CN106179381A - The preparation method of Hydrobon catalyst - Google Patents

Abstract

The invention discloses the preparation method of a kind of Hydrobon catalyst.This catalyst is body phase Hydrobon catalyst, its composition includes hydrogenation active metals component W, Ni and Mo, aluminium oxide, its preparation method is to carry out plastic containing addition sodium metaaluminate alkaline solution in Ni component saline solution A to react to obtain serosity I, carry out and flow plastic reacting to obtain serosity II with sodium metaaluminate alkaline solution containing W, Mo component saline mixed solution B, serosity I and serosity II mix homogeneously, hydrothermal treatment consists is carried out after aging, wherein add carbamide during hydrothermal treatment consists, then make Hydrobon catalyst through steps such as molding.The catalyst that the method prepares has higher hydrodesulfurization and hydrodenitrogeneration reactivity worth, particularly suitable application in diesel oil distillate ultra-deep hydrodesulfuration, denitrification reaction.

Description

The preparation method of Hydrobon catalyst

Technical field

The present invention relates to the preparation method of a kind of Hydrobon catalyst, the preparation method of the most highly active body phase hydrotreating catalyst.

Background technology

At present the most worldwide, crude oil heaviness increasingly and in poor quality, the sustainable development of World Economics and the increasingly stringent of environmental regulation, need to produce a large amount of light clean fuel in addition.Exploitation and to use super-low sulfur be even to clean the trend that fuel develops in the range of the world today without sulfur vapour, diesel oil.Traditional Hydrobon catalyst is used such as to improve reaction temperature, hydrogen dividing potential drop by increasing reaction severity or reduce reaction velocity etc., the deep desulfuration even ultra-deep desulfurization of diesel oil can also be realized, but the rising of reaction temperature can cause the variation of product colour and catalyst life to shorten, and reduces air speed and then means the minimizing for the treatment of capacity.For existing hydrogenation plant, its design pressure is the most fixing, and the amplitude improving hydrogen dividing potential drop is limited.Therefore, current is one of the important means of deep desulfuration by using the catalyst of more high desulfurization activity.

Containing various structures and the sulfur-containing compound of different molecular weight in petroleum distillate, but at ultra-deep desulfurization stage (sulfur content is less than 50 g/g), mainly removing 4, the sulfur-containing compound of the substituted bases such as 6-dimethyl Dibenzothiophene class.Owing to the methyl of sulphur atom next-door neighbour makes to create between sulphur atom and the active center of catalyst sterically hindered, the active center of the most accessible reaction of sulphur atom, thus result in reaction rate and significantly decline.

Conventional load type hydrogenation catalyst is limited by carrier hole structure, active metal load capacity is usually no more than 30wt%, the active center quantity that loaded catalyst can be provided by is limited, although the quantity in active center and type distribution can be optimized adjustment, but owing to the limit bottleneck of active center quantity cannot be broken through, increase substantially the limited space of hydrogenation activity, be difficult to the demand meeting refinery to manufacturing country V diesel product.Hydrogenation catalyst major part prepared by body phase method is made up of active metal component, the restriction of tenor can be broken away from, can any ratio of each active component in regulating catalyst, improve the Hydrogenation of catalyst, owing to bulk phase catalyst has the hydrogenation activity of excellence, can be under conditions of not improving device reaction severity, being directly produced the product without sulfur diesel meeting state V standard, original device is without transformation, it is possible to improve the treating capacity of device, reduce the production cost of refinery, it is achieved energy efficiency.

Although active metallic content is high in body phase hydrogenation catalyst, but by mechanical strength, the restriction of the aspects such as active metal easily gathering, need to add a certain amount of adhesive component, generally meet the requirement of mechanical strength, the addition of binding agent will be at more than 30wt%, the most, the most not only reduce the consumption of active metal, in making again amount of activated metal entrance body mutually, make it can not become hydrogenation sites, there is the problem that active metal utilization rate is low, simultaneously, the distribution making different hydrogenation active metals is not easily controlled, thus affect the distribution of different hydrogenation active metals.Therefore, for body phase hydrogenation catalyst, there is the distribution of good hydrogenation active metals, there is mating reaction between suitable hydrogenation active metals component, there is high catalyst surface active bit density, there is high active metal utilization rate, the activity of catalyst can be significantly improved.

CN1951561A discloses the method using co-precipitation to prepare hydrogenation catalyst, and catalyst uses active metal Ni, W component to generate Ni with precipitant co-precipitation_xW_yO_zComposite oxides precursor, in above process, can add aluminum salt solution, it is also possible to be directly added into aluminium hydroxide after plastic, then with MoO₃Making beating mixing, filtration, molding, activation are final catalyst.Bulk phase catalyst prepared by the method reaches to meet the use of mechanical strength when requiring, its surface activity bit density is relatively low, it is impossible to give full play to the advantage of high-load active metal component, reduces the utilization rate of active metal, adds the preparation cost of catalyst.

CN101306374A discloses a kind of hydrogenating catalyst composition, this catalyst is prepared by coprecipitation method, the compound of at least one metal component of group VIII, the compound of at least two metal component of group VIB, organic additive and water are mixed with mixed liquor, the pH using acid or alkali to adjust mixed liquor is 7～11, described mixed liquor is placed in reactor, react 1～24 hour under the airtight condition of room temperature to 250 DEG C, filter afterwards and be dried.The catalyst of the method gained is without high-temperature roasting, containing organic additive in final catalyst, the mechanical strength of catalyst to be made meets use requirement, needs to add more adhesive component, so can affect the distribution of different hydrogenation active metals, make catalyst surface active reduce.

