CN106179463B - Hydrocracking catalyst and its preparation method - Google Patents

Abstract

The invention discloses a kind of hydrocracking catalysts and preparation method thereof.The catalyst is body phase hydrocracking catalyst, and composition includes hydrogenation active metal component W and Ni, aluminium oxide, silica, rare-earth oxide and molecular sieve；Wherein table phase active metal component WO₃Weight content and body phase active metal component WO₃Weight content ratio be 1.2:1~6.0:The weight content of 1, table phase active metal component NiO are 1.2 with the ratio of the weight content of body phase active metal component NiO:1~5.0:1.The catalyst is especially suitable in single-stage hydrocracking technical process, having many advantages, such as liquid yield height, good product quality.

Description

Hydrocracking catalyst and its preparation method

Technical field

The present invention relates to a kind of hydrocracking catalysts and preparation method thereof for the treatment of of heavy hydrocarbon class.

Background technology

Currently, worldwide petroleum resources are insufficient, crude quality is deteriorated year by year, and intermediate oil demand increases, Petroleum chemicals upgrade and environmental regulation is more and more stringent, heavy oil lighting are greatly facilitated, and constitute accelerated development The very strong driving force of hydrogen addition technology.Be mainly characterized by adaptability to raw material strong, products scheme, the selection of purpose product of hydrocracking technology Property high, good product quality and added value it is high, can directly produce a variety of high-quality oil products（Such as gasoline, jet fuel, diesel oil, profit Lubricant base oil etc.）With high-quality industrial chemicals（Such as benzene,toluene,xylene, ethylene production raw material）.

It is hydrocracked and carries out at elevated pressures, hydrocarbon molecules carry out cracking and adding hydrogen in catalyst surface with hydrogen Reaction generates the conversion process of lighter molecule, while the hydrogenation reaction of hydrodesulfurization, denitrogenation and unsaturated hydrocarbons also occurs.Hydro carbons exists Cracking reaction in hydrocracking process is carried out on the acid centre of catalyst, it then follows carbon ion reaction mechanism, add hydrogen, With the generation of hydro carbons isomerization reaction while cracking reaction.Hydrocracking catalyst is made of hydrogenation component and acidic components , the two is added by a certain percentage as needed, makes that hydrogen and cracking performance is added to reach balance, effect is that hydrocarbon mixture is abundant Add hydrogen, cracking and isomerization orientation reaction.Therefore, the catalyst that distillate hydrocracking process needs should have stronger plus hydrogen There is moderate acid centre in activated centre again.

In general, following method can be used to prepare for hydrocracking catalyst, such as：Infusion process, kneading method, beating method, altogether The precipitation method may use ion-exchange for noble metal.Infusion process and kneading method are all made of first by carrier and acidic components Afterwards again plus metal, and coprecipitated rule to be acidic components and metal coprecipitation get off, and metal loading is unrestricted.It is such The hydrogenation sites of catalyst be on the catalyst channel surfaces that reactant molecule can approach, and coprecipitation method prepare urge Agent active metal is not fully present in catalyst channel surfaces, and amount of activated metal is present in caltalyst phase, coprecipitated The tenor that method prepares catalyst table phase decides catalyst activity.

US6299760, US6156695, US6537442, US6440888, US6652738 disclose containing group VIII/ VI B races active metal component is used for the bulk phase catalyst and preparation method thereof of hydrotreating.Catalyst metal content can reach 50wt%~100wt%.Active metal component can be Ni-Mo or Ni-Mo-W.Above-mentioned catalyst is prepared using coprecipitation method.US Hydrocracking catalyst disclosed in 3954671, hydrogenation conversion catalyst disclosed in US 4313817 are resistance to disclosed in CN1253988A The hydrocracking catalyst of nitrogen type fecund intermediate oil, heavy hydrocarbons hydrocraking catalyst disclosed in CN1253989A, this A little catalyst are prepared using coprecipitation method, since the deposition condition of different hydrogenation active metals is different, cause different plus hydrogen The distribution of active metal is not easily controlled, between the distribution and different activities metal to influence different hydrogenation active metals and Interaction relationship between active metal and carrier, to prevent hydrogenation activity with cracking activity from being coordinated well, Meanwhile these caltalyst phase active metallic contents are more, table phase active metallic content is relatively fewer, hydrogenation sites density Smaller, final influence catalyst is hydrocracked performance.High activity, High middle distillate, which are hydrocracked, disclosed in CN101239324A urges Agent is the addition precipitating reagent alkalescent ammoniac compounds into the slurries that amorphous silica-alumina, auxiliary agent and active metal are made into, and is carried out Then precipitation reaction is added molecular sieve suspension and is made.This method is also to be prepared using coprecipitation method, however it remains table is mutually lived Property tenor it is relatively fewer, hydrogenation sites density is smaller, and different hydrogenation active metals are unevenly distributed, hydrogenation activity gold Belong to and interactively coordinates bad problem between carrier.

CN103055923A discloses a kind of preparation method of hydrocracking catalyst.Using containing hydrogenation active metals acidity Solution, sodium metaaluminate alkaline solution and gas CO₂Plastic in the retort equipped with water purification is added in cocurrent；Then Y type molecules are added The suspension of sieve is uniformly mixed, and hydrocracking catalyst is made through filtering, drying, molding, then washed, dry, roasting.The party Method increases Kong Rong, the specific surface area of catalyst, makes using the releasing of gas in roasting process under the percussion of gas More metal active positions are exposed to the surface of catalyst, but such method can make cell channels collapse, pore size distribution disperse, machinery Strength reduction, and lead to active metal localized clusters, the metal active position being exposed is limited.

Coprecipitation method prepares catalyst technology, can be to duct table in catalyst using different coprecipitation modes, Gelation Conditions etc. On face between active metallic content and activated centre density, the distribution of different hydrogenation active metals and difference hydrogenation active metals Interaction relationship between hydrogenation active metals and carrier has a great impact.The coprecipitation method of above-mentioned use can make different plus hydrogen The distribution of active metal is not easily controlled, to influence different hydrogenation active metals distribution and different hydrogenation active metals it Between interaction relationship between active metal and carrier, to prevent hydrogenation activity with cracking activity from being matched well It closes, meanwhile, table phase active metallic content is smaller in catalyst and activated centre density is relatively low, and final influence catalyst adds hydrogen to split Change performance.Therefore, the distribution for how regulating and controlling hydrogenation active metals, makes between hydrogenation active metal component and hydrogenation active metals There is suitable mating reaction between component and carrier, it is close how to increase table phase active metallic content and activated centre in catalyst Degree, improves the utilization rate of hydrogenation active metal component, is the key that improve coprecipitation method to prepare hydrocracking catalyst Hydrogenation.

Invention content

In view of the deficiencies of the prior art, the present invention provides a kind of body phase hydrocracking catalysts and preparation method thereof.It should Method improve catalyst in hydrogenation active metals distribution, improve hydrogenation active metals between and the cooperation between carrier Effect improves catalyst surface active bit density, improves the utilization rate of hydrogenation active metals, while catalyst pore structure is reasonable, Active metal disperses evenly, catalyst to be made to have higher performance.

