CN114644939B

CN114644939B - Method for producing bunker fuel oil by hydrogenation

Info

Publication number: CN114644939B
Application number: CN202011519303.6A
Authority: CN
Inventors: 蒋立敬; 刘铁斌; 韩坤鹏; 金建辉; 袁胜华; 耿新国
Original assignee: China Petroleum and Chemical Corp; Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Current assignee: Sinopec Dalian Petrochemical Research Institute Co ltd; China Petroleum and Chemical Corp
Priority date: 2020-12-21
Filing date: 2020-12-21
Publication date: 2023-03-07
Anticipated expiration: 2040-12-21
Also published as: CN114644939A

Abstract

The invention discloses a method for producing low-sulfur marine fuel oil by hydrogenation. The method comprises the following steps: (1) Mixing a residual oil raw material with relatively good property with the effluent of the upflow hydrogenation reactor obtained in the step (2) and hydrogen, and allowing the mixture to enter a fixed bed hydrogenation unit for a first hydrofining reaction to obtain hydrogenated oil; the hydrogenation generated oil is subjected to atmospheric fractionation and vacuum fractionation in sequence to obtain hydrogenation vacuum residue oil and hydrogenation vacuum wax oil; (2) Mixing part of hydrogenated vacuum residue with residue raw material with relatively poor property and hydrogen, and allowing the mixture to enter an upflow hydrogenation reactor for a second hydrofining reaction to obtain an upflow hydrogenation reactor effluent; (3) And mixing part of the hydrogenated vacuum residue oil with the hydrogenated vacuum wax oil to obtain the marine fuel oil product. The method can be used for treating the inferior residual oil raw material, and can obtain the low-sulfur marine fuel oil product which meets the index requirements of sulfur content, viscosity and the like and has a stable peptization system.

Description

Method for producing bunker fuel oil by hydrogenation

Technical Field

The invention relates to a process method for producing clean fuel oil by using inferior residual oil, in particular to a process method for flexibly producing low-sulfur marine fuel oil by using inferior high-sulfur residual oil as a raw material.

Background

With the stricter global environmental protection regulations, after the upgrading and updating of light oil products such as clean gasoline and diesel oil, the clean low-sulfur marine fuel oil becomes one of the oil products which are focused in the next years. The International Maritime Organization (IMO) International convention for preventing pollution caused by ships stipulates that the sulfur mass fraction of the bunker fuel oil used for sailing in general offshore areas from 3.5 percent to 0.5 percent at present from 2020 to 01 month; when sailing in the emission control area, the sulphur content of bunker fuel should not exceed 0.1%. In the marine fuel oil demand market, the high-sulfur residue type marine fuel oil accounts for about 70% of the whole market in price dominance, the distillate type marine fuel oil accounts for about 25%, and the balance is low-sulfur fuel oil (the mass fraction of sulfur is less than 3.5%) and a small amount of liquefied natural gas. Therefore, new environmental regulations will have a great impact on the current market for bunker fuel oil based on high-sulfur fuel oil, and will also promote the further development of the technology for desulfurizing bunker fuel oil.

At present, the main ways to produce residual bunker fuel oil with sulfur mass fraction not more than 0.5 percent include: low-sulfur straight-run residual oil is adopted for blending production. But because the low-sulfur crude oil has limited resources and higher price, the production cost of the residual type bunker fuel oil can be greatly improved, and the route is not suitable for the residual type bunker fuel oil with lower production value; the technology for producing the low-sulfur residual type marine fuel oil by performing hydrodesulfurization on the high-sulfur residual oil is feasible, but the residual oil with the sulfur content of more than 2.0 percent and even more than 3.0 percent is directly subjected to desulfurization to directly produce the residual type marine fuel oil with the sulfur mass fraction of less than 0.5 percent, so that the processing cost is high, the hydrogenation severity is high, the operation cost is high, and the economical efficiency is poor.

The residual oil hydrotreating process has the main aims of greatly reducing the impurity content in the residual oil material, hydrogenating and converting non-ideal components such as polycyclic aromatic hydrocarbon, colloid, asphaltene and the like, reducing the viscosity and obviously improving the physical properties of the residual oil material through hydrotreating.

In the existing fixed bed hydrogenation technology, the raw materials are subjected to impurity removal reactions such as hydrodesulfurization and the like under the action of hydrogen and a residual oil hydrogenation catalyst, and the product index requirements can be realized under high-temperature and high-harsh conditions. The residual oil hydrogenation catalyst is usually loaded in a grading mode and comprises a protective agent, a demetallization catalyst, a desulfurization catalyst and a high-activity denitrification and carbon residue removal catalyst. Along the direction of liquid phase material flow, the reaction temperature is gradually increased, the route has the defects that the hydrogen consumption is high in the hydrogenation process, the hydrogenation amount is large, higher reaction severity is required under the condition that the sulfur content meets the index, the sulfur content meets the index requirement under the condition of high temperature and high pressure, other indexes such as carbon residue are greatly reduced, the conversion rate is improved, and the processing cost is high. In addition, the problems of poor adaptability to crude oil and poor raw material adaptability of fixed bed hydrotreatment are not solved, and meanwhile, the running period of the device for processing inferior vacuum residue oil is short and the economy is poor.

CN107001959B discloses a low-sulfur marine fuel composition and a preparation method thereof. The method comprises the following steps: 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 resid with no more than 10 vol% of a first diesel boiling range hydrocarbon stream and no more than 40 vol% of a second diesel boiling range hydrocarbon stream to form the low sulfur marine fuel composition, wherein the hydrotreated vacuum resid comprises at least 60 vol% of the low sulfur marine fuel composition, wherein the vacuum resid feed stream has from 1000wppm to 10000wppm sulfur, the first diesel boiling range hydrocarbon stream has no more than 20wppm sulfur, and the second diesel boiling range hydrocarbon stream has no more than 10wppm sulfur. The method needs to adopt a conventional residual oil hydrogenation process to reduce the sulfur in the residual oil raw material to be below 1500 wppm, but the problems of short production period, increased product blending difficulty, complex process and poor economy of the conventional residual oil hydrogenation process for processing the poor vacuum residual oil raw material still cannot be solved because the production cost of adding a large proportion of fractions such as diesel oil and the like is greatly increased.

Disclosure of Invention

Aiming at the defects of the prior art, the invention provides a method for producing bunker fuel oil by hydrogenation. The method can treat the poor residual oil raw material, can meet the index requirements of sulfur content, viscosity and the like of the product, can meet the requirements of controlling hydrogenation depth and reducing processing cost, and simultaneously, the hydrogenated product is used as low-sulfur marine fuel oil, and a peptization system of the hydrogenated product is stable.

