Hydrogenation catalyst, its production and application

Abstract

This application relates to a hydrogenation catalyst, a process for its production and its use in a feedstock oil hydrogenation operation. The process comprises at least the following steps: (1) contacting a first active metal moiety, an organic complexing agent, with a carrier to obtain a composite carrier, (2) calcining the composite carrier to obtain a calcined composite carrier, wherein the total carbon content is 1% by weight or less, and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst. The hydrogenation catalyst has both hydrogenation desulfurization activity and hydrogenation denitrogenation activity and has a very long service life.

Description

Hydrogenation catalyst, its production and application Technical background This application relates to a catalyst, in particular to a hydrogenation catalyst. The application also relates to a process for producing the hydrogenation catalyst and its use in the hydrogenation of feedstock oils. Prior knowledge The increasing environmental awareness and increasingly strict environmental regulations have forced the refining industry to focus more on the development of clean fuel production technologies. In the future market, vehicle fuels with low sulfur content will be very popular, and fuels that do not meet emission standards cannot enter this market. As an effective method for desulfurization, hydrogenation technology plays an increasingly important role in the production of clean vehicle fuels. At present, hydrogenation catalysts are the key point of this type of hydrogenation technology. Therefore, the development of new hydrogenation catalysts with high catalytic activity is one of the most urgent needs of the refining industry. It is known that hydrogenation catalysts are usually produced by an impregnation method. For example, Chinese Patent Application No. CN 103551162 A provides a process for producing a hydrogenation catalyst. However, the hydrogenation catalyst produced by the conventional impregnation method has room for further improvement in catalyst activity. Also, the hydrogenation catalyst can be produced by a complexation-impregnation method. For example, Chinese Patent Application No. CN 102909027 A provides a process for producing a hydrogenation catalyst by using an organic complexing agent during the impregnation step. Although the complexation-impregnation method can improve the activity of the hydrogenation catalyst to some extent, there is a problem that the catalyst activity decreases very quickly and the service life of the catalyst is very short. Therefore, there is still a need in the field of hydrogenation catalysts to improve catalyst activity and significantly increase service life compared to existing hydrogenation catalysts. Summary of the invention The inventors of this application have found through intensive research that, on the one hand, in the previous complexation-impregnation method, by introducing an organic complexing agent during the impregnation and drying process at low temperature, the reaction between the active moiety and the carrier can be weakened, the metal dispersion can be improved, and the metal sulfurization sequence can be changed, so that more active phases with high activity can be formed and the number of active centers can be increased. However, due to the low-temperature drying employed in the complexation-impregnation method and the absence of a high-temperature calcination process, the metal compound still exists on the surface of the carrier in the form of metal salts, and the reaction between the active moiety and the carrier is weak, which leads to a number of problems under the conditions of hydrogenation at high temperature, high pressure, and poor raw materials, including metal accumulation during the reaction process, weakening of the auxiliary effect, reduction of the number of active centers, and reduction of intrinsic activity. As a result, the catalyst activity and stability of the produced hydrogenation catalyst are reduced.On the other hand, although the hydrogenation catalyst produced by the previous impregnation method has better stability, the reaction between the active moiety and the carrier is strong and the intrinsic activity of the active site is low. In addition, due to the lack of dispersing and hindering effect of the complexing agent, the active site surfaces are large while the number of active sites is small. As a result, the catalytic activity is difficult to increase. Without being bound by any theory, the inventors of this application believe that the catalytic activity of the catalyst can be improved by adding an organic complexing agent during the first impregnation step and then calcining according to the process of this application. In addition, it is possible to effectively maintain the activity of the catalyst for a long time, thus greatly increasing the service life of the catalyst. This may be because when the organic complexing agent is added during the first impregnation step, the presence of the organic complexing agent prevents the aggregation of the active metal of the organic complexing agent during calcination, making its dispersion uniform, and at the same time, calcination after the first impregnation step can convert the metal compound into a metal oxide, thereby strengthening the bond between the active metal and the carrier, and improving the activity of the catalyst and the stability of the catalyst.In addition, by adding an organic complexing agent during the first impregnation step to coat the catalyst surface with it, the accumulation of active metal during the sulfurization process can be effectively prevented, so that the metal dispersion, which is very favorable for the formation of a class II active phase with higher activity and the formation of more active centers, is improved, thereby further increasing the catalytic activity of the catalyst. The inventors of this application have completed this invention based on previous findings and have solved the problems mentioned above in the prior art section. In particular, this statement relates to the following dimensions. 1. A process for producing a hydrogenation catalyst, which includes the following steps: (1) contacting the first active metal moiety, the organic complexing agent and an optional co-agent with a carrier to obtain a composite carrier, (2) calcining the composite carrier to obtain a calcined composite carrier, wherein the total carbon content on a dry basis is 1 wt% or less, 0.5 wt% or less, 0.4 wt% or less, 0.3 wt% or less, 0.1 wt% or less, 0.08 wt% or less, 0.06 wt% or less, 0.04 wt% or less, 0.03 wt% or less, 0.01 wt% or less, 0.005 wt% or less, based on the dry weight of the calcined composite carrier; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain a hydrogenation catalyst; and Optionally, the process includes one or more of the following steps: Carrier production, and (4) Sulfurization, hydrogenation catalyst 2. A process according to any of the previous dimensions, in which stage (0) includes the following steps: (0-1) forming a carrier precursor or a carrier precursor composition to obtain a preformed carrier, wherein the carrier precursor composition comprises a carrier precursor, a co-formulating agent, and an optional co-agent, (0-2) Calcination of the preformed carrier to obtain the carrier and (0-3) Optionally, contact of the co-agent or second active metal moiety with the carrier wherein the one or more agents selected from the group consisting of both metallic agents (preferably one or more selected from the group consisting of Group IIB metal elements (such as one or more selected from the group consisting of zinc and cadmium), Group IA metal elements (such as one or more selected from the group consisting of lithium, sodium, potassium, rubidium, cesium and francium), Group IIA metal elements (such as one or more selected from the group consisting of beryllium, magnesium, calcium, and strontium) and rare earth metal elements (such as one or more selected from the group consisting of lanthanum, cerium, praseodymium and neodymium), preferably one or more selected from the group consisting of zinc, sodium, potassium, magnesium, calcium, lanthanum and cerium) and non-metallic agents (preferably one or more selected from the group consisting of Group IVA elements (such as silicon), Group VIIA elements (such as one or more selected from the group consisting of fluorine, chlorine, bromine and iodine), Group VA elements (such as one or more selected from phosphorus and arsenic) and Group IIIA elements (such as bromine), preferably one or more selected from the group consisting of fluorine, silicon, phosphorus, and boron), and In it, in the hydrogenation catalyst, the amount of the metallic co-factor, calculated based on the metallic element, is in the range of 0 wt% to 10 wt%, preferably from 0.5 wt% to 6 wt%, based on the total weight of the hydrogenation catalyst, and the amount of the non-metallic co-factor, calculated based on the non-metallic element, is in the range of 0 wt% to 10 wt%, preferably from 0.5 wt% to 6 wt%, based on the total weight of the hydrogenation catalyst. 3. The process according to any one of the preceding aspects, wherein the calcination conditions employed in step (0-2) comprise: a calcination temperature in the range of from 250 °C to 500 °C, preferably from 350 °C to 450 °C, and a calcination time in the range of from 2 hours to 8 hours, preferably from 3 to 6 hours. 4. The process according to each of the previous dimensions, in which stage (0-3) includes the following steps: (0-3-1) impregnating the carrier with the co-agent or second active metal moiety to obtain an impregnated product, and (0-3-2) Drying the impregnated product at a temperature in the range of 100 °C to 250 °C (preferably from 100 °C to 200 °C), or calcining the impregnated product at a temperature in the range of 250 °C to 600 °C (preferably from 350 °C to 500 °C). 5. A process according to any of the preceding dimensions, wherein step (1) includes the following steps: (1-1) impregnating the carrier with the first active metal moiety, the first organic complexing agent, and the optional agent to obtain an impregnated product; and (1-2) Applying heat to the impregnated product at a temperature of from 100 °C to 250 °C (preferably from 100 °C to 200 °C) to obtain the composite carrier. 6. The process according to any one of the preceding aspects, wherein the calcination conditions employed in step (2) comprise: a calcination temperature in the range of 350 °C to 500 °C, preferably from 360 °C to 450 °C, a calcination time in the range of 0.5 hours to 8 hours, preferably from 1 to 6 hours, an oxygen-containing gas (preferably having an oxygen content of not less than 20 vol%) introduced in an amount of more than 0.2 L / (g·hr), preferably from 0.2 L / (g·hr) to 20 L / (g·hr), more preferably from 0.3 L / (g·hr) to 10 L / (g·hr) based on the weight of the carrier. 7. The process according to any of the preceding aspects, wherein step (3) includes the following steps: (3-1) impregnating the calcined composite carrier with a second organic complexing agent to obtain an impregnated product, and (3-2) Applying heat to the impregnation product at a temperature of from 100 °C to 250 °C (preferably from 100 °C to 200 °C) to obtain a hydrogenation catalyst. 8. The process according to any one of the preceding aspects, wherein the amount of the first active metal moiety or the total amount of the first active metal moiety and the amount of the second active metal moiety, calculated on the basis of oxides, is in the range of 6 wt% to 70 wt%, preferably from 15 wt% to 60 wt%, preferably from 20 wt% to 50 wt%, preferably from 20 wt% to 40 wt% based on the total weight of the hydrogenation catalyst, the molar ratio of the first organic complexing agent to the first active metal moiety is in the range of 0.03:1 to 2:1, preferably from 0.08:1 to 1.5:1, the molar ratio of the first organic complexing agent to the second organic complexing agent is in the range of 1:0.25 to 1:4, preferably from 1:0.5 to 1:2, and the molar ratio of the first active metal moiety to the second active metal moiety is in the range of 1:0 to 1:0.4, preferably from 1:0 to 1:0.1. 9. The process according to any of the preceding aspects, wherein the precursor carries one or more selected from the group consisting of alumina, silica, alumina-silica, titania, magnesium, silica-magnesium, silica-zirconia, silica-thuria, silica-beryllia, silica-titania, silica-zirconia, titania-zirconia, silica-alumina-titania, silica-alumina-magnesium and silica-alumina-zirconia, preferably alumina, among their precursors. 10. The process according to any one of the preceding aspects, wherein the first organic complexing agent and the second organic complexing agent are the same or different, each independently being one or more selected from the group consisting of the following species: An organic compound A obtained by truncating the carbon backbone of a C2-30 (preferably C2-10) branched or linear alkane with one or more (e.g., 1 to 5, 1 to 4, 1 to 3, 1 to 2 or 1) heterocyclic group selected from -O- and -NR1-(wherein the R1 group is selected from H and optionally replaces the C1-10 linear or branched alkyl group), (ii) an organic compound B obtained by replacing one or more (e.g. 1 to 5, 1 to 4, 1 to 3, 1 to 2 or 1) hydrogen atoms in the structure of a branched or linear C1-30 alkane (preferably C2-10), a branched or linear C2-30 alkyne (preferably C2-10), a C3-20 cycloalkane (preferably C5-10) which is optionally substituted or organic compound A with a group selected from -R2-OH (wherein the group R2 represents a single bond or a linear or branched C1-10 alkylene, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group), -R3-NR4R5 (wherein the group R2 represents a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group), That group R3 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group or a branched C1-3 alkyne group, preferably a linear or branched C1-3 alkylene group.R4 and R5 are the same or different, and each is independently selected from hydrogen, a linear or branched C1-10 alkyl group and -R6-C(=O)OM, preferably each is independently selected from hydrogen, a linear or branched C1-6 alkyl group and -R6-C(=O)OM, preferably each is independently selected from hydrogen, a linear or branched C1-3 alkyl group and -R6-C(=O)OM, preferably each is independently selected from -R6-C(=O)OM, wherein R6 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, M represents H, an alkali metal or alkaline earth metal) and -R6-C(=O)OM (wherein the R6 group represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, more preferably a linear or branched C1-3 alkylene group, M represents H, an alkali metal or alkaline earth metal), Provided that organic compound A and organic compound B do not contain any oxygen-oxygen, nitrogen-nitrogen, or nitrogen-oxygen bonds in their structure, and (iii) an alkylene oxide homopolymer or copolymer, Preferably, the first organic complexing agent and the second organic complexing agent are the same or different from each other, each independently being one or more selected from the group consisting of: (i) a C1-20 aliphatic (preferably C2-7) or C5-10 alicyclic monocarboxylic acid or polycarboxylic acid (such as one or more selected from the group consisting of acetic acid, maleic acid, oxalic acid, citric acid, tartaric acid, and malic acid) or a salt thereof, optionally substituted with one or more (e.g. 1 to 5, 1 to 3, 1 to 2 or 1) -R2-OH groups (wherein R2 is a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group), (ii) a C1-20 aliphatic (preferably C2-7) or alkyl monoamine or polyamine (such as one or more selected from the group consisting of ethylenediamine, triethylamine, hexamethyldiamine, ethanolamine, diethanolamine, triethanolamine, ethylenediaminetetraacetic acid or a salt thereof, nitrilotriacetic acid or a salt thereof, and 1,2-cyclohexanediaminetetraacetic acid or a salt thereof), which isoptionally substituted with one or more (e.g. 1 to 5, 1 to 4, 1 to 3, 1 to 2 or 1) groups selected from -R2-OH (wherein R2 represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group) and -R6-C(=O)OM (wherein R6 represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, M represents H, an alkali metal or an alkaline earth metal); and (iii) a C2-20 aliphatic (preferably C2-6) or alicyclic polyol C5-10, an oligomer or polymer thereof, or a linear or branched C1-6 alkyl etherate thereof (such as one or more selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, diethylene glycol monomethyl ether, and butylene glycol), more preferably each independently one or more selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol) having a molecular weight in the range of from 200 to 1500, preferably from 200 to 600), diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid or its salt, 1,2-glycohexadiaminetetraacetic acid or its salt, citric acid, tartaric acid, and malic acid, ethylenediamine, and ethylenediaminetetraacetic acid or its salt. 11. The process according to any one of the preceding claims, wherein the first active metal moiety and the second active metal moiety are the same or different, each independently selected from one or more selected from the group consisting of a Group VIB metal element (preferably one or more selected from the group consisting of molybdenum and tungsten) and a Group VIII metal element (preferably one or more selected from the group consisting of cobalt and nickel), preferably each selected from combinations of one or more Group VIB metal elements with one or more Group VIII metal elements, more preferably each selected from combinations of molybdenum and / or tungsten with cobalt or nickel. 12. The process according to any of the preceding aspects, wherein the process does not include any calcination step during or after step (3), or the process does not include any step for introducing a co-agent or metal element having hydrogenation activity during or after step (3). 13. A hydrogenation catalyst produced by the process according to any of the preceding aspects. 14. A hydrogenation catalyst composition comprising a hydrogenation catalyst I and a hydrogenation catalyst II, wherein hydrogenation catalyst I is different from hydrogenation catalyst II, hydrogenation catalyst I is present in an amount by volume of 5 to 95%, preferably 10 to 80%, preferably 20 to 70%, based on the total volume of the hydrogenation catalyst composition, and hydrogenation catalyst I is a hydrogenation catalyst produced by a process according to any of the preceding aspects. 15. A hydrogenation process comprising the step of contacting a feedstock oil with a hydrogenation catalyst according to any of the preceding aspects or a hydrogenation catalyst composition according to any of the preceding aspects in the presence of hydrogen to effect a hydrogenation reaction. 16. The process according to any one of the preceding aspects, wherein the feedstock oil is (i) first contacted with hydrogenation catalyst I and then with hydrogenation catalyst II, (ii) first contacted with hydrogenation catalyst II and then with hydrogenation catalyst I, or (iii) alternately contacted with hydrogenation catalyst I provided in multiple stages and hydrogenation catalyst II provided in multiple stages. 17. The process according to any one of the preceding aspects, wherein the hydrogenation conditions comprise: a reaction temperature in the range of 300°C to 400°C, preferably from 320°C to 380°C, a reaction pressure in the range of 1 MPa to 10 MPa (pressure at a given depth), and preferably from 1 MPa to 8 MPa (pressure at a given depth), a liquid hourly space velocity of the feedstock oil in the range of 0.5 h-1 to 3 h-1, preferably from 0.5 h-1 to 2.5 h-1, and a hydrogen to oil volume ratio in the range of 100 to 800, preferably from 100 to 700. Technical impact The hydrogenation catalyst according to this application has excellent hydrogenation desulfurization and hydrogenation denitrogenation activities. The hydrogenation catalyst according to this declaration shows a very long service life. Detailed description of the invention Specific embodiments of this disclosure are described in detail below, but it should be noted that the scope of this disclosure is not limited to these specific embodiments, but is defined in the appended claims. All publications, patent applications, patents, and other reference documents cited herein are included in the references. Unless otherwise defined, all technical and specific terms used herein have the meanings commonly understood by those skilled in the art. In the event of a conflict, the definition provided herein shall prevail. When a material, object, process, step, device, part or the like is defined herein using the words "known to those skilled in the art", "prior knowledge", "commonly known" or the like, the item defined by such words includes not only those common in the art at the time of filing this application but also those not currently commonly used but which may be recognized as suitable for use for similar purposes in the art. In the context of this application, any material or materials not mentioned are directly applicable to those skilled in the art without any modification. Furthermore, any example described herein may be freely combined with one or more examples described herein, and the resulting technical solution or technical concept shall be considered part of the main subject matter or description of this application and shall not be considered a new subject matter not disclosed or contemplated herein, unless it is clear to those skilled in the art that such a combination is completely unreasonable. In the context of this application, unless expressly stated otherwise, the term "optionally substituted" means optionally substituted with one or more groups selected from the group consisting of hydroxyl, amino, a linear or branched C1-10 alkyl group, a linear or branched C2-10 alkyl group, a cycloalkylC3-20 group, and a C6-20 aryl group. Alternatively, hydroxyl, amino, a linear or branched C1-10 alkyl group are preferred, and a linear or branched C1-10 alkyl group is more preferred. Here, as a C1-10 linear or branched alkyl group, for example, a C1-10 linear or branched alkyl group, a C1-6 linear or branched alkyl group or a C1-4 linear or branched alkyl group may be mentioned, and more specifically, for example, methyl, ethyl, propyl, n-butyl, isobutyl and n-hexyl may be mentioned. As a C2-10 linear or branched alkenyl group, for example, a C2-6 linear or branched alkenyl group or a C2-4 linear or branched alkenyl group may be mentioned, and more specifically, for example, vinyl, allyl, propenyl, n-butenyl, isobutenyl and n-hexenyl may be mentioned. In the context of this application, the term "C3-20 cycloalkane" refers to a monocyclic, bicyclic, or polycyclic cycloalkane having 3 to 20 ring carbon atoms. Specific examples of C3-20 cycloalkanes herein include monocyclic alkanes, such as cyclopropane, cyclohexane, and cyclopentane, and bicyclic or polycyclic spiro, bridged, or fused alkanes, such as dicyclopentane, decalin, adamantane, spiro[2.4]alkane, spiro[4.5]decane, bicyclo[3.2.1]octane, tricyclo[2.2.1.02,6]octane, norbrenane, and. As a C3-20 cycloalkane, a C3-15 cycloalkane is more preferred, and a C5-10 cycloalkane and a C5-7 cycloalkane are more preferred. Furthermore, the term "C3-20 cycloalkyl" denotes a monovalent group obtained by removing a hydrogen atom from a C3-20 cycloalkane. In the context of this application, the term "C6-20 aryl" refers to an aromatic group having 6 to 20 ring carbon atoms. Examples of the C6-20 aryl group include phenyl, a group in which two or more benzene rings are directly connected by a single bond, such as biphenyl and terphenyl, and a group in which two or more benzene rings are condensed, such as naphthyl, anthryl, and phenanthryl. As the C6-20 aryl group, C6-20, phenyl, naphthyl, and biphenyl are more preferred. In the context of this statement, unless otherwise clearly stated, the term "one or more" generally refers to 1 to 5, 1 to 4, 1 to 3, 1 to 2 or 1. In the context of this application, the term "unsaturated impregnation method", which is commonly understood in the art, means that the amount of wetting fluid for impregnation (referred to as the immersion or wetting fluid) is less than the absorption of the impregnated liquid by the article being impregnated (such as carrier particles, etc.) during impregnation. For example, for a volume of the article to be impregnated (such as carrier particles, etc.), the ratio of wetting fluid to the absorption of the impregnating liquid (which is converted to a volume amount) by the article to be impregnated is usually 0.01-0.6:1, preferably 0.02-0.4:1. The unsaturated impregnation method is usually carried out under normal temperature and normal pressure, but may also be carried out at elevated temperature or low or high pressure as required in some cases, without any limitation. In the context of this application, the term "saturated impregnation method" (also called equal volume impregnation method), which is commonly understood in the art, means that the amount of wetting fluid for impregnation (also called immersion or wetting fluid) is equal to the absorption of the impregnated liquid by the article being impregnated (such as carrier particles, etc.) during impregnation. For example, for a volume of the article to be impregnated (such as carrier particles, etc.), the volumetric ratio of the wetting fluid to the absorption of the impregnating liquid (which is converted to a volumetric amount) by the article to be impregnated is usually 0.9-1.1:1, preferably 0.95-1.05:1. The saturated impregnation method is usually carried out under normal temperature and normal pressure, but may also be carried out at elevated temperature or low or high pressure as required in some cases, without any limitation. In the context of this application, the term "over-impregnation method", which is commonly understood in the art, means that the amount of wetting fluid for impregnation (referred to as the immersion or wetting fluid) is greater than the absorption of the impregnated liquid by the article being impregnated (such as carrier particles, etc.) during impregnation. For example, for a volume of the article to be impregnated (such as carrier particles, etc.), the ratio of wetting fluid to the absorption of the impregnating liquid (which is converted to a volumetric amount) by the article to be impregnated is usually 1.5-15:1, preferably 5-10:1. The over-impregnation method is usually carried out under normal temperature and normal pressure, but may also be carried out at elevated temperature or low or high pressure as required