Hydrocracking catalyst of the present invention is body phase hydrocracking catalyst, and composition includes hydrogenation active metal component W With Ni, aluminium oxide, silica, rare-earth oxide and molecular sieve；Wherein table phase active metal component WO₃Weight content with Body phase active metal component WO₃Weight content ratio be 1.2:1~6.0:1, preferably 1.8:1~4.5:1, table phase active metal The ratio of the weight content of component NiO and the weight content of body phase active metal component NiO is 1.2:1~5.0:1, preferably 1.5 ~ 3.5:1。

In hydrocracking catalyst of the present invention, on the basis of the weight of catalyst, WO₃With the total content of NiO be 20%~ 65%, preferably 30%~50%, W/Ni atomic ratio are 0.05~1.0, preferably 0.1~0.7, the content of silica is 1%~ The content of 40%, preferably 5%~35%, aluminium oxide is 10%~40%, preferably 15%~40%, and rare earth metal is in terms of oxide Content is 1wt%~15wt%, preferably 3wt%~10wt%, and the content of molecular sieve is 5wt%~20wt%, preferably 5wt%~ 15wt%。

In the present invention, table phase active metal component WO₃Weight content be table phase in WO₃Weight content, body mutually activity gold Belong to component WO₃Weight content be catalyst in WO₃Weight content；The weight content of table phase active metal component NiO is table phase The weight content of middle NiO, the weight content of body phase active metal component NiO are the weight content of NiO in catalyst.

The property of hydrocracking catalyst of the present invention is as follows：Specific surface area is 250~650m²/ g, Kong Rongwei 0.35~ 0.80mL/g, pore-size distribution are as follows：Kong Rong shared by a diameter of holes below 4nm accounts for the 1% ~ 20% of total pore volume, a diameter of 4 ~ 8nm Hole shared by Kong Rong to account for total pore volume be 55% ~ 80%, the Kong Rong shared by the hole of a diameter of 8 ~ 15nm accounts for the 2% ~ 20% of total pore volume, directly It is 0.1% ~ 5.0% that the Kong Rong that diameter is 15nm or more, which accounts for total pore volume, and preferred pore-size distribution is as follows：A diameter of holes below 4nm Shared Kong Rong accounts for the 5% ~ 17% of total pore volume, and it is 61% ~ 75% that Kong Rong, which accounts for total pore volume, shared by the hole of a diameter of 4 ~ 8nm, and a diameter of 8 Kong Rong shared by the hole of ~ 15nm accounts for the 4% ~ 17% of total pore volume, the Kong Rong of a diameter of 15nm or more account for total pore volume be 0.5% ~ 5.0%。

In hydrocracking catalyst of the present invention, adjuvant component can also be contained, the adjuvant component is the IVth B races metal, Content of the IVth B family metal oxides in hydrocracking catalyst is 1wt%~10wt%.IVth B races metal is preferably Ti and/or Zr.

The preparation method of hydrocracking catalyst of the present invention, including：

（1）, prepare the mixed solution A containing Ni, Al component, precipitating reagent, which is added dropwise to solution A, carries out plastic reaction, and generation contains Nickel, aluminum precipitation object slurries I；

（2）, prepare the mixed solution B containing W, Si, Al component, precipitating reagent and solution B cocurrent are subjected to plastic reaction, generated Tungstenic, silicon, aluminum precipitation object slurries II；

（3）, by step（1）The slurries I and step of gained（2）The slurries II of gained is uniformly mixed, under agitation always Change, after aging, be filtered, washed, obtained material is added when carrying out hydro-thermal process, wherein hydro-thermal process with water vapour to be urinated Element；

（4）, step（3）After being beaten uniformly the suspension of molecular sieve is added, containing dilute in obtained material under stirring condition Native ion（RE³⁺）It with the mixed liquor of organic compound, stirs evenly, filters, obtain material through drying, molding, washing；

（5）, step（4）Hydrocracking catalyst is made through dry and roasting in resulting material.

The preferred Y type molecular sieve of institute's addition molecular sieve in the method for the present invention.Y type molecular sieve is usually with molecular sieve suspension Form is added, i.e., molecular sieve is ground to the mesh of 80 mesh ~ 140, and the mesh of preferably 100 mesh ~ 120, then plus suspension is made in water.Described Y type molecular sieve is the Y type molecular sieve used in conventional hydrocracking catalyst.

Step（1）Or step（2）Described in precipitating reagent be sodium carbonate, sodium bicarbonate, ammonium hydroxide, sodium hydroxide, hydroxide It is one or more in potassium, potassium carbonate, saleratus, preferably ammonium hydroxide.

Step（1）In mixed solution A, weight concentrations of the Ni in terms of NiO be 5~80g/L, preferably 10~60g/L, Al with Al₂O₃The weight concentration of meter is 10~80g/L, preferably 20~60g/L.Step（2）In mixed solution B, W is with WO₃The weight of meter A concentration of 10~100g/L, preferably 20~90g/L.Si is with SiO₂Weight concentration is 10~120g/L, preferably 20~80g/L , Al is with Al₂O₃The weight concentration of meter is 10~80g/L, preferably 20~60g/L.When preparing mixed solution A, generally use Nickel source can be one or more of nickel sulfate, nickel nitrate, basic nickel carbonate, nickel chloride, and silicon source can be aluminum nitrate, sulfuric acid One or more of aluminium, aluminium chloride or aluminium acetate etc..When preparing mixed solution B, the tungsten source generally used can be ethyl One or more of ammonium metatungstate, ammonium metatungstate；Silicon source can be one or more in Ludox, sodium metasilicate；Silicon source can be with For one or more of aluminum nitrate, aluminum sulfate, aluminium chloride or aluminium acetate etc..

Step（1）Middle reaction temperature is 20~90 DEG C, preferably 30~70 DEG C.When cemented into bundles pH value control for 6.0 ~ 11.0, preferably 7.0 ~ 9.0.Gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

Step（2）Weight contents of Si, the Al of middle introducing in terms of oxide in the catalyst is 5wt%~70wt%, preferably 10wt%~90wt% of the total weight of Si, Al in terms of oxide is accounted in terms of silica for 10wt%~55wt%, wherein Si, preferably 30wt%~80wt%；Step（1）Weight contents of the Al of middle introducing in terms of oxide in the catalyst is 5wt%~45wt%, compared with It is 10wt%~30wt% well.

Step（2）Middle reaction temperature is 30~90 DEG C, preferably 40~80 DEG C.When cocurrent plastic pH value control for 6.0 ~ 11.0, preferably 7.0 ~ 9.0.Gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

Step（1）And step（2）Middle gelling temperature and time can be the same or different.Step（1）And step（2）It can It can not also be carried out simultaneously with being carried out at the same time.

Step（3）Middle aging temperature is 40~90 DEG C, preferably 50~80 DEG C.PH value control is 6.0 ~ 10.0 when aging, Preferably 6.5 ~ 9.0.Ageing time is 0.5 ~ 6.0 hour, preferably 1.0 ~ 4.0 hours.

