Slurry bed reactant hydrogenation system and method

Abstract

The present application belongs to the technical field of slurry bed hydrogenation, and discloses a slurry bed reactant hydrogenation system and method. The system comprises a slurry bed residual oil hydrogenation reaction device, an oil-gas separation unit, an atmospheric distillation unit, a vacuum distillation unit and a raw oil feeding pipeline. The present application has the technical characteristics of simple structure, improved economic benefits, reduced investment cost and device operation energy consumption, etc.

Description

Technical Field

[0001] This invention belongs to the field of slurry bed hydrogenation technology, and more specifically, relates to a slurry bed reactant hydrogenation system and method. Background Technology

[0002] Currently, slurry-bed fuel oil hydrotreating units are increasingly widely used in petrochemical production processes due to their high feedstock hydrocracking conversion rate and high yield of high-value-added products. More than ten slurry-bed residue hydrotreating technologies have been developed domestically and internationally, including: the HDH-plus technology developed by INTEPE and Veba, the Uniflex technology developed by UOP (USA), the LC-Slurry technology developed by Chevron Lummus (USA), the EST technology developed by Enitecnologies, and the RMAC technology developed by the China Petroleum & Chemical Research Institute Co., Ltd. According to the report "Current Status and Prospect of Slurry-Bed Residue Hydrotreating Technology," the process flows of existing slurry-bed residue hydrotreating technologies differ slightly, but the following two points are basically consistent: 1. In the feed process, residue oil and hydrogen are mixed and then enter the slurry-bed reactor for reaction. 2. The reaction products are cooled and depressurized, and the recycled hydrogen is returned to the reaction unit. Low-grade oil and slurry enter atmospheric and vacuum distillation columns to separate hydrocarbon components of different fractions.

[0003] However, existing slurry-bed residue hydrotreating technology has the following two problems: 1. Due to the high viscosity of fuel oil (residue oil), such as vacuum residue and atmospheric residue, a certain proportion of diesel and / or heavy diesel is blended during the external sales process to reduce the viscosity and improve the fluidity of the residue oil. This leads to increased processing capacity and energy consumption in the slurry-bed hydrotreating reactor. At the same time, the high temperature and high pressure conditions of the slurry-bed hydrotreating reactor result in higher investment costs and greater difficulty in equipment manufacturing. 2. The slurry of the fuel oil hydrotreating product has a high solid content. After separation, it enters the vacuum distillation tower, where the trays are prone to coking under high temperature and low pressure conditions, clogging the tower and resulting in poor unit stability. It cannot operate stably for a long time and needs to be shut down once every eleven to twelve months, with one shutdown lasting up to one month to clean the bottom section of the vacuum distillation tower. To solve this problem, some units have set up a backup vacuum distillation tower, which increases additional investment costs. CN116194556A provides a scheme for the combined design of fluidized bed hydrocracking and coking units to improve the continuous operation capability of residue hydrocracking units. However, due to considerations of green energy conservation and environmental protection, existing refineries have chosen to stop building coking units.

[0004] Furthermore, to date, slurry bed residue hydrotreating units and atmospheric and vacuum distillation units in refineries have been operated as separate systems, each including a dedicated fractionation section. However, both systems have atmospheric and vacuum distillation towers, and both have similar feed characteristics, feeding wide-range oils. The separate construction of slurry bed residue hydrotreating units and atmospheric and vacuum distillation units in refineries has resulted in a waste of investment and land area.

[0005] Therefore, there is an urgent need to propose a new system and method for hydrogenating fuel oil in a slurry bed. Summary of the Invention

[0006] The purpose of this invention is to address the shortcomings of existing technologies by proposing a slurry-bed reactant hydrogenation system and method. This invention features simple structure, improved economic efficiency, reduced investment costs, and lower energy consumption during operation.

[0007] To achieve the above objectives, the present invention provides a slurry bed reactant hydrogenation system, the system comprising a slurry bed residue hydrogenation reactor, an oil-gas separation unit, an atmospheric distillation unit, a vacuum distillation unit, and a feedstock pipeline;

[0008] The slurry bed residue hydrotreating reactor is connected to the oil-gas separation unit via a product pipeline;

[0009] The oil-gas separation unit is equipped with a heavy component discharge pipeline, a medium component discharge pipeline, a light component discharge pipeline, and a circulating hydrogen pipeline.

[0010] The feed pipeline of the raw material oil merges with the discharge pipeline of the medium component and is then connected to the atmospheric distillation unit; the atmospheric distillation unit is equipped with a bottom oil discharge pipeline of the atmospheric distillation tower and at least one first light oil discharge pipeline.

[0011] The atmospheric distillation tower bottom oil discharge pipeline merges with the heavy component discharge pipeline and is then connected to the vacuum distillation unit. The vacuum distillation unit is equipped with a vacuum distillation tower bottom oil discharge pipeline and at least one second light oil discharge pipeline. The outlet of the vacuum distillation tower bottom oil discharge pipeline is divided into two paths: one is used as an external discharge pipeline, and the other is used as a circulating oil pipeline. The fresh hydrogen feed pipeline and the circulating hydrogen pipeline merge into a total hydrogen feed pipeline, which, together with the circulating oil pipeline, is connected to the slurry bed residue oil hydrogenation reactor.

[0012] According to the present invention, preferably, the feedstock oil inlet pipeline is first connected to the feedstock buffer tank and then merges with the discharge pipeline of the medium-quality components.

[0013] According to the present invention, preferably, the slurry bed residue hydrotreating reactor is further connected to a catalyst feed pipeline.

