CN107812525B

CN107812525B - A kind of method of hydrogenating catalyst composition and hydrotreating

Info

Publication number: CN107812525B
Application number: CN201610818804.1A
Authority: CN
Inventors: 张乐; 刘学芬; 李会峰; 胡志海; 李大东; 龙湘云; 聂红; 李明丰; 王轶凡; 鞠雪艳
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2016-09-12
Filing date: 2016-09-12
Publication date: 2019-04-16
Anticipated expiration: 2036-09-12
Also published as: CN107812525A

Abstract

This disclosure relates to a kind of method of hydrogenating catalyst composition and hydrotreating, which includes hydrogenation catalyst I and hydrogenation catalyst II；By volume and on the basis of the hydrogenating catalyst composition, the content of the hydrogenation catalyst I is 5-95%；The hydrogenation catalyst I includes carrier, hydrogenation active metals element and non-metal assistant element, and the hydrogenation active metals element contains vib metals element and group VIII metallic element；Wherein, the preparation method of the hydrogenation catalyst I includes: that the carrier of the compound that load is had the element containing hydrogenation active metals, the first organic complexing agent and non-metal assistant element carries out the first dry and roasting, obtains semi-finished product catalyst；Second organic complexing agent is loaded on the semi-finished product catalyst, and carries out second dry and without roasting, obtains the hydrogenation catalyst I.When the hydrogenating catalyst composition that the disclosure is provided is applied to hydrotreating, activity is good, and the service life is long.

Description

A kind of method of hydrogenating catalyst composition and hydrotreating

Technical field

This disclosure relates to a kind of method of hydrogenating catalyst composition and hydrotreating.

Background technique

It is raw that the environmental consciousness being increasingly enhanced and the environmental regulation being increasingly stringenter force oil refining circle more to focus on clean fuel Produce technological development.Future market vehicle fuel is intended to " super-low sulfur ", and the fuel for not being able to satisfy discharge standard will be unable to enter city ?.Hydrogen addition technology plays more and more important work as a kind of effective desulfurization means in the production of fuel for cleaning vehicle With, wherein efficient hydrogenation catalyst is then the core technology of hydrogen addition technology, therefore, develop have more high activity and selectivity it is new Type hydrogenation catalyst becomes most urgent one of the demand of petroleum refining industry.

Hydrogenation catalyst generallys use infusion process preparation, i.e., with molten containing required active component (such as Ni, Mo, Co, W) Liquid, impregnates certain carrier, the method for being dried and roasting later.

Chinese patent CN103551162A discloses a kind of diesel hydrogenation for removal sulphur denitrification catalyst, and the composition of catalyst includes carrying Body, auxiliary agent, active metal；Carrier is Al₂O₃-ZrO₂-TiO₂-SiO₂Multivariant oxide complex carrier；Auxiliary agent is phosphorus；With nickel, cobalt, Molybdenum and tungsten are active component；Weight percent content of each component on the basis of catalyst are as follows: in terms of oxide, cobalt oxide 1~ 6wt%；1~15wt% of nickel oxide, 2~12wt% of molybdenum oxide, 12~35wt% of tungsten oxide, auxiliary agent phosphorus pentoxide 1.5~ 5wt%；Kong Rong ≮ 0.2mL/g of catalyst, specific surface area are ≮ 140m²/ g, mechanical strength ≮ 15N/mm；It is each in complex carrier Shared specific gravity is respectively as follows: titanium oxide and accounts for 2~15wt% component in the carrier, and silica accounts for 2~20wt%, and zirconium oxide accounts for 5~ 15wt%；Surplus is aluminium oxide.The catalyst is made by step impregnation method: co-impregnated solution is divided into isometric two parts, point Two step impregnated carriers, and all roasted after the completion of each step dipping.

Chinese patent CN103657667A discloses a kind of preparation of new macroporous structure catalyst for heavy oil hydrogenation demetal Method specifically comprises the following steps: the preparation of 1) Aluminum sol；2) asphaltic residue powder and Aluminum sol are mixed with macroporous structure Catalyst carrier；3) catalyst carrier after molding is used to two step impregnations of isometric branch；Catalysis is finally made Agent.Two step infusion processes of the preparation method specifically: the first step first impregnates Mo, and second step impregnates Ni, and not including in maceration extract has Machine complexing agent.

Although above-mentioned preparation method can improve the Hydrogenation of catalyst to a certain extent, further study It has been found that, there are still the defects that catalyst activity is lower or catalyst life is shorter for catalyst made from the prior art.

Summary of the invention

Purpose of this disclosure is to provide a kind of methods of hydrogenating catalyst composition and hydrotreating, and the disclosure is provided When hydrogenating catalyst composition is applied to hydrotreating, activity is good, and the service life is long.

To achieve the goals above, the disclosure provides a kind of hydrogenating catalyst composition, the hydrogenating catalyst composition packet Include hydrogenation catalyst I and hydrogenation catalyst II；By volume and on the basis of the hydrogenating catalyst composition, described plus hydrogen is urged The content of agent I is 5-95%；The hydrogenation catalyst I includes carrier, hydrogenation active metals element and non-metal assistant element, The hydrogenation active metals element contains vib metals element and group VIII metallic element；Wherein, the hydrogenation catalyst The preparation method of I includes: the compound, the first organic complexing agent and non-metal assistant that load is had the element containing hydrogenation active metals The carrier of element carries out the first dry and roasting, obtains semi-finished product catalyst；Wherein, in terms of butt and with semi-finished product catalysis On the basis of the dry weight of agent, the carbon content of the semi-finished product catalyst is 0.01-0.5 weight %；By the second organic complexing agent It loads on the semi-finished product catalyst, and carries out second dry and without roasting, obtain the hydrogenation catalyst I.

Preferably, in hydrogenator, the type of feed of the hydrogenation catalyst I and hydrogenation catalyst II are layering dress It fills out or mixed packing；The mode of the layering filling includes: the flow direction according to feedstock oil, and the hydrogenation catalyst I is seated in institute State the upstream of hydrogenation catalyst II, the hydrogenation catalyst II is seated in the upstream of the hydrogenation catalyst I or described plus hydrogen is urged Agent I and the hydrogenation catalyst II alternatively layered load.

Preferably, described load has the compound of the element containing hydrogenation active metals, the first organic complexing agent and nonmetallic helps The preparation step of the carrier of agent element includes: with compound and the first organic complex containing the element containing hydrogenation active metals The aqueous solution dipping of agent contains the carrier of the non-metal assistant element；Alternatively, with the element containing hydrogenation active metals is contained Compound, non-metal assistant element and the first organic complexing agent solution impregnating carrier.

Preferably, it is counted by butt and on the basis of the dry weight of the semi-finished product catalyst, the semi-finished product catalyst Carbon content be 0.04-0.4 weight %.

