CN102451706A - Method for preparing hydrogenation catalyst composition - Google Patents

Abstract

The invention discloses a method for preparing a hydrogenation catalyst composition. The method comprises the following steps: preparing a mixture of a NixWyOz composite oxide precursor and an Al2O3 precursor by a coprecipitation method, using sodium meta-aluminate as an aluminum source, introducing a proper amount of CO2 gas during gelling process, beating and mixing with molybdenum oxide and an organic solvent after gelling, molding and drying to obtain the catalyst. The method of the invention is capable of solving the problem of difficult shaping of a bulk phase catalyst and adjusting the physicochemical property of the catalyst, possesses the advantages of large specific surface area, uniform aperture distribution, high effective utilization rate. The catalyst is especially suitable for producing super clean diesel oil in a super deep desulphurization reaction.

Description

The preparation method of hydrogenating catalyst composition

Technical field

The present invention relates to a kind of hydrogenating catalyst composition and preparation method thereof, take off the Preparation of catalysts method of impurity process especially for hydro carbons ultra-deep hydrodesulfuration, denitrogenation etc.

Background technology

Worldwide feedstock oil is further poor qualityization the time; The fuel oil standard is but more harsh to the index of communications and transportation fuel; Over past ten years; Comprise that North America, Europe, Japanese many countries have proposed the notion of ultra-low-sulphur diesel (ULSD) and constantly formulated the content that new fuel oil standard limits sulphur in motor petrol and the diesel oil, aromatic hydrocarbons etc., make the refinery need seek raw catelyst and are guaranteeing to satisfy product needed under the prerequisite of making a profit.

In petroleum distillate, contain the multiple structure sulfur-containing compound different, comprise mercaptan, thioether, thiophenes with molecular weight.These sulfur-containing compounds can carry out hydrogenation and desulphurization reaction and from raw material, remove sulphur atom (for example the sulfide of mercaptan, straight chain and ring-type is converted into saturated hydrocarbons or aromatic compound) under the industrial hydrodesulfurization reaction condition of routine.In deep desulfuration stage (sulfur content is lower than 500 μ g/g) and ultra-deep desulfurization stage (sulfur content is lower than 50 μ g/g), the sulfur-containing compound in the diesel oil distillate is mainly dibenzothiophenes class sulfide.The reactivity of this type sulfide and substituent quantity and position are closely related.4; 6-dimethyl Dibenzothiophene class sulfide is generally the most difficult one type of sulfide that removes; Because and sulphur atom next-door neighbour's methyl make produced between sulphur atom and the activity of such catalysts center sterically hindered, the not accessible reactive activity of sulphur atom center, thereby cause reaction rate to descend significantly.Therefore, realize that deep hydrodesulfurizationof must develop the catalyst that dibenzothiophenes and derivative thereof is had high hydrogenation activity.

Bulk phase catalyst refers to that the loaded catalyst that is dispersed on the carrier with active constituent is relative, is not carrier with inactive carrier.The catalyst major part is made up of active component, and the content of active constituent is generally unrestricted, also claims body catalyst sometimes.

Compare with load hydrogenation catalyst; It is high a lot of that body phase hydrogenation catalyst activated centre density is wanted; Have that superelevation is desulphurizing activated, denitrogenation and arene saturating activity, can under existing refinery device and operating condition, produce and satisfy Europe V standard or do not have the sulfur diesel product, and improve the disposal ability of device greatly; Satisfying factory reduces the basic device investment, solves to install always and expand requirement that can and satisfy new equipment production high-quality oil product; Therefore bulk phase catalyst is owing to can have high tenor, the advantage of strong hydrogenation function, the fine-quality diesel oil that is used for production super-low sulfur, low nitrogen, low aromatic hydrocarbons more and more widely.

The petroleum refining industry of 21st century must follow the strategy of sustainable development, the principle that must pay attention to economic benefit, protection environment simultaneously and economize on resources.Therefore, the preparation method of employing non-environmental-pollution produces bulk phase catalyst and becomes more important.Existing coprecipitation method prepares catalyst technology, uses NH mostly ₃H ₂O is as precipitating reagent, and this will produce the waste water that contains ammonia, nitrogen in a large number, and environment is polluted.

