Heavy oil efficient delay hydrocracking system and process method

Abstract

The invention relates to the technical field of petroleum processing, and particularly discloses a heavy oil efficient delayed hydrocracking system and process method.Raw oil, a retarder and hydrogen are mixed at the front end of an inlet of a heating furnace, heated and then driven by the hydrogen to rapidly flow into a delayed hydrocracking reactor; the retarder and hydrogen synergistically act to maintain stable properties in the material conveying process, and the hydrocracking reaction is concentrated in the reactor; and distilling the reaction product through a fractionating tower to obtain different fractions, and refluxing 85-90% of residual oil for retreatment. The retarder is introduced, a conventional hydrogen feeding mode is changed, hydrogen drives materials to rapidly flow, the retention time of the materials in a furnace tube and a pipeline is remarkably shortened, the retarder promotes hydrogen to be activated to form hydrogen free radicals, and the retarder and the hydrogen free radicals interact to maintain property stability of the materials in the transportation process; the hydrocracking reaction is carried out in a delayed hydrocracking reactor. Raw material loss is avoided, green coke of a reaction system is reduced, and long-period stable operation of the device is guaranteed.

Description

Technical Field

[0001] This invention relates to the field of petroleum processing technology, specifically to a high-efficiency delayed hydrocracking system and process for heavy oil. Background Technology

[0002] Petroleum, as a non-renewable resource, is a pillar of the world's energy system, but in recent years it has shown a trend towards lower quality and heavier composition in its supply. With increasingly stringent quality requirements for petroleum-related products and continuously updated environmental protection regulations and standards worldwide, the deep processing and conversion of heavy oil is urgently needed. Asphaltenes and gums, as inherent heavy components of petroleum, are highly susceptible to thermal condensation during processing, forming large molecular aggregates. This not only leads to raw material loss but also affects subsequent processing.

[0003] Currently, most hydrotreating processes use pipelines directly connected to the reactor for transporting hydrogen and catalyst, with the heater only heating the feedstock. The drawback of this feeding method is that the feedstock is prone to excessive cracking and free radical polymerization during heating, generating volatile gases and large molecular colloids and asphaltenes, leading to feedstock loss and pipeline blockage. Furthermore, both the catalyst and hydrogen require separate heating devices, increasing operating costs to some extent.

[0004] CN118440737A discloses a method for processing heavy oil, simultaneously improving the quality of feedstocks for ethylene cracking and catalytic reforming. CN118725901A invented an integrated hydrogenation method for crude oil to chemicals, achieving a conversion rate of over 85% from crude oil to chemicals. CN118580886A designed a suspended bed residue hydrogenation unit with a dual-pressure reduction tower mode, capable of switching the pressure reduction towers online. CN221319891U discloses a method for processing ethylene tar using suspended bed hydrogenation technology, achieving secondary conversion of ethylene tar while producing high-value-added petroleum products such as diesel. All of the above inventions employ a direct hydrogen injection method into the reactor, which leads to excessive cracking and free radical reactions of the feedstock before it enters the reactor, resulting in feedstock loss and coking in the transportation system, hindering efficient utilization of the feedstock. Summary of the Invention

[0005] Based on previous research and existing problems, this invention proposes a high-efficiency delayed hydrocracking system and process for heavy oil after further research and analysis.

[0006] To achieve the above objectives, the present invention provides the following technical solution: A high-efficiency delayed hydrocracking system for heavy oil includes a feedstock conveying unit, a delay agent conveying unit, a hydrogen conveying unit, a backflow preventer, a heater, a delayed hydrocracking reactor, and a fractionation tower. The raw material conveying unit conveys raw oil through pipeline No. 1, the delay agent conveying unit conveys delay agent through pipeline No. 2, and the hydrogen conveying unit conveys hydrogen through pipeline No. 3. The backflow preventer is connected in series with pipeline No. 3 to prevent feedstock oil and delay agent from flowing back into the hydrogen delivery unit; Pipeline No. 1, Pipeline No. 2, and Pipeline No. 3 converge at the front end of the heater inlet and connect to the mixing pipeline. The mixing pipeline is connected to the heater inlet. The heater outlet is connected to the delayed hydrocracking reactor inlet via a conveying pipeline. The delayed hydrocracking reactor outlet is connected to the fractionation tower inlet. A residue reflux pipeline is installed at the bottom of the fractionation tower and is connected to the delayed hydrocracking reactor inlet.