Preferably, the described first dry condition and the second dry condition include: dry temperature each independently Degree is 100-250 DEG C, and the dry time is 1-12 hours；The condition of the roasting includes: under conditions of being passed through oxygen-containing gas It carries out, on the basis of the weight of carrier, the intake of oxygen-containing gas is 0.2-20 liter/(gram hour)；The temperature of roasting is 350-500 DEG C, the time of roasting is 0.5-8 hours.

Preferably, first organic complexing agent and the second organic complexing agent include organic oxygen-containing compound each independently And/or nitrogen-containing organic compound；The organic oxygen-containing compound is Organic Alcohol and/or organic acid, the nitrogen-containing organic compound For organic amine and/or organic ammonium salt.

Preferably, first organic complexing agent and the second organic complexing agent include selected from ethylene glycol, third each independently Triol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, aminotriacetic acid, 1,2- cyclohexane diamine tetrem At least one of acid, citric acid, tartaric acid, malic acid, ethylenediamine and ethylenediamine tetra-acetic acid.

Preferably, the molar ratio of the hydrogenation active metals element and first organic complexing agent is 1:(0.03-2).

Preferably, the molar ratio of first organic complexing agent and second organic complexing agent is 1:(0.25-4).

Preferably, it is counted by oxide and on the basis of the total weight of the hydrogenation catalyst I, the hydrogenation active metals member The content of element is 6-70 weight %；Based on the element and on the basis of the total weight of the hydrogenation catalyst I, the non-metal assistant The content of element is no more than 10 weight %.

Preferably, the non-metal assistant element be selected from group IVA element, V Group IIA element, V A race's element and At least one of group III A element, the carrier be selected from gama-alumina, silica, aluminium oxide-silicon oxide, titanium oxide, Magnesia, silica-magnesias, silica-zirconia, silica thoria, silica-berylias, silica-titania, Titania-zirconia, silica-alumina thoria, silica-alumina-titania, silicaalumina-magnesia With one of silica-alumina, zirconia or a variety of.

Preferably, the vib metals element be molybdenum and/or tungsten, the group VIII metallic element be cobalt and/or Nickel；The non-metal assistant element is selected from least one of fluorine element, element silicon, P elements and boron element.

Preferably, it is counted by oxide and on the basis of the total weight of the hydrogenation catalyst I, the group VIII metal member The content of element is 1-10 weight %, and the content of the vib metals element is 5-60 weight %.

Preferably, the hydrogenation catalyst II contains at least one vib metals element and at least one group VIII Metallic element；It is counted by oxide and on the basis of the total weight of the hydrogenation catalyst II, the group VIII metallic element Content is 1-10 weight %, and the content of the vib metals element is 5-60 weight %.

The disclosure also provides a kind of method of hydrotreating, this method comprises: by adding provided by feedstock oil and the disclosure Hydrogen catalyst composition contacts and carries out hydrogenation reaction.

Preferably, it is 300-400 DEG C that the condition of the hydrogenation reaction, which includes: temperature, and pressure is 1-10 megapascal, feedstock oil Volume space velocity is 0.5-3 hours when liquid^-1, hydrogen to oil volume ratio 100-800.

Preferably, the feedstock oil is selected from gasoline, diesel oil, lubricating oil, kerosene, naphtha, reduced crude, decompression slag At least one of oil, pertroleum wax and Fischer-Tropsch synthesis oil.

The disclosed invention people discovery adds hydrogen to urge using the hydrogenation catalyst I and commonly used in the art of method of disclosure preparation After agent II is applied in combination, there is good hydrogenation activity and longer catalyst life, have to various hydrocarbon oil crude materials good Hydrodesulfurization, hydrodenitrogeneration performance.

In addition, the hydrogenating catalyst composition that the disclosure provides has both higher hydrodesulfurization activity and hydrodenitrogeneration is living Property, hence it is evident that extend the service life of catalyst.

Other feature and advantage of the disclosure will the following detailed description will be given in the detailed implementation section.

Specific embodiment

The specific embodiment of the disclosure is described in detail below.It should be understood that described herein specific Embodiment is only used for describing and explaining the disclosure, is not limited to the disclosure.

The disclosure provides a kind of hydrogenating catalyst composition, which includes hydrogenation catalyst I and add Hydrogen catalyst II；By volume and on the basis of the hydrogenating catalyst composition, the content of the hydrogenation catalyst I is 5- 95%；The hydrogenation catalyst I includes carrier, hydrogenation active metals element and non-metal assistant element, the hydrogenation activity gold Belong to element and contains vib metals element and group VIII metallic element；Wherein, the preparation method packet of the hydrogenation catalyst I Include: by load have the carrier of the compound of the element containing hydrogenation active metals, the first organic complexing agent and non-metal assistant element into Row first is dry and roasts, and obtains semi-finished product catalyst；Wherein, in terms of butt and with the dry weight of the semi-finished product catalyst On the basis of, the carbon content of the semi-finished product catalyst is 0.01-0.5 weight %, preferably 0.04-0.4 weight %；Second is had Machine complexing agent loads on the semi-finished product catalyst, and carries out second dry and without roasting, obtains the hydrogenation catalyst Agent I.It should be noted that the dry weight measuring method of semi-finished product catalyst described in the disclosure is: weighing constant weight The sample is roasted 3 hours for 450 DEG C in Muffle furnace, is weighed after cooling, which is sample by sample to be tested (such as 30 grams) The dry weight of product.

There is no special limits to type of feed in hydrogenator of hydrogenation catalyst I and hydrogenation catalyst II for the disclosure System, such as type of feed can be layering filling or mixed packing；The mode of the layering filling may include: according to feedstock oil Flow direction, the hydrogenation catalyst I is seated in the upstream of the hydrogenation catalyst II, the hydrogenation catalyst II be seated in it is described The upstream of hydrogenation catalyst I or the hydrogenation catalyst I and the hydrogenation catalyst II alternatively layered are loaded.Due to adding hydrogen to urge The better performances of agent I, last a long time, and hydrogenation catalyst I is preferably seated in downstream, under more exacting terms with raw material Oil is reacted.

The disclosure introduces complexing agent and complexing dipping dry at low temperature inventors have found that passing through in dipping process Technology can weaken active component and carrier interaction, the dispersion degree for improving hydrogenation active metals element, change metal vulcanization Sequentially, it forms the activity of more high activities mutually and improves activated centre number.But due to being used in complexing dipping technique Low temperature drying, there is no the process Jing Guo high-temperature roasting, hydrogenation active metals element exists still in the form of metallic salt In carrier surface, hydrogenation active metals element and carrier function power are weaker, cause in high temperature and pressure and severe raw material plus hydrogen Under reaction condition, metal is constantly assembled during the reaction, and auxiliary agent effect weakens, and activated centre number is reduced, latent active Decline, therefore activity and the stability decline of catalyst.Although and use high-temperature roasting method preparation catalyst stability it is preferable, But active component and carrier active force is stronger, the latent active in activated centre is lower, due to the dispersion and resistance of not no complexing agent Every effect, active component platelet is larger, and activated centre number is less, and activity is very low.Compared with traditional infusion process, complexing dipping Technology although the activity of such catalyst can be promoted further, but exist catalytic activity reduce it is too fast, cause catalyst to make With the defect that the service life is too short.