in some cases, without any limitation. Where not expressly stated, all percentages, parts, ratios, etc., given herein shall be understood to be by weight, unless such understanding satisfies the ordinary knowledge of a person skilled in the art. According to this statement, a process for producing a hydrogenation catalyst is first provided, which includes at least the following steps: (1) contacting a first active metal moiety and a first organic complexing agent with a carrier to obtain a composite carrier, (2) calcining the composite carrier to obtain a calcined composite carrier, wherein the total carbon content on a dry basis of the calcined composite carrier is 1% by weight or less based on the dry weight of the calcined composite carrier; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain a hydrogenation catalyst; and According to this disclosure, in step (1), as the carrier, any material known in the art that can be used as a carrier for a hydrogenation catalyst can be mentioned without any limitation. Specific examples include, for example, porous resistant carriers. Here, as the porous resistant carrier, for example, porous resistant oxide may be mentioned, and inorganic resistant oxides are more preferable. More specifically, examples of the porous inorganic resistant oxide include oxides of elements of Group II, Group III, Group IV of the periodic table, and more preferably, for example, alumina, silica, alumina-silica, titanium, magnesium, silica-magnesium, silica-zirconia, silica-alumina-thorium, silica-alumina, titanium, silica-alumina-magnesium and silica-alumina-zirconia, preferably alumina. Here, specific examples of alumina include γ-alumina, η-alumina, θ-alumina, δ-alumina, and χ-alumina, γ-alumina being more preferred. According to an embodiment of this disclosure, in step (1), the carrier comprises alumina as a main component. Here, specific examples of alumina include γ-alumina, η-alumina, θ-alumina, δ-alumina, and χ-alumina, γ-alumina are more preferred. According to this disclosure, in step (1), the carrier is a specific material (e.g., a shaped material) rather than an amorphous material such as powders. As the particle shape, various shapes commonly used for (shaped) carriers known in the art that are useful may be mentioned, and spherical, columnar, and sheet-like shapes may be examples to be mentioned, with columnar and spherical shapes being more preferable. Examples of the spherical shape include a spherical shape and an elliptical shape. Examples of the columnar shape include a cylindrical shape, a square columnar shape, and a columnar shape having a cross-section profile (e.g., clover). According to this disclosure, in step (1), the carrier can be formed into particles by any method commonly used in the art, and commercially available granular products can also be used. According to this application, in step (1), the specific surface area (BET method) of the carrier is typically in the range of 100 to 500 m2 / g, preferably from 150 to 400 m2 / g. According to this statement, in step (1), the pore volume of the carrier (BET method) is usually in the range of 0.1 to 1.0 ml / g, preferably 0.3 to 0.9 ml / g. According to this statement, in step (1), the bulk density (mechanical impact method) of the carrier is usually in the range of 40 to 100 g / 100 ml, preferably 45 to 70 g / 100 ml. According to this statement, in step (1), the absorption of the impregnated liquid carrier is usually in the range of 40 to 140 ml / 100 g, preferably 60 to 120 ml / 100 g. In order to determine the absorption of the impregnated liquid, 100 g of the porous granular resistant carrier was measured in a separatory funnel, and then 300 ml of pure water was added thereto until the water level was higher than the carrier level, then it was kept for 30 minutes, and then the excess water was drained into a graduated cylinder, and the amount of excess water L was obtained. Here, the absorption of the impregnated liquid can be obtained by calcination according to the equation (300-L) ÷ 100 (ml / 100 g). According to this statement, in step (1), the average carrier particle size (sieving method) is usually in the range of 2 mm to 8 mm, preferably 3 mm to 5 mm. According to this disclosure, in step (1), the order of contacting the first active metal moiety, the first organic complexing agent with the carrier is not particularly limited, and specific examples thereof include a process in which the first active metal moiety, the first organic complexing agent are contacted with the carrier simultaneously (which is called a one-step contacting process), and a process in which the first active metal moiety, the first organic complexing agent are contacted with the carrier sequentially (which is called a multi-step contacting process). When a multi-step contacting process is employed, it is preferable that the product obtained by the contact is subjected to a heat treatment (e.g., drying) after completion of each contacting step. Here, this disclosure does not impose any limitation on the drying process and drying conditions for the product obtained by the contact, and known knowledge in the art can be adopted. For example, as drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 to 12 hours, preferably from 1 to 10 hours. According to the example of this disclosure, in step (1), in addition to the first active metal moiety and the first organic complexing agent, a co-agent may also be introduced and contacted with the carrier. According to the example of this disclosure, in step (1), the order of contacting the first active metal moiety, the first organic complexing agent and the agent with the carrier is not particularly limited, and specific examples thereof include a process in which the first active metal moiety, the first organic complexing agent and the agent are contacted with the carrier simultaneously (which is called a one-step contacting process), and a process in which the first active metal moiety, the first organic complexing agent and the agent are contacted with the carrier sequentially (which is called a multi-step contacting process). When a multi-step contacting process is employed, it is preferable that the product obtained by the contact is subjected to a heat treatment (e.g., drying) after completion of each contacting step. Here, this disclosure does not impose any limitation on the drying process and drying conditions for the product obtained by the contact, and known knowledge in the art can be adopted. For example, as drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 to 12 hours, preferably from 1 to 10 hours.Alternatively, when a multi-step contact process is employed and the co-agent is contacted with the carrier in the first place, it is preferable that the product obtained from the contact is subjected to a heat treatment such as drying, calcination, or drying followed by calcination after completion of each contact step. Here, this specification does not impose any limitation on the drying process and drying conditions for the product obtained from the contact, and the known knowledge in the art can be accepted. For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 to 12 hours, preferably from 1 to 10 hours. Alternatively, when a multi-step contacting process is employed and both agents are contacted with the carrier in the first step, it is preferred that the contacting product be subjected to a heat treatment such as drying, calcination, or drying followed by calcination after completion of each contacting step. Furthermore, this application does not impose any limitations on the calcination process and calcination conditions for the contacting product, and the art in the art may be accepted.For example, as calcination conditions, the calcination temperature is usually in the range of 250 °C to 600 °C, preferably from 350 °C to 500 °C, and the calcination time is usually in the range of 2 to 8 hours, preferably from 3 to 6 hours. According to the present invention, in step (1), the method of contacting the first active metal moiety, the first organic complexing agent, and the optional agent with the carrier is not particularly limited. Specifically, for example, any method in which the first active metal moiety, the first organic complexing agent, and the optional agent may be supported may be mentioned, and more specifically, for example, the first active metal moiety, the first organic complexing agent, and the optional agent may be impregnated in the carrier to obtain an impregnated product. Here, the impregnation may be carried out by any method known in the art. For example, as the impregnation method, an unsaturated impregnation method, a saturated impregnation method, and an over-impregnation method may be mentioned. In addition, the impregnation temperature according to the present application is not particularly limited, and various temperatures that can be obtained using the impregnation liquid may be used, and the impregnation time is not particularly limited as long as a desired amount can be loaded. For example, the impregnation temperature may range from 15 to 60 °C and the impregnation time may range from 0.5 to 5 hours. According to this application, in step (1), in particular, as a contacting process, for example, a process in which the carrier may be first impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of co-impregnating agent to obtain a pre-impregnated carrier after drying and calcining as described above, and then the pre-impregnated carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of the first active metal moiety and a predetermined amount of the first organic complexing agent to obtain an impregnated product, or a process in which the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of the first active metal moiety and a predetermined amount of the first organic complexing agent and a predetermined amount of co-impregnating agent to obtain an impregnated product, or a process in which the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of the first active metal moiety First and a predetermined amount of organic complexing agent First and a predetermined amount of organic complexing agent are also impregnating agents to form a productimpregnated or a process in which the carrier is first impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first active metal moiety to obtain a pre-impregnated carrier after drying as described above and then the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first organic complexing agent to obtain an impregnated product or a process in which the carrier is first impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first organic complexing agent to obtain a pre-impregnated carrier after drying as described above and then the pre-impregnated carrier is impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first active metal moiety to obtain an impregnated product or a process in which the carrier is first impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first active metal moiety to obtain an impregnated product or a process in which the carrier is first impregnated with an impregnating liquid (preferably an aqueous solution) containing A quantity of organic complexing agent is first impregnated, and after drying, a pre-impregnated carrier is applied as described above.The pre-impregnated carrier may then be impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the first active metal moiety and the remaining amount of the first organic complexing agent to obtain an impregnated product. According to an example of this application, after step (1) is completely completed, the obtained composite carrier or impregnated product may be subjected to a heat treatment such as drying. Here, this application does not have any limitation on the drying process and drying conditions for the composite carrier or impregnated product, and the known knowledge in this field can be adopted. For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 hour to 12 hours, preferably from 1 hour to 10 hours. The heated product obtained after the heat treatment is also referred to as the composite carrier in this application. According to this application, in step (2), the composite carrier is calcined to obtain a calcined composite carrier. Here, the total carbon content on a dry basis of the calcined composite carrier should not exceed 1% by weight based on the dry weight of the calcined composite carrier. According to this application, in step (2), the calcination process and calcination conditions for the composite carrier are not limited as long as the amount of carbon on a dry basis of the calcined composite carrier finally obtained does not exceed 1% by weight based on the dry weight of the calcined composite carrier. Specific examples of the calcination conditions include, for example, a calcination temperature that is usually in the range of 350 °C to 500 °C, preferably from 360 °C to 450 °C, and a calcination time that is usually in the range of 0.5 hours to 6 hours, preferably from 1 hour to 6 hours. In addition, the calcination is preferably carried out under an oxygen-containing atmosphere, more preferably by introducing an oxygen-containing gas. In this case, the oxygen-containing gas is usually in an amount of more than 0.2 L / (g·hr), preferably 0.2 to 20 L / (g·hr), more preferably 0.3-10 L / (g·hr) based on the weight of the carrier. Here, the unit "g" represents the weight of the carrier. Here, as the oxygen-containing gas, for example, air, oxygen, and other oxygen-containing gases may be mentioned. Preferably, the volume content of oxygen in the oxygen-containing gas is usually not less than 20% by volume. According to this statement, in step (2), the total carbon content on a dry basis may be 0.5 wt% or less or less than 0.5 wt%, 0.4 wt% or less or less than 0.4 wt%, and 0.3 wt% or less or less than 0.3 wt%, 0.1 wt% or less or less than 0.1 wt%, 0.08 wt% or less or less than 0.08 wt% or less or less than 0.06 wt% or less or less than 0.06 wt% or less or less than 0.04 wt% or less or less than 0.04 wt% or less or less than 0.03 wt% or less or less than 0.01 wt% or less or less than 0.01 wt% or less or less than 0.005 wt% or less or less than 0.005 wt%, based on the dry weight of the calcined composite carrier. In addition, as a lower limit The total carbon content on a dry basis, especially for example, 0.4 wt%, 0.3 wt%, 0.01 wt%, 0.005 wt% or 0 wt%, based on the dry weight of the calcined composite carrier may be mentioned. Here, the "0 wt%" mentioned means that the value of the total carbon content is below the threshold of the measuring device and therefore cannot be effectively measured by the measuring device, but this does not necessarily mean that the total carbon content is literally zero, or that the calcined composite carrier is completely free of carbon.In addition, the "total carbon content" mentioned refers to the total amount of carbon present in any form in the calcined composite carrier, including but not limited to carbon present in organic compounds (such as organics), carbon present in inorganic compounds (such as carbonates), and carbon present as elemental carbon. According to this application, in step (3), a second organic complexing agent is contacted with the calcined composite carrier to obtain a hydrogenated catalyst of this application. According to the present invention, in step (3), the method of contacting the second organic complexing agent with the calcined composite carrier is not particularly limited. Specifically, for example, any method in which the second organic complexing agent may be supported on the calcined composite carrier may be mentioned, and more specifically, for example, the second organic complexing agent may be impregnated in the calcined composite carrier to obtain an impregnated product. Here, impregnation may be carried out by any method known in the art. For example, as the impregnation method, an unsaturated impregnation method, a saturated impregnation method, and an over-impregnation method may be mentioned. In addition, the impregnation temperature according to the present application is not particularly limited, and various temperatures that can be obtained using the impregnation liquid may be used, and the impregnation time is not particularly limited as long as a desired amount can be loaded. For example, the impregnation temperature may range from 15 to 60 °C and the impregnation time may range from 0.5 to 5 hours. According to this application, in step (3), specifically, as the contacting process, for example, a process in which the calcined composite carrier may be first impregnated with an impregnating liquid (preferably an aqueous solution) containing a predetermined amount of the second organic complexing agent to obtain an impregnated product, or a process in which the calcined composite carrier is impregnated with an impregnating liquid (preferably an aqueous solution) containing an amount of the second organic complexing agent to obtain a pre-impregnated carrier after drying, and then the pre-impregnated carrier is impregnated with an impregnating liquid (preferably an aqueous solution) containing an amount and a residual amount of the second organic complexing agent may be mentioned. Here, this application does not have any limitation on the drying process and drying conditions, and the known knowledge in the field can be adopted. For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 hour to 12 hours, preferably from 1 hour to 10 hours. According to an example of this application, after the step (3) is completely completed, the hydrogenation catalyst or the impregnated product obtained may be subjected to a heat treatment such as drying. Here, this application does not have any limitation on the drying process and drying conditions for the composite carrier or the impregnated product, and the known knowledge in this field can be adopted. For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 hour to 12 hours, preferably from 1 hour to 10 hours. The heated product obtained after the heat treatment is also referred to as the hydrogenation catalyst in this application. Here, it is preferable to perform the heat treatment in a manner such that at least 50% by weight (e.g., at least 60% by weight, at least 70% by weight, or at least 80% by weight) of the second organic complexing agent or its thermal decomposition product remains in the hydrogenation catalyst.More preferably, the heat treatment does not include calcination, or in other words, during or after step (3), the hydrogenation catalyst or the resulting impregnated product is not subjected to calcination. Here, the term "calcination" can be understood in accordance with the general knowledge in the art, for example, it can be understood as a process in which the sample to be treated is kept at a temperature in the range of 300 °C to 500 °C for at least 0.1 hour or more. According to one embodiment of this disclosure, in order for the technical effect of this disclosure to be fully understood, no input of an effective amount of the co-agent (as described below) or an effective amount of the metal element having hydrogenation activity (as described below) to the calcined composite carrier is made during or after step (3), preferably no input of an effective amount of the co-agent and an effective amount of the metal element having hydrogenation activity to the calcined composite carrier is made. Here, as will be understood by those skilled in the art, the term "effective amount" refers to the minimum amount of the relevant component required to provide the desired function or effect. According to an example of this disclosure, the hydrogenation catalyst production process may also include a carrier production step (referred to as step (0)). According to this embodiment of the present disclosure, the process for producing the carrier is not particularly limited, and any process known in the art can be used to produce carriers for hydrogenation catalysts without any limitation. For example, step (0) may be carried out in a manner comprising at least the following two steps. forming a carrier precursor or a carrier precursor combination to obtain a preformed carrier, and Calcination of pre-formed resin to obtain carrier According to this application, in step (0-1) the carrier precursor composition includes a carrier precursor and a forming aid. According to an example of this disclosure, in step (0-1), the carrier precursor composition may include a cofactor. According to this disclosure, in step (1-0), as the precursor, any material known in the art that can be used as a carrier precursor for a hydrogenation catalyst can be mentioned without any limitation. Specific examples include, for example, porous resistant oxides (including precursors thereof) and porous inorganic resistant oxides (including precursors thereof) which are more preferable. More specifically, examples of the porous inorganic resistant oxide include oxides of elements of Group II, Group III, Group IV of the periodic table, and more preferably, for example, alumina, silica, alumina-silica, titanium, magnesium, silica-magnesium, silica-zirconia, silica-alumina-thorium, silica-alumina, titanium, silica-alumina-magnesium and silica-alumina-zirconia, preferably alumina. In addition, as the alumina precursor, hydrided alumina, aluminum salts, organoaluminum, and aluminum sol can be specifically mentioned. More specifically, as hydrided alumina, alumina trihydrate, alumina monohydrate, amorphous aluminum hydroxide, and boehmite may be mentioned.Typical examples of silica precursors include water-soluble silicon-containing compounds or silicon-containing compounds that can form a silicon gel or a sol in an aqueous medium, more specifically, water glass, silica sol, silica gel, and silicate. These carrier precursors (including their precursors) may be used singly or in combination of two or more thereof in any ratio. Preferably, the carrier precursor has alumina (including their precursors) as the main component. According to this application, in step (0-1), as the forming aid, any material known in the art that can be useful for the hydrogenation catalyst may be used without any limitation. Typical examples thereof include water, compacting agents, thickening agents, modifiers, pore-forming agents, and blowing agents. More specifically, such as pthaliocyanine powder, citric acid, methyl cellulose, starch, polyvinyl alcohol, and polyethylene ethanol may be mentioned. These forming aids may be used alone or in combination of two or more thereof in any ratio. Furthermore, with regard to the amount of the forming aid, the known knowledge in the art may be adopted without any particular limitation. According to this disclosure, in step (0-1), the process for producing the carrier precursor composition is not particularly limited, and any process that can combine the carrier precursor, the co-formulating agent, and the optional agent can be used. For example, a process for producing the carrier precursor composition may include, for example, a process in which the carrier precursor, the co-formulating agent, and the optional agent are mixed at a predetermined ratio to become uniform. According to this application, in step (0-1), the process of forming the carrier precursor or the carrier precursor composition is not limited, and any known process in the production of carriers for hydrogenation catalysts can be used. Specific examples of the forming process include a drop molding process, a ball rolling granulation process, a hammer molding process, and a densification molding process, and more particularly, a drop molding process and a hammer molding process. According to this application, in step (0-1), the shape of the preformed carrier is not particularly limited, and various shapes commonly used in the field for hydrogenation catalysts can be used. Specific examples of the shape of the preformed carrier include a quasi-spherical shape, a cylindrical shape, a quasi-sheet shape and the like, and a spherical shape or a cylindrical shape is preferable. Examples of the spherical shape include a quasi-spherical shape, a spherical shape and an elliptical shape. According to this application, in step (0-1), the size of the preformed support is not particularly limited, and various sizes commonly used in the art for supports of hydrogenation catalysts can be used. Specifically, for example, the average particle size (sieving method) is usually in the range of 2 mm to 8 mm, preferably 3 mm to 5 mm. According to this application, in step (0-2), the calcination process and calcination conditions for the preformed support are not limited, and any calcination process and calcination conditions known in the art that are useful for producing supports for hydrogenation catalysts can be used. Specific examples of calcination conditions include, for example, a calcination temperature that is typically between 250°C and 500°C, preferably from 350°C to 450°C, and a calcination time that is typically in the range of 2 hours to 8 hours, preferably from 3 hours to 6 hours. According to an example of this application, the preformed carrier may be dried before step (0-2). Here, this application does not have any limitation on the drying process and drying conditions for the preformed carrier, and any drying process and drying conditions that are useful in the field for producing carriers for hydrogenation catalysts can be used. Specifically, as the drying conditions, for example, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is in the range of 1 hour to 12 hours, preferably from 1 hour to 10 hours. According to a specific example of this application, step (0) may include a step of contacting the co-agent with a carrier to obtain a contact product (referred to as step (0-3). Here, the carrier refers to the carrier obtained after step (0-2). According to a specific embodiment of the invention, step (0) may include a step of contacting the second active metal moiety with the carrier to obtain a contact product (referred to as step (0-3). Here, the carrier refers to the carrier obtained after step (0-2). According to a specific embodiment of the invention, step (0) may include a step of contacting the co-agent and the second active metal moiety with the carrier to obtain a contact product (referred to as step (0-3). Here, the carrier refers to the carrier obtained after step (0-2). According to this application, in step (0-3), when both the agent and the second active metal moiety are used simultaneously, the order of contacting both the agent and the second active metal moiety with the carrier is not particularly limited, and specific examples thereof include a process in which both the agent and the second active metal moiety are contacted with the carrier