The inventor finds that, when the fixed bed residual oil hydrogenation technology is used for treating the poor residual oil raw material to produce the low-sulfur marine fuel oil, harsh reaction conditions are usually required, except the economic problem, under the reaction conditions, the conversion rate is greatly improved, the light component is excessively hydrogenated, a large amount of colloid is hydrogenated and saturated, so that the stability of an oil peptization system is easily damaged, on one hand, the stable operation of a device is not facilitated, on the other hand, the produced marine fuel oil meets the requirements of various indexes on the surface, but also has the problem of oil stability reduction, and the blending, storage and use of the low-sulfur marine fuel oil are adversely affected. The inventor researches and discovers that when the low-sulfur marine fuel oil product is produced by processing residual oil raw materials with different properties, if the residual oil raw materials with relatively poor properties and the residual oil raw materials with relatively high properties enter a fixed bed residual oil hydrogenation device together, the performance and the service cycle of the catalyst are influenced and the properties of the product are influenced because the poor-quality raw materials need higher reaction severity. Under the condition of higher reaction severity and the condition of meeting the key product index such as sulfur, viscosity and the like, the carbon residue is greatly reduced, the processing cost is increased, the product use performance is also influenced, and more importantly, the whole economic benefit is influenced because the fixed bed reactor is easy to cause the rapid increase of pressure drop. The method introduces two residual oil raw materials with different properties through different feed inlets, can process inferior residual oil raw materials by optimizing a hydrogenation process route, can improve the comprehensive performance of the produced bunker fuel oil, and has good economic and social benefits.

The invention provides a method for producing bunker fuel oil by hydrogenation, which comprises the following steps:

(1) Mixing a residual oil raw material with relatively good properties, the effluent of the upflow hydrogenation reactor obtained in the step (2) and hydrogen, and allowing the mixture to enter a fixed bed hydrogenation unit for a first hydrofining reaction to obtain hydrogenated product oil; the hydrogenation generated oil is subjected to atmospheric fractionation and vacuum fractionation in sequence to obtain hydrogenation vacuum residue oil and hydrogenation vacuum wax oil;

(2) Mixing part of hydrogenated vacuum residue obtained in the step (1) with residue raw material and hydrogen with relatively poor properties, and allowing the mixture to enter an upflow hydrogenation reactor for a second hydrofining reaction to obtain an upflow hydrogenation reactor effluent;

(3) And (2) mixing part of the hydrogenated vacuum residue obtained in the step (1) with at least part of the hydrogenated vacuum wax oil to obtain the bunker fuel oil product.

In the method, part of the hydrogenated vacuum wax oil obtained in the step (1) can also be used as the feed of other devices such as a catalytic cracker and a hydrocracking device to produce other high-quality products.

In the method, the mass of the hydrogenation vacuum residue entering the upflow hydrogenation reactor in the step (2) accounts for 10-80%, preferably 20-50% of the total mass of the hydrogenation vacuum residue obtained in the step (1). The mass of the hydrogenated vacuum residue serving as the marine fuel oil component in the step (3) accounts for 20-90%, preferably 50-80% of the total mass of the hydrogenated vacuum residue obtained in the step (1).

In the method, the residual oil raw material in the step (1) comprises at least one of atmospheric residual oil and vacuum residual oil, and the residual oil raw material can also simultaneously contain one or more of coker gas oil, deasphalted oil and heavy distillate oil. In the residual oil raw material, the sulfur content is not higher than 5.0 percent and can be 1.0 to 5.0 percent by mass; the content of the Kangshi carbon residue is not higher than 18 percent and can be 9 to 14 percent; the total content of heavy metal nickel and vanadium is not higher than 200 mug/g, and can be 40-200 mug/g; the total nitrogen content is not higher than 0.80%, and may be 0.25% to 0.70%.

In the method, the residual oil raw material with relatively poor properties contains more than 3.5 percent of sulfur and more than 100 mu g/g of total content of heavy metal nickel and vanadium by mass. The residual oil raw material with relatively good properties contains no more than 3.5 percent of sulfur and no more than 100 mu g/g of total content of heavy metal nickel and vanadium by mass.

In the method, the relatively poor residual oil raw material and the relatively good residual oil raw material account for 10 to 90 percent, preferably 30 to 70 percent, and the relatively poor residual oil raw material accounts for 10 to 90 percent, preferably 30 to 70 percent of the total feeding mass based on the total feeding mass of the relatively poor residual oil raw material and the relatively good residual oil raw material.

In the method, the mixing mass ratio of the hydrogenated vacuum residue oil to the hydrogenated vacuum wax oil in the step (3) is 0.50-7: 1.

the hydrogen used in the fixed bed hydrogenation unit in the process of the present invention may be recycle hydrogen.

In the method, the hydrogen used by the upflow hydrogenation reactor is new hydrogen.

In the method of the present invention, the first hydrofining reaction in step (1) may adopt a fixed bed residual oil hydrotreating technology, and the fixed bed hydrogenation unit adopts at least one hydrogenation reactor. More preferably, a plurality of hydrogenation reactors are arranged in series, and most preferably, three to five hydrogenation reactors are arranged. And a residual oil hydrotreating catalyst is filled in the hydrogenation reactor. Each reactor is preferably provided with a catalyst bed layer, so that the waste catalyst is easy to discharge and the fresh catalyst is easy to fill. The residual oil hydrotreating catalyst is a catalyst with at least one of the functions of residual oil hydrodemetallization, hydrodesulfurization, hydrodenitrogenation and the like. The residual oil hydrotreating catalyst has porous refractory inorganic oxide, such as alumina, as carrier, VIB and/or VIII metal, as active component, and optional addition of other assistants, such as at least one of P, si, F, B and other elements.

In the method, the fixed bed residual oil hydrotreating catalyst used in the fixed bed hydrogenation unit in the step (1) comprises a residual oil hydrogenation protection catalyst, a residual oil hydrodemetallization catalyst and a residual oil hydrodesulfurization catalyst. Wherein, the residual oil hydrogenation protection catalyst accounts for 3-20% of the total filling volume by taking the total filling volume of the fixed bed residual oil hydrogenation treatment catalyst as a reference; the residual oil hydrodemetallization catalyst accounts for 20-60%, preferably 20-50% of the total filling volume; the residual oil hydrodesulfurization catalyst accounts for 10-50%, preferably 20-48% of the total packing volume. After the hydrodesulfurization catalyst, residual oil hydrodenitrogenation and carbon residue conversion catalysts can be selectively filled, wherein the filling volume of the residual oil hydrodenitrogenation and carbon residue conversion catalysts accounts for less than 28% of the total filling volume. The residual oil hydrotreating catalyst may be loaded in conventional grading order, and the loading order is that the material oil contacts with residual oil hydrogenating protection catalyst, residual oil hydrodemetalizing catalyst, residual oil hydrodesulfurizing catalyst, residual oil hydrodenitrifying catalyst and residual oil carbon converting catalyst successively. There is, of course, a technique of mixing and packing two or more kinds of catalysts. The residual oil hydrogenation protection catalyst, the residual oil hydrogenation demetalization catalyst, the residual oil hydrogenation desulfurization catalyst, the residual oil hydrogenation denitrification and residual carbon conversion catalyst can adopt catalysts with corresponding functions commonly adopted in the field, such as CEN, FZC, ZTN and ZTS series residual oil hydrotreating catalysts produced by catalyst division of China petrochemical industry, ltd.