The inventor of the disclosure by research it has furthermore been found that prepare catalyst by two steps load (such as impregnate) method, First step load and second step load are respectively used to introduce hydrogenation active metals element and organic complexing agent, load in the first step The first organic complexing agent is added in journey and is run through roasting and is converted into charcoal, the activity of catalyst, Er Qieneng can not only be improved Enough high activities for effectively keeping catalyst for a long time, to greatly improve the service life of catalyst.Speculate that its reason may It is because the first organic complexing agent being added in first step loading process hinders hydrogenation active metals element in roasting process Aggregation disperses it more uniform；Meanwhile roasting can make the compound of the element containing hydrogenation active metals after first step load It is converted into metal oxide, the first organic complexing agent is made to be converted into charcoal, to oxidize metal combination between object and carrier more Add securely, improves the activity and stability of catalyst.And the second organic complexing agent being added in second step loading process covers It covers in catalyst surface, aggregation of metal oxide during catalyst vulcanization can be effectively prevent, improve metal dispersity, It is more advantageous to be formed with higher active II class activity phase and form more activated centres, be urged to further improve The activity of agent.

The disclosure to the compound, the first organic complexing agent and non-metal assistant element of the element containing hydrogenation active metals with Which kind of form, which kind of sequentially load to it is not restricted on the carrier, only need to roasting when, the first organic complexing agent can hinder Hinder the aggregation of hydrogenation active metals element and form charcoal:

For example, described load the compound, the first organic complexing agent and non-metal assistant for having the element containing hydrogenation active metals The preparation step of the carrier of element includes: with compound and the first organic complexing agent containing the element containing hydrogenation active metals Aqueous solution dipping contain the non-metal assistant element carrier；Alternatively, with the element containing hydrogenation active metals is contained Dipping described in the solution impregnating carrier of compound, non-metal assistant element and the first organic complexing agent can be isometric leaching Stain, or the temperature of the dipping is not particularly limited in supersaturation dipping, and it is attainable various to can be maceration extract institute The time of dipping is not particularly limited in temperature, if the desired amount of required component can be loaded, such as: the temperature of dipping Degree can be 15-60 DEG C, and the time of dipping can be 0.5-5 hours.

According to the disclosure, hydrogenation active metals element be it is well-known to those skilled in the art, for example, the group VIB Metallic element is preferably molybdenum and/or tungsten, and the group VIII metallic element is preferably cobalt and/or nickel；In terms of oxide and with institute On the basis of the total weight for stating hydrogenation catalyst I, the content of the hydrogenation active metals element can be 6-70 weight %, preferably 15-60 weight %, preferably 20-50 weight %, further preferably 20-40 weight %；The group VIII metallic element Content can be 1-10 weight %, and the content of the vib metals element can be 5-60 weight %.

According to the disclosure, in the preparation method of hydrogenation catalyst I, the compound of the element containing hydrogenation active metals is this field Known to personnel, it can be various solubility and meet load requirement or can be formed in water in the presence of cosolvent molten The water soluble compound for the element containing hydrogenation active metals that Xie Du is met the requirements, such as can be salt and/or oxide, preferably For at least one of nitrate, chloride, sulfate, carbonate, more preferably nitrate.With elemental metal with aqueous solution On the basis of, the concentration of the water soluble salt of the element containing hydrogenation active metals can be 0.2-8mol/L, preferably 0.2-5mol/L, more Further preferably 0.2-2mol/L.Concentration herein is that the water soluble salt of the various elements containing hydrogenation active metals is respective dense Degree, rather than total concentration.

It will illustrate the compound of the compound and the metallic element containing group VIII of the element containing vib metals respectively below.

A kind of specific embodiment, the compound of the element containing vib metals can be selected from ammonium molybdates, ammonium paramolybdate, partially At least one of ammonium tungstate, molybdenum oxide and tungsten oxide.

Another specific embodiment, the compound of the metallic element containing group VIII can be selected from the nitre of group VIII metal Hydrochlorate, the chloride of group VIII metal, the sulfate of group VIII metal, the formates of group VIII metal, group VIII The acetate of metal, the phosphate of group VIII metal, the citrate of group VIII metal, group VIII metal oxalic acid Salt, the carbonate of group VIII metal, the subcarbonate of group VIII metal, the hydroxide of group VIII metal, The phosphate of group VIII metal, the phosphide of group VIII metal, the sulfide of group VIII metal, group VIII metal aluminium Hydrochlorate, the molybdate of group VIII metal, the tungstates of group VIII metal and group VIII metal water-soluble oxide in At least one.

The compound of a kind of preferred embodiment, the metallic element containing group VIII is selected from group VIII metal Oxalates, the nitrate of group VIII metal, the sulfate of group VIII metal, the acetate of group VIII metal, Section VIII The chloride of race's metal, the carbonate of group VIII metal, the subcarbonate of group VIII metal, group VIII metal hydrogen Oxide, the phosphate of group VIII metal, the molybdate of group VIII metal, the tungstates of group VIII metal and Section VIII At least one of the water-soluble oxide of race's metal.

The compound of a kind of further preferred embodiment, the metallic element containing group VIII can be selected from nitric acid In nickel, nickel sulfate, nickel acetate, basic nickel carbonate, cobalt nitrate, cobaltous sulfate, cobalt acetate, basic cobaltous carbonate, cobalt chloride and nickel chloride At least one.

According to the disclosure, the compound loaded sequence on carrier of the element containing hydrogenation active metals is not limited particularly It is fixed, hydrogenation activity can be contained for all by the solution impregnating carrier of the compound of the element containing hydrogenation active metals containing there are many On the compound mutual load to carrier of metallic element, the compound containing the element containing hydrogenation active metals can also be prepared respectively Solution step impregnation carrier, the compound of the element containing hydrogenation active metals is successively loaded on carrier.It is soaked when using substep When stain, preferably it is dried after each dipping.Dry mode and condition is referred to the prior art and is selected.

According to the disclosure, the mode that first organic complexing agent loads on carrier is not particularly limited.First has Machine complexing agent can at least one of the compound of the element containing hydrogenation active metals co-formulation at maceration extract impregnated carrier, Maceration extract impregnated carrier can also be individually configured to, preferably the former.