[0007] Preferably, the fractionation column can produce light, medium and heavy fractions through distillation. Light distillates are naphtha and / or liquefied petroleum gas, while medium distillates are kerosene and / or diesel. Heavy distillates are divided into wax oil and / or residue oil; The amount of residual oil refluxed in the residual oil reflux pipeline accounts for 85-90% of the total residual oil produced by the fractionation tower.

[0008] This invention also proposes a high-efficiency delayed hydrocracking process for heavy oil based on the aforementioned system, comprising the following steps: S1. The raw material oil, delay agent and hydrogen are transported to the mixing pipe at the front end of the heating furnace inlet through pipeline No. 1, pipeline No. 2 and pipeline No. 3 respectively to form a mixture. S2. The mixture enters the heating furnace for rapid heating, and after heating, it flows rapidly into the delayed hydrocracking reactor along the conveying pipeline under the drive of hydrogen. S3. The mixture undergoes hydrocracking in a delayed hydrocracking reactor to obtain delayed hydrocracking products; S4. The delayed hydrocracking products are fed into a fractionation tower for distillation and separation to obtain light, medium and heavy fractions. 85-90% of the residue oil is returned to the delayed hydrocracking reactor for further processing via a reflux line.

[0009] Preferably, in S1, the delay agent and hydrogen work synergistically in the mixing pipe. The delay agent is composed of an oxygen-containing organic compound and an active metal source in a molar ratio of 1:(0.1~0.4). The oxygen-containing organic compound is any one or a combination of several of isopropanol, n-butanol, cyclohexanol, benzyl alcohol, acetic acid, adipic acid, terephthalic acid, and citric acid. The active metal source is any one or a combination of several of molybdenum source and nickel source.

[0010] Preferably, the molybdenum source includes any one or more of molybdenum naphthenate, ammonium tetramolybdate, molybdenum acetylacetonate, and isopropyl molybdate. The nickel source includes any one or more of nickel naphthenate, nickel oleate, nickel octanoate, nickel acetylacetone, and nickel dithiocarbamate; The amount of the delay agent added is 10~1000μg / g, based on the concentration of the active metal.

[0011] Preferably, the volume ratio of hydrogen to the mixture in S1 is 100~1500 Nm³. 3 / m 3 In step S2, the outlet temperature of the heating furnace is controlled at 450℃, the material flow rate in the conveying pipeline is 2~8m / s, and the total residence time of the mixture in the heating furnace and conveying pipeline is ≤1.5min.

[0012] Preferably, the operating conditions of the delayed hydrocracking reactor in S3 are: hydrogen partial pressure 2~15 MPa, reaction temperature 420~450℃, and liquid hourly space velocity 0.1~3 h⁻¹. -1 .

[0013] Preferably, in S2, hydrogen gas drives the mixture to flow through the delivery pipeline in a turbulent state.

[0014] Preferably, the oxygen-containing organic matter in the delay agent is mixed with the active metal source to make the active metal source highly dispersed in the heavy oil, and at the same time, it acts as a second hydrogen donor to replenish the reaction system with active hydrogen.

[0015] Compared with existing technologies, this invention provides a high-efficiency delayed hydrocracking system and process for heavy oil, which has the following advantages: (1) This invention injects a delay agent and hydrogen at the front end of the furnace inlet in advance and works synergistically. Combined with the hydrogen, the material is driven to flow quickly through the furnace tube and conveying pipeline at a flow rate of 2~8m / s. This reduces the total residence time of the mixture in the conveying system to less than 1.5min, which greatly reduces the probability of excessive cracking reaction and free radical polymerization reaction of the material during the conveying process. It avoids the loss of raw materials caused by the generation of macromolecular colloids, asphaltene associative compounds or volatile gases, and ensures that the properties of the raw materials remain stable before entering the reactor.

[0016] (2) Turbulent flow greatly promotes the mixing and contact between oil, hydrogen and catalyst, making the system temperature distribution more uniform and preventing local overheating that leads to coking; at the same time, oxygen-containing organic matter in the delay agent can interact with hydrocarbon free radicals generated by the material when heated, further inhibiting coke formation, significantly reducing the frequency of equipment cleaning, and ensuring long-term stable operation of the unit.