simultaneously (referred to as a one-step contacting process) and a process in which both the agent and the second active metal moiety are contacted with the carrier sequentially (referred to as a multi-step contacting process). When a multi-step contacting process is used, it is preferable that the product obtained after completion of each contacting step is subjected to a heat treatment (such as calcination, or drying followed by calcination) after completion of each contacting step. Here, this application does not impose any limitation on the drying process and drying conditions for producing the product obtained by contacting, and known knowledge in the art can be adopted.For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 hour to 12 hours, preferably from 1 hour to 10 hours. Furthermore, this application does not impose any limitation on the calcination process and calcination conditions for producing the contact product, and the known knowledge in the art can be accepted. For example, as the calcination conditions, the calcination temperature is usually in the range of 250 °C to 600 °C, preferably from 350 °C to 500 °C, and the calcination time is usually in the range of 2 hours to 8 hours, preferably from 3 hours to 6 hours. According to the present invention, in step (0-3), the method of contacting the first active metal moiety or the first active metal moiety with the carrier is not particularly limited. Specifically, for example, any method in which the first active metal moiety or the first active metal moiety may be supported may be mentioned, and more specifically, for example, the first active metal moiety or the first active metal moiety may be impregnated in the carrier to obtain an impregnated product. Here, impregnation may be carried out by any method known in the art. For example, as the impregnation method, an unsaturated impregnation method, a saturated impregnation method, and an over-impregnation method may be mentioned. In addition, the impregnation temperature according to the present application is not particularly limited, and various temperatures that can be obtained using the impregnation liquid may be used, and the impregnation time is not particularly limited as long as a desired amount can be loaded. For example, the impregnation temperature may range from 15 to 60 °C and the impregnation time may range from 0.5 to 5 hours. According to this application, in step (0-3), specifically, as a contacting process, for example, a process in which the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of co-agent to obtain an impregnated product or a process in which the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety to obtain an impregnated product or a process in which the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of co-agent and a predetermined amount of a second active metal moiety to obtain an impregnated product or a process in which the carrier is first impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety to obtain a pre-impregnated carrier after drying and calcining as described above and then the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety to obtain a pre-impregnated carrier and then the carrier is impregnated with an impregnating liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety to obtain a pre-impregnated carrier after drying and calcining as described above preferably an aqueous solution) containing a predetermined amount of the impregnating agent to obtain an impregnated product or a process in which the carrier is treated with aThe impregnation liquid (preferably an aqueous solution) is impregnated with a predetermined amount of co-impregnation agent to obtain a pre-impregnated carrier after drying and calcining as described above, and then the pre-impregnated carrier is impregnated with an impregnated liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety to obtain an impregnated product, or a process in which the carrier is first impregnated with an impregnated liquid (preferably an aqueous solution) having a predetermined amount of co-impregnation agent to obtain a pre-impregnated carrier after drying and calcining as described above, and then the pre-impregnated carrier is impregnated with an impregnated liquid (preferably an aqueous solution) having a predetermined amount of a second active metal moiety and the remaining amount of co-impregnation agent to obtain an impregnated product may be mentioned. According to an example of this disclosure, in step (0-3), after the contact impregnation is completed, the product obtained by the contact or impregnation may be subjected to a heat treatment such as calcination, drying, or drying followed by calcination. Here, this disclosure has no limitation on the drying process and drying conditions for the product obtained by the contact, and the known knowledge in this field can be accepted. For example, as the drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 to 12 hours, preferably from 1 to 10 hours. Furthermore, this disclosure has no limitation on the calcination process and calcination conditions, and the known knowledge in this field can be accepted. For example, as calcination conditions, the calcination temperature is usually in the range of 250 °C to 600 °C, preferably from 350 °C to 500 °C, and the calcination time is usually in the range of 2 to 8 hours, preferably from 3 to 6 hours. The heat-treated product obtained after the heat treatment is also referred to as the carrier in this application. According to one embodiment of this disclosure, the process for producing a hydrogenation catalyst may include a step of sulfurizing the hydrogenation catalyst (referred to as step (4)). Here, the hydrogenation catalyst refers to any hydrogenation catalyst produced by the process described above in this disclosure for producing a hydrogenation catalyst. According to this disclosure, in step (4), any method known in the art useful in the desulfurization of hydrogenation catalysts can be employed. For example, desulfurization conditions typically include: the presence of hydrogen, a desulfurization temperature in the range of 180 °C to 450 °C, and a desulfurization reagent selected from sulfur, hydrogen sulfide, carbon disulfide, dimethyl disulfide or polysulfide, and a desulfurization time in the range of 2 hours to 48 hours. Here, the desulfurization can be carried out outside the reactor or inside the desulfurization reactor (such as in situ desulfurization). According to this application, in the process of producing the hydrogenation catalyst, as the first active metal portion and as the second active metal portion, any metal element known in the art having hydrogenation activity may be used, and in particular, a metal element of Group VIB of the periodic table and a metal element of Group VIII of the periodic table may be mentioned. Here, as the metal element of Group VIB of the periodic table, molybdenum and tungsten may be mentioned, in particular, for example, and as the metal element of Group VIII of the periodic table, cobalt and nickel may be mentioned, in particular, for example. These metal elements having hydrogenation activity may be used alone or in combination with two or more of them in any ratio. According to this application, in the process for producing a hydrogenation catalyst, the first active metal moiety and the second active metal moiety may be the same or different from each other, each independently representing a metal element having hydrogenation activity. In addition, the molar ratio of the first active metal moiety to the second active metal moiety is in the range of 1:0 to 1:0.4, preferably 1:0 to 1:0.1, and more preferably no secondary active metal moiety is introduced. According to a specific example of this application, as the active metal element, a metal element of Group VIB of the periodic table and a metal element of Group VIII of the periodic table are used in combination. Here, as the combination, in particular, for example, a combination of molybdenum and tungsten with cobalt and nickel, a molybdenum-nickel, molybdenum-cobalt or tungsten-nickel combination may be mentioned. According to this application, the metal element having hydrogenation activity can be used in any form known in the art. As the form of the metal element having hydrogenation activity, for example, any water-soluble compound whose solubility of the corresponding metal element can satisfy the load requirement or has satisfactory solubility in water in the presence of a quasi-solvent oil can be mentioned, and specific examples thereof include salts and oxides of metal elements, preferably nitrates, chlorides, sulfates and carbonates of the corresponding metal elements, more preferably nitrates of the corresponding metal elements. These water-soluble compounds may be used alone or in combination with two or more of them in any ratio. More specifically, the metal element of Group VIB of the Periodic Table can be used in any form known in the art. Examples of the form of the metal element of Group VIB of the Periodic Table include salts, oxysalts and oxides of the corresponding metal elements, and in particular ammonium molybdate, aluminum paramolybdate, aluminum metatungstate, molybdenum oxide and tungsten oxide.These forms of Group VIB of the periodic table may be used alone or in combinations of two or more of them in any ratio. The metal element of Group VIII can be used in any form known in the art. As the form of the metal element of Group VIII of the Periodic Table, for example, salts and oxides of the corresponding metal elements are preferably nitrates, chlorides, sulfates, formates, acetates, phosphates, citrates, aluminates, molybdates, tungstates, and water-soluble oxides are preferably oxalates, nitrates, sulfates, acetates, chlorides, carbonates, basic carbonates, hydroxides, phosphates, molybdates, tungstates, and water-soluble oxides of the corresponding metal elements are preferably nickel nitrate, nickel sulfate, nickel acetate, basic nickel carbonate, cobalt nitrate, cobalt sulfate, cobalt acetate, basic cobalt carbonate, cobalt chloride, and nickel chloride. These forms of the metal element of Group VIII of the Periodic Table may be used alone or in combination of two or more of them in any ratio. According to this application, in the process of producing a hydrogenation catalyst, for convenience of operation, a metal element having hydrogenation activity (including a metal element of Group VIB of the periodic table and a metal element of Group VIII of the periodic table) is usually used in the form of an impregnation liquid, preferably an aqueous solution, such as when carrying out the contacting or impregnation process in step (1) or step (0-3). For this purpose, the concentration of the metal element having hydrogenation activity, based on the corresponding metal element, in the impregnation liquid is usually in the range of 0.2 to 8 mol / L, preferably 0.2 to 5 mol / L, more preferably 0.2 to 2 mol / L. Here, the concentration refers to the concentration of each metal element having hydrogenation activity in the impregnation liquid, not to the concentration of all metal elements having hydrogenation activity. Furthermore, the impregnation liquid may, depending on the case, contain other compounds, such as the first organic complexing agent or co-agent, in addition to the metal element having hydrogenation activity. Therefore, the effort for separately preparing the impregnation liquid corresponding to the first organic complexing agent or co-agent can be reduced.In this case, the first organic complexing agent or co-agent is present in the impregnation solution in the amount specific to this case. Preferably, the impregnation liquid contains at least the first active metal moiety and the first organic complexing agent or co-agent simultaneously. As is known to those skilled in the art, according to this application, the amount of the hydrogenation-active metal element (including the hydrogenation-active metal element as the first active metal moiety or the hydrogenation-active metal element as the second active metal moiety) used is not particularly limited, as long as it is sufficient for the hydrogenation catalyst finally obtained according to this application to have effective catalytic activity (referred to as the effective amount).For example, the amount of the hydrogenation-active metal element (including the hydrogenation-active metal element as the first active metal moiety or the hydrogenation-active metal element as the second active metal moiety) is such that, in the hydrogenation catalyst ultimately obtained by the process of this application for producing a hydrogenation catalyst, the amount of the hydrogenation-active metal element, based on the corresponding metal element oxide, is usually in the range of 6 to 70% by weight, preferably 15 to 60% by weight, 20 to 50% by weight, most preferably 20 to 40% by weight, based on the total weight of the hydrogenation catalyst.Additionally, for example, the amount of the metal element of Group VIII of the Periodic Table (including the metal element of Group VIII of the Periodic Table as the first active metal moiety or the metal element of Group VIII of the Periodic Table as the second active metal moiety) used is such that in the hydrogenation catalyst ultimately obtained, the process of this application for producing the hydrogenation catalyst, the amount of the metal element of Group VIII of the Periodic Table, based on the corresponding metal element oxide, is typically in the range of 1 to 10% by weight, based on the total weight of the hydrogenation catalyst. In addition, for example, the amount of the metal element of Group VIB of the Periodic Table (including the metal element of Group VIB of the Periodic Table as the first active metal moiety or the metal element of Group VIB of the Periodic Table as the second active metal moiety) is such that in the hydrogenation catalyst ultimately obtained, the process of this application for producing the hydrogenation catalyst, the amount of the metal element of Group VIB of the Periodic Table, based on the oxide of the corresponding metal element, is typically in the range of 5 to 60% by weight, based on the total weight of the hydrogenation catalyst. According to this application, in step (1) or step (0-3), when a plurality of metal elements having hydrogenation activity are used in combination, the order of contacting (e.g., by impregnation) each of the metal elements having hydrogenation activity with the carrier is not particularly limited, and specific examples thereof include a process in which the metal elements having hydrogenation activity are contacted with the carrier simultaneously (which is called a one-step contacting process), and a process in which a plurality of metal elements having hydrogenation activity are contacted with the carrier sequentially or sequentially in different combinations (which is called a multi-step process) may be mentioned. When a multi-step process is used, it is preferable that the product obtained by the contact is subjected to a heat treatment (e.g., drying) after completion of each contacting step. Here, this application does not impose any limitation on the drying process and drying conditions for the product obtained by the contact, and the known knowledge in the art can be adopted.For example, as drying conditions, the drying temperature is usually in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, and the drying time is usually in the range of 1 hour to 12 hours, preferably from 1 to 10 hours. According to the present invention, in the process of producing the hydrogenation catalyst, as the first organic complexing agent and the second organic complexing agent, various additives commonly used in the field of producing hydrogenation catalysts can be used. Specific examples of the additives include organic compound A, organic compound B and an alkylene oxide polymer described below. These organic additives may be used alone or in combination of two or more of them in any ratio. According to the present invention, the first organic complexing agent and the second organic complexing agent may be the same or different from each other, each independently representing an organic additive. Furthermore, the molar ratio of the first organic complexing agent to the second organic complexing agent is usually in the range of 1:0.25 to 1:4, preferably 1:0.5 to 1:2. According to the present application, as organic compound A, it refers to an organic compound obtained by crosslinking a linear or branched C2-30 alkane carbon backbone with one or more hetero groups selected from -O- and -NR1-. The group R1 is selected from H and an optionally substituted linear or branched C1-10 alkyl group, preferably H. Therefore, as the linear or branched C1-10 alkyl group, for example, a linear or branched C1-6 alkyl group or a linear or branched C1-4 alkyl group may be mentioned, and very specifically, for example, methyl, ethyl, propyl, n-butyl, isobutyl and n-hexyl may be mentioned. Specific examples of C2-30 linear or branched alkyne include C2-20 linear or branched alkynes or C2-10 linear or branched alkynes, and more specifically, for example, ethane, n-propane, n-butane, tert-butane, isobutane, n-pentane, isopentane, neopentane, n-hexane, isohexane, neohexane, n-octane, isooctane, t-octane, n-nonane, n-decane, isodecane and tert-decane.From the point of view of structural stability, it is preferable that, where there are two or more such hetero groups, both hetero groups are not directly attached. It is clear that the hetero group is not at the end of the linear or branched alkene carbon skeleton of organic compound A. For example, organic compounds, such as CH3-O-CH2-CH2-CH3 or CH3-CH2-O-CH2-CH3, can be obtained by reacting a linear alkane (n-butane, CH3-CH2-CH2-CH3) with a hetero -O- group, organic compounds, such as CH3-O-CH2-O-CH2-CH3 or CH3-O-CH2-CH2-O-CH3, can be obtained by reacting a linear C4 alkane with two hetero -O- groups, and organic compounds, such as CH3-O-CH2-O-CH2-O-CH3, can be obtained by reacting a linear C4 alkane with two hetero -O- groups.Alternatively, organic compounds, such as CH3-NCH3-CH2-CH2-CH3 or CH3-CH2-NCH3-CH2-CH3, can be obtained by reacting a C4 linear alkane (n-butane, CH3-CH2-CH2-CH3) with one hetero group -NCH3-, organic compounds, such as CH3-NCH3-CH2-NCH3-CH2-CH3 or CH3-NCH3-CH2-CH2-NCH3-CH3-CH3, can be obtained by reacting a C4 linear alkane with two hetero groups -NCH3-, and organic groups, such as CH3-NCH3-CH2-NCH3-CH2-NCH3-CH3, can be obtained by reacting a C4 linear alkane with three hetero groups -NCH3-. These organic groups A can be used alone or in combination with two or more of them in any ratio. These organic compounds A can be obtained according to any known method, and can also be obtained commercially. According to the present application, as organic compound B, it refers to an organic compound obtained by replacing one or more hydrogen atoms in the structure of a linear or branched C1-30 alkane, a linear or branched C2-30 alkane, an optionally substituted C3-20 cycloalkane, or an organic compound A with a group selected from the group consisting of -R2-OH, -R3-NR4R5, and -R6-C(=O)OM. Here, as the linear or branched C1-30 alkane, specifically, for example, a linear or branched C2-20 alkane or a linear or branched C2-10 alkane may be mentioned, and very specifically, for example, ethane, n-propane, isopropane, n-butane, tert-butane, isobutane, n-pentane, isopentane, neopentane, n-hexane, isohexane, neohexane, n-octane, isooctane, tert-octane, n-nonane, n-decane, isodecane and tert-decane may be mentioned.Specific examples of linear or branched C2-30 alkene include linear or branched C2-20 alkene or linear or branched C2-10 alkene, and more specifically, for example, ethylene, propylene, 1-butylene, 2-butene, 1-pentene, 2-pentene, 2-methyl-1-butene, 1-hexene, 2-hexene, 3-hexene, 2-methyl-1-pentene, 1-heptene, 2-heptene, 2-methyl-1-hexene, 3-methyl-1-hexene, 1-octene, 2-octene, 2-methyl-1-octene, 4-methyl-2-octene, 4-ocene, 1-decene, 2-decene, 5-decene, 2-methyl-1-nonene, 3-methyl-1-nonene, 5-methyl-1-nonene, 3-methyl-2-nonene and 2-methyl-5-nonene. These organic compounds B may be used alone or in combination with two or more of them in any ratio. These organic compounds B can be produced according to a known method, and can also be obtained commercially. According to the present application, the group R2 represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, such as ethylene or methylene. According to the present application, the group R3 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, such as alkylene or methylene. According to the present application, R4 and R5 are the same or different, each independently selected from the group consisting of hydrogen, linear or branched C1-10 alkyl group and -R6-C(=O)OM, preferably each independently selected from hydrogen, linear or branched C1-6 alkyl group and -R6-C(=O)OM, most preferably each independently selected from linear or branched C1-3 alkyl group and -R6-C(=O)OM, preferably each independently represents -R6-C(=O)OM. Here, examples of linear or branched C1-3 alkyl group include ethyl or methyl. Furthermore, the -C(=O)OM group represents a carboxylate group. According to the present application, the group R6 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, such as ethylene or methylene. According to the present application, the group M represents H, and an alkali metal or an alkaline earth metal. Here, specific examples of the alkali metal include sodium and potassium, and specific examples of the alkaline earth metal include magnesium, calcium and barium. According to this declaration, from the point of view of structural stability, in the structures of organic compound A and organic compound B, there are no oxygen-oxygen bonds (such as OO), nitrogen-nitrogen bonds (such as NN or N=N), or nitrogen-oxygen bonds (such as NO or N=O). According to the present application, as an alkali oxide polymer, it refers to an alkylene oxide homopolymer or copolymer. Here, specific examples of an alkylene oxide homopolymer include polyethylene glycol and polypropylene glycol. Specific examples of an alkylene oxide copolymer include an ethylene oxide / propylene oxide copolymer. In the alkylene oxide copolymer, structural units derived from a multifunctional monomer such as glycerin may be incorporated as needed in addition to those derived from ethylene oxide or propylene oxide. The molecular weight of the alkylene oxide polymer is not particularly limited in the present application, and conventional knowledge is accepted in the prior art, but specifically, for example, it may be in the range of from 100 to 3000, preferably from 200 to 1500, most preferably from 200 to 600. These alkylene oxide polymers may be used alone or in combination with two or more of them in any ratio. These alkylene oxide polymers can be produced according to a specific method or obtained commercially. According to an example of the present application, as the organic additive, very specifically, for example, a C5-10 alicyclic or C1-20 aliphatic monoamine or polycarboxylic acid optionally containing one or more -R2-OH groups as substituents or a salt thereof can be mentioned. Here, the R2 group represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, such as ethylene or methylene. As the C1-20 aliphatic mono- or polycarboxylic acid or a salt thereof, an aliphatic mono- or polycarboxylic acid or a salt thereof is preferred, and very specifically, acetic acid, maleic acid, and oxalic acid can be mentioned.As the C1-20 aliphatic mono- or polycarboxylic acid containing one or more -R2-OH groups as substituents or a salt thereof, a C2-7 aliphatic mono- or polycarboxylic acid containing one or more -R2-OH groups as substituents or a salt thereof is preferred, and more particularly, for example, citric acid, tartaric acid can be mentioned. As the C5-10 alicyclic mono- or polycarboxylic acid or a salt thereof, a C5-7 alicyclic mono- or polycarboxylic acid or a salt thereof is preferred, and more particularly, for example, cyclohexanedicarboxylic acid can be mentioned. These mono- or polycarboxylic acids or their salts can be used singly or in combination of two or more of them in any ratio. These mono- or tricarboxylic acids or their corresponding salts can be produced according to known methods, and can also be obtained commercially. According to the present disclosure, as the organic additive, for example, an aliphatic C1-20 or alicyclic C5-10 mono- or polyamine optionally containing one or more substituents selected from the group consisting of -R2-OH and -R6-C(=O)OM may be mentioned. Here, the group R2 represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, such as ethylene or methylene. The group R6 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, such as ethylene or methylene. Group M represents H, and is an alkali metal or an alkaline earth metal. Specific examples of an alkali metal include sodium or potassium. Specific examples of an alkaline earth metal include manganese, calcium, and boron.In addition, as the C1-20 aliphatic mono- or polyamine, a C2-7 aliphatic mono- or polyamine is preferred, and very specifically, for example, ethylenediamine, triethylamine and hexamethylendiamine can be mentioned. As the C1-20 aliphatic mono- or polyamine containing one or more -R2-OH groups as a substituent, a C2-7 aliphatic mono- or polyamine containing one or more -R2-OH groups as a substituent is preferred, and very specifically, for example, ethanolamine, diethanolamine and triethanolamine can be mentioned. As the C1-20 aliphatic mono or polyamine containing one or more -R6-C(=O)OM groups as a substituent, C2-7 aliphatic mono or polyamine containing one or more -R6-C(=O)OM groups as a substituent is preferred, and very preferably, for example, ethylenediamine tetraacetic acid or a salt thereof and nitrilotetraacetic acid or a salt thereof can be mentioned. As the C5-10 alicyclic mono or polyamine, C5-7 alicyclic mono or polyamine is preferred, and very specifically, for example, 2,1-cyclohexanediamine can be mentioned.As the C5-10alicyclic mono- or polyamine containing one or more -R6-C(=O)OM groups as substituents, C5-7alicyclic mono- or polyamine containing one or more -R6-C(=O)OM groups as substituents are preferred, and very specifically, for example, 2,1-cyclohexanediaminetetraacetic acid or a corresponding salt thereof can be mentioned. These mono- or polyamines may be used alone or in combination of two or more of them in any ratio. These mono- or polyamines can be produced according to a known method or can be obtained commercially. According to the example of the present application, as the organic additive, for example, C2-20 aliphatic or C5-10 alicyclic