CN101255356A discloses the preparation method of a kind of unsupported catalyst, it is to use urea melting reaction technology, the VIIIth race and group VIB active metal precursor will be contained and carbamide will mix and is incorporated under urea melting state reaction, remove unnecessary carbamide, obtain catalyst particles, can be shaped by adding binding agent.In the method, carbamide adds as precipitant, need after reaction to add the carbamide that heat extraction is unnecessary, being subsequently adding binding agent to be shaped, such the method yet suffers from the addition of binding agent and makes the skewness of different hydrogenation active metals, the low density problem of catalyst surface active position simultaneously.

Hydrogenation catalyst prepared by body phase method, its hydrogenation sites be reactant molecule can be close catalyst channel surfaces on, although this type of catalyst activity tenor is higher, but not all active metal can become hydrogenation sites, therefore, how to make more active metal be distributed in channel surfaces and form hydrogenation sites, improve the active center density on bulk phase catalyst surface, the utilization rate improving hydrogenation active metals component is the most important research topic.

Body phase hydrogenation catalyst disclosed in CN102049265A, ammonium hydrogen carbonate is added during coprecipitated, body phase hydrogenation catalyst disclosed in CN102451703A, carbon dioxide is added during coprecipitated, generate carbonate or bicarbonate, said method is all to utilize it to release a certain amount of gas in roasting process, under the percussion of gas, increase the pore volume of catalyst, specific surface area, more metal active position is made to be exposed to the surface of catalyst, but this kind of method can make cell channels collapse, pore size distribution disperse, mechanical strength reduces, and cause active metal localized clusters, the metal active position come out is limited.

Under distillate ultra-deep hydrodesulfuration reaction environment, present in distillate, nitrogen-containing organic compound produces obvious inhibitory action to hydrodesulfurization reaction, hydrodesulfurization activity increases along with the nitrogen content in raw material and reduces, this is because there is competitive Adsorption on catalyst activity position in nitrogen-containing compound and sulfide in distillate, the absorbability of nitride is stronger, occupy the active sites on catalyst, sulfide is made to be difficult to close, inhibit hydrodesulfurization reaction, so when processing the high heavy diesel of nitrogen content and producing super-low sulfur product, catalyst needs the hydrodenitrogenationactivity activity with excellence, the hydrodenitrogenationactivity activity of catalyst improves, after nitrogen content reduces, reduce with the nitride of sulfide generation competitive Adsorption, sulfide is easier to, adsorb the most more on catalyst activity position, promote hydrodesulfurization reaction.Therefore the hydrodenitrogenationactivity activity improving catalyst has extremely important effect to the ultra-deep hydrodesulfuration activity improving bulk phase catalyst.

The petroleum refining industry of 21st century must comply with the strategy of sustainable development, it is necessary to pay attention to economic benefit, protection environment and the principle economized on resources simultaneously.Therefore, the preparation method using non-environmental-pollution produces bulk phase catalyst and becomes more important.Existing coprecipitation method prepares catalyst technology, is used mostly NH₃·H₂O is as precipitant, and these are a large amount of containing ammonia, the waste water of nitrogen, to environment by producing.

Coprecipitation method prepares bulk phase catalyst technology, use different coprecipitation mode, Gelation Conditions etc., all can to active metallic content on channel surfaces in catalyst and between active center density, the distribution of different hydrogenation active metals and different hydrogenation active metals interaction relationship have a great impact.The coprecipitation method of above-mentioned employing can make the distribution of different hydrogenation active metals be not easily controlled, thus affect the distribution of different hydrogenation active metals, reduce the effect of cooperating between active metal, simultaneously, in catalyst, table phase active metallic content is less and active center density is relatively low, finally affects the ultra-deep hydrodesulfuration performance of catalyst.Therefore, how to regulate and control the distribution of hydrogenation active metals, make to have between hydrogenation active metals component suitable mating reaction, how to increase table phase active metallic content and active center density in catalyst, improve the utilization rate of hydrogenation active metals component, be the key improving body phase Hydrobon catalyst Hydrogenation.

Summary of the invention

For the deficiencies in the prior art, the invention provides the preparation method of a kind of Hydrobon catalyst.This catalyst table phase active site density is big, hydrogenation active metals utilization rate is high, improve the distribution of hydrogenation active metals in catalyst, improve mating reaction between hydrogenation active metals, catalyst pore structure is reasonable simultaneously, active metal disperses evenly, and mechanical strength is high, particularly suitable application in diesel oil distillate ultra-deep hydrodesulfuration, denitrification reaction.

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

(1), prepare the component saline solution A Han Ni, sodium metaaluminate alkaline solution is added dropwise to solution A and carries out plastic reaction, generate nickeliferous, aluminum precipitation thing serosity I；

(2), preparing the component saline mixed solution B Han W, Mo, in the while of by solution B and sodium metaaluminate alkaline solution, also stream is equipped with the retort of water purification, plastic reaction, generates tungstenic, molybdenum, aluminum precipitation thing serosity II；

(3), by the serosity I of step (1) gained and the serosity II mix homogeneously of step (2) gained, the most aging, after aging end, filter, the material water vapour obtained carries out hydrothermal treatment consists, wherein adds carbamide during hydrothermal treatment consists；

(4), step (3) gained material drying, molding, washing, then drying, roasting obtain final Hydrobon catalyst.

The Hydrobon catalyst of the present invention, containing tri-kinds of active metal components of W, Ni, Mo and aluminium oxide, on the basis of the weight of Hydrobon catalyst, NiO, WO₃And MoO₃Gross weight content be 40% ~ 95%, preferably 50% ~ 85%, alumina content is 5% ~ 60%, preferably 15% ~ 50%.In the Hydrobon catalyst of the present invention, the mol ratio of Ni/W is 1:8 ~ 8:1, preferably 1:4 ~ 4:1, and (Ni+W)/Mo mol ratio is 1:10 ~ 10:1, preferably 1:5 ~ 5:1.

