the stripping tower T1, and the second gas phase 11 and the stripping tower bottom oil 12 are stripped out. The stripping tower bottom oil 12 is sent to the atmospheric distillation tower T2 to obtain the third gas phase 13, the hydrogen supply agent 15 after hydrogenation, the light oil product 16 and the atmospheric tower bottom oil 20. The atmospheric tower bottom oil 20 enters the vacuum distillation tower T3, and after further distillation, the fourth gas phase 21, the heavy oil product 22 and the unconverted oil 23 containing the catalyst oil are obtained. A part of the unconverted oil 23 containing the catalyst is returned to the inlet of the feed pump P1, and a part of the unconverted oil 24 containing the catalyst is thrown out of the sending device for further processing;

[0049] The hydrogen supply agent 15 after hydrogen supply is mixed with hydrogen 14 and heated by the reaction feed heating furnace F2 and then enters the hydrogenation reactor R2 for hydrogenation reaction. A part of the reaction product is thrown out of the hydrogen supply agent 18 as light distillate oil and sent out of the boundary area, and a part of the regenerated hydrogen supply agent 19 is returned to the inlet of the feed pump P1.

[0050] The embodiments of the present invention will be described in detail below in conjunction with the examples, but it will be appreciated by those skilled in the art that the following examples are only used to illustrate the present invention and should not be considered as limiting the scope of the present invention. If no specific conditions are specified in the examples, the conditions are carried out according to normal conditions or the conditions recommended by the manufacturer. If the manufacturer of the reagents or instruments used is not specified, they are all conventional products that can be obtained commercially.

[0051] The raw material oil used in the following examples and comparative examples is vacuum residue oil, and the specific parameters are shown in Table 1; the catalyst is an oil-soluble organic homogeneous molybdenum catalyst.

[0052] Table 1 Crude oil index

[0053] index Numeric <![CDATA[Density (20 °C) / (g / cm 3 )]]> 1073 Viscosity (20℃) / (mPa·s) 900 Sulfur wt% 3.6 Ni(ppm) 41 V(ppm) 108 Asphaltene wt% 11

[0054] Example 1

[0055] 100 t / h of crude oil 1, hydrogen donor 2 (cyclohexane, 100 t of charge at one time, 10 t / h of flow rate after stabilization) and oil-soluble organic homogeneous molybdenum catalyst 3 (20 t of charge at one time, 1.5 t / h of flow rate after stable operation) are mixed, and after being pressurized and heated to 70 bar and 425° C. by feed pump P1, feed heat exchanger E and reaction feed heating furnace F1, the mixture is fed into slurry bed reactor R1, and hydrogenation reaction is carried out at 425° C. and 7 MPa for 1 h; wherein the mass ratio of hydrogen donor to crude oil is 0.5:1; the hydrogenation reaction product 7 is heat exchanged by feed heat exchanger E, and then enters cold / hot high-pressure separator D1 to separate into first gas phase 9 and high-fraction oil 10, and high-fraction oil 10 enters stripping tower T1, and stripping out second gas phase 9 and high-fraction oil 10; The gas phase 11 and the stripping tower bottom oil 12 are sent to the atmospheric distillation tower T2 to obtain the third gas phase 13 (distillation range is 40-80°C), the hydrogen supply agent 15 after hydrogen supply (distillation range is 80-140°C), the light oil product 16 (distillation range is 140-350°C) and the atmospheric tower bottom oil 20 (distillation range is>350°C). The atmospheric tower bottom oil 20 enters the vacuum distillation tower T3, and is further distilled under a negative pressure of 7 mmHg to obtain the fourth gas phase 21 (distillation range is 40-120°C), the heavy oil product 22 (distillation range is 350-520°C) and the unconverted oil 23 containing catalyst oil (distillation range is>520°C). 95% by weight of the unconverted oil 23 containing catalyst is returned to the inlet of the feed pump P1, and the unconverted oil 24 containing catalyst is thrown out of the sending device for further treatment.

[0056] The hydrogen supply agent 15 after hydrogen supply is mixed with hydrogen 14 and heated by the reaction feed heating furnace F2 and then enters the hydrogenation reactor R2, and the hydrogenation reaction is carried out at 200°C and 2MPa for 0.5h. 40t / h of the regenerated hydrogen supply agent 19 in the reaction product is returned to the inlet of the feed pump P1, and the remaining hydrogen supply agent 18 is sent out of the boundary area as the external light distillate oil. The weight ratio of the regenerated hydrogen supply agent 19 to the external light distillate oil is 9:1.

[0057] Example 2

[0058] The method for treating heavy crude oil is the same as that in Example 1, except that the reaction conditions of the hydrogenation reaction include: a reaction temperature of 425° C., a reaction pressure of 70 bar, a reaction time of 1 h, and a mass ratio of the hydrogen donor to the crude oil of 0.3:1.