polyols can be mentioned very specifically. Here, as the C2-20 aliphatic polyol, C2-6 aliphatic polyols are preferred, and very specifically, ethylene glycol, butylene glycol and glycerin can be mentioned. As the C5-10 alicyclic polyol, C5-7 alicyclic polyols are preferred, and very specifically, cyclohexanedimethanol can be mentioned. In addition, as the organic additive, for example, polymers of polyols, including oligomers or polymers of polyols, for example, polyethylene glycol, polypropylene glycol, diethylene glycol, triethylene glycol or tripropylene glycol, or the like can be mentioned very specifically. Here, the molecular weight of the polymer is generally in the range of 100 to 3000, preferably from 200 to 1500, most preferably 200 to 600, but is not limited thereto.In addition, as an additive, for example, C1-6 linear or branched alkyl ethers of polymers may be mentioned in addition, and very very particularly, diethylene glycol monomethyl ether may be mentioned. These polyols, polymers or ethers may be used alone or in combination of two or more of them in any ratio. These polymers or ethers can be produced in a known manner, or they can also be commercially available. According to the present application, as the organic additive, very specifically, for example, ethylene glycol, glycerin, polyethylene glycol (having a molecular weight generally in the range of 200 to 1500, very preferably from 200 to 600), diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid or a salt thereof, 2,1-cyclohexanediaminetetraacetic acid or a salt thereof, citric acid, tartaric acid, maleic acid, ethylenediamine and ethylenediaminetetraacetic acid or a salt thereof may be mentioned. These organic additives may be used singly or in combination of two or more of them in any ratio. These organic additives can be produced by a known method, and can also be commercially available. According to the present application, in the process for producing the hydrogenation catalyst, for ease of operation, the organic additive (including the organic additive as the primary organic complexing agent and / or the organic additive as the secondary organic complexing agent) is generally used in the form of an impregnation liquid, preferably an aqueous liquid, such as during the contacting or impregnation in step (1) or step (3). In the impregnation liquid, the organic additive is present in any amount conventionally used in the prior art. Furthermore, in addition to the organic additive, the impregnation liquid may further comprise other components as appropriate, such as a primary active metal component or co-agent. This avoids the effort of separately preparing the respective impregnation liquid for the primary active metal component or co-agent. In this case, the primary active metal component or co-agent is present in the impregnation solution in the amount specified in the content of the present document. According to the present application, in the hydrogenation catalyst production process, especially in step (1), as the amount of the primary organic complexing agent, for example, the molar ratio of the primary organic complexing agent to the primary active metal component, is generally in the range of 0.03:1 to 2:1, preferably from 0.08:1 to 1.5:1. According to the present disclosure, in the process for producing a hydrogenation catalyst, there is no limitation on the co-agent present in each of the respective steps, such as step (1), step (0-1) or step (0-3), and, for example, various active elements known in the prior art that can be used to improve the performance of the hydrogenation catalyst can be mentioned. These active elements can be used singly or in a combination of two or more of them in any ratio. Here, as the active element, for example, both metallic and non-metallic elements may be mentioned. More specifically, examples of the metallic co-agent include Group IIB metal elements, Group IA metal elements, Group IIA metal elements, and rare earth metal elements. Examples of the Group IIB metal element include zinc or cadmium. Examples of the Group IA metal element include lithium, sodium, potassium, radium, cesium, and cesium. As group IIA metallic elements, for example, beryllium, magnesium, calcium, and strontium may be mentioned.As the earth metal element, for example, lanthanum, cesium, praseodymium and neodymium may be mentioned. As the metal cofactor, zinc, sodium, potassium, magnesium, calcium, lanthanum and cesium are preferred. These metal cofactors may be used alone or in combination with two or more of them in any ratio. In addition, as the non-metal cofactor, very specifically, for example, group IVA elements, group VIIA elements, group VA elements and group IIIA elements may be mentioned. Specific examples of the group IVA element include silicon. Examples of the group VIIA element include fluorine, chlorine, bromine and iodine. Examples of the group VA element include phosphorus and arsenic. As the group IIIA element, for example, boron can be mentioned. As the non-metal cofactor, fluorine, silicon, phosphorus and boron are more preferred. These non-metallic agents may be used alone or in combination with two or more of them in any ratio.It should be specifically noted that, as explained above, the carrier precursor or a carrier may be involved in the hydrogenation catalyst production process, and both the carrier precursor or carrier and the non-metallic co-agent may contain silicon. In this regard, in the context of the present document, unless otherwise specified, when the amount of silicon exceeds 10% by weight and the silicon is present in the oxide form, it is considered as the carrier precursor or carrier, or otherwise it is considered as the non-metallic co-agent. According to the present application, the non-metallic hematopoietic agent may be used in any form known in the prior art. As the form of the non-metallic hematopoietic agent, for example, various water-soluble salts of the corresponding non-metallic elements may be mentioned, and very specifically, for example, oxides, chlorides, oxysalts and ammonium salts of the corresponding non-metallic elements may be mentioned. These water-soluble salts may be used alone or in combination with two or more of them in any ratio. In addition, the metallic hematopoietic agent may be used in any form known in the prior art. As the form of the metallic hematopoietic agent, for example, various water-soluble salts of the corresponding metallic elements may be mentioned, and very specifically, for example, chlorides, nitrates and sulfates of the corresponding metallic elements may be mentioned. These water-soluble salts may be used alone or in combination with two or more of them in any ratio. According to the present disclosure, in the process of producing a hydrogenation catalyst, for convenience of operation, the hemi-agent (including both a metal agent and a non-metal agent) may sometimes be used in the form of an impregnation liquid (preferably an aqueous solution). Here, the amount of the hemi-agent, based on the corresponding metal element or the corresponding non-metal element, in the impregnation liquid is generally in the range of 0.05 to 3 mol / L. In addition, the impregnation liquid may additionally contain other components depending on the case, such as a primary active metal component, a primary organic complexing agent or a secondary active metal component, in addition to the hemi-agent, thereby avoiding the effort of separately preparing the respective impregnation liquid for the primary active metal component, the primary organic complexing agent or the secondary active metal component. In this case, the primary active metal component, the primary organic complexing agent or the secondary active metal component is present in the impregnation liquid in the amount specified in the contents of the present disclosure. According to the present application, the co-agents used in each of the relevant steps, such as step (1), step (0-1) or step (0-3), may be the same or different from each other, each independently representing an activity element. In addition, the specific amount of co-agent used in each of the relevant steps in the present application is not particularly limited as long as the total amount of co-agents used in the process for producing the hydrogenation catalyst of the present application, i.e., the sum of the amounts used in the relevant steps, is such that the amount of co-agent in the hydrogenation catalyst obtained by the hydrogenation catalyst production process reaches the amount conventionally known in the prior art. More specifically, as the amount of the metal cofactor used in the hydrogenation catalyst production process of the present application, for example, it can be mentioned that in the hydrogenation catalyst obtained by the hydrogenation catalyst production process, the metal cofactor is generally present in an amount, based on the metal element, in the range of 0% by weight, preferably from 0.5% by weight to 6% by weight, based on the total weight of the hydrogenation catalyst.In addition, as the total amount of non-metallic co-factor used in the hydrogenation catalyst production process of the present application, for example, it can be mentioned that, in the hydrogenation catalyst obtained by the hydrogenation catalyst production process, the metal element is generally present in an amount, based on the non-metallic element, in the range of 0% by weight to 10% by weight, preferably from 0.5% by weight to 6% by weight, based on the total weight of the hydrogenation catalyst. According to the present application, a hydrogenation catalyst is also provided. The hydrogenation catalyst is produced in accordance with the process previously mentioned for producing the hydrogenation catalyst of the present application. According to the present application, there is further provided a hydrogenation catalyst composition. The hydrogenation catalyst composition comprises at least two different hydrogenation catalysts, namely hydrogenation catalyst I and hydrogenation catalyst II. Herein, the term "different" may specifically refer to a difference in structure, composition, production process, or function. And where a person skilled in the art believes that there is an indisputable difference between two hydrogenation catalysts, the two hydrogenation catalysts may be considered different. According to the present application, hydrogenation catalyst I is a hydrogenation catalyst produced by the hydrogenation catalyst production process of the present application or the hydrogenation catalyst of the present application, and hydrogenation catalyst II is another hydrogenation catalyst known in the prior art. These other hydrogenation catalysts may be used alone or in combination with two or more of them in any ratio. In addition, the other hydrogenation catalyst may be produced according to the production process known in the prior art, or may be commercially obtained. Specifically, hydrogenation catalyst II may, for example, comprise a carrier, a Group VIB metal element and a Group VIII metal element, and, based on the respective metal oxide, the amount of the Group VIII metal element may be 1-10% by weight, and the amount of the Group VIB metal element may be 5-60% by weight, based on the total weight of hydrogenation catalyst II. Here, in connection with the carrier, the metal element of group VIB, and the metal element of group VIII, reference may be made to the corresponding value described above in this document. According to the present application, in the hydrogenation catalyst composition, hydrogenation catalyst I is generally present in an amount of 5 to 95%, preferably 10 to 80%, most preferably 20 to 70% by volume, based on the total volume of the hydrogenation catalyst composition, and hydrogenation catalyst II is generally present in an amount of 5 to 95%, preferably 20 to 90%, most preferably 30 to 80%. In accordance with the present application, there is further provided a hydrogenation process. The hydrogenation process comprises the step of contacting a crude oil with a hydrogenation catalyst of the present application, a hydrogenation catalyst produced by a hydrogenation catalyst production process of the present application, or a hydrogenation catalyst composition of the present application in the presence of hydrogen to conduct a hydrogenation reaction. Here, hydrogenation is directly applicable to the understanding of a person skilled in the art, and specific examples thereof include hydrorefining, and in particular, hydrodesulfurization and hydrodenitrogenation. The application is not limited thereto. According to the present application, examples of crude oils include, for example, those known to a person skilled in the art, and specific examples include gasoline, diesel oil, lubricating oil, kerosene, naphtha, atmospheric residue, vacuum residue, petroleum wax and Fischer-Tropsch synthetic oil. The crude oils may be used alone or in combination with two or more thereof in any ratio. According to the present disclosure, as hydrogenation conditions, the reaction temperature is generally in the range of 300 °C to 400 °C, preferably 320 °C to 380 °C. According to the present disclosure, as hydrogenation conditions, the reaction pressure is generally in the range of 1 MPa to 10 MPa (gauge pressure), preferably from 1 MPa to 8 MPa (gauge pressure). According to the present application, as the hydrogenation conditions, the liquid hourly space velocity of the crude oil is generally in the range of 0.5 h-1 to 0.5 h-1, preferably from 0.5 h-1 to 2.5 h-1. According to the present disclosure, as the hydrogenation conditions, the hydrogen to oil volume ratio is generally in the range of 100 to 800, preferably from 100 to 700. Here, the hydrogen to oil volume ratio is the ratio of the hydrogen gas volumetric flow rate to the crude oil volumetric flow rate. According to a specific embodiment of the present application, the crude oil is contacted with a hydrogenation catalyst composition in the presence of hydrogen. Here, the mode for contacting the crude oil with the hydrogenation catalyst composition is, in particular, for example, the crude oil may be contacted first with hydrogenation catalyst I, and then with hydrogenation catalyst II, or the crude oil may be contacted first with hydrogenation catalyst II and then with hydrogenation catalyst I, or, where there are multiple stages of hydrogenation catalyst I and multiple stages of hydrogenation catalyst II, the crude oil may be contacted alternately with these hydrogenation catalysts. Since hydrogenation catalyst I has a higher catalytic activity and a higher service life than hydrogenation catalyst II, it is preferable to contact hydrogenation catalyst I with the crude oil later, so that the hydrogenation reaction can be carried out by contacting it with the crude oil under more severe reaction conditions. According to the present disclosure, during the hydrogenation reaction using the catalyst combination, the loading mode of the hydrogenation catalyst I and the hydrogenation catalyst II in the hydrogenation reactor for carrying out the hydrogenation reaction is not particularly limited. Specific examples of the loading mode include a layered loading mode and a combined loading mode. Specific examples of the layered loading mode include a process of loading the hydrogenation catalyst I upstream of the hydrogenation catalyst II along the crude oil flow direction, or loading the hydrogenation catalyst II upstream of the hydrogenation catalyst I, or alternately loading the hydrogenation catalyst I and the hydrogenation catalyst II in a layered manner, and preferably loading the hydrogenation catalyst II upstream of the hydrogenation catalyst I. In addition, the hydrogenation catalyst I and the hydrogenation catalyst II may be loaded in the same hydrogenation reactor to form the same catalyst bed or different catalyst beds, or may be loaded separately in each combination in hydrogenation reactors placed in series, respectively. According to the present application, in addition, any additional catalyst or filler that may be useful for improving the useful characteristics of these hydrogenation catalysts may be provided before, after and / or in the hydrogenation catalyst bed I, and / or before, and / or in the hydrogenation catalyst bed II. Here, as the type or method of using the filler, conventional knowledge in the prior art can be accepted. For example, as fillers, ceramic tubes and active support materials can be mentioned. In addition, for example, if the hydrogenation catalyst bed I is placed upstream of the hydrogenation catalyst bed II, a bed consisting of filler may be provided in front of the hydrogenation catalyst bed I in order to improve the distribution of the crude oil in the hydrogenation reactor. Example This statement is further illustrated by the following examples, but is not limited to these examples. In the context of this application, in the following examples and comparative examples, the amount of each element in the hydrogenation catalyst was determined using a Nippon Science and Technology Corporation Type 3271 E X-ray fluorescence spectrometer. In the context of this application, including the following examples and comparative examples, the total carbon content of the calcined composite carrier (hereinafter sometimes referred to as the semi-finished catalyst) was determined using a carbon-sulfur analyzer manufactured by HORIBA, Japan. In the context of this application, in the following examples and comparative examples, the dry weight of the calcined composite carrier (hereinafter sometimes referred to as the semi-finished catalyst) was determined in the following manner: a certain amount (e.g. 30 g) of the sample to be tested was measured, calcined in a muffle furnace at 450 °C for 3 hours, and measured again after cooling, and the weight thus obtained was recorded as the dry weight. In the context of this application, in the following examples and comparative examples, the dry basis of hydrided alumina or aluminum hydroxide powder was measured as follows: a specified amount (e.g. 30 g) of the sample to be tested was measured, calcined in a muffle furnace at 600 °C for 3 hours, and measured again after cooling, and the weight thus obtained was recorded as the dry weight. The ratio of the specified dry weight to the initial weight of the sample to be tested is based on the sample to be tested. Example I-1 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 20 g of phosphoric acid, 20 g of citric acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear impregnated solution. 200 g of alumina carrier was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 400 °C for 2 h, with a gas to reagent ratio of 2 L / (g•hr) to obtain a semi-finished catalyst Z-S1, the total carbon content of which is shown in Table I-1. 5 g of ethanol was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S1 was impregnated with the above solution by saturated impregnation method for 2 hours, and then dried at 110 °C for 3 hours to obtain a S1 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the S1 value is shown in Table I-1. Comparative Example I The hydrogenation catalyst was prepared in the same manner as Example I-1, except that the hydrogenation catalyst S1 prepared in Example I-1 was calcined at 400 °C for 3 hours to obtain a catalyst D1. The amount of the metal element having hydrogenation activity of the catalyst, based on the oxide, based on the amount of S1 is shown in Table I-1. Example I-2 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 54 g of molybdenum trioxide, 21 g of basic cobalt carbonate, 13 g of phosphoric acid, 30 g of citric acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear impregnated solution. 200 g of zirconia carrier was impregnated with the above solution by saturated impregnation method for 2 h, dried at 150 °C for 2 h, and then calcined under air flow at 360 °C for 3 h, with a gas to reagent ratio of 10 L / (g·hr) to obtain a semi-finished Z-S2 catalyst, the total carbon content of which is shown in Table I-1. 30 g of citric acid was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S2 was impregnated with the above solution by saturated impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain an S2 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of S2 is shown in Table I-1. Example I-3 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 30 g of nickel nitrate, 45 g of ammonium metatungstate and 15 g of oxalic acid were measured in 140 g of deionized water, and heated while stirring to dissolve and obtain a clear solution. 200 g of silica carrier was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 450 °C for 4 h, with a gas to reagent ratio of 0.3 L / (g•hr) to obtain a semi-finished Z-S3 catalyst, the total carbon content of which is shown in Table I-1. 10 g of diethylene glycol was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S3 was impregnated with the above solution by saturated impregnation method for 2 hours, and then dried at 120 °C for 6 hours to obtain an S3 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of S3 is shown in Table I-1. Comparative Example I-2 30 g of nickel nitrate, 45 g of ammonium metatungstate and 15 g of oxalic acid were weighed into 140 g of deionized water, and heated while stirring to dissolve and obtain a clear solution. 200 g of silica carrier was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 450 °C for 4 h, with a gas to reagent ratio of 0.3 L / (g•hr) to obtain a D2 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of D2 is shown in Table I-1. Comparative Example I-3 30 g of nickel nitrate, 45 g of ammonium metatungstate and 15 g of oxalic acid and 10 g of ethylene glycol were measured in 140 g of deionized water, and heated while stirring to dissolve and obtain a clear solution. 200 g of silica carrier was impregnated with the above solution by saturated impregnation method for 2 hours, dried at 120 °C for 2 hours to obtain a D3 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of D3 is shown in Table I-1. Example I-4 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate and 20 g of citric acid were measured in 140 g of deionized water, and heated while stirring to dissolve and obtain a clear solution. 200 g of alumina-silica carrier (with a weight ratio of 1:1) was impregnated with the above solution by saturated impregnation method with a gas to reagent ratio of 0.8 L / (g·hr) for 2 h, dried at 450 °C for 3 h to obtain a semi-finished catalyst Z-S4, the total carbon content of which is shown in Table I-1. 15 g of ethylene diamine was added to 150 g of deionized water and stirred to obtain a clear solution. Then, Z-S4 was dried at 120 °C for 3 h to obtain a catalyst S4. The amount of metal element with catalytic hydrogenation activity, based on oxide, based on the total amount of S4 is shown in Table I-1. Example I-5 This example is provided to explain the hydrogenation catalyst and its production process according to this application. A hydrogenation catalyst was prepared in the same manner as in Example I-3 except that, after the active metal portion was impregnated into the carrier, the carrier was calcined at 480 °C for 6 hours. The total carbon content of the semi-finished catalyst is shown in Table I-1. The amount of the hydrogenation active metal element of the catalyst, based on the oxide, based on the total amount of catalyst S5 is shown in Table I-1. Example I-6 This example is provided to explain the hydrogenation catalyst and its production process according to this application. A hydrogenation catalyst was prepared in the same manner as in Example I-2 except that the gas to reagent ratio used during calcination was 1.0 L / (g·hr). In catalyst S6, the amount of metal element with hydrogenation activity in the catalyst, on an oxide basis, based on the total amount of catalyst S6 is shown in Table I-1. Example I-7 This example is provided to explain the hydrogenation catalyst and its production process according to this application. A hydrogenation catalyst was prepared in the same manner as in Example I-2 except that the ratio of the first organic complexing agent to the second organic complexing agent used was changed from 30 g:30 g to 50 g:10 g. In Catalyst S6, the amount of the metal element having catalytic hydrogenation activity, based on the oxide, based on the total amount of Catalyst S7 is shown in Table I-1. Table I-1 Total carbon content in the semi-finished catalyst, wt% MoO3, wt% CoO, wt% NiO, wt% WO3, wt% Example. I-1 0.04 20.0 3.9 - - Comparative example. I-1 0.04 21.4 4.3 - - Example. I-2 0.4 20.1 - 3.9 - Example. I-3 0.1 - - 3.3 15.1 Comparative example. I-2 - - - 3.9 16.5 Comparative example. I-3 - - - 3.1 15.0 Example. I-4 0.08 3.2 - 7.6 20.3 Example. I-5 0.03 - - 3.2 15.3 Example. I-6 0.45 20.0 - 3.7 - Example. I-7 0.5 20.3 - 3.8 - Experimental Example I-1 In this experimental example, the desulfurization activity and denitrogenation activity of the hydrogenation catalyst produced by the process of this application and the hydrogenation catalyst produced in the comparative examples were evaluated by the following method, and the evaluation results are shown in Table I-2. Middle Eastern blended diesel (85% straight-run diesel + 15% catalytic cracked diesel) was used as raw material and the characteristics are as follows: S value 12000 μg / g N value 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 The desulfurization and denitrogenation activities of the catalyst were evaluated on a 30 ml diesel hydrogenation unit. The catalyst was sulfurized before the reaction, and 30 ml of catalyst was loaded. The pre-desulfurization conditions were as follows: 6.4 MPa, 320 °C, 4 h, hydrogen to oil volume ratio of 300:1, and oil feed rate of 8 mL / h. The reaction conditions were as follows: hydrogen partial pressure of 6.4 MPa, reaction temperature of 350 °C, hydrogen to oil volume ratio of 300, and liquid hourly space velocity of 1.5 h-1. The samples were collected after 4 h of reaction, respectively, and the sulfur and nitrogen contents of the raw materials used in the hydrogenation-desulfurization and hydrogenation-denitrogenation reactions and the obtained product were determined by gas chromatography. The hydrogenation desulfurization activity of the catalyst was evaluated relative to the reference factor D (i.e., the catalyst produced in Comparative Example I-2), and the hydrogenation desulfurization reaction was considered to be a 1.65 order reaction. The reaction rate constant k(X)HDS of catalyst X was calculated according to the following equation (1): (1) LHSV in equation (1) represents the liquid space velocity per hour of the hydrocarbon oil used during the hydrotreating reaction. The relative hydrogenation desulfurization activity of catalyst X was calculated according to equation (2) using the hydrogenation desulfurization activity of the catalyst (specified as k(D2)HDS) produced in Comparative Example I-2 as a baseline reference. (2) The hydrogenation desulfurization activity of the catalyst was evaluated relative to the reference agent D (i.e., the catalyst produced in Comparative Example I-2), and the hydrogenation desulfurization reaction was considered as a first-order reaction. The reaction rate constant k(X)HDS of catalyst X was calculated according to the following equation (3): (3) LHSV in equation (3) represents the liquid hourly space velocity of the hydrocarbon oil used during the hydrotreating reaction. The relative hydrogenation desulfurization activity of catalyst X was calculated according to equation (4) using the hydrogenation desulfurization activity of the catalyst (specified as k(D2)HDS) produced in Comparative Example I-2 as a baseline reference. (4) The results of the hydrogen purification evaluation of the hydrogenation catalyst produced in the corresponding examples and comparative examples are shown in Table I-2. Table I-2 Examples Number Relative activity Hydrogenation Desulfurization, % Relative activity Hydrogenation Desulfurization, % 4 hours of reaction 500 hours of reaction 4 hours of reaction 500 hours of reaction Ex. I-1 S1 129 - 114 - Comparative example. I-1 D1 103 - 100 - Ex. I-2 S2 125 - 116 - Ex. I-3 S3 127 120 119 115 Comparative example. I-2 D2 100 - 100 - Comparative example. I-3 D3 111 70 104 81 Ex. I-4 S4 132 - 118 - Ex. I-5 S5 115 - 105 - Ex. I-6 S6 123 - 112 - Ex. I-7 S7 117 - 106 - Note: “-” in Table I-2 indicates that no recovery was performed. The results of Tables I-1 and I-2 show that the catalyst provided by this application significantly improves the desulfurization hydrogenation activity and the desulfurization hydrogenation activity compared with the desulfurization hydrogenation catalyst produced by the previous process. Furthermore, when comparing the data of the relative desulfurization hydrogenation activity and the relative desulfurization hydrogenation activity after 4 hours and 500 hours of reaction shown in Table I-2, it can be seen that the decrease in the activity of the catalyst provided by this application after a long reaction time is very small, and much less than that of the comparative example. Therefore, the catalyst produced by the process of this application shows a very long service life. The above results clearly show that the process provided by this application has advantages that are not matched by other existing processes. Example II-1 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 270g of magnesium nitrate was measured, heated, after adding deionized water, while stirring to dissolve, followed by adding deionized water to 850 ml. 1000g of alumina carrier was impregnated with the resulting solution by saturated impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined at 400 °C for 2 hours to obtain magnesium aluminate Z1 with water absorption of 0.85. 