US 4,880, and 526 disclose a kind of Ni of containing, Mo, W, Co high activity is used for bulk phase catalyst of hydrotreatment and preparation method thereof.This method is the preparation alumina gel earlier, and adding contains active metal component solubility salt and mixes dry, roasting then.After also can taking in addition to prepare alumina gel earlier, drying and contains active metal component non-solubility salt and mixes, and rolls, dry, roasting.Perhaps the different activities metal component adopt different above-mentioned dual modes any one prepare.There is the lower problem of using rate of metal in the similar kneading method of this method.

US 6; 299; 760 disclosed methods are a kind of comparatively excellent bulk phase catalysts of hydrotreatment and preparation method thereof that are used for; But in the related Preparation of Catalyst, the moulding of catalyst is adopted and prepared the metal dust that contains Ni-Mo or Ni-Mo-W earlier in its patent, and is bonding or the metal dust of Ni-Mo or Ni-Mo-W mixed dehydration afterwards, extrusion, drying with alumina gel with aluminium oxide again.Because the catalyst metal content of this method preparation is high, often lacks enough interactions between metal and aluminium oxide and can cause catalyst strength poor.Active component part is made up of a large amount of metals, in forming Ni-Mo or Ni-Mo-W powder process, has some interior metal components and can not be fully utilized and cause loss of activity, and this problem can not be able to solution through simple bonding.CN1342102A discloses a kind of mixed metal catalyst, and concrete grammar is for to obtain three kinds of reactive metal co-precipitation, and its main weak point is not find the cooperation effect between the different activities metal.US 6; 162,350, CN 1339985A discloses a kind of mixed metal catalyst composition, and it is solid-state in the preparation process, keeping at least a metal; Form another kind of soild oxide in this solid metallic compound surface reaction, finally form the core-shell type composition.The method can not make different metal obtain good cooperation.

CN1951561A discloses a kind of preparation method of hydrotreatment catalyst, comprising: (1) coprecipitation generates Ni _xW _yO _zThe composite oxides precursor; (2) Ni _xW _yO _zComposite oxides precursor and MoO ₃Making beating mixes, filters; (3) moulding, activation are final catalyst.The precipitating reagent that this method adopts is an Ammonia; The problem that has ammonia and nitrogen pollution, catalyst metal content is high simultaneously, and specific surface area of catalyst is little; The pore structure skewness; Cause the reactive metal bad dispersibility, lack the cooperation effect between the active metal component, can not fully play the hydrogenation performance of its reactive metal.

CN101172261A discloses a kind of hydrogenation catalyst of body phase method preparation, and this catalyst adopts the saline mixed solution and the sodium aluminate solution of reactive metal Ni, W component and auxiliary agent and flows co-precipitation and generates Ni _xW _yO _zThe composite oxides precursor is then with MoO ₃Making beating mixing, filtration, moulding, activation are final catalyst.Aluminium in this method catalyst when having avoided ammoniacal liquor to become glue, produces ammonia, polluted by nitrogen all from sodium metaaluminate.But when having replaced soluble inorganic aluminates such as aluminium chloride, aluminum nitrate when sodium metaaluminate and doing the aluminium source, will reduce a large amount of NO ₃ ^-, Cl ^-Deng heteroion, preparation precipitated metal thing bad adhesion causes the shaping of catalyst difficulty.

CN200710121982.X discloses a kind of multi-metal body catalyst that is used for the diesel oil ultra-deep hydrodesulfuration, and this catalyst group vib metal is present in organic solution with solid form, and the group VIII metal is dissolved in organic solution; Under reflux, adding organic formwork agent high temperature reacts; Because the group VIII metal exists with solid-state form, lack interaction between the metal, reactive metal is not fully utilized; Organic reagent adopts reflux type to reclaim; But at high temperature the part organic reagent decomposes, and has changed the composition of organic reagent, and it is solid-state in the preparation process, keeping a kind of metal; Lack caking property between the metal in the sediment that obtains, be difficult to moulding.

CN101306374A discloses a kind of hydrogenating catalyst composition; This catalyst is prepared by coprecipitation method; With a kind ofly contain the compound of at least a group VIII metal component, compound, organic additive and the water of at least two kinds of group vib metal components is mixed with mixed liquor, adopting the pH of acid or alkali adjustment mixed liquor is 7～11, and said mixed liquor is placed in the agitated reactor; Reaction is 1～24 hour under the airtight condition of room temperature to 250 ℃, filters afterwards and dry.It is under HTHP, to carry out that this catalyst becomes glue to react, high to equipment requirements, has increased the cost of catalyst, and the organic additive that adds appearance decomposition easily under HTHP, can reduce activity of such catalysts like this.Because it is nearly 100% that the activity of such catalysts tenor has reached, the pore volume of catalyst and specific area are less relatively, have also influenced activity of such catalysts, and simultaneously, shaping of catalyst is also difficult relatively.

