CN114806638B

CN114806638B - Production method of low-sulfur marine fuel oil

Info

Publication number: CN114806638B
Application number: CN202110068055.6A
Authority: CN
Inventors: 孟兆会; 葛海龙; 杨涛; 张文芳; 刘玲; 仝玉军; 殷冬冬
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: 2021-01-19
Filing date: 2021-01-19
Publication date: 2023-02-03
Anticipated expiration: 2041-01-19
Also published as: CN114806638A

Abstract

The invention provides a method for producing low-sulfur marine fuel oil, which comprises the steps of pretreating inferior hydrocarbon-containing raw materials, and separating to obtain a 1 st liquid-phase material flow; separating the reaction product obtained after the hydrogenation reaction of the 1 st liquid phase material flow to obtain a 2 nd liquid phase material flow and a 3 rd liquid phase material flow; treating the 3 rd liquid phase material flow with a treating agent, and separating to obtain a 4 th liquid phase material flow and a 5 th liquid phase material flow, wherein the 4 th liquid phase material flow is subjected to sedimentation separation to obtain a 6 th liquid phase material flow and a 7 th liquid phase material flow; and (3) circulating and recycling hydrogenated heavy fractions obtained after the 7 th liquid phase material flow is subjected to hydrogenation reaction, and mixing the obtained 2 nd liquid phase material flow, the 5 th liquid phase material flow and the 6 th liquid phase material flow to obtain the low-sulfur marine fuel oil. The production method provided by the invention has the advantages of simple process flow, cheap and easily-obtained raw materials and low production cost, and can meet the requirement of realizing mass production.

Description

Production method of low-sulfur marine fuel oil

Technical Field

The invention belongs to the field of oil refining chemical industry, relates to a fuel oil production method, and particularly relates to a method for producing marine fuel oil by hydrogenation.

Background

The MAPPOL convention provides detailed regulations on the emission control region of fuel oil sulfur content used by a ship, the limit value and the implementation time of the fuel oil sulfur content, and the sulfur content of the fuel oil for the ship is not more than 0.5% when the ship sails in a general region on the sea after 1 month 1 day 2020; when sailing in the emission control area, the sulfur content of the fuel used on the ship should not exceed 0.1 percent. Research shows that the sulfur content of the conventional bunker fuel oil is generally controlled to be 3.5%, and the low-sulfur fuel oil has a huge gap if the use requirement of MAPPOL convention on the sulfur content of the fuel oil is strictly implemented. The current low-sulfur ship fuel production technology mainly uses low-sulfur crude oil as a raw material, and can be used as low-sulfur ship fuel oil or blending components by simple distillation and proper increase of viscosity. On one hand, the low-sulfur crude oil resource is limited, and the low-sulfur ship combustion gap is difficult to make up; on the other hand, the low sulfur crude oil has a relatively high price, which is not favorable for realizing the requirement of low cost of the low sulfur fuel oil. In order to meet the requirements of low-cost and large-scale production of low-sulfur marine fuel oil products, a more reasonable low-sulfur marine fuel oil production technology is urgently needed to be developed.

Patent CN 106753611A introduces a bunker fuel oil and a production process and a production device thereof, and specifically relates to a method for producing bunker fuel oil by blending FCC slurry oil, coal tar, catalytic diesel oil, methanol, ethanol, shale oil, vacuum residue oil and an auxiliary agent according to a certain proportion, and in order to reduce the influence of catalyst powder in the FCC slurry oil on blended products, the invention adopts an improved electrostatic separation device to realize the de-solidification of the FCC slurry oil. The patent of the invention requires a plurality of blending components, and the implementation difficulty in actual production is larger.