54 g of molybdenum trioxide, 21 g of basic cobalt carbonate, 13 g of phosphoric acid, 30 g of citric acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear impregnated solution. 200 g of magnesium-containing alumina carrier Z1 was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 360 °C for 6 h, with a gas to reagent ratio of 10.0 L / (g·hr) to obtain a semi-finished catalyst Z-S1, the total carbon content of which is shown in Table II-1. 30 g of citric acid was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S1 was impregnated with the above solution by saturated impregnation method for 2 hours, and then dried at 120 °C for 2 hours to obtain a S1 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the S1 value is shown in Table II-1. Comparative Example II-1 The hydrogenation catalyst was prepared in the same manner as Example II-1, except that the hydrogenation catalyst S1 prepared in Example II-1 was calcined at 400 °C for 3 hours to obtain a catalyst D1. The amount of the metal element having hydrogenation activity of the catalyst, based on the oxide, based on the amount of catalyst D1 is shown in Table II-2. Example II-2 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 37g of lanthanum nitrate was measured, heated, after adding deionized water, while stirring to dissolve, followed by adding deionized water to 850 ml. 1000g of alumina carrier was impregnated with the resulting solution by saturated impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined at 500 °C for 4 hours to obtain lanthanum-containing alumina Z2 with a water absorption of 0.85. 30 g of nickel nitrate, 45 g of ammonium metatungstate, 15 g of oxalic acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear solution. 200 g of lanthanum-containing alumina carrier Z2 was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 400 °C for 2 h, with a gas to reagent ratio of 1.0 L / (g·hr) to obtain a semi-finished Z-S2 catalyst with a total carbon content shown in Table II-1. 10 g of diethylene glycol was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S2 was impregnated with the above solution by saturated impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain an S2 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the amount of S2 is shown in Table II-1. Example II-3 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 37g of lanthanum nitrate was measured, heated, after adding deionized water, while stirring to dissolve, followed by adding deionized water to 850 ml. 1000g of alumina carrier was impregnated with the resulting solution by saturated impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined at 500 °C for 4 hours to obtain lanthanum-containing silica Z3 with a water absorption of 0.85. 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate, 20 g of citric acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear solution. 200 g of lanthanum-containing silica carrier Z3 was impregnated with the above solution by saturated impregnation method for 2 h, dried at 180 °C for 2 h, and then calcined under air flow at 430 °C for 3 h, with a gas to reagent ratio of 0.3 L / (g·hr) to obtain a semi-finished Z-S3 catalyst with a total carbon content shown in Table II-1. 10 g of ethylene diamine was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S3 was impregnated with the above solution by saturated impregnation method for 1 hour, and then dried at 150 °C for 3 hours to obtain an S3 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the amount of S3 is shown in Table II-1. Example II-4 This example is provided to explain the hydrogenation catalyst and its production process according to this application. 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 20 g of phosphoric acid, 20 g of citric acid were measured in 140 g of deionized water, and heated while stirring to obtain a clear saturated solution. 200 g of alumina-silica carrier Z2 (with a weight ratio of 1:1) was impregnated with the above solution by saturated impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under air flow at 400 °C for 2 h, with a gas to reagent ratio of 2.0 L / (g·hr) to obtain a semi-finished catalyst Z-S4, the total carbon content of which is shown in Table II-1. 5 g of ethanol was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S4 was impregnated with the above solution by saturated impregnation method for 0.5 h, and then dried at 110 °C for 3 h to obtain an S4 catalyst. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the amount of S4 is shown in Table II-1. Comparative Example II-2 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 20 g of phosphoric acid, 20 g of citric acid, 20 g of zinc nitrate were measured in 140 g of deionized water, and heated while stirring to obtain a clear saturated solution. 200 g of the same carrier as in Example II-4 was impregnated with the above solution by the saturated impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under air flow at 400 °C for 2 hours, with a gas to reagent ratio of 2.0 L / (g·hr) to obtain a D2 catalyst. The amount of the metal element having the hydrogenation activity of the catalyst, based on the oxide, based on the D2 amount is shown in Table II-1. Comparative Example II-3 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 20 g of phosphoric acid, 20 g of citric acid, 20 g of zinc nitrate were measured in 140 g of deionized water, and heated while stirring to obtain a clear saturated solution. 200 g of the same carrier as in Example II-4 was impregnated with the above solution by the saturated impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under air flow at 400 °C for 2 hours, with a gas to reagent ratio of 2.0 L / (g·hr) to obtain a D3 catalyst. The amount of the metal element having the hydrogenation activity of the catalyst, based on the oxide, based on the D3 amount is shown in Table II-1. Example II-5 A hydrogenation catalyst was prepared in the same manner as in Example II-2 except that, after the active metal portion was impregnated into the carrier, the carrier was calcined at 450 °C for 6 hours. The total carbon content of the semi-finished catalyst obtained is shown in Table II-1. In the obtained catalyst S5, the amount of the metal element having hydrogenation activity, based on the oxide, based on the total amount of catalyst S5 is shown in Table II-1. Example II-6 A hydrogenation catalyst was prepared in the same manner as in Example II-1 except that the gas to reagent ratio used during calcination was 1.0 L / (g·hr). The amount of metal element with catalytic hydrogenation activity in the obtained S6 catalyst, based on the oxide, based on the total amount of S6 catalyst is shown in Table II-1. Example II-7 A hydrogenation catalyst was prepared in the same manner as in Example II-1 except that the ratio of the first organic complexing agent to the second organic complexing agent used was changed from 30 g:30 g to 50 g:10 g. In Catalyst S7, the amount of the metal element having catalytic hydrogenation activity, on an oxide basis, based on the total amount of Catalyst S7 is shown in Table II-1. Table II-1 Example. II-1 example. II-2 Example. II-3 example. II-4 example. II-5 example. II-6 example. II-7 MoO3, wt% 20.1 - 3.0 20.0 - 20.0 20.3 CoO, wt% - - - 3.9 - - - NiO, wt% 3.9 2.3 7.8 - 2.4 3.8 4.0 WO3, wt% - 15.3 20.0 - 15.4 - - ZnO, wt% - - - 2.1 - - - MgO, wt% 2.8 - - - - 2.9 2.7 La2O3, wt% - 1.0 1.0 - 1.0 - - Total carbon content of semi-finished catalyst, wt% 0.4 0.05 0.12 0.05 0.01 0.45 0.5 Table II-2 Comparative Example. II-1 Comparative Example. II-2 Comparative Example. II-3 MoO3, wt% 20.6 20.3 20.2 CoO, wt% - 4.1 4.0 NiO, wt% 4.3 - - WO3, wt% - - - ZnO, wt% - 2.35 2.3 MgO, wt% 3.1 - - La2O3, wt% - - - Total amount of carbon in the semi-finished catalyst, wt% 0.4 - - Test Example II-1 In this test example, the defluorination activity and denitrogenation activity of the hydrogenation catalyst produced by the process of the present application and the hydrogenation catalyst produced in the comparative examples were evaluated by the following method, and the evaluation results are shown in Table II-4 below. Middle Eastern blended diesel (85% straight-run diesel + 15% catalytic cracked diesel) was used as raw material, and its specifications are as follows: S content 12000 μg / g N content 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 The desulfurization and denitrogenation activities of the catalyst were evaluated on a 30 mL diesel hydrogenation unit. The catalyst was pre-sulfurized before the reaction, and 30 mL of the catalyst was loaded. The pre-sulfurization conditions were as follows: 6.4 MPa, 320 °C, 4 h, hydrogen-to-oil volume ratio of 300:1, and sulfurized oil feed rate of 8 mL / h. The reaction conditions were as follows: hydrogen partial pressure of 6.4 MPa, reaction temperature of 350 °C, hydrogen-to-oil volume ratio of 300, and liquid hourly space velocity of 1.5 h-1. Samples were collected after 4 h and 500 h of reaction, respectively, and the sulfur and nitrogen contents of the raw materials were used in the hydrodesulfurization, hydrodenitrogenation reaction, and the obtained product was determined by gas chromatography. The hydrodesulfurization activity of the catalyst was evaluated relative to the reference agent D (i.e., the catalyst produced in Comparative Example II-2), and the hydrodesulfurization reaction was considered to be a -1.65 order reaction. The reaction rate constant k(X)HDS of catalyst X was calculated according to equation (1): (1) LHSV in equation (1) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrosulfurization activity of catalyst X was calculated according to equation (2) using the hydrosulfurization activity of catalyst D2 (specified as k(D2)HDS) produced in Comparative Example II-2 as the baseline reference: (2) The hydronitrogenation activity of the catalyst was evaluated relative to the reference agent D (i.e., the catalyst prepared in Comparative Example II-2), and the hydrodenitrogenation reaction was considered as a first-order reaction. The reaction rate constant k(X)HDN of catalyst X was evaluated according to equation (3). (3) LHSV in equation (3) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodehydrogenation activity of catalyst X was calculated according to equation (4) using the hydrodenitrogenation activity of catalyst D2 (denoted as k(D2)HDN) produced in Comparative Example II-2 as a baseline reference. (4) The results of the hydrorefining evaluation of the hydrogenation catalyst produced in the relevant examples and comparative examples are shown in Table II-3. Table II-3 Examples No. Relative hydrodesulfurization activity, % Relative hydrodenitrogenation activity, % 4 h of reaction 500 h of reaction 4 h of reaction 500 h of reaction Example II-1 S1 142 - 124 - Comparative example II-1 D1 104 - 101 - Example II-2 S2 157 154 133 129 Example II-3 S3 153 - 129 - Example II-4 S4 139 130 121 116 Comparative example II-2 D2 100 - 100 - Comparative example II-3 D3 112 75 106 86 Example II-5 S5 110 - 108 - Example II-6 S6 140 - 120 - Example II-7 S7 133 - 112 - Note: “-” in Table II-3 indicates that no test was performed. The results of Tables II-1 to II-3 show that the catalyst produced by the present application exhibits a large improvement in hydrodesulfurization activity and hydrodenitrogenation activity, compared with the hydrogenation catalyst produced by the previous process. In addition, when comparing the data of relative hydrodesulfurization activity and hydrodenitrogenation activity determined after 4 hours of reaction shown in Table II-3, it is observed that the decrease in activity of the catalyst produced by the present application after a long time of reaction is very small, and much smaller than that of the comparative example. Therefore, the catalyst produced by the process of the present application exhibits an extended service life. The above results fully demonstrate that the process produced by the present application has advantages that are not obtained by other processes. Example III-1 This example is provided to illustrate a hydrogenation catalyst and a process for its production in accordance with the present application. 2000 g of aluminum hydroxide powder (dry rubber powder produced by Changling Refining & Chemical Co., Ltd. Catalyst Plant, 71% by weight on a dry basis) and 1039 g of silica sol (commercially available from Qingdao Ocean Chemical Plant, 30% by weight) were uniformly mixed. The final mixture was extruded into a propeller strip having a limited peripheral diameter of 1.4 mm by an extruder, and the extruded wet strip was dried at 120 °C for 4 h, followed by calcination at 600 °C for 3 h to obtain a Z1 carrier. In the Z1 carrier, the silica content was 18.0% by weight and the alumina content was 82.0% by weight. 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 13 g of phosphoric acid, 30 g of citric acid were added to 140 g of deionized water, and heated with stirring until dissolved to obtain a clear aqueous solution. 200 g of carrier Z1 was impregnated with the above solution by the aqueous impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 400 °C for 2 hours, with a gas-to-identifier ratio of 1 L / (g·hr), to obtain a semi-finished catalyst Z-S1, the carbon content of which is shown in Table III-1; 30 g of citric acid was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S1 was impregnated with the above solution by a mixed impregnation method, impregnated for 2 hours, and dried at 150 °C for 3 hours to obtain a catalyst S1. The amount of metal element with hydrogenation activity of the catalyst, based on the oxide, based on the total amount of S1 is shown in Table III-1. Comparative Example III-1 The hydrogenation catalyst was prepared in the same manner as in Example III-1 except that the hydrogenation catalyst S1 prepared in Example III-1 was calcined at 400 °C for 3 hours to obtain a catalyst D1. In catalyst D1, the amount of the metal element having the catalytic hydrogenation activity, based on the oxide, based on the total amount of D1 is shown in Table III-2. Example III-2 This example is provided to illustrate a hydrogenation catalyst and a process for its production in accordance with the present application. 30 g of nickel nitrate, 45 g of ammonium metatungsten, 15 g of oxalic acid and 21 g of ammonium fluoride were added into 140 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of the alumina carrier with the above solution was impregnated by the mixed impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 360 °C for 6 hours, with a gas to reagent ratio of 10.0 L / (g·hr), to obtain a semi-finished Z-S2 catalyst, the total carbon weight of which is shown in Table III-1; 10 g of diethylene glycol was added to 150 g of deionized water, and stirred to obtain a clear solution. Z-S2 was impregnated with the above solution by a mixed impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain catalyst S2. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of S2 is shown in Table III-1. Comparative Example III-2 30 g of nickel nitrate, 45 g of ammonium metatungstate, 15 g of oxalic acid and 21 g of ammonium fluoride were added into 140 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of the ammonia carrier with the above solution was impregnated by a mixed impregnation method, impregnated for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 350 °C for 6 hours, with a gas to indicator ratio of L / (g·hr), to obtain a D2 catalyst. The amount of the metal element having hydrogenation activity of the catalyst, based on the oxide, based on the total amount of D2 is shown in Table III-2. Comparative Example III-3 30 g of nickel nitrate, 45 g of metatungstate, 15 g of oxalic acid, 10 g of diethylene glycol and 21 g of ammonium fluoride were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of the above ammonia carrier was impregnated with the solution by the Eshwa impregnation method for 2 hours, and dried at 120 °C for 2 hours to obtain catalyst D3. The amount of the metal element with hydrogenation activity of the catalyst, based on the oxide, based on the total amount of D3 is shown in Table III-2. Example III-3 This example is provided to illustrate a hydrogenation catalyst and a process for producing it in accordance with the present disclosure. 60 g of ammonium fluoride was weighed, and heated, after adding deionized water, while stirring to dissolve, it was continued by adding deionized water to 850 ml. 1000 g of zirconia carrier was impregnated with the final solution by the mixed impregnation method for 2 h, then dried at 120 °C for 2 h, and calcined at 400 °C for 4 h to obtain fluorine-containing zirconia Z3. 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate and 20 g of citric acid were added to 180 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of fluorine-containing zirconia Z3 with the above solution was impregnated by the mixed impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 450 °C for 3 hours, with a gas-to-reagent ratio of 0.3 L / (g·hr) to obtain a semi-finished Z-S3 catalyst, the total carbon content of which is shown in Table III-1; 15 g of ethylene diamine was added to 150 g of deionized water and stirred to obtain a clear solution. Z-S3 was impregnated with the above solution by the mixed impregnation method for 2 hours, and then dried at 120 °C for 3 hours to obtain catalyst S3. The amount of metal element with hydrogenation activity of the catalyst, based on the oxide, based on the amount of S3 is shown in Table III-1. Example III-4 The hydrogenation catalyst was prepared in a similar manner to Example III-1 except that, after the metal active component was impregnated in the carrier, the final catalyst was calcined at 480 °C for 6 hours. The total carbon content of the semi-finished crystal obtained is shown in Table III-1. In the final crystal S4, the amount of the metal element with catalytic hydrogenation activity, based on the oxide, based on the total amount of S4 is shown in Table III-1. Example III-5 The hydrogenation catalyst was prepared in the same manner as in Example III-2 except that the gas to reagent ratio during calcination was 1.0 L / (g·hr). In the final catalyst S5, the amount of metal element with catalytic hydrogenation activity, based on oxide, based on the total amount of S5 is shown in Table III-1. Example III-6 The hydrogenation catalyst was prepared in the same manner as in Example III-1 except that the ratio of primary organic complexing agent to secondary organic complexing agent used varied from 30 g:30 g to 50 g:10 g. In catalyst S6, the amount of hydrogenation-active metal element, based on oxide, based on the total amount of S6 is shown in Table III-1. Table III-1 Example III-1 Example III-2 Example III-3 Example III-4 Example III-5 Example III-6 MoO3, wt% 20.2 - 3.2 20.0 - 20.1 CoO, wt% 4.0 - - 4.1 - 3.9 NiO, wt% - 3.1 7.9 - 3.0 - WO3, wt% - 15.2 21.0 - 15.5 - F, wt% - 3.3 1.2 - 3.1 - Si, wt% 5.8 - - 5.9 - 6.1 Total carbon content of the semi-finished catalyst, wt% 0.04 0.4 0.1 0.03 0.45 0.5 Table III-2 Comparative Example III-1 Comparative Example III-2 Comparative Example III-3 MoO3, wt% 20.5 - - CoO, wt% 4.7 - - NiO, wt% - 3.5 3.3 WO3, wt% - 15.9 15.8 F, wt% - 3.6 3.4 Si, wt% 6.2 - - Total carbon content of the semi-finished catalyst, wt% 0.04 - - Test Example III-1 In this example, the desulfurization activity and denitrogenation activity of the hydrogenation catalyst produced by the process of the present application and the hydrogenation catalyst produced in the comparative examples are evaluated by the following method, and the evaluation results are shown in Table III-3. Middle Eastern pure diesel (85% straight-run diesel + 15% catalytic cracked diesel) was used as raw material, and its specifications are as follows: S value 12000 μg / g N value 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 The sulfurization and nitrogenization activities of the catalyst were evaluated on a 30 mL diesel hydrogenation unit. The catalyst was pre-sulfurized before the reaction, and 30 mL of the catalyst was loaded. The pre-sulfurization conditions were as follows: 6.4 MPa, 320 °C, 4 h, hydrogen-to-oil volume ratio of 300:1, and sulfurized oil feed rate of 8 mL / h. The reaction conditions were as follows: hydrogen partial pressure of 6.4 MPa, reaction temperature of 350 °C, hydrogen-to-oil volume ratio of 300, and liquid hourly space velocity of 1.5 h-1. Samples were collected after 4 h and 500 h of reaction, respectively, and the sulfur and nitrogen contents of the feedstock used in the hydrodesulfurization, hydrodenitrogenation reaction, and the obtained product were determined by gas chromatography. The hydrodesulfurization activity of the catalyst was evaluated relative to the reference agent D (i.e., the catalyst produced in Comparative Example III-2), and the hydrodesulfurization reaction was considered as a reaction of order -1.65. The reaction rate constant k(X)HDS of catalyst X was calculated according to equation (1): (1) LHSV in equation (1) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodesulfurization activity of catalyst X was calculated according to equation (2) using the hydrodesulfurization activity of catalyst D2 (denoted as k(D2)HDS) produced in Comparative Example III-2 as a baseline reference: (2) The hydrodenitrogenation activity of the catalyst was evaluated relative to the reference agent D (i.e., the catalyst produced in Comparative Example III-2), and the hydrodenitrogenation reaction was considered as a first-order reaction. The reaction rate constant k(X)HDN of catalyst X was calculated according to equation (3): (3) LHSV in equation (3) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The hydrodenitrogenation activity of catalyst X was calculated according to equation (4) using the hydrodenitrogenation activity of catalyst D2 (denoted as k(D2)HDN) produced in Comparative Example III-2 as a baseline reference: (4) The results of hydrorefining evaluation of the hydrogenation catalysts produced in the relevant examples and comparative examples are shown in Table III-3. Table III-3 Examples Number of active ingredients Relative hydrodesulfurization, % Relative hydrodenitrogenation activity, % 4 hours of reaction 500 hours of reaction 4 hours of reaction 500 hours of reaction Example III-1 S1 135 - 126 - Comparative example III-1 D1 92 - 89 - Example III-2 S2 141 134 131 125 Comparative example III-2 D2 100 - 100 - Comparative example III-3 D3 109 74 110 89 Example III-3 S3 137 - 128 - Example III-4 S4 118 - 105 - Example III-5 S5 139 - 128 - Example III-6 S6 130 - 123 - Note: “-” in Table III-3 indicates that no test was performed. The results of Tables III-1 to III-3 show that the catalyst produced by the present application exhibits improved hydrodesulfurization activity and improved hydrodenitrogenation activity when compared with the hydrogenation catalyst produced by the previous process. In addition, when the data of relative hydrodesulfurization activity and relative hydrodenitrogenation activity determined after 4 hours and 500 hours of reaction shown in Table III-3 are compared, it can be seen that the decrease in activity of the catalyst produced by the present application after a long time of reaction is very small, and much smaller than that of the comparative example. Therefore, the catalyst produced by the process of the present application exhibits an extended service life. The above results fully demonstrate that the process provided by the present application has advantages that are not available by other existing methods. Examples IV-1 to IV-7 are used to illustrate hydrogenation catalyst I and a process for producing it in accordance with the present application, and Comparative Example IV-1 is used to illustrate a comparative catalyst and a process for producing it. Example IV-1 54 g of molybdenum trioxide, 21 g of nickel carbonate, 13 g of phosphoric acid, 30 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear saturated solution. 