[0014] According to the present invention, preferably, the slurry bed residue hydrotreating apparatus is provided with at least one slurry bed residue hydrotreating reactor. In the present invention, as a preferred embodiment, when using multiple slurry bed residue hydrotreating reactors, the multiple slurry bed residue hydrotreating reactors can be arranged in series, in parallel, or in a series-parallel combination.

[0015] In this invention, based on the boiling point of the effluent from the slurry-bed residue hydrotreating reactor, the effluent can be separated into two or more fractions, three or more fractions, or four or more fractions. In some embodiments, the effluent from the slurry-bed residue hydrotreating reactor can be separated into: (i) one or more heavy fractions having the boiling point of heavy vacuum gas oil; (ii) one or more medium fractions having the boiling point of medium vacuum gas oil; and (iii) a light gaseous fraction containing hydrogen and hydrocarbons with a boiling point below 35°C. In this invention, as a preferred embodiment, the oil-gas separation unit includes one or more separators and flash tanks.

[0016] According to the present invention, preferably, the oil and gas separation unit includes a heavy hydrogenation product separator, a medium hydrogenation product separator, and a hydrogen recovery separator;

[0017] The heavy hydrotreating product separator is used to separate the heavy components and gaseous streams from the hydrotreating products of the slurry bed residue hydrotreating reactor.

[0018] The medium-quality hydrogenation product separator is used to separate the medium-quality components and the hydrogen-containing gaseous light hydrocarbon fraction in the gaseous stream.

[0019] The hydrogen recovery separator is used to separate the circulating hydrogen and light components in the hydrogen-containing gas phase light hydrocarbon fraction.

[0020] In this invention, medium-grade components and desalted, dehydrated crude oil can be fed together into an atmospheric distillation unit, whereby hydrocarbons are separated into two, three, or four or more fractions. The atmospheric distillation unit can be used, for example, to separate the feed into one or more distillate fractions and an atmospheric residue fraction. The one or more distillate fractions can include hydrocarbons from the range of naphtha, diesel, kerosene, jet fuel, light gas oil, and heavy gas oil, which can be recovered individually or in various combined fractions.

[0021] According to the present invention, preferably, the atmospheric distillation unit includes a first heating furnace and an atmospheric distillation column;

[0022] The feed pipeline of the raw oil and the discharge pipeline of the medium components are connected to the atmospheric distillation tower through the first heating furnace.

[0023] The bottom oil discharge pipeline of the atmospheric distillation tower and at least one first light oil discharge pipeline are installed on the atmospheric distillation tower; the atmospheric distillation tower is the atmospheric distillation tower in the atmospheric and vacuum distillation unit of the refinery (that is, the atmospheric distillation tower can be shared with the atmospheric distillation tower in the atmospheric and vacuum distillation unit of the refinery).

[0024] The first light oil discharge pipeline includes at least one of a naphtha discharge pipeline, a diesel discharge pipeline, and a dry gas discharge pipeline.

[0025] In this invention, atmospheric distillation bottoms oil and heavy components can be fed into a vacuum distillation unit, whereby hydrocarbons are separated into two, three, or four or more fractions. The vacuum distillation unit can be used, for example, to separate the feed into one or more vacuum distillate fractions and vacuum residue fractions. One or more vacuum distillate fractions may include hydrocarbons boiling within the range of light and heavy vacuum gas oils, which can be recovered in individual or combined fractions.

[0026] According to the present invention, preferably, the vacuum distillation unit includes a second heating furnace and a vacuum distillation column;

[0027] The bottom oil discharge pipeline of the atmospheric distillation tower is connected to the second heater and then merges with the heavy component discharge pipeline, and then connects to the vacuum distillation tower.

[0028] The bottom oil discharge pipeline of the vacuum distillation tower and at least one second light oil discharge pipeline are installed on the vacuum distillation tower; the vacuum distillation tower is a vacuum distillation tower in the atmospheric and vacuum distillation unit of the refinery (that is, the vacuum distillation tower can be shared with the vacuum distillation tower in the atmospheric and vacuum distillation unit of the refinery).

[0029] The second light oil discharge pipeline includes at least one of a light wax oil discharge pipeline and a heavy wax oil discharge pipeline.

[0030] According to the present invention, preferably, the system further includes a hydrogen heater, and the total hydrogen feed line is connected to the hydrogen heater and then connected to the slurry bed residue oil hydrogenation reactor together with the circulating oil line.

[0031] Another aspect of the present invention provides a slurry bed reactant hydrogenation method, the method employing the aforementioned system and comprising the following steps:

[0032] S1: The effluent from the slurry bed residue hydrotreating reactor is sent to the oil-gas separation unit, where it is separated to obtain heavy components, medium components, light components, and recycled hydrogen;

[0033] S2: The feedstock oil and the medium-quality components are sent to the atmospheric distillation unit for atmospheric distillation to obtain atmospheric distillation bottom oil and first light oil (one or more atmospheric distillate fractions); the atmospheric distillation bottom oil and the heavy-quality components are sent to the vacuum distillation unit for vacuum distillation to obtain vacuum distillation bottom oil and second light oil (one or more vacuum distillate fractions).

[0034] S3: The bottom oil of the vacuum distillation tower is divided into two parts, one part is discharged and the remaining part is used as circulating oil; the circulating hydrogen and fresh hydrogen feed are combined into total hydrogen and sent together with the circulating oil to the slurry bed residue oil hydrogenation reactor for hydrogenation reaction.

[0035] According to the present invention, preferably, the feedstock oil is at least one of desalted and dehydrated crude oil, residue oil, wax oil, deasphalted oil, bottom stream from atmospheric distillation column, bottom stream from vacuum distillation column, catalytic cracking slurry oil, base oil, tar sand asphalt, tall oil, and black oil.