In step (1) mixed solution A, Ni weight concentration in terms of NiO is 5～80g/L, preferably 10～60g/L.Containing Al in described sodium metaaluminate alkaline solution₂O₃Concentration is 10 ~ 70g/L, preferably 20 ~ 50g/L.When preparing solution A, the general nickel source used can be one or more in nickel sulfate, nickel nitrate, basic nickel carbonate, Nickel dichloride..

In step (2) mixed solution B, W is with WO₃The weight concentration of meter is 10～100g/L, and preferably 20～80g/L, Mo is with MoO₃The weight concentration 5～80g/L of meter, preferably 10～60g/L.Containing Al in described sodium metaaluminate alkaline solution₂O₃Concentration is 10 ~ 60g/L, preferably 10 ~ 40g/L.When preparing mixed solution B, the general tungsten source used can be one or more in ethyl ammonium metatungstate, ammonium metatungstate；Molybdenum source is ammonium molybdate.

In step (1), reaction temperature is 20～90 DEG C, preferably 30～70 DEG C.During cemented into bundles, pH value controls is 6.0 ~ 11.0, preferably 7.0 ~ 9.0.Gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

In step (2), reaction temperature is 30～90 DEG C, preferably 40～80 DEG C.And pH value control is 6.0 ~ 11.0 when flowing plastic, preferably 7.0 ~ 9.0.Gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

In step (1) and step (2), gelling temperature and time can be the same or different.Step (1) and step (2) can carry out can also carrying out during difference simultaneously.

In step (3), aging temperature is 40～90 DEG C, preferably 50～80 DEG C.Time aging, pH value controls is 6.0 ~ 10.0, preferably 6.5 ~ 9.0.Ageing time is 0.5 ~ 6.0 hour, preferably 1.0 ~ 4.0 hours.

Hydrothermal conditions described in step (3) is as follows: carry out under airtight container, and temperature is 200 ~ 300 DEG C, preferably 210 ~ 260 DEG C, and pressure is 1.0 ~ 8.0 MPa, preferably 3.0 ~ 6.0MPa, and the process time is 0.5 ~ 10.0 hour, preferably 1.0 ~ 6.0 hours.During hydrothermal treatment consists, the addition of carbamide is 0.5:1 ~ 10.0:1, preferably 2.0:1 ~ 8.0:1 with the mol ratio of active metal (tungsten, molybdenum, nickel) atom total amount in catalyst.

Dry, molding and washing described in step (4) can use this area conventional method to carry out.Drying condition is as follows: being dried 1 ~ 48 hour at 50 ~ 250 DEG C, preferably 80 ~ 180 DEG C are dried 4 ~ 36 hours.In forming process, the shaping assistant of routine, one or more in such as peptizer, extrusion aid etc. can be added as required.Described peptizer is one or more in hydrochloric acid, nitric acid, sulphuric acid, acetic acid, oxalic acid etc., described extrusion aid refers to the most extruded material, such as one or more in sesbania powder, white carbon black, graphite powder, citric acid etc., the consumption of extrusion aid accounts for 1wt%～10wt% of total material butt.Washing is usually and uses deionized water or wash containing decomposable asymmetric choice net salt (such as ammonium acetate, ammonium chloride, ammonium nitrate etc.) solution, is washed till neutrality.

Being dried that step (4) is used after formation can use this area normal condition with roasting, drying condition is as follows: be dried 1 ~ 48 hour at 50 ~ 250 DEG C, roasting condition was as follows: 350 ~ 650 DEG C of roastings 1 ~ 24 hour, preferably drying condition is as follows: being dried 4 ~ 36 hours at 80 ~ 180 DEG C, roasting condition was as follows: 400 ~ 600 DEG C of roastings 2 ~ 12 hours.

In the inventive method, can contain adjuvant component as required, adjuvant component is one or more in silicon, phosphorus, titanium, zirconium, boron etc., preferably titanium and/or zirconium, in terms of element, adjuvant component weight content in Hydrobon catalyst is 0 ~ 20%, preferably 1% ~ 15%.In Hydrobon catalyst preparation process of the present invention, preferably during preparation mixed solution A, add the compound containing adjuvant component, i.e. titanium source and/or zirconium source.Titanium source can use one or more in Titanium Nitrate, titanium sulfate, titanium chloride etc., zirconium source can use one or more in zirconium nitrate, zirconium chloride, zirconium oxychloride etc..

In the inventive method, the shape of catalyst can be as needed for lamellar, spherical, cylindrical bars and irregular bar (Herba Trifolii Pratentis, Herba Galii Bungei), preferably cylindrical bars and irregular bar (Herba Trifolii Pratentis, Herba Galii Bungei).The diameter of carrier can be slice and the thick bar of ＞ 2.5mm of 0.8 ~ 2.0mm.

Hydrobon catalyst of the present invention is the body phase Hydrobon catalyst of oxidation state, and conventional method can be used before use to carry out presulfurization.

Hydrobon catalyst prepared by the inventive method is body phase Hydrobon catalyst, and its composition includes hydrogenation active metals component W, Ni and Mo, aluminium oxide；Wherein table phase active metal component WO₃Weight content and body phase active metal component WO₃The ratio of weight content be 2.0:1 ~ 7.0:1, it is preferably 2.5:1 ~ 5.0:1, the weight content of table phase active metal component NiO is 1.2:1 ~ 4.5:1 with the ratio of the weight content of body phase active metal component NiO, is preferably: 1.8 ~ 3.0:1, table phase active metal component MoO₃Weight content and body phase active metal component MoO₃The ratio of weight content be 1.8:1 ~ 6:1, preferably 2.0:1 ~ 4.5:1.