Patent CN 103642539A introduces a blending method of bunker fuel oil, which comprises the following specific steps of naturally settling FCC slurry oil and thermal cracking residual oil, filtering with a filter screen, removing catalyst fine powder and other impurities contained in raw materials, adding hydrogenation tail oil and ethylene tar into a blending tank in advance, gradually heating, stirring until the FCC slurry oil and the thermal cracking residual oil are uniformly mixed, adding the treated FCC slurry oil and the thermal cracking residual oil into the blending tank, raising the temperature, uniformly mixing the components, sequentially adding a desulfurizing agent, a cosolvent and a combustion improver into the blending tank, and uniformly mixing the components to obtain a final product. According to the method, the standing sedimentation is adopted to treat the catalyst powder in the FCC oil slurry, the catalyst powder in the FCC oil slurry is high in content and small in particle size (mostly below 25 mu m), practice proves that the catalyst powder is difficult to remove by adopting the standing sedimentation alone, the requirement on the content of precipitates in the low-sulfur ship fuel index is high, the doping amount of the catalytic oil slurry containing the catalyst powder is limited, and the production process is complex comprehensively.

Disclosure of Invention

The invention aims at the problems that the traditional low-sulfur ship fuel production technology has high cost, and the solid content of a low-sulfur ship fuel product exceeds the standard and the operation period of a device is influenced because the system is easy to be unstable when inferior residual oil is used as a raw material for carrying out deep hydrogenation desulfurization, and the like. The production method provided by the invention has the advantages of simple process flow, cheap and easily-obtained raw materials and low production cost, and can meet the requirement of realizing mass production.

The invention provides a production method of low-sulfur marine fuel oil, which comprises the following steps:

(1) Under the contact condition, the inferior hydrocarbon-containing raw material reacts with the resin catalyst, and the material after the reaction is subjected to gas-liquid separation to obtain a 1 st liquid phase material flow;

(2) Under the existence of hydrogen and a boiling bed hydrogenation catalyst, the 1 st liquid phase material flow obtained in the step (1) enters a boiling bed hydrogenation reaction zone for hydrogenation reaction, and a 2 nd liquid phase material flow and a 3 rd liquid phase material flow are obtained after reaction products are separated;

(3) Treating the 3 rd liquid phase flow obtained in the step (2) with a treating agent under a contact condition, and treating and separating to obtain a 4 th liquid phase flow and a 5 th liquid phase flow, wherein the 4 th liquid phase flow enters a separation tower and is subjected to settling separation to obtain a 6 th liquid phase flow and a 7 th liquid phase flow;

(4) Feeding the 7 th liquid phase material flow obtained in the step (3) into a supplementary hydrogenation reactor, carrying out hydrogenation reaction in the presence of hydrogen and a supplementary hydrogenation catalyst, and circulating hydrogenated heavy fraction obtained after hydrogenation reaction back to a fluidized bed hydrogenation reaction zone for treatment;

(5) And (3) mixing the 2 nd liquid phase flow obtained in the step (2), the 5 th liquid phase flow obtained in the step (3) and the 6 th liquid phase flow to obtain the low-sulfur marine fuel oil.

Further, in the above technical solution, the inferior hydrocarbon-containing material in step (1) may be one or more of atmospheric residue, vacuum residue, oil sand bitumenOne or more of partial wax oil and catalytic diesel oil can be blended. The kinematic viscosity (100 ℃) of the poor hydrocarbon-containing raw material is 2000 to 8000mm ² /s。

Furthermore, in the above technical solution, the resin catalyst in step (1) may specifically be a polystyrene resin catalyst, and the average pore diameter of the polystyrene resin catalyst is 10 to 500nm, preferably 30 to 100nm. The preparation method of the catalyst comprises the steps of taking styrene as a monomer, carrying out polymerization reaction to generate a polyethylene polymer, then carrying out sulfonation reaction with concentrated sulfuric acid, and adding a pore-forming agent in the sulfonation process of polystyrene so as to generate a multifunctional structure with large pore diameter and porous channel distribution on the surface and inside of polystyrene resin.

Further, in the above technical scheme, the reaction conditions in step (1) are as follows: the reaction temperature is 300-430 ℃, and the preferable reaction temperature is 350-420 ℃; the reaction pressure is 0.15MPa to 5.0MPa, and the preferable reaction pressure is 0.45MPa to 3.0MPa; the volume space velocity is 0.5 to 4.0h ^-1 The preferred volume space velocity is 1.0-3.0 h ^-1 。

Further, in the above technical scheme, the ebullated-bed hydrogenation reaction zone in step (2) is provided with at least one ebullated-bed hydrogenation reactor, preferably 1 or 2 ebullated-bed hydrogenation reactors, and when more than 2 ebullated-bed hydrogenation reactors are provided, the plurality of ebullated-bed hydrogenation reactors may be connected in series and/or in parallel. The fluidized bed hydrogenation reactor preferably adopts a fluidized bed reactor with a built-in three-phase separator, and specifically can adopt a fluidized bed reactor with a built-in three-phase separator developed by the petrochemical industry research institute of China.

