Hydrodeolefination method and system of reformate

Abstract

The invention relates to the technical field of oil refining and chemical engineering, and discloses a hydrogenation olefin removal method and system for reformate. The invention relates to a hydrogenation olefin removal method for reformate. The method comprises the following steps: sequentially carrying out gas-phase hydrogenation reaction, gas-liquid separation and liquid-phase hydrogenation reaction on a reformate raw material, the gas-phase hydrogenation reaction comprises the following steps: in the presence of hydrogen, carrying out gas-phase hydrogenation reaction on the reformate raw material to obtain a gas-phase reaction product; the gas-liquid separation comprises the following steps: carrying out gas-liquid separation on the gas-phase reaction product to obtain a gas-phase component and a liquid-phase component; the liquid-phase hydrogenation reaction comprises the following steps: pressurizing the liquid-phase component, and then carrying out the liquid-phase hydrogenation reaction to obtain a liquid-phase deolefination reaction product. The method can effectively remove the olefin in the reformate, well controls the loss of aromatic hydrocarbon, omits a depentanizer, simplifies the process, improves the efficiency, and is easy to popularize and apply.

Description

Technical Field

[0001] The invention relates to the technical field of oil refining and chemical engineering, and in particular to a method and system for hydrogenating and deolefinating reformed oil. Background Art

[0002] Reforming oil is the main product of catalytic reforming process technology. It is a light distillate oil rich in aromatics. With the rapid development and expansion of my country's aromatics industry, reforming oil provides an important source of raw materials for the extraction of aromatics to obtain chemical raw materials such as benzene, toluene, and xylene. However, due to the harsh reaction conditions of catalytic reforming, the reforming oil contains a certain amount of olefins, which will affect the subsequent aromatics extraction process. Therefore, the reforming oil needs to be deolefinated before it can enter the subsequent extraction step.

[0003] In the early days, my country mainly used clay refining to remove olefins from reforming oil. However, the used clay is a hazardous waste chemical, and the subsequent treatment cost is high and will cause pollution to the environment. Therefore, in recent years, clay refining technology has been replaced by selective hydrogenation and deolefination technology, such as the FHDO reforming oil selective liquid phase hydrogenation and deolefination technology developed by FRIPP. Using HDO-18 precious metal catalyst, it can achieve the removal of olefins under mild conditions and retain the aromatics. The technical process is that the reforming oil after catalytic reforming passes through the dechlorination tank and the re-contact tower, enters the liquid phase hydrogenation reactor, and then enters the depentanizer for separation. The depentanizer oil at the bottom of the tower enters the subsequent aromatic extraction step.

[0004] However, in the application process of the existing technology, the catalyst activity in the hydrogenation reactor is relatively high at the initial stage of the reaction, and since some large molecular olefins (C6, C7) are difficult to remove, the reaction temperature or reaction pressure needs to be appropriately increased, which leads to the loss of aromatic hydrogenation, especially important chemicals such as benzene, toluene and xylene. The hydrogenation saturation will cause the production enterprises to reduce their profits.

[0005] Patent application CN107304371A discloses a reforming oil hydroprocessing method, in which a connection line is set between the bottom of the depentanizer and the inlet of the hydrogenation reactor, and the depentanizer oil is first introduced at the beginning of the operation, and fresh raw materials are introduced after the initial activation of the catalyst is stabilized to ensure the stability of the product quality in the initial stage of the reaction. However, such a design has the risk of pipeline leakage causing the fresh raw materials to directly enter the depentanizer, and increases the complexity of the process.

[0006] Patent application CN102911721A discloses a reforming oil liquid phase circulation selective hydrogenation deolefination method, in which the liquid phase product after hydrogenation is partially circulated and mixed with fresh raw materials and then enters the liquid phase hydrogenation reactor in stages. However, the product circulation requires the installation of a circulation pump, which increases the investment in device construction, and the invention does not solve the problem of aromatics loss in the initial stage of the reaction. Summary of the invention

[0007] The purpose of the present invention is to overcome the shortcomings of the prior art and provide a method and system for hydrogenating and deolefinating reformed oil. The method can effectively remove olefins in the reformed oil, while well controlling the loss of aromatics, and eliminating the need for a depentanizer, thereby simplifying the process, improving efficiency, and being easy to promote and apply.