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 ℃ to 420 ℃, preferably 330 ℃ to 400 ℃, and the hourly volume space velocity of the total feeding liquid is generally 0.1h ^-1 ～5.0h ^-1 Preferably 0.15h ^-1 ～2.0h ^-1 The volume ratio of the total hydrogen to the oil is 100 to 5000, preferably 300 to 3000. Wherein, the total feed refers to all feeds to the fixed bed hydrogenation unit.

In the method, the hydrogenation product oil obtained in the step (1) can be subjected to gas-liquid separation firstly and then subjected to normal pressure fractionation, wherein the gas-liquid separation is performed under the condition of the same pressure grade as the hydrogenation reaction, and the operation temperature is 300-400 ℃, and is preferably 330-370 ℃. The gas phase obtained by separation is mainly hydrogen and is circularly used in a fixed bed hydrogenation unit. And the liquid phase obtained by separation enters an atmospheric fractionation system to obtain hydrogenated naphtha, hydrogenated diesel oil and hydrogenated atmospheric residue oil. And the hydrogenated atmospheric residue oil enters a vacuum fractionation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue oil. The initial boiling point of the hydrogenated atmospheric residue is 330-370 ℃. The initial boiling point of the hydrogenation vacuum residue oil is 520-540 ℃, the initial boiling point of the hydrogenation vacuum residue oil is 330-370 ℃, and the final boiling point of the hydrogenation vacuum residue oil is 520-540 ℃.

In the method, the step (2) adopts an upflow hydrogenation reactor residual oil hydrotreating technology. And (2) circulating the hydrogenated vacuum residue obtained in the step (1) to an inlet of the upflow hydrogenation reactor, mixing the hydrogenated vacuum residue with new hydrogen, entering the upflow hydrogenation reactor, and carrying out a second hydrofining reaction under the action of an upflow hydrotreating catalyst.

The upflow hydrogenation reactor (UFR) is technically characterized in that reactant flows from bottom to top, so that a catalyst bed layer slightly expands, the pressure drop is small, and the UFR is usually used for solving the problem that the pressure drop changes greatly in the initial stage and the final stage when a conventional fixed bed reactor processes inferior residual oil, so that a downstream fixed bed reactor is protected, and the operation period of a device is prolonged. In the method, the upflow hydrogenation reactor (UFR) is adopted to further hydrofining the hydrogenated vacuum residue to remove sulfur and metals in the hydrogenated vacuum residue. Because the coking precursor and metal are also enriched in asphaltene, namely slag reduction, the upflow hydrogenation reactor adopts the operating conditions of high temperature and high hydrogen partial pressure, which is beneficial to inhibiting coking, deep impurity removal reaction of hydrogenation vacuum residue oil, more stable reaction material flow state in the subsequent hydrofining process and long-period operation of the device.

In the method, at least one hydrogenation reactor is adopted in the upflow hydrogenation reactor in the step (2). Each hydrogenation reactor is generally provided with a plurality of catalyst beds, and cold hydrogen or quenching oil is injected between the beds to control the reaction temperature. An upflow residual oil hydrotreating catalyst is filled in the upflow hydrogenation reactor. The upflow residual oil hydrotreating catalyst used in the present invention includes hydrodemetallization catalyst and hydrodesulfurization catalyst, and may also optionally include hydrogenation protection catalyst. The upflow residual oil hydrotreating catalyst generally uses porous refractory inorganic oxide such as alumina as a carrier, and uses group VIB and/or group VIII metal (such as at least one of W, mo, co, ni, etc.) as an active component, and optionally adds at least one of other various auxiliary agents such as P, si, F, B, etc. The hydrogenation protection catalyst, the hydrogenation demetalization catalyst and the hydrogenation desulfurization catalyst can adopt catalysts with corresponding functions commonly adopted in the field, such as FZC series up-flow residual oil hydrotreating catalysts produced by catalyst division of China petrochemical industry Co.

In the method, in the upflow hydrogenation reactor, the total filling volume of the upflow residual oil hydrotreating catalyst is taken as a reference, and the hydrogenation protection catalyst accounts for 0-20 percent of the total filling volume, can be 3-20 percent, and is preferably 5-20 percent; the hydrodemetallization catalyst accounts for 20-80%, preferably 35-75% of the total packing volume; the hydrodesulfurization catalyst comprises from 5% to 70%, preferably from 10% to 65%, of the total packing volume.

In the process of the present invention, the reaction conditions of the second hydrorefining reaction in the step (2) are as follows: the hydrogen partial pressure is 12MPa to 35MPa, preferably 15MPa to 22MPa, the reaction temperature is 350 ℃ to 500 ℃, preferably 380 ℃ to 420 ℃, and the total feeding liquid hourly space velocity is generally 0.1h ^-1 ～5.0h ^-1 Preferably 0.15h ^-1 ～2.0h ^-1 The total hydrogen-oil volume ratio is 200 to 400, preferably 210 to 350. Wherein, the total feed refers to all feeds entering the upflow reactor. The upflow reactor strictly controls the inlet temperature and the inlet hydrogen amount to keep the steady distribution state of the upflow reactor. The upflow reactor adopts new hydrogen, the purity of the hydrogen is more than 99 percent, and the hydrogen has higher partial pressure.

