Hydrogenation system comprising on-line blending device

Abstract

The utility model discloses a hydrogenation system comprising an on-line blending device, and relates to the field of petrochemical hydrogenation, the hydrogenation system comprises a raw oil buffer tank, a reaction device, a steam stripping device, a fractionation device and an on-line blending device, an outlet of the fractionation device is connected with the raw oil buffer tank through a first pipeline; the first pipeline is sequentially provided with a first regulating valve and a second regulating valve from the outlet of the fractionation device; the on-line blending device comprises a passivation oil tank of which the feed port is connected with the outlet of the fractionation device through a second pipeline, and the discharge port of the passivation oil tank is connected with a raw oil buffer tank through a third pipeline; the second pipeline is sequentially provided with a third regulating valve and a fourth regulating valve from one end of the fractionation device, and product oil is produced from one end, which is not connected with the passivation oil tank, of the second pipeline. The self-produced oil product of the hydrogenation system is used for online blending of the passivated oil, the use amount of finished oil in blending of the passivated oil is remarkably reduced, a qualified product tank is directly improved after the product is qualified, and the yield of unqualified diesel oil is reduced.

Description

Technical Field

[0001] This application relates to the field of petrochemical hydrogenation, and more particularly to a hydrogenation system including an online blending unit. Background Technology

[0002] Diesel hydrorefining mainly refers to the processing of oil products in the presence of catalysts and hydrogen, where hydrocarbon molecules undergo a hydrogenation saturation reaction, while simultaneously removing impurities such as sulfur and nitrogen. Figure 1 These are schematic diagrams of some existing hydrogenation systems, where 1 is the feedstock buffer tank, 2 is the reactor, 3 is the stripping tower, 4 is the fractionation tower, and 5 is the circulating hydrogen desulfurization tower. The feedstock to be hydrogenated enters the feedstock buffer tank 1, and after pressurization, it enters the hydrorefining reactor 2, which typically contains a catalyst bed. The effluent from reactor 2 undergoes three-phase separation of oil, gas, and water in a high-pressure separator. The hot high-phase oil phase enters the low-pressure separator, where it exchanges heat to form cold low-phase oil, which then enters the diesel stripping tower 3. Acidic gas is produced at the top of the tower, and the effluent from the bottom enters the fractionation tower 4, where naphtha and refined diesel are produced through fractionation. The refined diesel is directly sent to the finished product tank. Additionally, the hot high-phase gas exchanges heat to form cold high-phase gas, which then enters the circulating hydrogen desulfurization tower 5.

[0003] In the catalytic hydrogenation reaction unit, the catalyst, after sulfidation, forms a sulfidated metallic active phase, which significantly improves the catalytic hydrogenation performance. However, directly introducing low-quality secondary processing feedstock or feedstock with a high bromine value after sulfidation can lead to excessive coke deposition, reducing catalyst activity and even causing irreversible deactivation. Therefore, during the start-up phase of industrial hydrogenation systems, the sulfidated catalyst is typically subjected to at least 72 hours of initial activation stabilization (i.e., passivation of the hydrogenation catalyst) to ensure optimal catalyst activity and stability and reduce the deactivation rate. AkzoNobel's research found that directly introducing low-quality secondary processing feedstock after sulfidation results in catalyst activity that is approximately 10% lower than that of a catalyst that has undergone 72 hours of initial activation stabilization after sulfidation, and this activity loss is irreversible. The initial activation stabilization process primarily promotes the formation of coke deposits on the active phase, and the presence of these coke deposits can moderately modify the surface structure of the active phase, contributing to improved catalyst stability.