Step（3）Described in hydrothermal conditions it is as follows：It is carried out under closed container, temperature is 200 ~ 300 DEG C, excellent 210 ~ 260 DEG C are selected as, pressure is 1.0 ~ 8.0MPa, and preferably 3.0 ~ 6.0MPa, processing time is 0.5 ~ 10.0 hour, preferably 1.0 ~ 6.0 hours.

Step（3）In, when hydro-thermal process, active metal in the addition and catalyst of urea（Tungsten, nickel）Atom total amount Molar ratio is 0.5：1~10.0：1, preferably 2.0：1~8.0:1.

Step（4）The one kind or more of the organic compound in oxygen-containing organic compound and organic compounds containing nitrogen Kind.Wherein oxygen-containing organic compound is preferably one or more of Organic Alcohol, aldehyde and ester, such as：Ethylene glycol, glycerine, two It is one or more in ethylene glycol, butanediol, dodecanol, hexadecanol, pyroracemic aldehyde, diglyceride, triglycerides etc., it is nitrogenous The preferred organic amine of organic compound, such as：One or both of ethylenediamine, nitrilotriacetic acid (NTA).The rare earth is It is one or more in lanthanum, cerium, praseodymium, rubidium.Step（4）Described contains RE³⁺In the mixed liquor of organic compound, RE³⁺Weight A concentration of 0.01%~4.0%, preferably 0.5%~3.0%, a concentration of 0.05~5.0 mol/L of organic compound, preferably 0.5~3.0mol/L.Rare earth ion（RE³⁺）With the mixeding liquid volume and step of organic compound（3）Obtained volume of material Than being 1.0~2.0, preferably 1.0~1.5.Organic compound and the hydrogenation active metals in terms of oxide（Tungsten and nickel）Total amount Molar ratio is 0.1 ~ 3.0, preferably 0.3 ~ 2.0.Step（4）The suspension of molecular sieve is added, contains rare earth ion（RE³⁺）With it is organic After the mixed liquor of compound, the time of stir process is 1.0~10.0h, and preferably 3.0~7.0h, the temperature of stir process is 20 Between~90 DEG C, preferably 30~70 DEG C.

Step（4）The drying, molding, washing may be used this field conventional method and carry out.The drying is general It is 1 ~ 48 hour dry at 50 ~ 200 DEG C.In forming process, it can be added conventional shaping assistant as needed, such as peptizing agent, It is one or more in extrusion aid etc..The peptizing agent is one or more in hydrochloric acid, nitric acid, sulfuric acid, acetic acid, oxalic acid etc., The extrusion aid refer to be conducive to one kind in the substance of extrusion forming, such as sesbania powder, carbon black, graphite powder, citric acid or Several, the dosage of auxiliary agent accounts for 1wt%~10wt% of total material butt.Washing is usually used deionized water or contains decomposable asymmetric choice net salt Class（Such as ammonium acetate, ammonium chloride, ammonium nitrate）Solution washs, and is washed till neutrality.The shape of the molding, catalyst can be according to need To be sheet, spherical, cylindrical bars and irregular bar（Clover, bunge bedstraw herb）, preferably cylindrical bars and irregular bar（Clover, four leaves Grass）.The diameter of carrier can be the slice of 0.8 ~ 2.0mm and the thick item of ＞ 2.5mm.

Step（5）This field normal condition may be used in the drying and roasting, and such as at 50 ~ 200 DEG C, drying 1 ~ 48 is small When, 1 ~ 24 hour, preferably 2 ~ 8 hours are roasted at 450 ~ 600 DEG C.

In hydrocracking catalyst of the present invention, adjuvant component can also be contained, the adjuvant component is the IVth B races metal, Content of the IVth B family metal oxides in hydrocracking catalyst is 1wt%~10wt%.IVth B races metal is preferably Ti and/or Zr.In hydrocracking catalyst preparation process of the present invention, preferably it is added to contain during preparing mixed solution A and helps The compound of agent component, i.e. titanium source and/or zirconium source.One kind or more in Titanium Nitrate, titanium sulfate, titanium chloride etc. can be used in titanium source Kind, zirconium source can be used one or more in zirconium nitrate, zirconium chloride, zirconium oxychloride etc..

In hydrocracking catalyst of the present invention, all in the prior art can be used for plus hydrogen can be used in Y type molecular sieve used Y type molecular sieve in Cracking catalyst, such as：CN101343068A、CN1508228A、CN101450319A、CN 1209357A Disclosed in Y type molecular sieve.Y type molecular sieve disclosed in the preferred CN101343068A of the present invention, property are as follows：Compare table Area is 700m²/ g~950m²/ g, preferably 800~950m²/ g, total pore volume is 0.30mL/g~0.55mL/g, opposite to crystallize Degree is 90%~130%, SiO₂/Al₂O₃Molar ratio is 30~150, preferably 50~150, and cell parameter is 2.425~2.445nm, Meleic acid amount is 0.1~1.0mmol/g, and B Suan ∕ L acid is 7.0 or more, preferably 8.0 or more, sodium oxide content≤0.05wt%, Preferably≤0.01wt%.

Hydrocracking catalyst of the present invention is the body phase hydrocracking catalyst of oxidation state, and conventional side can be used before use Method carries out presulfurization.

The heavy charge range that catalyst prepared by the method for the present invention is applicable in is very wide, they include vacuum gas oil (VGO), coking The various hydrocarbon ils such as gas oil, deasphalted oil, thermal cracking gas oil, catalytic gas oil, catalytic cracking recycle oil, can also group It closes and uses, the hydro carbons that raw material is usually 250~550 DEG C containing boiling point, nitrogen content can be in 50~2500 μ g/g.

The method of the present invention uses positive addition（The acid precipitation method, that is, alkaline precipitating agent is added in acid metal salt solution and carries out Precipitation）Nickel aluminium mixed sediment is prepared, tungsten, silicon and aluminium mixed sediment are prepared using parallel flow precipitation, then after the two is mixed Aging.The present invention prepares the relatively large nickel of crystal grain, aluminum precipitation object by using positive addition, and it is relatively small that cocurrent process prepares crystal grain Tungsten, silicon and aluminum precipitation object, above two sediment is mixed, and can control the distribution of different hydrogenation active metals, is conducive to live Property tungsten, nickel between form high activity phase, and improve the interaction between active metal and carrier, being hydrocracked for gained made to urge The hydrogenation activity of agent obtains good cooperation with cracking activity, improves the performance of hydrocracking catalyst.

In the preparation method of catalyst of the present invention, steam treatment is simultaneously under appropriate conditions for the material that is obtained after co-precipitation Urea is added, urea is decomposed into NH under high temperature environment₃And CO₂, NH₃And CO₂NH is generated in the presence of water vapour₄ ⁺With HCO₃ ^-Ion, NH₄ ⁺And HCO₃ ^-Ion at high temperature under high pressure has a significant impact the microscopic pattern of material, material before hydro-thermal process Phase structure is in cylinder, and material phase structure is changed into the irregular body that irregular sheet is piled into from cylinder after hydro-thermal process, this The transformation of structure makes distribution of the active metal in table phase obviously increase, and disperses evenly, is conducive to improve surface work The density of property position.In addition, urea is added in steam treatment, make the transformation of material form that can also make the pore size distribution of catalyst More uniformly, be conducive to improve the mechanical strength of catalyst.