The method of the invention has the following advantages:

1. the method adopts a mode of combining an up-flow hydrogenation process and a fixed bed hydrogenation process, and residual oil raw materials with different properties are respectively fed into the up-flow hydrogenation process and the fixed bed hydrogenation process, so that the hydrogenation effect and the conversion depth can be better controlled, particularly the conversion depth of residual carbon can be controlled under the condition that the sulfur content can meet the index, excessive hydrogenation conversion is prevented, low-sulfur marine fuel products with different viscosity indexes can be flexibly produced, and the economy is better;

2. in the method, the residue oil raw material with poor properties enters an up-flow hydrogenation reactor for hydrofining reaction, the up-flow process advantage is fully utilized, the higher reaction hydrogen partial pressure and the lower pressure drop are realized, and the prerefining reaction and the desulfurization target are realized; residual oil raw materials with better properties enter a fixed bed hydrogenation process, and are subjected to refining reaction under a milder condition, so that the rapid increase of the pressure drop of a reactor is avoided, and the advantage of deep hydrodesulfurization is achieved;

3. according to the method, the upflow hydrogenation reactor is adopted to treat the hydrogenation vacuum residue, so that the hydrogenation vacuum residue is deeply desulfurized, and meanwhile, the excessive hydrogenation saturation of aromatic components and colloid in an oil product due to the hydrogenation of a fixed bed is avoided, the stability of a peptization system of the oil product is improved, and the stability of the marine fuel oil is further improved;

4. in the method, the up-flow hydrogenation reactor can realize deep desulfurization effect under the condition of lower hydrogen-oil volume ratio, improve the metal capacity and enhance the adaptability and processing flexibility of the raw materials; the fixed bed hydrogenation can meet the design requirements by adopting a small amount of or not adopting a high-activity denitrification carbon residue removal catalyst, can be carried out under mild reaction conditions, can produce the bunker fuel oil with good comprehensive performance, can also produce hydrogenated naphtha and diesel oil, and has the advantages of low energy consumption of the device, long running period of the device and good economic benefit;

5. in the method, the product atmospheric and vacuum distillation equipment is adopted, the processing mode is flexible, and the maximization of benefit is realized.

Drawings

FIG. 1 is a schematic process flow diagram of one embodiment of the method for producing low sulfur bunker fuel oil according to the present invention;

FIG. 2 is a schematic diagram of a process flow of hydrogenation in a fixed bed using a conventional upflow reactor in comparative example 1.

Detailed Description

The method provided by the present invention is further described below with reference to the accompanying drawings, but the protection scope of the present invention is not limited thereby.

As shown in fig. 1, a residue raw material 1 with relatively good properties is mixed with an effluent 18 of an upflow hydrogenation reactor 17, the mixture is pressurized and then mixed with recycle hydrogen 5 to enter a fixed bed hydrogenation unit 2, and the mixture is contacted with a fixed bed residue hydrotreating catalyst to remove impurities such as metal, sulfur, nitrogen and the like in the raw material oil, and simultaneously, 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 a high-low pressure separator 4 for gas-liquid separation, the separated gas phase material flow is subjected to hydrogen sulfide removal treatment and the like, then the pressure of a circulating compressor is increased, then the circulating hydrogen 5 enters the inlet of the fixed bed hydrogenation unit 2, the separated liquid phase material flow 6 passes through an atmospheric fractionating tower 7 to obtain fuel gas 8, hydrogenation naphtha 9, hydrogenation diesel oil 10 and hydrogenation atmospheric residue oil 11, and the obtained hydrogenation atmospheric residue oil 11 enters a vacuum fractionating tower 12 for vacuum fractionation to obtain hydrogenation vacuum residue oil 14 and hydrogenation vacuum wax oil 13. Part of hydrogenation vacuum residuum 14, residuum raw material 16 with relatively inferior properties and new hydrogen 15 are mixed and enter an upflow hydrogenation reactor 17, and are contacted with an upflow residuum hydrotreating catalyst to further remove impurities such as metal, sulfur and the like in the raw material oil, so as to obtain an upflow hydrogenation reactor effluent 18. And mixing part of the hydrogenated vacuum residue 14 with at least part of the hydrogenated vacuum wax oil 13 to obtain the bunker fuel oil product. The partial hydrogenation vacuum wax oil 13 can also be used as the feed of other devices such as a catalytic cracker and a hydrocracking unit to produce other high-quality products.

As shown in fig. 2, the residue raw material 1 with relatively good properties, the residue raw material 16 with relatively poor properties and the recycle hydrogen 5 are mixed and enter an upflow hydrogenation reactor 17 for hydrogenation reaction, the effluent 18 of the upflow hydrogenation reactor is pressurized and then mixed with the new hydrogen 15 (and/or the recycle hydrogen 5) and enters a fixed bed hydrogenation unit 2, and the mixture is contacted with a fixed bed residue hydrotreating catalyst to remove impurities such as metal, sulfur, nitrogen and the like in the raw material oil, and simultaneously, the viscosity and the 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 a high-low pressure separator 4 for gas-liquid separation, the separated gas phase material flow is subjected to hydrogen sulfide removal treatment and the like, then the pressure of a circulating compressor is increased, then the circulating hydrogen 5 enters the inlet of the fixed bed hydrogenation unit 2, and the separated liquid phase material flow 6 passes through an atmospheric fractionating tower 7 to obtain fuel gas 8, hydrogenation naphtha 9, hydrogenation diesel oil 10 and hydrogenation atmospheric residue 11.

The process provided by the present invention is further illustrated by the following examples, which are not intended to limit the scope of the invention. The feed oil used in the examples was a middle east high sulfur residual oil, and its properties are shown in Table 1. The fixed bed hydrotreating catalyst and the upflow residual oil hydrotreating catalyst used in the examples are all FZC series residual oil hydrotreating catalysts produced by catalyst division of petrochemical company ltd. The fixed bed residual oil hydrotreating catalyst specifically comprises a hydrogenation protective agent, a hydrogenation demetallization catalyst, a hydrodesulfurization catalyst, a hydrodenitrogenation catalyst and a carbon residue removal catalyst, and the loading sequence is that the raw oil is sequentially contacted with the hydrogenation protective agent, the hydrogenation demetallization catalyst, the hydrodesulfurization catalyst, the hydrodenitrogenation catalyst and the carbon residue removal catalyst. The upflow residual oil hydrotreating catalyst specifically comprises a hydrodemetallization catalyst and a hydrodesulfurization catalyst.

Example 1

According to the method for producing the low-sulfur marine fuel oil (see figure 1), the residual oil raw material A with relatively good properties and the residual oil raw material B with relatively poor properties are adopted, the properties of the residual oil raw materials are shown in table 1, and it can be seen that the sulfur content of the residual oil raw material A with relatively good properties is 1.74wt%, the residual carbon content is 9.95wt%, the metal (Ni + V) content is 64 microgram/g, and the total nitrogen content is 4520 microgram/g. The residue raw material B with relatively poor properties shows that the sulfur content of the residue is up to 3.80wt%, the carbon residue content is 14.60wt%, and the metal (Ni + V) content is 136 mug/g, and belongs to high-sulfur poor residue. Both feedstocks must be hydrotreated to produce a low sulfur marine fuel product. The mass ratio of the feeding volume of the residual oil raw material A with relatively good properties to the feeding volume of the residual oil raw material B with relatively poor properties is 1:1.

three residual oil hydrogenation protective agents are reversely filled in one reactor, and the filling volumes of the three residual oil hydrogenation protective agents are 22mL of FZC-12B catalyst, 25mL of FZC-103D catalyst and 53mL of FZC-103E catalyst respectively; secondly, filling two residual oil hydrodemetallization catalysts in reverse direction, wherein the filling volumes are 82mL of FZC-28A catalyst and 118mL of FZC-204 catalyst respectively; a residual oil hydrodesulfurization catalyst FZC-34A with the filling volume of 123mL and a denitrification and carbon residue removal catalyst FZC-41A with the filling volume of 77mL are filled in three inversions. The catalyst properties are shown in Table 2.