Existing coprecipitation method prepares catalyst technology, adopts sodium metaaluminate to do aluminium source and precipitating reagent, avoids producing in the catalyst preparation process ammonia, polluted by nitrogen.But because active metallic content is higher; The moulding of bulk phase catalyst becomes bulk phase catalyst and prepares one of process committed step; Contain the caking property that suitable heteroion can increase the precipitated metal thing in the body phase method metalliferous material, help the high material extruded moulding of active metallic content.Do the aluminium source if sodium metaaluminate has replaced soluble inorganic aluminates such as aluminium chloride, aluminum nitrate, aluminum sulfate, will reduce a large amount of NO ₃ ^-, Cl ^-, SO ₄ ^2-Deng heteroion, the composite oxides precursor peptization property of preparation is relatively poor, the metalliferous material difficult forming.Coprecipitation method prepares catalyst, and to also have a difficult point be that the metal mixture grain size difference that obtains of different aluminium source and precipitating reagent is big and then specific area, the intensity of catalyst had considerable influence.In order to reduce pollution, how to solve and adopt sodium metaaluminate to replace the problem that ammoniacal liquor is done the material bad adhesion that the body phase clean method for preparing of precipitating reagent produces.The Ni that how to let coprecipitation method prepare _xW _yO _zComposite oxides and Al ₂O ₃The growth of the mixture uniform crystal particles of precursor makes catalyst have bigger serface, good scattered characteristics of pore structure, reactive metal, improves the big molecule sulfur compound of catalyst removal dibenzothiophenes class hydrogenation activity.How rationally to use organic additive to play one's part to the full, improve the hydrogenation activity of catalyst by a large amount of active metal components in the bulk phase catalyst.

Summary of the invention

Deficiency to prior art; The invention provides a kind of preparation method of hydrogenating catalyst composition; Particularly adopt clean method for preparing, solve the difficult problem of bulk phase catalyst moulding simultaneously, catalyst has than bigger serface and evenly pore size distribution, the high good physico-chemical property of active metal component effective rate of utilization; Bigger pore volume helps big hydrocarbon molecules turnover; Can process heavier raw material, can be used in hydrodesulfurization, the hydrodenitrogeneration reaction, be particularly useful for producing in the ultra-deep desulfurization reaction of ultra clean diesel.

The assorted anion that has appropriate amount in the material, the caking property that increases metalliferous material helps shaping of catalyst.In becoming the glue process, if the negative heteroion of extra adding will be considered so and possibly bring different cations, like metal, H ⁺, NH ₄ ⁺Plasma, these all possibly change composition, the one-tenth glue pH value of catalyst and bring ammonia and nitrogen pollution, and the increase of simultaneously a large amount of ions has also increased the difficulty of washing.Simultaneously, the Ni that obtains of different aluminium source and precipitating reagent _xW _yO _zComposite oxides and Al ₂O ₃The mixture grain size of precursor and then specific area, the intensity of catalyst had considerable influence.Also have an importance, generally contain a large amount of reactive metals in the general bulk phase catalyst, and have the part active metal component not to be utilized in the catalyst.The present invention finds through a large amount of experiments, feeds CO when metallic solution becomes glue with sodium metaaluminate ₂Gas has been avoided adopting conventional ammoniacal liquor to do the ammonia and nitrogen pollution that precipitating reagent brings, and reaction generates HCO ₃ ^-Or CO ₃ ^2-Ion has increased the caking property of metalliferous material, helps shaping of catalyst, can also improve the physico-chemical property of catalyst, adds an amount of organic reagent simultaneously, can let reactive metal plays one's part to the full in the bulk phase catalyst.

