A hydrogenation process for producing solvent oil
By combining reforming residue oil and alkane-containing feedstock for processing and catalyst matching, the problem of only being able to produce a single solvent oil in existing technologies has been solved, realizing the co-production and stable operation of multiple high-quality solvent oils and improving economic efficiency.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- CHINA PETROLEUM & CHEMICAL CORP
- Filing Date
- 2024-12-06
- Publication Date
- 2026-06-09
AI Technical Summary
Existing processes can only produce a single type of solvent oil, and cannot produce multiple high-quality solvent oils in combination. They also suffer from short operating cycles and poor economic efficiency.
By combining reformate residue oil and alkane-containing feedstock, and through specific processing pathways and catalyst matching, including hydrorefining and dearomatization reactions, multiple solvent oils can be co-produced. The reaction conditions are optimized through pre-fractionation and hydrogenation treatment.
It has achieved the co-production of multiple high-quality solvent oils, with product performance indicators exceeding the standards. The unit operates stably, solving the problem of producing a single product from a single raw material and improving the unit's operating cycle and economy.
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Figure CN122168332A_ABST
Abstract
Description
Technical Field
[0001] This invention belongs to the field of petrochemical technology, and relates to solvent oil production processes, particularly a method for producing solvent oil by hydrogenation. Background Technology
[0002] Solvent oils are important industrial solvents, widely used in coatings, edible oil extraction, printing inks, leather, pesticides, insecticides, rubber, cosmetics, fragrances, pharmaceuticals, electronics and other industries.
[0003] Solvent oils can be classified according to their uses into pentane foaming agents, food-grade petroleum ethers, vegetable oil extraction solvents, food additive hexane, industrial hexane, rubber industry solvents, paint industry solvents and thinners, aluminum foil oil, odorless kerosene, insecticide aerosol oil, D-series dearomatized solvent oils (light white oil), ink solvent oils, washing solvent oils, and n / isoalkane solvent oils, etc. Among them, vegetable oil extraction solvents, food additive hexane, light white oils, and n / isoalkane solvent oils have strict requirements for aromatic (benzene) content and bromine index, and often require deep hydrogenation refining processes for preparation, resulting in long process routes and high production costs.
[0004] Patent CN116410790A discloses a method for producing solvent oil from reforming residue oil. The method includes sequentially feeding the reforming residue oil into a first distillation column, an adsorption reactor, and a fixed-bed hydrotreating reactor for distillation, adsorption desulfurization and dehydration, and hydrotreating for benzene and olefin removal, respectively. The reaction products are separated by a separator to obtain gaseous and liquid products. The resulting liquid product is sequentially fed into a second distillation column for distillation and a third distillation column for fractionation. The resulting product is fed into a normalization reactor and undergoes isohexane normalization under the action of a molecular sieve catalyst. The resulting product is then fed into a fourth distillation column for fractionation to obtain solvent oil. This invention effectively solves the problem of comprehensive utilization of reforming residue oil, achieving efficient utilization of various carbon groups from a molecular refining perspective, increasing the hexane yield, and allowing the obtained C5 component to be used as a pentane foaming agent and the C7 component to be used as 120# solvent oil, thus achieving the goal of producing high-value-added products from reforming residue oil.
[0005] Patent CN101921621A discloses a method for producing isomeric alkane solvent oils. Using distillate oils or light de-oiled oils as raw materials, a combined process of hydrotreating, hydroisomerization, and supplementary hydrorefining is employed to produce isomeric alkane solvent oils. This method can use common feedstocks to obtain high-quality isomeric alkane solvent oil products of various distillate fractions, and features strong feedstock adaptability, good product quality, and flexible production.