According to the disclosure, it can be commonly used in the art that non-metal assistant element, which is well-known to those skilled in the art, The various nonmetalloids that can improve the performance with hydrogenation catalyst action catalysts, can be according to the applicable cases of catalyst It is selected.Such as it can be in group IVA element, V Group IIA element, V A race's element and group III A element At least, group IVA metallic element is preferably silicon and/or carbon, V Group IIA metallic element be preferably in fluorine, chlorine, bromine and iodine extremely Few one kind, V A race metallic element are preferably at least one of phosphorus and/or arsenic, and group III A element for example can be boron, more Preferably, the non-metal assistant element is selected from least one of fluorine element, element silicon, P elements, boron element, nonmetallic to help The content of agent element is usually no more than 10 weight %, preferably 0.5-6 weight %.Due to equal in carrier and non-metal assistant element Element silicon can be contained, unless otherwise noted, if silicon content is more than 10 weight %, and exists in the form of silica, be included into Carrier, otherwise element silicon belongs to non-metal assistant element.

According to the disclosure, the non-metal assistant element loads to the mode on carrier and limits there is no specific, described The carrying method of non-metal assistant element can through a variety of ways, for example, can load in carrier preparation process, can also be with By various modes as the mode of dipping loads after carrier preparation.

It should be noted that needing introducing non-gold when loading non-metal assistant element by the method for impregnated carrier It is roasted after belonging to auxiliary element, the maturing temperature can be 250-600 DEG C, and preferably 350-500 DEG C, calcining time can be with It is 2-8 hours, preferably 3-6 hours.

According to the disclosure, the load of non-metal assistant element described in catalyst I need to load it in the second organic complexing agent Preceding progress, to ensure that the second organic complexing agent does not suffer from roasting process.

When using infusion process, preferably non-metal assistant element and the compound of the element containing hydrogenation active metals and first are had Machine complexing agent loads on carrier together.The various soluble-salts that non-metal assistant can be used in non-metal assistant element are born It carries, such as is selected from oxide, chloride, contains at least one of hydrochlorate and ammonium salt.In terms of nonmetalloid, non-gold in maceration extract The dosage for belonging to auxiliary element can be 0.05-3mol/L, preferably 0.1-2mol/L.

The disclosure controls the carbon content of semi-finished product catalyst by condition that is dry and roasting, for example, described first is dry It is 100-250 DEG C that dry condition and the second dry condition include: dry temperature each independently, preferably 100- 200 DEG C, the dry time is 1-12 hours, preferably 1-10 hours；The condition of the roasting includes: to be passed through oxygen-containing gas Under the conditions of carry out, on the basis of the weight of carrier, the intake of oxygen-containing gas be greater than 0.2 liter/(gram hour), preferably 0.2-20 liter/(gram hour), further preferably 0.3-10 liter/(gram hour)；The temperature of roasting is 350-500 DEG C, excellent It is selected as 360-450 DEG C, the time of roasting is 0.5-8 hours, preferably 1-6 hours, wherein the oxygen-containing gas can be sky Gas, oxygen and other oxygen-containing gas, preferably oxygen volume content are not less than 20 body %, and being passed through for oxygen-containing gas on the one hand can Meet burning condition, make the compound of the element containing hydrogenation active metals, for example, the element containing hydrogenation active metals salt conversion and For hydrogenation active metals oxide, and the first organic complex is made to be converted into charcoal, the dioxy that on the other hand can also form burning Change carbon and water and other compositions emit, causes to hinder the vacancy of active phase on catalyst I to avoid being deposited on.

According to the disclosure, first organic complexing agent and the second organic complexing agent include organic oxygen-containing each independently Object and/or nitrogen-containing organic compound are closed, the organic oxygen-containing compound can be Organic Alcohol and/or organic acid, the Organic Alcohol Preferably polyalcohol, further preferably carbon atom number are polyalcohol, the oligomer of polyalcohol and the poly of polyalcohol of 2-6 Body, for example, in ethylene glycol, glycerine, polyethylene glycol, diethylene glycol and butanediol at least one in, the polyethylene glycol Molecular weight be preferably 200-1500, the organic acid is preferably C₂-C₇The organic acid containing one or more carboxyls, for example, choosing From in acetic acid, maleic acid, oxalic acid, aminotriacetic acid, 1,2- cyclohexanediamine tetraacetic acid, citric acid, tartaric acid and malic acid It is at least one.The nitrogen-containing organic compound can be organic amine and/or organic ammonium salt, and the organic amine is preferably C₂-C₇Contain The compound of one or more amino groups, such as selected from least one of primary amine, secondary amine and tertiary amine, preferably ethylenediamine, The organic ammonium salt is preferably ethylenediamine tetra-acetic acid.Specifically, first organic complexing agent and the second organic complexing agent are preferred It each independently include being selected from ethylene glycol, glycerine, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, ammonia In base triacetic acid, 1,2- cyclohexanediamine tetraacetic acid, citric acid, tartaric acid, malic acid, ethylenediamine and ethylenediamine tetra-acetic acid extremely Few one kind.It is further preferred that first organic complexing agent and the second organic complexing agent are organic acid, so that catalyst obtains Obtain higher hydrogenation activity.The molar ratio of the hydrogenation active metals element and first organic complexing agent can be 1: (0.03-2), preferably 1:(0.08-1.5), the molar ratio of first organic complexing agent and second organic complexing agent can Think 1:(0.25-4), preferably 1:(0.5-2).

According to the disclosure, carrier is well-known to those skilled in the art, for example, the carrier can be for selected from γ-oxygen Change aluminium, silica, aluminium oxide-silicon oxide, titanium oxide, magnesia, silica-magnesias, silica-zirconia, silica-oxygen Change thorium, silica-berylias, silica-titania, titania-zirconia, silica-alumina thoria, silica-oxygen Change at least one of aluminium-titanium oxide, silicaalumina-magnesia and silica-alumina, zirconia, wherein aluminium oxide The oxidation obtained after further preferably a kind of hydrated alumina (aluminium hydroxide, such as boehmite) glue compound roasting Aluminium.

According to the disclosure, hydrogenation catalyst II can be the hydrogenation catalyst of this field routine, generally comprise carrier and gold Belong to component, hydrogenation catalyst II is not particularly limited in the disclosure, can be commercially available commodity, can also be using arbitrary existing There is technology preparation.For example, the hydrogenation catalyst II can contain vib metals element and group VIII metallic element；With Oxide meter and on the basis of the total weight of the hydrogenation catalyst II, the content of the group VIII metallic element can be 1- 10 weight %, the content of the vib metals element can be 5-60 weight %.