200 g of the ammonia carrier with the above solution was impregnated by the ash impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under a stream of air at a calcination temperature of 360 °C for 6 h, with a gas-to-carrier ratio of 2 L / (g·hr). To obtain the IZ-S1 catalyst precursor, its carbon cycle is shown in Table IV-1; 5 g of ethanol was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S1 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 110 °C for 3 hours to obtain catalyst I-1. The amount of hydrogenation-active metal element, based on oxide, based on the total weight of catalyst I-1 is shown in Table IV-1. Comparative Example IV-1 The hydrogenation catalyst was prepared in a similar manner to Example IV-1 except that the hydrogenation catalyst I-1 prepared in Example IV-1 was calcined at 400 °C for 3 hours to obtain catalyst D1. The amount of hydrogenation-active metal element, on an oxide basis, based on the total weight of catalyst D1 is shown in Table IV-1. Example IV-2 54 g of molybdenum trioxide, 21 g of nickel carbonate, 13 g of phosphoric acid, 30 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear impregnated solution. 200 g of zirconia carrier was impregnated with the above solution by the ash impregnation method for 2 hours, dried at 150 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 360 °C for 3 hours, with a gas to carrier ratio of 10 L / (g·hr), to obtain the catalyst precursor IZ-S2, the total carbon content is shown in Table IV-1; 30 g of citric acid was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S2 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain catalyst I-2. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of I-2 is shown in Table IV-1. Example IV-3 30g of nickel nitrate, 45g of ammonium metatungstate and 15g of oxalic acid were added to 140g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200g of the silica carrier with the above solution was impregnated by the ash impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 450 °C for 4 hours, with a gas-to-carrier ratio of 0.3 L / (g·hr) to obtain the IZ-S3 catalyst precursor, the total carbon content of which is shown in Table IV-1; 10g of diethylene glycol was added to 150g of deionized water, and stirred to form a clear solution. IZ-S3 was calcined with the above solution by the steam impregnation method for 2 hours, and dried at 120 °C for 6 hours to obtain catalyst I-3. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of I-3 is shown in Table IV-1. Example IV-4 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate and 20 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of alumina-silica carrier (in a weight ratio of 1:1) was impregnated with the above solution by the steam impregnation method for 2 h, dried at 120 °C for 2 h, and then calcined under a stream of air at a calcination temperature of 450 °C for 3 h, with a gas-to-carrier ratio of 0.8 L / (g·hr), to obtain the catalyst precursor IZ-S4, the total carbon content of which is shown in Table IV-1; 15 g of ethylene diamine was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S4 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 120 °C for 3 hours to obtain catalyst I-4. The amount of metal element with hydrogenation activity of the catalyst, based on the oxide, based on the total amount of I-4 is shown in Table IV-1. Example IV-5 The hydrogenation catalyst was prepared in a similar manner to Example IV-3 except that, after the metal active component was impregnated on the support, the resulting material was calcined at 480 °C for 6 hours. The total carbon content of the resulting catalyst precursor is shown in Table IV-1. In the resulting catalyst I-5, the amount of the metal element having catalytic hydrogenation activity, based on the oxide, based on the total amount of I-5 is shown in Table IV-1. Example IV-6 The hydrogenation catalyst was prepared in the same manner as in Example IV-2 except that the gas to carrier ratio during calcination was 1.0 L / (g·hr). In the resulting catalyst I-6, the amount of hydrogenation-active metal element, based on oxide, based on the total amount of I-6 is shown in Table IV-1. Example IV-7 The hydrogenation catalyst was prepared in a similar manner to Example IV-2 except that the ratio of primary organic complexing agent to secondary organic complexing agent used varied from 30 g:30 g to 50 g:10 g. In Catalyst I-7, the amount of the metal element having hydrogenation activity of the catalyst, based on the oxide, based on the total amount of I-7 is shown in Table IV-1. Table IV-1 Examples Total amount of carbon in the catalyst precursor, wt% MoO3, wt% CoO, wt% NiO, wt% WO3, wt% P amount, wt% Comparative example IV-1 0.04 21.4 4.3 - - 2.9 Example IV-1 0.04 20.0 3.9 - - 2.8 Example IV-2 0.4 20.1 - 3.9 - 3.0 Example IV-3 0.1 - - 3.3 15.1 - Example IV-4 0.08 3.2 - 7.6 20.3 4.9 Example IV-5 0.03 - - 3.2 15.3 - Example IV-6 0.45 20.0 - 3.7 - 2.8 Example IV-7 0.5 20.3 - 3.8 - 2.9 Examples IV-8 to IV-11 show a process for producing Catalyst II. Example IV-8 Hydrogenation catalyst II-2 was produced as follows: A specific amount of microporous alumina precursor (primary hydrated alumina, an industrial product obtained by the metaaluminate-carbon dioxide method, product name dry boehmite, produced by Shandong Aluminum Factory, containing 80% by weight of boehmite and 5% by weight of gibbsite) was weighed. A specific amount of microporous alumina precursor (secondary hydrated alumina, an industrial product obtained by the sodium metaaluminate-aluminum sulfate method, product name Changling dry rubber powder, produced by Changling Catalyst Refinery, containing 68% by weight of boehmite and 5% by weight of gibbsite) was also weighed. Two types of hydrated alumina were uniformly mixed in a dry weight ratio of 75:25, and an extrusion aid, binder and water were added, and then extruded into three-blade strips with a peripheral circle diameter of 1.4 mm, dried at 120 °C, and calcined at 550-650 °C for 4 h, respectively, to produce hydrogenation catalyst carriers.A certain amount of alumina carriers were weighed in order, impregnated with an aqueous solution of fluoride (chemically pure) for 1 hour, dried at 120 °C, and calcined at 530 °C for 4 hours to obtain fluorine-containing alumina carriers. The fluorine-containing alumina carriers were impregnated with an aqueous solution mixed with ammonium metathesis (chemically pure) and nickel nitrate (chemically pure) for 4 hours, dried at 120 °C, and calcined at 530 °C for 4 hours to obtain hydrogenation catalyst II-1, which contains 4 wt% nickel (based on NiO), 30 wt% tungsten (based on tungsten oxide), 4 wt% fluorine (based on germanium fluoride), with the balance amount of alumina. Example IV-9 Hydrogenation catalyst II-2 was produced as follows: 27.2 g of molybdenum trioxide, 9.1 g of basic cobalt carbonate, 5.5 g of phosphoric acid, and 7.6 g of citric acid were separately introduced into 55 mL of deionized water, heated to 80 °C while stirring to dissolve, producing a clear brown-red solution after about 1 h. The solution was added to a beaker, heated to 90 °C and kept under stirring for 8 h, and water was added to 85 mL to produce a clear saturated solution. 2000 g of aluminum hydroxide powder (dry rubber powder produced by Changling Refining & Chemical Co., Ltd. Catalyst Plant, 71% by weight based on dry weight) and 1039 g of silica sol (product of Qingdao Ocean Chemical Plant, silica content: 30% by weight) were uniformly mixed. The resulting mixture was extruded into a butterfly strip with a peripheral circular diameter of 1.4 mm by an extruder, and the extruded wet strip was dried at 120 °C for 4 hours, followed by calcination at 600 °C for 3 hours to obtain a carrier composed of 18.0 wt% silica and 82.0 wt% aluminum. The water absorption of the carrier was 0.85.100 g of the carrier was impregnated with 85 mL of impregnating solution by the Ashba impregnation method for 2 h. It was dried at 120 °C for 2 h. And further dried at 250 °C for 3 h to obtain a hydrogenation catalyst II-2 containing 3.9 wt% Co (based on CoO), and 20.1 wt% molybdenum (based on MoO3), 2.1 wt% phosphorus (based on P2O5), 5.6 wt% citric acid, with an equilibrium amount of alumina. Example IV-10 Hydrogenation catalyst II-3 was produced as follows: A high-concentration NaAlO2 solution containing 210 g of alumina / L and having an acoustic coefficient of 1.62 was mixed with deionized water to prepare 5 L of a solution with an Al2O3 content of 40 g / L, and then 16.3 g of sodium gluconate was added to obtain a NaAlO2 solution containing sodium gluconate. The solution was then transferred to a gelation reactor with a total volume of 8 L and a height-diameter ratio of 8, equipped with a CO2 gas distributor at the bottom. The solution temperature was controlled at 25±5°C, and a CO2 gas with a volume concentration of 90% was introduced from the bottom of the reactor to drive the gelation reaction. The gelation temperature was controlled at 20–40 °C, and the CO2 gas flow rate was set to 15±2 L / min. The pH reached 8.0-8.5 in 4-6 minutes at the end of the reaction, at which time the reaction was stopped, and the gelation reaction was completed. The resulting slurry was heated to 70 °C and held for 4 hours, and then filtered using a vacuum filter. After filtration, the filter cake was washed with 20 liters of deionized water (at 70 °C) for about 30 minutes. The washed filter cake was added to 1.5 liters of deionized water and stirred to form a slurry.The slurry was pumped into a spray dryer and dried to obtain hydrated alumina P1-2. 300 g of pseudo-uomeite P1-2 and 700 g of pseudo-boehmite P2-3 (SD pseudo-boehmite powder produced by Shandong Aluminum Co., Ltd.) were mixed and extruded into cloverleaf strips with a peripheral diameter of 1.6 mm by an extruder, and dried at 120 °C for 8 h. 300 g of the resulting material was taken and subjected to air flow at 800 °C for 4 h to obtain a carrier, with an air flow rate of 1.5 normal cubic meters / kg·hr. 100 g of the carrier was weighed and impregnated with 85 ml of an aqueous solution containing 20.6 g of nickel nitrate, 34.8 g of ammonium paramolybdate and 11.4 g of phosphoric acid for 1.5 h, dried at 120 °C for 5 h, cured at 380 °C for 4 h, and then impregnated with 55 ml of an aqueous solution containing 8.4 g of glycerol for 2 h, and dried at 140 °C for 5 h to obtain hydrogenation catalyst II-3 containing 3.5 wt% nickel (based on NiO), 19.1 wt% molybdenum (based on MoO3), 4.8 wt% phosphorus (based on P2O5), 5.7% organic additives, with a balanced amount of alumina. Example IV-11 Hydrogenation catalyst II-4 was produced as follows: 2000g of aluminum hydroxide powder (dry rubber powder produced by Changling Branch Catalyst Factory, 70% by weight on a dry basis) and 299g of silica sol containing 25% silica (Qingdao Ocean Chemical Plant) were weighed, and extruded into a butterfly strip with a peripheral diameter of 1.3 mm, and the wet strip was dried at 120 °C for 4 h and calcined at 600 °C for 3 h to obtain a carrier containing 5.0% by weight of silica. 200 g of the carrier was weighed, and the carrier was impregnated with 176 ml of an aqueous solution containing 16.9 g of ammonium fluoride for 2 h, dried at 120 °C for 3 h, and calcined at 420 °C for 3 h to obtain a fluorine-containing silica-alumina carrier. The carrier was impregnated with 170 ml of an aqueous solution containing 23.0 g of ammonium paramolybdate for 3 h, dried at 120 °C for 4 h, and further dried at 170 °C for 4 h to obtain a molybdenum-containing carrier. Then, the carrier was impregnated with 162 ml of an aqueous solution containing 53.2 g of nickel nitrate, 140.7 g of ammonium metatungstate, and 18.1 g of phosphoric acid was impregnated for 3 h, dried at 200 °C for 4 h, and impregnated with 121 ml of an aqueous solution containing 77.3 g of ethylene glycol, and dried at 120 °C for 6 h, to obtain a hydrogenation catalyst II-4 containing 3.6 wt% nickel (based on NiO), 5.0 wt% molybdenum (based on MoO3), and 32.5 wt% tungsten (based on tungsten oxide), 2.2 wt% fluorine (based on germanium fluoride), 3.0 wt% phosphorus (based on P2O5), 5.0 wt% ethylene glycol, with an alumina-silica balance. Example IV-12 to Example IV-18 In Examples IV-12 to IV-18, the desulfurization activity and denitrification activity of the hydrogenation catalyst produced by the process according to the present application and the hydrogenation catalyst produced in the comparative examples were subjected to hydrorefining evaluation in accordance with the following method. Calculations were made in accordance with the calculation method for the results of hydrorefining evaluation, and the results are shown in Table IV-2 below. Middle Eastern straight-run diesel fraction mixed with 15% catalytic diesel was used as raw materials, and their characteristics are shown in Table IV-3. The desulfurization and denitrification activities of the catalyst were evaluated on a 30 mL diesel hydrogenation unit. The catalyst was pre-sulfurized before the reaction, and 30 mL of the catalyst was loaded. The crude oil inlet was placed at the top of the hydrogenation unit, hydrogenation catalyst II was placed in the upper bed of the reactor, and hydrogenation catalyst I (or D1) was loaded in the lower bed of the hydrogenation reactor, i.e. downstream of hydrogenation catalyst II. The pre-sulfurization conditions were as follows: hydrogen partial pressure 6.4 MPa, reaction temperature 350 °C, hydrogen to oil volume ratio 300, and liquid hourly space velocity 1.5 h-1. Samples were collected after 4 h and 500 h of reaction, respectively, and the sulfur and nitrogen contents of the raw materials and final products were determined by gas chromatography. Comparative Example IV-2 to Comparative Example IV-4 Catalyst D1, catalyst D1+II-1 combination and catalyst II-1 were subjected to hydrorefining evaluation according to the process described in Examples IV-12 to IV-18, and the results were calculated according to the calculation method for hydrorefining evaluation results, and the results are shown in Table IV-2. Calculation method for hydrorefining evaluation results: The hydrodesulfurization activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example IV-1), and the hydrodesulfurization reaction was considered to be a 1.65-order reaction. The reaction rate value k(X)HDS of catalyst X was calculated according to equation (1): (1) LHSV in equation (1) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodesulfurization activity of catalyst X was calculated according to equation (2) using the hydrodesulfurization activity of catalyst D1 (denoted as k(D1)HDS) produced in Comparative Example IV-1 as a baseline reference: (2) The hydrodenitrogenation activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example IV-1), and the hydrodenitrogenation reaction was considered as a first-order equation. The reaction rate constant k(X)HDN of catalyst X was evaluated according to equation (3): (3) LHSV in equation (3) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodenitrogenation activity of catalyst X was calculated according to equation (4) using the hydrodenitrogenation activity of catalyst D1 (denoted as k(D1)HDN) produced in Comparative Example IV-1 as a baseline reference: (4) The results of Table IV-2 show that the hydrogenation catalyst compositions according to the present application show relative hydrodesulfurization activity and relative hydrodenitrogenation activity, the reduction rate per unit time of relative activity is small, and the service life is long. Table IV-2 Examples Catalyst composition Catalyst ratio I / vol% Relative hydrodesulfurization activity, % Relative hydrodenitrogenation activity, % 4 h of reaction 500 h of reaction 4 h of reaction 500 h of reaction Comparative example IV-2 D1 100 76 100 85 Comparative example IV-3 D1+II-1 20(D1) 106 81 107 89 Comparative example IV-4 II-1 104 - 109 - Example IV-12 I-1+II-1 20 130 124 120 114 Example IV-13 I-2+II-2 30 134 - 118 - Example IV-14 I-3+II-2 40 138 131 125 120 Example IV-15 I-4+II-3 50 143 - 124 - Example IV-16 I-5+II-3 60 127 - 110 - Example IV-17 I-6+II-4 70 131 - 120 - Example IV-18 I-7+II-4 80 129 - 113 - Note: “-” in Table IV-2 indicates that no diagnosis was made. Table IV-3 S value 12000 μg / g N value 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 Example V-1 This example is provided to illustrate hydrogenation catalyst I and its production process according to the present application. 270 g of magnesium nitrate was weighed, and heated, after adding deionized water, while stirring to dissolve, then deionized water was added to 850 ml. 1000 g of alumina carrier was impregnated with the solution obtained by the steam impregnation method for 2 hours, then impregnated at 120 °C for 2 hours, and calcined at 400 °C for 4 hours to obtain I-Z1 magnesium-containing alumina with a water absorption of 0.85. 54 g of molybdenum trioxide, 21 g of basic nickel carbonate, 13 g of phosphoric acid, 30 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear impregnation solution. 200 g of magnesium-containing alumina carrier I-Z1 was impregnated with the above solution by the ash impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 360 °C for 6 hours, with a gas to carrier ratio of 10.0 L / (g·hr), to obtain a semi-finished catalyst IZ-S1, the total carbon content of which is shown in Table V-1; 30 g of citric acid was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S1 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 200 °C for 2 hours to obtain catalyst I-1. The amount of the hydrogenation-active metal element and the co-reactive metal element, based on the oxide, based on the total weight of catalyst I-1 is shown in Table V-1. Comparative Example V-1 The hydrogenation catalyst was prepared in a similar manner to Example V-1 except that the hydrogenation catalyst prepared in Example V-1 was calcined at 400 °C for 4 hours to obtain Catalyst D1. The amount of hydrogenation-active metal element and co-reactive metal element, based on oxide, based on the total weight of Catalyst D1 is shown in Table V-1. Example V-2 This example is provided to illustrate the hydrogenation catalyst and its production process according to the present application. 37 g of lanthanum nitrate was weighed, and heated, after adding deionized water, while stirring to dissolve, it was continued by adding deionized water to 850 ml. 1000 g of alumina carrier was impregnated with the resulting solution by the Ashba impregnation method for 2 hours, then dried at 100 °C for 2 hours, and calcined at 500 °C for 4 hours to obtain lanthanum-containing alumina I-Z2 with a water absorption of 0.85. 30 g of nickel nitrate, 45 g of ammonium metatungstate, 15 g of oxalic acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of lanthanum-containing alumina carrier I-Z2 was impregnated with the above solution by the steam impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 400 °C for 2 hours, with a gas to carrier ratio of 1.0 L / (g·hour), to obtain a semi-finished catalyst IZ-S2, the total carbon content of which is shown in Table V-1; 10 g of diethylene glycol was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S2 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain catalyst I-2. The amount of hydrogenation-active metal element and co-reactive metal element, based on oxide, based on the total weight of catalyst I-2 is shown in Table V-1. Example V-3 This example is provided to illustrate the hydrogenation catalyst and its production process according to the present application. 37 g of lanthanum nitrate was weighed, heated, and after adding deionized water, while stirring until dissolved, it was continued by adding deionized water to 850 ml. 1000 g of silica carrier was impregnated with the resulting solution by the Ashba impregnation method for 2 hours, then dried at 100 °C for 2 hours, and calcined at 500 °C for 4 hours to obtain lanthanum-containing silica I-Z3 with a water absorption of 0.85. 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate, 20 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve until a clear solution was obtained. 200 g of lanthanum-containing silica carrier I-Z3 was impregnated with the above solution by the steam impregnation method for 2 hours, dried at 180 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 430 °C for 3 hours, with a gas to carrier ratio of L / (g·hr), to obtain a semi-finished catalyst IZ-S3, the total carbon content is shown in Table V-1; 15 g of ethylene diamine was added to 150 g of deionized water and stirred to obtain a clear solution. IZ-S3 was impregnated with the above solution by the Eschbach impregnation method for 1 hour, and then dried at 120 °C for 3 hours to obtain catalyst I-3. The amount of the hydrogenation-active metal element and the co-reactive metal element, based on the oxide, based on the total weight of catalyst I-3 is shown in Table V-1. Example V-4 This example is provided to illustrate the hydrogenation catalyst and its production process according to the present application. 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 20 g of phosphoric acid, 20 g of citric acid, 20 g of zinc nitrate were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear impregnation solution. 200 g of alumina-silica carrier (in an alumina to silica ratio of 1:1) was impregnated with the above solution by the steam impregnation method for 2 hours, and dried at 120 °C for 2 hours, then continued under a stream of air at a calcination temperature of 400 °C for 2 hours, with a gas to carrier ratio of 2.0 L / (g·hr), to obtain a semi-finished catalyst IZ-S4, the total carbon content of which is shown in Table V-1; 5 g of ethanol was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S4 was impregnated with the above solution by the steam impregnation method for 0.5 h, and then dried at 110 °C for 3 h to obtain catalyst I-4. The amount of metal element containing hydrogenase activity and co-reactive metal element, based on oxide, based on the total weight of catalyst I-4 is shown in Table V-1. Example V-5 A hydrogenation catalyst was prepared similar to Example V-2 except that, after the metal active component was impregnated with the carrier, the carrier was calcined at 450 °C for 6 hours. The total carbon content of the resulting semi-finished catalyst is shown in Table V-1. In the resulting catalyst I-5, the content of the hydrogenation-active metal element and the co-reactive metal element, based on the oxide, based on the total weight of the catalyst I-5 is shown in Table V-1. Example V-6 A hydrogenation catalyst was prepared similar to Example V-1 except that the gas to carrier ratio used during calcination was 1.0 L / (g·hr). In the resulting catalyst I-6, the amount of hydrogenation-active metal element and co-reactive metal element, based on oxide, based on the total weight of catalyst I-6 is shown in Table V-1. Example V-7 A hydrogenation catalyst similar to Example V-1 was produced except that the ratio of primary organic complexing agent to secondary organic complexing agent was changed from 30 g and 30 g to 50 g and 10 g, respectively. In the resulting catalyst I-7, the amount of hydrogenation-active metal element and co-reactive metal element, based on oxide, based on the total weight of catalyst I-7 is shown in Table V-1. Examples V-8 to V-11 illustrate the process for producing hydrogenation catalyst II. V-8 example Hydrogenation catalyst II-1 was produced as follows: A certain amount of microporous alumina precursor (primary hydrated alumina, industrial product obtained by sodium metaaluminate-carbon dioxide method, product name dry boehmite, produced by Shandong Aluminum Factory, containing 80% by weight of boehmite and 5% by weight of gibbsite) was weighed. A certain amount of microporous alumina precursor (secondary hydrated alumina, industrial product obtained by sodium metaaluminate-aluminum sulfate method, product name Changling dry rubber powder, produced by Catalyst Plant of Changling Refinery, containing 68% by weight of boehmite and 5% by weight of gibbsite) was also weighed. Two types of hydrated alumina were uniformly mixed in a dry weight ratio of 75:25, and extrusion aid, binder and water were added, and then extruded into a three-piece strip with a peripheral diameter of 1.4 mm, dried at 120 °C, and calcined at 550-650 °C for 4 h, respectively, to produce hydrogenation catalyst carriers.A certain amount of alumina carriers was weighed, impregnated with an aqueous solution of ammonium fluoride (chemically pure) for 1 hour, dried at 120 °C, and calcined at 530 °C for 4 hours to obtain fluorine-containing alumina carriers. The fluorine-containing alumina carriers were impregnated with an aqueous solution mixed with ammonium metatungstate (chemically pure) and nickel nitrate (chemically pure) for 4 hours at 120 °C, and calcined at 530 °C for 4 hours to obtain hydrogenation catalyst II-1, which contained 4 wt% nickel (based on NiO), 30 wt% tungsten (based on tungsten oxide), 4 wt% fluorine (based on germanium fluoride), which was the equilibrium amount of alumina. Example V-9 Hydrogenation catalyst II-2 was produced as follows: 27.2 g of molybdenum trioxide, 9.1 g of basic cobalt carbonate, 5.5 g of phosphoric acid, and 7.6 g of citric acid were added to 55 mL of deionized water, heated to 80 °C while stirring to dissolve, to produce a clear brown-red solution after 1 h. The solution was added to the beaker, heated to 90 °C and kept under stirring for 8 h, and water was added to 85 mL to obtain a clear impregnation solution. 