[0008] In order to achieve the above object, the first aspect of the present invention provides a method for hydrodeolefination of reformed oil, wherein the method comprises: The reformed oil raw material is subjected to gas phase hydrogenation reaction, gas-liquid separation and liquid phase hydrogenation reaction in sequence; The gas phase hydrogenation reaction comprises: subjecting the reformed oil feedstock to a gas phase hydrogenation reaction 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; The liquid phase hydrogenation reaction comprises: pressurizing the liquid phase components and then performing a liquid phase hydrogenation reaction to obtain a liquid phase deolefination reaction product.

[0009] The second aspect of the present invention provides a reforming oil hydrodeolefination system, wherein the system comprises a gas phase hydrogenation reactor, a gas-liquid separation unit, a pressurizing unit and a liquid phase hydrogenation reactor which are connected in sequence; the liquid phase component outlet of the gas-liquid separation unit is connected to the inlet of the pressurizing unit; The gas phase hydrogenation reactor is used to carry out a gas phase hydrogenation reaction on the reformed oil feedstock and hydrogen to obtain a gas phase reaction product; The pressurizing unit is used to pressurize the liquid phase component obtained by the gas-liquid separation unit to obtain a pressurized logistics; The liquid phase hydrogenation reactor is used to carry out liquid phase hydrogenation reaction on the pressurized logistics to obtain a liquid phase deolefination reaction product.

[0010] Compared with the prior art, the method of the present invention has the following advantages: The method provided by the present invention can remove C6 and C7 olefins which are the most difficult to remove in reformed oil, and the aromatic hydrocarbon loss rate is low.

[0011] The method provided by the present invention uses a gas phase hydrogenation reaction to fully saturate C6 and lower olefins (accounting for about 70% of the total olefin content), and then retains the gas phase components through gas-liquid separation, so that benzene enters the gas phase without further hydrogenation saturation. The liquid phase components (C7 olefins and toluene, ethylbenzene, xylene, etc.) undergo a selective hydrogenation deolefination reaction, further reducing the loss of aromatics.

[0012] In the method provided by the present invention, preferably, the gas phase hydrogenation reaction is carried out under low pressure and high hydrogen-to-oil ratio conditions, which can promote olefin hydrogenation reaction and retain benzene to the maximum extent. After the gas phase hydrogenation reaction, hydrogen consumption is relatively high, and the hydrogen-dissolved liquid phase component is pressurized to carry out hydrogenation reaction of the heavy component. At this time, since the liquid phase component is in a slightly "hydrogen-poor" state, that is, a small amount of dissolved hydrogen is only used to meet the hydrogenation of C7 olefins, thereby avoiding the hydrogenation loss of toluene, ethylbenzene and xylene.

[0013] The system provided by the present invention does not need to use 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. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 It is a schematic diagram of the process flow of the present invention.

[0015] Reference numerals DETAILED DESCRIPTION The endpoints and any values ​​of the ranges disclosed in this article 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 each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0016] The description of the exemplary embodiments is intended to be read in conjunction with the accompanying drawings, which are considered a part of the entire written description. In the specification, relative terms such as "lower", "upper", "horizontal", "vertical", "above", "below", "upward", "downward", "top" and "bottom" and their derivatives (for example, "horizontally", "downwardly", "upwardly", etc.) should be interpreted as the directions shown in the drawings being described at the time. These relative terms are for convenience of description and do not require that the device be constructed or operated in a particular orientation. Unless otherwise specified, "connected" as used herein refers to a relationship whereby structures are directly or indirectly fixed or connected to each other through intermediate structures.

[0017] In the present invention, the symbol “≯” means not greater than.

[0018] The first aspect of the present invention provides a method for hydrodeolefination of reforming oil, wherein the method comprises: The reformed oil raw material is subjected to gas phase hydrogenation reaction, gas-liquid separation and liquid phase hydrogenation reaction in sequence; The gas phase hydrogenation reaction comprises: in the presence of hydrogen, subjecting the reformed oil feedstock to a gas phase hydrogenation reaction 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; The liquid phase hydrogenation reaction comprises: pressurizing the liquid phase components and then performing a liquid phase hydrogenation reaction to obtain a liquid phase deolefination reaction product.