The preparation method of hydrogenating catalyst composition according to the invention comprises: (1), coprecipitation generate Ni _xW _yO _zComposite oxides precursor and Al ₂O ₃The mixture of precursor; (2), with mixture, the MoO of step (1) gained ₃Making beating mixes with organic solvent, then filtration, drying; (3), step (2) gained material obtains final catalyst through moulding, drying, wherein step (1) process is following: preparation contains Ni, W component saline mixed solution A, preparation contains the alkaline solution B of aluminium, with material A, material B and CO ₂Gas also flows simultaneously to add and becomes glue in the retort that water purification is housed, and the pH value of controlling the interior slurries of retort is 7.0～9.0, processes composite oxides Ni _xW _yO _zPrecursor and Al ₂O ₃The mixture of precursor wherein adds CO ₂The total amount of gas and the Al that contains among the alkaline solution B of aluminium ₂O ₃Mol ratio is 2～8; The described organic solvent of step (2) is selected from one or more in oxygen-containing organic compound and the organic compounds containing nitrogen, and said organic solvent is 0.1～3.0 with mol ratio in active metal nickel, molybdenum and the tungsten sum of oxide, is preferably 0.3～2.0.

The used oxygen-containing organic compound of step (2) is preferably one or more in organic pure and mild organic acid; For example: one or more in ethylene glycol, glycerine, diethylene glycol, butanediol, the aminotriacetic acid etc.; In the preferred organic amine of organic compounds containing nitrogen one or more, for example: one or more in ethylenediamine, EDTA, tetraethylammonium bromide, tetraethyl ammonium hydroxide, 4-propyl bromide, the softex kw etc.

In the inventive method, the described alkaline solution B that contains aluminium can be inorganic or organic alkaline aluminum contained compound solution, is preferably sodium aluminate solution.

Hydrogenating catalyst composition of the present invention contains Mo, W, three kinds of metal components of Ni, and wherein W, Ni exist with the composite oxides form: Ni _xW _yO _z, z=x+3y, Mo exists with oxide form: MoO ₃, composite oxides Ni _xW _yO _zThe ratio of middle x and y is 1: 8～8: 1, is preferably 1: 4～4: 1, composite oxides Ni _xW _yO _zWith oxide M oO ₃Weight ratio be 1: 10～10: 1, be preferably 1: 5～5: 1.Weight with hydrogenating catalyst composition is benchmark, composite oxides Ni _xW _yO _zWith oxide M oO ₃Gross weight content be 40%～95%, be preferably 45%～85%, alumina content is 5%～60%, is preferably 15%～55%.The specific area of hydrogenating catalyst composition of the present invention is 150～450m ²/ g, pore volume are 0.20～0.60ml/g.

In the inventive method, add required catalyst promoter and/or add component in a step that can be in above-mentioned steps or a few step.Auxiliary agent generally comprises one or more among P, F, Ti, Si, B, the Zr etc.The interpolation component is generally one or more in silica, zirconia, clay, sial, titanium oxide, the magnesia etc.Auxiliary agent and/or the weight content of interpolation component in carbon monoxide-olefin polymeric are 0～50%, are preferably 1%～20%.

It is the aluminium source that the present invention has adopted sodium metaaluminate, becomes to feed proper C O in the glue process ₂Gas makes in the glue thing except forming precipitation of hydroxide, has formed CO after the reaction ₃ ^2-Or HCO ₃ ^-, increased that precipitated metal thing caking property strengthens behind the heteroion, make the easy moulding of catalyst, simultaneously CO ₃ ^2-Or HCO ₃ ^-Can remove during the ion roasting, pollution-free with need not washing, and the Ni that generates _xW _yO _zComposite oxides and Al ₂O ₃The mixture homogeneous grain size of precursor is improved the physico-chemical property of catalyst, has bigger specific area and pore volume, rational pore structure.Simultaneously in roasting process, emit a certain amount of carbon dioxide, under the percussion of gas, not only improved the pore structure of catalyst, but also make more metal active position be exposed to the surface of catalyst, improved the utilization rate of reactive metal.Once more, after the adding appropriate amount of organic, reactive metal is given full play to its effect, has increased substantially its hydrogenation activity.The inventive method is pollution-free in the preparation process; The catalyst easy-formation has bigger specific area and pore volume, reasonably pore size distribution, can original intensive reactive metal decentralization be improved; Fully expose the high hydrogenation sites of Ni-W; Make contain heteroatomic labyrinth hydrocarbon molecule have more multimachine can be near Ni-W high activity center effective hydrogenation, reduce and take off the sterically hindered of impurity, more easily remove impurity.

