CN105542843B - Boiling bed residue oil hydrogenation method - Google Patents

Abstract

A method for hydrogenation of ebullated-bed residual oil. The raw material of residual oil enters the ebullated-bed hydrogenation reactor and the hydrogen is subjected to a hydrogenation reaction under the action of an ebullated-bed hydrogenation catalyst to obtain hydrogenated oil, which is separated under high pressure The liquid phase separated by the high-pressure separator is fractionated into gas, naphtha fraction, diesel fraction and hydrogenated atmospheric residue in the fractionation tower. The present invention can carry out hydrogenation reaction on low-quality residual oil raw materials, remove most of the impurities such as sulfur and metals in the raw materials, greatly reduce the residual carbon value, and obtain hydrogenated atmospheric pressure residual oils as raw materials for catalytic cracking, which improves the Utilization rate of inferior raw material oil.

Description

A kind of fluidized bed residual oil hydrogenation method

technical field

The invention relates to a method for hydrogenation using ebullating bed, more specifically, a method for hydrogenating residual oil in ebullating bed to produce catalytic cracking raw material.

Background technique

The efficient utilization and clean processing of heavy oil is becoming a major topic of concern in the global oil refining industry. Coking, solvent deasphalting and other processes have a large number of low-value by-products, which affect the utilization efficiency and economic benefits of residual oil. Hydrogenation of residual oil can simultaneously meet the requirements of efficient utilization of heavy oil and environmental protection. Four process types have been developed for residual oil hydrogenation: fixed bed, ebullating bed, slurry bed and moving bed. Among the four process types, the fixed bed process is mature, easy to operate, and relatively low device investment; hydrogenated residue can be used as RFCC feed. However, the operation period of the fixed bed is greatly affected by the impurity content of the raw material. For the raw material with high Ni and V metal content, the metal will be deposited in the micropores of the catalyst during the hydrogenation reaction, which will block the micropores of the catalyst and cause catalyst deactivation, which seriously affects The operation cycle of the residual oil hydrogenation unit; for raw materials with too high metal calcium and iron in the raw material, calcium and iron are easy to deposit on the surface of the catalyst and in the gaps between the catalyst particles, blocking the catalyst pores and causing catalyst deactivation , and cause the bed pressure drop to rise rapidly, and the operation cycle is shorter. As crude oil becomes heavier and inferior, more and more residues are no longer suitable for fixed-bed residue hydrotreating.

The ebullating bed hydrogenation process can overcome the problem of too short operation cycle caused by pressure drop rise. In an ebullating bed reactor, the catalyst is boiling, so there is no pressure drop problem. At the same time, because the catalyst can be unloaded and added online, it can maintain a steady state and process high metal content residue.

For the ebullating bed hydrogenation process, the ebullating bed hydrogenation reactor is the core of the ebullating bed hydrogenation, especially the oil circulation in the reactor to increase the upward flow of oil in the reactor is the key to keep the catalyst in a boiling state. At present, there are several types of technologies for increasing the oil flow in the fluidized bed hydrogenation reactor: one is to use the circulating pump to provide power to realize the oil circulation in the reactor, and increase the upward oil flow in the reactor. The other is to use an external jet pump to return the oil back to the reactor to increase the upward flow of oil in the reactor.

U.S. Patent US3414386 describes that a circulating pump is installed at the bottom of the reactor, and the oil is guided to the pump from the upper part of the reactor, and then the pump provides a pressure head to make the oil pass through the distribution plate upwards, so that the oil can circulate in the reactor and make the catalyst Keep the boiling fluidized state; but this technology has serious disadvantages. Once the circulating pump inside the reactor is broken, the reactor must be shut down to open the reactor and the catalyst must be unloaded before maintenance, and the loss of shutdown is huge.