[0019] In the present invention, the hydrogen in the gas phase hydrogenation reaction can be any hydrogen-containing gas that can provide hydrogen, which can be fresh hydrogen, recycled hydrogen, or hydrogen-rich gas. Those skilled in the art can clearly understand the hydrogen-containing gas described in the present invention after understanding the technical solution of the present invention.

[0020] In the present invention, the reforming oil raw material can be any reforming oil that needs to be processed conventionally in the art, and the present invention has no particular limitation on the properties of the reforming oil raw material. Preferably, the reforming oil has a distillation range of 40-180°C, a bromine index of ≯8000mg Br / 100g, and an aromatics content of 60-85wt%.

[0021] In the present invention, preferably, the method further comprises dechlorinating and / or re-contacting the reformed oil, and then performing a gas phase hydrogenation reaction. In the present invention, the specific operation mode and conditions of dechlorination and / or re-contacting are not particularly limited, and those skilled in the art can select according to actual needs.

[0022] In the present invention, the gas phase hydrogenation reaction conditions can be selected in a wide range. 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 space velocity of 0.5-10 h -1 ; Further preferably, the conditions of the gas phase hydrogenation reaction include: pressure of 0.3-1MPa, temperature of 150-200°C, hydrogen-to-oil volume ratio of 5-30, for example, 5, 10, 15, 20, 25, 30 and values ​​between any two groups, volume space velocity of 4-8h -1 Under lower reaction pressure and higher hydrogen-oil conditions, olefins can be removed to the greatest extent and aromatic components can be retained during the gas phase hydrogenation reaction.

[0023] In the present invention, preferably, the method further comprises subjecting the gas phase reaction product to heat exchange and cooling before performing the gas-liquid separation.

[0024] The present invention has no particular limitation on the specific operation of the heat exchange, and any heat exchange medium commonly used in the art can be used for the heat exchange. The heat exchange can be performed in a heat exchange unit such as a heat exchanger, and the present invention has no particular limitation on the specific type of the heat exchanger, for example, it can be a commercial heat exchanger commonly defined in the art, or a tubular heat exchanger.

[0025] The present invention uses a small amount of heat exchange under high temperature conditions for the gas phase reaction product, retains a large amount of reaction heat under the condition of ensuring that the macromolecules are liquefied, and meets the feeding conditions of the liquid phase hydrogenation reactor, saving energy consumption. In addition, since only C7 olefins and components such as toluene, ethylbenzene, and xylene enter the liquid phase reaction, the saturation loss of aromatics can be further avoided by controlling the amount of hydrogen dissolved in the liquid phase components, reaction conditions, and catalyst selectivity. The present invention has no particular limitation on the heat exchange conditions, and it is preferred that the liquefaction of macromolecular heavy substances in the gas phase reaction product can be ensured.

[0026] In the present invention, the gas-liquid balance of the effluent after the heat exchanger is achieved, so that the gas phase components flow out upward and the liquid phase components flow out downward. The present invention has a wide range of conditions for the gas-liquid separation, and those skilled in the art can make appropriate selections based on the composition of the reformed oil feedstock, so as to satisfy the requirement that the components that need further hydrofining remain in the liquid phase components. Preferably, based on the total amount of the gas phase reaction product, the mass percentage of the liquid phase component is 20-80%, more preferably 40-75%, and even more preferably 60-75%. The use of this preferred embodiment is more conducive to accurately controlling the separation cut point of the aromatic component and retaining the aromatic content.

[0027] In the present invention, the liquid phase hydrogenation reaction conditions can be selected in a wide range. Preferably, the liquid phase hydrogenation reaction conditions include: a pressure of 1-3 MPa, a temperature of 50-200°C, a volume space velocity of 0.5-10 h -1 Further preferably, the conditions of the liquid phase hydrogenation reaction include: pressure of 1.5-2MPa, temperature of 80-150°C, volume space velocity of 6-9h -1 .

[0028] In the present 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, preferably 0.5-2 MPa higher. In the present invention, by controlling the pressure of the liquid phase hydrogenation reaction and the gas phase hydrogenation reaction, the selectivity of the hydrogenation reaction of olefins and aromatics in the light and heavy components can be improved, and aromatics can be retained under the condition of removing olefins as much as possible.