2000 g of aluminum hydroxide powder (dry rubber powder produced by Catalyst Plant of Changling Refining & Chemical Co., Ltd., 71% by weight on a dry basis) and 1039 g of silica sol (produced by Qingdao Ocean Chemical Plant, silica content: 30% by weight) were mixed uniformly. The resulting mixture was extruded into a propeller strip with a peripheral diameter of 1.4 mm by an extruder, and the extruded wet strip was dried at 120 °C for 4 hours, then calcined at 600 °C for 3 hours to obtain a carrier composed of 18.0 wt% silica and 82.0 wt% alumina. The water absorption of the carrier was 0.85.100 g of the carrier was impregnated with 85 mL of the chelate impregnation solution by the Ashba impregnation method for 2 h, dried at 120 °C for 2 h, and further dried at 250 °C for 3 h to obtain a hydrogenation catalyst II-2 containing 3.9 wt% Co (based on CoO), 20.1 wt% molybdenum (based on MoO3), 2.1 wt% phosphorus (based on P2O5), 5.6% citric acid, with an equilibrium amount of alumina. Example V-10 Hydrogenation catalyst II-3 was produced as follows: A high-concentration NaAlO2 solution containing 210 g of alumina / L and having an acoustic coefficient of 1.62 was mixed with deionized water to prepare 5 L of a solution containing Al2O3 with a concentration of 40 g / L, and then 16.3 g of sodium gluconate was added to obtain a NaAlO2 solution containing sodium gluconate. The solution was then transferred to a gelation reactor with a total volume of 8 L and a height-to-diameter ratio of 8, equipped with a CO2 gas distributor at the bottom. The solution temperature was controlled at 25±5°C, and CO2 gas with a concentration of 90% by volume was introduced from the bottom of the reactor to drive the gelation reaction. The gelation temperature was controlled at 20–40 °C, and the CO2 gas flow rate was adjusted to 15±2 L / min. The pH reached 8.0-8.5 within 4-6 minutes at the end of the reaction, at which time, aeration was stopped, and the gelation reaction was stopped. The resulting slurry was heated to 70 °C and aged for 4 hours, and then filtered using a vacuum filter. After filtration, the filter cake was washed with 20 liters of deionized water (at 70 °C) for 30 minutes. The washed cake was added to 1.5 liters of deionized water and stirred to form a slurry.The slurry was poured into a spray dryer and dried to obtain hydrated alumina P1-2. 300 g of pseudo-boehmite P1-2 and 700 g of pseudo-boehmite P2-3 (commercial pseudo-boehmite SD powder produced by Shandong Aluminum Co., Ltd.) were mixed and extruded into a cloverleaf strip with a peripheral diameter of 1.6 mm by an extruder, and dried at 120 °C for 8 h. 300 g of the resulting material was taken out and calcined at 800 °C for 4 h under an air stream to obtain the carrier, with an air flow rate of 1.5 normal cubic meters / kg·hr. 100 g of carrier was weighed and impregnated with 85 mL of an aqueous solution containing 20.6 g of nickel nitrate, 34.8 g of ammonium paramolybdate, and 11.4 g of phosphoric acid for 1.5 h, dried at 120 °C for 5 h, cured at 380 °C for 4 h, and then impregnated with 55 mL of an aqueous solution containing 8.4 g of glycerol for 2 h, and dried at 140 °C for 5 h to obtain hydrogenation catalyst II-3 containing 3.5 wt% nickel (based on NiO), 19.1 wt% molybdenum (based on MoO3), 4.8 wt% phosphorus (based on P2O5), 5.7% organic additive, with a balanced amount of alumina. Example V-11 Hydrogenation catalyst II-2 was prepared as follows: 2000g of aluminum hydroxide powder (dried rubber powder produced by Catalyst Plant of Changling Branch, 70% by weight on a dry basis) and 299g of silica sol containing 25% silica (Qingdao Ocean Chemical Plant) were weighed, and extruded into a impeller strip with a peripheral diameter of 1.3 mm, and the wet strip was dried at 120 °C for 4 hours and calcined at 600 °C for 3 hours to obtain a fused carrier of 5.0% by weight of silica. 200g of the carrier was weighed, and the carrier was impregnated with 176 mL of an aqueous solution containing 16.9 g of ammonium fluoride for 2 hours, and dried at 120 °C for 3 hours, and calcined at 420 °C for 3 hours to obtain a fluorine-containing silica-alumina carrier. The carrier was impregnated with 170 mL of an aqueous solution containing 23.0 g of ammonium paramolybdate for 3 h, dried at 120 °C for 4 h, and further dried at 170 °C for 4 h to obtain a molybdenum-containing carrier. Then, the carrier was impregnated with 162 mL of an aqueous solution containing 53.2 g of nickel nitrate, 140.7 g of ammonium metatungstate, and 18.1 g of phosphoric acid was impregnated for 3 h, dried at 200 °C for 4 h, and then impregnated with 121 g of an aqueous solution containing 77.3 g of ethylene glycol, and dried at 120 °C for 6 h, to obtain a hydrogenation catalyst II-4 containing 3.6 wt% nickel (based on NiO), 5.0 wt% molybdenum (based on MoO3), and 32.5 wt% tungsten (based on tungsten oxide), 2.2 wt% fluorine (based on germanium fluoride), 3.0 wt% phosphorus (based on P2O5), 5.0 wt% ethylene glycol, with an alumina-silica balance. Example V-12 to Example V-18 In Examples V-12 to V-18, the desulfurization activity and denitrification activity of the hydrogenation catalyst produced by the process according to the present application and the hydrogenation catalyst prepared in the comparative examples were subjected to hydrorefining evaluation in accordance with the following method. Calculations were made in accordance with the calculation method for hydrorefining evaluation results, and the results are shown in Table V-2. The Middle East straight-run diesel fraction was mixed with 15% catalytic diesel used as raw material, and its characteristics are shown in Table V-3. The desulfurization and denitrification activities of the catalyst were evaluated in a 30 ml diesel hydrogenation unit, and 30 ml of the catalyst was loaded. The inlet for the feed oil was placed at the top of the hydrogenation unit, and the hydrogenation catalyst II was placed in the upper bed of the reactor, the hydrogenation catalyst I (or D1) was loaded in the lower bed of the hydrogenation reactor, that is, downstream of the hydrogenation catalyst II. The catalyst was pre-sulfurized before the reaction. The sulfurization conditions were as follows: hydrogen partial pressure 6.4 MPa, temperature 320 °C, liquid hourly space velocity 4 h-1, hydrogen to oil volumetric ratio 300, and sulfurized oil feed rate 8 mL / h. The reaction conditions were as follows: hydrogen partial pressure of 4 MPa, reaction temperature of 350 °C, hydrogen to oil volume ratio of 300, and liquid hourly space velocity of 1.5 h-1.Samples were collected after 4 h and 500 h of reaction, respectively, and the sulfur and nitrogen contents of the raw material and final product were determined by gas chromatography. Comparative Example V-2 to Comparative Example V-4 Catalyst D1, Catalyst D1+II-1 combination and Catalyst II-1 were subjected to hydrorefining evaluation according to the process described in Example V-12 to Example V-18, and the results were calculated according to the calculation method for hydrorefining evaluation results, and the results are shown in Table V-2 below. Method for calculating hydrorefining evaluation results: The hydrodesulfurization activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example V-1), and the hydrodesulfurization reaction was considered to be a 1.65-order reaction. The reaction rate constant k(X)HDS of catalyst X was calculated according to equation (1): (1) LHSV in equation (1) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodesulfurization activity of catalyst X was calculated according to equation (2) using the hydrodesulfurization activity of catalyst D1 (denoted as k(D1)HDS) produced in Comparative Example V-1 as a baseline reference: (2) The hydrodenitrogenation activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example V-1), and the hydrodenitrogenation reaction was considered as a first-order equation. The reaction rate constant k(X)HDN of catalyst X was calculated according to equation (3): (3) LHSV in equation (3) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodenitrogenation activity of catalyst X was calculated according to equation (4) using the hydrodenitrogenation activity of catalyst D1 (denoted as k(D1)HDN) produced in Comparative Example V-1 as a baseline reference: (4) The results of Table V-2 show that the hydrogenation catalyst composition according to the present application has better relative hydrodesulfurization activity and relative hydrodenitrogenation activity, the reduction rate per unit time of relative activity is small, and the service life is longer. Table V-1 Item Comparative Example V-1 Example V-1 Example V-2 Example V-3 Example V-4 Example V-5 Example V-6 Example V-7 MoO3, wt% 20.6 20.1 - 3.0 20.0 - 20.0 20.3 CoO, wt% - - - - 3.9 - - - NiO, wt% 4.3 3.9 2.3 7.8 - 2.4 3.8 4.0 WO3, wt% - - 15.3 20.0 - 15.4 - - ZnO, wt% - - - - 2.1 - - - MgO, wt% 3.1 2.8 - - - - 2.9 2.7 La2O3, wt% - - 1.0 1.0 - 1.0 - - Total carbon content of semi-finished catalyst, wt% 0.4 0.4 0.05 0.12 0.05 0.01 0.45 0.5 Table V-2 Examples Catalyst composition Catalyst ratio I / vol% Relative hydrodesulfurization activity, % Relative hydrodenitrogenation activity, % 4 h reaction 500 h reaction 4 h reaction 500 h reaction Comparative example V-2 D1 100(D1) 100 76 100 87 Comparative example V-3 D1+II-1 20(D1) 105 80 105 90 Comparative example V-4 II-1 0 104 - 107 - Example V-12 I-1+ II-1 20 147 137 126 117 Example V-13 I-2+ II-2 30 169 162 138 132 Example V-14 I-3+ II-2 40 161 - 134 - Example V-15 I-4+ II-3 50 150 144 130 125 Example V-16 I-5+ II-3 60 123 - 114 - Example V-17 I-6+ II-4 70 152 - 126 - Example V-18 I-7+ II-4 80 144 - 120 - Note: “-” in Table V-2 indicates that no diagnosis was made. Table V-3 S value 12000 μg / g N value 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 Example VI-1 This example is provided to illustrate hydrogenation catalyst I and its production process in accordance with the present application. 2000 g of aluminum hydroxide powder (dry rubber powder produced by Catalyst Plant of Changling Refining & Chemical Co., Ltd., 71% by weight on a dry basis) and 1039 g of silica sol (product of Qingdao Ocean Chemical Plant, silica content: 30% by weight) were uniformly mixed. The resulting mixture was extruded into a propeller strip with a peripheral diameter of 1.4 mm by an extruder, and the extruded wet strip was dried at 120 °C for 4 hours, then calcined at 600 °C for 3 hours to obtain carrier I-Z1. Carrier I-Z1 contains 18.0% by weight of silica and 82.0% by weight of alumina. 54 g of molybdenum trioxide, 19 g of basic cobalt carbonate, 13 g of phosphoric acid, 30 g of citric acid were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a clear impregnation solution. 200 g of the I-Z1 carrier with the above solution was impregnated by the vapor impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 400 °C for 2 hours, with a gas to reagent ratio of 1 L / (g·hr), to obtain a semi-finished IZ-S1 catalyst, the total carbon content is shown in Table VI-1; 30 g of citric acid was added to 150 g of deionized water, stirred to obtain a clear solution. IZ-S1 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain catalyst I-1. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of catalyst I-1 is shown in Table VI-1. Comparative Example VI-1 The hydrogenation catalyst was prepared in the same manner as in Example VI-1 except that the hydrogenation catalyst I-1 prepared in Example VI-1 was calcined at 400 °C for 3 hours to obtain catalyst D1. The amount of hydrogenation-active metal element, based on oxide, based on the total amount of catalyst D1 is shown in Table VI-1. Example VI-2 This example is provided to illustrate hydrogenation catalyst I and its production process in accordance with the present application. 30 g of nickel nitrate, 45 g of ammonium metatungstate, 15 g of oxalic acid and 21 g of ammonium fluoride were added to 140 g of deionized water, and heated while stirring to dissolve to obtain a Scheffle solution. 200 g of the ammonia carrier with the above solution was impregnated by the Ashba impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 360 °C for 6 hours, with a gas to reagent ratio of 10.0 L / (g·hr), to obtain a semi-finished IZ-S2 catalyst, the total carbon content is shown in Table VI-1; 10 g of diethylene glycol was added to 150 g of deionized water, and stirred to obtain a clear solution. IZ-S2 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 150 °C for 3 hours to obtain catalyst I-2. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of catalyst I-2 is shown in Table VI-1. Example VI-3 This example is provided to illustrate hydrogenation catalyst I and its production process in accordance with the present application. 60 g of ammonium fluoride was weighed, and heated, after adding deionized water, while stirring to dissolve, it was continued by adding deionized water to 850 ml. 1000 g of zirconia carrier was impregnated with the resulting solution by the Ashba impregnation method for 2 hours, then dried at 120 °C for 2 hours, and calcined at 400 °C for 4 hours to obtain a fluorine-containing zirconia carrier I-Z3. 83 g of nickel nitrate, 60 g of ammonium metatungstate, 10 g of ammonium molybdate, 20 g of ammonium dihydrogen phosphate and 20 g of citric acid were added to 180 g of deionized water, and heated while stirring to dissolve to obtain a clear solution. 200 g of fluorine-containing zirconia carrier I-Z3 was impregnated with the above solution by the steam impregnation method for 2 hours, dried at 120 °C for 2 hours, and then calcined under a stream of air at a calcination temperature of 450 °C for 3 hours, with a gas-to-detector ratio of 0.3 L / (g·hr), to obtain the semi-finished catalyst IZ-S3, the total carbon content is shown in Table VI-1; 15 g of ethylene diamine was added to 150 g of deionized water and stirred to obtain a clear solution. IZ-S3 was impregnated with the above solution by the steam impregnation method for 2 hours, and then dried at 120 °C for 3 hours to obtain catalyst I-3. The amount of metal element with hydrogenation activity of the catalyst, based on oxide, based on the total amount of catalyst I-3 is shown in Table VI-1. Example VI-4 Hydrogenation catalyst I was prepared in a similar manner to Example VI-1 except that, after the metal active component was impregnated with the carrier, the carrier was impregnated at 480 °C for 6 hours. The total carbon content of the semi-finished catalyst obtained is shown in Table VI-1. In the resulting catalyst I-4, the amount of the metal element having catalytic hydrogenation activity, based on the oxide, based on the total amount of catalyst I-4 is shown in Table VI-1. Example VI-5 Hydrogenation catalyst I was prepared in a similar manner to Example VI-2 except that the gas to reagent ratio used during calcination was 1.0 L / (g·hr). In the resulting catalyst I-5, the amount of metal element having catalytic hydrogenation activity, based on oxide, based on the total amount of catalyst I-5 is shown in Table VI-1. Example VI-6 A hydrogenation catalyst similar to Example VI-1 was produced except that the ratio of primary organic complexing agent to secondary organic complexing agent was changed from 30 g:30 g to 50 g:10 g. In the resulting catalyst I-6, the amount of metal element having catalytic hydrogenation activity, based on oxide, based on the total amount of catalyst I-6 is shown in Table VI-1. Examples VI-7 to VI-10 show the process for producing Catalyst II. Example VI-7 Hydrogenation catalyst II-1 was produced as follows: A specific amount of microporous alumina precursor (primary hydrated alumina, an industrial product obtained by the metaaluminate-carbon dioxide method, product name dry boehmite, produced by Shandong Aluminum Factory, containing 80% by weight of boehmite and 5% by weight of gibbsite) was weighed. A specific amount of microporous alumina precursor (secondary hydrated alumina, an industrial product obtained by the sodium metaaluminate-aluminum sulfate method, product name Changling dry rubber powder, produced by Changling Catalyst Refinery, containing 68% by weight of boehmite and 5% by weight of gibbsite) was also weighed. Two types of hydrated alumina were uniformly mixed in a dry weight ratio of 75:25, and an extrusion aid, binder and water were added, and then extruded into three-blade strips with a peripheral circle diameter of 1.4 mm, dried at 120 °C, and calcined at 550-650 °C for 4 h, respectively, to produce hydrogenation catalyst carriers.A certain amount of alumina carriers were weighed in order, impregnated with an aqueous solution of fluoride (chemically pure) for 1 hour, dried at 120 °C, and calcined at 530 °C for 4 hours to obtain fluorine-containing alumina carriers. The fluorine-containing alumina carriers were impregnated with an aqueous solution mixed with ammonium metathesis (chemically pure) and nickel nitrate (chemically pure) for 4 hours, dried at 120 °C, and calcined at 530 °C for 4 hours to obtain hydrogenation catalyst II-1, which contains 4 wt% nickel (based on NiO), 30 wt% tungsten (based on tungsten oxide), 4 wt% fluorine (based on germanium fluoride), with the balance amount of alumina. Example VI-8 Hydrogenation catalyst II-2 was produced as follows: 27.2 g of molybdenum trioxide, 9.1 g of basic cobalt carbonate, 5.5 g of phosphoric acid, and 7.6 g of citric acid were separately introduced into 55 mL of deionized water, heated to 80 °C while stirring to dissolve, producing a clear brown-red solution after about 1 h. The solution was added to a beaker, heated to 90 °C and kept under stirring for 8 h, and water was added to 85 mL to produce a clear saturated solution. 2000 g of aluminum hydroxide powder (dry rubber powder produced by Changling Refining & Chemical Co., Ltd. Catalyst Plant, 71% by weight based on dry weight) and 1039 g of silica sol (product of Qingdao Ocean Chemical Plant, silica content: 30% by weight) were uniformly mixed. The resulting mixture was extruded into a butterfly strip with a peripheral circular diameter of 1.4 mm by an extruder, and the extruded wet strip was dried at 120 °C for 4 hours, followed by calcination at 600 °C for 3 hours to obtain a carrier composed of 18.0 wt% silica and 82.0 wt% aluminum. The water absorption of the carrier was 0.85.100 g of the carrier was impregnated with 85 mL of impregnating solution by the Ashba impregnation method for 2 h. It was dried at 120 °C for 2 h. And further dried at 250 °C for 3 h to obtain a hydrogenation catalyst II-2 containing 3.9 wt% Co (based on CoO), and 20.1 wt% molybdenum (based on MoO3), 2.1 wt% phosphorus (based on P2O5), 5.6 wt% citric acid, with an equilibrium amount of alumina. Example VI-9 Hydrogenation catalyst II-3 was produced as follows: A high-concentration NaAlO2 solution containing 210 g of alumina / L and having an acoustic coefficient of 1.62 was mixed with deionized water to prepare 5 L of a solution with an Al2O3 content of 40 g / L, and then 16.3 g of sodium gluconate was added to obtain a NaAlO2 solution containing sodium gluconate. The solution was then transferred to a gelation reactor with a total volume of 8 L and a height-diameter ratio of 8, equipped with a CO2 gas distributor at the bottom. The solution temperature was controlled at 25±5°C, and a CO2 gas with a volume concentration of 90% was introduced from the bottom of the reactor to drive the gelation reaction. The gelation temperature was controlled at 20–40 °C, and the CO2 gas flow rate was set to 15±2 L / min. The pH reached 8.0-8.5 in 4-6 minutes at the end of the reaction, at which time the reaction was stopped, and the gelation reaction was completed. The resulting slurry was heated to 70 °C and held for 4 hours, and then filtered using a vacuum filter. After filtration, the filter cake was washed with 20 liters of deionized water (at 70 °C) for about 30 minutes. The washed filter cake was added to 1.5 liters of deionized water and stirred to form a slurry.The slurry was pumped into a spray dryer and dried to obtain hydrated alumina P1-2. 300 g of pseudo-uomeite P1-2 and 700 g of pseudo-boehmite P2-3 (SD pseudo-boehmite powder produced by Shandong Aluminum Co., Ltd.) were mixed and extruded into cloverleaf strips with a peripheral diameter of 1.6 mm by an extruder, and dried at 120 °C for 8 h. 300 g of the resulting material was taken and subjected to air flow at 800 °C for 4 h to obtain a carrier, with an air flow rate of 1.5 normal cubic meters / kg·hr. 100 g of the carrier was weighed and impregnated with 85 ml of an aqueous solution containing 20.6 g of nickel nitrate, 34.8 g of ammonium paramolybdate and 11.4 g of phosphoric acid for 1.5 h, dried at 120 °C for 5 h, cured at 380 °C for 4 h, and then impregnated with 55 ml of an aqueous solution containing 8.4 g of glycerol for 2 h, and dried at 140 °C for 5 h to obtain hydrogenation catalyst II-3 containing 3.5 wt% nickel (based on NiO), 19.1 wt% molybdenum (based on MoO3), 4.8 wt% phosphorus (based on P2O5), 5.7% organic additives, with a balanced amount of alumina. Example VI-10 Hydrogenation catalyst II-4 was produced as follows: 2000g of aluminum hydroxide powder (dry rubber powder produced by Changling Branch Catalyst Factory, 70% by weight on a dry basis) and 299g of silica sol containing 25% silica (Qingdao Ocean Chemical Plant) were weighed, and extruded into a butterfly strip with a peripheral diameter of 1.3 mm, and the wet strip was dried at 120 °C for 4 h and calcined at 600 °C for 3 h to obtain a carrier containing 5.0% by weight of silica. 200 g of the carrier was weighed, and the carrier was impregnated with 176 ml of an aqueous solution containing 16.9 g of ammonium fluoride for 2 h, dried at 120 °C for 3 h, and calcined at 420 °C for 3 h to obtain a fluorine-containing silica-alumina carrier. The carrier was impregnated with 170 ml of an aqueous solution containing 23.0 g of ammonium paramolybdate for 3 h, dried at 120 °C for 4 h, and further dried at 170 °C for 4 h to obtain a molybdenum-containing carrier. Then, the carrier was impregnated with 162 ml of an aqueous solution containing 53.2 g of nickel nitrate, 140.7 g of ammonium metatungstate, and 18.1 g of phosphoric acid was impregnated for 3 h, dried at 200 °C for 4 h, and impregnated with 121 ml of an aqueous solution containing 77.3 g of ethylene glycol, and dried at 120 °C for 6 h, to obtain a hydrogenation catalyst II-4 containing 3.6 wt% nickel (based on NiO), 5.0 wt% molybdenum (based on MoO3), and 32.5 wt% tungsten (based on tungsten oxide), 2.2 wt% fluorine (based on germanium fluoride), 3.0 wt% phosphorus (based on P2O5), 5.0 wt% ethylene glycol, with an alumina-silica balance. Example VI-11 to Example VI-16 In Examples VI-11 to VI-6, the desulfurization activity and denitrification activity of the hydrogenation catalyst produced by the process according to the present application and the hydrogenation catalyst produced in the comparative examples were subjected to hydrorefining evaluation in accordance with the following method. Calculations were made in accordance with the calculation method for the results of hydrorefining evaluation, and the results are shown in Table VI-2 below. The Middle East straight-run diesel fraction was mixed with 15% catalytic diesel used as raw material, and its characteristics are shown in Table VI-3. The desulfurization and denitrification activities of the catalyst were evaluated in a 30 ml diesel hydrogenation unit, and 30 ml of the catalyst was loaded. The inlet for the feed oil was placed at the top of the hydrogenation unit, and the hydrogenation catalyst II was placed in the upper bed of the reactor, the hydrogenation catalyst I (or D1) was loaded in the lower bed of the hydrogenation reactor, that is, downstream of the hydrogenation catalyst II. The catalyst was pre-sulfurized before the reaction. The sulfurization conditions were as follows: hydrogen partial pressure 6.4 MPa, temperature 320 °C, liquid hourly space velocity 4 h-1, hydrogen to oil volumetric ratio 300, and sulfurized oil feed rate 8 mL / h. The reaction conditions were as follows: hydrogen partial pressure of 4 MPa, reaction temperature of 350 °C, hydrogen to oil volume ratio of 300, and liquid hourly space velocity of 1.5 h-1.Samples were collected after 4 h and 500 h of reaction, respectively, and the sulfur and nitrogen contents of the raw material and final product were determined by gas chromatography. Comparative Example VI-2 to Comparative Example VI-4 Catalyst D1, catalyst D1+II-1 combination and catalyst II-1 were subjected to hydrorefining evaluation according to the process described in Examples VI-11 to VI-16, and the results were calculated according to the calculation method for hydrorefining evaluation results, and the results are shown in Table VI-2. Calculation method for hydrorefining evaluation results: The hydrodesulfurization activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example VI-1), and the hydrodesulfurization reaction was considered to be a 1.65-order reaction. The reaction rate value k(X)HDS of catalyst X was calculated according to equation (1): (1) LHSV in equation (1) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The relative hydrodesulfurization activity of catalyst X was calculated according to equation (2) using the hydrodesulfurization activity of catalyst D2 (denoted as k(D2)HDS) produced in Comparative Example VI-1 as a baseline reference: (2) The hydrodenitrogenation activity of the catalyst was evaluated relative to the reference agent D1 (i.e., the catalyst produced in Comparative Example V-1), and the hydrodenitrogenation reaction was considered as a first-order reaction. The reaction rate constant k(X)HDN of catalyst X was calculated according to equation (3): (3) LHSV in equation (3) refers to the liquid hourly space velocity of the hydrocarbon oil used during the hydrorefining reaction. The hydrodenitrogenation activity of catalyst X was calculated according to equation (4) using the hydrodenitrogenation activity of catalyst D1 (denoted as k(D2)HDN) produced in Comparative Example VI-1 as a baseline reference: (4) The results of Table VI-2 show that the hydrogenation catalyst composition according to the present application has better relative hydrodefluorination activity and relative hydrodenitrogenation activity, the reduction rate per unit time of relative activity is small, and the service life is longer. Table VI-1 Item Comparative Example VI-1 Example VI-1 Example VI-2 Example VI-3 Example VI-4 Example VI-5 Example VI-6 MoO3, wt% 20.5 20.2 - 3.2 20.0 - 20.1 CoO, wt% 4.7 4.0 - - 4.1 - 3.9 NiO, wt% - - 3.1 7.9 - 3.0 - WO3, wt% - - 15.2 21.0 - 15.5 - F, wt% - - 3.3 1.2 - 3.1 - Si, wt% 6.2 5.8 - - 5.9 - 6.1 Total carbon content of semi-finished catalyst, wt% 0.04 0.04 0.4 0.1 0.03 0.45 0.5 Table VI-2 Examples Catalyst composition Catalyst ratio I / % Relative hydrodesulfurization activity, % Relative hydrodenitrogenation activity, % 4 h reaction 500 h reaction 4 h reaction 500 h reaction Comparative example VI-2 D1 100(D1) 100 71 100 82 Comparative example VI-3 D1+II-1 20(D1) 125 80 112 86 Comparative example VI-4 II-1 0 120 - 118 - Example VI-11 I-1+ II-1 20 146 138 131 123 Example VI-12 I-2+ II-2 30 156 149 136 130 Example VI-13 I-3+ II-2 40 151 - 132 - Example VI-14 I-4+ II-3 50 133 - 114 - Example VI-15 I-5+ II-3 60 152 - 131 - Example VI-16 I-6+ II-4 70 147 - 130 - Note: “-” in Table VI-2 indicates that no diagnosis was made. Table VI-3 S value 12000 μg / g N value 220 μg / g Density (20°C) 0.8588 g / cm3 Refractive index (20°C) 1.4841 The embodiments of the present disclosure have been described in more detail with reference to the worked examples, and the scope of the present disclosure is not limited to these embodiments, but is defined by the appended claims. A person skilled in the art can make appropriate modifications to these embodiments without departing from the spirit and scope of the present disclosure, and such modified embodiments are clearly covered by the scope of the present disclosure.