U.S. Patent No. 5,360,535 proposes to use an external jet pump to realize oil circulation, and use static equipment to replace dynamic equipment. The method is to set a jet pump high-pressure facility outside the reactor, and the reactor effluent enters the first high-pressure separator and the second high-pressure separator in sequence, and uses a high-pressure pump to extract oil from the bottom of the second high-pressure separator as injector power oil, Push the 1 to 10 times oil stream drawn from the bottom of the first high-pressure separator to the bottom of the reactor together, pass through the distribution plate together with fresh raw materials and hydrogen, and keep the catalyst in the reactor in a boiling state. However, this method still needs to build a set of external high-pressure injection pump equipment and high-pressure pumps, and requires more high-pressure pipelines and more sealing systems, increasing high-pressure equipment and investment.

Contents of the invention

The object of the present invention is to provide a new method for hydrogenating fluidized bed residue in order to overcome the defects of complex processing method and high equipment investment in the existing fluidized bed residue hydrogenation method.

The invention provides a method for hydrogenation of ebullated-bed residual oil, which comprises that the raw material of residual oil enters an ebullated-bed hydrogenation reactor and hydrogenation reaction is carried out with hydrogen under the action of an ebullated-bed hydrogenation catalyst to obtain hydrogenated oil, and the obtained hydrogenated The hydrogen-generated oil undergoes gas-liquid separation in the high-pressure separator, and the liquid phase separated by the high-pressure separator is fractionated into gas, naphtha fraction, diesel fraction and hydrogenated atmospheric residue in the fractionating tower;

The ebullated bed hydrogenation reactor has a reactor cylindrical shell 1, an upper head and a lower head, and a gas-liquid separator 3, a vertical oil guide pipe 4 and a distribution plate 9 are sequentially arranged in the reactor, The inlet of the oil gas outlet 2 and the high-pressure oil guide pipe 5 are set at the upper head of the reactor, and the inlet of the hydrogen feed pipe 10 is set at the lower head of the reactor. In the reactor, the lower end of the gas-liquid separator 3 is connected to the vertical The inlet of the oil guide pipe 4 is connected, the lower part of the vertical oil guide pipe 4 is connected with the distribution plate 9, the outlet of the vertical oil guide pipe 4 is located below the distribution plate 9, and a high-pressure oil guide pipe 5 is arranged on the upper part of the reactor, wherein the high-pressure oil guide pipe 5 The outlet end of the vertical oil guide pipe 4 is located in the vertical oil guide pipe 4, and the ratio of the axial distance between the outlet end of the high pressure oil guide pipe 5 and the inlet end of the vertical oil guide pipe 4 to the length of the vertical oil guide pipe 4 is 0.1-8:10.

The method provided by the present invention can process low-quality residual oil raw materials, remove most of the impurities such as sulfur and metals in the raw materials, and greatly reduce the residual carbon value, and the obtained hydrogenated atmospheric residual oil can be used as catalytic cracking raw materials, improving Lower the utilization rate of inferior raw material oil. In the fluidized bed hydrogenation method provided by the present invention, the high-pressure oil guide pipe sprays the driving oil higher than the pressure of the reactor into the vertical oil guide pipe, and forms a high-speed oil flow when spraying out, driving a larger amount of liquid in the reactor The internal circulation, thereby promoting the catalyst, and maintaining the catalyst in an ebullating bed state. Compared with the existing ebullated bed reactor with internal circulation pump and external circulation pump, the structure of the ebullated bed hydrogenation reactor in the hydrogenation method of the present invention is simple, easy to realize internal circulation, and saves moving equipment, saving investment costs and operating costs.

Description of drawings

Fig. 1 is a schematic structural diagram of an ebullating bed hydrogenation reactor in the hydrogenation method provided by the present invention.

