A method for producing marine fuel oil by hydrogenation

Abstract

The present invention discloses a method for producing marine fuel oil by hydrogenation. The method comprises: mixing a relatively good residual oil raw material with the effluent of the upflow hydrogenation reactor in step (2) and hydrogen into a fixed bed hydrogenation unit for a first hydrogenation refining reaction to obtain a hydrogenated product oil; the hydrogenated product oil is subjected to atmospheric fractionation to obtain a hydrogenated atmospheric residue oil; part of the hydrogenated atmospheric residue oil is subjected to vacuum fractionation to obtain a hydrogenated vacuum residue oil and a hydrogenated vacuum wax oil; part of the hydrogenated vacuum residue oil obtained in step (1) is mixed with a relatively poor residual oil raw material and hydrogen and is subjected to a second hydrogenation refining reaction to obtain an upflow hydrogenation reactor effluent; part of the hydrogenated atmospheric residue oil obtained in step (1) and part of the hydrogenated vacuum residue oil obtained in step (2) are mixed with at least part of the hydrogenated vacuum wax oil to obtain a marine fuel oil product. The method processes inferior residual oil raw materials and can improve the comprehensive performance of the produced marine fuel oil.

Description

Technical Field

[0001] The invention relates to a process for producing clean fuel oil from inferior residual oil, in particular to a process for producing low-sulfur marine fuel oil from inferior high-sulfur residual oil as raw material. Background Art

[0002] As global environmental regulations become increasingly stringent, clean low-sulfur marine fuel oil will become one of the key oil products in the next few years after clean gasoline and diesel and other light oil products are upgraded. The International Maritime Organization (IMO) "International Convention for the Prevention of Pollution from Ships" stipulates that from January 2020, the sulfur mass fraction of marine fuel oil used for navigation in general areas at sea will be reduced from the current no more than 3.5% to no more than 0.5%; when sailing in emission control areas, the sulfur content of marine fuel oil should not exceed 0.1%. In the marine fuel oil demand market, high-sulfur residual marine fuel oil accounts for about 70% of the entire market with its price advantage, distillate marine fuel oil accounts for about 25%, and the rest is low-sulfur fuel oil (sulfur mass fraction less than 3.5%) and a small amount of liquefied natural gas. Therefore, the new environmental regulations will have a significant impact on the marine fuel oil market, which is currently dominated by high-sulfur fuel oil, and will also promote the further development of marine fuel oil desulfurization technology.

[0003] At present, the main ways to produce residual marine fuel oil with a sulfur content of no more than 0.5% include: using low-sulfur straight-run residual oil for blending production. However, due to the limited resources and high prices of low-sulfur crude oil, the production cost of residual marine fuel oil will be greatly increased, and this route is not suitable for producing residual marine fuel oil with low value; it is feasible to produce low-sulfur residual marine fuel oil by hydrodesulfurization of high-sulfur residual oil, but for residual oil with a sulfur content of more than 2.0% or even 3.0%, directly desulfurizing the residual oil to directly produce residual marine fuel oil with a sulfur content of less than 0.5% has high processing costs, high hydrogenation severity, high operating costs, and poor economic efficiency.

[0004] The main purpose of the residue oil hydrotreating process is to significantly reduce the impurity content in the residue oil raw material through hydrotreating, hydrogenate and transform non-ideal components such as polycyclic aromatic hydrocarbons, resins, asphaltene, etc., reduce the viscosity, and significantly improve its physical properties.

[0005] In the existing fixed-bed hydrogenation technology, the raw materials undergo decontamination reactions such as hydrodesulfurization under the action of hydrogen and residue oil hydrogenation catalysts, and the product index requirements can be achieved under high temperature and high harsh conditions. Residue oil hydrogenation catalysts are usually loaded in a graded manner, including protective agents, demetallization catalysts, desulfurization catalysts and high-activity denitrification and decarbonization catalysts. Along the direction of liquid phase logistics, the reaction temperature gradually increases. The disadvantage of this route is that the hydrogenation process has high hydrogen consumption and large hydrogenation volume. Usually, when the sulfur content meets the index, a higher reaction severity is required. Under high temperature and high pressure conditions, the sulfur content meets the index requirements, and other indicators such as carbon residue are greatly reduced, the conversion rate is improved, and the processing cost is high. In addition, the adaptability to crude oil is poor, and the problem of poor adaptability of raw materials for fixed bed hydrogenation treatment has not been solved. At the same time, the device has a short operating cycle for processing inferior vacuum residue oil and poor economic efficiency.

[0006] CN107001959A discloses a low-sulfur marine fuel composition and a preparation method thereof. The method comprises: hydrotreating a vacuum residue feed stream with hydrogen in the presence of a hydrotreating catalyst to reduce sulfur to no more than 1500 parts per million (wppm) without substantially cracking the vacuum residue; blending the hydrotreated vacuum residue with no more than 10% by volume of a first diesel boiling range hydrocarbon stream and no more than 40% by volume of a second diesel boiling range hydrocarbon stream to form the low-sulfur marine fuel composition, wherein the hydrotreated vacuum residue accounts for at least 60% by volume of the low-sulfur marine fuel composition, wherein the vacuum residue feed stream has 1000 wppm to 10000 wppm of sulfur, the first diesel boiling range hydrocarbon stream has no more than 20 wppm of sulfur, and the second diesel boiling range hydrocarbon stream has no more than 10 wppm of sulfur. This method requires the use of conventional residue oil hydrogenation technology to reduce the sulfur in the residue oil feedstock to below 1500wppm. However, since the addition of a large proportion of diesel and other fractions significantly increases the production cost, it still cannot overcome the problems of short production cycle, increased difficulty in product blending, complex process and poor economy in processing inferior vacuum residue oil feedstock by conventional residue oil hydrogenation technology. Summary of the invention

[0007] In view of the shortcomings of the prior art, the present invention provides a method for producing marine fuel oil by hydrogenation. The method can process low-quality vacuum residue raw materials, can meet the index requirements of product sulfur content, viscosity, etc., can control the depth of hydrogenation and reduce processing costs, and at the same time, the hydrogenated product is used as low-sulfur marine fuel oil, and its peptization system is stable.