Further, in the above technical scheme, the fluidized bed hydrogenation catalyst in step (2) may be one or more of the existing fluidized bed hydrogenation catalysts in the field, such as fluidized bed hydrogenation catalysts developed by petrochemical corporation, in china, and may specifically be commercial catalysts under the trade designations FES-30 and FEM-10 developed by the franchise petrochemical research institute, or may be a TEX2720 catalyst purchased from the market. Typically, the ebullated bed is hydrogenatedThe catalyst comprises a carrier and active metal, wherein the active metal can be one or more of nickel, cobalt, molybdenum or tungsten; the catalyst composition may include, in weight percent: 0.5-10% of nickel or cobalt (calculated according to the oxide thereof), 1-25% of molybdenum or tungsten (calculated according to the oxide thereof), and the carrier can be one or more of alumina, silica, alumina-silica or titanium oxide. The catalyst is in the shape of extrudate or sphere, and the bulk density is 0.5-0.9 g/cm ³ The diameter of the particles (spherical diameter or strip diameter) is 0.04-1.0 mm, and the specific surface area is 80-300 m ² /g。

Further, in the above technical solution, the operating conditions of the ebullated-bed hydrogenation reaction zone in the step (2) are as follows: the reaction temperature is 380-450 ℃, the reaction pressure is 13 MPa-20.0 MPa, and the volume space velocity is 0.2-4.0 h ^-1 The hydrogen-oil volume ratio is 300-1500, and the preferred operating conditions are as follows: the reaction temperature is 400-440 ℃, the reaction pressure is 14-18.0 MPa, and the volume space velocity is 0.3-1.5 h ^-1 The volume ratio of hydrogen to oil is 600-1000.

Further, in the above technical solution, the temperature of the division point of the 2 nd liquid phase stream and the 3 rd liquid phase stream in the step (2) is 480 to 560 ℃, preferably 500 to 540 ℃.

Further, in the above technical solution, the treating agent in step (3) may be one or more of propane, n-butane, isobutane, n-pentane, isopentane, and naphtha, preferably one or more of n-butane, isopentane, and naphtha; furthermore, the volume ratio of n-butane to isopentane is 4.

Further, in the above technical solution, the treatment conditions in step (3) are as follows: the pressure is 4.0-8.0 MPa, the treatment temperature is 130-170 ℃, the volume ratio of the treating agent to the No. 3 liquid phase material flow is 2-1, and the preferable treatment conditions are as follows: the pressure is 4.5-6.5 MPa, the treatment temperature is 135-160 ℃, and the volume ratio of the treating agent to the No. 3 liquid phase material flow is 4.

Further, in the above technical scheme, the temperature of the separation tower in the step (3) is controlled to be 160-190 ℃, preferably 150-170 ℃, a 6 th liquid phase material flow is obtained at the top of the separation tower, and a 7 th liquid phase material flow is obtained at the bottom of the separation tower.

Further, in the above technical solution, the operating conditions of the make-up hydrogenation reactor in step (4) are as follows: the reaction temperature is 350-400 ℃, the reaction pressure is 10-15.0 MPa, and the volume space velocity is 0.8-3.0 h ^-1 Hydrogen-oil volume ratio of 200-1000, and the preferred operating conditions are as follows: the reaction temperature is 360-380 ℃, the reaction pressure is 11 MPa-14.0 MPa, and the volume space velocity is 1.0-2.0 h ^-1 The volume ratio of hydrogen to oil is 250-400.

Further, in the above technical scheme, the supplementary hydrogenation catalyst loaded in the supplementary hydrogenation reactor in step (4) may be one or more of the existing hydrofining catalysts in the field, may be a commercially available product, or may be prepared according to the existing method.