Illustration of the drawings:

1—Cylindrical shell of the reactor, 2—Oil and gas outlet, 3—Gas-liquid separator, 4—Vertical oil guide pipe, 5—High pressure oil guide pipe, 6—The reduced diameter part of the outlet end of the high pressure oil guide pipe, 7—Catalyst inlet Feed pipe, 8—catalyst discharge pipe, 9—distribution plate, 10—hydrogen gas feed pipe.

detailed description

The present invention will be described below in conjunction with the drawings and embodiments. For the sake of clarity, representation and description of components and processes that are not related to the present invention and known to those of ordinary skill in the art are omitted from the drawings and descriptions.

The residual oil raw material enters the ebullated bed hydrogenation reactor after heat exchange and heating by the heating furnace, and the hydrogen gas also enters the ebullated bed hydrogenation reactor after heat exchange or heating; under the action of the ebullated bed hydrogenation catalyst, the residual crude oil is Hydrogenation reaction removes most of the sulfur, metals and asphaltenes, and at the same time, the carbon residue value of the residual oil raw material is also greatly reduced. Carry out gas-liquid separation, and the hydrogen-enriched circulating gas obtained from the separation is compressed by the circulator and mixed with new hydrogen, and then returned to the ebullating bed hydrogenation reactor for continued use. The liquid phase separated by the high-pressure separator is fractionated in the fractionating tower into Gases, naphtha fractions, diesel fractions and hydrotreated atmospheric residues.

The structure of the fluidized bed hydrogenation reactor adopted in the present invention is shown in Fig. 1, which has a reactor cylindrical shell 1, an upper head and a lower head. The cylindrical shell of the reactor has an aspect ratio of 0.8:1˜100:1. A gas-liquid separator 3, a vertical oil guide pipe 4 and a distribution plate 9 are sequentially arranged in the ebullated bed hydrogenation reactor. The lower end of the gas-liquid separator 3 is connected to the inlet of the vertical oil guide pipe 4, the bottom of the vertical oil guide pipe 4 is connected to the distribution plate 9, the outlet of the vertical oil guide pipe 4 is located below the distribution plate 9, and the reaction The cylindrical shell 1 of the device, the gas-liquid separator 3, the vertical oil guide pipe 4 and the distribution plate 9 are mutually coaxial.

The oil gas outlet 2 and the inlet of the high-pressure oil guide pipe 5 are arranged at the upper head of the ebullated bed hydrogenation reactor, and the inlet of the hydrogen feed pipe 10 is arranged at the lower head of the reactor. The hydrogen feed pipe 10 enters the reactor from the lower head of the reactor and is located below the distribution plate 9 .

In the fluidized bed hydrogenation reactor, a high-pressure oil guide pipe 5 is arranged on the upper part of the reactor, wherein the outlet end of the high-pressure oil guide pipe 5 is located in the vertical oil guide pipe 4, and the direction of the outlet end of the high-pressure oil guide pipe 5 is vertically downward, and The outlet end of the high pressure oil guide pipe 5 and the vertical oil guide pipe 4 are mutually coaxial. The ratio of the axial distance between the outlet end of the high-pressure oil guide pipe 5 and the inlet end of the vertical oil guide pipe 4 to the length of the vertical oil guide pipe 4 is 0.1-2:10.

The outlet end of the high-pressure oil guide pipe 5 is located in the vertical oil guide pipe 4, and the ratio of the distance in the radial direction between the outer wall of the outlet end of the high-pressure oil guide pipe 5 and the inner wall of the vertical oil guide pipe 4 and the inner diameter of the vertical oil guide pipe 4 is 0.05～ 0.5:1.

The high-pressure oil guide pipe 5 has a uniform wall thickness, preferably at the outlet of the high-pressure oil guide pipe 5, a reduced-diameter portion 6 is provided, and the inner diameter of the reduced-diameter portion 6 gradually decreases along the axial direction of the high-pressure oil guide pipe 5, and at high pressure The outlet end of the oil guide pipe 5 has the smallest inner diameter. The diameter-reducing portion 6 is coaxial with the vertical oil guide pipe 4 .

The ratio of the largest inner diameter to the smallest inner diameter of the diameter-reduced portion 6 at the outlet of the high-pressure oil guide pipe 5 is 20-2:1.