By containing the material after urea hydro-thermal process, containing rare earth ion in the present invention（RE³⁺）And organic compound Mixed solution processing, the distribution of different hydrogenation active metals can be promoted, be conducive to be formed between active metal tungsten, nickel in table phase High activity phase, while rare earth metal being made to be come into full contact with hydrogenation active metals in table phase, improve active metal and the phase between carrier Interaction makes the hydrogenation activity of the hydrocracking catalyst of gained obtain good cooperation with cracking activity.

In catalyst of the present invention, different hydrogenation active metals have good distribution, and surface-active bit density is big, activity Intermetallic cooperation is good, and active metal utilization rate is high, and improves the interaction between active metal and carrier, makes gained The hydrogenation activity of hydrocracking catalyst obtains good cooperation with cracking activity, while catalyst pore structure is reasonable, and machinery is strong Degree is high, has excellent hydrogenation cracking activity.

The present invention is using rare earth contained hydrocracking catalyst made of preferred Y type molecular sieve particularly suitable as senior middle school's oil Type hydrocracking catalyst not only has high hydrogenation cracking activity, but also has high middle distillates oil selectivity, while also having relatively strong resistance to The good performance such as nitrogen ability.Catalyst of the present invention is suitable for single hop once by hydrocracking process, hydrogen being added to split It is as follows to change operating condition：Reaction temperature is 300~500 DEG C, more preferably 350~450 DEG C；Pressure be 6~20MPa, more preferably 13 ~17MPa；Volume space velocity is 0.5~3 h when liquid^-1, preferably 0.8~1.5 h^-1；Hydrogen to oil volume ratio is 400~2000:1, most It is well 800~1500:1.The catalyst is used in single-stage hydrocracking technical process, has liquid yield height, good product quality The advantages that.

Specific implementation mode

In the present invention, specific surface area and Kong Rong use low temperature liquid nitrogen physisorphtion, and relative crystallinity and cell parameter are adopted With x-ray diffraction method, silica alumina ratio uses chemical method, sodium content to use plasma emission spectrometry, and mutually activity is golden for catalyst table Belong to content and uses x-ray photoelectron spectroscopy（XPS）It measures, caltalyst phase active metallic content uses inductively coupled plasma Body atomic emission spectrum（ICP-AES）It measures, transmission electron microscope（TEM catalyst surface WS) is measured₂Density.Mechanical strength is to use What side pressure method measured.In the present invention, wt% is mass fraction, and v% is volume fraction.

Embodiment 1

Nickel chloride, liquor alumini chloridi and zirconium oxychloride are dissolved in water purification respectively, are configured to mixed solution A, in mixed solution A The weight concentration of NiO is 21g/L, Al₂O₃Weight concentration be 5g/L, ZrO₂Weight concentration 5g/L.Respectively by ammonium metatungstate, Liquor alumini chloridi is dissolved in water purification, and dilute water glass solution is added, and is configured to mixed solution B, WO in mixed solution B₃Weight concentration For 25g/L, Al₂O₃Weight concentration be 18g/L, SiO₂Weight concentration be 20g/L.The ammonium hydroxide of a concentration of 10wt% is being stirred Lower addition solution A, gelling temperature are maintained at 55 DEG C, at the end of pH value control 7.6, gelation time control was generated at 60 minutes Nickeliferous, aluminum precipitation object slurries I.1000mL water purifications are added in retort, the ammonium hydroxide of a concentration of 10wt% and solution B cocurrent are added Enter in retort, gelling temperature is maintained at 55 DEG C, and 7.6, gelation time control exists for pH value control in cocurrent plastic reaction process 60 minutes, generate tungstenic, silicon, aluminum precipitation object slurries II.Aging after above two is mixed containing sediment slurry, ageing time 2 are small When, 75 DEG C of aging temperature, pH value is controlled 7.6 at the end of aging, is then filtered, washed, filter cake is in the water vapour containing urea Lower carry out hydro-thermal process, the condition of hydro-thermal process are：The molar ratio of urea and active metal atom total amount is 7:1, temperature 230 DEG C, pressure 4.5MPa, processing time is 3 hours, is beaten filter cake after processing, is added that account for catalyst total into mix slurry The Y type molecular sieve suspension of weight 10wt% is in terms of butt（It is prepared by CN101343068A embodiments 7）It is dilute with lanthanum, cerium, praseodymium and rubidium Earthmetal cations（On the basis of rare-earth oxide total weight, La₂O₃Account for 48.1%, CeO₂Account for 44.7%, Pr₂O₅5.8% is accounted for, Nd₂O₃Account for 1.4%）With the mixed solution of triglycerides, handle 5 hours（RE in mixed solution³⁺Weight concentration 2.5wt%, it is organic A concentration of 2.1 mol/L of compound), treatment temperature is 50 DEG C, and mixed solution is 1.0 with volume of material ratio, filtering, 100 It DEG C dry 8 hours, rolls, extruded moulding.It is washed at room temperature with water purification.Then 10 hours dry at 80 DEG C, 550 DEG C of roastings 4 are small When, obtain catalyst A.Catalyst composition, pore size distribution and main character are shown in Table 1.

Embodiment 2

According to the method for embodiment 1, is matched by the constituent content of the catalyst B in table 1, nitric acid is added into dissolving tank 1 Nickel, titanium chloride, aluminum nitrate solution prepare working solution A, after into dissolving tank 2, addition aluminum nitrate, ammonium metatungstate are dissolved in water purification, Dilute waterglass is added and prepares working solution B.Solution A is added in the ammonium hydroxide of a concentration of 15wt% under stiring, gelling temperature is maintained at 45 DEG C, at the end of pH value control 8.0, gelation time control generated nickeliferous, aluminum precipitation object slurries I at 60 minutes.By 800mL Water purification is added in retort, the ammonium hydroxide of a concentration of 15wt% and solution B cocurrent is added in retort, gelling temperature is maintained at 50 DEG C, 8.2, gelation time control generated tungstenic, silicon, aluminum precipitation object at 60 minutes for pH value control in cocurrent plastic reaction process Slurries II.Aging after above two is mixed containing sediment slurry, ageing time 3 hours, 70 DEG C of aging temperature, pH at the end of aging Then value control is filtered 8.0, wash, and filter cake carries out hydro-thermal process, the condition of hydro-thermal process under the water vapour containing urea For：The molar ratio of urea and active metal atom total amount is 6:1, temperature is 250 DEG C, pressure 3.5MPa, and processing time is 3 small When, filter cake is beaten after processing, the Y type molecular sieve suspension for accounting for total catalyst weight 12wt% is added to slurries（In terms of butt） （It is prepared by CN101343068A embodiments 7）With lanthanum, cerium, praseodymium metal ion（On the basis of rare-earth oxide total weight, La₂O₃Account for 40.3%, CeO₂Account for 52.1%, Pr₂O₅Account for 7.6%）Rare earth ion and pyroracemic aldehyde mixed solution in processing it is 7 small When（RE in mixed solution³⁺Weight concentration 2.8wt%, a concentration of 2.5 mol/L of organic compound）, treatment temperature is 40 DEG C, Mixed solution is 1.2 with volume of material ratio, filtering, 7 hours dry at 120 DEG C, is rolled, extruded moulding.It is washed at room temperature with water purification It washs.Then 12 hours dry at 100 DEG C, 500 DEG C roast 5 hours, obtain catalyst B.Catalyst composition, pore size distribution and main property Matter is shown in Table 1.