The upflow reactor of the device adopts a reactor and is provided with two beds, wherein the first bed is filled with 165mL of FZC-10U upflow residual oil hydrodemetallization catalyst, and the second bed is filled with 175mL of FZC-11U upflow residual oil hydrodesulfurization catalyst. The catalyst properties are shown in Table 3.

And further carrying out hydrotreatment to obtain fixed bed hydrogenation reaction generated oil. The main operating conditions are shown in Table 4, and the properties of the product obtained by the reaction are shown in Table 5.

The raw material A, the effluent of the up-flow hydrogenation reactor and circulating hydrogen are mixed, and then subjected to hydrotreating by a fixed bed hydrogenation reactor, and then subjected to gas-liquid separation to obtain a gas-phase product and a liquid-phase product, wherein the liquid-phase product is subjected to atmospheric fractionation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated atmospheric residue. And fractionating all the hydrogenated atmospheric residue oil by a vacuum fractionation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue oil. And mixing the obtained 45 percent hydrogenated vacuum residue oil and hydrogenated vacuum wax oil to obtain a low-sulfur bunker fuel oil product. And returning 55% of hydrogenation vacuum residue to the upflow reactor to be mixed with new hydrogen for further hydrofining.

Example 2

Example 2 a process for producing a low-sulfur marine fuel according to the present invention (see fig. 1) was used with a residual feedstock a having relatively good properties and a residual feedstock B having relatively poor properties, the properties of which are shown in table 1. Both feedstocks must be hydrotreated to produce a low sulfur marine fuel product. The mass ratio of the residual oil raw material A with relatively good properties to the residual oil raw material B with relatively poor properties is 2:3.

the hydrogenation device adopts four fixed bed reactors connected in series, wherein one reactor is reversely filled with three residual oil hydrogenation protective agents, and the filling volumes are 30mL for FZC-12B catalyst, 35mL for FZC-103D catalyst and 35mL for FZC-103E catalyst respectively; secondly, filling two residual oil hydrodemetallization catalysts with the filling volumes of 150mL of FZC-28A catalyst and 130mL of FZC-204 catalyst respectively; a residual oil hydrodesulfurization catalyst FZC-34A is filled in the third reaction, and the filling volume is 200mL; a residual oil hydrodenitrogenation and carbon residue removal catalyst FZC-41A is filled in the four-way reaction, the filling volume is 80mL, and the specific catalyst properties are shown in Table 2.

The upflow reactor of the device adopts a reactor and is provided with three beds, wherein 200mL of FZC-10U upflow residual oil hydrodemetallization catalyst is filled in the first bed, 70mL of FZC-10U catalyst is filled in the lower part of the second bed, 130mL of FZC-11U upflow residual oil hydrodemetallization catalyst is filled in the upper part of the second bed, and 180mL of FZC-11U upflow residual oil hydrodesulfurization catalyst is filled in the third bed. The catalyst properties are shown in Table 3.

And further carrying out hydrotreatment to obtain fixed bed hydrogenation reaction generated oil. The main operating conditions are shown in Table 3, and the distribution of the products obtained in the reaction is shown in Table 5.

And mixing the raw material B, the effluent of the up-flow hydrogenation reactor and circulating hydrogen, carrying out hydrotreating by a fixed bed hydrogenation reactor, and carrying out gas-liquid separation to obtain a gas-phase product and a liquid-phase product, wherein the liquid-phase product is subjected to atmospheric fractionation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated atmospheric residue. All the obtained hydrogenated atmospheric residue is fractionated by a vacuum fractionation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. 66 percent of hydrogenated vacuum residue oil and hydrogenated vacuum wax oil are mixed to be used as a low-sulfur bunker fuel oil product. And returning 34 percent of hydrogenated vacuum residue to the upflow reactor to be mixed with new hydrogen for further hydrofining.

Example 3

This example uses the process for producing low sulfur bunker fuel oil according to the present invention (see fig. 1), using a relatively good residual feedstock a and a relatively poor residual feedstock B, the properties of which are shown in table 1. The feeding mass ratio of the residual oil raw material A with relatively good property to the residual oil raw material B with relatively poor property is 7:3.

three fixed bed reactors are connected in series, wherein one reactor is reversely filled with two residual oil hydrogenation protective agents, the filling volumes are 60mL of FZC-12B catalyst and 90mL of FZC-103E catalyst respectively; secondly, filling two residual oil hydrodemetallization catalysts in reverse directions, wherein the filling volumes of the two residual oil hydrodemetallization catalysts are 70mL of FZC-28A catalyst and 170mL of FZC-204 catalyst respectively; and a residual oil hydrodesulfurization catalyst FZC-34A is filled in the three reactors in a volume of 240mL. The catalyst properties are shown in Table 2.

The upflow reactor of the device adopts one reactor and is provided with two beds, wherein 180mL of the FZC-10U upflow type residual oil hydrodemetallization catalyst is filled in the first bed, and 190mL of the FZC-11U upflow type residual oil hydrodesulfurization catalyst is filled in the second bed. The catalyst properties are shown in Table 3.

The raw material A, the effluent of the up-flow hydrogenation reactor and circulating hydrogen are mixed, and then subjected to hydrotreating by a fixed bed hydrogenation reactor, and then subjected to gas-liquid separation to obtain a gas-phase product and a liquid-phase product, wherein the liquid-phase product is subjected to atmospheric fractionation to obtain fuel gas, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated atmospheric residue. All the hydrogenated atmospheric residue is fractionated by a vacuum fractionation system to obtain hydrogenated vacuum wax oil and hydrogenated vacuum residue. 50 percent of hydrogenated vacuum residue oil and hydrogenated vacuum wax oil are mixed to be used as a low-sulfur marine fuel oil product. And returning 50% of the hydrogenated vacuum residue to the upflow reactor to be mixed with new hydrogen for further hydrofining.