Further, in the above technical solution, the mass ratio of the hydrogenated heavy components obtained after the reaction obtained in step (3) in step (4) to the poor hydrocarbon-containing raw material can be generally controlled to be 1.

Compared with the prior art, the production method of the low-sulfur marine fuel oil provided by the invention has the following advantages:

1. the invention relates to a low-sulfur marine fuel oil production method, which is characterized in that a pretreatment reactor is arranged, an inferior heavy oil raw material is contacted with a treating agent, the molecular structure of a residual oil system can be changed under the action of the treating agent, and the viscosity and the impurity content of the residual oil system are reduced.

2. According to the invention, the heavy fraction obtained after hydrogenation reaction in the fluidized bed is separated, and then the heavy fraction obtained after separation is returned to the hydrogenation reaction zone in the fluidized bed after hydrogenation, and research processes show that the return of the heavy fraction after hydrogenation to the hydrogenation reaction zone in the fluidized bed can greatly improve the stability of a hydrogenation system in the fluidized bed, and is beneficial to improving the running stability of the device.

3. In the method for producing the low-sulfur marine fuel oil, the low-sulfur marine fuel oil with the sulfur content of less than 0.5 percent can be produced by taking the inferior residual oil as the raw material. Compared with the prior technical routes of blending and producing the bunker fuel oil by using low-sulfur crude oil or high-quality light components and the like, the method has the advantages of lower cost, wider raw material source and low price.

Drawings

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

Detailed Description

The following detailed description of the embodiments of the present invention will be described with reference to the accompanying drawings and specific examples, but it should be noted that the scope of the present invention is not limited by these embodiments, but is defined by the claims.

All percentages, parts, ratios, etc. referred to in this specification are by weight unless otherwise specifically indicated.

In the context of this specification, any two or more embodiments of the invention may be combined in any combination, and the resulting solution is part of the original disclosure of this specification, and is within the scope of the invention.

As shown in fig. 1, the present invention provides a method for producing low-sulfur bunker fuel oil, comprising the following steps: the inferior hydrocarbon-containing material 1 enters a preprocessor 2 to contact with a resin catalyst for reaction, and the reacted material enters a gas-liquid separator 4 to obtain gas 3 and a 1 st liquid phase material flow 5 after gas-liquid separation; the obtained 1 st liquid phase material flow 5 and hydrogen 6 enter a fluidized bed hydrogenation reaction zone 7 for hydrogenation reaction, and the reaction product enters a gas-liquid separation unit 8 for separation to obtain a 2 nd liquid phase material flow 9 and a 3 rd liquid phase material flow 10; mixing the obtained 3 rd liquid phase material flow 10 with a treating agent 11, then, sending the mixture into a processor 12 for treatment, and obtaining a 4 th liquid phase material flow 13 and a 5 th liquid phase material flow 19 after treatment and separation, wherein the 4 th liquid phase material flow enters a separation tower 14 for settling and separation to obtain a 6 th liquid phase material flow 15 and a 7 th liquid phase material flow 16; the obtained 7 th liquid phase material flow 16 and hydrogen 6 enter a supplementary hydrogenation reactor 17, hydrogenation reaction is carried out in the presence of a supplementary hydrogenation catalyst, and the hydrogenated 7 th liquid phase material flow 18 obtained after hydrogenation reaction is circulated back to the fluidized bed hydrogenation reaction zone 7 for treatment; the resulting 2 nd

liquid phase stream

9, 5 th

liquid phase stream

19 and 6 th liquid phase stream 15 can be combined to obtain the low sulfur bunker fuel oil.

The raw materials used in the examples of the present invention and the comparative examples were vacuum residue, and specific raw material properties are shown in table 1.

The treating agent used in the pretreatment reactors of the examples and comparative examples of the present invention was a polystyrene resin catalyst having an average pore diameter of 30 to 100nm, an average resin catalyst diameter of 0.45mm and a specific surface area of 21m ² G, average pore volume 0.26cm ³ (ii) in terms of/g. The polystyrene resin catalyst can be prepared according to the prior method, and D072 styrene resin can be washed by distilled water to be colorless, and then H with the volume concentration of 30 percent ₂ SO ₄ Washing to strong acidity, washing to neutrality with distilled water, washing with NaOH with volume concentration of 45%, washing to neutrality with distilled water, soaking sodium metaaluminate compound, soaking the washed styrene resin in 500mL sulfuric acid solution, stirring at room temperature for 12 hr, washing to neutrality with distilled water, and drying at 100 deg.C for 8 hr.