[0006] Patent CN107312569A discloses a method for producing isoparaffin solvent oil from Fischer-Tropsch naphtha, comprising: (1) subjecting Fischer-Tropsch naphtha to an alcohol dehydration reaction in the presence of a catalyst to prepare olefins; (2) subjecting the product obtained in step (1) to a polymerization reaction in the presence of a polymerization catalyst; (3) subjecting the product obtained in step (2) to a hydrogenation reaction in the presence of a hydrogenation catalyst; and (4) fractionating the product of step (3) to a fraction with an initial boiling point of not less than 160°C and a final boiling point of not more than 340°C to obtain isoparaffin solvent oil. The method for producing isoparaffin solvent oil from Fischer-Tropsch naphtha of this invention yields isoparaffin solvent oil with high yield and purity. Furthermore, the isoparaffin solvent oil product obtained by this method has a light color, good oxidation stability and thermal stability, and the content of aromatics, sulfur, and nitrogen compounds is negligible. Summary of the Invention
[0007] The core objective of this invention is to provide a hydrogenation process for producing solvent oils. Based on the comprehensive selection of raw materials, processing paths, and the matching use of catalysts, it enables the co-production of different types of high-quality solvent oils, such as n-alkanes / isoalkanes, pentane foaming agents, food additive n-hexane / industrial n-hexane, vegetable oil extraction solvents, and food-grade petroleum ethers. The resulting products exhibit performance indicators far exceeding the corresponding product standards. Furthermore, the entire production process can operate stably for extended periods. This solves the problems of existing processes that can only produce a single type of solvent oil product from a single raw material, cannot co-produce multiple solvent oil products, and suffer from fluctuations in benzene content in n-hexane / vegetable oil extraction solvents, poor stability of n-alkanes / isoalkanes, short operating cycles, and poor economic efficiency.
[0008] This invention provides a hydrogenation process for producing solvent oil, comprising the following steps:
[0009] (1) The reformate residue feedstock is cut to obtain light components and heavy components;
[0010] (2) In the presence of hydrogen, the alkane-containing feedstock enters the hydrorefining reaction zone through the first feed port, and the heavy components obtained in step (1) enter the hydrorefining reaction zone through the second feed port. After the reaction is completed, hydrorefined product oil is obtained.
[0011] (3) The hydrorefined product oil obtained in step (2) is stripped to obtain a gas phase stream and a liquid phase stream;
[0012] (4) The light component obtained in step (1) and hydrogen are dissolved in a hydrogen mixer and then the liquid phase stream obtained in step (3) enters the dearomatization reaction zone for hydrogenation dearomatization reaction. The oil produced by the reaction is separated to obtain a series of solvent oil products.
[0013] Furthermore, as some specific implementation methods, the cutting temperature of the light component and the heavy component in step (1) is 70°C to 120°C, preferably 90°C to 100°C.
[0014] Furthermore, as some specific implementation methods, the reformate residue oil in step (1) is the distillate oil remaining after the aromatics are extracted from the catalytic reforming product rich in aromatics. The reformate residue oil includes C6-C8 alkanes, cycloalkanes, and small amounts of aromatics (benzene) and sulfides, wherein the aromatic content is 0.05wt% to 2.0wt% and the sulfur content is 0.5ppm to 3ppm.
[0015] Furthermore, as some specific implementation methods, the alkane-containing raw material in step (2) can be at least one of the following: alkane-containing byproducts in the production of isononanol using the "olefin oligomerization-hydroformylation" process; alkane-containing byproducts in the production of isononanoic acid using the "olefin oligomerization-hydroformylation" process; and alkane-containing byproducts in the production of isononal using the "olefin oligomerization-hydroformylation" process.
[0016] Furthermore, as some specific implementation methods, the alkanes containing 12-20 carbon atoms in the alkane-containing raw material in step (2) have a content of 90wt% to 99wt%.
[0017] Furthermore, as some specific implementation methods, the hydrorefining reaction zone is provided with a first inlet and a second inlet. The liquid phase material flows sequentially through the first and second inlets within the hydrorefining reaction zone reactor, respectively. The first inlet is located at the top or bottom of the reactor, and the second inlet is located on the reactor shell. The area between the first and second inlets is the first reaction zone, and the remaining area is the second reaction zone. The volume of the first reaction zone accounts for 1% to 50% of the total reactor volume, preferably 10% to 30%. More specifically, when the hydrorefining reaction zone uses bottom feeding, the first inlet is located at the top of the reactor, and the second inlet is located in the upper middle part of the reactor shell. When the hydrorefining reaction zone uses top feeding, the first inlet is located at the bottom of the reactor, and the second inlet is located in the lower middle part of the reactor shell.
[0018] Furthermore, as some specific implementation methods, the process conditions of the hydrorefining reaction zone in step (2) are: hydrogen partial pressure of 0.1 MPa to 6.0 MPa, preferably 1.0 MPa to 3.0 MPa, and volume hourly space velocity of 0.01 h⁻¹. -1 ~4.0h -1 Preferably 0.5h -1 ~2.5h -1The hydrogen-to-oil volume ratio is 100:1 to 1000:1, preferably 200:1 to 600:1; the reaction temperature of the first reaction zone is 60℃ to 130℃, preferably 80℃ to 110℃; the reaction temperature of the second reaction zone is 140℃ to 280℃, preferably 180℃ to 240℃.