The disclosure also provides a kind of method of hydrotreating, this method comprises: by adding provided by feedstock oil and the disclosure Hydrogen catalyst composition contacts and carries out hydrogenation reaction.Compared with using conventional hydrogenation catalyst, provided using the disclosure Hydrogenating catalyst composition has higher hydrogenation activity.

According to the disclosure, hydrogenation catalyst I and hydrogenation catalyst II can be layered and be loaded on the same of the same reactor In catalyst bed or different catalysts bed, it can also be loaded in several concatenated reactors and use, not have to this disclosure There is special limitation.

According to the disclosure, before hydrogenation catalyst I, later and among and hydrogenation catalyst II before, later and it In, any other catalyst or filler for helping to improve hydrogenation catalyst performance can be set.For example, if hydrogenation catalyst I is located at the upstream hydrogenation catalyst II, can add such as porcelain ball, active supporter filler, before hydrogenation catalyst I to improve The distribution etc. of feedstock oil in the reactor.The usage mode of filler is known to those skilled in the art, and the disclosure does not repeat.

According to the disclosure, hydrotreating is well-known to those skilled in the art, such as can be hydrodesulfurization and plus hydrogen The unifining process such as denitrogenation, the condition of the hydrogenation reaction may include: that temperature is 300-400 DEG C, preferably 320-380 DEG C, pressure is 1-10 megapascal (in terms of gauge pressure), preferably 1-8 megapascal, and volume space velocity is 0.5-3 hours when the liquid of feedstock oil^-1, excellent It is selected as 0.5-2.5 hours^-1, hydrogen to oil volume ratio 100-800, preferably 100-700, the hydrogen to oil volume ratio refers to the body of hydrogen The ratio of the volume flow rate of product flow velocity and feedstock oil.The feedstock oil be it is well-known to those skilled in the art, be for example, selected from At least one in gasoline, diesel oil, lubricating oil, kerosene, naphtha, reduced crude, decompression residuum, pertroleum wax and Fischer-Tropsch synthesis oil Kind.

According to the disclosure, the hydrogenating catalyst composition is preferably carrying out sulphur using the conventional method of this field using preceding Change.Generally, the condition of the vulcanization may include: in presence of hydrogen, at a temperature of 360-400 DEG C, with sulphur, vulcanization At least one of hydrogen, carbon disulfide, dimethyl disulfide and polysulfide carry out presulfurization in 2-4 hours, and the presulfurization can It carries out, can also be carried out in reactor In-situ sulphiding outside reactor.

The disclosure will be further illustrated by embodiment below, but therefore the disclosure is not any way limited.

Rigaku electric machine industry Co., Ltd. 3271E type X-ray fluorescence spectra is used in following embodiment and comparative example Instrument carries out analysis measurement to the content of each element in catalyst.Carbon content uses HORIBA company, Japan in semi-finished product catalyst The EMIA-320V carbon and sulfur analytical instrument of production carries out analysis measurement.

The butt measuring method of hydrated alumina or aluminium hydrate powder used in embodiment are as follows: weigh the to be measured of constant weight The sample is roasted 3 hours for 600 DEG C in Muffle furnace, is weighed after cooling, which is dry basis by sample (such as 30 grams) The ratio of amount, the weight and sample to be tested is the butt of sample.

Embodiment 1

The present embodiment is used to illustrate the hydrogenation catalyst I and preparation method thereof according to the disclosure.

By 2000 grams of aluminium hydrate powders (Chang Ling refinery company catalyst plant production dry glue powder, 71 weight % of butt) and 1039 grams of silica solution (Haiyang Chemical Plant, Qingdao's product, dioxide-containing silica are 30 weight %) are uniformly mixed.The mixing that will be obtained Object is extruded into the butterfly item that circumscribed circle diameter is 1.4 millimeters with banded extruder, and the wet bar of extrusion is 4 hours dry at 120 DEG C, then It is roasted 3 hours at 600 DEG C, carrier I-Z1 is made, silica content is 18.0 weight % in carrier I-Z1, and alumina content is 82.0 weight %.

Weigh respectively 54 grams of molybdenum trioxides, 19 grams of basic cobaltous carbonates, 13 grams of phosphoric acid, 30 grams of citric acids be put into 140 grams go from In sub- water, heating stirring dissolves to obtain clarification dipping solution, impregnates 200 grams of I-Z1 using the above-mentioned solution of saturation infusion process and carries Body, dip time are 2 hours, then, 2 hours dry at 120 DEG C, then roast it in the state of being passed through air stream Burn, maturing temperature be 400 DEG C, the time be 2 hours, gas agent ratio be 1 liter/(gram hour), obtain semi-finished product catalyst I-Z-S1, Carbon content is shown in Table 1；30 grams of citric acids are added in 150 grams of deionized waters, clear solution is stirred to get, are used using saturation infusion process Above-mentioned solution impregnates I-Z-S1, and dip time is 2 hours, then, in 150 DEG C of dry 3 hours, obtains catalyst I-1.To urge On the basis of the total amount of agent I-1, in terms of oxide, the content of hydrogenation active metal component is shown in Table 1.

Comparative example 1

Hydrogenation catalyst is prepared using method same as Example 1, unlike, by catalyst obtained by embodiment 1 I-1 is roasted 3 hours at 400 DEG C, obtains catalyst D1, on the basis of the total amount of catalyst D1, in terms of oxide, and hydrogenation activity gold The content for belonging to component is shown in Table 1.

Embodiment 2

30 grams of nickel nitrates, 45 grams of ammonium metatungstates, 15 grams of oxalic acid and 21 grams of ammonium fluorides are weighed respectively is put into 140 grams of deionized waters In, stirring and dissolving obtains clear solution, impregnates 200 grams of alumina supports, dip time using the above-mentioned solution of saturation infusion process It is 2 hours, it is then, 2 hours dry at 120 DEG C, then it is roasted in the state of being passed through air stream, maturing temperature is 360 DEG C, the time be 6 hours, gas agent ratio be 10.0 liters/(gram hour), obtain semi-finished product catalyst I-Z-S2, carbon content is shown in Table 1；10 grams of diethylene glycol (DEG)s are put into 150 grams of deionized waters, clear solution is stirred to get, are soaked using the saturation above-mentioned solution of infusion process Stain I-Z-S2, dip time are 2 hours, then, in 150 DEG C of dry 3 hours, obtain catalyst I-2.With catalyst I-2's On the basis of total amount, in terms of oxide, the content of hydrogenation active metal component is shown in Table 1.

Embodiment 3

60 grams of ammonium fluorides are weighed, deionized water stirring and dissolving is added, adds deionized water to 850 milliliters, saturation dipping 1000 Grams Zirconia carrier 2 hours, then 2 hours dry at 120 DEG C, 400 DEG C roast 4 hours, obtain fluorine-containing Zirconia carrier I-Z3.