Embodiment 3

According to the method for embodiment 1, is matched by the constituent content of the catalyst C in table 1, chlorination is added into dissolving tank 1 Nickel, liquor alumini chloridi prepare working solution A, and after addition aluminium chloride, ammonium metatungstate are dissolved in water purification into dissolving tank 2, dilute water is added Glass prepares working solution B.Solution A is added in the ammonium hydroxide of a concentration of 10wt% under stiring, gelling temperature is maintained at 55 DEG C, knot 7.6, gelation time control generated nickeliferous, aluminum precipitation object slurries I at 90 minutes for pH value control when beam.It is added in retort and fills There are 900mL water purifications, the ammonium hydroxide of a concentration of 10wt% and solution B cocurrent are added in retort, gelling temperature is maintained at 45 DEG C, and Flowing pH value control in plastic reaction process, 8.0, gelation time control generated tungstenic, silicon, aluminum precipitation object slurries at 60 minutes II.Above two is mixed containing sediment slurry.Aging after above two is mixed containing sediment slurry, ageing time 2.5 hours, always Change 72 DEG C of temperature, pH value is controlled 7.8 at the end of aging, is then filtered, washed, filter cake carries out under the water vapour containing urea The condition of hydro-thermal process, hydro-thermal process is：The molar ratio of urea and active metal atom total amount is 4:1, temperature is 240 DEG C, pressure Power is 6.0MPa, and processing time is 4 hours, is beaten filter cake after processing, and total catalyst weight is accounted for the addition of sediment slurries The Y type molecular sieve suspension of 15wt%（In terms of butt）（It is prepared by CN101343068A embodiments 7）With lanthanum, cerium mischmetal metal from Son（On the basis of rare-earth oxide total weight, La₂O₃Account for 53.1%, CeO₂Account for 46.9%）With the mixed solution of hexadecanol Middle processing 4 hours（RE in mixed solution³⁺Weight concentration 1.8wt%, a concentration of 2.4mol/L of organic compound）, processing temperature Degree is 60 DEG C, and mixed solution is 1.1 with volume of material ratio, filtering, 10 hours dry at 70 DEG C, is rolled, extruded moulding.Room is then 8 hours dry at 80 DEG C, 530 DEG C roast 4.5 hours, obtain catalyst C.Catalyst composition, pore size distribution and main character are shown in Table 1。

Embodiment 4

According to the method for embodiment 1, is matched by the constituent content of the catalyst D in table 1, chlorination is added into dissolving tank 1 Nickel, liquor alumini chloridi, preparating acid sex work solution A are added after into dissolving tank 2, addition aluminium chloride, ammonium metatungstate are dissolved in water purification Dilute waterglass preparating acid sex work solution B.Solution A is added in the ammonium hydroxide of a concentration of 10wt% under stiring, gelling temperature is maintained at 50 DEG C, at the end of pH value control 7.6, gelation time control generated nickeliferous, aluminum precipitation object slurries I at 80 minutes.Reaction is added 1000mL water purifications are housed in tank, the ammonium hydroxide of a concentration of 10wt% and solution B cocurrent are added in retort, gelling temperature is maintained at 55 DEG C, 8.0, gelation time control generated tungstenic, silicon, aluminum precipitation at 60 minutes for pH value control in cocurrent plastic reaction process Object slurries II.Above two is mixed containing sediment slurry.Aging after above two is mixed containing sediment slurry, ageing time 2 are small When, 75 DEG C of aging temperature, pH value is controlled 7.8 at the end of aging, is then filtered, filter cake carries out under the water vapour containing urea The condition of hydro-thermal process, hydro-thermal process is：The molar ratio of urea and active metal atom total amount is 3.0:1, temperature is 260 DEG C, Pressure is 5.0MPa, and processing time is 5 hours, is beaten filter cake after processing, and it is total to account for catalyst to the mixing addition of sediment slurries The Y type molecular sieve suspension of weight 8wt%（In terms of butt）（It is prepared by CN101343068A embodiments 7）With lanthanum, cerium, praseodymium, rubidium gold Belong to ion（On the basis of the total weight of rare-earth oxide, La₂O₃Account for 45.5%, CeO₂Account for 36.5%, Pr₂O₅15.2% is accounted for, Nd₂O₃Account for 2.8%）It is handled 6 hours with the mixed solution of nitrilotriacetic acid（RE in mixed solution³⁺Weight concentration 2.0wt%, have A concentration of 2.8 mol/L of machine compound）, treatment temperature is 35 DEG C, and mixed solution is 1.0 with volume of material ratio, filtering, 80 It DEG C dry 10 hours, rolls, extruded moulding.It is washed at room temperature with water purification, then 10 hours dry at 110 DEG C, 480 DEG C of roastings 6 Hour, obtain catalyst D.Catalyst composition, pore size distribution and main character are shown in Table 1.

Comparative example 1

It is prepared according to method disclosed in CN101239324A, catalyst composition forms identical with embodiment 1, and specific steps are such as Under：

(1) by Al₂O₃220 milliliters of the liquor alumini chloridi of a concentration of 120g/L, containing the nickel chloride solution 18 that NiO is 44g/L Milliliter contains ZrO₂50 milliliters of 100g/L zirconyl chloride solutions are mixed in the container of a 5L, and 2000 milliliters of water purification dilutions are added；

(2) dilute water glass solution is prepared, SiO is contained₂310 milliliters of the water glass solution of 100g/L under agitation will (2) it is added in (1)；

(3) ammonium hydroxide is added to (1) under agitation with the mixture of (2) until pH value 5.2；

(4) 240 milliliters of sodium tungstate solution is prepared, WO is contained₃For 80g/L, and be added under agitation (1)+(2)+ (3) in mixture；

(5) ammonium hydroxide is continuously added until pH value is 7.6；

(6) entire plastic process should be carried out at 55 DEG C；

(7) mixture stands aging 2.0 hours at 75 DEG C, and pH value control is 7.6 at the end of aging；It is added and accounts for before aging The Y type molecular sieve suspension of total catalyst weight 10wt%（In terms of butt）（It is prepared by CN101343068A embodiments 7）, Y types point Son sieve property is shown in Table 6,

(8) it filters, in 100 DEG C of oven dryings 8 hours, rolls, with 3 millimeters of orifice plate extruded moulding of diameter；At room temperature It is washed with the ammonium acetate solution of pH=8.8；Then in 80 DEG C of oven dryings 10 hours, 550 DEG C roast 4 hours, obtain reference agent E, Catalyst composition, pore size distribution and main character are shown in Table 1.

Comparative example 2

It is added without urea by 1 catalyst of embodiment composition and preparation method, when hydro-thermal process, prepares reference agent F.Catalyst Composition, pore size distribution and main character are shown in Table 1.

