Hydrodeolefinization process and system for reformate generation

Abstract

The present application relates to the field of oil refining and chemical industry, and discloses a hydrogenation deolefin method and system for reforming oil. The hydrogenation deolefin method for reforming oil comprises: sequentially performing gas phase hydrogenation reaction, gas-liquid separation and liquid phase hydrogenation reaction on reforming oil raw material; the gas phase hydrogenation reaction comprises: performing gas phase hydrogenation reaction on the reforming oil raw material in the presence of hydrogen to obtain a gas phase reaction product; the gas-liquid separation comprises: performing gas-liquid separation on the gas phase reaction product to obtain a gas phase component and a liquid phase component; and the liquid phase hydrogenation reaction comprises: pressurizing the liquid phase component and then performing liquid phase hydrogenation reaction to obtain a liquid phase deolefin reaction product. The method can effectively remove olefins in the reforming oil, well control aromatic loss, save a de-pentane column, simplify the process, improve efficiency and be easy to popularize and apply.

Description

Technical Field

[0001] This invention relates to the field of oil refining and chemical technology, specifically to a method and system for hydrodeolefination of reformed oil. Background Technology

[0002] Reformate is the main product of catalytic reforming technology. It is a light distillate oil rich in aromatics. With the rapid development and expansion of my country's aromatics industry, reformate provides an important source of raw materials for the extraction of chemical feedstocks such as benzene, toluene, and xylene from aromatics. However, due to the harsh reaction conditions of catalytic reforming, reformate contains a certain amount of olefins. Olefins can affect the subsequent aromatics extraction process. Therefore, reformate needs to undergo olefin removal before proceeding to the next extraction step.

[0003] In the past, my country mainly used clay refining to remove olefins from reforming products. However, the used clay is a hazardous chemical, with high subsequent treatment costs and environmental pollution. Therefore, in recent years, clay refining technology has been replaced by selective hydrodeolefins technology, such as the FHDO reforming product selective liquid-phase hydrodeolefins technology developed by FRIPP. This technology uses the HDO-18 precious metal catalyst to remove olefins under mild conditions while retaining aromatics. The process involves the reforming product, after catalytic reforming, passing through a dechlorination tank and a re-contacting tower, entering a liquid-phase hydrotreating reactor, and then entering a depentane tower for separation. The depentane-removed oil at the bottom of the tower is then used for subsequent aromatics extraction.

[0004] However, existing technologies have drawbacks in application. In the initial stage of the reaction in the hydrogenation reactor, the catalyst activity is high, and because some large olefin molecules (C6 and C7) are difficult to remove, the reaction temperature or pressure needs to be increased appropriately. This leads to the loss of aromatics during hydrogenation, especially important chemical products such as benzene, toluene, and xylene. Hydrogenation saturation of these products can reduce the profits of production enterprises.

[0005] Patent application CN107304371A discloses a method for hydrotreating reforming product oil. This method involves connecting the bottom of the depentanizer to the inlet of the hydrotreating reactor. Initially, depentanized oil is introduced, and once the catalyst is initially activated and stabilized, fresh feedstock is introduced to ensure stable product quality in the early stages of the reaction. However, this design carries the risk of pipeline leaks leading to fresh feedstock directly entering the depentanizer, and it also increases process complexity.

[0006] Patent application CN102911721A discloses a method for selective hydrogenation and deolefination of reformed oil in a liquid phase, in which part of the hydrogenated liquid phase product is recycled and then mixed with fresh feedstock and fed into the liquid phase hydrogenation reactor in stages. However, product recycling requires the installation of a circulation pump, increasing the investment in equipment construction, and this invention does not solve the problem of aromatics loss in the early stage of the reaction. Summary of the Invention

[0007] The purpose of this invention is to overcome the shortcomings of the existing technology and provide a method and system for hydrodeolefins of reforming oil. This method can effectively remove olefins from reforming oil, while controlling aromatics loss well, eliminating the need for a depentanizer, simplifying the process, improving efficiency, and making it easy to promote and apply.

[0008] To achieve the above objectives, a first aspect of the present invention provides a method for hydrodeolefination of reformed oil, wherein the method includes:

[0009] The reformed oil feedstock is subjected to gas-phase hydrogenation, gas-liquid separation, and liquid-phase hydrogenation in sequence.