83 grams of nickel nitrates, 60 grams of ammonium metatungstates, 10 grams of ammonium molybdates, 20 grams of ammonium dihydrogen phosphates and 20 grams of citric acids are weighed respectively It is put into 180 grams of deionized waters, stirring and dissolving obtains clear solution, impregnates 200 grams with above-mentioned solution using saturation infusion process and contains Fluorine Zirconia carrier I-Z3, dip time are 2 hours, then, 2 hours dry at 120 DEG C, it is then being passed through air stream Roasted under state, maturing temperature is 450 DEG C, and the time is 3 hours, and gas agent ratio is 0.3 liter/(gram hour), obtain half at Product catalyst I-Z-S3, carbon content are shown in Table 1；15 grams of ethylenediamines are put into 150 grams of deionized waters, clear solution is stirred to get, I-Z-S3 is impregnated using the above-mentioned solution of saturation infusion process, dip time is 2 hours, then, in 120 DEG C of dry 3 hours, is obtained To catalyst I-3.On the basis of the total amount of catalyst I-3, in terms of oxide, the content of hydrogenation active metal component is shown in Table 1.

Embodiment 4

Hydrogenation catalyst I is prepared using method same as Example 1, unlike, metal active constituent is impregnated into load After body, when roasting to carrier, maturing temperature is 480 DEG C, and the time is 6 hours.Carbon content in obtained catalyst semi-finished product It is shown in Table 1, in obtained catalyst I-4, on the basis of the total amount of catalyst I-4, in terms of oxide, hydrogenation active metal component Content is shown in Table 1.

Embodiment 5

Hydrogenation catalyst I is prepared using method same as Example 2, unlike, gas agent ratio when roasting is 1.0 It rises/(gram hour), in obtained catalyst I-5, on the basis of the total amount of catalyst I-5, in terms of oxide, hydrogenation activity gold The content for belonging to component is shown in Table 1.

Embodiment 6

Hydrogenation catalyst I is prepared using method same as Example 1, unlike, step (1) and step (2) are organic The amount ratio of complexing agent is changed to 50 grams: 10 grams by 30 grams: 30 grams, and in obtained catalyst I-6, the total amount with catalyst I-6 is Benchmark, in terms of oxide, the content of hydrogenation active metal component is shown in Table 1.

Embodiment 7-10 illustrates the preparation method of catalyst II.

Embodiment 7

Hydrogenation catalyst II-1 the preparation method is as follows:

Weigh a certain amount of small porous aluminum oxide precursor (the first hydrated alumina, sodium metaaluminate-carbon dioxide process be made Industrial products, name of product be dry boehmite, Shandong Aluminum Plant produce, wherein the heavy % of a diaspore content 80, three water The heavy % of aluminium stone content 5).Separately weigh precursor (second of hydrated alumina, the sodium metaaluminate-sulfuric acid of a certain amount of macroporous aluminium oxide Industrial products made from aluminium method, name of product are Chang Ling dry glue powder, and Chang Ling oil plant catalyst plant is produced, a diaspore content 68 Weight %, gibbsite content 5 are % heavy).By two kinds of hydrated aluminas by 75: 25 dry weight than being uniformly mixed, addition helps crowded Agent, adhesive and water, are extruded into the trilobal cross item that circumscribed circle diameter is 1.4 millimeters, and 120 DEG C of drying are roasted at 550~650 DEG C respectively It burns 4 hours, catalyst carrier is made, weighs a certain amount of alumina support respectively, with ammonium fluoride (chemistry is pure) aqueous solution dipping 1 Hour, 120 DEG C of drying roast 4 hours at 530 DEG C, obtain fluoro-containing alumina carrier.With quantitative ammonium metatungstate (chemistry pure) and The mixed aqueous solution of nickel nitrate (chemistry is pure) impregnates fluoro-containing alumina carrier 4 hours, 120 DEG C of drying, in 530 DEG C of roasting temperatures 4 hours, hydrogenation catalyst II-1 is made, it includes the nickel (in terms of NiO) of 4 weight %, the tungsten (in terms of tungsten oxide) of 30 weight %, The fluorine (being calculated with element fluorine) of 4 weight %, remaining is aluminium oxide.

Embodiment 8

Hydrogenation catalyst II-2's the preparation method is as follows:

27.2 grams of molybdenum trioxides, 9.1 grams of basic cobaltous carbonates, 5.5 grams of phosphoric acid, 7.6 grams of citric acids are weighed respectively is put into 55mL In deionized water, it is heated to 80 DEG C and is stirred dissolution, become brownish red clear solution after about 1 hour.The solution is put into burning In cup, 90 DEG C and under stiring constant temperature 8 hours are heated to, 85mL is added water to, obtains clarification dipping solution.By 2000 grams of hydroxides Aluminium powder (dry glue powder of Chang Ling refinery company catalyst plant production, 71 weight % of butt) and 1039 grams of silica solution (Qingdao Haiyangs Factory products, dioxide-containing silica are 30 weight %) it is uniformly mixed.Obtained mixture is extruded into circumscribed circle diameter with banded extruder For 1.4 millimeters of butterfly item, and the wet bar of extrusion is 4 hours dry at 120 DEG C, it is then roasted 3 hours at 600 DEG C, is made and carries Body, silica content is 18.0 weight % in carrier, and alumina content is 82.0 weight %.The water absorption rate of carrier is 0.85.With It clarifies dipping solution 85mL saturation and impregnates 100 grams carrier 2 hours, 2 hours of 120 DEG C of dryings, obtain 3 hours of 250 DEG C of dryings Hydrogenation catalyst II-2, wherein including the Co (in terms of CoO) of 3.9 weight %, the molybdenum of 20.1 weight % is (with MoO₃Meter), 2.1% The phosphorus of weight % is (with P₂O₅Meter), 5.6% citric acid, remaining is aluminium oxide.