The specific embodiment

In the inventive method step (1), preparation contains the saline mixed solution of reactive metal Ni, W component, and wherein Ni is 20～80g/L in the weight concentration of NiO, 30～60g/L preferably, and W is with WO ₃The weight concentration of meter is 50～120g/L, preferably 70～100g/L; Contain nickel salt and can be in nickelous sulfate, nickel nitrate, basic nickel carbonate, the nickel chloride one or more, tungstenic salt can be in sodium tungstate, ethyl ammonium metatungstate, the ammonium metatungstate one or more; The weight concentration that preparation contains the alkaline solution of aluminium is 20～80gAl ₂O ₃/ L is preferably 30～60gAl ₂O ₃/ L.

In the inventive method, the one-tenth glue temperature of step (1) is 30～80 ℃, and preferably 40～70 ℃, the time is 0.5～5.0 hour, is preferably 1.0～4.0 hours, and the pH value of slurries is 7.0～9.0 in the retort, CO ₂Gas concentration is 20v%～60v%.Preferably warp is aging after becoming glue, and ageing time is 1.0～5.0 hours, is preferably 0.5～3.0 hour.Can filter or not filter after becoming glue; Add solid molybdenum trioxide, organic solvent making beating mixing then; Filter then and obtain filter cake, filter cake can wash or not wash, and the drying condition of step (2) is following: drying is 0.5～24.0 hour under 5-150 ℃ of condition.

The described drying condition of step (3) was following: 50～200 ℃ of dryings 1～48 hour.

Catalyst of the present invention can add extrusion aid for the ease of moulding.Described extrusion aid is sesbania powder, methylcellulose, starch, polyvinyl alcohol and gathers in the ethanol one or more, preferred sesbania powder.

In the inventive method, the shape of catalyst can be sheet, spherical, cylinder bar and special-shaped bar (clover, bunge bedstraw herb), preferably cylinder bar and special-shaped bar (clover, bunge bedstraw herb) as required.The diameter of carrier can be 0.8～2.0mm slice and＞the thick bar of 2.5mm.

Catalyst of the present invention has higher hydrodesulfurization and hydrodenitrogeneration reactivity worth, can be used for diesel oil hydrogenation ultra-deep desulfurization technology, and this catalyst also can be used in other hydrofinishing and the hydroprocessing technique.

Further specify scheme of the present invention and effect through specific embodiment below.Wt% is a mass fraction.The specific area of catalyst adopts and pore structure adopts the low temperature liquid nitrogen determination of adsorption method, and intensity adopts the side pressure method to measure.

Embodiment 1

In dissolving tank 1, add 500mL water, add 40g nickel chloride, the dissolving of 46g ammonium metatungstate respectively, preparating acid sex work solution A adds 500mL water in dissolving tank 2, adds sodium metaaluminate 30 gram dissolvings then, prepares alkaline working solution B.In retort, add 350mL water, temperature rises to 45 ℃.Under condition of stirring, with solution A, solution B and CO ₂And stream adds one-tenth glue in the retort, CO ₂Concentration is 40v%, becomes 45 ℃ of glue temperature, gelation time 1 hour, and becoming the pH value of rubber cement liquid is 8.5.Become in the glue process and add CO ₂Al among the total amount of gas and the alkaline working solution B ₂O ₃Mol ratio is 3.5, wears out 2 hours behind the one-tenth glue.Filter then, add 600ml water purification, 12.4g molybdenum trioxide and 180 gram tetraethylammonium bromide making beating in the filter cake and stir, filter; Filter cake was 80 ℃ of dryings 5 hours; Extruded moulding then, with water purification washing 3 times, wet bar was 110 ℃ of dryings 5 hours; Obtain final catalyst A, composition and main character are seen table 1.

Embodiment 2

According to the method for embodiment 1, press the constituent content proportioning of the catalyst B in the table 1, in dissolving tank 1, add nickel chloride, ammonium metatungstate and zirconium oxychloride preparating acid sex work solution A, in dissolving tank 2, add sodium metaaluminate alkalescence working solution B then.In retort, add 350mL water, temperature rises to 40 ℃.Under condition of stirring, with solution A, solution B and CO ₂And stream adds one-tenth glue in the retort, CO ₂Concentration is 45v%, becomes 40 ℃ of glue temperature, gelation time 1.5 hours, and becoming the pH value of rubber cement liquid is 7.5.Become in the glue process and add CO ₂Al among the total amount of gas and the alkaline working solution B ₂O ₃Mol ratio is 4.0, wears out 1.5 hours behind the one-tenth glue.Filter then, add 500ml water purification, 10.3g molybdenum trioxide and 210 gram softex kws in the filter cake, making beating stirs; Filter, filter cake is at 70 ℃ of dryings 7 hours, extruded moulding then; With water purification washing 2 times; Wet bar obtains final catalyst B 100 ℃ of dryings 8 hours, forms and main character is seen table 1.