The fluidized bed hydrogenation reaction zone uses a fluidized bed reactor, in particular to a fluidized bed hydrogenation reactor with a built-in three-phase separator developed by the company of petrochemical industry limited in China. The fluidized bed hydrogenation catalyst adopts a commercial grade FES-30 microspheric fluidized bed hydrogenation catalyst developed by the comforting petrochemical research institute. The supplementary hydrogenation reactor adopts FF-66 hydrogenation catalyst developed by the research institute of the comforting petrochemical industry.

Example 1

Example 1 vacuum residue as a feedstock, the first step of the process of the invention was to start with vacuum residueThe mixture is put into a pretreatment reactor for pretreatment reaction, and the reaction conditions of the pretreatment reactor are as follows: reaction temperature: the reaction pressure is 0.65MPa at 360 ℃, and the volume space velocity is 1.5h ^-1 Then, after gas-liquid separation, the liquid phase enters a fluidized bed hydrogenation reactor for deep impurity removal reaction, and the reaction conditions of the hydrogenation reaction zone are as follows: reaction temperature: the reaction pressure is 14MPa at 420 ℃, and the volume space velocity is 0.45h ^-1 Hydrogen to oil volume ratio 800. The split point temperature of the 2 nd and 3 rd liquid phase streams is 510 ℃; the treating agents are n-butane and isopentane, the volume ratio of n-butane to isopentane is 1, the pressure is 5.0MPa, the treating temperature is 145 ℃, the solvent ratio is 5. Operating conditions of the make-up hydrogenation reactor: the reaction temperature is 370 ℃, the reaction pressure is 13.0MPa, and the volume space velocity is 1.8h ^-1 Hydrogen to oil volume ratio 300. And (3) recycling the hydrogenated heavy fraction to the fluidized bed hydrogenation reactor, wherein the mass ratio of the hydrogenated heavy fraction to the vacuum residue is 1. The specific test results are shown in tables 2 and 3.

Example 2

Example 1 using vacuum residue as a raw material, according to the method of the present invention, vacuum residue first enters a pretreatment reactor for a pretreatment reaction, and the reaction conditions of the pretreatment reactor are as follows: reaction temperature: the reaction pressure is 0.65MPa at 360 ℃, and the volume space velocity is 1.5h ^-1 Then, after gas-liquid separation, the liquid phase enters a fluidized bed hydrogenation reactor for deep impurity removal reaction, and the reaction conditions of the hydrogenation reaction zone are as follows: reaction temperature: the reaction pressure is 14MPa at 420 ℃, and the volume space velocity is 0.45h ^-1 Hydrogen to oil volume ratio 800. The split point temperature of the 2 nd and 3 rd liquid phase streams was 510 ℃. The treating agent is naphtha, the pressure is 5.0MPa, the temperature is 145 ℃, the solvent ratio is 5; operating conditions of the make-up hydrogenation reactor: the reaction temperature is 370 ℃, the reaction pressure is 13.0MPa, and the volume space velocity is 1.5h ^-1 Hydrogen to oil volume ratio 300; and (3) recycling the hydrogenated heavy fraction to the fluidized bed hydrogenation reactor, wherein the mass ratio of the hydrogenated heavy fraction to the vacuum residue is 1. The specific test results are shown in tables 2 and 3.