[0036] More preferably, the desalted and dehydrated crude oil is at least one of fully electro-desalted and dehydrated crude oil, fully heavy electro-desalted and dehydrated crude oil, and bio-based electro-desalted and dehydrated crude oil;

[0037] More preferably, the residue oil is atmospheric residue oil containing a flow promoter and / or vacuum residue oil containing a flow promoter, wherein the flow promoter is at least one of naphtha, diesel oil and wax oil, and more preferably, the blending ratio of the flow promoter in the residue oil is 0% to 60 wt%, and even more preferably 15% to 50 wt%.

[0038] More preferably, the wax oil is vacuum-pressed wax oil and / or coking wax oil;

[0039] More preferably, the base oil is derived from shale-based oil and / or coal-based oil;

[0040] Optionally, the feedstock oil undergoes at least one of the following processes before entering the atmospheric distillation unit: straight distillation, process derivatization, hydrocracking, desulfurization, and demetallization.

[0041] In this invention, when the feedstock is desalted and dehydrated crude oil, the dilution effect of diesel and wax oil fractions in the crude oil on heavy components can be used to eliminate coking in the vacuum tower and improve the operating cycle of the slurry bed residue oil hydrotreating unit.

[0042] In this invention, a suitable type of desalted and dehydrated crude oil can be selected based on factors such as an appropriate H:C ratio, aromaticity, and other factors that provide a dissolving effect on heavy components. Since the effluent from the slurry bed residue hydrotreating reactor may depend on the reactor feed, reactor harshness, and numerous other factors, the feedstock oil used to achieve dilution and dissolution effects should be appropriately selected.

[0043] In this invention, the vacuum distillation bottom oil is a hydrocarbon fraction with a boiling point or boiling range higher than 340°C. As a preferred embodiment, the vacuum distillation bottom oil includes hydrocarbons with a standard boiling point of at least 480°C, at least 520°C, or at least 565°C.

[0044] According to the present invention, preferably, the light component is a hydrocarbon with a boiling point below 35°C, which is discharged from the system through a light component discharge pipeline.

[0045] According to the present invention, preferably, the heavy hydrotreating product separator of the oil-gas separation unit separates the heavy components and gaseous streams from the effluent of the slurry bed residue hydrotreating reactor at a temperature of 350°C to 450°C and a pressure of 0.2 MPa to 25 MPa. Therefore, the heavy components are the liquid phase obtained by separation at a pressure of 0.2 to 25 MPa and a temperature of 350°C to 450°C.

[0046] According to the present invention, preferably, the medium-quality hydrotreating product separator of the oil-gas separation unit separates the medium-quality components and the hydrogen-containing light hydrocarbon fraction from the gaseous stream at a temperature of 35°C to 350°C and a pressure of 0.2 MPa to 25 MPa. Therefore, the medium-quality components are the liquid phase obtained by separation at a pressure of 0.2 to 25 MPa and a temperature of 35°C to 350°C.

[0047] According to the present invention, preferably, the feedstock oil and the medium-quality components are first fed to the first heating furnace of the atmospheric distillation unit to obtain a mixture at a temperature of 300-380°C; the mixture is then fed to the atmospheric distillation column of the atmospheric distillation unit for atmospheric distillation to obtain atmospheric distillation column bottom oil and a first light oil.

[0048] According to the present invention, preferably, the bottom oil of the atmospheric distillation column is sent to the second heating furnace of the vacuum distillation unit to obtain heated atmospheric distillation column bottom oil, the temperature of which is 340-380°C; the heated atmospheric distillation column bottom oil and the heavy component are sent together to the vacuum distillation column of the vacuum distillation unit for vacuum distillation to obtain vacuum distillation column bottom oil and a second light oil.

[0049] According to the present invention, preferably, the bottom oil of the atmospheric distillation column is a fraction with a temperature >300°C.

[0050] According to the present invention, preferably, the bottom oil of the vacuum distillation tower is a fraction with a temperature >400°C.

[0051] According to the present invention, preferably, the first light oil comprises at least one of overhead dry gas, naphtha, and diesel oil. In the present invention, the overhead dry gas, naphtha, and diesel oil comprise the dry gas, naphtha, and diesel oil generated in step S1, as well as the naphtha and diesel oil carried into the system by the feedstock oil.

[0052] According to the present invention, preferably, the second light oil includes at least one of light wax oil and heavy wax oil. In the present invention, the light wax oil and heavy wax oil include the light wax oil and heavy wax oil generated in step S1, as well as the light wax oil and heavy wax oil carried in by the raw material oil.

[0053] In this invention, depending on the actual conditions of the refinery, the recovered distillate fractions (first light oil and second light oil) can be sent for further processing to further convert, treat, or otherwise process the distillate fractions to form the desired products. Additional processing, such as further cracking of hydrocarbons, removal of nitrogen, CCR, metals, sulfur, and other impurities, may include hydrotreating, hydrocracking, hydrodesulfurization, hydrodenitrogenation, hydrodemetallization, or various other hydrotreating processes of the distillate fractions, depending on the purpose of the apparatus.

[0054] According to the present invention, preferably, the feed of the slurry bed residue hydrotreating reactor further includes a catalyst, the catalyst being selected with the aim of having good fluidization and wear resistance as well as selective hydrocracking performance. More preferably, the catalyst is at least one of molybdenum, nickel, cobalt, molybdenum alloy, nickel alloy, cobalt alloy, molybdenum-containing cobalt alloy, cobalt and / or molybdenum-containing nickel alloy, molybdenum oxide, nickel oxide and cobalt oxide.