In the present invention, table phase active metal component WO₃Weight content be table mutually in WO₃Weight content, body phase active metal component WO₃Weight content be WO in catalyst₃Weight content；The weight content of table phase active metal component NiO is the weight content of table middle NiO mutually, and the weight content of body phase active metal component NiO is the weight content of NiO in catalyst；Table phase active metal component MoO₃Weight content be table mutually in MoO₃Weight content, body phase active metal component MoO₃Weight content be MoO in catalyst₃Weight content.

The character of Hydrobon catalyst prepared by the inventive method is as follows: specific surface area is 180 ~ 450m²null/g，Pore volume is 0.20 ~ 0.80ml/g，Pore-size distribution is as follows: the pore volume shared by the hole of a diameter of below 4nm accounts for the 1% ~ 20% of total pore volume，Pore volume shared by the hole of a diameter of 4 ~ 8nm accounts for the 55% ~ 80% of total pore volume，Pore volume shared by the hole of a diameter of 8 ~ 15nm accounts for the 2% ~ 20% of total pore volume，The pore volume of a diameter of more than 15nm account for total pore volume for 0.1% ~ 5.0%，Preferably pore-size distribution is as follows: the pore volume shared by the hole of a diameter of below 4nm accounts for the 5% ~ 17% of total pore volume，Pore volume shared by the hole of a diameter of 4 ~ 8nm account for total pore volume for 61% ~ 75%，Pore volume shared by the hole of a diameter of 8 ~ 15nm accounts for the 4% ~ 17% of total pore volume，The pore volume of a diameter of more than 15nm account for total pore volume for 0.5% ~ 5.0%.

Hydrobon catalyst prepared by the inventive method, surface activity bit density is big, active metal disperses evenly, cooperation between active metal is good, active metal utilization rate is high, and catalyst pore structure is reasonable simultaneously, and mechanical strength is high, there is higher hydrodesulfurization and hydrodenitrogeneration reactivity worth, particularly suitable application in diesel oil distillate ultra-deep hydrodesulfuration, denitrification reaction.

The inventive method uses positive addition (the acid sedimentation method i.e. alkaline precipitating agent is added in the metal salt solution of acidity precipitate) to prepare nickel aluminum mixed sediment, uses parallel flow precipitation to prepare tungsten, molybdenum and aluminum mixed sediment, then by aging after both mixing.The present invention prepares the relatively large nickel of crystal grain, aluminum precipitation thing by using positive addition, cocurrent process prepares the relatively small tungsten of crystal grain, molybdenum and aluminum precipitation thing, above two precipitate is mixed, the distribution of different hydrogenation active metals can be controlled, be conducive to being formed between active metal tungsten, molybdenum, nickel high activity phase, and improve the interaction between active metal, improve the ultra-deep hydrodesulfuration performance of body phase Hydrobon catalyst.

In the preparation method of catalyst of the present invention, the material steam treatment under appropriate conditions that obtains add carbamide after the co-precipitation of W, Ni, Mo, Al component, carbamide is decomposed into NH in high temperature environments₃And CO₂, NH₃And CO₂NH is generated in the presence of water vapour₄ ⁺And HCO₃ ^-Ion, NH₄ ⁺And HCO₃ ^-The microscopic pattern of material is had a significant impact by ion at high temperature under high pressure, before hydrothermal treatment consists, material phase structure is cylinder, after hydrothermal treatment consists, material phase structure is changed into, from cylinder, the irregular body that irregular lamellar is piled into, the transformation of this structure make active metal table mutually in distribution substantially increase, and disperse evenly, be conducive to improving the density of Adsorption.Additionally, add carbamide when steam treatment, make the transformation of material form that the pore size distribution of catalyst can also be made more to concentrate, more uniformly, be conducive to improving the mechanical strength of catalyst.The Hydrobon catalyst of the present invention is in deeply desulfurizing fractional oil and denitrification process, there is the hydrodenitrogenationactivity activity of excellence, the reduction of nitrogen content, it is more beneficial for the carrying out of hydrodesulfurization reaction, so Hydrobon catalyst is when the heavy distillate that processed nitrogen content is high, there is the ultra-deep hydrodesulfuration activity of excellence.

In the preparation method of catalyst of the present invention, using containing the sodium metaaluminate alkaline solution of Al is that precipitant avoids and uses NH₃·H₂O is as precipitant, produce a large amount of containing ammonia, the waste water of nitrogen, simultaneous reactions precipitate particles is uniform, be more beneficial for W, Ni, Mo active metal be distributed in table mutually in, and W, Ni, Mo active metal is more uniform in table middle distribution mutually, is conducive to improving the ultra-deep hydrodesulfuration of bulk phase catalyst, denitrification activity.

Detailed description of the invention

In the present invention, specific surface area and pore volume use low temperature liquid nitrogen determination of adsorption method, and mechanical strength uses side pressure method to measure.Catalyst table phase active metallic content uses x-ray photoelectron spectroscopy (XPS) to measure, and caltalyst phase active metallic content uses inductively coupled plasma atomic emission spectrum (ICP-AES) to measure, transmissioning electric mirror determining catalyst surface WS₂/MoS₂Density i.e. WS₂And MoS₂Density.In the present invention, wt% is mass fraction, and v% is volume fraction.