Embodiment 9

Hydrogenation catalyst II-3's the preparation method is as follows:

Will containing 210 grams of aluminium oxide/liter, causticity coefficient be 1.62 high concentration NaAlO₂Solution is configured to deionized water Al₂O₃Concentration is 5 liters of solution of 40 grams per liters, is then added 16.3 grams of sodium gluconate and obtains the NaAlO containing sodium gluconate₂It is molten Liquid is then transferred in the plastic reaction kettle of total volume 8L, and reaction kettle ratio of height to diameter is 8, lower bands CO₂Gas distributor.Control Solution temperature is 25 ± 5 DEG C, and the CO of 90 volume % of concentration is passed through from reactor bottom₂Gas carries out plastic reaction, gelling temperature Control adjusts CO at 20-40 DEG C₂Gas flow is 15 ± 2 liters/min, and reaction end pH value is made to reach 8.0- in 4-6 minutes 8.5, that is, stop ventilation, terminates plastic reaction.Gained slurries are heated to 70 DEG C of agings 4 hours, then use vacuum filter Machine is filtered, it is to be filtered it is complete after, supplement is added 20 liters of deionized waters (temperature 70 C) and rinses filter cake about 30 minutes on filter cake. The qualified filter cake of washing is added in 1.5 liters of deionized waters and stirs into slurries, slurries are done with spray dryer is pumped into It is dry, obtain hydrated alumina P1-2.Weighing 300 grams of boehmite P1-2 and 700 grams of boehmite P2-3, (Shandong Aluminum Co., Ltd. is public Take charge of the business boehmite SD powder of production), after mixing, the cloverleaf pattern that circumscribed circle diameter is 1.6 millimeters is extruded into banded extruder Item, 120 DEG C drying 8 hours.Wherein 300 grams are taken, at 800 DEG C, carrier is made in calcination process 4 hours under the conditions of blowing air, wherein Air mass flow is 1.5 standard cubic meters/kilogram hour.100 grams of carrier are weighed, with containing 20.6 grams of nickel nitrate, ammonium paramolybdate 85 milliliters of aqueous solution of 34.8 grams and 1.4 grams of phosphatase 11 impregnate 1.5 hours, 120 DEG C drying 5 hours, 380 DEG C processing 4 hours, so It being impregnated 2 hours with 55 milliliters of aqueous solution containing 8.4 grams of glycerine afterwards, 140 DEG C of dryings obtain hydrogenation catalyst II-3 in 5 hours, In include 3.5 weight % nickel (in terms of NiO), the molybdenum of 19.1 weight % is (with MoO₃Meter), the phosphorus of 4.8% weight % is (with P₂O₅ Meter), 5.7% organic additive, remaining is aluminium oxide.

Embodiment 10

Hydrogenation catalyst II-4's the preparation method is as follows:

Weigh 2000 grams of aluminium hydrate powders (Chang Ling branch company catalyst plant production dry glue powder, 70 weight % of butt) and 299 grams of silica solution (Haiyang Chemical Plant, Qingdao's product) containing silica 25%, being extruded into circumscribed circle diameter with banded extruder is 1.3 millis The butterfly item of rice roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, carrier is made, silica contains in carrier Amount is 5.0 weight %.200 grams of carrier are weighed, 176 milliliters of aqueous solution of the carrier containing 16.9 grams of ammonium fluoride are impregnated 2 hours, 120 DEG C drying 3 hours, 420 DEG C roast 3 hours, be made fluorinated silicon oxide-alumina support.With containing 23.0 grams of ammonium paramolybdate 170 milliliters of aqueous solution dipping above-mentioned carrier 3 hours, 120 DEG C drying 4 hours, then 170 DEG C drying 4 hours, obtain carrier containing molybdenum. Then small with the carrier 3 is impregnated containing 53.2 grams of nickel nitrate, 140.7 grams of ammonium metatungstate, 162 milliliters of aqueous solution of 8.1 grams of phosphatase 11 When, 200 DEG C drying 4 hours, later with containing 121 milliliters of aqueous solution of 77.3 grams of ethylene glycol dippings, 120 DEG C must after drying 6 hours To hydrogenation catalyst II-4, wherein including the nickel (in terms of NiO) of 3.6 weight %, the molybdenum of 5.0 weight % is (with MoO₃Meter), 32.5 The tungsten (in terms of tungsten oxide) of weight %, the fluorine (being calculated with element fluorine) of 2.2 weight %, the phosphorus of 3.0% weight % is (with P₂O₅Meter), The ethylene glycol of 5.0 weight %, remaining is aluminium oxide-silicon oxide.

Embodiment 11-16

In embodiment 11-16, provide using the hydrogenation catalyst and comparative example of the preparation of method provided by the disclosure The desulphurizing activated and denitrification activity of hydrogenation catalyst carry out hydrofinishing evaluation in accordance with the following methods, and commented according to hydrofinishing Valence result computational method is calculated, and evaluation result is as shown in table 2 below.

Using the Middle East straight(-run) diesel distillate of 15% catalytic diesel oil of blending as raw material, property is as shown in table 3, in 30 milliliters of diesel oil Desulfurization, the denitrification activity of catalyst are evaluated on hydrogenation plant, Catalyst packing 30mL, raw material oil-in is located on hydrogenation plant Side, hydrogenation catalyst II are seated in the upper bed layer of hydrogenation plant, and hydrogenation catalyst I (or D1) is seated in leaving the bed for hydrogenation plant Layer, the i.e. downstream of hydrogenation catalyst II.It needs to carry out presulfurization, presulfurization condition are as follows: hydrogen partial pressure to catalyst before the reaction 6.4MPa, 320 DEG C of temperature, liquid hourly space velocity (LHSV) 4h^-1, hydrogen to oil volume ratio 300, sulfurized oil oil inlet speed is 8mL/h.Reaction condition are as follows: Hydrogen partial pressure 6.4MPa, 350 DEG C of reaction temperature, hydrogen to oil volume ratio 300, liquid hourly space velocity (LHSV) 1.5h^-1.It negates respectively and answers 4 hours, reaction 500 hours samples, with sulphur, the nitrogen content in gas Chromatographic Determination raw material and the product of acquisition.

Comparative example 2-4

Catalyst D1, catalyst combination D1+II-1 and catalyst II-1 are carried out to add hydrogen according to the method for embodiment 11-16 Purification evaluation, and calculated according to hydrofinishing evaluation result calculation method, evaluation result is as shown in table 2 below.

Hydrofinishing evaluation result calculation method:

Catalysis is evaluated using the opposite hydrodesulfurization activity relative to reference agent D1 (catalyst prepared in comparative example 1) The hydrodesulfurization activity of agent is handled hydrodesulfurization reaction as 1.65 order reactions, and the reaction speed of catalyst X is calculated by formula (1) Rate constant k (X)_HDS:

Volume space velocity when LHSV is the liquid of hydrocarbon ils when carrying out hydrofining reaction in formula (1).

The hydrodesulfurization activity of the catalyst D1 prepared with comparative example 1 [is denoted as k (D1)_HDS] on the basis of, it is calculated by formula (2) The opposite hydrodesulfurization activity of catalyst X:

Catalysis is evaluated using the opposite hydrodenitrogenationactivity activity relative to reference agent D1 (catalyst prepared in comparative example 1) The hydrodenitrogenationactivity activity of agent handles hydrodenitrogeneration reaction as 1 order reaction, and the reaction rate for calculating catalyst X by formula (3) is normal Number k (X)_HDN:

Volume space velocity when LHSV is the liquid of hydrocarbon ils when carrying out hydrofining reaction in formula (3).