The maximum inner diameter part of the reduced-diameter portion 6 at the outlet of the high-pressure oil guide pipe 5 is located in the vertical oil guide pipe 4, and the distance between the corresponding outer wall and the inner wall of the vertical oil guide pipe 4 in the radial direction is equal to the inner diameter of the vertical oil guide pipe 4. The ratio is 0.05～0.5:1.

In this ebullating bed reactor, the pressure of the driving oil in the high-pressure oil guide pipe 5 is higher than the internal pressure of the reactor, and when the driving oil in the high-pressure oil guide pipe 5 flows out from the outlet (or the reduced diameter part 6), the pressure is converted into kinetic energy, Make the driving oil flow down the vertical oil guide pipe 4 at a faster speed, and form a relatively low pressure area at the gap between the outlet end of the reduced diameter part 6 and the inner wall of the vertical oil guide pipe 4, and Therefore, the oil on the upper part of the gas-liquid separator 3 in the suction reactor enters the vertical oil guide pipe 4 and then flows to this gap, and is driven by the driving oil flow ejected from the outlet end of the reduced diameter part 6 to flow along the vertical oil guide pipe together. 4 flow down. The driving oil from the high-pressure oil guide pipe 5 and sprayed out through the reduced diameter part 6 is mixed with the oil from the upper part of the gas-liquid separator 3 in the reactor, and together reach the bottom of the reactor through the vertical oil guide pipe 4, then turn back upwards, and mix with the oil from the hydrogen gas. After the hydrogen gas in the feed pipe 10 is mixed, it continues to flow upward through the distribution plate 9 . The gas-liquid propulsion inside the reactor makes the catalyst in a boiling state, and it is possible to control the appropriate process conditions so that the material level of the catalyst in the ebullating bed hydrogenation reactor rises and maintains a certain height.

When hydrogenation reaction is carried out in ebullating bed hydrogenation reactor, in order to facilitate on-line replacement of catalyst in the production process, a catalyst feeding pipe 7 is arranged on the upper part of the ebullating bed hydrogenation reactor, and the catalyst feeding pipe 7 passes through the gas Liquid distributor 3, the outlet of which is located below the gas-liquid separator 3. A catalyst discharge pipe 8 is arranged at the lower part of the ebullated bed hydrogenation reactor, and the catalyst discharge pipe 8 passes through a distribution plate 9 , and its inlet is located above the distribution plate 9 . The catalyst feed pipe 7 and the catalyst discharge pipe 8 enable the reactor to replace the catalyst by adding and discharging the catalyst on-line during normal production without shutting down, so as to keep the overall activity of the catalyst stable. The catalyst feed pipe 7 and the catalyst discharge pipe 8 can also be omitted if there is no need to replace the catalyst during operation.

The pressure in the high-pressure oil guide pipe 5 is 0.5-10MPa higher than the pressure in the reactor.

In a preferred embodiment of the present invention, part of the obtained hydrogenated atmospheric residue is recycled back to the ebullating bed hydrogenation reactor, and hydrogenation reaction is carried out together with the residue raw material.

In another preferred embodiment of the present invention, the obtained hydrogenated atmospheric residue is partially subjected to vacuum distillation, and the obtained hydrogenated vacuum wax oil and the remaining part of the hydrogenated atmospheric residue are used as catalytic cracking raw materials; vacuum distillation The obtained hydrogenated vacuum residue is circulated back to the ebullating bed hydrogenation reactor, and the hydrogenation reaction is carried out together with the residue raw material.

The reaction conditions of the ebullated bed residual oil hydrogenation described in the present invention are: hydrogen partial pressure 2.0-22.0MPa, reaction temperature 300-450°C, volume space velocity 0.1-5.0 hours ^-1 , hydrogen-oil volume ratio 100-2000Nm ³ / m ³ .