Embodiment 1

Respectively Nickel dichloride. being dissolved in water purification, be configured to solution A, in solution A, the weight concentration of NiO is 19g/L.Respectively ammonium metatungstate, ammonium molybdate are dissolved in water purification, are configured to mixed solution B, WO in mixed solution B₃Weight concentration be 39g/L, MoO₃Weight concentration is 16g/L.Al will be contained₂O₃The sodium aluminate solution of 20g/L 500 milliliters under agitation adds solution A, and gelling temperature is maintained at 60 DEG C, at the end of pH value control 7.8, gelation time control, at 60 minutes, generates nickeliferous, aluminum precipitation thing serosity I.1000mL water purification is added in retort, Al will be contained₂O₃The sodium aluminate solution of 20g/L 500 milliliters and solution B also flow in addition retort, and gelling temperature is maintained at 60 DEG C, and flow pH value in plastic course of reaction and control 7.8, and gelation time control, at 60 minutes, generates tungstenic, molybdenum, aluminum precipitation thing serosity II.By above two containing aging after sediment slurry mixing, ageing time 2 hours, aging temperature 75 DEG C, at the end of aging, pH value controls 7.6, then filtering, filter cake carries out hydrothermal treatment consists under the water vapour containing carbamide, and the condition of hydrothermal treatment consists is: the mol ratio of carbamide and active metal atom total amount is 7:1, temperature is 250 DEG C, pressure is 4.0MPa, and the process time is 4 hours, and filter cake is dried 8 hours at 100 DEG C, roll, extruded moulding.Wash with water purification under room temperature.Then it is dried 10 hours at 80 DEG C, 530 DEG C of roastings 4 hours, obtains catalyst A.Catalyst composition, pore size distribution and main character are shown in Table 1.

Embodiment 2

According to the method for embodiment 1, by the constituent content proportioning of the catalyst B in table 1, in dissolving tank 1, add nickel nitrate, zirconyl chloride solution, prepare working solution A, in dissolving tank 2, add ammonium metatungstate and ammonium molybdate preparation working solution B.Al will be contained₂O₃The sodium aluminate solution of 30g/L 400 milliliters under agitation adds solution A, and gelling temperature is maintained at 55 DEG C, at the end of pH value control 8.0, gelation time control, at 50 minutes, generates nickeliferous, aluminum precipitation thing serosity I.600mL water purification is added in retort, Al will be contained₂O₃The sodium aluminate solution of 20g/L 800 milliliters and solution B also flow in addition retort, and gelling temperature is maintained at 50 DEG C, and flow pH value in plastic course of reaction and control 7.8, and gelation time control, at 60 minutes, generates tungstenic, molybdenum, aluminum precipitation thing serosity II.By above two containing aging after sediment slurry mixing, ageing time 3 hours, aging temperature 72 DEG C, at the end of aging, pH value controls 8.0, then filter, filter cake carries out hydrothermal treatment consists under the water vapour containing carbamide, hydrothermal conditions: the mol ratio of carbamide and active metal atom total amount is 3:1, temperature is 230 DEG C, pressure is 3.5MPa, the process time is 4 hours, material after hydrothermal treatment consists is dried 12 hours at 70 DEG C, then extruded moulding, wash 3 times with water purification, wet bar is dried 10 hours at 100 DEG C, 480 DEG C of roastings 5 hours, obtain final catalyst B, composition, pore size distribution and main character are shown in Table 1.

Embodiment 3

According to the method for embodiment 1, by the constituent content proportioning of the catalyst C in table 1, in dissolving tank 1, add Nickel dichloride., phosphoric acid solution, prepare working solution A, in dissolving tank 2, add ammonium metatungstate and ammonium molybdate preparation working solution B.Al will be contained₂O₃The sodium aluminate solution of 25g/L 600 milliliters under agitation adds solution A, and gelling temperature is maintained at 45 DEG C, at the end of pH value control 7.6, gelation time control, at 60 minutes, generates nickeliferous, aluminum precipitation thing serosity I.1000mL water purification is added in retort, Al will be contained₂O₃The sodium aluminate solution of 20g/L 400 milliliters and solution B also flow in addition retort, and gelling temperature is maintained at 60 DEG C, and flow pH value in plastic course of reaction and control 8.0, and gelation time control, at 60 minutes, generates tungstenic, molybdenum, aluminum precipitation thing serosity II.By above two containing aging after sediment slurry mixing, ageing time 2 hours, aging temperature 70 DEG C, at the end of aging, pH value controls 7.6, then filter, filter cake carries out hydrothermal treatment consists under the water vapour containing carbamide, hydrothermal conditions: the mol ratio of carbamide and active metal atom total amount is 6:1, temperature is 220 DEG C, pressure is 5.0MPa, the process time is 4 hours, material after hydrothermal treatment consists is dried 8 hours at 120 DEG C, then extruded moulding, wash 1 time with water, wet bar is dried 6 hours at 110 DEG C, 600 DEG C of roastings 4 hours, obtain final catalyst C, composition, pore size distribution and main character are shown in Table 1.

Embodiment 4

According to the method for embodiment 1, by the constituent content proportioning of the catalyst D in table 1, in dissolving tank 1, add Nickel dichloride., titanium chloride solution, prepare working solution A, in dissolving tank 2, add ammonium metatungstate and ammonium molybdate preparation working solution B.Al will be contained₂O₃The sodium aluminate solution of 25g/L 600 milliliters under agitation adds solution A, and gelling temperature is maintained at 40 DEG C, at the end of pH value control 7.8, gelation time control, at 60 minutes, generates nickeliferous, aluminum precipitation thing serosity I.800mL water purification is added in retort, Al will be contained₂O₃1000 milliliters of ammonia of the sodium aluminate solution of 15g/L and solution B also flow in addition retort, and gelling temperature is maintained at 50 DEG C, and flow pH value in plastic course of reaction and control 8.0, and gelation time control, at 60 minutes, generates tungstenic, molybdenum, aluminum precipitation thing serosity II.By above two containing aging after sediment slurry mixing, ageing time 3 hours, aging temperature 70 DEG C, at the end of aging, pH value controls 8.2, then filter, filter cake carries out hydrothermal treatment consists under the water vapour containing carbamide, hydrothermal conditions: the mol ratio of carbamide and active metal atom total amount is 4:1, temperature is 250 DEG C, pressure is 3.0MPa, the process time is 6 hours, material after hydrothermal treatment consists is dried 6 hours at 80 DEG C, then extruded moulding, wash 4 times with water purification, wet bar is dried 8 hours at 100 DEG C, 550 DEG C of roastings 5 hours, obtain final catalyst D, composition, pore size distribution and main character are shown in Table 1.