[0010] The gas-phase hydrogenation reaction includes: in the presence of hydrogen, performing a gas-phase hydrogenation reaction on the reformed oil feedstock to obtain a gas-phase reaction product;

[0011] The gas-liquid separation includes: separating the gas-phase reaction products into gas-liquid components to obtain gas-phase components and liquid-phase components;

[0012] The liquid-phase hydrogenation reaction includes: pressurizing the liquid-phase component and then carrying out the liquid-phase hydrogenation reaction to obtain the liquid-phase deolefination reaction product.

[0013] A second aspect of the present invention provides a hydrodeolefination system for reformed oil, wherein the system comprises a gas-phase hydrogenation reactor, a gas-liquid separation unit, a pressurization unit, and a liquid-phase hydrogenation reactor connected in sequence; the liquid phase component outlet of the gas-liquid separation unit is connected to the inlet of the pressurization unit.

[0014] The gas-phase hydrogenation reactor is used to perform a gas-phase hydrogenation reaction between reformed oil feedstock and hydrogen to obtain gas-phase reaction products.

[0015] The pressurization unit is used to pressurize the liquid phase component obtained by the gas-liquid separation unit to obtain a pressurized stream.

[0016] The liquid-phase hydrogenation reactor is used to perform a liquid-phase hydrogenation reaction on the pressurized stream to obtain liquid-phase deolefination reaction products.

[0017] Compared with the prior art, the method of the present invention has the following advantages:

[0018] The method provided by this invention can remove C6 and C7 olefins, which are the most difficult to remove from reformed oils, with a low aromatic loss rate.

[0019] The method provided by this invention involves a gas-phase hydrogenation reaction that fully saturates C6 and lower olefins (approximately 70% of the total olefin content). The gas-phase components are then retained through gas-liquid separation, allowing benzene to enter the gas phase without further hydrogenation saturation. The liquid-phase components (C7 olefins and toluene, ethylbenzene, xylene, etc.) undergo selective hydrogenation to remove olefins, further reducing aromatic hydrocarbon loss.

[0020] The method provided by this invention, preferably, involves a gas-phase hydrogenation reaction carried out under low pressure and a high hydrogen-to-oil ratio, which promotes the hydrogenation reaction of olefins and maximizes the retention of benzene. After the gas-phase hydrogenation reaction, a significant amount of hydrogen is consumed. The dissolved hydrogen liquid phase component is then pressurized to undergo hydrogenation of the heavier components. At this point, because the liquid phase component is in a slightly "hydrogen-poor" state, meaning that a small amount of dissolved hydrogen is used only to meet the hydrogenation needs of C7 olefins, the hydrogenation loss of toluene, ethylbenzene, and xylene is avoided.

[0021] The system provided by this invention eliminates the need for a hydrogen compressor in a fixed-bed reaction system and a circulating oil pump in a liquid-phase hydrogenation reaction system, thereby reducing investment costs, simplifying the process flow, improving reaction efficiency, and reducing reaction severity. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the process flow of the present invention.

[0023] Figure Labels

[0024] Detailed Implementation

[0025] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0026] The description of exemplary embodiments is intended to be read in conjunction with the accompanying drawings, which are considered an integral part of the entire written description. In this specification, relative terms such as “lower,” “upper,” “horizontal,” “vertical,” “above,” “below,” “upward,” “downward,” “top,” and “bottom,” and their derivatives (e.g., “horizontally,” “downward,” “upward,” etc.) should be interpreted as referring to the orientation shown in the accompanying drawings as described at the time. These relative terms are for ease of description and do not require the device to be constructed or operated in a particular orientation. Unless otherwise stated, “connection” as used in this invention refers to a relationship in which structures are directly or indirectly fixed or connected to each other via an intermediate structure.

[0027] In this invention, the symbol “≯” indicates that it is not greater than.

[0028] The first aspect of this invention provides a method for hydrodeolefination of reformed oil, wherein the method includes:

[0029] The reformed oil feedstock is subjected to gas-phase hydrogenation, gas-liquid separation, and liquid-phase hydrogenation in sequence.

[0030] The gas-phase hydrogenation reaction includes: in the presence of hydrogen, the reformed oil feedstock undergoes a gas-phase hydrogenation reaction to obtain a gas-phase reaction product;

[0031] The gas-liquid separation includes: separating the gas-phase reaction products into gas-liquid components to obtain gas-phase components and liquid-phase components;

[0032] The liquid-phase hydrogenation reaction includes: pressurizing the liquid-phase component and then carrying out the liquid-phase hydrogenation reaction to obtain the liquid-phase deolefination reaction product.