The hydrodenitrogenationactivity activity of the catalyst D1 prepared with comparative example 1 [is denoted as k (D1)_HDN] on the basis of, it is calculated by formula (4) The opposite hydrodenitrogenationactivity activity of catalyst X:

The result of table 2 illustrates that the hydrogenating catalyst composition that the disclosure provides has preferably opposite hydrodesulfurization activity With opposite hydrodenitrogenationactivity activity, and relative activity fall is small in the unit time, and the service life is longer.

Table 1

Table 2

Note: in table 2, "-" expression is not detected.

Table 3

S content	12000μg/g
		N content	220μg/g
Density (20 DEG C)	0.8588g/cm³
		Refraction index (20 DEG C)	1.4841

Claims

1. a kind of hydrogenating catalyst composition, which includes hydrogenation catalyst I and hydrogenation catalyst II；With Stereometer and on the basis of the hydrogenating catalyst composition, the content of the hydrogenation catalyst I are 5-95%；Described plus hydrogen is urged Agent I includes carrier, hydrogenation active metals element and non-metal assistant element, and the hydrogenation active metals element contains Section VI B Race's metallic element and group VIII metallic element；

Wherein, the preparation method of the hydrogenation catalyst I includes:

By load have the carrier of the compound of the element containing hydrogenation active metals, the first organic complexing agent and non-metal assistant element into Row first is dry and roasts, and obtains semi-finished product catalyst；Wherein, in terms of butt and with the dry weight of the semi-finished product catalyst On the basis of, the carbon content of the semi-finished product catalyst is 0.01-0.5 weight %；

Second organic complexing agent is loaded on the semi-finished product catalyst, and carries out second dry and without roasting, is obtained The hydrogenation catalyst I.

2. hydrogenating catalyst composition according to claim 1, wherein in hydrogenator, the hydrogenation catalyst I Type of feed with hydrogenation catalyst II is layering filling or mixed packing；The mode of the layering filling includes: according to raw material The flow direction of oil, the hydrogenation catalyst I is seated in the upstream of the hydrogenation catalyst II, the hydrogenation catalyst II is seated in institute The upstream or the hydrogenation catalyst I for stating hydrogenation catalyst I are loaded with the hydrogenation catalyst II alternatively layered.

3. hydrogenating catalyst composition according to claim 1, wherein the load has the element containing hydrogenation active metals The preparation step of the carrier of compound, the first organic complexing agent and non-metal assistant element includes:

With the aqueous solution dipping of the compound containing the element containing hydrogenation active metals and the first organic complexing agent containing described The carrier of non-metal assistant element；

Alternatively, with compound, non-metal assistant element and the first organic complexing agent containing the element containing hydrogenation active metals Solution impregnating carrier.

4. hydrogenating catalyst composition according to claim 1, wherein in terms of butt and with the semi-finished product catalyst On the basis of dry weight, the carbon content of the semi-finished product catalyst is 0.04-0.4 weight %.

5. hydrogenating catalyst composition according to claim 1, wherein the described first dry condition and described second dry Dry condition includes: that dry temperature is 100-250 DEG C each independently, and the dry time is 1-12 hours；The roasting Condition includes: to carry out under conditions of being passed through oxygen-containing gas, and on the basis of the weight of carrier, the intake of oxygen-containing gas is 0.2- 20 liters/(gram hour)；The temperature of roasting is 350-500 DEG C, and the time of roasting is 0.5-8 hours.

6. hydrogenating catalyst composition according to claim 1, wherein first organic complexing agent and second organic network Mixture includes organic oxygen-containing compound and/or nitrogen-containing organic compound each independently；The organic oxygen-containing compound is organic Alcohol and/or organic acid, the nitrogen-containing organic compound are organic amine and/or organic ammonium salt.

7. hydrogenating catalyst composition according to claim 1, wherein first organic complexing agent and second organic network Mixture includes selected from ethylene glycol, glycerine, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, grass each independently Acid, aminotriacetic acid, 1,2- cyclohexanediamine tetraacetic acid, citric acid, tartaric acid, malic acid, ethylenediamine and ethylenediamine tetra-acetic acid At least one of.

8. hydrogenating catalyst composition according to claim 1, wherein the hydrogenation active metals element and described first The molar ratio of organic complexing agent is 1:(0.03-2).

9. hydrogenating catalyst composition according to claim 1, wherein first organic complexing agent has with described second The molar ratio of machine complexing agent is 1:(0.25-4).

10. hydrogenating catalyst composition according to claim 1, wherein in terms of oxide and with the hydrogenation catalyst I Total weight on the basis of, the content of the hydrogenation active metals element is 6-70 weight %；It urges based on the element and with described plus hydrogen On the basis of the total weight of agent I, the content of the non-metal assistant element is no more than 10 weight %.

11. hydrogenating catalyst composition according to claim 1, wherein the non-metal assistant element is selected from Section IV A At least one of race's element, V Group IIA element, V A race's element and group III A element, the carrier are selected from γ-oxygen Change aluminium, silica, aluminium oxide-silicon oxide, titanium oxide, magnesia, silica-magnesias, silica-zirconia, silica-oxygen Change thorium, silica-berylias, silica-titania, titania-zirconia, silica-alumina thoria, silica-oxygen Change one of aluminium-titanium oxide, silicaalumina-magnesia and silica-alumina, zirconia or a variety of.

12. hydrogenating catalyst composition according to claim 11, wherein the vib metals element be molybdenum and/or Tungsten, the group VIII metallic element are cobalt and/or nickel；The non-metal assistant element is selected from fluorine element, element silicon, phosphorus member At least one of element and boron element.

13. hydrogenating catalyst composition according to claim 1, wherein in terms of oxide and with the hydrogenation catalyst I Total weight on the basis of, the content of the group VIII metallic element is 1-10 weight %, and the vib metals element contains Amount is 5-60 weight %.

14. hydrogenating catalyst composition according to claim 1, wherein the hydrogenation catalyst II contains at least one Vib metals element and at least one group VIII metallic element；In terms of oxide and with the total of the hydrogenation catalyst II On the basis of weight, the content of the group VIII metallic element is 1-10 weight %, and the content of the vib metals element is 5-60 weight %.

15. a kind of method of hydrotreating, this method comprises: by adding described in any one of feedstock oil and claim 1-14 Hydrogen catalyst composition contacts and carries out hydrogenation reaction.

16. according to the method for claim 15, wherein the condition of the hydrogenation reaction includes: that temperature is 300-400 DEG C, Pressure is 1-10 megapascal, and volume space velocity is 0.5-3 hours when the liquid of feedstock oil^-1, hydrogen to oil volume ratio 100-800.

17. according to the method for claim 15, wherein the feedstock oil is selected from gasoline, diesel oil, lubricating oil, kerosene, stone At least one of cerebrol, reduced crude, decompression residuum, pertroleum wax and Fischer-Tropsch synthesis oil.