[0029] In the present invention, preferably, the temperature of the liquid phase hydrogenation reaction is at least 10° C. lower than that of the gas phase hydrogenation reaction, preferably 30-50° C. lower. The advantage of adopting this preferred embodiment is to accurately control the separation cut point of the aromatic components and retain the aromatic content.

[0030] In the present 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 independently carried out in a fixed bed reactor.

[0031] In the present invention, preferably, the gas phase hydrogenation reaction and the liquid phase hydrogenation reaction are each independently carried out in the presence of a hydrodeolefination catalyst, and the hydrodeolefination catalyst is a precious metal catalyst.

[0032] In the present invention, preferably, the noble metal catalyst comprises a carrier and a noble metal component supported on the carrier.

[0033] In the present invention, there is no particular limitation on the type of carrier, and for example, the carrier may be a carrier conventionally defined in the art, such as alumina.

[0034] In the present invention, there is no particular limitation on the type of the noble metal in the noble metal catalyst, and it can be any noble metal conventionally defined in the art. Preferably, the noble metal component is Pt and / or Pd.

[0035] In the present invention, the source of the hydrodeolefination catalyst is not particularly limited, and it can be prepared by any method or purchased commercially, for example, HDO-18 developed by Fushun Research Institute of Petrochemicals (FRIPP) of Sinopec.

[0036] In the present invention, there is no particular limitation on the application of the gas phase component (also referred to as hydrogenation light component) and the liquid phase deolefination reaction product obtained by gas-liquid separation, and they can be adaptively treated according to the specific needs of the product. Preferably, the method further comprises mixing the gas phase component and the liquid phase deolefination reaction product to obtain a reforming product oil product. In the present invention, preferably, the bromine index of the reforming product oil product is ≯100mg Br / 100g, and the aromatic loss rate is less than 0.1%.

[0037] In the present invention, the specific operation and conditions for pressurizing the liquid phase component are relatively wide. The pressurization is used to pressurize the liquid phase component, preferably to a pressure that can meet the reaction conditions in the liquid phase hydrogenation reactor. In the present invention, there is no particular limitation on the specific operation mode of pressurization, and the specific process can be that the liquid phase component is pressurized to a pressure slightly higher than the pressure required for the liquid phase reaction through a pressurization unit (preferably a booster pump).

[0038] The second aspect of the present invention provides a reforming oil hydrodeolefination system, wherein the system comprises a gas phase hydrogenation reactor, a gas-liquid separation unit, a pressurizing unit and a liquid phase hydrogenation reactor which are connected in sequence; the liquid phase component outlet of the gas-liquid separation unit is connected to the inlet of the pressurizing unit; The gas phase hydrogenation reactor is used to carry out a gas phase hydrogenation reaction on the reformed oil feedstock and hydrogen to obtain a gas phase reaction product; The pressurizing unit is used to pressurize the liquid phase component obtained by the gas-liquid separation unit to obtain a pressurized logistics; The liquid phase hydrogenation reactor is used to carry out liquid phase hydrogenation reaction on the pressurized logistics to obtain a liquid phase deolefination reaction product.

[0039] In the present invention, preferably, the gas phase hydrogenation reactor and the liquid phase hydrogenation reactor are each independently loaded with a hydrodeolefination catalyst. The corresponding catalysts are matched in different reactors, and the amount of the catalyst is controlled to achieve the hydrodeolefination reaction.

[0040] In the present invention, the types of gas phase hydrogenation reactor and liquid phase hydrogenation reactor have been described in the first aspect and will not be described in detail here.

[0041] In the present 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.

[0042] In the present invention, preferably, a liquid-phase deolefination reaction product outlet is provided at the bottom of the liquid-phase hydrogenation reactor.

[0043] In the present invention, preferably, the system further comprises a heat exchange unit disposed between the gas phase hydrogenation reactor and the gas-liquid separation unit, the heat exchange unit being used to perform heat exchange on the gas phase reaction product and then perform gas-liquid separation. In the present invention, the heat exchange unit is not particularly limited and can be a conventional choice in the art, such as a heat exchanger.

[0044] In the present invention, there is no particular limitation on the gas-liquid separation unit, and it can be a conventional choice in the art, for example, it can be a gas-liquid separator.