[0033] In this invention, the hydrogen gas used in the gas-phase hydrogenation reaction can be any hydrogen-containing gas capable of providing hydrogen, including fresh hydrogen, recycled hydrogen, and hydrogen-rich gas. Those skilled in the art, after understanding the technical solution of this invention, can clearly understand the hydrogen-containing gas described in this invention.

[0034] In this invention, the reforming oil feedstock can be any type of reforming oil that is conventionally required for processing in the art, and the properties of the reforming oil feedstock are not particularly limited. Preferably, the reforming oil has a distillation range of 40-180℃, a bromine index ≤ 8000 mg Br / 100g, and an aromatic content of 60-85 wt%.

[0035] In a preferred embodiment of this invention, the method further includes dechlorinating and / or re-contaminating the reformed oil, followed by a gas-phase hydrogenation reaction. The specific operating methods and conditions for dechlorination and / or re-contamination are not particularly limited in this invention, and those skilled in the art can select them according to actual needs.

[0036] In this invention, the selection range for gas-phase hydrogenation reaction conditions is relatively wide. Preferably, the gas-phase hydrogenation reaction conditions include: a pressure of 0.1-1.5 MPa, a temperature of 80-200°C, a hydrogen-to-oil volume ratio of 3-50, and a volume hourly space velocity of 0.5-10 h⁻¹. -1 Further preferably, the conditions for the gas-phase hydrogenation reaction include: a pressure of 0.3-1 MPa, a temperature of 150-200°C, a hydrogen-to-oil volume ratio of 5-30 (for example, values ​​of 5, 10, 15, 20, 25, 30, or any combination thereof), and a volume hourly space velocity of 4-8 h⁻¹. -1Under relatively low reaction pressure and high hydrogen oil conditions, the gas-phase hydrogenation reaction can remove olefins to the greatest extent while retaining aromatic components.

[0037] In this invention, preferably, the method further includes cooling the gas-phase reaction products by heat exchange before performing the gas-liquid separation.

[0038] The present invention does not particularly limit the specific operation of the heat exchange, and any heat exchange medium conventionally used in the art can be used. The heat exchange can be carried out in a heat exchange unit, such as a heat exchanger. The present invention does not particularly limit the specific type of heat exchanger, for example, it can be a commercially available heat exchanger conventionally defined in the art, or it can be a tubular heat exchanger.

[0039] This invention utilizes a small amount of heat exchange at high temperature for the gas-phase reaction products, preserving a significant amount of heat of reaction while ensuring the liquefaction of macromolecules. This satisfies the feed conditions for a liquid-phase hydrogenation reactor, saving energy. Furthermore, since only C7 olefins and components such as toluene, ethylbenzene, and xylene enter the liquid-phase reaction, the loss of aromatic hydrocarbons due to saturation can be further avoided by controlling the dissolved hydrogen content, reaction conditions, and catalyst selectivity. This invention does not impose particular limitations on the heat exchange conditions; preferably, conditions sufficient to ensure the liquefaction of large, heavy molecular weight substances in the gas-phase reaction products are preferred.

[0040] In this invention, the gas-liquid balance of the effluent after the heat exchanger is achieved, resulting in the upward flow of the gas phase component and the downward flow of the liquid phase component. This invention offers a wide range of conditions for gas-liquid separation, allowing those skilled in the art to make appropriate selections based on the composition of the reformed oil feedstock, ensuring that components requiring further hydrorefining remain in the liquid phase. Preferably, based on the total amount of the gas-phase reaction products, the mass percentage of the liquid phase component is 20-80%, more preferably 40-75%, and even more preferably 60-75%. This preferred embodiment is more advantageous for precisely controlling the separation cut-off point of the aromatic components and preserving the aromatic content.

[0041] In this invention, the selection range for liquid-phase hydrogenation reaction conditions is relatively wide. Preferably, the conditions for the liquid-phase hydrogenation reaction include: a pressure of 1-3 MPa, a temperature of 50-200°C, and a volume hourly space velocity of 0.5-10 h⁻¹. -1 Further preferably, the conditions for the liquid-phase hydrogenation reaction include: a pressure of 1.5-2 MPa, a temperature of 80-150 °C, and a volume hourly space velocity of 6-9 h⁻¹. -1 .