[0004] Currently, domestic refineries generally use atmospheric diesel for catalyst passivation. However, with the increasing deterioration of raw material quality, the bromine value of atmospheric diesel is constantly rising, making it unable to meet the demand for passivation oil. Therefore, it is necessary to use refined oil with a lower bromine value for blending, which seriously affects the company's economic benefits. At the same time, in the initial stage of passivation, the diesel produced by the hydrotreating system cannot meet the requirements for qualified products and enters the unqualified product tank. This leads to an increase in unqualified products for the company, which is detrimental to hydrotreating production. Utility Model Content

[0005] To address the shortcomings of existing technologies, this application provides a hydrogenation system that includes an online blending device. Using this hydrogenation system for start-up passivation can significantly reduce the amount of finished oil used in the passivation oil blending process. At the same time, once the product is qualified, the qualified product tank can be directly improved, which can reduce the production of unqualified diesel.

[0006] This application provides a hydrogenation system including an online blending device, comprising a feedstock buffer tank, a reaction unit, a stripping unit, a fractionation unit, and an online blending device. The outlet of the fractionation unit is connected to the feedstock buffer tank via a first pipeline. The first pipeline is provided with a first regulating valve and a second regulating valve sequentially starting from the outlet of the fractionation unit.

[0007] The online blending device includes: a passivation oil tank whose inlet is connected to the outlet of the fractionation unit via a second pipeline, and whose outlet is connected to the raw material oil buffer tank via a third pipeline; the second pipeline is provided with a third regulating valve and a fourth regulating valve in sequence from one end of the fractionation unit, and the product oil is produced from the end of the second pipeline that is not connected to the passivation oil tank.

[0008] In an embodiment of this application, the first pipeline is provided with a first flow meter between the first regulating valve and the second regulating valve.

[0009] In an embodiment of this application, the second pipeline is provided with a second flow meter before the third regulating valve.

[0010] In an embodiment of this application, a fifth regulating valve is provided on the third pipeline.

[0011] In an embodiment of this application, a sixth regulating valve is provided at the end of the second pipeline that produces product oil.

[0012] In an embodiment of this application, the reaction apparatus includes a reactor and a connected separator, wherein the reactor is filled with a protective agent and a hydrogenation catalyst; the liquid phase outlet of the separator is connected to the inlet of a stripping unit.

[0013] Compared with existing technologies, the hydrogenation system provided in this application includes: a feedstock buffer tank, a reaction unit, a stripping unit, a fractionation unit, and an online blending unit. The outlet of the fractionation unit is connected to the feedstock buffer tank via a first pipeline. The first pipeline is equipped with a first regulating valve and a second regulating valve sequentially starting from the outlet of the fractionation unit. The online blending unit includes: a passivation oil tank whose inlet is connected to the outlet of the fractionation unit via a second pipeline, and whose outlet is connected to the feedstock buffer tank via a third pipeline. The second pipeline is equipped with a third regulating valve and a fourth regulating valve sequentially starting from one end of the fractionation unit, and product oil is produced from the end of the second pipeline not connected to the passivation oil tank. In the initial passivation stage of the hydrogenation system described in this application, the first and second regulating valves are opened, and diesel fuel enters the feedstock buffer tank. The valve opening is adjusted according to the passivation oil flow rate and index requirements, as well as the bromine value and sulfur content of the diesel fuel. Simultaneously, the third and fourth regulating valves are opened, allowing the remaining blended oil to enter the passivation oil tank for use. Open the diesel valve in the passivation oil tank to complete the blending of passivation oil within the tank. During the later stages of passivation in the hydrotreating system, when the blended oil meets the product diesel specifications, close the second and fourth regulating valves, close the diesel feedstock buffer tank valve, and then open the fifth and sixth regulating valves. The system's product oil can then be fed into the qualified oil tank, while the passivation oil is dispensed from the passivation oil tank until passivation is complete. This start-up method uses the hydrotreating system's own produced oil to blend the passivation oil online, significantly reducing the amount of finished oil used in the passivation oil blending process. Furthermore, once the product is qualified, the qualified product tank can be directly improved, reducing the production of substandard diesel. Attached Figure Description

[0014] The above and other features, advantages, and aspects of the embodiments of this application will become more apparent from the accompanying drawings and the following detailed description. Throughout the drawings, the same or similar reference numerals denote the same or similar elements. It should be understood that the drawings are schematic, and the originals and elements are not necessarily drawn to scale.