The properties of the raw materials are shown in Table 1. Tables 2, 3, 4, 5, and 6-8 show the properties of the fixed bed residue hydrotreating catalyst, the properties of the upflow hydrotreating catalyst, the main operating conditions, the distribution of the hydrogenation reaction products, and the properties of the main products of each example, respectively. Tables 9 and 10 show properties of bunker fuel oil products, wherein the mass fractions of the hydrogenated vacuum residue and the hydrogenated vacuum wax oil are based on the mass of the fresh residue feedstock.

TABLE 1 residual feedstock Properties

Item	Starting materials A	Raw material B
			S，wt%	1.74	3.80
N，μg/g	4520	3362
			Carbon Residue (CCR), wt%	9.95	14.60
Density (20 ℃ C.), kg/m ³	980.1	996.2
			Viscosity (100 ℃ C.), mm ² /s	72	266
Ni+V，µg/g	64	136
			Saturated hydrocarbons, wt.%	40.34	38.26
Aromatic hydrocarbons, wt.%	38.76	37.1
			Colloidal in wt%	18.53	20.52
Asphaltenes, wt.%	2.37	4.12

TABLE 2 Properties of fixed bed residuum hydroprocessing catalysts

Catalyst brand

FZC-12B

FZC-103D

FZC-103E

FZC-28A

FZC-204

FZC-34A

FZC-41A

Function(s)

Protecting agent

Demetallization catalyst

Desulfurization catalyst

Denitrification catalyst

Particle size, mm

3-10

2-8

Particle shape

Four-impeller

Bar shape

Strip shape

Bar shape

Strip shape

Strength, N.mm ^-1

6

10

16

18

20

26

Specific surface area, m ² /g

100

82

88

133

169

182

228

Make up of

Mo-Ni

Carrier

Al ₂ O ₃

TABLE 3 Properties of the upflow hydroprocessing catalyst

Catalyst brand	FZC-10U	FZC-11U
			Function(s)	Demetallization catalyst	Desulfurization catalyst
Particle shape	Spherical shape	Spherical shape
			Outer diameter of the granule mm	2.9	2.9
Strength, N.mm ^-1	32	30
			Specific surface area, m ² /g	110	148
Rate of wear, wt%	0.3	0.4
			Make up of	Mo-Ni	Mo-Ni
Carrier	Al ₂ O ₃	Al ₂ O ₃
			Metal content in the catalyst, wt%
MoO ₃	5.2	10.8
			NiO	1.2	2.4

Table 4 examples main operating conditions

Item	Example 1	Example 2	Example 3
				Upflow hydroprocessing catalyst numbering	FZC-10U and FZC-11U	FZC-10U and FZC-11U	FZC-10U and FZC-11U
Operating conditions of UFR reactor
				Partial pressure of hydrogen, MPa	16.6	16.6	16.2
Liquid hourly volume space velocity, h ^-1	0.20	0.12	0.14
				Volume ratio of hydrogen to oil	280	290	260
Reaction temperature of	380	384	377
				Fixed bed operating conditions
Partial pressure of hydrogen, MPa	16.4	16.4	16.0
				Reaction temperature, deg.C	375	372	373
Liquid hourly volume space velocity, h ^-1	0.23	0.17	0.19
				Volume ratio of hydrogen to oil	700	630	760
Total hydrogen consumption of chemical reaction%	1.64	1.67	1.56

TABLE 5 hydrogenation reaction product distribution

Item	Example 1	Example 2	Example 3
				Atmospheric and vacuum fractionation
Fuel gas (wt.%)	3.50	3.48	3.56
				Hydrogenated naphtha,% by weight	2.89	2.81	2.55
Hydrogenated diesel oil, wt%	9.32	9.11	8.64
				Hydrogenated vacuum residue, wt.%	37.93	35.53	40.07
Hydrogenation vacuum wax oil, wt%	46.36	49.07	45.18
				Is totaled	100.00	100.00	100.00

Table 6 example 1 key product properties

Hydrogenated product	Hydrogenated naphtha	Hydrogenated diesel oil	Hydrogenated vacuum wax oil	Hydrogenated vacuum residue
					Density (20 ℃ C.), g/cm ³	0.732	0.845	0.865	0.974
Viscosity (100 ℃ C.), mm ² /s	-	-	19	244
					Viscosity (50 ℃ C.), mm ² /s	-	-	79	-
Carbon residue value, wt%	-	-	0.21	9.34
					S，μg/g	51	220	2480	8218
N，μg/g	26	180	780	3877
					Ni+V，μg/g	-	-	-	25.5

Table 7 example 2 key product properties

Hydrogenated product	Hydrogenated naphtha	Hydrogenated diesel oil	Hydrogenated vacuum wax oil	Hydrogenated vacuum residue
					Density (20 ℃ C.), g/cm ³	0.732	0.847	0.874	0.975
Viscosity (100 ℃ C.), mm ² /s	-	-	26	285
					Viscosity (50 ℃ C.), mm ² /s	-	-	97	-
Carbon residue value, wt%	-	-	0.35	9.98
					S，μg/g	55	290	2465	8320
N，μg/g	46	228	1830	4560
					Ni+V，μg/g	-	-	-	26.3

Table 8 example 3 main product properties

Hydrogenated product	Hydrogenated naphtha	Hydrogenated diesel oil	Hydrogenated vacuum wax oil	Hydrogenated vacuum residue
					Density (20 ℃ C.), g/cm ³	0.735	0.844	0.868	0.976
Viscosity (100 ℃ C.), mm ² /s	-	-	23	267
					Viscosity (50 ℃ C.), mm ² /s	-	-	-	-
Carbon residue value, wt%	-	-	0.31	9.33
					S，μg/g	45	233	1743	7561
N，μg/g	22	180	1760	4322
					Ni+V，μg/g	-	-	-	22.3

TABLE 9 Low Sulfur Marine Fuel Primary product Properties

Item	Example 1	Example 2	Example 3
				Hydrogenated vacuum residue, wt.%	20.86	23.45	20.03
Hydrogenated vacuum wax oil, wt%	28.00	40.00	18.00
				Density (20 ℃ C.), g/cm ³	0.912	0.911	0.925
Viscosity (50 ℃ C.), mm ² /s	230	284	242
				S，µg/g	4930	4591	4808
Carbon residue in wt%	4.11	3.91	5.06
				Acid number (calculated as KOH), mg/g	0.022	0.022	0.021
Ash content, wt.%	0.03	0.02	0.03
				Carbon aromatic index CCAI	853	853	851
Ni+V，µg/g	10.89	9.72	11.75
				Saturated hydrocarbons, wt.%	57.16	57.25	58.14
Aromatic hydrocarbon wt%	31.21	30.43	29.45
				Colloidal, wt.%	10.67	11.23	11.73
Asphaltenes, wt.%	0.96	1.09	0.68