[0045] In the present invention, preferably, the pressurizing unit is used to pressurize the liquid phase component, preferably to a level that satisfies the reaction conditions in the liquid phase hydrogenation reactor. The type of the pressurizing unit has been described in the first aspect of the present invention and will not be described in detail here.

[0046] The present invention will be described in detail below through examples.

[0047] In the present invention, unless otherwise explicitly stated, percentages and contents are all based on mass.

[0048] 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; the reformed oil feedstock and hydrogen 1 enter the heat exchange unit 4 (heat exchanger), where the heat exchange unit 4 cools the reformed oil feedstock and enters 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 upward from the gas-liquid separator, and the liquid phase component 6 is discharged downward from the gas-liquid separator; the reformed oil feedstock and hydrogen 1 then pass through the booster unit 8 (boosting pump) and enter the liquid phase hydrogenation reactor 9 for a liquid phase hydrogenation reaction to obtain a liquid phase deolefination reaction product 10; the gas phase component 7 is mixed with the liquid phase deolefination reaction product 10 to finally obtain a reformed oil product 11.

[0049] Examples 1-3 Use Figure 1 Schematic diagram of the process. Two 100mL fixed-bed hydrogenation reactors are connected in series, namely a gas phase hydrogenation reactor and a liquid phase hydrogenation reactor. A heat exchanger, a gas-liquid separator and a booster pump are set between the reactors. The gas phase hydrogenation reactor is filled with 60mL Pt-Pd type hydrogenation catalyst A, and the liquid phase hydrogenation reactor is filled with 40mL Pt-Pd type hydrogenation catalyst A. A gas phase component outlet is set above the gas-liquid separator, which is connected to the bottom effluent of the liquid phase hydrogenation reactor to obtain the reforming oil product together.

[0050] Reforming oil was used as the raw material. The properties of the catalyst are shown in Table 1, the properties of the raw oil are shown in Table 2, and the reaction process conditions and results are shown in Table 3.

[0051] Example 4 The process flow is the same as that of Example 1-3, except that the liquid phase reaction pressure is increased. The reaction process conditions and results are shown in Table 3.

[0052] Example 5 The process flow is the same as that of Example 1-3, except that the liquid phase reaction temperature is increased. The reaction process conditions and results are shown in Table 3.

[0053] Example 6 The same process flow as in Example 1-3 is different only in that the hydrogen-to-oil volume ratio at the inlet of the gas phase hydrogenation reactor is reduced, and the booster system (boost pump) before the liquid phase hydrogenation reactor is changed to a booster and hydrogen mixing system. The gas phase hydrogenation reactor is loaded with 60 mL Pt-Pd type hydrogenation catalyst A, and the liquid phase hydrogenation reactor is loaded with 40 mL Pt-Pd type hydrogenation catalyst A. The reaction process conditions and results are shown in Table 3.

[0054] Comparative Example 1 A conventional fixed bed hydrogenation process was used, with only one hydrogenation reactor. The gas phase hydrogenation reactor was loaded with 100 mL of Pt-Pd type hydrogenation catalyst A. After hydrogen sulfide was removed, the hydrogen was pressurized and recycled by a circulating hydrogen compressor. The properties of the raw materials and catalyst were the same as those of Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0055] Comparative Example 2 A conventional liquid phase hydrogenation process was adopted, and only one liquid phase hydrogenation reactor was provided. The liquid phase hydrogenation reactor was loaded with 100 mL Pt-Pd type hydrogenation catalyst A. Hydrogen was mixed with the raw oil through the hydrogen mixer and then entered the reactor. The raw materials and catalyst properties were the same as those in Examples 1-3, and the reaction process conditions and results are shown in Table 3.

[0056] Table 1 Table 2 Table 3 Note: In Table 3, the amount of hydrogen replenished refers to the amount relative to 1m 3 The amount of hydrogen required for the liquid phase component.

[0057] As can be seen from Table 3, Comparative Example 1 uses conventional fixed bed hydrogenation technology, and the hydrogen cycle requires the installation of a circulating hydrogen compressor, which is costly and causes large aromatic losses. Comparative Example 2 uses liquid phase hydrogenation technology, and since hydrogen needs to be dissolved once to meet the hydrogen consumption required for the reaction, the pressure is relatively high, resulting in increased aromatic losses.