Claims

Amendment to Claim 1. A process for producing a hydrogenation catalyst comprising the steps of: (1) contacting a first active metal moiety, an organic complexing agent and an optional co-agent with a support to obtain a composite support, (2) calcining the composite support to obtain a calcined composite support, wherein the total carbon content on a dry basis is 1 wt% or less, 0.5 wt% or less, 0.4 wt% or less, 0.3 wt% or less, 0.1 wt% or less, 0.08 wt% or less, 0.06 wt% or less, 0.04 wt% or less, 0.03 wt% or less, 0.01 wt% or less, 0.005 wt% or less, based on the dry weight of the calcined composite support, and (3) contacting a second organic complexing agent with the calcined composite support to obtain a hydrogenation catalyst, wherein the process includes a calcining step during or after this step. Not (3).

2. The process according to claim 1, wherein said step further comprises one or more of the following steps: (0) producing a carrier; and (4) sulfurizing the hydrogenation catalyst and step (0) further comprising the steps of: (0-1) forming a carrier precursor or a carrier precursor composition to obtain a preformed carrier, wherein the carrier precursor composition comprises a carrier precursor, a co-former, and an optional co-agent, (0-2) calcining the preformed carrier to obtain the carrier, and (0-3) optionally, contacting the co-agent or a second active metal moiety with the carrier, wherein the co-agent is one or more selected from the group consisting of metal co-agents (preferably one or more selected from the group consisting of Group IIB metal elements (e.g., one or more selected from the group consisting of zinc and cadmium), Group IA metal elements (e.g., one or more selected from the group consisting of lithium, sodium, potassium, rubidium, cesium, and francium), Group IIA metal elements (e.g., one or more selected from the group consisting of beryllium, magnesium, calcium, and strontium), and rare earth metal elements (e.g., one or more selected from the group consisting of lanthanum, cerium, praseodymium and neodymium), preferably oneor more selected from the group consisting of zinc, sodium, potassium, magnesium, calcium, lanthanum and cerium) and non-metallic cofactors (preferably one or more selected from the group consisting of Group IVA elements (such as silicon), Group VIIA elements (such as one or more selected from the group consisting of fluorine, chlorine, bromine and iodine), Group VA elements (such as one or more selected from phosphorus and arsenic) and Group IIIA elements (such as bromine), preferably one or more selected from the group consisting of fluorine, silicon, phosphorus and bromine), and wherein, in the hydrogenation catalyst, the amount of the metallic cofactor, calculated based on the metallic element, is in the range of 0 wt% to 10 wt%, preferably from 0.5 wt% to 6 wt%, based on the total weight of the hydrogenation catalyst and the amount of the non-metallic cofactor, calculated based on the non-metallic element, is in the range of 0 wt% to 10 wt%, preferably from 0.5 wt% to 6% by weight, based on the total weight of the hydrogenation catalyst.

3. The process according to claim 2, wherein the calcination conditions employed in step (0-2) comprise: a calcination temperature in the range of 250 °C to 500 °C, preferably from 350 °C to 450 °C, and a calcination time in the range of 2 hours to 8 hours, preferably from 3 to 6 hours.

4. The process according to claim 2, wherein step (0-3) comprises the following steps: (0-3-1) impregnating the carrier with the co-agent or the second active metal moiety to obtain an impregnated product, and (0-3-2) drying the impregnated product at a temperature in the range of 100 °C to 250 °C, preferably from 100 °C to 200 °C, or calcining the impregnated product at a temperature in the range of 250 °C to 600 °C, preferably from 350 °C to 500 °C.

5. The process according to claim 1, wherein step (1) comprises the following steps: (1-1) impregnating the carrier with the first active metal moiety, the first organic complexing agent, and the optional agent to obtain an impregnated product; and (1-2) applying heat to the impregnated product at a temperature of from 100 °C to 250 °C (preferably from 100 °C to 200 °C) to obtain a composite carrier.

6. The process according to claim 1, wherein the calcination conditions employed in step (2) comprise: a calcination temperature in the range of 350 °C to 500 °C, preferably from 360 °C to 450 °C, a calcination time in the range of 0.5 hours to 8 hours, preferably from 1 to 6 hours, an oxygen-containing gas (preferably having an oxygen content of not less than 20 vol%) introduced in an amount of more than 0.2 L / (g·hr), preferably from 0.2 L / (g·hr) to 20 L / (g·hr), more preferably from 0.3 L / (g·hr) to 10 L / (g·hr) based on the weight of the carrier.

7. The process according to claim 1, wherein step (3) comprises the following steps: (3-1) impregnating the calcined composite carrier with a second organic complexing agent to obtain an impregnated product, and (3-2) applying heat to the impregnated product at a temperature of from 100 °C to 250 °C (preferably from 100 °C to 200 °C) to obtain a hydrogenation catalyst.

8. The process according to claim 1 or 2, wherein the amount of the first active metal moiety or the total amount of the first active metal moiety and the amount of the second active metal moiety, calculated on the basis of oxides, is in the range of 6 wt% to 70 wt%, preferably from 15 wt% to 60 wt%, preferably from 20 wt% to 50 wt%, preferably from 20 wt% to 40 wt% based on the total weight of the hydrogenation catalyst, the molar ratio of the first organic complexing agent to the first active metal moiety is in the range of 0.03:1 to 2:1, preferably from 0.08:1 to 1.5:1, the molar ratio of the first organic complexing agent to the second organic complexing agent is in the range of 1:0.25 to 1:4, preferably from 1:0.5 to 1:2, and the molar ratio of the first active metal moiety to the second active metal moiety is in the range of From 1:0 to 1:0.4, preferably from 1:0 to 1:0.

1.

9. The process according to claim 2, wherein the precursor carries one or more selected from the group consisting of alumina, silica, alumina-silica, titania, magnesium, silica-magnesium, silica-zirconia, silica-thuria, silica-beryllia, silica-titania, silica-zirconia, titania-zirconia, silica-alumina-titania, silica-alumina-magnesium and silica-alumina-zirconia, preferably alumina, among their precursors.

10. The process according to claim 1, wherein the first organic complexing agent and the second organic complexing agent are the same or different, each independently being one or more selected from the group consisting of the following species: (i) an organic compound A obtained by truncating the carbon backbone of a C2-30 branched or linear alkane, preferably a C2-10 linear or branched alkane, with one or more heterocyclic groups selected from -O- and -NR1-, wherein the R1 group is selected from H and optionally substituted with a C1-10 linear or branched alkyl group, (ii) an organic compound B obtained by replacing one or more hydrogen atoms in the structure of a C1-30 branched or linear alkane, a C2-30 branched or linear alkyne, a C3-20 cycloalkane which is optionally substituted, or organic compound A with a group selected from the group consisting of: -R2-OH, wherein the R2 group represents a single bond or an alkylene linear or branched C1-10, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, -R3-NR4R5 where the R3 group isrepresents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group or a branched C1-3 alkyne group, preferably a linear or branched C1-3 alkylene group. R4 and R5 are the same or different, and each independently represents hydrogen, a linear or branched C1-10 alkyl group and -R6-C(=O)OM, preferably each independently represents hydrogen, a linear or branched C1-6 alkyl group and -R6-C(=O)OM, preferably each independently represents hydrogen, a linear or branched C1-3 alkyl group and -R6-C(=O)OM, preferably each independently represents -R6-C(=O)OM, wherein R6 represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, M represents H, an alkali metal or alkaline earth metal, and -R6-C(=O)OM wherein the R6 group represents a single bond or a linear or branched C1-10 alkylene group, preferably a linear or branched C1-6 alkylene group, preferably a linear or branched C1-3 alkylene group, M represents H, ais an alkali metal or alkaline earth metal, provided that organic compound A and organic compound B do not contain any oxygen-oxygen, nitrogen-nitrogen, or nitrogen-oxygen bonds in their structure and (iii) an alkylene oxide homopolymer or copolymer, preferably, the first organic complexing agent and the second organic complexing agent are the same or different from each other, each independently one or more selected from the group consisting of: (i) a C1-20 aliphatic or C5-10 alicyclic monocarboxylic acid or polycarboxylic acid or salt thereof, optionally substituted with one or more -R2-OH groups where R2 is a single bond or a C1-10 linear or branched alkylene group, preferably a single bond or a C1-6 linear or branched alkylene group, preferably a single bond or a C1-3 linear or branched alkylene group, (ii) a C1-20 aliphatic or alkynyl monoamine or polyamine, optionally substituted with one or more groups selected from -R2-OH where the R2 group represents a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group,branched C1-3 and -R6-C(=O)OM where R6 is a single bond or a linear or branched C1-10 alkylene group, preferably a single bond or a linear or branched C1-6 alkylene group, preferably a single bond or a linear or branched C1-3 alkylene group, M is H, an alkali metal or an alkaline earth metal, and (iii) a C2-20 aliphatic, preferably C2-6 or C5-10 alicyclic polyol, an oligomer or polymer thereof, or a linear or branched C1-6 alkyl etherate thereof, more preferably each independently one or more selected from the group consisting of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid or a salt thereof, 1,2-glycohexadiamine Tetraacetic acid or its salt, citric acid, tartaric acid, and malic acid, ethylenediamine, and ethylenediamine tetraacetic acid or its salt.

11. The process of claim 2, wherein the first active metal moiety and the second active metal moiety are the same or different, each independently selected from one or more of a Group VIB metal element (preferably one or more of a Group VIII metal element (preferably one or more of a Group VIB metal element) and a Group VIII metal element (preferably one or more of a Group VIII metal element), preferably each of compounds of one or more of a Group VIB metal element with one or more of a Group VIII metal element, more preferably each of compounds of molybdenum and / or tungsten with cobalt or / or nickel.

12. The process according to claim 1, wherein the process does not include any step of introducing a co-agent or metal element having hydrogenation activity during or after step (3).