[0017] (3) Hydrogen is pre-activated under the action of the delay agent and can be decomposed into hydrogen free radicals by the active metal group in the delay agent within a short residence time. The oxygen-containing organic components in the delay agent can not only achieve high dispersion of active metals in heavy oil, but also serve as a second hydrogen donor to supplement active hydrogen in the reaction system, ensuring timely annihilation of hydrocarbon free radicals generated by heating, and effectively inhibiting the generation of dry gas, liquefied gas and coke.

[0018] (4) Furthermore, the extremely short residence time means that petroleum molecules enter the reactor before completing the adsorption with the active metal components, resulting in a lack of necessary reaction conditions for the hydrocracking reaction. This ensures that the materials remain stable before entering the delayed hydrocracking reactor, avoiding feedstock loss. This creates a pure, efficient, and controllable starting point for subsequent catalytic reactions, thereby synergistically achieving multiple objectives such as inhibiting coking, delaying hydrocracking, and increasing light oil yield. The overall process has advantages such as simple operation, high feedstock utilization, ideal distribution of beneficial reactions, and stable long-term operation of the reaction unit. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the system structure for delayed hydrocracking of heavy oil proposed in this invention; Figure 2 This is a schematic diagram of a conventional suspended bed hydrogenation process. Figure 3 This is a schematic diagram of a conventional fixed-bed hydrogenation process. In the diagram, 1. Feedstock; 2. Delaying agent; 3. Hydrogen; 4. Backflow preventer; 5. Heater; 6. Heated mixture; 7. Delayed hydrocracking reactor; 8. Delayed hydrocracking products; 9. Fractionating column; 10. Light fraction; 11. Middle fraction; 12. Heavy fraction; 13. 85-90% reflux residue; 14. Catalyst; 15. Hydrogenation products; 16. Suspended bed reactor; 17. Fixed bed reactor. Detailed Implementation

[0020] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0021] As attached Figure 1 As shown, this embodiment proposes a high-efficiency delayed hydrocracking system for heavy oil, including a feedstock conveying unit, a delay agent conveying unit, a hydrogen conveying unit, a backflow preventer, a heater, a delayed hydrocracking reactor, and a fractionation tower; The raw material conveying unit conveys raw oil through pipeline No. 1, the delay agent conveying unit conveys delay agent through pipeline No. 2, and the hydrogen conveying unit conveys hydrogen through pipeline No. 3. The backflow preventer is connected in series with pipeline No. 3 to prevent feedstock oil and delay agent from flowing back into the hydrogen delivery unit; Pipeline No. 1, Pipeline No. 2, and Pipeline No. 3 converge at the front end of the heater inlet and connect to the mixing pipeline. The mixing pipeline is connected to the heater inlet. The heater outlet is connected to the delayed hydrocracking reactor inlet via a conveying pipeline. The delayed hydrocracking reactor outlet is connected to the fractionation tower inlet. A residue reflux pipeline is installed at the bottom of the fractionation tower and is connected to the delayed hydrocracking reactor inlet.

[0022] Specifically, the detailed process of the delayed hydrocracking method for heavy oil is described as follows: Feed oil 1 in pipeline 1, delay agent 2 in pipeline 2, and hydrogen 3 in pipeline 3 are mixed before the heater; hydrogen 3 drives the mixed feed to flow rapidly through the furnace tubes and transport pipelines, significantly reducing the residence time of the material in the transport system, so that the hydrocracking process takes place in the delayed hydrocracking reactor 7; the pre-injected hydrogen 3 can provide active hydrogen in the presence of delay agent 2, inhibiting the occurrence of free radical reactions and reducing coking; the delayed hydrocracking product 8 enters the fractionation tower 9 for distillation treatment to obtain light fractions (naphtha, LPG) 10, medium fractions (kerosene, diesel) 11, and heavy fractions (wax oil, residue oil) 12; 85-90% of the residue oil 13 is recycled back to the delayed hydrocracking reactor 7 for further processing.