[0058] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to 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 raw material is subjected to gas phase hydrogenation reaction, gas-liquid separation and liquid phase hydrogenation reaction in sequence; The gas phase hydrogenation reaction comprises: in the presence of hydrogen, subjecting the reformed oil feedstock to a gas phase hydrogenation reaction 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; The liquid phase hydrogenation reaction comprises: pressurizing the liquid phase components and then performing a liquid phase hydrogenation reaction to obtain a liquid phase deolefination reaction product.

2. The method according to claim 1, wherein: The reformed oil has a distillation range of 40-180°C, a bromine index of ≯8000mg Br / 100g, and an aromatic content of 60-85wt%; Preferably, the conditions of the gas phase hydrogenation reaction include: pressure of 0.1-1.5 MPa, temperature of 80-200°C, hydrogen-to-oil volume ratio of 3-50, volume space velocity of 0.5-10 h -1 ; Further preferably, the conditions of the gas phase hydrogenation reaction include: pressure of 0.3-1 MPa, temperature of 150-200°C, hydrogen-oil volume ratio of 5-30, volume space velocity of 4-8 h -1 .

3. The method according to claim 1 or 2, wherein: The method further comprises, before performing the gas-liquid separation, subjecting the gas phase reaction product to heat exchange and cooling; Preferably, based on the total amount of the gas phase reaction product, the mass percentage of the liquid phase component is 20-80%, and more preferably 40-75%.

4. The method according to any one of claims 1 to 3, wherein: The conditions of the liquid phase hydrogenation reaction include: pressure of 1-3 MPa, temperature of 50-200°C, volume space velocity of 0.5-10 h -1 ; Preferably, the conditions of the liquid phase hydrogenation reaction include: pressure of 1.5-2 MPa, temperature of 80-150°C, volume space velocity of 6-9 h -1 .

5. The method according to any one of claims 1 to 4, wherein: The pressure of the liquid phase hydrogenation reaction is at least 0.5 MPa higher than the pressure of the gas phase hydrogenation reaction, preferably 0.5-2 MPa higher; Preferably, the temperature of the liquid phase hydrogenation reaction is at least 10°C lower than the temperature of the gas phase hydrogenation reaction, preferably 30-50°C lower.

6. The method according to any one of claims 1 to 5, wherein: The gas phase hydrogenation reaction and the liquid phase hydrogenation reaction are each independently carried out in a fixed bed reactor; Preferably, the gas phase hydrogenation reaction and the liquid phase hydrogenation reaction are each independently carried out in the presence of a hydrodeolefination catalyst, and the hydrodeolefination catalyst is a precious metal catalyst; Preferably, the noble metal catalyst comprises a carrier and a noble metal component supported on the carrier; Preferably, the noble metal component is Pt and / or Pd.

7. The method according to any one of claims 1 to 6, wherein: The method further comprises mixing the gas phase component with the liquid phase deolefination reaction product to obtain a reformed oil product; Preferably, the bromine index of the reformed oil product is ≯100 mg Br / 100 g, and the aromatics loss rate is less than 0.1%.

8. A system for hydrodeolefination of reformed oil, wherein: The system comprises a gas phase hydrogenation reactor, a gas-liquid separation unit, a pressurizing unit and a liquid phase hydrogenation reactor which are connected in sequence; the liquid phase component outlet of the gas-liquid separation unit is connected to the inlet of the pressurizing unit; The gas phase hydrogenation reactor is used to carry out a gas phase hydrogenation reaction on the reformed oil feedstock and hydrogen to obtain a gas phase reaction product; The pressurizing unit is used to pressurize the liquid phase component obtained by the gas-liquid separation unit to obtain a pressurized logistics; The liquid phase hydrogenation reactor is used to carry out liquid phase hydrogenation reaction on the pressurized logistics to obtain a liquid phase deolefination reaction product.

9. The system according to claim 8, wherein: The gas phase hydrogenation reactor and the liquid phase hydrogenation reactor are each independently filled with a hydrogenation deolefination catalyst.

10. The system according to claim 8 or 9, wherein: The gas phase hydrogenation reactor and the liquid phase hydrogenation reactor are each independently a fixed bed reactor.

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