[0008] The inventor has found through research that when the fixed bed residue oil hydrogenation technology is used to process low-quality residue oil raw materials to produce low-sulfur marine fuel oil, relatively harsh reaction conditions are usually required. In addition to the economic problem, under such reaction conditions, the conversion rate is greatly improved, which will cause excessive hydrogenation of light components and a large amount of colloids to be saturated with hydrogenation, which is easy to destroy the stability of the oil peptization system. On the one hand, it is not conducive to the stable operation of the device. On the other hand, the produced marine fuel oil, on the surface, meets the requirements of various indicators, but there will also be a problem of reduced oil stability, which has an adverse effect on the blending, storage and use of low-sulfur marine fuel oil. The inventor has also found through research that when facing the processing of residue oil raw materials of different properties to produce low-sulfur marine fuel oil products, if the relatively inferior residue oil raw materials and the relatively high-quality residue oil raw materials are put into the fixed bed residue oil hydrogenation device together, because the inferior raw materials require a higher reaction severity, it will not only affect the performance and service life of the catalyst, but also affect the product properties. Under the condition of high reaction severity and meeting the key product indicators such as sulfur and viscosity, the residual carbon is greatly reduced, which increases the processing cost and affects the product performance. More importantly, the fixed bed reactor is prone to cause a rapid increase in pressure drop, which affects the overall economic benefits. The method of the present invention introduces two residual oil raw materials with different properties through different feed ports, and by optimizing the hydrogenation process route, it can not only process inferior residual oil raw materials, but also improve the comprehensive performance of the produced marine fuel oil, and has good economic and social benefits.

[0009] The present invention provides a method for producing marine fuel oil by hydrogenation, comprising:

[0010] (1) mixing a relatively good residual oil feedstock with the effluent of the upflow hydrogenation reactor obtained in step (2) and hydrogen into a fixed bed hydrogenation unit for a first hydrofining reaction to obtain a hydrogenated product oil; the hydrogenated product oil is first subjected to atmospheric distillation to obtain a hydrogenated atmospheric residue oil; and a portion of the hydrogenated atmospheric residue oil is further subjected to vacuum distillation to obtain a hydrogenated vacuum residue oil and a hydrogenated vacuum wax oil;

[0011] (2) the partially hydrogenated vacuum residue obtained in step (1) is mixed with a relatively inferior residue feedstock and hydrogen and fed into an upflow hydrogenation reactor for a second hydrofining reaction to obtain an effluent from the upflow hydrogenation reactor;

[0012] (3) The partially hydrogenated atmospheric residue obtained in step (1) and the partially hydrogenated vacuum residue obtained in step (2) are mixed with at least a portion of the hydrogenated vacuum wax oil to obtain a marine fuel oil product.

[0013] In the method of the present invention, part of the hydrogenated vacuum wax oil obtained in step (1) can also be used as feed for other devices such as catalytic cracking devices and hydrocracking devices to produce other high-quality products.

[0014] In the method of the present invention, the volume of the hydrogenated atmospheric residue entering the vacuum fractionation unit in step (1) accounts for 20% to 90% of the total volume of the obtained hydrogenated atmospheric residue, preferably 30% to 80%; the volume of the hydrogenated atmospheric residue used as a marine fuel oil component in step (3) accounts for 10% to 80% of the total volume of the obtained hydrogenated atmospheric residue, preferably 20% to 70%.

[0015] In the method of the present invention, the volume of the hydrogenated vacuum residue entering the upflow hydrogenation reactor in step (2) accounts for 10% to 80% of the total volume of the hydrogenated vacuum residue obtained in step (1), preferably 20% to 50%; and the volume of the hydrogenated vacuum residue used as a marine fuel oil component in step (3) accounts for 20% to 90% of the total volume of the hydrogenated vacuum residue obtained in step (1), preferably 50% to 80%.

[0016] In the method of the present invention, the residual oil raw material in step (1) includes at least one of atmospheric residual oil or vacuum residual oil, and the residual oil raw material may also contain one or more of coker wax oil, deasphalted oil, and heavy distillate oil. In the residual oil raw material, the sulfur content is not higher than 5.0% by mass, and may be 2.0% to 5.0%; the Conradson carbon residue is not higher than 18%, and may be 10% to 14%; the total content of heavy metal nickel and vanadium is not higher than 200 μg / g, and may be 50 μg / g to 200 μg / g; the total nitrogen content is not higher than 0.80%, and may be 0.25% to 0.45%.

[0017] In the method of the present invention, the sulfur content of the relatively inferior residual oil raw material is greater than 3.5%, further 3.5% to 5.0%, and the total content of heavy metal nickel and vanadium is greater than 100 μg / g, further 100 μg / g to 200 μg / g. The sulfur content of the relatively good residual oil raw material is not more than 3.5%, further 1.0% to 3.5%, and the total content of heavy metal nickel and vanadium is not more than 100 μg / g, further 50 μg / g to 100 μg / g.

[0018] In the method of the present invention, based on the total feed volume of the residual oil raw material with relatively inferior properties and the residual oil raw material with relatively better properties, the residual oil raw material with relatively better properties accounts for 10% to 90% of the total feed volume, preferably 30% to 70%, and the residual oil raw material with relatively inferior properties accounts for 10% to 90% of the total feed volume, preferably 30% to 70%.

[0019] In the method of the present invention, in step (3), hydrogenated atmospheric residue oil is mixed with hydrogenated vacuum wax oil and hydrogenated vacuum residue oil in a mixing volume ratio of 0.1-100:0.1-100:1, preferably 0.1-25:0.1-15:1.

[0020] In the method of the present invention, the hydrogen used in the fixed bed hydrogenation unit may be circulating hydrogen.

[0021] In the method of the present invention, the hydrogen used in the upflow hydrogenation reactor is new hydrogen.

[0022] In the method of the present invention, the first hydrofining reaction in step (1) can adopt a fixed bed residue oil hydrotreating technology, and the fixed bed hydrogenation unit adopts at least one hydrogenation reactor. It is more preferred to set a plurality of hydrogenation reactors in series, and it is most preferred to set three to five hydrogenation reactors. The hydrogenation reactor is filled with a residue oil hydrotreating catalyst. Each reactor is preferably provided with a catalyst bed layer, which is easy to unload the waste catalyst and load the fresh catalyst. The residue oil hydrotreating catalyst used refers to a catalyst having at least one function of residue oil hydrodemetallization, hydrodesulfurization, hydrodenitrogenation, etc. The residue oil hydrotreating catalyst is generally based on a porous refractory inorganic oxide such as alumina as a carrier, a VIB group and / or a VIII group metal (such as at least one of the oxides of W, Mo, Co, Ni, etc.) as an active component, and various other additives such as P, Si, F, B, etc. are selectively added. At least one of the elements.