Comparative example 3

By 1 catalyst of embodiment composition and preparation method, when hydro-thermal process, is added without urea, but NH is added₃, NH₃And work Property metallic atom total amount molar ratio be 7:1, temperature is 230 DEG C, pressure 4.5MPa, and processing time is 3 hours, prepares reference Agent G.Catalyst composition, pore size distribution and main character are shown in Table 1.

Comparative example 4

By 1 catalyst of embodiment composition and preparation method, when hydro-thermal process, is added without urea, but CO is added₂, CO₂And work Property metallic atom total amount molar ratio be 7:1, temperature is 230 DEG C, pressure 4.5MPa, and processing time is 3 hours, prepares reference Agent H.Catalyst composition, pore size distribution and main character are shown in Table 1.

Comparative example 5

It is prepared by method disclosed in CN103055923A, catalyst composition forms identical with embodiment 1, and specific steps are such as Under：

(1) acid solution A is prepared：It is formed by 1 catalyst of embodiment, nickel chloride, ammonium metatungstate, zirconium oxychloride is mixed In one 5 liters of container, 1000 milliliters of water purification dilutions are added.It prepares containing with SiO in embodiment 1₂The identical dilute water glass of content Glass solution is added under agitation in mixing salt solution above.

(2) configuration alkaline solution B：Configuration is containing the same as Al in embodiment 1₂O₃The identical alkaline sodium aluminate solution of content 3000mL。

(3) by solution A, solution B and CO₂Plastic in plastic cans is added in gas cocurrent, and gelling temperature is maintained at 55 DEG C, pH Value is 7.6.CO wherein used₂Gas concentration is 45v%, and CO is added₂Al in the total amount and alkaline solution of gas₂O₃Molar ratio 3, A, B solution flow velocity are adjusted, ensure while being dripped off, to ensure that it is constant that catalyst distribution uniformly forms.

(4) after cemented into bundles, in the case where being stirred continuously, the Y type molecular sieve for accounting for total catalyst weight 10wt% is added Suspension（In terms of butt）（It is prepared by CN101343068A embodiments 7）, Y type molecular sieve property is shown in Table 6, it made to be dispersed in In the mixed serum that plastic obtains, aging 2 hours are stood at 75 DEG C or so.

(5) it filters, it is 8 hours dry at 100 DEG C, it rolls, extruded moulding.It is washed at room temperature with water purification.Then it is done at 80 DEG C Dry 10 hours, 550 DEG C roasted 4 hours, obtain catalyst I.Catalyst composition, pore size distribution and main character are shown in Table 1.

Embodiment 5

By middle oil type hydrocracking catalyst A, B, C, D of the present invention and reference catalyst E, F, G, H, I in midget plant Upper evaluation result is compared.Evaluation condition is：React stagnation pressure 14.7MPa, hydrogen to oil volume ratio 1200, volume space velocity when liquid 1.5h^-1, evaluation is Iranian VGO heavy distillates with raw material, and main character is shown in Table 4, and table 5 lists evaluation result.

From table 2 and table 3 as can be seen that catalyst table phase active metallic content prepared by the method for the present invention is apparently higher than body phase Active metallic content, activity mutually increases considerably in catalyst.It can be seen that the catalysis prepared using the present invention from the data of table 5 The activity and middle distillates oil selectivity of agent A, B, C, D are better than reference agent, illustrate catalyst activity metal profit prepared by the method for the present invention With rate height, catalyst reaction activity significantly improves.

1 catalyst of table forms and property

Catalyst is numbered	A	B	C	D	E
						Catalyst forms
NiO, wt%	20	16	18	24	20
						WO3, wt%	24	26	20	18	24
SiO2, wt%	19	18	20	20	19
						Al2O3, wt%	22	21	27	30	22
Y molecular sieve, wt%	10	12	15	8	10
						Other/wt%	ZrO2/5.0	TiO2/7.0	-	-	ZrO2/5.0
Catalyst property
						Specific surface area, m2/g	391	383	385	392	288
Kong Rong, mL/g	0.404	0.389	0.394	0.413	0.285
						Mechanical strength, N/mm	22.9	21.9	23.1	22 .3	19.7
Pore size distribution, %
						＜ 4nm	15.18	16.12	15.31	14.19	52.33
4nm~8nm	65.68	65.61	66.41	67.57	44.15
						8nm~15nm	15.41	14.31	15.49	15.34	1.41
＞ 15nm	3.73	3.96	2.79	2.90	2.11

Continued 1

Catalyst is numbered	F	G	H	I
					Catalyst forms
NiO, wt%	20	20	20	20
					WO3, wt%	24	24	24	24
SiO2, wt%	19	19	19	19
					Al2O3, wt%	22	22	22	22
Y molecular sieve, wt%	10	10	10	10
					Other/wt%	ZrO2/5.0	ZrO2/5.0	ZrO2/5.0	ZrO2/5.0
Catalyst property
					Specific surface area, m2/g	382	379	385	312
Kong Rong, mL/g	0.365	0.373	0.394	0.355
					Intensity, N/mm	19.5	18.9	18.2	17.8
Pore size distribution, %
					＜ 4nm	28.35	24.41	25.54	14.25
4nm~8nm	34.47	38.96	33.74	35.42
					8nm~15nm	23.98	22.51	24.91	36.84
＞ 15nm	13.20	14.12	15.81	13.49

The weight content of the weight content and body phase reactive metal oxides of 2 catalyst table phase reactive metal oxides of table The ratio between

Catalyst is numbered	A	B	C	D	E
						Table phase IW/ body phase IW	4.31	3.98	3.75	2.65	0.99
Table phase INi/ body phase INi	3.45	3.56	2.92	2.54	0.94

Continued 2

Catalyst is numbered	F	G	H	I
					Table phase IW/ body phase IW	1.05	1.13	1.16	1.22
Table phase INi/ body phase INi	1.07	1.18	1.14	1.18

3 catalyst surface WS of table₂Density

Catalyst is numbered	A	B	C	D	E	F	G	H	I
										WS2Density, grain/100nm	81	79	75	78	39	46	45	45	47

4 feedstock oil main character of table

Project	Analysis result
		Density (20 DEG C), g/cm3	0.9113
Boiling range range, DEG C	314-539
		S, μ g/g	9800
N, μ g/g	1710
		Carbon residue, wt%	0.14
Condensation point, DEG C	34
		Cetane number	43.9

5 evaluating catalyst result of table

Catalyst is numbered	A	B	C	D	E
						Reaction temperature, DEG C	388	389	390	389	397
Product distribution, wt%
						Light naphthar（C5~82℃）	5.4	5.9	5.3	5.5	6.9
Heavy naphtha（82~138℃）	9.2	9.0	9.3	9.4	9.9
						Jet fuel（138℃~249℃）	27.4	26.3	26.7	26.1	23.0
Diesel oil（249℃~371℃）	26.7	28.5	28.1	27.9	24.5
						Tail oil（>371℃）	31.5	30.3	30.6	31.1	35.7
Middle distillates oil selectivity, wt%	79.0	78.6	78.9	78.3	73.8