Embodiment 3

According to the method for embodiment 1, press the constituent content proportioning of the catalyst C in the table 1, in dissolving tank 1, add nickel chloride, ammonium metatungstate and phosphorylated ligand relieving haperacidity sex work solution A, in dissolving tank 2, add sodium metaaluminate alkalescence working solution B then.In retort, add 350mL water, temperature rises to 50 ℃.Under condition of stirring, with solution A, solution B and CO ₂And stream adds one-tenth glue in the retort, CO ₂Concentration is 35v%, becomes 50 ℃ of glue temperature, gelation time 1.5 hours, and becoming the pH value of rubber cement liquid is 8.0.Become in the glue process and add CO ₂Al among the total amount of gas and the alkaline working solution B ₂O ₃Mol ratio is 3.0, wears out 2.0 hours behind the one-tenth glue.Filter then, add 500ml water purification, 11.2g molybdenum trioxide and 191 gram aminotriacetic acids in the filter cake, making beating stirs; Making beating stirs, and filters, and filter cake was 120 ℃ of dryings 2 hours; Extruded moulding then; Wet bar obtains final catalyst C 150 ℃ of dryings 5 hours, forms and main character is seen table 1.

Embodiment 4

According to the method for embodiment 1, press the constituent content proportioning of the catalyst D in the table 1, in dissolving tank 1, add nickel chloride, ammonium metatungstate and titanium dioxide preparating acid sex work solution A, in dissolving tank 2, add sodium metaaluminate alkalescence working solution B then.In retort, add 350mL water, temperature rises to 40 ℃.Under condition of stirring, with solution A, solution B and CO ₂And stream adds one-tenth glue in the retort, CO ₂Concentration is 45v%, becomes 40 ℃ of glue temperature, gelation time 2 hours, and becoming the pH value of rubber cement liquid is 7.8.Become in the glue process and add CO ₂Al among the total amount of gas and the alkaline working solution B ₂O ₃Mol ratio is 5.0, wears out 2.5 hours behind the one-tenth glue.Filter then, add 500ml water purification, 13.3g molybdenum trioxide and 120 gram butanediols in the filter cake, making beating stirs; Filter, filter cake is at 80 ℃ of dryings 5 hours, extruded moulding then; With water purification washing 3 times; Wet bar obtains final catalyst D 120 ℃ of dryings 6 hours, forms and main character is seen table 1.

Comparative example 1

Press the disclosed method for preparing catalyst of CN1951558A, preparation is formed identical reference agent E with the catalyst of embodiment 3.

In dissolving tank, add 1000mL water, add nickel chloride 40g, ammonium metatungstate 46g dissolving then, adding solubility again is 10.9g/cm ^-3Liquor alumini chloridi is the phosphoric acid 7.5 gram preparating acid sex work solution A of 85wt% with concentration for 450 milliliters,, preparating acid sex work solution A, the pH value of solution A is 1.8.In retort, add 350mL water, temperature rises to 60 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with 18% ammoniacal liquor, become 60 ℃ of glue temperature, gelation time 0.5 hour, becoming the pH value of glue slurry during is 8.5.Become aging 1 hour of glued bundle back.Filter then, filter cake adds 600ml water purification and 12.4g molybdenum trioxide, and making beating stirs; Filter, filter cake is at 80 ℃ of dryings 5 hours, extruded moulding then; With water purification washing 3 times, wet bar is 120 ℃ of dryings 5 hours, 500 ℃ of roastings 4 hours; Obtain final catalyst E, composition and main character are seen table 1.

Comparative example 2

Press the disclosed method for preparing catalyst of CN101172261A, preparation is formed identical reference agent F with the catalyst of embodiment 3.