[0023] In the method of the present invention, the fixed bed residue oil hydroprocessing catalyst used in the fixed bed hydrogenation unit in step (1) includes a residue oil hydroprocessing protection catalyst, a residue oil hydrodemetallization catalyst and a residue oil hydrodesulfurization catalyst. Wherein, based on the total loading volume of the fixed bed residue oil hydroprocessing catalyst, the residue oil hydroprocessing protection catalyst accounts for 3% to 20% of the total loading volume; the residue oil hydrodemetallization catalyst accounts for 20% to 60% of the total loading volume, preferably 20% to 50%; the residue oil hydrodesulfurization catalyst accounts for 10% to 50% of the total loading volume, preferably 20% to 48%. After the hydrodesulfurization catalyst, the residue oil hydrodenitrogenation and carbon residue conversion catalysts can also be selectively loaded, and their loading volume accounts for less than 28% of the total loading volume. The residual oil hydroprocessing catalyst can be loaded in a conventional grading order, and the loading order is generally to contact the feedstock oil with the residual oil hydroprocessing protection catalyst, the residual oil hydrodemetallization catalyst, the residual oil hydrodesulfurization catalyst and the residual oil hydrodenitrogenation and carbon residue conversion catalyst in sequence. Of course, there is also a technology of mixing and loading two or more of the catalysts. The residual oil hydroprocessing protection catalyst, the residual oil hydrodemetallization catalyst, the residual oil hydrodesulfurization catalyst, the residual oil hydrodenitrogenation and carbon residue conversion catalyst can adopt the catalyst with corresponding functions commonly used in the art, such as the CEN, FZC, ZTN, and ZTS series residual oil hydroprocessing catalysts produced by the Catalyst Branch of Sinopec.

[0024] In the method of the present invention, the conditions of the first hydrofining reaction in step (1) are as follows: the hydrogen partial pressure is 5MPa to 35MPa, preferably 13MPa to 20MPa, the reaction temperature is 300°C to 420°C, preferably 330°C to 400°C, and the total feed liquid volume space velocity is generally 0.1h-1 ~5.0h -1 , preferably 0.15h -1 ~2.0h -1 , the total hydrogen to oil volume ratio is 100 to 5000, preferably 300 to 3000. The total feed refers to all feeds entering the fixed bed hydrogenation unit.

[0025] In the method of the present invention, the hydrogenated oil obtained in step (1) can be first subjected to gas-liquid separation and then subjected to atmospheric fractionation. The gas-liquid separation is carried out under the same pressure level as the hydrogenation reaction, and the operating temperature is 300°C to 400°C, preferably 330°C to 370°C. The gas phase obtained by separation is mainly hydrogen, which is circulated for use in the fixed bed hydrogenation unit. The liquid phase obtained by separation enters the atmospheric fractionation system to obtain hydrogenated naphtha, hydrogenated diesel and hydrogenated atmospheric residue. The hydrogenated atmospheric residue enters the vacuum fractionation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. The hydrogenated atmospheric residue has an initial boiling point of 330°C to 370°C. The initial boiling point of the hydrogenated vacuum residue is 520°C to 540°C, the initial boiling point of the hydrogenated vacuum wax oil is 330°C to 370°C, and the final boiling point is 520°C to 540°C.

[0026] In the method of the present invention, step (2) adopts the upflow hydrogenation reactor residue oil hydrotreating technology. The hydrogenated vacuum residue oil obtained in step (1) is circulated to the inlet of the upflow hydrogenation reactor and mixed with new hydrogen to enter the upflow hydrogenation reactor, and a second hydrotreating reaction is carried out under the action of the upflow hydrogenation catalyst.

[0027] The technical feature of the upflow hydrogenation reactor (UFR) is that the reactant stream flows from bottom to top, causing the catalyst bed to expand slightly, so the pressure drop is small. It is usually used to solve the problem of large changes in the initial and final pressure drops when processing inferior residual oil in a conventional fixed-bed reactor, in order to protect the downstream fixed-bed reactor and extend the device operation cycle. In the method of the present invention, an upflow hydrogenation reactor (UFR) is used to further hydrofinish the hydrogenated vacuum residue to remove sulfur and metals therein. Since coking precursors and metals are also enriched in asphaltene, i.e., in the reduced residue, the upflow hydrogenation reactor adopts the operating conditions of high temperature and high hydrogen partial pressure, which is conducive to suppressing coking and at the same time conducive to deep removal of impurities from the hydrogenated vacuum residue, and is conducive to a more stable state of the reactant stream in the subsequent hydrofining process, and is conducive to long-term operation of the device.

[0028] In the method of the present invention, at least one hydrogenation reactor is used in the upflow hydrogenation reactor of step (2). Each hydrogenation reactor is generally provided with a plurality of catalyst beds, and cold hydrogen or quench oil is injected between the beds to control the reaction temperature. The upflow hydrogenation reactor is filled with an upflow residue oil hydrotreating catalyst. The upflow residue oil hydrotreating catalyst used in the present invention includes a hydrodemetallization catalyst and a hydrodesulfurization catalyst, and may also selectively include a hydroprotection catalyst. The upflow residue oil hydrotreating catalyst is generally based on a porous refractory inorganic oxide such as alumina as a carrier, a VIB group and / or a VIII group metal (such as at least one of W, Mo, Co, Ni, etc.) as an active component, and selectively adds various other additives such as at least one of P, Si, F, B and other elements. The hydroprotection catalyst, the hydrodemetallization catalyst, and the hydrodesulfurization catalyst can adopt catalysts with corresponding functions commonly used in the art, such as the FZC series upflow residue oil hydrotreating catalyst produced by the Catalyst Branch of Sinopec.

[0029] In the method of the present invention, in the upflow hydrogenation reactor, based on the total loading volume of the upflow residue hydroprocessing catalyst, the hydrogenation protection catalyst accounts for less than 20% of the total loading volume, which can be 3% to 20%, preferably 5% to 20%; the hydrodemetallization catalyst accounts for 20% to 80% of the total loading volume, preferably 35% to 75%; the hydrodesulfurization catalyst accounts for 5% to 70% of the total loading volume, preferably 10% to 65%.

[0030] In the method of the present invention, the reaction conditions of the second hydrofining reaction described in step (2) are as follows: the hydrogen partial pressure is 12MPa to 35MPa, preferably 15MPa to 22MPa, the reaction temperature is 350°C to 500°C, preferably 380°C to 420°C, and the total feed liquid volume space velocity is generally 0.1h -1 ~5.0h -1 , preferably 0.15h -1 ~2.0h -1 , the total hydrogen to oil volume ratio is 200-400, preferably 210-350. Among them, the total feed refers to all the feeds entering the upflow reactor. The upflow reactor strictly controls the inlet temperature and the inlet hydrogen volume to maintain the stable distribution state of the upflow reactor logistics. The upflow reactor uses new hydrogen with a hydrogen purity of more than 99% and a higher hydrogen partial pressure.