[0019] Furthermore, as some specific embodiments, the hydrorefining reaction zone includes at least one hydrorefining reactor, which is filled with a hydrorefining catalyst. The hydrorefining catalyst can be a commercially available product or prepared as needed according to common knowledge in the art.
[0020] Furthermore, as some specific implementation methods, the first reaction zone is filled with a precious metal hydrorefining catalyst, wherein the precious metal is one or more of Pt and Pd; the precious metal content is 0.2-0.7 wt% based on the catalyst weight. Specifically, the precious metal hydrorefining catalyst can be one or more combinations of the FHDA series of precious metal hydrorefining catalysts developed by Sinopec (Dalian) Petrochemical Research Institute Co., Ltd. (FRIPP), specifically at least one of FHDA-10 hydrorefining catalyst and FHDA-1 hydrorefining catalyst.
[0021] Furthermore, as some specific embodiments, the second reaction zone is filled with a precious metal hydrorefining catalyst, wherein the precious metal is one or more of Pt and Pd; the precious metal content is 0.2-0.7 wt% based on the catalyst weight. Specifically, the precious metal hydrorefining catalyst can be any one or more combinations of the FMTA series of precious metal hydrorefining catalysts developed by Sinopec (Dalian) Petrochemical Research Institute Co., Ltd. (FRIPP), specifically at least one of FMTA-20 hydrorefining catalyst and FAMTA-2 hydrorefining catalyst.
[0022] Furthermore, as some specific embodiments, the precious metal content in the precious metal hydrorefining catalyst packed in the second reaction zone is 0.01wt% to 0.18wt% lower than the precious metal content in the precious metal hydrorefining catalyst packed in the first reaction zone.
[0023] Furthermore, as some specific implementation methods, the heavy components obtained in step (1) are generally heated to 160°C to 300°C, preferably to 200°C to 260°C, and then fed into the hydrorefining reaction zone through the second feed inlet. Moreover, the heavy components may not undergo adsorption desulfurization treatment.
[0024] Furthermore, as some specific implementation methods, hydrogen can be used as the stripping gas in step (3). The main purpose is to strip out gaseous components such as hydrogen sulfide, dry gas, and liquefied petroleum gas from the hydrorefined oil. The specific operating methods and conditions can be selected according to actual needs. In this invention, the stripping operation conditions are as follows: the stripping tower operating pressure is 0.1 MPa to 6.0 MPa, preferably 1.0 MPa to 3.0 MPa; the stripping tower feed temperature is 30°C to 60°C, preferably 40°C to 50°C.
[0025] Furthermore, as some specific implementation methods, the process conditions of the dearomatization reaction zone in step (4) are as follows: reaction temperature is 40℃~150℃, preferably 70℃~120℃, hydrogen partial pressure is 0.1MPa~6.0MPa, preferably 1.0MPa~3.0MPa, and volume hourly space velocity is 0.01h. -1 ~3.0h -1 Preferably 0.4h -1 ~2.0h -1 The hydrogen-to-oil volume ratio is 10:1 to 300:1, preferably 40:1 to 100:1.
[0026] Furthermore, as some specific implementation methods, the dearomatization reaction zone in step (4) can be a trickle bed hydrogenation or a liquid phase hydrogenation, preferably a liquid phase hydrogenation.
[0027] Furthermore, as some specific implementation methods, the dearomatization reaction zone in step (4) is filled with a hydrorefining catalyst, which is a nickel-based hydrorefining catalyst, that is, a hydrorefining catalyst with nickel as the active metal for hydrogenation. The hydrorefining catalyst can be prepared according to methods disclosed in the art, or a commercially available product can be selected. Furthermore, the hydrorefining catalyst can be selected from one or more combinations of the FHJ series nickel-based hydrorefining catalysts developed by Sinopec (Dalian) Petrochemical Research Institute (FRIPP), specifically at least one of FHJ-1 hydrorefining catalyst, FHJ-2 hydrorefining catalyst, and FHJ-3 hydrorefining catalyst.
[0028] Furthermore, as some specific implementation methods, the operating conditions for dissolving the light component obtained in step (1) in step (4) with hydrogen in a hydrogen mixer are generally a pressure of 0.1 MPa to 6.0 MPa, preferably 1.0 MPa to 3.0 MPa; and a hydrogen-to-oil volume ratio of 10:1 to 300:1, preferably 40:1 to 100:1.