Example 3

Example 1 vacuum residue as feedstock by the process of the inventionOil firstly enters a pretreatment reactor for pretreatment reaction, and the reaction conditions of the pretreatment reactor are as follows: reaction temperature: the reaction pressure is 0.65MPa at 360 ℃, and the volume space velocity is 1.5h ^-1 Then, after gas-liquid separation, the liquid phase enters a fluidized bed hydrogenation reactor for deep impurity removal reaction, and the reaction conditions of the hydrogenation reaction zone are as follows: reaction temperature: 430 ℃, the reaction pressure is 14MPa, and the volume space velocity is 0.45h ^-1 Hydrogen to oil volume ratio 800. The split point temperature of the 2 nd and 3 rd liquid phase streams is 530 ℃. The treating agent is naphtha. The pressure is 5.0MPa, the temperature is 145 ℃, the solvent ratio is 5; operating conditions of the make-up hydrogenation reactor: the reaction temperature is 370 ℃, the reaction pressure is 13.0MPa, and the volume space velocity is 1.3h ^-1 Hydrogen to oil volume ratio 300; and (3) recycling the hydrogenated heavy fraction to the fluidized bed hydrogenation reactor, wherein the mass ratio of the hydrogenated heavy fraction to the vacuum residue is 1. The specific test results are shown in tables 2 and 3.

Comparative example 1

The process is substantially the same as example 1, except that a pretreatment reactor and a supplementary hydrogenation reactor are not provided, and the separated 7 th liquid phase is directly sent to a fluidized bed hydrogenation reaction zone without supplementary hydrogenation. The specific test results are shown in tables 2 and 3.

Comparative example 2

Essentially the same as example 1, except that no pretreatment reactor was provided, the poor quality hydrocarbonaceous feedstock was passed directly to the ebullated bed hydrogenation reaction zone without any treatment. The specific test results are shown in tables 2 and 3.

TABLE 1 Properties of the raw materials

TABLE 2 results of the reaction

TABLE 3 operating cycle of ebullated bed reactor for different embodiments

The embodiment and the comparative example show that the production method for producing the low-sulfur marine fuel oil by the fluidized bed hydrogenation reduces the difficulty of residual oil macromolecule hydrogenation reaction by arranging the pretreatment reactor, improves the stability of a fluidized bed hydrogenation system by arranging the hydrogen supplement hydrogenation reactor to circulate the hydrogenated heavy oil back to the fluidized bed reactor, reduces the content of toluene insoluble substances in the generated oil, improves the online rate of an auxiliary fractionation system of a fluidized bed hydrogenation unit while realizing the production of the low-sulfur marine fuel oil by deep desulfurization, and improves the operation stability.

Claims

1. A method for producing low-sulfur marine fuel oil, comprising the following steps:

(1) Under the contact condition, the inferior hydrocarbon-containing raw material reacts with the resin catalyst, and the material after the reaction is subjected to gas-liquid separation to obtain a 1 st liquid phase material flow; the resin catalyst is a polystyrene resin catalyst, and the average pore diameter of the polystyrene resin catalyst is 10-500 nm; the reaction conditions were as follows: the reaction temperature is 300-430 ℃, the reaction pressure is 0.15-5.0 MPa, and the volume space velocity is 0.5-4.0 h ^-1 ；

(2) Under the existence of hydrogen and a boiling bed hydrogenation catalyst, the 1 st liquid phase material flow obtained in the step (1) enters a boiling bed hydrogenation reaction zone for hydrogenation reaction, and the reaction product is separated to obtain an upper light component 2 nd liquid phase material flow and a lower heavy component 3 rd liquid phase material flow; the temperature of the division point of the upper light component 2 nd liquid phase flow and the lower heavy component 3 rd liquid phase flow is between 480 and 560 ℃; the operating conditions of the ebullated-bed hydrogenation reaction zone were as follows: the reaction temperature is 380-450 ℃, the reaction pressure is 13 MPa-20.0 MPa, and the volume space velocity is 0.2-4.0 h ^-1 The volume ratio of the hydrogen to the oil is 300-1500,

(3) Under the contact condition, treating the 3 rd liquid phase flow of the lower heavy component obtained in the step (2) with a treating agent, and separating to obtain a 4 th liquid phase flow of the upper light component and a 5 th liquid phase flow of the lower heavy component, wherein the 4 th liquid phase flow of the upper light component enters a separation tower to be settled and separated to obtain a 6 th liquid phase flow and a 7 th liquid phase flow; the treating agent is one or more of propane, n-butane, isobutane, n-pentane, isopentane and naphtha; the conditions of the treatment were as follows: the pressure is 4.0-8.0 MPa, the treatment temperature is 130-170 ℃, and the volume ratio of the treating agent to the No. 3 liquid phase material flow of the lower heavy component is 2; controlling the temperature of the separation tower to be 150-190 ℃, obtaining a 6 th liquid phase material flow at the top of the separation tower and a 7 th liquid phase material flow at the bottom of the separation tower;