The ebullated bed hydrogenation catalyst is one or more catalysts with porous inorganic oxides as the carrier and one or more oxides of Group VIB and/or Group VIII metals as active components . Various other additives such as P, Si, F and B are optionally added to the catalyst.

The carrier is selected from any one or more of alumina, silicon dioxide, amorphous silica-alumina or zeolite. The metal element of the active component is preferably a combination of nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, cobalt-molybdenum or nickel-cobalt-molybdenum.

The residual oil raw materials described in the present invention are heavy crude oil, acid-containing crude oil, atmospheric residual oil, atmospheric wax oil, vacuum residual oil, coking wax oil, tank bottom oil, shale oil, direct coal liquefaction oil, deasphalted One or more of crude oil, heavy oil, hydrocracking tail oil and secondary processed distillate oil of hydrocracking tail oil.

The invention can make the residual oil raw material with high metal content or the residual oil raw material with high calcium content undergo hydrogenation reaction, remove most of the impurities such as sulfur and metal in the raw material, greatly reduce the residual carbon value, and obtain hydrogenated atmospheric pressure slag The oil can be used as a raw material for catalytic cracking, which improves the utilization rate of inferior raw material oil.

One of the advantages of the ebullated bed reactor described in the hydrogenation method of the present invention is to form a high-speed oil flow when the oil with less pressure higher than the reactor pressure is sprayed out, driving a larger amount of oil to realize the oil in the reactor The cycle is used to push the catalyst to maintain the state of the catalyst ebullating bed, all of which are static devices with simple structure and high reliability.

The second advantage is that all components that make the catalyst in the fluidized bed state are located in the reactor, and constitute an open structure, without sealing and high pressure, saving investment.

The following examples are provided to better describe the present invention, but the present invention is not limited by the following examples.

Example 1

The raw material residue F1 is an atmospheric residue with high Ca content, and its properties are shown in Table 1. The hydrogenation reaction was carried out in an ebullating bed reactor as shown in Fig. 1 . Wherein, a diameter-reducing part 6 is provided at the outlet of the high-pressure oil guide pipe 5, and the ratio of the maximum inner diameter to the minimum inner diameter of the diameter-reducing part 6 is 7:1. The largest inner diameter part of the reduced diameter part 6 is located in the vertical oil guide pipe 4, and the ratio of the radial distance between the corresponding outer wall and the inner wall of the vertical oil guide pipe 4 to the inner diameter of the vertical oil guide pipe 4 is 0.2:1. The ratio of the axial distance between the outlet end of the high pressure oil guide pipe 5 and the inlet end of the vertical oil guide pipe 4 to the length of the vertical oil guide pipe 4 is 1:10.

The ebullating bed hydrogenation catalyst is the RMS-30 produced by Sinopec Catalyst Changling Branch developed by the Research Institute of Petroleum and Chemical Industry. It is made into a cylindrical shape with a diameter of 0.8mm to adapt to the ebullating bed hydrogenation reactor catalyst. 1.5 liters of RMS-30 catalyst was charged into the ebullating bed hydrogenation reactor, and the height of the catalyst material level was 50% of the height of the ebullating bed reactor.

The residual oil raw material is fed into the fluidized bed hydrogenation reactor through the high-pressure oil guide pipe 5 , and hydrogen gas is fed into the reactor through the hydrogen gas feeding pipe 10 . The flow rate of the residual oil introduced is 500g/h, that is, the volumetric space velocity of the residual oil is 0.5h ^-1 relative to the loaded volume of the catalyst, and the flow rate of the hydrogen gas is 165L/h under standard conditions. Other operating conditions are that the pressure inside the high-pressure oil guide pipe 5 is 19.8MPa, the pressure inside the reactor is 15.0MPa, and the reaction temperature is 400°C. The driving oil in the high-pressure oil guide pipe 5 flows out at a high speed at the reduced diameter part of the outlet, driving the gas-liquid separator 3 More oil from the upper part goes down to the bottom of the reactor along the vertical oil guide pipe 4 and turns back upwards, mixes with hydrogen and passes through the distribution plate 9 upwards, pushing the catalyst to make the catalyst boil. The material level of the catalyst in the ebullating bed hydrogenation reactor is measured by a radioactive measurement method, the height of the catalyst material level is 1.25 times of the filling height, and the catalyst expansion rate is 25%.