TABLE 10 Low Sulfur Marine Fuel Primary product Properties

Item	Example 1	Example 2	Example 3
				Hydrogenated vacuum residue, wt.%	20.86	23.45	20.03
Hydrogenation vacuum wax oil, wt%	45.00	30.00	38.00
				Density (20 ℃ C.), g/cm ³	0.900	0.918	0.905
Viscosity (50 ℃ C.), mm ² /s	178	362	153
				S，µg/g	4298	4989	3751
Carbon residue in wt%	3.10	4.58	3.42
				Acid number (calculated as KOH), mg/g	0.021	0.021	0.02
Ash content wt%	0.02	0.02	0.02
				Carbon aromatic index CCAI	851	852	851
Ni+V，µg/g	8.08	11.54	7.70

As can be seen from tables 9 and 10, in examples 1 to 3, blending hydrogenated wax oil with different proportions can meet the requirements of different viscosities, simultaneously meet the requirement that the sulfur content is less than 0.5%, and meet the requirement of fuel oil properties by other indexes. The hydrogenated wax oil has good quality, and can be used as a hydrocracking and catalytic cracking raw material to produce high-added-value products on one hand, and on the other hand, the hydrogenated normal slag can be adjusted and added with hydrogenated wax oil in different proportions to flexibly produce ship combustion products with different viscosities. The method of the invention can flexibly produce low-sulfur marine fuel products and can well meet the requirement of enterprises which want to increase the yield of light oil.

In addition, the hydrogenation vacuum residue is treated by the upflow hydrogenation reactor, so that the hydrogenation vacuum residue is deeply desulfurized, the saturated component mass fraction of the product is 57-59%, the aromatic component is about 30%, and the colloid content is 10-12%. The sum of the two is 40%. The inventor finds that the fixed bed hydrogenation causes the sum of aromatic components and colloid in the oil product to be excessively hydrogenated and saturated to be less than 35 percent, and influences the stability of the oil product system. Therefore, the invention can improve the stability of the marine fuel oil under various product index conditions.

Comparative example 1

The comparative example adopts a process route (see figure 2) of series connection of an upflow type and a fixed bed reactor, wherein a residual oil raw material A with relatively good property and a residual oil raw material B with relatively poor property (the properties of the residual oil raw materials are shown in a table 1) enter the upflow type reactor to carry out hydrogenation reaction, then enter the fixed bed reactor to carry out hydrogenation reaction, and the hydrogenation generated oil is fractionated to obtain fuel gas, hydrogenation naphtha, hydrogenation diesel oil and hydrogenation atmospheric residue. Hydrogenated atmospheric residue is used as a low sulfur ship combustion product. The mass ratio of the feeding quantity of the residual oil raw material A with relatively good properties to the feeding quantity of the residual oil raw material B with relatively poor properties is 1:1.

Three residual oil hydrogenation protective agents are reversely filled in one reactor, and the filling volumes of the three residual oil hydrogenation protective agents are 22mL of FZC-12B catalyst, 25mL of FZC-103D catalyst and 53mL of FZC-103E catalyst respectively; secondly, filling two residual oil hydrodemetallization catalysts in reverse direction, wherein the filling volumes are 82mL of FZC-28A catalyst and 118mL of FZC-204 catalyst respectively; and a residual oil hydrodesulfurization catalyst FZC-34A is filled in the three-way reaction, the filling volume is 123mL, and a denitrification and carbon residue removal catalyst FZC-41A is filled in the three-way reaction, and the filling volume is 77mL. The catalyst properties were the same as in example 1. Table 11 shows the main operating process conditions, table 12 shows the hydrogenation product distribution and table 13 shows the main product properties.

Table 11 comparative example 1 main operating conditions

Item	Comparative example 1
		Upflow catalyst numbering	FZC-10U and FZC-11U
Operating conditions of UFR reactor
		Partial pressure of hydrogen, MPa	16.6
Liquid hourly volume space velocity, h ^-1	0.29
		Volume ratio of hydrogen to oil	280
Reaction temperature of	385
		Fixed bed operating conditions
Partial pressure of hydrogen, MPa	16.4
		Reaction temperature of	387
Liquid hourly volume space velocity, h ^-1	0.20
		Volume ratio of hydrogen to oil	700
Total hydrogen consumption of chemical reaction%	1.75

TABLE 12 hydrogenation reaction product distribution

Item	Comparative example 1
		Hydrogenation reaction part
Fuel gas (wt.%)	4.18
		Hydrogenated naphtha,% by weight	3.72
Hydrogenated diesel oil, wt%	12.67
		Hydrogenated atmospheric residue, wt.%	79.43

TABLE 13 comparative example 1 Primary product Properties

Hydrogenated product	Hydrogenated naphtha	Hydrogenated diesel oil	Hydrogenated atmospheric residue
				Density (20 ℃ C.), g/cm ³	0.734	0.845	0.924
Viscosity (100 ℃ C.), mm ² /s	/	/	46
				Viscosity (50 ℃ C.), mm ² /s	/	/	363
Carbon residue value, wt%	/	/	4.05
				S，μg/g	61	280	4890
N，μg/g	26	215	2235
				Ni+V，μg/g	/	/	10.87
Saturated hydrocarbons, wt.%	/	/	66.38
				Aromatic hydrocarbons, wt.%	/	/	22.87
Colloidal, wt.%	/	/	9.10
				Asphaltenes, wt.%	/	/	1.65

As can be seen from Table 13, under the condition of processing the same feeding amount, the conventional upflow and fixed bed combined process is adopted in the comparative example 1, so that the content of impurities such as sulfur, nitrogen and carbon residue in the hydrogenated residual oil meets the index requirement, the higher reaction temperature is adopted, the upflow reaction temperature is 385 ℃, the fixed bed reaction temperature is 387 ℃, and meanwhile, the hydrogen consumption is far higher than that of the example 1. In addition, in order to meet the index requirements of the impurity content, especially the sulfur content, of the product, the yield of the light oil product of the hydrogenated product is increased at a higher reaction temperature, especially the yield of fuel gas is increased, the processing cost is increased, the yield of the hydrogenated residual oil of the target product is reduced, and the product yield is influenced. The hydrogenation slag property sulfur content is 0.4890%, but the viscosity (50 ℃) is 363 mm ² As a high viscosity ship fuel product only, blending other products is required if other low viscosity products are produced.