Continued 5

Catalyst is numbered	F	G	H	I
					Reaction temperature, DEG C	397	398	396	397
Product distribution, wt%
					Light naphthar（C5~82℃）	5.9	5.8	6.6	5.8
Heavy naphtha（82~138℃）	9.9	10..6	9.5	10.0
					Jet fuel（138℃~249℃）	23.1	23.6	23.9	23.1
Diesel oil（249℃~371℃）	25.1	23.5	23.7	24.2
					Tail oil（>371℃）	36.1	36.5	36.3	36.9
Middle distillates oil selectivity, wt%	75.4	74.2	74.7	74.9

The property of Y type molecular sieve used in 6 embodiment of the present invention of table and comparative example

Molecular sieve property	Y
		Relative crystallinity, %	117
Cell parameter, nm	2.429
		SiO2/Al2O3Molar ratio	80.4
Specific surface area, m2/g	876
		Kong Rong, mL/g	0.493
Infrared total acid, mmol/g	0.240
		B Suan ∕ L acid	11.36
Na2O, wt%	<0.01

Claims (37)

1. a kind of hydrocracking catalyst, which is body phase hydrocracking catalyst, and composition includes hydrogenation active metals Component W and Ni, aluminium oxide, silica, rare-earth oxide and molecular sieve；Wherein table phase active metal component WO₃Weight Content and body phase active metal component WO₃Weight content ratio be 1.2:1~6.0:1, the weight of table phase active metal component NiO The ratio for measuring content and the weight content of body phase active metal component NiO is 1.2:1~5.0:1；The aperture of the hydrocracking catalyst Distribution is as follows：Kong Rong shared by a diameter of holes below 4nm accounts for the 1% ~ 20% of total pore volume, Kong Rong shared by the hole of a diameter of 4 ~ 8nm It is 55% ~ 80% to account for total pore volume, and the Kong Rong shared by the hole of a diameter of 8 ~ 15nm accounts for the 2% ~ 20% of total pore volume, a diameter of 15nm or more Kong Rong to account for total pore volume be 0.1% ~ 5.0%.

2. catalyst described in accordance with the claim 1, it is characterised in that：In the hydrocracking catalyst, table phase active metal Component WO₃Weight content and body phase active metal component WO₃Weight content ratio be 1.8:1~4.5:1, table phase active metal The ratio of the weight content of component NiO and the weight content of body phase active metal component NiO is 1.5 ~ 3.5:1.

3. catalyst described in accordance with the claim 1, it is characterised in that：In the hydrocracking catalyst, with the weight of catalyst On the basis of amount, WO₃Total content with NiO is that 20%~65%, W/Ni atomic ratios are 0.05~1.0, and the content of silica is 1wt% The content of~40wt%, aluminium oxide are 10wt%~40wt%, and the content of rare-earth oxide is 1wt%~15wt%, molecular sieve Content is 5wt%~20wt%.

4. catalyst described in accordance with the claim 1, it is characterised in that：In the hydrocracking catalyst, with the weight of catalyst On the basis of amount, WO₃Total content with NiO is that 30%~50%, W/Ni atomic ratios are 0.1~0.7, the content of silica be 5wt%~ The content of 35wt%, aluminium oxide are 15wt%~40wt%, and the content of rare-earth oxide is 3wt%~10wt%, and molecular sieve contains Amount is 5wt%~15wt%.

5. catalyst described in accordance with the claim 1, it is characterised in that：The molecular sieve is Y type molecular sieve, and property is as follows： Specific surface area is 700m²/ g~950m²/ g, total pore volume are 0.30mL/g~0.55mL/g, and relative crystallinity is 90%~130%, SiO₂/Al₂O₃Molar ratio is 30~150, and cell parameter is 2.425~2.445nm, and meleic acid amount is 0.1~1.0mmol/g, B Suan ∕ L acid is 7.0 or more, sodium oxide content≤0.05wt%.

6. according to any catalyst of claim 1-5, it is characterised in that：The property of the hydrocracking catalyst is such as Under：Specific surface area is 250~650m²0.35~0.80mL/g of/g, Kong Rongwei.

7. according to any catalyst of claim 1-5, it is characterised in that：The pore-size distribution of the hydrocracking catalyst It is as follows：Kong Rong shared by a diameter of holes below 4nm accounts for the 5% ~ 17% of total pore volume, and Kong Rong is accounted for always shared by the hole of a diameter of 4 ~ 8nm Kong Rong is 61% ~ 75%, and the Kong Rong shared by the hole of a diameter of 8 ~ 15nm accounts for the 4% ~ 17% of total pore volume, the hole of a diameter of 15nm or more It is 0.5% ~ 5.0% that appearance, which accounts for total pore volume,.

8. according to any catalyst of claim 1-5, it is characterised in that：In the hydrocracking catalyst, containing helping Agent component, the adjuvant component are Ti and/or Zr, content in terms of oxide in hydrocracking catalyst for 1wt%~ 10wt%。

9. the preparation method of any catalyst of claim 1-7, including：

（1）, prepare the mixed solution A containing Ni, Al component, by precipitating reagent be added dropwise to solution A carry out plastic reaction, generate it is nickeliferous, Aluminum precipitation object slurries I；

（2）, prepare the mixed solution B containing W, Si, Al component, precipitating reagent and solution B cocurrent are subjected to plastic reaction, generation contains Tungsten, silicon, aluminum precipitation object slurries II；

（3）, by step（1）The slurries I and step of gained（2）The slurries II of gained is uniformly mixed, aging under agitation, always After change, urea is added when carrying out hydro-thermal process, wherein hydro-thermal process with water vapour in filtering, obtained material；

（4）, step（3）Obtained material through be beaten uniformly after, under stirring condition be added molecular sieve suspension, containing rare earth from The mixed liquor of son and organic compound, stirs evenly, and filters, obtains material through drying, molding, washing；

（5）, step（4）Through dry and roasting, hydrocracking catalyst is made again in resulting material.

10. according to the method for claim 9, it is characterised in that：Institute's addition molecular sieve is Y type molecular sieve, and molecular sieve is suspended Molecular sieve is ground to the mesh of 80 mesh ~ 140 by liquid, and then plus suspension is made in water.

11. according to the method for claim 10, it is characterised in that：Institute's addition molecular sieve is Y type molecular sieve, and molecular sieve is suspended Molecular sieve is ground to the mesh of 100 mesh ~ 120 by liquid, and then plus suspension is made in water.

12. according to the method for claim 9, it is characterised in that：Step（1）Or step（2）Described in precipitating reagent be carbon It is one or more in sour sodium, sodium bicarbonate, ammonium hydroxide, sodium hydroxide, potassium hydroxide, potassium carbonate, saleratus.

13. according to the method for claim 12, it is characterised in that：Step（1）Or step（2）Described in precipitating reagent be ammonia Water.

14. according to the method for claim 9, it is characterised in that：Step（1）In mixed solution A, weight of the Ni in terms of NiO A concentration of 5~80g/L, Al is with Al₂O₃The weight concentration of meter is 10~80g/L.

15. according to the method for claim 14, it is characterised in that：Step（1）In mixed solution A, weight of the Ni in terms of NiO A concentration of 10~60g/L, Al is with Al₂O₃The weight concentration of meter is 20~60g/L.