[0059] Example 3

[0060] The method for treating heavy crude oil is the same as that in Example 1, except that the reaction conditions of the hydrogenation reaction include: a reaction temperature of 425° C., a reaction pressure of 70 bar, a reaction time of 1 h, and a mass ratio of the hydrogen donor to the crude oil of 0.2:1.

[0061] Example 4

[0062] The method for treating heavy crude oil is the same as that in Example 1, except that the reaction conditions of the hydrogenation reaction include: a reaction temperature of 425° C., a reaction pressure of 70 bar, a reaction time of 1 h, and a mass ratio of the hydrogen donor to the crude oil of 0.1:1.

[0063] Comparative Example 1

[0064] The crude oil and catalyst are pressurized and heated respectively before mixing. The hydrogen is compressed by a new hydrogen compressor, heated by a hydrogen heating furnace, mixed with the crude oil and catalyst, and then enters the slurry bed reactor. The reaction pressure is 18MPag, the reaction temperature is 430°C, the hydrogen partial pressure is 11MPag, and the catalyst-to-oil ratio is 200ppm.

[0065] Table 2 Product properties of examples and comparative examples

[0066]

[0067] As shown in Table 2, by comparing the data in Examples 1 to 4 with Comparative Example 1, it can be seen that the method and system described in the present disclosure can improve the conversion rate of the reaction. By comparing the data in Examples 1 to 4, it can be seen that when the mass ratio of the hydrogen donor to the feedstock oil is preferably 0.3 to 1, the reaction effect is good.

[0068] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings; however, the present disclosure is not limited to the specific details in the above embodiments. Within the technical concept of the present disclosure, a variety of simple modifications can be made to the technical solution of the present disclosure, and these simple modifications all fall within the protection scope of the present disclosure.

[0069] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present disclosure will not further describe various possible combinations.

[0070] In addition, various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A method for treating heavy crude oil, characterized in that: The method includes: The feedstock oil, the catalyst and the hydrogen donor are contacted in a slurry bed reactor to carry out a hydrogenation reaction to obtain a hydrogenation reaction product; The hydrogenation reaction product is subjected to hot high-pressure separation and cold high-pressure separation to obtain a first gas phase and a high-fraction oil; subjecting the high-fraction oil to a stripping treatment to obtain a second gas phase and stripping tower bottom oil; The stripping tower bottom oil is subjected to atmospheric distillation to obtain a third gas phase, a hydrogen supply agent after hydrogen supply, a light oil product and atmospheric tower bottom oil; The atmospheric tower bottom oil is subjected to vacuum distillation to obtain a fourth gas phase, a heavy oil product, and unconverted oil containing a catalyst; and a portion of the unconverted oil is returned to the slurry bed reactor to continue the reaction; The hydrogen supply agent and hydrogen after hydrogen supply are sent to the hydrogen supply agent regeneration unit for hydrogenation regeneration treatment to obtain a regenerated hydrogen supply agent; part of the regenerated hydrogen supply agent is returned to the slurry bed reactor for recycling, and the other part of the regenerated hydrogen supply agent is sent out of the system as a light fraction; The reaction conditions of the hydrogenation reaction include: reaction temperature of 150-450°C, reaction pressure of 5-70 bar, reaction time of 0.5-10 h, and a mass ratio of hydrogen donor to feedstock oil of less than 2; The hydrogen donor is selected from one or more of cyclohexane, methylcyclohexane and cyclohexadiene.

2. The method according to claim 1, characterized in that The raw oil is selected from one or more of atmospheric residue oil, vacuum residue oil, vacuum wax oil, coker wax oil, deasphalted oil and coal tar; The catalyst is an oil-soluble organic homogeneous molybdenum catalyst and / or a supported nickel-molybdenum ultrafine powder catalyst.

3. The method according to claim 1, characterized in that The mass ratio of the hydrogen donor to the feedstock oil is 1 or less.

4. The method according to claim 1, characterized in that: The method further comprises, before entering the slurry bed reactor, increasing the pressure of the mixed raw material obtained by mixing the raw oil, the catalyst and the hydrogen donor to 0.5-7 MPa, exchanging heat with the hydrogenation reaction product, and then increasing the temperature to 150-450° C.; The stripping medium of the stripping treatment is water vapor.

5. The method according to claim 1, characterized in that The temperature cut-off point between the third gas phase and the hydrogen supply agent after hydrogen supply is 40-80°C, the temperature cut-off point between the hydrogen supply agent after hydrogen supply and the light oil product is 130-160°C, and the temperature cut-off point between the light oil product and the atmospheric tower bottom oil is 300-360°C; The temperature cut point between the fourth gas phase and the heavy oil product is 300-360°C, and the temperature cut point between the heavy oil product and the unconverted oil is 480-540°C.