[0042] In this invention, preferably, the pressure of the liquid-phase hydrogenation reaction is at least 0.5 MPa higher than the pressure of the gas-phase hydrogenation reaction, and more preferably 0.5-2 MPa higher. In this invention, by controlling the pressures of the liquid-phase and gas-phase hydrogenation reactions, the selectivity of the hydrogenation reactions of olefins and aromatics in light and heavy components can be improved, retaining aromatics while removing olefins as much as possible.

[0043] In this invention, preferably, the temperature of the liquid-phase hydrogenation reaction is at least 10°C lower than the temperature of the gas-phase hydrogenation reaction, and more preferably 30-50°C lower. The advantage of this preferred embodiment is that it allows for precise control of the separation and cutting point of the aromatic components, preserving the aromatic content.

[0044] In this invention, there is no particular limitation on the type of reactor used in the gas-phase hydrogenation reaction and the liquid-phase hydrogenation reaction. Preferably, the gas-phase hydrogenation reaction and the liquid-phase hydrogenation reaction are each carried out independently in a fixed-bed reactor.

[0045] In this invention, preferably, the gas-phase hydrogenation reaction and the liquid-phase hydrogenation reaction are each carried out independently in the presence of a hydrodeolefination catalyst, which is a noble metal catalyst.

[0046] In this invention, preferably, the noble metal catalyst includes a support and a noble metal component supported on the support.

[0047] In this invention, there is no particular limitation on the type of carrier. For example, a carrier conventionally defined in the art, such as alumina, can be used.

[0048] In this invention, the type of noble metal in the noble metal catalyst is not particularly limited, and can be any noble metal conventionally defined in the art. Preferably, the noble metal component is Pt and / or Pd.

[0049] In this invention, there is no particular limitation on the source of the hydrodeolefin catalyst. For example, it can be prepared by any method or obtained commercially, such as HDO-18 developed by the Fushun Petrochemical Research Institute of Sinopec (FRIPP).

[0050] In this invention, there are no particular limitations on the application of the gaseous component (also referred to as the hydrogenated light component) and the liquid-phase de-olefin reaction product obtained through gas-liquid separation; they can be adapted to meet specific product requirements. Preferably, the method further includes mixing the gaseous component and the liquid-phase de-olefin reaction product to obtain a reformed oil product. Preferably, in this invention, the bromine index of the reformed oil product is ≤100 mg Br / 100 g, and the aromatic hydrocarbon loss rate is less than 0.1%.

[0051] In this invention, the specific operation and conditions for pressurizing the liquid phase component are subject to a wide range of selection. The pressurization is used to increase the pressure of the liquid phase component, preferably to a level sufficient to meet the reaction conditions in the liquid-phase hydrogenation reactor. In this invention, there are no particular limitations on the specific operation of pressurization; a specific process may involve pressurizing the liquid phase component via a pressurization unit (preferably a pressurization pump) to a pressure slightly higher than that required for the liquid-phase reaction.

[0052] A second aspect of the present invention provides a hydrodeolefination system for reformed oil, wherein the system comprises a gas-phase hydrogenation reactor, a gas-liquid separation unit, a pressurization unit, and a liquid-phase hydrogenation reactor connected in sequence; the liquid phase component outlet of the gas-liquid separation unit is connected to the inlet of the pressurization unit.

[0053] The gas-phase hydrogenation reactor is used to perform a gas-phase hydrogenation reaction between reformed oil feedstock and hydrogen to obtain gas-phase reaction products.

[0054] The pressurization unit is used to pressurize the liquid phase component obtained by the gas-liquid separation unit to obtain a pressurized stream.

[0055] The liquid-phase hydrogenation reactor is used to perform a liquid-phase hydrogenation reaction on the pressurized stream to obtain liquid-phase deolefination reaction products.

[0056] In this invention, preferably, the gas-phase hydrogenation reactor and the liquid-phase hydrogenation reactor are each independently packed with a hydrodeolefination catalyst. By matching appropriate catalysts in different reactors and controlling the amount of catalyst used, the hydrodeolefination reaction is achieved.

[0057] In this invention, the types of gas-phase hydrogenation reactors and liquid-phase hydrogenation reactors have been described in the first aspect and will not be repeated here.

[0058] In this invention, preferably, the gas-liquid separation unit is provided with a gas phase component outlet at the top and a liquid phase component outlet at the bottom.

[0059] In this invention, preferably, the bottom of the liquid-phase hydrogenation reactor is provided with a liquid-phase deolefin reaction product outlet.