Comparative example 1

Method for preparing catalyst as disclosed in CN102049265A, prepares the reference agent E identical with the catalyst composition of embodiment 1.In dissolving tank, add aluminum chloride, Nickel dichloride., ammonium metatungstate preparating acid sex work solution A, take 100g ammonium hydrogen carbonate and be made into the solution that molar concentration is 2.0mol/l.Adding 500mL water in retort, temperature rises to 60 DEG C.Stirring in the case of, by solution A, ammonium bicarbonate aqueous solution and concentration be 10%(weight) ammonia and flow addition retort in plastic, gelling temperature 60 DEG C, gelation time 1.0 hours, the pH value of plastic slurry is 7.8.After cemented into bundles aging 2 hours.Then filtering, the filter cake obtained and molybdenum trioxide, making beating stirs, and filters, and filter cake is dried 8 hours at 100 DEG C, rolls, extruded moulding.Wash with water purification under room temperature.Then being dried 10 hours at 80 DEG C, 530 DEG C of roastings 4 hours, obtain final catalyst E, composition, pore size distribution and main character are shown in Table 1.

Comparative example 2

By embodiment 1 catalyst composition and preparation method, it is added without carbamide during hydrothermal treatment consists, prepares reference agent F.Composition, pore size distribution and main character are shown in Table 1.

Comparative example 3

By embodiment 1 catalyst composition and preparation method, it is added without carbamide during hydrothermal treatment consists, but adds NH₃, temperature is 250 DEG C, and pressure is 4.0MPa, and the process time is 4 hours, and the mol ratio of ammonia and active metal atom total amount is 7:1, prepares reference agent G.Composition, pore size distribution and main character are shown in Table 1.

Comparative example 4

By embodiment 1 catalyst composition and preparation method, it is added without carbamide during hydrothermal treatment consists, but adds CO₂, temperature is 250 DEG C, and pressure is 4.0MPa, and the process time is 4 hours, CO₂It is 7:1 with the mol ratio of active metal atom total amount, prepares reference agent H.Composition, pore size distribution and main character are shown in Table 1.

Comparative example 5

The reference agent I that method for preparing catalyst preparation as disclosed in CN101255356A is identical with the catalyst composition of embodiment 1.By catalytic component content proportioning in embodiment 1, by MoO₃, wolframic acid, basic nickel carbonate, carbamide (quality of carbamide with active metal mass ratio 2.5) join in there-necked flask, and add a small amount of water and make it be uniformly dispersed, it is placed in oil bath and stirs 4 hours in 130 DEG C, while hot reactant is poured in pallet and cool down, with pulverizer, the product of cooling is pulverized, it is placed in 150 DEG C of baking ovens drying, makes unnecessary carbamide decompose.The dilute nitric acid solution weighing the boehmite addition 10wt% accounting for pressed powder 30wt% makes Alumina gel, pressed powder is added in Alumina gel, with become pasty state, through kneading, extrusion, make the catalyst bar of diameter 1.6mm, after being dried 5h under infrared lamp, put in baking oven and be dried 10 hours at 110 DEG C, 400 DEG C of roasting 5h in Muffle furnace, prepare reference agent I.Catalyst composition, pore size distribution and main character are shown in Table 1.

Comparative example 6

The reference agent J that method for preparing catalyst preparation as disclosed in CN102451703A is identical with the catalyst composition of embodiment 1.By the catalytic component content proportioning in embodiment 1, in dissolving tank 1, add Nickel dichloride., ammonium metatungstate and zirconium oxychloride preparating acid sex work solution A, in dissolving tank 2, then add sodium metaaluminate alkalescence working solution B.Adding 350mL water in retort, temperature rises to 40 DEG C.In the case of stirring, by solution A, solution B and CO₂And flow plastic in addition retort, CO₂Concentration is 45v%, gelling temperature 60 DEG C, gelation time 1 hour, and the pH value of plastic serosity is 7.8.CO is added during plastic₂The total amount of gas and the Al in alkalescence working solution B₂O₃Mol ratio is 4.0.After plastic aging 2 hours.Then filtering, filter cake adds 500ml water purification and molybdenum trioxide, and making beating stirs, and filters, and filter cake is dried 8 hours at 100 DEG C, rolls, extruded moulding.Wash with water purification under room temperature.Then being dried 10 hours at 80 DEG C, 530 DEG C of roastings 4 hours, obtain final catalyst J, composition, pore size distribution and main character are shown in Table 1.

Comparative example 7

Method as disclosed in CN1951561A, detailed process is as follows:

Forming by the catalyst of embodiment 1, Nickel dichloride. and ammonium metatungstate are prepared and be dissolved in water purification, be configured to mixed solution, wherein the weight concentration of NiO is 19g/L, WO₃Weight concentration be 39g/L.Be 10%(weight by concentration) ammonia under agitation adds and carries out plastic in mixed solution, gelling temperature is maintained at 60 DEG C, at the end of pH value control 7.8, gelation time control, at 60 minutes, generates nickeliferous, tungsten precipitate serosity.Then carry out aging, ageing time 2 hours, aging temperature 75 DEG C, aging at the end of pH value control 7.6, after filtration, after adding water purification, aluminium hydroxide and molybdenum trioxide mix homogeneously in filter cake, extruded moulding, wash with water purification under room temperature.Then it is dried 10 hours at 80 DEG C, 530 DEG C of roastings 4 hours, obtains catalyst K.Catalyst composition, pore size distribution and main character are shown in Table 1.