The produced oil after the hydrogenation reaction is separated and fractionated to obtain gas, naphtha fraction, diesel fraction and hydrogenated atmospheric residue. The product distribution is shown in Table 2, and the properties of the hydrogenated atmospheric residue are shown in Table 3.

It can be seen from Table 3 that the content of sulfur, acid value, metal and residual carbon in the hydrogenated atmospheric residue product is significantly lower than that of the raw material atmospheric residue, and it can be used as a qualified catalytic cracking raw material for processing in a catalytic cracking unit.

Table 1

project F1 Density (20℃), g/ ^cm3 0.9613 Carbon residue content, wt% 11.0 Element content, wt% sulfur 2.2 nitrogen 0.48 Metal content, μg/g nickel 47.6 vanadium 5.1 iron 18.6 calcium 42.0 sodium 5.1

Table 2

project Yield, % by weight H ₂ S+NH ₃ 2.0 C1～C4 1.9 naphtha fraction 2.0 diesel fraction 11.1 Hydrogenated Atmospheric Residue 83.0

table 3

project Density (20℃), g/ ^cm3 0.9350 Carbon residue content, wt% 6.0 Element content, wt% Sulfur, % by weight 0.48 Nitrogen, wt% 0.34 Nickel + vanadium, μg/g 18

Example 2

The raw material residue F2 is an atmospheric residue with high Ni and V content, and its properties are shown in Table 4. The hydrogenation reaction was carried out in an ebullating bed reactor as shown in Fig. 1 . The catalyst is RDM-33 produced by Sinopec Catalyst Changling Branch developed by the Research Institute of Petroleum and Chemical Industry. The catalyst is made into a cylindrical shape with a diameter of 0.7mm to adapt to the ebullated bed hydrogenation reactor catalyst. 1.5 liters of RDM-33 catalyst was loaded into the ebullating bed hydrogenation reactor, and the height of the catalyst material level was 50% of the height of the ebullating bed reactor.

Through the high-pressure oil guide pipe 5, feed the residual oil raw material and the hydrogenated vacuum residual oil circulated by the fractionation system into the fluidized bed hydrogenation reactor. The flow rate of the residual oil raw material introduced is 400g/h, and the hydrogenated vacuum residual oil The flow rate is 160g/h, and hydrogen is passed into the reactor through the hydrogen feed pipe 10 . The hydrogen flow rate is 170L/h under standard conditions. Other operating conditions are that the pressure inside the high-pressure oil guide pipe 5 is 19.0 MPa, the pressure inside the reactor is 14.5 MPa, and the reaction temperature is 410°C. More oil in the upper part goes down to the bottom of the reactor along the vertical oil guide pipe 4 and turns back upwards, mixes with hydrogen and passes through the distribution plate 9 upwards, pushing the catalyst to make the catalyst boil. The material level of the catalyst in the ebullating bed hydrogenation reactor was measured by a radioactive measurement method, the height of the catalyst material level was 1.26 times of the filling height, and the catalyst expansion rate was 26%.

The resulting hydrogenated oil is separated and fractionated to obtain gas, naphtha fraction, diesel fraction, and hydrogenated atmospheric residue; a part of the hydrogenated atmospheric residue is subjected to vacuum distillation, and the hydrogenated vacuum residue is recycled Return to the raw material system, mix with the residual oil raw material and enter the ebullated bed hydrogenation reactor for hydrogenation reaction. The hydrogenated wax oil product obtained by vacuum distillation and the hydrogenated atmospheric residue without vacuum distillation are mixed as the raw material for catalytic cracking. The product yield is shown in Table 5, and the properties of the catalytic cracking feedstock are shown in Table 6. It can be seen from Table 6 that the content of sulfur, acid value, metal and residual carbon in catalytic cracking raw materials is greatly reduced compared with the raw material atmospheric residue, and can be processed in catalytic cracking units alone or as a blended raw material for catalytic cracking.