[0015] Figure 1 Here are some schematic diagrams of existing hydrogenation systems;

[0016] Figure 2 A schematic diagram of the structure and flow of a hydrogenation system including an online blending device is provided for embodiments of this application;

[0017] Figure label:

[0018] 1-Raw oil buffer tank; 2-Reaction unit; 3-Stripping unit; 4-Fracturing unit; 5-Passivation oil tank; 101-First flow meter; 201-Second flow meter; ZT-A-First regulating valve; ZT-B-Second regulating valve; ZT-C-Third regulating valve; ZT-D-Fourth regulating valve; ZT-E-Fif-Sixth regulating valve. Detailed Implementation

[0019] The embodiments of this application are described below with reference to the accompanying drawings. The terminology used in the implementation section of this application is only for explaining specific embodiments and is not intended to limit the application. Those skilled in the art will recognize that, with technological advancements and the emergence of new scenarios, the technical solutions provided in the embodiments of this application are also applicable to similar technical problems.

[0020] The terms "first," "second," etc., used in the specification, claims, and accompanying drawings of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such terms are interchangeable where appropriate; this is merely a way of distinguishing objects with the same attributes in the embodiments of this application. Furthermore, the terms "comprising" and "having," and any variations thereof, are intended to cover non-exclusive inclusion, so that a process, method, system, product, or apparatus that comprises a series of elements is not necessarily limited to those elements, but may include other elements not explicitly listed or inherent to those processes, methods, products, or apparatuses.

[0021] This application provides a hydrogenation system including an online blending device, comprising a feedstock buffer tank, a reaction unit, a stripping unit, a fractionation unit, and an online blending device. The outlet of the fractionation unit is connected to the feedstock buffer tank via a first pipeline. The first pipeline is provided with a first regulating valve and a second regulating valve sequentially starting from the outlet of the fractionation unit.

[0022] The online blending device includes: a passivation oil tank whose inlet is connected to the outlet of the fractionation unit via a second pipeline, and whose outlet is connected to the raw material oil buffer tank via a third pipeline; the second pipeline is provided with a third regulating valve and a fourth regulating valve in sequence from one end of the fractionation unit, and the product oil is produced from the end of the second pipeline that is not connected to the passivation oil tank.

[0023] Using the hydrogenation system, which includes the online blending unit, for start-up passivation can significantly reduce the amount of finished oil used in the passivation oil blending process. At the same time, once the product is qualified, the qualified product tank can be directly improved, reducing the production of unqualified diesel.

[0024] See Figure 2 , Figure 2 This application provides a schematic diagram of the structure and flow of a hydrogenation system including an online blending device. The hydrogenation system may include a feedstock buffer tank 1, a reaction unit 2, a stripping unit 3, a fractionation unit 4, and an online blending device. The online blending device includes a passivation tank 5, as well as some pipelines and regulating valves.

[0025] The crude oil buffer tank 1 has a diesel inlet, a blending oil inlet, and respective control valves. The crude oil buffer tank is well-known to those skilled in the art and is not subject to any particular limitation.

[0026] The reaction unit 2 includes a reactor and a connected separator. The reactor is filled with a protective agent and a hydrogenation catalyst, and can perform start-up passivation and catalytic hydrogenation reactions. A hydrogenation feed pump, a heat exchanger, and a heater are also provided between the feedstock buffer tank 1 and the reaction unit 2. The blended oil (feedstock oil) enters the reactor of the reaction unit 2 after being pressurized by the hydrogenation feed pump, heated by the heat exchanger and heater, and passed through the feedstock buffer tank 1. The reaction unit 2 may include a compressor, a high-pressure separator, etc., all of which are conventional equipment in the art. For example, the liquid phase outlet of the separator is connected to the inlet of the stripping unit.