[0055] According to the present invention, preferably, the operating conditions of the slurry bed residue hydrotreating reactor include: a reaction pressure of 15.0 MPa to 25.0 MPa, a reaction temperature of 380°C to 450°C, and a volume hourly space velocity of 0.05 h⁻¹. -1 ~0.2h -1 The hydrogen-to-oil volume ratio is 500–1200:1.

[0056] In this invention, the slurry-bed residue hydrotreating reactor absorbs the heat of reaction during the hydrotreating process as the enthalpy of the feedstock entering the reaction system. A temperature difference of 50–200°C can exist between the feed temperature and the temperature inside the slurry-bed residue hydrotreating reactor. Furthermore, unlike typical fixed-bed hydrocracking reactors, the slurry-bed reactor can operate at a substantially uniform catalyst temperature throughout the entire operating cycle.

[0057] According to the present invention, preferably, the hydrogenation reaction is at least one of hydrodeoxygenation, hydrodemetallization, hydrodesulfurization, and hydrocracking.

[0058] According to the present invention, preferably, the amount of vacuum distillation column bottom oil discharged from the system accounts for 3-20% of the total amount of vacuum distillation column bottom oil, with the remainder used as circulating oil. In the present invention, the circulating oil includes heavy oil with a distillation range >400°C from the feed oil and unreacted oil from step S1.

[0059] The beneficial effects of the technical solution of the present invention are as follows:

[0060] This invention features a simple process, improved economic efficiency, reduced investment costs, and lower energy consumption during equipment operation.

[0061] Typically, light oils such as naphtha and diesel added to residue oil to improve its fluidity do not participate in the reaction after entering the slurry bed hydrotreating reactor, leading to an increase in the reactor's throughput. In the method of this invention, the residue oil first passes through an atmospheric distillation column and a vacuum distillation column to separate the light fractions, and the heavy components then enter the slurry bed residue oil hydrotreating reactor. This helps to improve the operating cycle of the vacuum distillation subsystem, reduce the throughput of the slurry bed hydrotreating reactor, and lower the design load, thus saving energy and reducing investment costs.

[0062] After being heated, the bottom oil of the atmospheric distillation column is mixed with heavy components. The temperature of the mixture flow can be controlled by adjusting the temperature of the second heater, so that the feed temperature of the vacuum distillation column can be kept stable, which has the advantage of controllable temperature of the vacuum distillation column.

[0063] Typically, the feed to a vacuum distillation column includes heavy components, which have a high concentration of tetrahydrofuran insolubles and / or unconverted heavy asphalt. This makes the trays of the vacuum distillation column prone to coking and results in a short operating cycle. In the method of this invention, the bottom oil of the atmospheric distillation column can dilute the heavy components, reduce the concentration of tetrahydrofuran insolubles, and / or provide a dissolving effect on unconverted heavy asphalt. This helps to alleviate scaling in the bottom section of the vacuum distillation column, has the advantage of increasing the operating cycle of the vacuum distillation column, and improves the overall system uptime.

[0064] This invention utilizes the vacuum distillation column and atmospheric distillation column of a refinery's atmospheric and vacuum distillation unit as the vacuum distillation column and atmospheric distillation column in its system, forming a coupled system. This reduces the number of equipment units in the system and the atmospheric and vacuum distillation unit, lowering investment expenditure, energy consumption, and plant footprint, and also reducing carbon emissions. Specifically, since the atmospheric and vacuum distillation unit and the system of this invention share a set of vacuum distillation columns and atmospheric distillation columns, instead of using separate sets, this reduction in the number of units is possible. Therefore, due to reduced fouling and downtime, as well as lower capital costs resulting from the reduced number of units, the coupled system of this invention can provide better plant operability and profitability. Because a single set of vacuum and atmospheric distillation columns is used to fractionate the feed to the atmospheric distillation column, this invention can also minimize total energy requirements. The reduced number of units and energy consumption provides advantages in terms of lower CO2 footprint and smaller plant footprint.

[0065] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0066] The above and other objects, features and advantages of the present invention will become more apparent from the more detailed description of exemplary embodiments of the invention in conjunction with the accompanying drawings, wherein the same reference numerals generally represent the same components in the exemplary embodiments of the invention.

[0067] Figure 1 A schematic diagram of a slurry bed reactant hydrogenation system provided in Embodiment 1 of the present invention is shown.

[0068] Figure 2 A schematic diagram of a slurry bed reactant hydrogenation method provided in Comparative Example 1 of the present invention is shown.

[0069] The annotations in the attached figures are explained as follows:

[0070] 1-1 Feedstock oil, 1-2 Feedstock buffer tank, 1-3 Mixture of feedstock oil and medium components, 1-4 First heater, 1-5 Heated mixture, 1-6 Atmospheric distillation column, 1-7 Atmospheric distillation column bottom oil, 1-8 Naphtha, 1-9 Diesel oil, 1-10 Top dry gas, 1-11 Second heater, 1-12 Heated atmospheric distillation column bottom oil, 1-13 Heated atmospheric distillation column bottom oil and heavy components mixture, 1-14 Vacuum distillation column, 1-15 Light wax oil, 1-16 Heavy wax oil, 1-17 Vacuum distillation column bottom oil 1-18 External tail oil, 1-19 Circulating oil, 1-20 Catalyst, 1-21 Circulating oil containing catalyst, 1-22 Fresh hydrogen feed, 1-23 Total hydrogen, 1-24 Hydrogen heater, 1-25 Slurry bed residue hydrotreating unit, 1-26 Outflow product of slurry bed residue hydrotreating unit, 1-27 Separator of oil-gas separation unit, 1-28 Hydrogen-containing gas phase light hydrocarbon fraction, 1-29 Middle components, 1-30 Heavy components, 1-31 Hydrogen recovery separator, 1-32 Circulating hydrogen, 1-33 Light components;