[0031] In the method of the present invention, the mass content of aromatics and gum in the marine fuel oil product obtained in step (3) is above 35%, preferably 37% to 50%, and more preferably 38% to 45%.

[0032] In the method of the present invention, the mass content of sulfur in the marine fuel oil product obtained in step (3) is less than 0.5%, and further less than 0.4%. The advantages of the method of the present invention are as follows:

[0033] 1. The method of the present invention adopts a combination of an upflow hydrogenation process and a fixed bed hydrogenation process, and the residual oil raw materials of different properties enter the upflow hydrogenation process and the fixed bed hydrogenation process respectively, so that the hydrogenation effect and the conversion depth can be better controlled, especially under the condition that the sulfur content can meet the index, the conversion depth of the residual carbon can be controlled, and excessive hydrogenation conversion can be prevented. Low-sulfur marine fuel products with different viscosity indicators can be flexibly produced, and have better economic efficiency;

[0034] 2. In the method of the present invention, the residual oil raw material with inferior properties is fed into the upflow hydrogenation reactor for hydrofining reaction, which fully utilizes the process advantages of the upflow type, has a higher reaction hydrogen partial pressure and a lower pressure drop, and achieves the pre-refining reaction and desulfurization goals; the residual oil raw material with better properties is fed into the fixed bed hydrogenation process, and the refining reaction is carried out under milder conditions, which not only avoids the rapid increase of the reactor pressure drop, but also has the advantage of deep hydrodesulfurization;

[0035] 3. The method of the present invention uses an upflow hydrogenation reactor to treat hydrogenated vacuum residue oil, which allows deep desulfurization while avoiding fixed-bed hydrogenation that causes aromatic components and colloids in the oil product to be over-saturated with hydrogen, thereby improving the stability of the oil product peptization system and thus improving the stability of marine fuel oil;

[0036] 4. In the method of the present invention, the upflow hydrogenation reactor can achieve deep desulfurization effect under the condition of lower hydrogen-to-oil volume ratio, improve metal tolerance, enhance raw material adaptability and processing flexibility; fixed bed hydrogenation can meet the design requirements by using a small amount or no high-activity denitrification and carbon residue removal catalyst, and can be carried out under mild reaction conditions, not only can it produce marine fuel oil with good comprehensive performance, but also can produce hydrogenated naphtha and diesel, and has the advantages of low device energy consumption, long device operation cycle and good economic benefits;

[0037] 5. In the method of the present invention, the product atmospheric and vacuum fractionation equipment is used, and the processing method is flexible, thereby achieving maximum benefit. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 It is a process flow diagram of a specific implementation method of the production method of low-sulfur marine fuel oil of the present invention;

[0039] Figure 2 This is a schematic diagram of the process flow of comparative example 1 using a conventional upflow reactor and a fixed bed hydrogenation. DETAILED DESCRIPTION

[0040] The method provided by the present invention is further described below in conjunction with the accompanying drawings, but the protection scope of the present invention is not limited thereby.

[0041] like Figure 1 As shown, the residual oil raw material 1 with relatively good properties is mixed with the effluent 18 of the upflow hydrogenation reactor 17, and after being pressurized, it is mixed with the circulating hydrogen 5 and enters the fixed bed hydrogenation unit 2. By contacting with the fixed bed residual oil hydroprocessing catalyst, the metal, sulfur, nitrogen and other impurities in the raw oil are removed, and the viscosity and density of the raw material are reduced to meet the product requirements. The hydrogenated oil 3 of the fixed bed hydrogenation unit 2 enters the high and low pressure separator 4 for gas-liquid separation, and the separated gas phase logistics is treated with desulfurization and hydrogenation, and then enters the circulating compressor to increase the pressure and then the circulating hydrogen 5 is sent to the entrance of the fixed bed hydrogenation unit 2. The separated liquid phase logistics 6 passes through the atmospheric fractionation tower 7 to obtain fuel gas 8, hydrogenated naphtha 9, hydrogenated diesel 10 and hydrogenated atmospheric residue 11. The partially hydrogenated atmospheric residue 11 obtained enters the vacuum fractionation tower 12 for vacuum fractionation to obtain hydrogenated vacuum residue 14 and hydrogenated vacuum wax oil 13. The partially hydrogenated vacuum residue 14 is mixed with the relatively inferior residue feedstock 16 and the new hydrogen 15 and enters the upflow hydrogenation reactor 17. By contacting with the upflow residue hydrotreating catalyst, the metal, sulfur and other impurities in the feedstock oil are further removed to obtain the upflow hydrogenation reactor effluent 18. The obtained partially hydrogenated vacuum residue 14 is mixed with the obtained partially hydrogenated atmospheric residue 11 and at least part of the hydrogenated vacuum wax oil 13 to obtain a marine fuel oil product. The partially hydrogenated vacuum wax oil 13 can also be used as feed for other devices such as catalytic cracking units and hydrocracking units to produce other high-quality products.

[0042] like Figure 2 As shown, the relatively good residual oil raw material 1 is mixed with the relatively poor residual oil raw material 16 and the circulating hydrogen 5 and enters the upflow hydrogenation reactor 17 for hydrogenation reaction, and the effluent 18 of the upflow hydrogenation reactor is pressurized and mixed with the new hydrogen 15 (and / or the circulating hydrogen 5) and enters the fixed bed hydrogenation unit 2. By contacting with the fixed bed residual oil hydroprocessing catalyst, the metal, sulfur, nitrogen and other impurities in the raw oil are removed, and the viscosity and density of the raw material are reduced to meet the product requirements. The hydrogenation generated oil 3 of the fixed bed hydrogenation unit 2 enters the high and low pressure separator 4 for gas-liquid separation, and the separated gas phase flow is treated with desulfurization and hydrogenation, and then enters the circulating compressor to increase the pressure and then the circulating hydrogen 5 is sent to the entrance of the fixed bed hydrogenation unit 2, and the separated liquid phase flow 6 passes through the atmospheric fractionation tower 7 to obtain fuel gas 8, hydrogenated naphtha 9, hydrogenated diesel 10 and hydrogenated atmospheric residue 11.