(4) Feeding the 7 th liquid phase material flow obtained in the step (3) into a supplementary hydrogenation reactor, carrying out hydrogenation reaction in the presence of hydrogen and a supplementary hydrogenation catalyst, and circulating hydrogenated heavy fraction obtained after hydrogenation reaction to a fluidized bed hydrogenation reaction zone for treatment; the make-up hydrogenation reactor operating conditions were as follows: the reaction temperature is 350-400 ℃, the reaction pressure is 10-15.0 MPa, and the volume space velocity is 0.8-3.0 h ^-1 The volume ratio of hydrogen to oil is 200-1000;

2. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein said low-quality hydrocarbon-containing feedstock in step (1) is one or more of atmospheric residue, vacuum residue, oil sand bitumen, with or without blending one or more of partial wax oil and catalytic diesel oil.

3. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein said polystyrene resin catalyst in step (1) has an average pore diameter of 30 to 100nm.

4. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein the reaction conditions in step (1) are as follows: the reaction temperature is 350-420 ℃; the reaction pressure is 0.45MPa to 3.0MPa; the volume space velocity is 1.0 to 3.0h ^-1 。

5. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein said ebullated-bed hydrogenation reaction zone in step (2) is provided with at least one ebullated-bed hydrogenation reactor.

6. The method for producing low-sulfur bunker fuel oil according to claim 1 or 5, wherein 1 or 2 ebullated-bed hydrogenation reactors are provided in the ebullated-bed hydrogenation reaction zone in the step (2).

7. The method for producing low-sulfur bunker fuel oil according to claim 5, wherein when 2 or more ebullated-bed hydrogenation reactors are provided, the 2 or more ebullated-bed hydrogenation reactors are connected in series and/or in parallel.

8. The process for producing low-sulfur bunker fuel oil according to claim 1, wherein the operating conditions of the ebullated-bed hydrogenation reaction zone in the step (2) are as follows: the reaction temperature is 400-440 ℃, the reaction pressure is 14 MPa-18.0 MPa, and the volume space velocity is 0.3-1.5 h ^-1 The volume ratio of hydrogen to oil is 600-1000.

9. The low sulfur bunker fuel oil production process of claim 1, wherein the split point temperature of the 2 nd and 3 rd liquid phase streams in step (2) is from 500 to 540 ℃.

10. A method for producing low sulfur bunker fuel oil as claimed in claim 1, wherein said treating agent in step (3) is one or more of n-butane and isopentane, naphtha.

11. A process for the production of low sulfur bunker fuel oil as claimed in claim 10 wherein the volume ratio of n-butane to isopentane is from 4.

12. A process for producing low-sulfur bunker fuel oil according to claim 10, wherein the volume ratio of n-butane to isopentane is from 2.

13. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein the conditions of said treatment in the step (3) are as follows: the pressure is 4.5-6.5 MPa, the treatment temperature is 135-160 ℃, and the volume ratio of the treating agent to the No. 3 liquid phase material flow is 4.

14. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein the temperature of said separation column in step (3) is controlled to 160 to 170 ℃.

15. The process for the production of low sulfur bunker fuel oil of claim 1 wherein said supplemental hydrogenation reactor operating conditions in step (4) are as follows: the reaction temperature is 360-380 ℃, the reaction pressure is 11 MPa-14.0 MPa, and the volume space velocity is 1.0-2.0 h ^-1 The volume ratio of hydrogen to oil is 250-400.

16. The method for producing low-sulfur bunker fuel oil according to claim 1, wherein the mass ratio of the heavy fraction after hydrogenation to the poor-quality hydrocarbon-containing raw material in the step (4) is controlled to be 1.

17. The method for producing low-sulfur bunker fuel oil according to claim 1 or 16, wherein the mass ratio of the heavy fraction after hydrogenation to the inferior hydrocarbonaceous feedstock in step (4) is controlled to be 1.