[0029] Furthermore, as some specific implementation methods, the series of solvent oil products in step (4) include light solvent oil products and heavy solvent oil products. The light solvent oil products can be at least one of pentane foaming agent, industrial isohexane, industrial hexane, food additive n-hexane, food additive vegetable oil extraction solvent, and food-grade petroleum ether. The heavy solvent oil products can be at least one of n-alkane solvent oil products and isoalkane solvent oil products.
[0030] Compared with existing processes, the technical advantages of the hydrogenation process for producing solvent oil provided by this invention include one or more of the following aspects:
[0031] 1. The hydrogenation process for producing solvent oil provided by this invention combines reforming residue oil and alkane-containing feedstocks for processing. By controlling the processing path and matching catalysts, it solves the problems of strong exothermic coking of alkane-containing feedstocks and the short service life of highly active nickel-based catalysts due to sulfur poisoning. It enables the co-production of different types of high-quality solvent oils, such as n-alkanes / isoalkanes, pentane foaming agents, food additive n-hexane / industrial n-hexane, vegetable oil extraction solvents, and food-grade petroleum ethers. The performance indicators of the obtained products are far superior to the corresponding product standard indicators. Moreover, the entire production process can operate stably for a long period of time. It solves the problems of existing processes that can only produce a single type of solvent oil product from a single feedstock, cannot co-produce multiple solvent oil products, and have fluctuating benzene content in n-hexane / vegetable oil extraction solvents, poor stability of n- / isoalkanes, short operating cycles, and poor economic efficiency.
[0032] 2. In the hydrogenation process for producing solvent oil provided by this invention, the heavy components of reforming raffinate are introduced into the second reaction zone of the hydrorefining reaction zone through a second feed inlet. This effectively controls the strongly exothermic reaction of the olefin hydrogenation saturation process in the first reaction zone for high-olefin-content alkane-containing feedstocks. Furthermore, the relatively high reaction temperature in the second reaction zone allows for the hydrorefining of the heavy components of the reforming raffinate. Suitable processing paths and conditions are selected for both feedstocks, significantly improving the unit's operating cycle and reducing energy consumption. Simultaneously, the light components of the reforming raffinate are dissolved in hydrogen and then mixed with the hydrorefined product before being introduced into the dearomatization reaction zone. This effectively increases the hydrogen concentration in the dearomatization reaction zone, improves the deep dearomatization effect, and addresses the issues of benzene content fluctuations and poor product stability in the series of solvent oil products. Attached Figure Description
[0033] Figure 1 This is a schematic diagram of the hydrogenation process for producing solvent oil according to the present invention. Detailed Implementation
[0034] The present invention will now be described in further detail with reference to the accompanying drawings and specific embodiments. The following embodiments will further illustrate the method provided by the present invention, but do not limit the scope of the invention.
[0035] 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.
[0036] 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.
[0037] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.
[0038] In this document, all numeric values of parameters (e.g., quantity or condition) should be understood to be modified by the term “about” in all cases, regardless of whether “about” actually appears before the numeric value.
[0039] like Figure 1As shown, the specific process of the hydrogenation process for producing solvent oil provided by the present invention is as follows: Reformate raffinate 1 is fractionated in a pre-fractionation tower to obtain light component 2 and heavy component 3; alkane-containing feedstock 4 is mixed with fresh hydrogen 5 and, after heat exchange, enters the hydrorefining reaction zone through the first feed inlet, where it contacts the hydrorefining catalyst packed therein for a hydrogenation reaction; the heavy component 3 obtained after fractionation and cutting of the reformate raffinate is heated in a furnace and then enters the hydrorefining reaction zone through the second feed inlet, where it mixes with the effluent from the first reaction zone of the hydrorefining reaction zone and enters the second reaction zone of the hydrorefining reaction zone, where it reacts with the catalyst packed therein. The hydrogenation reaction is carried out in contact with the hydrorefining catalyst. The hydrorefined product oil 6 obtained after the reaction is heat-exchanged by heat exchanger 7 and then enters the stripping tower for separation to obtain gas stream 8 and liquid stream 11. The light component 2 obtained after fractionation and cutting of reforming residue oil is mixed with fresh hydrogen 5 in hydrogen mixer 9 to obtain stream 10 and liquid stream 11, which are then mixed and enter the dearomatization reaction zone to contact the hydrorefining catalyst for hydrogenation reaction. The reaction product oil 12 enters the fractionation tower to separate industrial hexane, food additive vegetable oil extraction solvent, food-grade petroleum ether, and n / isoalkanes solvent oil, etc.