[0043] The method provided by the present invention is further illustrated by examples below, but the scope of protection of the present invention is not limited thereby. The feedstock oil used in the examples is a high-sulfur residue oil from the Middle East, and its properties are listed in Table 1. The fixed-bed hydroprocessing catalyst and the upflow residue hydroprocessing catalyst used in the examples are both FZC series residue hydroprocessing catalysts produced by the Catalyst Branch of Sinopec. The fixed-bed residue hydroprocessing catalyst specifically includes a hydrogenation protective agent, a hydrodemetallization catalyst, a hydrodesulfurization catalyst, a hydrodenitrogenation, and a carbon removal catalyst, and the loading order is to contact the feedstock oil with the hydrogenation protective agent, the hydrodemetallization catalyst, the hydrodesulfurization catalyst, the hydrodenitrogenation, and the carbon removal catalyst in turn. The upflow residue hydroprocessing catalyst specifically includes a hydrodemetallization catalyst and a hydrodesulfurization catalyst.

[0044] Example 1

[0045] This embodiment adopts the production method of low-sulfur marine fuel oil provided by the present invention (see Figure 1 ), using a relatively good residual oil raw material A and a relatively poor residual oil raw material B. The properties of the residual oil raw materials are shown in Table 1. It can be seen that the relatively good residual oil raw material A has a sulfur content of 1.55wt%, a residual carbon content of 9.75wt%, a metal (Ni+V) content of 62μg / g, and a total nitrogen content of 4326μg / g. The relatively poor residual oil raw material B shows that the residual oil sulfur content is as high as 3.84wt%, the residual carbon content is 13.58wt%, and the metal (Ni+V) content is 121μg / g, which belongs to the high-sulfur inferior residual oil. Both raw materials must be hydrotreated to produce low-sulfur marine fuel products. The feed volume ratio of the relatively good residual oil raw material A to the relatively poor residual oil raw material B is 1:1.

[0046] The fixed bed reactor of the device adopts three series connection, among which the first reactor is filled with three kinds of residual oil hydrogenation protective agents, with the filling volume of FZC-12B catalyst 20mL, FZC-103D catalyst 20mL, and FZC-103E catalyst 60mL respectively; the second reactor is filled with two kinds of residual oil hydrogenation demetallization catalysts, with the filling volume of FZC-28A catalyst 100mL and FZC-204 catalyst 200mL respectively; the third reactor is filled with a residual oil hydrogenation desulfurization catalyst FZC-34A, with a filling volume of 210mL, and a denitrification and carbon removal catalyst FZC-41A, with a filling volume of 90mL. Catalyst properties are shown in Table 2.

[0047] The upflow reactor of the device adopts one reactor and is provided with two beds, wherein the first bed is filled with 300 mL of FZC-10U upflow residue oil hydrodemetallization catalyst, and the second bed is filled with 350 mL of FZC-11U upflow residue oil hydrodesulfurization catalyst. The catalyst properties are shown in Table 3.

[0048] After further hydrogenation treatment, the fixed bed hydrogenation reaction product oil is obtained. The main operating conditions are shown in Table 4, and the properties of the reaction products are shown in Table 5.

[0049] The raw material A is mixed with the effluent of the upflow hydrogenation reactor and the circulating hydrogen, and then hydrogenated in a fixed bed hydrogenation reactor, and then separated by gas-liquid separation to obtain gas phase products and liquid phase products, wherein the liquid phase product is subjected to atmospheric distillation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel and hydrogenated atmospheric residue. 70% of the hydrogenated atmospheric residue is fractionated by a vacuum distillation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. The obtained 50% hydrogenated vacuum residue is mixed with 30% hydrogenated atmospheric residue and part of the hydrogenated vacuum wax oil as a low-sulfur marine fuel oil product. The 50% hydrogenated vacuum residue is returned to the upflow reactor and mixed with new hydrogen for further hydrogenation refining.

[0050] Example 2

[0051] Example 2 The production method of low sulfur marine fuel provided by the present invention (see Figure 1 ), using relatively good residual oil raw material A and relatively poor residual oil raw material B, the properties of the residual oil raw materials are shown in Table 1. Both raw materials must be hydrotreated to produce low-sulfur marine fuel products. The feed volume ratio of the relatively good residual oil raw material A to the relatively poor residual oil raw material B is 1:2.

[0052] The hydrogenation unit adopts four fixed-bed reactors connected in series, of which the first reactor is filled with three kinds of residue oil hydrogenation protective agents, with the filling volumes of FZC-12B catalyst 30mL, FZC-103D catalyst 40mL, and FZC-103E catalyst 80mL respectively; the second reactor is filled with two kinds of residue oil hydrodemetallization catalysts, with the filling volumes of FZC-28A catalyst 200mL and FZC-204 catalyst 230mL respectively; the third reactor is filled with a residue oil hydrodesulfurization catalyst FZC-34A, with a filling volume of 200mL; the fourth reactor is filled with a residue oil hydrodenitrogenation and carbon removal catalyst FZC-41A, with a filling volume of 100mL. The specific catalyst properties are shown in Table 2.

[0053] The upflow reactor of the device adopts one reactor and is provided with three beds, wherein the first bed is filled with 260 mL of FZC-10U upflow residue oil hydrodemetallization catalyst, the lower part of the second bed is filled with 190 mL of FZC-10U catalyst, the upper part is filled with 110 mL of FZC-11U upflow residue oil hydrodemetallization catalyst, and the third bed is filled with 240 mL of FZC-11U upflow residue oil hydrodesulfurization catalyst. Catalyst properties are shown in Table 3.

[0054] After further hydrogenation treatment, the fixed bed hydrogenation reaction product oil is obtained. The main operating conditions are shown in Table 3, and the distribution of the reaction products is shown in Table 5.

[0055] The raw material A is mixed with the effluent of the upflow hydrogenation reactor and the circulating hydrogen, and then hydrogenated in a fixed bed hydrogenation reactor, and then separated by gas and liquid to obtain gas phase products and liquid phase products, wherein the liquid phase product is subjected to atmospheric distillation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel and hydrogenated atmospheric residue. The obtained 40% hydrogenated atmospheric residue is fractionated by a vacuum distillation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. 30% of the hydrogenated vacuum residue is mixed with 60% of the hydrogenated atmospheric residue and part of the hydrogenated vacuum wax oil as a low-sulfur marine fuel oil product. 70% of the hydrogenated vacuum residue is returned to the upflow reactor and mixed with new hydrogen for further hydrogenation refining.

[0056] Example 3

[0057] This embodiment adopts the production method of low-sulfur marine fuel oil provided by the present invention (see Figure 1 ), using residual oil raw material A with relatively better properties and residual oil raw material B with relatively inferior properties, the properties of the residual oil raw materials are shown in Table 1. The feed volume ratio of the residual oil raw material A with relatively better properties to the residual oil raw material B with relatively inferior properties is 3:1.