[0071] 2-1 Feedstock Oil, 2-2 Fresh Feed Heater, 2-3 Mixing Feed Tank, 2-4 New Hydrogen, 2-5 Mixed Hydrogen Heater, 2-6 Feed to Slurry Bed Residue Hydrogenation Reactor, 2-7 Slurry Bed Residue Hydrogenation Reactor, 2-8 Separation Unit, 2-9 Gas Phase Products, 2-10 Low-Efficiency Oil, 2-11 Slurry, 2-12 Hydrogen Recovery Unit, 2-13 Recovered Recycled Hydrogen, 2-14 Light Hydrocarbon Exhaust, 2-15 Low-Efficiency Oil 2-16 Low-grade oil atmospheric distillation tower, 2-17 Atmospheric tower top dry gas, 2-18 Atmospheric naphtha, 2-19 Atmospheric diesel oil, 2-20 Slurry vacuum distillation tower, 2-21 Light wax oil, 2-22 Heavy wax oil, 2-23 Vacuum bottom oil, 2-24 External discharge oil, 2-25 Return circulating oil, 2-26 Reaction catalyst, 2-27 Product of slurry bed residue oil hydrotreating reactor, 2-28 Atmospheric bottom oil. Detailed Implementation

[0072] Preferred embodiments of the invention will now be described in more detail. While preferred embodiments of the invention are described below, it should be understood that the invention can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that the invention will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.

[0073] Example 1

[0074] This embodiment provides a slurry-bed reactant hydrogenation system, such as... Figure 1 As shown, the system includes a slurry bed residue hydrotreating reactor 1-25, an oil-gas separation unit, an atmospheric distillation unit, a vacuum distillation unit, and a feedstock pipeline;

[0075] The slurry bed residue hydrotreating reactor 1-25 is connected to the oil-gas separation unit via a product pipeline;

[0076] The oil-gas separation unit includes a heavy hydrotreating product separator, a medium hydrotreating product separator, and a hydrogen recovery separator 1-31. The heavy hydrotreating product separator separates the heavy components 1-30 from the hydrotreating products 1-26 of the slurry bed residue hydrotreating reactor from the gaseous stream. The medium hydrotreating product separator separates the medium components 1-29 from the gaseous stream from the hydrogen-containing light hydrocarbon fraction 1-28. The hydrogen recovery separator 1-31 separates the circulating hydrogen 1-32 from the hydrogen-containing light hydrocarbon fraction 1-28 from the circulating hydrogen fraction 1-33. The oil-gas separation unit is equipped with heavy component discharge pipelines, medium component discharge pipelines, light component discharge pipelines, and circulating hydrogen pipelines.

[0077] The atmospheric distillation unit includes a first heating furnace 1-4 and an atmospheric distillation tower 1-6; the feedstock oil inlet pipeline is first connected to the feedstock buffer tank 1-2 and then merges with the medium component outlet pipeline, and then connects to the atmospheric distillation tower 1-6 through the first heating furnace 1-4; the atmospheric distillation tower 1-6 is provided with an atmospheric distillation tower bottom oil outlet pipeline and a first light oil outlet pipeline; the atmospheric distillation tower 1-6 is an atmospheric distillation tower in the atmospheric and vacuum distillation unit of the refinery; the first light oil outlet pipeline includes a naphtha outlet pipeline, a diesel outlet pipeline and a dry gas outlet pipeline.

[0078] The vacuum distillation unit includes a second heater 1-11 and a vacuum distillation tower 1-14. The bottom oil discharge pipeline of the atmospheric distillation tower is connected to the second heater 1-11 and then merges with the heavy component discharge pipeline, and then connects to the vacuum distillation tower 1-14. The vacuum distillation tower 1-14 is equipped with a vacuum distillation tower bottom oil discharge pipeline and a second light oil discharge pipeline. The vacuum distillation tower 1-14 is a vacuum distillation tower in the atmospheric and vacuum distillation unit of the refinery. The second light oil discharge pipeline includes a light wax oil discharge pipeline and a heavy wax oil discharge pipeline. The outlet of the bottom oil discharge pipeline of the vacuum distillation tower is divided into two paths: one is used as an external discharge pipeline, and the other is used as a circulating oil pipeline. The fresh hydrogen feed pipeline and the circulating hydrogen pipeline merge into a total hydrogen feed pipeline. The total hydrogen feed pipeline is connected to the hydrogen heater 1-24 and then connected to the slurry bed residue oil hydrotreating reactor 1-25 together with the circulating oil pipeline.

[0079] The slurry bed residue oil hydrogenation reactor 1-25 is also connected to a catalyst feed pipeline.

[0080] This embodiment also provides a slurry bed reactant hydrogenation method, which uses the above-described system and includes the following steps:

[0081] S1: The effluent products 1-26 from the slurry bed residue hydrotreating unit are sent to the oil-gas separation unit, wherein:

[0082] The heavy hydrotreating product separator of the oil-gas separation unit separates the heavy component 1-30 and the gaseous stream from the effluent 1-26 of the slurry bed residue hydrotreating reactor at a temperature of 350℃~450℃ and a pressure of 16.0MPa~20.5MPa.