[0027] Specifically, the stripping unit 3 can be a stripping tower, and the fractionation unit 4 can be a fractionation tower; this application does not impose any specific limitations. In the embodiments of this application, the product flowing out of the reaction device 2 undergoes gas-liquid phase separation in a separator. The liquid phase passes through the stripping tower and the fractionation tower, and then flows out from the bottom of the fractionation tower.

[0028] Furthermore, the outlet of the fractionation unit 4 is connected to the feedstock buffer tank 1 via a first pipeline, allowing the oil flowing out from the bottom of the tower to enter the feedstock buffer tank 1. Starting from the bottom outlet of the fractionation unit 4, the first pipeline is sequentially equipped with a first regulating valve ZT-A and a second regulating valve ZT-B; preferably, a first flow meter 101 is installed between the two regulating valves.

[0029] The hydrogenation system described in this application includes an online blending device, comprising: a passivation oil tank 5 whose inlet is connected to the outlet of the fractionation unit 4 via a second pipeline; and an outlet of the passivation oil tank 5 connected to a feedstock oil buffer tank 1 via a third pipeline, for online blending of passivation oil and introduction into the feedstock oil buffer tank 1. Starting from one end of the fractionation unit 4, the second pipeline is sequentially equipped with a third regulating valve ZT-C and a fourth regulating valve ZT-D, and product oil is produced from the end of the second pipeline not connected to the passivation oil tank 5.

[0030] In some preferred embodiments of this application, a second flow meter 201 is provided before the third regulating valve ZT-C in the second pipeline; and / or, a fifth regulating valve ZT-E is provided on the third pipeline. Furthermore, a sixth regulating valve ZT-F is provided at the end of the second pipeline where the product oil is produced.

[0031] Specifically, in this embodiment, the fractionation tower outlet is connected to the feedstock buffer tank 1 via a first regulating valve ZT-A, a first flow meter 101, and a second regulating valve ZT-B. It is also connected to the passivation oil tank 5 via a first regulating valve ZT-A, a second flow meter 201, a third regulating valve ZT-C, and a fourth regulating valve ZT-D. The passivation oil tank 5 is connected to the feedstock buffer tank 1 via a fifth regulating valve ZT-E. Furthermore, it is connected to the finished product oil tank via a first regulating valve ZT-A, a second flow meter 201, a third regulating valve ZT-C, and a sixth regulating valve ZT-F. This embodiment allows for the control of material flow rate through the cooperation of flow meters and regulating valves; the valves and flow meters are components well-known to those skilled in the art.

[0032] In the initial passivation stage of the hydrogenation system described in this application embodiment, the first regulating valve ZT-A (fully open) and the second regulating valve ZT-B are opened, allowing diesel fuel to enter the feedstock buffer tank 1. The valve opening is adjusted according to the passivation oil flow rate and index requirements, as well as the bromine value and sulfur content of the diesel fuel. During this initial passivation stage, the flow rate of blended oil entering the feedstock buffer tank is adjusted by controlling the opening of the second regulating valve ZT-B according to the blending ratio. The remaining portion enters the passivation oil tank, and its flow rate is observed using a mass flow meter. Simultaneously, the third regulating valve ZT-C and the fourth regulating valve ZT-D are opened, allowing the remaining blended oil to enter the passivation oil tank 5 for later use. The diesel valve in the passivation oil tank is opened to complete the blending of the passivation oil in the passivation oil tank 5. During the blending process in the passivation oil tank 5, conventional diesel fuel (referred to as "conventional diesel") can be added to the tank simultaneously in a certain proportion or blended later.

[0033] During the later stages of passivation after the start-up of the hydrogenation system, when the blended oil meets the product diesel specifications, the second regulating valve ZT-B and the fourth regulating valve ZT-D are closed, and the diesel feedstock buffer tank valve is closed. The fifth regulating valve ZT-E and the sixth regulating valve ZT-F can then be opened, allowing the system's product oil to enter the qualified oil tank (finished product tank). The passivation oil is then dispensed from the passivation oil tank until passivation is complete. During the later stages of passivation after the start-up of the hydrogenation system, when the oil stored in passivation oil tank 5 meets the system's 72-hour passivation requirement (online blending and passivation time + passivation tank dispensing time), the online blending of the passivation oil is completed. If the blended oil quality meets the product oil standards, the qualified oil tank is improved; if the blended oil quality does not meet the product oil standards, the unqualified oil tank is improved.