[0060] Preferably, in this invention, the system further includes a heat exchange unit disposed between the gas-phase hydrogenation reactor and the gas-liquid separation unit. The heat exchange unit is used to exchange heat with the gas-phase reaction products before gas-liquid separation. This invention does not impose any particular limitation on the heat exchange unit; any conventional choice in the art, such as a heat exchanger, can be used.

[0061] In this invention, there is no particular limitation on the gas-liquid separation unit, and it can be any conventional choice in the art, such as a gas-liquid separator.

[0062] In this invention, preferably, the pressurization unit is used to pressurize the liquid phase component, more preferably to pressurize it to a level sufficient to meet the reaction conditions in the liquid phase hydrogenation reactor. The types of pressurization units have already been described in the first aspect of this invention and will not be repeated here.

[0063] The present invention will be described in detail below through embodiments.

[0064] In this invention, unless otherwise explicitly stated, percentages and percentage contents are all expressed by mass.

[0065] The reformed oil feedstock and hydrogen 1 enter the gas phase hydrogenation reactor 2, where a gas phase hydrogenation reaction occurs to obtain a gas phase reaction product 3. This product then enters the heat exchange unit 4 (heat exchanger), where it is cooled before entering the gas-liquid separation unit 5 (gas-liquid separator) to obtain a liquid phase component 6 and a gas phase component 7. The gas phase component 7 is discharged upwards from the gas-liquid separator, while the liquid phase component 6 is discharged downwards. After passing through the pressurization unit 8 (pressurization pump), the product enters the liquid phase hydrogenation reactor 9 for a liquid phase hydrogenation reaction to obtain a liquid phase de-olefin reaction product 10. The gas phase component 7 and the liquid phase de-olefin reaction product 10 are mixed to finally obtain the reformed oil product 11.

[0066] Examples 1-3

[0067] Adopting such Figure 1 The process flow diagram is shown below. Two 100mL fixed-bed hydrogenation reactors are connected in series: a gas-phase hydrogenation reactor and a liquid-phase hydrogenation reactor. A heat exchanger, a gas-liquid separator, and a booster pump are installed between the reactors. The gas-phase hydrogenation reactor is loaded with 60mL of Lpt-Pd type hydrogenation catalyst A, and the liquid-phase hydrogenation reactor is loaded with 40mL of Lpt-Pd type hydrogenation catalyst A. A gas phase component outlet is located above the gas-liquid separator, which connects to the bottom effluent of the liquid-phase hydrogenation reactor, and together they yield the reformed product oil.

[0068] Reformed oil was used as feedstock. Catalyst properties are shown in Table 1, feedstock oil properties are shown in Table 2, and reaction process conditions and results are shown in Table 3.

[0069] Example 4

[0070] The process flow is the same as in Examples 1-3, except that the liquid phase reaction pressure is increased. The reaction process conditions and results are shown in Table 3.

[0071] Example 5

[0072] The process flow is the same as in Examples 1-3, except that the liquid phase reaction temperature is increased. The reaction process conditions and results are shown in Table 3.

[0073] Example 6

[0074] Examples 1-3 follow the same process flow, differing only in reducing the hydrogen-to-oil volume ratio at the inlet of the gas-phase hydrogenation reactor and replacing the booster system (booster pump) before the liquid-phase hydrogenation reactor with a booster and hydrogen mixing system. The gas-phase hydrogenation reactor is loaded with 60 mL of Pt-Pd type hydrogenation catalyst A, and the liquid-phase hydrogenation reactor is loaded with 40 mL of Pt-Pd type hydrogenation catalyst A. The reaction process conditions and results are shown in Table 3.

[0075] Comparative Example 1

[0076] A conventional fixed-bed hydrogenation process was adopted, with only one hydrogenation reactor. The gas-phase hydrogenation reactor was loaded with 100 mL Pt-Pd type hydrogenation catalyst A. After hydrogen sulfide removal, the hydrogen was pressurized and recycled using a circulating hydrogen compressor. The properties of the feedstock and catalyst were the same as in Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0077] Comparative Example 2

[0078] A conventional liquid-phase hydrogenation process was adopted, with only one liquid-phase hydrogenation reactor. The liquid-phase hydrogenation reactor was loaded with 100 mL Pt-Pd type hydrogenation catalyst A. Hydrogen gas was mixed with feedstock oil via a hydrogen mixer before entering the reactor. The properties of the feedstock and catalyst were the same as in Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0079] Table 1

[0080]

[0081] Table 2

[0082]

[0083] Table 3

[0084]

[0085] Note: In Table 3, the hydrogen replenishment amount refers to the amount relative to 1m. 3 The amount of hydrogen required to supplement the liquid phase components.