Table 4

Raw oil F2 Density (20℃), g/ ^cm3 0.9625 Carbon residue content, wt% 10.6 Element content, wt% sulfur 3.1 nitrogen 0.43 Metal content, μg/g nickel 50.5 vanadium 151

table 5

project Yield, % by weight H ₂ S+NH ₃ 3 C1～C4 2.2 naphtha 2.2 diesel fuel 12.7 Catalytic Cracking Feedstock 79.9

Table 6

project Density (20℃), g/ ^cm3 0.9295 Carbon residue content, wt% 5.4 Sulfur, % by weight 0.55 Nitrogen, wt% 0.30 Nickel + vanadium, μg/g 30

Claims (18)

1. A method for hydrogenation of ebullated bed residual oil, wherein the residual oil raw material enters the ebullated bed hydrogenation reactor and hydrogen carries out the hydrogenation reaction under the action of the ebullated bed hydrogenation catalyst to obtain the hydrogenated oil, and the resulting hydrogenated oil is The high-pressure separator performs gas-liquid separation, and the liquid phase separated by the high-pressure separator is fractionated into gas, naphtha fraction, diesel fraction and hydrogenated atmospheric residue in the fractionating tower; The ebullated bed hydrogenation reactor has a reactor cylindrical shell (1), an upper head and a lower head, and a gas-liquid separator (3), a vertical oil guide pipe (4) and a The distribution plate (9) is characterized in that the inlet of the oil gas outlet (2) and the high-pressure oil guide pipe (5) are arranged at the upper head of the reactor, and the inlet of the hydrogen feed pipe (10) is arranged at the lower head of the reactor , in the reactor, the lower end of the gas-liquid separator (3) is connected with the inlet of the vertical oil guide pipe (4), the lower part of the vertical oil guide pipe (4) is connected with the distribution plate (9), and the vertical oil guide pipe (4) ) is located below the distribution plate (9), and a high-pressure oil guide pipe (5) is arranged on the top of the reactor, wherein the outlet end of the high-pressure oil guide pipe (5) is positioned in the vertical oil guide pipe (4), and the high-pressure oil guide pipe (5) ) The ratio of the axial distance between the outlet end of the vertical oil guide pipe (4) and the inlet end of the vertical oil guide pipe (4) to the length of the vertical oil guide pipe (4) is 0.1-8:10. 2. The hydrogenation method according to claim 1, characterized in that, the top of the ebullated bed hydrogenation reactor is provided with a catalyst feed pipe (7), and the outlet of the catalyst feed pipe (7) is located at the gas-liquid separator (3) below. 3. hydrogenation method according to claim 1, is characterized in that, the bottom of described ebullated-bed hydrogenation reactor is provided with catalyst unloading pipe (8), and described catalyst unloading pipe (8) passes distribution plate ( 9), its inlet is located above the distribution plate (9). 4. The hydrogenation method according to claim 1, characterized in that, the hydrogen feed pipe (10) of the ebullated bed hydrogenation reactor is located below the distribution plate (9). 5. The hydrogenation method according to claim 1, characterized in that the height-to-diameter ratio of the reactor cylindrical shell of the ebullated bed hydrogenation reactor is 0.8:1-100:1. 6. The hydrogenation method according to claim 1, characterized in that, in the ebullated bed hydrogenation reactor, the reactor cylindrical shell (1), gas-liquid separator (3), vertical oil guide pipe (4) and distribution disc (9) are mutually coaxial. 7. The hydrogenation method according to claim 1, characterized in that, the direction of the outlet end of the high-pressure oil guide pipe (5) is vertically downward, and the outlet end of the high-pressure oil guide pipe (5) is connected to the vertical oil guide pipe (4) are coaxial with each other. 