[0023] The outlet temperature of the heating furnace is approximately 450℃; the volume ratio of hydrogen to material is 100~1500 Nm³. 3 / m 3 The flow velocity inside the furnace tube is 2~8 m / s, and the residence time of the mixture during transportation is shortened to less than 1.5 min; the operating conditions of the delayed hydrocracking reactor are: hydrogen partial pressure in the reactor is 2~15 MPa, reaction temperature is 420~450℃, and liquid hourly space velocity is 0.1~3 h⁻¹. -1 The amount of delay agent added is based on the concentration of the active metal, ranging from 10 to 1000 μg / g.

[0024] To make the above-mentioned objectives, features and advantages of the present invention more concise and understandable, the technical content and effects of the present invention will be further explained in detail below with reference to specific embodiments. Example 1

[0025] According to the method provided in this invention, delayed hydrocracking of Marie heavy oil was carried out. Delaying agent D-1 was prepared by selecting isopropanol and ammonium tetramolybdate at a molar ratio of 1:(0.1~0.4). The feedstock, the heated mixture, and the delayed hydrocracking products were evaluated. The evaluation results are shown in Table 1.

[0026] Table 1 Evaluation results of Marie heavy oil, heated mixtures and delayed hydrocracking products

[0027] As shown in Table 1, the delayed hydrocracking method provided by this invention ensures the stability of the Marie heavy oil during transportation. The density, viscosity, and sulfur and nitrogen content of the Marie heavy oil and the heated mixture are essentially the same, while their asphaltene contents are 7.34 wt% and 7.51 wt%, respectively, indicating that no free radical reaction leading to coking occurred during transportation. Furthermore, the yields of each fraction are very similar, within ±0.5 wt%, indicating that no hydrocracking reaction occurred. Conversely, the delayed hydrocracking product shows a significant decrease in density, viscosity, and sulfur and nitrogen content compared to the former, with an asphaltene content of only 3.41 wt%, indicating that the macromolecular aggregates were effectively disintegrated in the delayed hydrocracking reaction unit. Moreover, the yield of the <520℃ fraction increased by 33.07 wt%, and the yield of light oil was significantly improved, achieving the purpose of delayed hydrocracking. Example 2

[0028] According to the method provided in this invention, terephthalic acid and ammonium tetramolybdate were selected to prepare a delayed hydrocracking agent D-2 at a molar ratio of 1:(0.1~0.4). The delayed hydrocracking products were evaluated to demonstrate the rationality of the selection of the delayed agent raw materials. Example 3

[0029] According to the method provided in this invention, delayed hydrocracking of Marie heavy oil was carried out, and a delay agent D-3 was prepared by selecting isopropanol and nickel acetylacetone at a molar ratio of 1:(0.1~0.4). The delayed hydrocracking products were evaluated to prove the rationality of the selection of the delay agent raw materials. Example 4

[0030] According to the method provided in this invention, terephthalic acid and nickel acetylacetonate were selected to prepare a delayed hydrocracking agent D-4 at a molar ratio of 1:(0.1~0.4). The delayed hydrocracking products were evaluated to demonstrate the rationality of the selection of the delayed agent raw materials. Example 5

[0031] According to the method provided in this invention, delayed hydrocracking of Marie heavy oil was carried out. Isopropanol, terephthalic acid, ammonium tetramolybdate, and nickel acetylacetone were selected and prepared as a delay agent D-5 in a molar ratio of 1:(0.1~0.4). The delayed hydrocracking products were evaluated to demonstrate the rationality of the selection of the delay agent raw materials.

[0032] Tables 2 and 3 show the comparative effects of the delay agents made from different raw materials used in Examples 1, 2, 3, 4, and 5 of this invention on the delayed hydrocracking of Marie heavy oil.

[0033] Table 2 Comparison of properties of mixtures after heating under different delaying agents

[0034] Table 3 Comparison of properties of delayed hydrocracking products under different retarders

[0035] Comparative data from Tables 2 and 3 show that the different types of delaying agents prepared from various raw materials provided by this invention all exhibit excellent delayed hydrocracking effects on Marie heavy oil. The viscosity, density, elemental composition, and asphaltene content of each heated mixture remain essentially consistent. However, the properties of each delayed hydrocracking product are significantly reduced compared to the heated mixture, and the yield of the <520℃ fraction can reach over 80 wt%, an increase of over 30 wt% compared to the raw materials. This demonstrates the rationality of the raw material selection for the delaying agents provided by this method, which can effectively suppress free radical reactions and hydrocracking reactions during material transportation, maintain basic property stability, and ensure that the hydrocracking reaction proceeds within the reactor, achieving an ideal distribution of beneficial reactions.