[0058] The fixed bed reactor of the device adopts three series connection, among which the first reactor is filled with two kinds of residual oil hydrogenation protective agents, with the filling volume of FZC-12B catalyst 50mL and FZC-103E catalyst 100mL respectively; the second reactor is filled with two kinds of residual oil hydrogenation demetallization catalysts, with the filling volume of FZC-28A catalyst 120mL and FZC-204 catalyst 180mL respectively; the third reactor is filled with a residual oil hydrogenation desulfurization catalyst FZC-34A, with the filling volume of 300mL. Catalyst properties are shown in Table 2.

[0059] The upflow reactor of the device adopts one reactor and is provided with two beds, wherein the first bed is filled with 200 mL of FZC-10U upflow residue oil hydrodemetallization catalyst, and the second bed is filled with 220 mL of FZC-11U upflow residue oil hydrodesulfurization catalyst. The catalyst properties are shown in Table 3.

[0060] After further hydrogenation treatment, the fixed bed hydrogenation reaction product oil is obtained. The main operating conditions are shown in Table 4, and the properties of the reaction products are shown in Table 5.

[0061] The raw material A is mixed with the effluent of the upflow hydrogenation reactor and the circulating hydrogen, and then hydrogenated in a fixed bed hydrogenation reactor, and then separated by gas and liquid to obtain gas phase products and liquid phase products, wherein the liquid phase product is subjected to atmospheric distillation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel and hydrogenated atmospheric residue. The 50% hydrogenated atmospheric residue obtained is fractionated by a vacuum distillation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. The 65% hydrogenated vacuum residue is mixed with the 50% hydrogenated atmospheric residue and part of the hydrogenated vacuum wax oil as a low-sulfur marine fuel oil product. The 35% hydrogenated vacuum residue is returned to the upflow reactor and mixed with new hydrogen for further hydrogenation refining.

[0062] Table 1 Residue oil raw material properties

[0063] project Raw material A Raw material B S, wt% 1.55 3.84 N, μg / g 4326 3288 Carbon residue (CCR), wt% 9.75 13.58 <![CDATA[Density (20 °C), kg / m 3 > 980.1 996.2 <![CDATA[Viscosity (100 °C), mm 2 / s]]> 67 254 Ni+V, μg / g 62 121 Saturated hydrocarbons, wt% 40.67 38.45 Aromatic hydrocarbons, wt% 38.96 37.75 Gel, wt% 18.1 20.02 Asphaltene, wt% 2.27 3.78

[0064] Table 2 Properties of fixed bed residue hydrotreating catalyst

[0065]

[0066] Table 3 Properties of upflow hydroprocessing catalyst

[0067]

[0068]

[0069] Table 4 Main operating conditions of the embodiment

[0070]

[0071] Table 5 Distribution of hydrogenation reaction products

[0072]

[0073]

[0074] Table 6 Main product properties of Example 1

[0075] Hydrogenation products Hydrogenated naphtha Hydrogenated diesel Hydrotreated atmospheric residue Hydrogenated vacuum wax oil Hydrogenated vacuum residue <![CDATA[Density (20 °C), g / cm 3 > 0.731 0.842 0.928 0.882 0.965 <![CDATA[Viscosity (100 °C), mm 2 / s]]> - - 30 12 230 <![CDATA[Viscosity (50 °C), mm 2 / s]]> - - - 77 - Carbon residue value, wt% - - 5.10 0.20 8.82 S, μg / g 55 210 4343 2230 6513 N, μg / g 22 163 2260 1200 4877 Ni+V, μg / g - - 9.8 - 19.3

[0076] Table 7 Main product properties of Example 2

[0077] Hydrogenation products Hydrogenated naphtha Hydrogenated diesel Hydrotreated atmospheric residue Hydrogenated vacuum wax oil Hydrogenated vacuum residue <![CDATA[Density (20 °C), g / cm 3 > 0.730 0.843 0.933 0.882 0.976 <![CDATA[Viscosity (100 °C), mm 2 / s]]> - - 31 22 283 <![CDATA[Viscosity (50 °C), mm 2 / s]]> - - - 86 - Carbon residue value, wt% - - 5.73 0.26 8.80 S, μg / g 50 271 4270 2170 7520 N, μg / g 43 213 2110 1452 5320 Ni+V, μg / g - - 12.6 - 25.2

[0078] Table 8 Main product properties of Example 3

[0079]

[0080]

[0081] Table 9 Main properties of low sulfur marine fuel

[0082] project Example 1 Example 2 Example 3 Hydrogenated atmospheric residue, wt% 11.14 36.34 20.31 Hydrogenated vacuum residue, wt% 11.91 1.89 11.88 Hydrogenated vacuum wax oil, wt% 15.01 3.84 8.26 <![CDATA[Density (20 °C), g / cm 3 > 0.921 0.935 0.930 <![CDATA[Viscosity (50 °C), mm 2 / s]]> 210 202 238 S, μg / g 4189 4424 4341 Carbon residue, wt% 4.78 6.40 5.66 Acid value (in KOH), mg / g 0.020 0.021 0.022 Ash, wt% 0.03 0.02 0.03 Carbon Aromatic Index CCAI 855 854 852 Ni+V, μg / g 8.908 13.184 12.876 Saturated hydrocarbons, wt% 60.75 59.77 58.86 Aromatic hydrocarbons, wt% 28.72 29.68 29.11 Gel, wt% 9.95 9.98 11.32 Asphaltene, wt% 0.58 0.57 0.71

[0083] Table 10 Main product properties of low sulfur marine fuel

[0084]

[0085]

[0086] As can be seen from Tables 9 and 10, Examples 1-3 show that blending different proportions of hydrogenated wax oil can achieve different viscosity requirements, while satisfying the sulfur content of less than 0.5%, and other indicators can also meet the requirements of fuel oil properties. Hydrogenated wax oil has good properties. On the one hand, it can be used as a raw material for hydrocracking and catalytic cracking to produce high value-added products. On the other hand, it can flexibly produce marine fuel products of different viscosities by adjusting the addition of different proportions of hydrogenated wax oil. The method of the present invention flexibly produces low-sulfur marine fuel products, and at the same time can well meet the needs of enterprises that want to increase the yield of light oil.

[0087] In addition, it can be seen that the low-sulfur marine fuel prepared by the method of the present invention has a saturated mass fraction of 58% to 61% in the product; the aromatic fraction is about 28 to 30%, and the colloid content is 9% to 12%. The sum of the two reaches more than 38.5%. The inventor found that the fixed bed hydrogenation makes the aromatic components and colloids in the oil product excessively hydrogenated and saturated, and the sum of the two is less than 35%, which will affect the stability of the oil system. Therefore, the present invention can improve the stability of marine fuel oil under the conditions of meeting various product indicators.