16. according to the method for claim 9, it is characterised in that：Step（2）In mixed solution B, W is with WO₃The weight of meter is dense Degree is 10~100g/L, and Si is with SiO₂Weight concentration is 10~120g/L, and Al is with Al₂O₃The weight concentration of meter is 10~80g/L.

17. according to the method for claim 16, it is characterised in that：Step（2）In mixed solution B, W is with WO₃The weight of meter is dense Degree is 20~90g/L, and Si is with SiO₂Weight concentration is 20~80g/L, and Al is with Al₂O₃The weight concentration of meter is 20~60g/L.

18. according to the method for claim 9, it is characterised in that：Step（1）Middle reaction temperature is 20~90 DEG C, when plastic Between be 0.2 ~ 4.0 hour, pH value control is 6.0 ~ 11.0 when cemented into bundles.

19. according to the method for claim 18, it is characterised in that：Step（1）Middle reaction temperature is 30~70 DEG C, when plastic Between be 0.5 ~ 3.0 hour, pH value control is 7.0 ~ 9.0 when cemented into bundles.

20. according to the method for claim 9, it is characterised in that：Step（2）Si, Al of middle introducing are being urged in terms of oxide Weight content in agent is 10wt%~70wt%, and wherein Si accounts for the total weight of Si, Al in terms of oxide in terms of silica 10wt%~90wt%；Step（1）Weight contents of the Al of middle introducing in terms of oxide in the catalyst is 5wt%~45wt%.

21. according to the method for claim 20, it is characterised in that：Step（2）Si, Al of middle introducing are being urged in terms of oxide Weight content in agent is 20wt%~55wt%, and wherein Si accounts for the total weight of Si, Al in terms of oxide in terms of silica 30wt%~80wt%；Step（1）Weight contents of the Al of middle introducing in terms of oxide in the catalyst is 10wt%~30wt%.

22. according to the method for claim 9, it is characterised in that：Step（2）Middle reaction temperature be 30~90 DEG C, cocurrent at PH value control is 6.0 ~ 11.0 when glue, and gelation time is 0.2 ~ 4.0 hour.

23. according to the method for claim 22, it is characterised in that：Step（2）Middle reaction temperature be 40~80 DEG C, cocurrent at PH value control is 7.0 ~ 9.0 when glue, and gelation time is 0.5 ~ 3.0 hour.

24. according to the method for claim 9, it is characterised in that：Step（3）Middle aging temperature is 40~90 DEG C, when aging PH value control is 6.0 ~ 10.0, and ageing time is 0.5 ~ 6.0 hour.

25. according to the method for claim 24, it is characterised in that：Step（3）Middle aging temperature is 50~80 DEG C, when aging PH value control is 6.5 ~ 9.0, and ageing time is 1.0 ~ 4.0 hours.

26. according to the method for claim 9, it is characterised in that：Step（3）Described in hydrothermal conditions it is as follows： It is carried out under closed container, temperature is 200 ~ 300 DEG C, and pressure is 1.0 ~ 8.0MPa, and processing time is 0.5 ~ 10.0 hour；Step （3）In, when hydro-thermal process, the molar ratio of active metal atom total amount is 0.5 in the addition and catalyst of urea：1~10.0： 1。

27. according to the method for claim 26, it is characterised in that：Step（3）Described in hydrothermal conditions it is as follows： It is carried out under closed container, temperature is 210 ~ 260 DEG C, and pressure is 3.0 ~ 6.0MPa, and processing time is 1.0 ~ 6.0 hours；Step （3）In, when hydro-thermal process, the molar ratio of active metal atom total amount is 2.0 in the addition and catalyst of urea：1~8.0:1.

28. according to the method for claim 9, it is characterised in that：Step（4）The organic compound is selected from oxygen-containing organic One or more in conjunction object and organic compounds containing nitrogen, wherein oxygen-containing organic compound is one kind in Organic Alcohol, aldehyde and ester Or it is several, organic compounds containing nitrogen is organic amine；The rare earth is one or more in lanthanum, cerium, praseodymium, rubidium.

29. according to the method for claim 28, it is characterised in that：The oxygen-containing organic compound is selected from ethylene glycol, the third three It is one or more in alcohol, diethylene glycol, butanediol, dodecanol, hexadecanol, pyroracemic aldehyde, diglyceride, triglycerides, Organic compounds containing nitrogen is selected from one or both of ethylenediamine, nitrilotriacetic acid.

30. according to the method for claim 9, it is characterised in that：Step（4）Described contains rare earth ion and organic compound Mixed liquor in, rare earth ion RE³⁺Weight concentration be 0.01%~4.0%, a concentration of 0.05~5.0mol/ of organic compound L。

31. according to the method for claim 30, it is characterised in that：Step（4）Described contains rare earth ion and organic compound In the mixed liquor of object, rare earth ion RE³⁺Weight concentration be 0.5%~3.0%, a concentration of 0.5~3.0mol/ of organic compound L。

32. according to the method for claim 9, it is characterised in that：Step（4）It is described containing rare earth ion and organic compound Mixeding liquid volume and step（3）Obtained volume of material ratio is 1.0~2.0, organic compound and in terms of oxide plus hydrogen The molar ratio of active metal tungsten and nickel total amount is 0.1 ~ 3.0, step（4）The suspension of molecular sieve is added, containing rare earth ion and has After the mixed liquor of machine compound, the time of stir process is 1.0~10.0h, and the temperature of stir process is between 20~90 DEG C；Step Suddenly（4）The drying is 1 ~ 48 hour dry at 50 ~ 200 DEG C.

33. according to the method described in claim 32, it is characterised in that：Step（4）It is described to contain rare earth ion and organic compound Mixeding liquid volume and step（3）Obtained volume of material ratio is 1.0~1.5, organic compound and adding in terms of oxide The molar ratio of hydrogen activity tungsten and nickel total amount is 0.3 ~ 2.0, step（4）The suspension of molecular sieve is added, containing rare earth ion and After the mixed liquor of organic compound, the time of stir process is 3.0~7.0h, and the temperature of stir process is between 30~70 DEG C.

34. according to the method for claim 9, it is characterised in that：Step（5）The drying and roasting condition is as follows： 50 ~ 200 DEG C of dryings 1 ~ 48 hour, roast 1 ~ 24 hour at 450 ~ 600 DEG C.

35. according to the method for claim 9, it is characterised in that：It is molten mixing in hydrocracking catalyst preparation process The compound containing adjuvant component, i.e. titanium source and/or zirconium source are added in liquid A, titanium source is using in Titanium Nitrate, titanium sulfate, titanium chloride One or more, zirconium source is using one or more in zirconium nitrate, zirconium chloride, zirconium oxychloride.

36. a kind of method for hydrogen cracking, it is characterised in that use any catalyst of claim 1-8.

37. according to the method described in claim 36, it is characterised in that：Using single hop once by hydrocracking process, adding Hydrogen cracking operation condition is as follows：Reaction temperature is 300~500 DEG C, and pressure is 6~20MPa, when liquid volume space velocity be 0.5~ 3.0h^-1, hydrogen to oil volume ratio is 400~2000:1.