[0034] In some specific embodiments of this application, the passivation oil specifications are as follows: bromine value < 2 g / 100 g, sulfur content ≥ 3000 ppm. The self-produced blended oil of the hydrogenation system has a bromine value ≤ 0.5 g / 100 g and a sulfur content < 100 ppm. As feedstock, diesel oil from the tank farm can have a bromine value of 3-10 g / 100 g and a sulfur content > 5000 ppm. Some self-produced blended oils (too low sulfur content) and conventional diesel oil (too high bromine value) do not meet the passivation oil specifications. During the initial passivation stage of the hydrogenation system and the online blending stage of the passivation oil, the valve opening is adjusted according to the passivation oil specifications, the bromine value of the diesel oil, and the sulfur content to ensure that the blended product meets the passivation oil specifications, achieving simultaneous passivation and blending, thus allowing the self-produced substandard oil to replace the finished diesel oil.

[0035] Preferably, the total amount of blended oil and diesel entering the feedstock oil buffer tank 1 is equal to the amount of oil dispensed from the feedstock oil buffer tank, and the liquid level in the feedstock oil buffer tank 1 can be maintained at 80%. In some embodiments, the flow rate of passivation oil entering the reaction unit can be 120 t / h; the flow rate of diesel entering the feedstock oil buffer tank is 30-55 t / h, and the flow rate of diesel entering the passivation oil tank is 8-45 t / h.

[0036] In summary, the start-up system and method of this application use self-produced oil from the hydrogenation system to perform online blending and passivation oil, which greatly reduces the amount of finished oil used in the passivation oil blending process. At the same time, after the product is qualified, the qualified product tank can be directly improved to reduce the production of unqualified diesel.

[0037] To better understand the technical content of this application, specific embodiments are provided below to further illustrate this application. All the following embodiments employ... Figure 2 The hydrogenation system shown is in operation, primarily using the system's own produced oil for online blending. The reactor is filled with a protective agent and a hydrogenation catalyst. The fractionation tower outlet is connected to feedstock buffer tank 1 via first regulating valve ZT-A, first flow meter 101, and second regulating valve ZT-B. It is also connected to passivation tank 5 via first regulating valve ZT-A, second flow meter 201, third regulating valve ZT-C, and fourth regulating valve ZT-D. Passivation tank 5 is connected to feedstock buffer tank 1 via fifth regulating valve ZT-E. Furthermore, it is connected to the finished product tank via first regulating valve ZT-A, second flow meter 201, third regulating valve ZT-C, and sixth regulating valve ZT-F. The total amount of blended oil and diesel entering feedstock buffer tank 1 equals the feedstock buffer tank's output, and the liquid level in feedstock buffer tank 1 is maintained at 80%.

[0038] Example 1

[0039] The passivation oil flow rate is 100 t / h, with the following specifications; the passivation oil in the passivation oil tank is simultaneously being blended online in real time. Furthermore, the system's self-produced blended oil and regular diesel fuel data are as follows.

[0040] Table 1 Passivation Oil Indicators:

[0041] project unit index Dry ℃ 315-370 Sulfur content ppm ≮3000 bromine value g / 100g ＜2 density <![CDATA[g / cm 3 ]]> 0.82-0.86

[0042] Table 2: System-produced blended oil test data:

[0043] project unit Test data Dry ℃ 345.2 Sulfur content ppm 60.8 bromine value g / 100g 0.36 density <![CDATA[g / cm 3 ]]> 816.2

[0044] Table 3 Changchai test data:

[0045] project unit Test data Dry ℃ 361.1 Sulfur content ppm 14500 bromine value g / 100g 5.5 density <![CDATA[g / cm 3 ]]> 857.8

[0046] The passivation oil flow rate into the reaction unit is 120 t / h, the flow rate reading of the first flow meter 101 is 75 t / h, the flow rate reading of the second flow meter 201 is 40 t / h, the flow rate of the diesel fuel entering the feed oil buffer tank is 45 t / h, and the flow rate of the diesel fuel entering the passivation oil tank is 35 t / h; the oil quality indicators are as follows.