[0088] Comparative Example 1

[0089] This comparative example adopts an upflow and fixed bed reactor series process route (see Figure 2 ), this comparative example uses the same raw material feed as Example 1, and the feed amount is the same, and the volume ratio of the feed amount of the residual oil raw material A with relatively better properties to the feed amount of the residual oil raw material B with relatively inferior properties is 1:1. The properties of the residual oil raw materials are shown in Table 1. Different from the separate feeding method of the two feeds in Example 1, the residual oil raw material A with relatively better properties and the residual oil raw material B with relatively inferior properties in this comparative example both enter the upflow reactor for hydrogenation reaction, and then enter the fixed bed reactor for hydrogenation reaction, and the hydrogenated oil is fractionated to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel and hydrogenated atmospheric residue. Hydrogenated atmospheric residue is used as a low-sulfur marine fuel product.

[0090] The upflow reactor of the device adopts one reactor and is provided with two beds, wherein the first bed is filled with 300 mL of FZC-10U upflow residue oil hydrodemetallization catalyst, and the second bed is filled with 350 mL of FZC-11U upflow residue oil hydrodesulfurization catalyst. The catalyst properties are shown in Table 3.

[0091] The fixed bed reactor of the device adopts three series connection, among which one is loaded with three kinds of residual oil hydrogenation protective agents, and the filling volumes are respectively 20mL of FZC-12B catalyst, 20mL of FZC-103D catalyst, and 60mL of FZC-103E catalyst; the second is loaded with two kinds of residual oil hydrogenation demetallization catalysts, and the filling volumes are respectively 100mL of FZC-28A catalyst and 200mL of FZC-204 catalyst; the third is loaded with a residual oil hydrogenation desulfurization catalyst FZC-34A, and the filling volume is 210mL, and a denitrification and decarbonization catalyst FZC-41A, and the filling volume is 90mL. The catalyst properties are the same as those in Example 1. Table 11 shows the main operating process conditions, Table 12 shows the distribution of hydrogenation reaction products, and Table 13 shows the main product properties.

[0092] Table 11 Main operating conditions of comparative example 1

[0093]

[0094] Table 12 Distribution of hydrogenation reaction products

[0095] project Comparative Example 1 Hydrogenation reaction part Fuel gas, wt% 3.81 Hydrogenated naphtha, wt% 2.66 Hydrogenated diesel, wt% 11.35 Hydrogenated atmospheric residue, wt% 82.18

[0096] Table 13 Main product properties of Comparative Example 1

[0097] Hydrogenation products Hydrogenated naphtha Hydrogenated diesel Hydrogenated atmospheric residue <![CDATA[Density (20 °C), g / cm 3 > 0.733 0.842 0.923 <![CDATA[Viscosity (100 °C), mm 2 / s]]> / / 42 <![CDATA[Viscosity (50 °C), mm 2 / s]]> / / 342 Carbon residue value, wt% / / 4.52 S, μg / g 62 263 4722 N, μg / g 24 211 2325 Ni+V, μg / g / / 11.23 Saturated hydrocarbons, wt% / / 65.69 Aromatic hydrocarbons, wt% / / 22.73 Gel, wt% / / 10.35 Asphaltene, wt% / / 1.23

[0098] As can be seen from Table 13, Comparative Example 1 adopts a conventional upflow and fixed bed combined process. In order to meet the index requirements for the impurity content of sulfur, nitrogen and residual carbon in the hydrogenated residue oil, a higher reaction temperature is required. The upflow reaction temperature is 387°C, and the fixed bed reaction temperature is 384°C. At the same time, the hydrogen consumption is much higher than that of Example 1. In addition, it can be seen that in order to meet the index requirements for product impurity content, especially sulfur content, at a higher reaction temperature, the yield of light oil products of hydrogenated products increases, especially the output of fuel gas increases, which increases the processing cost, and the yield of the target product hydrogenated residue oil decreases, affecting the product yield. The sulfur content of the hydrogenated slag is 0.47%, but the viscosity (50°C) is 342mm 2 / s, can only be used as a high-viscosity marine fuel product. If other low-viscosity products are to be produced, they need to be blended with other products.

[0099] In addition, in the hydrogenated product obtained in Comparative Example 1, the yield of aromatic hydrocarbons was 22.73%, and the content of colloid was 10.35%, and the sum of the two did not reach 35%. It can be seen that in order to achieve the required high hydrogenation depth of impurity content and viscosity, the content of saturated hydrocarbons reached 65.69%. However, the excessively high content of saturated hydrocarbons and the low content of colloid and aromatic hydrocarbons affect the stability of the oil system, which is not conducive to the storage and transportation of marine fuel oil, and further affects its performance.

Claims

1. A method for producing marine fuel oil by hydrogenation, comprising: (1) mixing the residual oil feedstock with relatively good properties with the effluent of the upflow hydrogenation reactor obtained in step (2) and hydrogen into a fixed bed hydrogenation unit for a first hydrofining reaction to obtain a hydrogenated product oil; the hydrogenated product oil is first subjected to atmospheric distillation to obtain a hydrogenated atmospheric residue oil; and part of the hydrogenated atmospheric residue oil is further subjected to vacuum distillation to obtain a hydrogenated vacuum residue oil and a hydrogenated vacuum wax oil; (2) the partially hydrogenated vacuum residue obtained in step (1) is mixed with a relatively inferior residue feedstock and hydrogen and fed into an upflow hydrogenation reactor for a second hydrofining reaction to obtain an effluent from the upflow hydrogenation reactor; (3) mixing the partially hydrogenated atmospheric residue obtained in step (1) and the partially hydrogenated vacuum residue obtained in step (2) with at least a portion of the hydrogenated vacuum wax oil to obtain a marine fuel oil product; Among them, the residual oil raw materials with relatively inferior properties have a sulfur content of more than 3.5% by mass and a total content of heavy metals nickel and vanadium of more than 100μg / g; the residual oil raw materials with relatively good properties have a sulfur content of no more than 3.5% by mass and a total content of heavy metals nickel and vanadium of no more than 100μg / g; The volume of the hydrogenated atmospheric residue entering the vacuum fractionation unit in step (1) accounts for 20% to 90% of the total volume of the hydrogenated atmospheric residue obtained; the volume of the hydrogenated atmospheric residue used as a marine fuel oil component in step (3) accounts for 10% to 80% of the total volume of the hydrogenated atmospheric residue obtained; Based on the total feed volume of the residual oil raw materials with relatively inferior properties and the residual oil raw materials with relatively better properties, the residual oil raw materials with relatively better properties account for 10% to 90% of the total feed volume, and the residual oil raw materials with relatively inferior properties account for 10% of the total feed volume.