6. The method according to claim 1, characterized in that The ratio of the weight of the part of the unconverted oil returned to the slurry bed reactor to the total weight of the unconverted oil is less than 1; The ratio of the total weight of the partially regenerated hydrogen supply agent returned to the slurry bed reactor to the total weight of the regenerated hydrogen supply agent is 0.2-1.

7. The method according to claim 6, characterized in that The ratio of the part of the unconverted oil returned to the slurry bed reactor to the total weight of the unconverted oil is less than 0.8; The ratio of the total weight of the partially regenerated hydrogen supply agent returned to the slurry bed reactor to the total weight of the regenerated hydrogen supply agent is 0.8-1.

8. The method according to claim 1, characterized in that The conditions of the hydrogenation regeneration treatment include: a reaction temperature of 150-250° C., a reaction pressure of 0.5-5 MPa, a reaction time of 0.1-1 h, and a volume ratio of the hydrogen gas to the hydrogen supply agent after hydrogen supply of 10-300:

1.

9. A system for treating heavy crude oil using the method according to any one of claims 1 to 8, characterized in that: The system includes a hydrogenation reaction unit, a high-pressure separation unit, a stripping unit, a normal-pressure distillation unit, a vacuum distillation unit and a hydrogen supply agent regeneration unit; The hydrogenation reaction unit comprises a slurry bed reactor, a feedstock oil inlet, a catalyst inlet, a hydrogen supply agent inlet and a hydrogenation reaction product outlet; The high-pressure separation unit comprises a hydrogenation reaction product inlet, a first gas phase outlet and a high-pressure oil separation outlet; The stripping unit comprises a high-fraction oil inlet, a stripping medium inlet, a second gas phase outlet and a stripping tower bottom oil outlet; The atmospheric distillation unit comprises an atmospheric distillation tower; the atmospheric distillation tower comprises a stripping tower bottom oil inlet, a third gas phase outlet, a hydrogen supply agent outlet after hydrogen supply, a light oil product outlet and an atmospheric tower bottom oil outlet; The vacuum distillation unit comprises a vacuum distillation tower; the vacuum distillation tower comprises an atmospheric tower bottom oil inlet, a fourth gas phase outlet, a heavy oil product outlet and an unconverted oil outlet; The hydrogen supply agent regeneration unit comprises a hydrogenation reactor; the hydrogenation reactor comprises a hydrogen supply agent inlet after hydrogen supply, a hydrogen gas inlet and a regenerated hydrogen supply agent outlet; Wherein, the hydrogenation reaction product outlet of the hydrogenation reaction unit is connected with the hydrogenation reaction product inlet of the high-pressure separation unit through the hydrogenation reaction product pipeline; the high-fraction oil outlet of the high-pressure separation unit is connected with the high-fraction oil inlet of the stripping unit; the stripping tower bottom oil outlet of the stripping unit is connected with the stripping tower bottom oil inlet of the atmospheric distillation tower; the atmospheric tower bottom oil outlet of the atmospheric distillation tower is connected with the atmospheric tower bottom oil inlet of the vacuum distillation tower; the unconverted oil outlet of the vacuum distillation tower is connected with the feed oil inlet of the hydrogenation reaction unit; the hydrogen supply agent outlet after hydrogen supply of the atmospheric distillation tower is connected with the hydrogen supply agent inlet after hydrogen supply of the hydrogen supply agent regeneration unit; the regenerated hydrogen supply agent outlet of the hydrogen supply agent regeneration unit is connected with the hydrogen supply agent inlet of the hydrogenation reaction unit.

10. The system according to claim 9, characterized in that According to the flow direction of the raw materials, the hydrogenation reaction unit also includes a feed pipeline, a feed pump, a feed heat exchanger and a reaction feed heating furnace connected in sequence; The feed pipeline is provided with the feed oil inlet, the catalyst inlet and the hydrogen supply agent inlet, the feed pump outlet is connected to the cold medium side inlet of the feed heat exchanger, the cold medium side outlet of the feed heat exchanger is connected to the inlet of the reaction feed heating furnace, and the outlet of the reaction feed heating furnace is connected to the raw material inlet of the slurry bed reactor; The heat medium side of the feed heat exchanger is in communication with the hydrogenation reaction product pipeline.

11. The system according to claim 9, characterized in that The unconverted oil outlet pipeline of the vacuum distillation tower is divided into two branches, one of which is connected to the feed oil inlet of the slurry bed reactor, and the other is sent out of the system; The regenerated hydrogen supply agent outlet pipeline of the hydrogen supply agent regeneration unit is divided into two branches, one of which is connected to the hydrogen supply agent inlet of the slurry bed reactor, and the other is sent out of the system.

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