[0047] Table 4. Detection data of passivation oil in the feedstock buffer tank:

[0048] project unit Test data Dry ℃ 350.3 Sulfur content ppm 5426 bromine value g / 100g 1.32 density <![CDATA[g / cm 3 ]]> 829.5

[0049] Table 5. Detection data of passivating oil in the passivating oil tank:

[0050]

[0051]

[0052] Example 2

[0053] The passivation oil flow rate is 120 t / h, with the following specifications; the passivation oil in the passivation oil tank is simultaneously being blended online in real time. Furthermore, the system's self-produced blended oil and regular diesel fuel data are as follows.

[0054] Table 6 Passivation Oil Indicators:

[0055] project unit index Dry ℃ 315-370 Sulfur content ppm ≮3000 bromine value g / 100g ＜2 density <![CDATA[g / cm 3 ]]> 0.82-0.86

[0056] Table 7. Test data of blended oil produced by the unit system:

[0057] project unit Test data Dry ℃ 345.2 Sulfur content ppm 60.8 bromine value g / 100g 0.36 density <![CDATA[g / cm 3 ]]> 816.2

[0058] Table 8 Changchai Test Data:

[0059] project unit Test data Dry ℃ 361.1 Sulfur content ppm 14500 bromine value g / 100g 5.5 density <![CDATA[g / cm 3 ]]> 857.8

[0060] The passivation oil flow rate into the reaction unit is 120 t / h, the flow reading of the first flow meter 101 is 65 t / h, the flow reading of the second flow meter 201 is 50 t / h, the flow rate of the diesel fuel entering the feed oil buffer tank is 55 t / h, and the flow rate of the diesel fuel entering the passivation oil tank is 40 t / h; the oil quality indicators are as follows.

[0061] Table 9. Detection data of passivated oil in the feedstock buffer tank:

[0062] project unit Test data Dry ℃ 352.1 Sulfur content ppm 5823 bromine value g / 100g 1.58 density <![CDATA[g / cm 3 ]]> 832.1

[0063] Table 10. Detection data of passivation oil in the passivation oil tank:

[0064] project unit Test data Dry ℃ 352.5 Sulfur content ppm 5835 bromine value g / 100g 1.61 density <![CDATA[g / cm 3 ]]> 835.6

[0065] Example 3

[0066] The passivation oil flow rate is 120 t / h, with the following specifications; the passivation oil in the passivation oil tank is simultaneously being blended online in real time. Furthermore, the system's self-produced blended oil and regular diesel fuel data are as follows.

[0067] Table 11 Passivation Oil Indicators:

[0068] project unit index Dry ℃ 315-370 Sulfur content ppm ≮3000 bromine value g / 100g ＜1 density <![CDATA[g / cm 3 ]]> 0.82-0.86

[0069] Table 12 Test data of self-produced blended oil from the unit system:

[0070] project unit Test data Dry ℃ 340.1 Sulfur content ppm 11 bromine value g / 100g 0.1 density <![CDATA[g / cm 3 ]]> 812.2

[0071] Table 13 Changchai Test Data:

[0072] project unit Test data Dry ℃ 363.1 Sulfur content ppm 14700 bromine value g / 100g 3.6 density <![CDATA[g / cm 3 ]]> 858.2

[0073] The passivation oil flow rate into the reaction unit is 120 t / h, the flow reading of the first flow meter 101 is 90 t / h, the flow reading of the second flow meter 201 is 25 t / h, the flow rate of the diesel fuel entering the feed oil buffer tank is 30 t / h, and the flow rate of the diesel fuel entering the passivation oil tank is 8 t / h; the oil quality indicators are as follows.