[0083] The medium-quality hydrogenation product separator of the oil-gas separation unit separates the medium-quality components 1-29 and the hydrogen-containing gaseous light hydrocarbon fractions 1-28 in the gaseous stream at a temperature of 35℃~350℃ and a pressure of 2.0MPa~16.0MPa.

[0084] At a temperature of 45°C and a pressure of 16.5 MPa, the hydrogen recovery separator is used to separate the circulating hydrogen and light components in the hydrogen-containing gas phase light hydrocarbon fraction.

[0085] The oil and gas separation unit separated heavy components 1-30, medium components 1-29, light components (hydrocarbons with boiling points below 35°C) 1-33, and recycled hydrogen 1-32.

[0086] S2: The feedstock oil and the medium components 1-29 are first sent to the first heater 1-4 of the atmospheric distillation unit to obtain a mixture at a temperature of 340°C; the mixture is then sent to the atmospheric distillation column 1-6 of the atmospheric distillation unit for atmospheric distillation to obtain atmospheric distillation column bottom oil 1-7 and the first light oil (including column top dry gas 1-10, naphtha 1-8 and diesel 1-9);

[0087] The atmospheric distillation column bottom oil 1-7 is sent to the second heater 1-11 of the vacuum distillation unit to obtain heated atmospheric distillation column bottom oil 1-12, the temperature of which is 343°C. The heated atmospheric distillation column bottom oil 1-12 and the heavy component 1-30 are sent together to the vacuum distillation column 1-14 of the vacuum distillation unit for vacuum distillation to obtain vacuum distillation column bottom oil 1-17 and a second light oil (including light wax oil 1-15 and heavy wax oil 1-16).

[0088] S3: The vacuum distillation tower bottom oil is divided into two parts. One part is discharged (the amount of vacuum distillation tower bottom oil discharged from the system accounts for 11.5% of the total amount of vacuum distillation tower bottom oil), and the remaining part is used as circulating oil 1-19. The circulating hydrogen 1-32 and fresh hydrogen feed 1-22 are combined into total hydrogen 1-23 and then sent together with circulating oil 1-32 and catalyst 1-20 to the slurry bed residue oil hydrotreating reactor 1-25 for hydrotreating reaction (at least one of hydrodeoxygenation, hydrodemetallization, hydrodesulfurization and hydrocracking).

[0089] Catalysts 1-20 are molybdenum-based catalysts; the operating conditions of the slurry-bed residue hydrotreating reactor include: reaction pressure 22.0 MPa, reaction temperature 430 °C, and volume hourly space velocity (VHSV) of 0.1 h⁻¹. -1 The hydrogen-to-oil volume ratio is 800:1.

[0090] The raw material oil in Example 1 is raw material 1.

[0091] Example 2

[0092] The only difference between this embodiment and embodiment 1 is that the raw material oil in this embodiment is raw material 2.

[0093] Comparative Example 1

[0094] This comparative example provides a slurry bed reactant hydrogenation method, such as... Figure 2 As shown, the method includes the following steps:

[0095] S1: The product 2-27 from the slurry bed residue hydrotreating reactor is sent to the separation unit 2-8 to separate slurry 2-11, low-grade oil 2-10 and gaseous product 2-9. The gaseous product 2-9 is separated by the hydrogen recovery unit 2-12 to obtain recovered recycled hydrogen 2-13 and discharged light hydrocarbons 2-14.

[0096] S2: The low-grade oil 2-10 is sequentially sent to the low-grade oil heater 2-15 and the low-grade oil atmospheric distillation tower 2-16 for atmospheric distillation to obtain atmospheric bottom oil 2-28, atmospheric tower top dry gas 2-17, atmospheric naphtha 2-18 and atmospheric diesel 2-19.

[0097] The atmospheric pressure bottom oil 2-28 and slurry 2-11 were sent together to the slurry vacuum distillation tower 2-20. After vacuum distillation, vacuum bottom oil 2-23, light wax oil 2-21 and heavy wax oil 2-22 were obtained.

[0098] S3: Divide the vacuum bottom oil 2-23 into two parts, one part is discharged externally, and the remaining part is used as return circulating oil 2-25;

[0099] The recycled oil 2-25, the reaction catalyst 2-26, and the feedstock oil heated by the fresh feed heater 2-2 are sent together to the mixing feed tank 2-3; the recovered recycled hydrogen 2-13 and the new hydrogen 2-4 are heated by the hydrogen mixing heater 2-5 and then sent together with the discharge from the mixing feed tank 2-3 to the slurry bed residue hydrotreating reactor 2-7 for hydrotreating reaction (at least one of hydrodeoxygenation, hydrodemetallization, hydrodesulfurization, and hydrocracking).

[0100] The reaction catalysts 2-26 are the same as those 1-20 in Example 1. The operating conditions (temperature, pressure, etc.) for each step of Comparative Example 1 are the same as those in Example 1.

[0101] The feedstock oil 2-1 for Comparative Example 1 is feedstock 1.

[0102] Comparative Example 2

[0103] The only difference between this comparative example and Comparative Example 1 is that the feedstock oil 2-1 in this comparative example is feedstock 2.

[0104] Raw material 1: 90% Refinery A fuel oil + 10% Refinery A heavy diesel oil. The composition and properties of the raw materials are shown in Table 1.

[0105] Raw material 2: 80% Refinery B fuel oil + 20% Refinery B heavy diesel oil. The composition and properties of the raw materials are shown in Table 1.

[0106] Table 1

[0107]

[0108]

[0109] The product composition, equipment energy consumption, and equipment operation cycle of the method of the present invention and the conventional process of the comparative example were compared using raw material 1 and raw material 2 respectively.

[0110] Table 2 shows the test results of raw material 1 in the method of Example 1 of this invention.