[0036] Comparative Example 1 This comparative example uses a conventional suspended bed hydrogenation process, and the process flow diagram is shown below. Figure 2 As shown.

[0037] A. Heavy oil 1 from pipeline No. 1 enters heater 5 for heating; B. The heated feedstock oil 1 obtained in step A is mixed with the catalyst 14 transported by pipeline No. 2 and the hydrogen 3 transported by pipeline No. 3 to form the heated mixture 6. C. The heated mixture 6 obtained in step B is subjected to hydrogenation treatment in the slurry bed reactor 16; D. The hydrogenated product 15 obtained in step C is distilled in fractionation column 9. E. In step D, the fractionation tower 9 distills to obtain light fractions (naphtha, liquefied petroleum gas) 10, medium fractions (kerosene, diesel) 11 and heavy fractions (wax oil, residue oil) 12.

[0038] Comparative Example 2 This comparative example uses a conventional fixed-bed hydrogenation process, and the process flow is the same as that of Comparative Example 1.

[0039] A. Raw oil 1 from pipeline 1 enters heating furnace 5 for heating; B. The heated feedstock oil 1 obtained in step A is mixed with the catalyst 14 transported by pipeline No. 2 and the hydrogen 3 transported by pipeline No. 3 to form the heated mixture 6. C. The heated mixture 6 obtained in step B is subjected to hydrogenation treatment in a fixed-bed reactor 17; D. The hydrogenated product 15 obtained in step C is distilled in fractionation column 9. E. In step D, the fractionation tower 9 distills to obtain light fractions (naphtha, liquefied petroleum gas) 10, medium fractions (kerosene, diesel) 11 and heavy fractions (wax oil, residue oil) 12.

[0040] Relevant samples were taken for evaluation, and the results are shown in Table 4.

[0041] Table 4 Evaluation results of Marie heavy oil and mixtures after heating using different hydrotreating processes

[0042] Table 4 shows that the evaluation results of the heated mixtures from the two conventional hydrotreating processes differ significantly from those in Example 1. The yield of the <350℃ fraction increased significantly compared to the feedstock, indicating that the Marie heavy oil undergoes excessive cracking reaction in the heating furnace. In the slurry-bed hydrotreating process, the contents of asphaltenes and the >520℃ fraction increased by 1.91 wt% and 7.49 wt%, respectively; in the fixed-bed reaction process, the contents of asphaltenes and the >520℃ fraction increased by 3.18 wt% and 7.98 wt%, respectively, and both their densities and viscosities also increased. This indicates that the material transport process in conventional hydrotreating processes involves free radical reactions leading to association of heavy components, resulting in feedstock loss and coking, which is detrimental to subsequent processing.

[0043] Comparative Example 3 In this comparative example, the reflux flow rate of the residue oil was optimized. The Marie heavy oil was subjected to delayed hydrocracking treatment according to the method provided in this invention. The residue oil reflux flow rates of 80-85%, 85-90%, and 90-95% were set for reprocessing. Samples after hydrocracking with different reflux flow rates were taken for four-component evaluation. The results are shown in Table 5.

[0044] Table 5 Evaluation results of hydrogenation products from residue oil with different reflux rates

[0045] Table 5 shows that the asphaltene content of the products after rehydrogenation of residue oil varies significantly with different reflux rates, being 9.74 wt%, 8.85 wt%, and 13.23 wt%, respectively. The highest asphaltene content is observed at a reflux rate of 90–95%, indicating a relatively severe tendency for coking. When the residue oil reflux rate is 80–85% and 85–90%, the separation results of the four components are similar. Therefore, a higher residue oil reflux rate is selected for this method to improve the yield of light components and enhance economic benefits.

[0046] The above embodiments are only used to illustrate the technical solutions of the present invention, and are not intended to limit them. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. However, these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions claimed by the present invention.

Claims

1. A high-efficiency delayed hydrocracking system for heavy oil, characterized in that, It includes a raw material conveying unit, a delay agent conveying unit, a hydrogen conveying unit, a backflow preventer, a heater, a delayed hydrocracking reactor, and a fractionation tower; The raw material conveying unit conveys raw oil through pipeline No. 1, the delay agent conveying unit conveys delay agent through pipeline No. 2, and the hydrogen conveying unit conveys hydrogen through pipeline No.