[0074] Table 14. Detection data of passivation oil in the feedstock buffer tank:

[0075] project unit Test data Dry ℃ 346.2 Sulfur content ppm 3852 bromine value g / 100g 0.9 density <![CDATA[g / cm 3 ]]> 826.1

[0076] Table 15. Detection data of passivation oil in the passivation oil tank:

[0077]

[0078]

[0079] As can be seen from the above embodiments, in the initial stage of passivation during the start-up of the hydrogenation system described in this application embodiment, the first and second regulating valves are opened, and diesel fuel enters the feedstock buffer tank. The valve opening is adjusted according to the passivation oil flow rate and index requirements, as well as the bromine value and sulfur content of the diesel fuel. Simultaneously, the third and fourth regulating valves are opened, allowing the remaining blended oil to enter the passivation oil tank for use. The diesel valve in the passivation oil tank is opened to complete the blending of the passivation oil in the passivation oil tank. In the later stage of passivation during the start-up of the hydrogenation system, when the blended oil meets the product diesel fuel index, the second and fourth regulating valves are closed, the diesel fuel feedstock buffer tank valve is closed, and the fifth and sixth regulating valves can be opened. The system product oil can enter the qualified oil tank, and the passivation oil is dispensed from the passivation oil tank until the passivation is completed. The start-up method described uses the hydrogenation system's own produced oil to blend and passivate oil online, significantly reducing the amount of finished oil used in the passivation oil blending process. At the same time, after the product is qualified, the qualified product tank can be directly improved, reducing the production of unqualified diesel fuel.

[0080] This document uses specific examples to illustrate the principles and implementation methods of this application. The examples are merely for the purpose of helping to understand the device technology and core ideas of this application. The above descriptions are only preferred embodiments of this application. It should be noted that due to the limitations of written expression, and the existence of an infinite number of specific structures, those skilled in the art can make various improvements, modifications, or variations without departing from the principles of this application, and can also combine the above technical features in an appropriate manner. These improvements, modifications, variations, or combinations, or the direct application of the concept and technical solution of this application to other situations without modification, should all be considered within the scope of protection of this application.

Claims

1. A hydrogenation system including an online blending device, characterized in that, It includes a feedstock oil buffer tank (1), a reaction device (2), a stripping device (3), a fractionation device (4), and an online blending device. The outlet of the fractionation device (4) is connected to the feedstock oil buffer tank (1) through a first pipeline. The first pipeline is equipped with a first regulating valve and a second regulating valve in sequence starting from the outlet of the fractionation device. The online blending device includes: a passivation oil tank (5) whose inlet is connected to the outlet of the fractionation device (4) via a second pipeline; the outlet of the passivation oil tank (5) is connected to the raw material oil buffer tank (1) via a third pipeline; the second pipeline is provided with a third regulating valve and a fourth regulating valve in sequence starting from one end of the fractionation device, and the product oil is produced from the end of the second pipeline that is not connected to the passivation oil tank.

2. The hydrogenation system according to claim 1, characterized in that, The first pipeline is equipped with a first flow meter between the first regulating valve and the second regulating valve.

3. The hydrogenation system according to claim 1, characterized in that, The second pipeline is equipped with a second flow meter before the third regulating valve.

4. The hydrogenation system according to any one of claims 1-3, characterized in that, A fifth regulating valve is installed on the third pipeline.

5. The hydrogenation system according to claim 4, characterized in that, A sixth regulating valve is provided at the end of the second pipeline where the product oil is produced.

6. The hydrogenation system according to any one of claims 1-3, characterized in that, The reaction device (2) includes a reactor and a connected separator. The reactor is filled with a protective agent and a hydrogenation catalyst. The liquid phase outlet of the separator is connected to the inlet of the stripping device (3).

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