[0111]

[0112] Table 3 shows the test results of raw material 2 in the method of Example 2 of this invention.

[0113]

[0114] Table 4 shows the test results of raw material 1 in the conventional process method of Comparative Example 1.

[0115]

[0116] Table 5 shows the test results of raw material 2 in the conventional process method of Comparative Example 2.

[0117]

[0118]

[0119] As shown in Table 1-5:

[0120] Comparative Example 1 and Comparative Example 1:

[0121] Both methods can achieve the goal of processing feedstock oil, and the products meet the requirements of downstream equipment.

[0122] The energy consumption of the method of the present invention is reduced by 11.5% compared with the energy consumption of the traditional method.

[0123] The continuous running time of the method of this invention is improved by 48.7% compared with the continuous running time of the traditional method.

[0124] The investment accounting method of this invention reduces costs by 7.72% compared to traditional methods.

[0125] Comparative Example 2 and Comparative Example 2:

[0126] Both methods can achieve the goal of processing feedstock oil, and the products meet the requirements of downstream equipment.

[0127] The energy consumption of the method of the present invention is reduced by 12.8% compared with the energy consumption of the traditional method.

[0128] The continuous running time of the method of this invention is improved by 53.6% compared with the continuous running time of the traditional method.

[0129] The investment accounting method of this invention reduces costs by 7.72% compared to traditional methods.

[0130] This invention improves the operating cycle of slurry-bed residue hydrotreating reactors, which is critical for refineries. For typical slurry-bed residue hydrotreating systems, scaling in the fractionation section can cause shutdowns one or more times per year, depending on the feed and severity, and may require more than a month to clean the bottom section of the vacuum distillation column. In many cases, this necessitates operating the entire refinery at below-design capacity. In contrast, this invention utilizes the dissolving and diluting effects of the bottom oil from the vacuum distillation column to improve operations within the slurry-bed residue hydrotreating fractionation system, thereby improving the overall refinery operating cycle. As mentioned above, this invention can further reduce the number of equipment and associated capital expenditures in slurry-bed residue hydrotreating reactors and atmospheric / vacuum distillation units, and can also reduce carbon emissions and plant footprint.

[0131] The various embodiments of the present invention have been described above. These descriptions are exemplary and not exhaustive, nor are they limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A slurry-bed reactant hydrogenation system, characterized in that, The system includes a slurry bed residue hydrotreating reactor, an oil-gas separation unit, an atmospheric distillation unit, a vacuum distillation unit, and a feedstock pipeline; The slurry bed residue hydrotreating reactor is connected to the oil-gas separation unit via a product pipeline; The oil-gas separation unit is equipped with a heavy component discharge pipeline, a medium component discharge pipeline, a light component discharge pipeline, and a circulating hydrogen pipeline. The feed pipeline of the raw material oil merges with the discharge pipeline of the medium component and is then connected to the atmospheric distillation unit; the atmospheric distillation unit is equipped with a bottom oil discharge pipeline of the atmospheric distillation tower and at least one first light oil discharge pipeline. The atmospheric distillation tower bottom oil discharge pipeline merges with the heavy component discharge pipeline and is then connected to the vacuum distillation unit. The vacuum distillation unit is equipped with a vacuum distillation tower bottom oil discharge pipeline and at least one second light oil discharge pipeline. The outlet of the vacuum distillation tower bottom oil discharge pipeline is divided into two paths: one is used as an external discharge pipeline, and the other is used as a circulating oil pipeline. The fresh hydrogen feed pipeline and the circulating hydrogen pipeline merge into a total hydrogen feed pipeline, which, together with the circulating oil pipeline, is connected to the slurry bed residue oil hydrogenation reactor.

2. The slurry-bed reactant hydrogenation system according to claim 1, wherein, The feed oil pipeline is first connected to the feed buffer tank and then merges with the discharge pipeline of the medium-quality components. The slurry bed residue hydrotreating reactor is also connected to a catalyst feed pipeline; The slurry bed residue oil hydrogenation reactor is equipped with at least one slurry bed residue oil hydrogenation reactor.

3. The slurry-bed reactant hydrogenation system according to claim 1, wherein, The oil and gas separation unit includes a heavy hydrogenation product separator, a medium hydrogenation product separator, and a hydrogen recovery separator. The heavy hydrotreating product separator is used to separate the heavy components and gaseous streams from the hydrotreating products of the slurry bed residue hydrotreating reactor. The medium-quality hydrogenation product separator is used to separate the medium-quality components and the hydrogen-containing gaseous light hydrocarbon fraction in the gaseous stream. The hydrogen recovery separator is used to separate the circulating hydrogen and light components in the hydrogen-containing gas phase light hydrocarbon fraction.

4. The slurry-bed reactant hydrogenation system according to claim 1, wherein, The atmospheric distillation unit includes a first heating furnace and an atmospheric distillation column; The feed pipeline of the raw oil and the discharge pipeline of the medium components are connected to the atmospheric distillation tower through the first heating furnace. The bottom oil discharge pipeline of the atmospheric distillation tower and at least one first light oil discharge pipeline are installed on the atmospheric distillation tower; the atmospheric distillation tower is the atmospheric distillation tower in the atmospheric and vacuum distillation unit of the refinery; The first light oil discharge pipeline includes at least one of a naphtha discharge pipeline, a diesel discharge pipeline, and a dry gas discharge pipeline.