8. according to the described hydrogenation method of claim 1 or 7, it is characterized in that, the high-pressure oil guide pipe (5) outlet end outer wall of the ebullated bed hydrogenation reactor and the vertical oil guide pipe (4) inner wall along the radial direction The ratio of the distance to the inner diameter of the vertical oil guide pipe (4) is 0.05-0.5:1. 9. The hydrogenation method according to claim 1 or 7, characterized in that the high-pressure oil guide pipe (5) of the fluidized bed hydrogenation reactor has a uniform wall thickness, and the outlet of the high-pressure oil guide pipe (5) is provided with a reduced diameter part (6), the inner diameter of the reduced-diameter part (6) gradually decreases along the axial direction of the high-pressure oil guide pipe (5), and the inner diameter of the outlet end of the high-pressure oil guide pipe (5) is the smallest. 10. The hydrogenation method according to claim 9, characterized in that the ratio of the largest inner diameter to the smallest inner diameter of the reduced diameter portion (6) at the outlet of the high-pressure oil guide pipe (5) is 20-2:1. 11. The hydrogenation method according to claim 9, characterized in that the maximum inner diameter part of the reduced diameter portion (6) at the outlet of the high-pressure oil guide pipe (5) is located in the vertical oil guide pipe (4), and its corresponding outer wall The ratio of the distance in the radial direction from the inner wall of the vertical oil guide pipe (4) to the inner diameter of the vertical oil guide pipe (4) is 0.05˜0.5:1. 12. The hydrogenation method according to claim 10, characterized in that the maximum inner diameter part of the reduced diameter portion (6) at the outlet of the high-pressure oil guide pipe (5) is located in the vertical oil guide pipe (4), and its corresponding outer wall The ratio of the distance in the radial direction from the inner wall of the vertical oil guide pipe (4) to the inner diameter of the vertical oil guide pipe (4) is 0.05˜0.5:1. 13. The hydrogenation method according to claim 1, wherein the pressure in the high-pressure oil guide pipe (5) is 0.5-10 MPa higher than the pressure in the reactor. 14. The hydrogenation method according to claim 1, wherein part of the obtained hydrogenated atmospheric residue is recycled back to the ebullating bed hydrogenation reactor, and hydrogenation reaction is carried out together with the residue raw material. 15. The hydrogenation method according to claim 1, the hydrogenated atmospheric residue part of gained carries out vacuum distillation, and the gained hydrogenated vacuum wax oil and the remaining part of the hydrogenated atmospheric residue are used as catalytic cracking raw materials together; The hydrogenated vacuum residue obtained by the pressure distillation is recycled to the ebullating bed hydrogenation reactor, and the hydrogenation reaction is carried out together with the residue raw material. 16. The hydrogenation method according to claim 1, the reaction conditions for hydrogenation of ebullated bed residual oil are: hydrogen partial pressure 2.0-22.0 MPa, reaction temperature 300-450°C, volume space velocity 0.1-5.0 hours ^-1 , hydrogen The oil volume ratio is 100-2000Nm ³ /m ³ . 17. The hydrogenation method according to claim 1, wherein the ebullated bed hydrogenation catalyst is supported by a porous inorganic oxide, and is oxidized by one or more of Group VIB and/or Group VIII metals Catalysts in which one or more substances are active components. 18. The hydrogenation method according to any one of claims 1-7, 10-17, wherein the residue raw material is heavy crude oil, acid-containing crude oil, atmospheric residue, atmospheric wax oil, reduced Pressed residue, coker wax oil, tank bottom oil, shale oil, coal direct liquefaction oil, deasphalted oil, heavy oil, hydrocracking tail oil and secondary processed distillate oil of hydrocracking tail oil or Various.