[0086] As shown in Table 3, Comparative Example 1 uses conventional fixed-bed hydrogenation technology, which requires a circulating hydrogen compressor, resulting in high costs and significant aromatic hydrocarbon losses. Comparative Example 2 uses liquid-phase hydrogenation technology, which requires dissolving hydrogen in one step to meet the hydrogen consumption of the reaction, thus requiring higher pressure and leading to increased aromatic hydrocarbon losses.

[0087] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for hydrodeolefination of reformed oil, characterized in that, The method includes: The reformed oil feedstock is subjected to gas-phase hydrogenation, gas-liquid separation, and liquid-phase hydrogenation in sequence. The gas-phase hydrogenation reaction includes: in the presence of hydrogen, the reformed oil feedstock undergoes a gas-phase hydrogenation reaction to obtain a gas-phase reaction product; The gas-liquid separation includes: separating the gas-phase reaction products into gas-liquid components to obtain gas-phase components and liquid-phase components; The liquid-phase hydrogenation reaction includes: pressurizing the liquid-phase component and then carrying out the liquid-phase hydrogenation reaction to obtain the liquid-phase deolefination reaction product; The pressure of the liquid-phase hydrogenation reaction is at least 0.5 MPa higher than the pressure of the gas-phase hydrogenation reaction; The gas-phase hydrogenation reaction and the liquid-phase hydrogenation reaction are each carried out independently in a fixed-bed reactor; The conditions for the gas-phase hydrogenation reaction include: a pressure of 0.1-1 MPa, a temperature of 150-200℃, a hydrogen-to-oil volume ratio of 3-50, and a volume hourly space velocity of 0.5-10 h⁻¹. -1 ; Based on the total amount of the gas-phase reaction products, the mass percentage of the liquid-phase components is 20-80%; The conditions for the liquid-phase hydrogenation reaction include: a pressure of 1-2 MPa, a temperature of 50-200 °C, and a volume hourly space velocity of 0.5-10 h⁻¹. -1 ; The temperature of the liquid-phase hydrogenation reaction is at least 10°C lower than the temperature of the gas-phase hydrogenation reaction; The gas-phase hydrogenation reaction and the liquid-phase hydrogenation reaction are each carried out independently in the presence of a hydrodeolefination catalyst, which is a noble metal catalyst. The method also includes mixing the gas phase component with the liquid phase deolefination reaction product to obtain a reformed oil product.

2. The method according to claim 1, wherein, The reformed oil has a distillation range of 40-180℃, a bromine index of ≤8000mgBr / 100g, and an aromatic content of 60-85wt%.

3. The method according to claim 1, wherein, The conditions for the gas-phase hydrogenation reaction include: a pressure of 0.3-1 MPa, a temperature of 170-200℃, a hydrogen-to-oil volume ratio of 5-30, and a volume hourly space velocity of 4-8 h⁻¹. -1 .

4. The method according to any one of claims 1-3, wherein, The method further includes cooling the gas-phase reaction products by heat exchange before performing the gas-liquid separation.

5. The method according to any one of claims 1-3, wherein, Based on the total amount of the gas phase reaction products, the mass percentage of the liquid phase components is 40-75%.

6. The method according to any one of claims 1-3, wherein, The conditions for the liquid-phase hydrogenation reaction include: a pressure of 1.5-2 MPa, a temperature of 80-150 °C, and a volume hourly space velocity of 6-9 h⁻¹. -1 .

7. The method according to any one of claims 1-3, wherein, The pressure of the liquid-phase hydrogenation reaction is 0.5-2 MPa higher than that of the gas-phase hydrogenation reaction.

8. The method according to any one of claims 1-3, wherein, The temperature of the liquid-phase hydrogenation reaction is 30-50°C lower than that of the gas-phase hydrogenation reaction.

9. The method according to any one of claims 1-3, wherein, The noble metal catalyst includes a support and a noble metal component supported on the support.

10. The method according to claim 9, wherein, The noble metal component is Pt and / or Pd.

11. The method according to any one of claims 1-3, wherein, The reformed oil product has a bromine index ≤100mgBr / 100g and an aromatics loss rate of less than 0.1%.

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