In addition, in the hydrogenated product obtained in comparative example 1, the yield of aromatic hydrocarbon was 22.87%, the gum content was 9.10%, and the sum of the two was less than 35%. It can be seen that the required hydrogenation depth for achieving impurity levels and viscosity is high, with a saturated hydrocarbon content of 66.38%. However, the high content of saturated hydrocarbon and the low content of colloid and aromatic hydrocarbon affect the stability of the oil system, are not beneficial to the storage and transportation of the marine fuel oil, and further affect the service performance of the marine fuel oil.

Claims

1. A process for the hydroprocessing of bunker fuel oil, comprising:

(2) Mixing part of hydrogenated vacuum residue obtained in the step (1) with residue raw material with relatively poor property and hydrogen, and allowing the mixture to enter an up-flow hydrogenation reactor for a second hydrofining reaction to obtain an up-flow hydrogenation reactor effluent;

(3) Mixing part of hydrogenated vacuum residue oil obtained in the step (1) with at least part of hydrogenated vacuum wax oil to obtain a bunker fuel oil product;

wherein, the residual oil raw material with relatively inferior properties contains more than 3.5 percent of sulfur and more than 100 mu g/g of total content of heavy metal nickel and vanadium by mass content; the residual oil raw material with relatively good properties contains, by mass, not more than 3.5% of sulfur and not more than 100 mu g/g of total content of heavy metal nickel and vanadium;

taking the total feeding mass of the residual oil raw material with relatively poor properties and the residual oil raw material with relatively good properties as a reference, the residual oil raw material with relatively good properties accounts for 10% -90% of the total feeding mass, and the residual oil raw material with relatively poor properties accounts for 10% -90% of the total feeding mass;

the mass of the hydrogenation vacuum residue entering the upflow hydrogenation reactor in the step (2) accounts for 10-80% of the total mass of the hydrogenation vacuum residue obtained in the step (1); the mass of the hydrogenated vacuum residue serving as the marine fuel oil component in the step (3) accounts for 20-90% of the total mass of the hydrogenated vacuum residue obtained in the step (1).

2. The method of claim 1, wherein: the residual oil raw material in the step (1) comprises at least one of atmospheric residual oil or vacuum residual oil, wherein the sulfur content in the residual oil raw material is not higher than 5.0 percent, the Conradson carbon residue is not higher than 18 percent, the total content of heavy metal nickel and vanadium is not higher than 200 mu g/g, and the total nitrogen content is not higher than 0.80 percent.

3. A method as claimed in claim 2, characterized in that: in the residual oil raw material, the content of the Conradson carbon residue is 9-14% and the content of the total nitrogen is 0.25-0.70% by mass.

4. The method of claim 1, wherein: based on the total feeding mass of the residual oil raw materials with relatively poor properties and the residual oil raw materials with relatively good properties, the residual oil raw materials with relatively good properties account for 30% -70% of the total feeding mass, and the residual oil raw materials with relatively poor properties account for 30% -70% of the total feeding mass.

5. The method of claim 1, wherein: the mass of the hydrogenation vacuum residue entering the upflow hydrogenation reactor in the step (2) accounts for 20-50% of the total mass of the hydrogenation vacuum residue obtained in the step (1); the mass of the hydrogenated vacuum residue serving as the marine fuel oil component in the step (3) accounts for 50-80% of the total mass of the hydrogenated vacuum residue obtained in the step (1).

6. The method of claim 1, wherein: in the step (3), the mixing mass ratio of the hydrogenated vacuum residue oil to the hydrogenated vacuum wax oil is 0.50-7: 1.

7. the method of claim 1, wherein: the hydrogen used in the fixed bed hydrogenation unit is recycle hydrogen, and the hydrogen used in the upflow hydrogenation reactor is fresh hydrogen.

8. The method of claim 1, wherein: the first hydrofining reaction in the step (1) adopts a fixed bed residual oil hydrotreating technology.

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

10. The method of claim 9, wherein: taking the total filling volume of the fixed bed residual oil hydrotreating catalyst as a reference, wherein the residual oil hydrodemetallization catalyst accounts for 20-50% of the total filling volume; the residual oil hydrodesulfurization catalyst accounts for 20-48% of the total filling volume.

11. A method according to claim 1, 8 or 9, characterized by: the conditions of the first hydrofining reaction in step (1) are as follows: the hydrogen partial pressure is 5MPa to 35MPa, the reaction temperature is 300 ℃ to 420 ℃, and the total feeding liquid hourly space velocity is 0.1h ^-1 ～5.0h ^-1 The volume ratio of the total hydrogen to the oil is 100-5000.

12. The method of claim 11, wherein: the conditions of the first hydrofining reaction in step (1) are as follows: the hydrogen partial pressure is 13MPa to 20MPa, the reaction temperature is 330 ℃ to 400 ℃, and the total feeding liquid hourly space velocity is 0.15h ^-1 ～2.0h ^-1 The volume ratio of the total hydrogen oil is 300-3000.

13. The method of claim 1, wherein: the hydrogenation generated oil obtained in the step (1) is fractionated under normal pressure, and the initial boiling point of the obtained hydrogenation atmospheric residue oil is 330-370 ℃; the initial boiling point of the hydrogenation vacuum residue oil is 520-540 ℃, the initial boiling point of the hydrogenation vacuum wax oil is 330-370 ℃, and the final boiling point is 520-540 ℃.

14. The method of claim 1, wherein: and (2) adopting an upflow hydrogenation reactor residual oil hydrotreating technology.

15. The method of claim 1, wherein: in the up-flow hydrogenation reactor, the hydrogenation protection catalyst accounts for less than 20% of the total filling volume; the hydrodemetallization catalyst accounts for 20-80% of the total filling volume; the hydrodesulfurization catalyst accounts for 5-70% of the total packing volume.

16. The method of claim 15, wherein: in the up-flow hydrogenation reactor, the hydrogenation protection catalyst accounts for 5-20% of the total loading volume; the hydrodemetallization catalyst accounts for 35-75% of the total filling volume; the hydrodesulfurization catalyst accounts for 10-65% of the total packing volume.

17. A method according to claim 1 or 10, characterized in that: the reaction conditions of the second hydrofining reaction in step (2) are as follows: the hydrogen partial pressure is 12MPa to 35MPa, the reaction temperature is 350 ℃ to 500 ℃, and the total feeding liquid hourly space velocity is 0.1h ^-1 ～5.0h ^-1 The volume ratio of the total hydrogen oil is 200-400.

18. The method of claim 17, wherein: the reaction conditions of the second hydrofining reaction in the step (2) are as follows: the hydrogen partial pressure is 15MPa to 22MPa, the reaction temperature is 380 ℃ to 420 ℃, and the hourly space velocity of the total feed liquid is 0.15h ^-1 ～2.0h ^-1 The volume ratio of the total hydrogen to the oil is 210-350.