[0040] In this paper, the feedstock oil used is C12 alkane and reformate residue oil, which are byproducts of the production of isononol. The specific properties are shown in Table 1.
[0041] Table 1 Properties of Crude Oil
[0042]
[0043]
[0044] In this study, the first reaction zone uses FHDA-1 hydrorefining catalyst, the second reaction zone uses FMTA-20 hydrorefining catalyst, and the dearomatization reaction zone uses FHJ-3 catalyst. The first reaction zone accounts for 20% of the total volume of the hydrorefining reaction zone.
[0045] In this paper, the process conditions for each embodiment and comparative example are shown in Table 2.
[0046] Table 2 Process conditions for the Examples and Comparative Examples
[0047]
[0048]
[0049] Example 1
[0050] Using C12 alkanes and reformate raffinate from Table 1 as raw materials, with the cutting temperature of the light and heavy components of the reformate raffinate being 95°C, the process was carried out under the conditions in Table 2.
[0051] Example 2
[0052] Using C12 alkanes and reformate raffinate from Table 1 as raw materials, with the cutting temperature of the light and heavy components of the reformate raffinate being 70°C, the process was carried out under the conditions in Table 2.
[0053] Example 3
[0054] Using C12 alkanes and reformate raffinate from Table 1 as raw materials, with the cutting temperature of the light and heavy components of the reformate raffinate being 120°C, the process was carried out under the conditions in Table 2.
[0055] Comparative Example 1
[0056] The process is basically the same as in Example 1, except that a pre-fractionation tower and a hydrogen mixer are not set up. The reforming residue oil is directly mixed with C12 alkanes without fractionation treatment and enters the hydrorefining reaction zone, stripping tower and dearomatization reaction zone through the first feed inlet for processing.
[0057] Comparative Example 2
[0058] The process is basically the same as in Example 1, except that a pre-fractionation tower and a hydrogen mixer are not installed. The reforming raffinate oil is fed into the hydrorefining reaction zone through the second feed inlet without fractionation.
[0059] Comparative Example 3
[0060] It is basically the same as Example 1, except that the light components obtained from the pre-fractionation tower do not enter the dearomatization reaction zone for hydrogenation.
[0061] In this paper, the main product properties obtained from each embodiment and comparative example are shown in Table 4.
[0062] Table 4. Main Product Properties
[0063]
[0064]
Claims
1. A hydrogenation process for producing solvent oil, comprising the following steps: (1) The reformate residue feedstock is cut to obtain light components and heavy components; (2) In the presence of hydrogen, the alkane-containing feedstock enters the hydrorefining reaction zone through the first feed port, and the heavy components obtained in step (1) enter the hydrorefining reaction zone through the second feed port. After the reaction is completed, hydrorefined product oil is obtained. (3) The hydrorefined product oil obtained in step (2) is stripped to obtain a gaseous stream and a liquid stream; (4) The light component obtained in step (1) and hydrogen are dissolved in a hydrogen mixer and then the liquid phase stream obtained in step (3) enters the dearomatization reaction zone for hydrogenation dearomatization reaction. The reaction-generated oil is separated to obtain a series of solvent oil products.
2. The hydrogenation process for producing solvent oil according to claim 1, wherein, The cutting temperature of the light and heavy components in step (1) is 70℃~120℃, preferably 90℃~100℃.
3. The hydrogenation process for producing solvent oil according to claim 1, wherein, The alkane-containing raw material in step (2) is at least one of the following: alkane-containing byproducts in the production of isononanol using the "olefin oligomerization-hydroformylation" process; alkane-containing byproducts in the production of isononanoic acid using the "olefin oligomerization-hydroformylation" process; and alkane-containing byproducts in the production of isononanaldehyde using the "olefin oligomerization-hydroformylation" process.
4. The hydrogenation process for producing solvent oil according to claim 1, wherein, In step (2), the alkanes containing 12-20 carbon atoms in the raw material contain 90wt% to 99wt%.