Embodiment 5

The present embodiment is catalyst activity evaluation experimental of the present invention, and contrasts with comparative example catalyst.Using A, B, C, D catalyst of the present invention and comparative example E, F, G, H, I, J, K catalyst, carry out comparative evaluation's test on 200mL small hydrogenation device, test raw material is Zhenghai mixed diesel (catalytic diesel oil accounts for the 40% of miscella weight).Raw material main character is shown in Table 4, and catalyst activity evaluates process conditions: hydrogen dividing potential drop is 6.4MPa, and reaction temperature is 360 DEG C, and during liquid, volume space velocity is 2.0h^-1, hydrogen to oil volume ratio is 500:1, and evaluation result is shown in Table 5.Use sulfur compound in gas chromatography-atomic emission detector device (GC-AED) detection hydrofined oil, the results are shown in Table 6.

Can be seen that from table 1, table 2 and table 3, catalyst of the present invention is not in the case of active metal amount changes, catalyst surface active metal atom concentration increases, hydrogenation sites density increases, pore size distribution$ is more concentrated, find out that catalyst has the hydrodenitrogenationactivity activity of excellence from evaluation result table 6, in removing 4, during 6-DMDBT class macromole sulfide, demonstrate high hydrogenation activity.Catalyst is used for processed distillate, during in particular for processing nitrogen content high heavier diesel fraction, has the ultra-deep hydrodesulfuration activity of excellence.

Table 1 catalyst composition and character

Catalyst is numbered	A	B	C	D
					Catalyst forms
NiO, wt%	19	16	18	22
					WO3, wt%	38	36	32	28
MoO3, wt%	16	20	16	20
					Al2O3, wt%	Surplus	Surplus	Surplus	Surplus
Other/wt%	Nothing	ZrO2/2.0	P2O5/2.0	TiO2/3.0
					Catalyst property
Specific surface area, m2/g	238	231	222	227
					Pore volume, mL/g	0.345	0.325	0.338	0.321
Mechanical strength, N/mm	23.1	22.8	22.2	23.3
					Pore size distribution, %
＜ 4nm	10.98	11.92	13.18	12.89
					4nm~8nm	71.84	70.16	70.94	72.11
8nm~15nm	15.29	14.35	13.24	12.42
					＞ 15nm	2.89	3.57	2.64	2.58

Continued 1

Catalyst is numbered	E	F	G	H	I	J	K
								Catalyst forms
NiO, wt%	19	19	19	19	19	19	19
								WO3, wt%	38	38	38	38	38	38	38
MoO3, wt%	16	16	16	16	16	16	16
								Al2O3, wt%	Surplus	Surplus	Surplus	Surplus	Surplus	Surplus	Surplus
Other/wt%	Nothing	Nothing	Nothing	Nothing	Nothing	Nothing	Nothing
								Catalyst property
Specific surface area, m2/g	212	202	223	208	232	218	198
								Pore volume, mL/g	0.315	0.301	0.317	0.324	0.340	0.242	0.212
Mechanical strength, N/mm	20.1	18.9	18.5	19.1	11.5	20.5	18.5
								Pore size distribution, %
＜ 4nm	19.23	17.11	15.18	15.23	14.25	17.25	54.45
								4nm~8nm	32.45	32.22	37.89	34.25	28.42	35.28	21.14
8nm~15nm	38.17	34.42	32.33	35.59	38.81	33.85	18.32
								＞ 15nm	10.15	16.25	14.60	14.93	19.52	13.62	6.09

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

Catalyst is numbered	A	B	C	D	E
						Table phase IW/ body phase IW	4.28	3.71	4.16	3.92	0.95
Table phase INi/ body phase INi	2.99	2.44	2.98	2.83	0.91
						Table phase IMo/ body phase IMo	4.28	3.65	4.25	3.96	-

Continued 2

Catalyst is numbered	F	G	H	I	J	K
							Table phase IW/ body phase IW	1.13	1.08	1.19	0.99	1.42	1.04
Table phase INi/ body phase INi	1.11	1.18	1.17	0.94	1.38	0.99
							Table phase IMo/ body phase IMo	0.99	1.05	1.06	-	-	-

Table 3 transmissioning electric mirror determining catalyst surface MoS₂/WS₂Density

Catalyst is numbered	A	B	C	D	E	F	G	H	I	J	K
												MoS2/WS2Density, grain/100nm	93	90	89	84	51	55	56	54	50	66	51

Table 4 raw oil main character

Project	Analysis result
		Density (20 DEG C), g/cm3	0.8814
Boiling range scope, DEG C	178-375
		S, g/g	13300
N, g/g	728
		Cetane number	41.5

Table 5 catalyst activity evaluation result

Catalyst is numbered	A	B	C	D	E
						Generate oil density (20 DEG C), g/cm3	0.8389	0.8404	0.8403	0.8402	0.8534
Boiling range scope, DEG C	168-366	171-367	170-367	173-368	176-376
						S, g/g	8.3	9.2	8.6	9.0	189.8
N, g/g	1.0	1.0	1.0	1.0	19.4
						Cetane number	51.8	51.2	51.4	51.7	45.6

Continued 5

Catalyst is numbered	F	G	H	I	J	K
							Generate oil density (20 DEG C), g/cm3	0.8491	0.8512	0.8509	0.8539	0.8498	0.8516
Boiling range scope, DEG C	185-373	174-372	169-375	169-375	169-373	169-374
							S, g/g	163.2	169.5	185.6	215.2	169.8	204.8
N, g/g	16.1	17.8	16.6	21.8	16.4	19.7
							Cetane number	49.9	50.1	47.8	46.1	45.6	45.9

The content of different sulfide in table 6 hydrofined oil

Catalyst is numbered	A	B	C	D	E
						Nitrogen content in hydrofined oil, g/g	1.0	1.0	1.0	1.0	19.4
Sulfur content in hydrofined oil, g/g	8.3	9.2	8.6	9.0	189.8
						C1-DBT, g/g	0	0	0	0	28.3
4-BMDBT, g/g	1.5	2.0	1.7	1.8	39.2
						6-BMDBT, g/g	0.9	1.6	1.5	1.2	35.6
4,6-BMDBT, g/g	5.9	5.6	5.4	6.0	86.7