5. The slurry-bed reactor hydrogenation system according to claim 1, wherein, The vacuum distillation unit includes a second heating furnace and a vacuum distillation column; The bottom oil discharge pipeline of the atmospheric distillation tower is connected to the second heater and then merges with the heavy component discharge pipeline, and then connects to the vacuum distillation tower. The vacuum distillation tower bottom oil discharge pipeline and at least one second light oil discharge pipeline are installed on the vacuum distillation tower; the vacuum distillation tower is a vacuum distillation tower in the atmospheric and vacuum distillation unit of a refinery. The second light oil discharge pipeline includes at least one of a light wax oil discharge pipeline and a heavy wax oil discharge pipeline.

6. The slurry-bed reactant hydrogenation system according to claim 1, wherein, The system also includes a hydrogen heater, and the main hydrogen feed line is connected to the hydrogen heater and then connected to the slurry bed residue oil hydrogenation reactor together with the circulating oil line.

7. A method for hydrogenating reactants in a slurry bed, characterized in that, The method employs the system described in any one of claims 1-6 and includes the following steps: S1: The effluent from the slurry bed residue hydrotreating reactor is sent to the oil-gas separation unit, where it is separated to obtain heavy components, medium components, light components, and recycled hydrogen; S2: The feedstock oil and the medium components are sent to the atmospheric distillation unit for atmospheric distillation to obtain atmospheric distillation bottom oil and the first light oil; the atmospheric distillation bottom oil and the heavy components are sent to the vacuum distillation unit for vacuum distillation to obtain vacuum distillation bottom oil and the second light oil. S3: The bottom oil of the vacuum distillation tower is divided into two parts, one part is discharged and the remaining part is used as circulating oil; the circulating hydrogen and fresh hydrogen feed are combined into total hydrogen and sent together with the circulating oil to the slurry bed residue oil hydrogenation reactor for hydrogenation reaction.

8. The slurry bed reactant hydrogenation method according to claim 7, wherein, The feedstock oil is at least one of the following: desalted and dehydrated crude oil, residue oil, wax oil, deasphalted oil, bottom stream from atmospheric distillation column, bottom stream from vacuum distillation column, catalytic cracking slurry oil, base oil, tar sand asphalt, tall oil, and black oil. Preferably, the desalted and dehydrated crude oil is at least one of fully electro-desalted and dehydrated crude oil, fully heavy electro-desalted and dehydrated crude oil, and bio-based electro-desalted and dehydrated crude oil; Preferably, the residue oil is atmospheric residue oil containing a flow promoter and / or vacuum residue oil containing a flow promoter, wherein the flow promoter is at least one of naphtha, diesel oil and wax oil; more preferably, the blending ratio of the flow promoter in the residue oil is 0% to 60 wt%. Preferably, the wax oil is vacuum-pressed wax oil and / or coking wax oil; Preferably, the base oil is derived from shale-based oil and / or coal-based oil; Optionally, the feedstock oil undergoes at least one of the following processes before entering the atmospheric distillation unit: straight distillation, process derivatization, hydrocracking, desulfurization, and demetallization.

9. The slurry bed reactant hydrogenation method according to claim 8, wherein, The light component is a hydrocarbon with a boiling point below 35°C; The heavy hydrotreating product separator of the oil-gas separation unit separates the heavy components and gaseous streams from the effluent of the slurry bed residue hydrotreating reactor at a temperature of 350℃~450℃ and a pressure of 0.2MPa~25MPa. The medium-quality hydrogenation product separator of the oil-gas separation unit separates the medium-quality components and hydrogen-containing light hydrocarbon fractions in the gaseous stream at temperatures of 35℃ to 350℃ and pressures of 0.2MPa to 25MPa.

10. The slurry bed reactant hydrogenation method according to claim 8, wherein, The feedstock oil and the medium-quality components are first fed to the first heating furnace of the atmospheric distillation unit to obtain a mixture at a temperature of 300-380°C; the mixture is then fed to the atmospheric distillation column of the atmospheric distillation unit for atmospheric distillation to obtain atmospheric distillation column bottom oil and the first light oil. The bottom oil from the atmospheric distillation column is sent to the second heater of the vacuum distillation unit to obtain heated atmospheric distillation column bottom oil, the temperature of which is 340-380°C; the heated atmospheric distillation column bottom oil and the heavy component are sent together to the vacuum distillation column of the vacuum distillation unit for vacuum distillation to obtain vacuum distillation column bottom oil and a second light oil. The bottom oil of the atmospheric distillation tower is a fraction with a temperature >300℃; The bottom oil of the vacuum distillation tower is a fraction with a temperature >400℃; The first light oil includes at least one of overhead dry gas, naphtha, and diesel oil; The second light oil includes at least one of light wax oil and heavy wax oil.

11. The slurry bed reactant hydrogenation method according to claim 8, wherein, The feed to the slurry bed residue hydrotreating reactor also includes a catalyst, which is at least one of molybdenum, nickel, cobalt, molybdenum alloy, nickel alloy, cobalt alloy, molybdenum-containing cobalt alloy, cobalt-containing and / or molybdenum-containing nickel alloy, molybdenum oxide, nickel oxide and cobalt oxide. The operating conditions of the slurry-bed residue hydrotreating reactor include: reaction pressure of 15.0 MPa to 25.0 MPa, reaction temperature of 380℃ to 450℃, and volume hourly space velocity of 0.05 h⁻¹. -1 ~0.2h -1 The hydrogen-to-oil volume ratio is 500–1200:1; The hydrogenation reaction is at least one of the following: hydrodeoxygenation, hydrodemetallization, hydrodesulfurization, and hydrocracking. The amount of vacuum distillation tower bottom oil discharged from the system accounts for 3-20% of the total amount of vacuum distillation tower bottom oil, and the remainder is used as circulating oil.

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