In dissolving tank 1, add 500mL water, 40g nickel chloride, 46g ammonium metatungstate stir and make its dissolving, and adding concentration again is phosphoric acid 7.5 grams of 85wt%, is mixed with acid working solution A.In dissolving tank 2, add 500mL water, add sodium metaaluminate 37g dissolving then, be mixed with alkaline working solution B.In retort, add 350mL water, temperature rises to 50 ℃.Under condition of stirring, solution A is also become glue in the stream adding retort with solution B, become 50 ℃ of glue temperature, gelation time 2 hours, becoming the pH value of glue slurry during is 7.5.Add the 12.4g molybdenum trioxide then, making beating stirs, and filters, and filter cake was 120 ℃ of dryings 1 hour; Extruded moulding then, with water purification washing 3 times, wet bar was 130 ℃ of dryings 3 hours; 600 ℃ of roastings 3 hours, obtain final catalyst F, composition and main character are seen table 1.

Comparative example 3

Press embodiment 3 catalyst and form and the preparation method, do not add organic reagent, preparation reference agent G.Composition and main character are seen table 1.

Embodiment 5

Present embodiment is a catalyst activity evaluation experimental of the present invention, and compares with the Comparative Examples catalyst.Adopt A of the present invention, C catalyst and Comparative Examples E, F, G catalyst, on the 200ml small hydrogenation device, carry out comparative evaluation's test, test raw material is Maoming mixed diesel.The raw material main character sees Table 2, and catalyst activity is estimated process conditions and evaluation result sees Table 3.Adopt gas-chromatography-atomic emission spectrum detector (GC-AED) to detect sulfur compound in the hydrofined oil, the result sees table 4.

Can find out that from catalyst preparation process reference agent F becomes glue process of preparing metalliferous material bad adhesion, clover can't moulding during extrusion, have to the cylinder moulding, and material particles is big, intensity difference.See from catalyst property, adopt the catalyst of the inventive method preparation, have bigger serface and pore volume, reasonably pore size distribution.Can find out that from the evaluation test result catalyst of the present invention is removing 4, demonstrate high hydrogenation activity during the big molecule sulfide of 6-DMDBT class.The catalyst of the inventive method preparation has especially shown more tangible removal effect to having sterically hindered sulfide; Have excellent hydrogenation and desulphurizing ability; Can be used in the hydrodesulfurization reaction, be particularly useful for producing the ultra-deep desulfurization reaction of ultra clean diesel.

Table 1 catalyst is formed and character

Table 2 feedstock oil main character

Project	Analysis result
		Density (20 ℃), g/cm 3	0.8614
The boiling range scope, ℃	178-373
		S，μg/g	12200
N，μg/g	288
		Cetane number	46.5

Table 3 catalyst hydrogenation desulphurization reaction process conditions and evaluation result

The content of different sulfide in table 4 hydrofined oil

Catalyst	A	C	E	F	G
						Sulfur content in the hydrofined oil, μ g/g	6.1	5.3	74.1	81.5	21.5
?C 1-DBT，μg/g	0	0	0	0	0
						?4-BMDBT，μg/g	0	0	10.6	12.1	1.2
?6-BMDBT，μg/g	0	0	11.5	17.6	1.5
						?4，6-BMDBT，μg/g	1.6	1.2	32.3	31.5	12.3
?2，4，6-BMDBT，μg/g	4.5	4.1	19.7	20.3	6.5

Claims (15)

1. the preparation method of a hydrogenating catalyst composition comprises: (1), coprecipitation generation Ni _xW _yO _zComposite oxides precursor and Al ₂O ₃The mixture of precursor; (2), with mixture, the MoO of step (1) gained ₃Mix making beating with organic solvent, then filtration, drying; (3), step (2) gained material obtains final catalyst through moulding, drying, wherein step (1) process is following: preparation contains Ni, W component saline mixed solution A, preparation contains the alkaline solution B of aluminium, with material A, material B and CO ₂Gas also flows simultaneously to add and becomes glue in the retort that water purification is housed, and the pH value of controlling the interior slurries of retort is 7.0～9.0, processes composite oxides Ni _xW _yO _zPrecursor and Al ₂O ₃The mixture of precursor wherein adds CO ₂The total amount of gas and the Al that contains among the alkaline solution B of aluminium ₂O ₃Mol ratio is 2～8; The described organic solvent of step (2) is selected from one or more in oxygen-containing organic compound and the organic compounds containing nitrogen, and said organic solvent is 0.1～3.0 with mol ratio in active metal nickel, molybdenum and the tungsten sum of oxide.