5. The hydrogenation process for producing solvent oil according to claim 1, wherein, The hydrorefining reaction zone is provided with a first inlet and a second inlet. The liquid phase material flows sequentially through the first inlet and the second inlet of the reactor in the hydrorefining reaction zone. The first inlet is located at the top or bottom of the reactor, and the second inlet is located on the reactor shell. The area between the first inlet and the second inlet is the first reaction zone, and the remainder is the second reaction zone. The volume of the first reaction zone accounts for 1% to 50% of the total volume of the reactor, preferably 10% to 30%.
6. The hydrogenation process for producing solvent oil according to claim 1, wherein, The process conditions in the hydrorefining reaction zone in step (2) are: hydrogen partial pressure of 0.1 MPa to 6.0 MPa, preferably 1.0 MPa to 3.0 MPa, and volume hourly space velocity of 0.01 h⁻¹. -1 ~4.0h -1 Preferably 0.5h -1 ~2.5h -1 The hydrogen-to-oil volume ratio is 100:1 to 1000:1, preferably 200:1 to 600:1; the reaction temperature of the first reaction zone is 60℃ to 130℃, preferably 80℃ to 110℃; the reaction temperature of the second reaction zone is 140℃ to 280℃, preferably 180℃ to 240℃.
7. The hydrogenation process for producing solvent oil according to claim 5, wherein, The first reaction zone is filled with a precious metal hydrogenation refining catalyst, wherein the precious metal is one or more of Pt and Pd; the content of the precious metal is 0.2 to 0.7 wt% based on the weight of the catalyst.
8. The hydrogenation process for producing solvent oil according to claim 5, wherein, The second reaction zone is filled with a precious metal hydrogenation refining catalyst, wherein the precious metal is one or more of Pt and Pd; the content of the precious metal is 0.2 to 0.7 wt% based on the weight of the catalyst.
9. The hydrogenation process for producing solvent oil according to claim 8, wherein, The precious metal content in the second reaction zone, which is filled with a precious metal hydrorefining catalyst, is 0.01 wt% to 0.18 wt% lower than that in the first reaction zone, which is filled with a precious metal hydrorefining catalyst.
10. The hydrogenation process for producing solvent oil according to claim 1, wherein, The heavy components obtained in step (1) are heated to 160°C to 300°C, preferably to 200°C to 260°C, and then fed into the hydrogenation refining reaction zone through the second feed port.
11. The hydrogenation process for producing solvent oil according to claim 1, wherein, In step (3), hydrogen is used as the stripping gas for the stripping process. The operating conditions for the stripping process are as follows: the operating pressure of the stripping tower is 0.1MPa to 6.0MPa, preferably 1.0MPa to 3.0MPa; the feed temperature of the stripping tower is 30℃ to 60℃, preferably 40℃ to 50℃.
12. The hydrogenation process for producing solvent oil according to claim 1, wherein, The process conditions for the dearomatization reaction zone in step (4) are as follows: reaction temperature 40℃~150℃, preferably 70℃~120℃; hydrogen partial pressure 0.1MPa~6.0MPa, preferably 1.0MPa~3.0MPa; and volume hourly space velocity 0.01h. -1 ~3.0h -1 Preferably 0.4h -1 ~2.0h -1 The hydrogen-to-oil volume ratio is 10:1 to 300:1, preferably 40:1 to 100:
1.
13. The hydrogenation process for producing solvent oil according to claim 1, wherein, In step (4), the dearomatization reaction zone is hydrogenated by trickle bed or liquid phase hydrogenation, preferably by liquid phase hydrogenation.
14. The hydrogenation process for producing solvent oil according to claim 1, wherein, The dearomatization reaction zone in step (4) is filled with a hydrogenation refining catalyst, which is a nickel-based hydrogenation refining catalyst.
15. The hydrogenation process for producing solvent oil according to claim 1, wherein, The operating conditions for dissolving the light component obtained in step (1) in step (4) with hydrogen in a hydrogen mixer are: pressure 0.1 MPa to 6.0 MPa, preferably 1.0 MPa to 3.0 MPa; hydrogen-to-oil volume ratio 10:1 to 300:1, preferably 40:1 to 100:
1.
16. The hydrogenation process for producing solvent oil according to claim 1, wherein, The series of solvent oil products in step (4) include light solvent oil products and heavy solvent oil products. The light solvent oil products are at least one of pentane foaming agent, industrial isohexane, industrial hexane, food additive n-hexane, food additive vegetable oil extraction solvent, and food-grade petroleum ether. The heavy solvent oil products are at least one of n-alkane solvent oil products and isoalkane solvent oil products.