3. The backflow preventer is connected in series with pipeline No. 3 to prevent feedstock oil and delay agent from flowing back into the hydrogen delivery unit; Pipeline No. 1, Pipeline No. 2, and Pipeline No. 3 converge at the front end of the heater inlet and connect to the mixing pipeline. The mixing pipeline is connected to the heater inlet. The heater outlet is connected to the delayed hydrocracking reactor inlet via a conveying pipeline. The delayed hydrocracking reactor outlet is connected to the fractionation tower inlet. A residue reflux pipeline is installed at the bottom of the fractionation tower and is connected to the delayed hydrocracking reactor inlet.

2. The high-efficiency delayed hydrocracking system for heavy oil according to claim 1, characterized in that, The fractionation column can produce light, medium and heavy fractions through distillation. Light distillates are naphtha and / or liquefied petroleum gas, while medium distillates are kerosene and / or diesel. Heavy distillates are divided into wax oil and / or residue oil; The amount of residual oil refluxed in the residual oil reflux pipeline accounts for 85-90% of the total residual oil produced by the fractionation tower.

3. A method for efficient delayed hydrocracking of heavy oil based on the system described in claim 1, characterized in that, Includes the following steps: S1. The raw material oil, delay agent and hydrogen are transported to the mixing pipe at the front end of the heating furnace inlet through pipeline No. 1, pipeline No. 2 and pipeline No. 3 respectively to form a mixture. S2. The mixture enters the heating furnace for rapid heating, and after heating, it flows rapidly into the delayed hydrocracking reactor along the conveying pipeline under the drive of hydrogen. S3. The mixture undergoes hydrocracking in a delayed hydrocracking reactor to obtain delayed hydrocracking products; S4. The delayed hydrocracking products are fed into a fractionation tower for distillation and separation to obtain light, medium and heavy fractions. 85-90% of the residue oil is returned to the delayed hydrocracking reactor for further processing via a reflux line.

4. The method for high-efficiency delayed hydrocracking of heavy oil according to claim 3, characterized in that, In S1, the delay agent and hydrogen work synergistically in the mixing pipe. The delay agent is composed of an oxygen-containing organic compound and an active metal source in a molar ratio of 1:(0.1~0.4). The oxygen-containing organic compound is any one or a combination of several of isopropanol, n-butanol, cyclohexanol, benzyl alcohol, acetic acid, adipic acid, terephthalic acid, and citric acid. The active metal source is any one or a combination of several of molybdenum source and nickel source.

5. The method for high-efficiency delayed hydrocracking of heavy oil according to claim 4, characterized in that, The molybdenum source includes any one or more of molybdenum naphthenate, ammonium tetramolybdate, molybdenum acetylacetonate, and isopropyl molybdate; The nickel source includes any one or more of nickel naphthenate, nickel oleate, nickel octanoate, nickel acetylacetone, and nickel dithiocarbamate; The amount of the delay agent added is 10~1000μg / g, based on the concentration of the active metal.

6. The method for high-efficiency delayed hydrocracking of heavy oil according to claim 3, characterized in that, The volume ratio of hydrogen to the mixture in S1 is 100~1500 Nm. 3 / m 3 In step S2, the outlet temperature of the heating furnace is controlled at 450℃, the material flow rate in the conveying pipeline is 2~8m / s, and the total residence time of the mixture in the heating furnace and conveying pipeline is ≤1.5min.

7. The method for high-efficiency delayed hydrocracking of heavy oil according to claim 3, characterized in that, The operating conditions for the delayed hydrocracking reactor in S3 are: hydrogen partial pressure 2~15 MPa, reaction temperature 420~450℃, and liquid hourly space velocity 0.1~3 h⁻¹. -1 .

8. The method for high-efficiency delayed hydrocracking of heavy oil according to claim 3, characterized in that, In S2, hydrogen gas drives the mixture to flow in a turbulent state through the delivery pipeline.

9. The method for efficient delayed hydrocracking of heavy oil according to claim 4, characterized in that, When the oxygen-containing organic matter in the delay agent is mixed with the active metal source, the active metal source is highly dispersed in the heavy oil, and at the same time, it acts as a second hydrogen donor to replenish the reaction system with active hydrogen.

Images