2. according to the described method of claim 1, it is characterized in that said organic solvent and mol ratio in active metal nickel, molybdenum and the tungsten sum of oxide are 0.3～2.0.

3. according to the described method of claim 1, it is characterized in that the used oxygen-containing organic compound of step (2) is one or more in organic pure and mild organic acid; Organic compounds containing nitrogen is one or more in the organic amine.

4. according to the described method of claim 3; It is characterized in that used oxygen-containing organic compound is one or more in ethylene glycol, glycerine, diethylene glycol, butanediol, the aminotriacetic acid, organic compounds containing nitrogen is one or more in ethylenediamine, EDTA, tetraethylammonium bromide, tetraethyl ammonium hydroxide, 4-propyl bromide, the softex kw.

5. according to the described method of claim 1, it is characterized in that the described alkaline solution B that contains aluminium is a sodium aluminate solution.

6. according to claim 1 or 5 described methods, it is characterized in that described hydrogenating catalyst composition, contain Mo, W, three kinds of metal components of Ni, wherein W, Ni exist with the composite oxides form: Ni _xW _yO _z, z=x+3y, Mo exists with oxide form: MoO ₃, composite oxides Ni _xW _yO _zThe ratio of middle x and y is 1: 8～8: 1, composite oxides Ni _xW _yO _zWith oxide M oO ₃Weight ratio be 1: 10～10: 1; Weight with hydrogenating catalyst composition is benchmark, composite oxides Ni _xW _yO _zWith oxide M oO ₃Gross weight content be 40%～95%, alumina content is 5%～60%.

7. according to claim 1 or 5 described methods, it is characterized in that described hydrogenating catalyst composition, contain Mo, W, three kinds of metal components of Ni, wherein W, Ni exist with the composite oxides form: Ni _xW _yO _z, z=x+3y, Mo exists with oxide form: MoO ₃, composite oxides Ni _xW _yO _zThe ratio of middle x and y is 1: 4～4: 1, composite oxides Ni _xW _yO _zWith oxide M oO ₃Weight ratio be 1: 5～5: 1; Weight with hydrogenating catalyst composition is benchmark, composite oxides Ni _xW _yO _zWith oxide M oO ₃Gross weight content be 45%～85%, alumina content is 15%～55%.

8. according to claim 1 or 6 described methods; It is characterized in that; Add required catalyst promoter and/or add component in a step in step (1), (2) and (3) or a few step; Auxiliary agent comprises one or more among P, F, Ti, Si, B, the Zr, and the interpolation component is one or more in silica, zirconia, clay, sial, titanium oxide, the magnesia; Described auxiliary agent and/or the weight content of interpolation component in carbon monoxide-olefin polymeric are 1%～20%.

9. according to claim 1 or 6 described methods, it is characterized in that in the step (1) that the saline mixed solution that contains reactive metal Ni, W component wherein Ni is 20～80g/L in the weight concentration of NiO, W is with WO ₃The weight concentration of meter is 50～120g/L; The weight concentration that preparation contains the alkaline solution of aluminium is 20～80gAl ₂O ₃/ L.

10. according to claim 1 or 6 described methods; It is characterized in that in the step (1); It is in nickelous sulfate, nickel nitrate, basic nickel carbonate, the nickel chloride one or more that preparation contains the used nickel salt that contains of the saline mixed solution of reactive metal Ni, W component, and tungstenic salt is one or more in sodium tungstate, ethyl ammonium metatungstate, the ammonium metatungstate.

11. according to claim 1 or 6 described methods, it is characterized in that the one-tenth glue temperature of step (1) is 30～80 ℃, the time is 0.5～5.0 hour, becoming glue pH value is 7.0～9.0.

12., it is characterized in that said CO according to claim 1 or 6 described methods ₂The concentration of gas is 20v%～60v%.

13. according to claim 1 or 6 described methods, it is characterized in that wearing out after step (1) becomes glue, ageing time is 1.0～5.0 hours.

14. according to claim 1 or 6 described methods, it is characterized in that step (2) drying condition is following: drying is 0.5～24.0 hour under 50～150 ℃ of conditions.

15., it is characterized in that the described drying condition of step (3) is following: 50～200 ℃ of dryings 1～48 hour according to claim 1 or 6 described methods.