Continued 6

Catalyst is numbered	E	G	H	I	J	K
							Nitrogen content in hydrofined oil, g/g	16.1	17.8	16.6	21.2	16.4	19.7
Sulfur content in hydrofined oil, g/g	163.2	169.5	185.6	215.2	169.8	204.8
							C1-DBT, g/g	21.5	28.3	29.8	35.1	30.3	35.4
4-BMDBT, g/g	33.5	32.6	32.7	39.9	38.1	40.8
							6-BMDBT, g/g	34.6	31.8	38.9	36.7	34.6	44.5
4,6-BMDBT, g/g	73.6	76.8	84.2	103.5	66.8	84.1

Claims (12)

1. a preparation method for Hydrobon catalyst, including:

(1), prepare the component saline solution A Han Ni, sodium metaaluminate alkaline solution is added dropwise to solution A and carries out plastic reaction, generate nickeliferous, aluminum precipitation thing serosity I；

(2), preparing the component saline mixed solution B Han W, Mo, in the while of by solution B and sodium metaaluminate alkaline solution, also stream is equipped with the retort of water purification, plastic reaction, generates tungstenic, molybdenum, aluminum precipitation thing serosity II；

(3), by the serosity I of step (1) gained and the serosity II mix homogeneously of step (2) gained, the most aging, after aging end, filter, the material water vapour obtained carries out hydrothermal treatment consists, wherein adds carbamide during hydrothermal treatment consists；

(4), step (3) gained material drying, molding, washing, then drying, roasting obtain Hydrobon catalyst.

The most in accordance with the method for claim 1, it is characterised in that: on the basis of the weight of Hydrobon catalyst, NiO, WO₃And MoO₃Gross weight content be 40% ~ 95%, preferably 50% ~ 85%, alumina content is 5% ~ 60%, being preferably 15% ~ 50%, in described catalyst, the mol ratio of Ni/W is 1:8 ~ 8:1, being preferably 1:4 ~ 4:1, (Ni+W)/Mo mol ratio is 1:10 ~ 10:1, preferably 1:5 ~ 5:1.

The most in accordance with the method for claim 1, it is characterised in that: step (1) is containing in Ni component saline solution A, and Ni weight concentration in terms of NiO is 5～80g/L, preferably 10～60g/L, preferably 30～60g/L；Containing Al in described sodium metaaluminate alkaline solution₂O₃Concentration is 10 ~ 70g/L, preferably 20 ~ 50g/L.

The most in accordance with the method for claim 1, it is characterised in that: step (2) is containing in W, Mo component saline mixed solution B, and W is with WO₃The weight concentration of meter is 10～100g/L, and preferably 20～80g/L, Mo is with MoO₃The weight concentration 5～80g/L of meter；Containing Al in described sodium metaaluminate alkaline solution₂O₃Concentration is 10 ~ 60g/L, preferably 10 ~ 40g/L.

The most in accordance with the method for claim 1, it is characterised in that: in step (1), reaction temperature is 20～90 DEG C, preferably 30～70 DEG C, during cemented into bundles, pH value controls is 6.0 ~ 11.0, being preferably 7.0 ~ 9.0, gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

The most in accordance with the method for claim 1, it is characterised in that: in step (2), reaction temperature is 30～90 DEG C, preferably 40～80 DEG C, and when flowing plastic, pH value control is 6.0 ~ 11.0, preferably 7.0 ~ 9.0.

7. gelation time is 0.2 ~ 4.0 hour, preferably 0.5 ~ 3.0 hour.

The most in accordance with the method for claim 1, it is characterised in that: in step (3), aging temperature is 40～90 DEG C, preferably 50～80 DEG C, time aging, pH value controls is 6.0 ~ 10.0, being preferably 6.5 ~ 9.0, ageing time is 0.5 ~ 6.0 hour, preferably 1.0 ~ 4.0 hours.

The most in accordance with the method for claim 1, it is characterised in that: the hydrothermal conditions described in step (3) is as follows: carry out under airtight container, and temperature is 200 ~ 300 DEG C, and pressure is 1.0 ~ 8.0 MPa, and the process time is 0.5 ~ 10.0 hour；During hydrothermal treatment consists, the addition of carbamide is 0.5:1 ~ 10.0:1 with active metal tungsten, molybdenum, the mol ratio of nickle atom total amount in catalyst.

The most in accordance with the method for claim 1, it is characterised in that: the hydrothermal conditions described in step (3) is as follows: carry out under airtight container, and temperature is 210 ~ 260 DEG C, and pressure is 3.0 ~ 6.0MPa, and the process time is 1.0 ~ 6.0 hours；During hydrothermal treatment consists, the addition of carbamide is 2.0:1 ~ 8.0:1 with active metal tungsten, molybdenum, the mol ratio of nickle atom total amount in catalyst.

11. in accordance with the method for claim 1, it is characterized in that: step (4) drying condition before shaping is as follows: be dried 1 ~ 48 hour at 50 ~ 250 DEG C, drying condition after molding is as follows: being dried 1 ~ 48 hour at 50 ~ 250 DEG C, roasting condition was as follows: 350 ~ 650 DEG C of roastings 1 ~ 24 hour.

12. in accordance with the method for claim 1, it is characterized in that: in Hydrobon catalyst preparation process, the compound containing adjuvant component is added in mixed solution A, i.e. titanium source and/or zirconium source, titanium source uses one or more in Titanium Nitrate, titanium sulfate, titanium chloride, and zirconium source uses one or more in zirconium nitrate, zirconium chloride, zirconium oxychloride.