2. The method according to claim 1, characterized in that: The volume of the hydrogenated atmospheric residue entering the vacuum fractionation unit in step (1) accounts for 30% to 80% of the total volume of the hydrogenated atmospheric residue obtained; the volume of the hydrogenated atmospheric residue used as a marine fuel oil component in step (3) accounts for 20% to 70% of the total volume of the hydrogenated atmospheric residue obtained.

3. The method according to claim 1, characterized in that: The volume of the hydrogenated vacuum residue oil entering the upflow hydrogenation reactor in step (2) accounts for 10% to 80% of the total volume of the hydrogenated vacuum residue oil obtained in step (1); the volume of the hydrogenated vacuum residue oil used as a marine fuel oil component in step (3) accounts for 20% to 90% of the total volume of the hydrogenated vacuum residue oil obtained in step (1).

4. The method according to claim 3, characterized in that: The volume of the hydrogenated vacuum residue oil entering the upflow hydrogenation reactor in step (2) accounts for 20% to 50% of the total volume of the hydrogenated vacuum residue oil obtained in step (1); the volume of the hydrogenated vacuum residue oil used as a marine fuel oil component in step (3) accounts for 50% to 80% of the total volume of the hydrogenated vacuum residue oil obtained in step (1).

5. The method according to claim 1, characterized in that: Based on the total feed volume of residual oil raw materials with relatively inferior properties and residual oil raw materials with relatively better properties, the residual oil raw materials with relatively better properties account for 30% to 70% of the total feed volume, and the residual oil raw materials with relatively inferior properties account for 30% to 70% of the total feed volume.

6. The method according to claim 1, characterized in that: In step (3), hydrogenated atmospheric residue oil is mixed with hydrogenated vacuum wax oil and hydrogenated vacuum residue oil in a mixing volume ratio of 0.1-100:0.1-100:

1.

7. The method according to claim 6, characterized in that: In step (3), the hydrogenated atmospheric residue oil is mixed with the hydrogenated vacuum wax oil and the hydrogenated vacuum residue oil in a mixing volume ratio of 0.1-25:0.1-15:

1.

8. The method according to claim 1, characterized in that: The hydrogen used in the fixed-bed hydrogenation unit is recycled hydrogen; the hydrogen used in the upflow hydrogenation reactor is new hydrogen.

9. The method according to claim 1, characterized in that: The first hydrotreating reaction in step (1) adopts fixed bed residue oil hydrotreating technology.

10. The method according to claim 1, characterized in that: The fixed bed residue oil hydrotreating catalyst used in the fixed bed hydrogenation unit in step (1) comprises a residue oil hydrotreating protection catalyst, a residue oil hydrodemetallization catalyst and a residue oil hydrodesulfurization catalyst, wherein, based on the total loading volume of the fixed bed residue oil hydrotreating catalyst, the residue oil hydrotreating protection catalyst accounts for 3% to 20% of the total loading volume; the residue oil hydrodemetallization catalyst accounts for 20% to 60% of the total loading volume; the residue oil hydrodesulfurization catalyst accounts for 10% to 50% of the total loading volume; and after the hydrodesulfurization catalyst, a residue oil hydrodenitrogenation and residual carbon conversion catalyst is selectively loaded, and its loading volume accounts for less than 28% of the total loading volume.

11. The method according to claim 10, characterized in that: In the fixed bed residue oil hydrotreating catalyst used in the fixed bed hydrogenation unit in step (1), the residue oil hydrodemetallization catalyst accounts for 20% to 50% of the total loading volume; the residue oil hydrodesulfurization catalyst accounts for 20% to 48% of the total loading volume.

12. The method according to claim 1, 9 or 10, characterized in that: The conditions of the first hydrofining reaction in step (1) are as follows: hydrogen partial pressure of 5 MPa to 35 MPa, reaction temperature of 300°C to 420°C, total feed liquid hourly volume space velocity of 0.1 h -1 ~5.0h -1 , the total hydrogen-to-oil volume ratio is 100-5000.

13. The method according to claim 12, characterized in that: The conditions of the first hydrofining reaction in step (1) are as follows: hydrogen partial pressure of 13 MPa to 20 MPa, reaction temperature of 330°C to 400°C, total feed liquid hourly volume space velocity of 0.15 h -1 ~2.0h -1 , the total hydrogen-to-oil volume ratio is 300-3000.

14. The method according to claim 1, characterized in that: The initial distillation point of the hydrogenated atmospheric residue is 330°C to 370°C, the initial distillation point of the hydrogenated vacuum residue is 520°C to 540°C, the initial distillation point of the hydrogenated vacuum wax oil is 330°C to 370°C, and the final distillation point is 520°C to 540°C.

15. The method according to claim 1, characterized in that: Step (2) adopts the upflow hydrogenation reactor residue oil hydrotreating technology.

16. The method according to claim 1, characterized in that: In the upflow hydrogenation reactor, based on the total loading volume of the upflow residue hydrotreating catalyst, the hydrogenation protection catalyst accounts for less than 20% of the total loading volume; the hydrodemetallization catalyst accounts for 20% to 80% of the total loading volume; and the hydrodesulfurization catalyst accounts for 5% to 70% of the total loading volume.

17. The method according to claim 16, characterized in that: In the upflow hydrogenation reactor, based on the total loading volume of the upflow residue hydrotreating catalyst, the hydrogenation protection catalyst accounts for 5% to 20% of the total loading volume; the hydrodemetallization catalyst accounts for 35% to 75% of the total loading volume; and the hydrodesulfurization catalyst accounts for 10% to 65% of the total loading volume.

18. The method according to claim 1, 15 or 16, characterized in that: The reaction conditions of the second hydrofining reaction in step (2) are as follows: hydrogen partial pressure of 12 MPa to 35 MPa, reaction temperature of 350°C to 500°C, total feed liquid volume space velocity of 0.1 h -1 ~5.0h -1 , the total hydrogen-to-oil volume ratio is 200-400.

19. The method according to claim 18, characterized in that: The reaction conditions of the second hydrofining reaction in step (2) are as follows: hydrogen partial pressure of 15 MPa to 22 MPa, reaction temperature of 380°C to 420°C, total feed liquid hourly volume space velocity of 0.15 h -1 ~2.0h -1 , the total hydrogen-to-oil volume ratio is 210-350.

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