CN103100410A - Preparation method of hydrogenation catalyst containing molecular sieve - Google Patents
Preparation method of hydrogenation catalyst containing molecular sieve Download PDFInfo
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- CN103100410A CN103100410A CN2011103558302A CN201110355830A CN103100410A CN 103100410 A CN103100410 A CN 103100410A CN 2011103558302 A CN2011103558302 A CN 2011103558302A CN 201110355830 A CN201110355830 A CN 201110355830A CN 103100410 A CN103100410 A CN 103100410A
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Abstract
The invention discloses a preparation method of a hydrogenation catalyst containing a molecular sieve. The preparation method comprises the following steps of preparing a catalyst carrier material and introducing a hydrogenation active component by a dipping method or a coprecipitation method to obtain the hydrogenation catalyst. The preparation process of the catalyst carrier material comprises the following steps of adding a mixture of a molecular sieve and an organic amine into amorphous alumina in gelling, after amorphous alumina gelling, carrying out aging, then carrying out hydrothermal treatment, and then carrying out filtration, washing and drying to obtain the catalyst carrier material. The preparation method realizes ordered arrangement and uniform deposition of alumina on the surface of the molecular sieve, improves the binding strength of the molecular sieve and alumina, avoids agglomeration of the amorphous alumina and the molecular sieve and channel blocking caused by the agglomeration, realizes mutual communication of channels of the alumina and the molecular sieve, fully develops synergism of the alumina and the molecular sieve, and improves catalyst use performances. The hydrogenation catalyst obtained by the preparation method can be used for various hydrogenation processes.
Description
Technical field
The present invention relates to a kind of preparation method of hydrogenation catalyst, especially for the preparation method of the hydrogenation catalyst that contains molecular sieve.
Background technology
Developing rapidly and crude oil heaviness and in poor quality progressively of World Economics makes market increase year by year light-end products (aeroamphibious are handed over oil universal, agricultural oils and heating oil etc.) and the demand of industrial chemicals (light aromatics, alkene and ethylene cracking material etc.); For the living environment of to protect mankind self, the progressively appearance of all kinds of environmental regulations is to the requirement that has also proposed increasingly stringent that cleans of all kinds of oil products.Hydrocracking technology is one of important means of crude oil secondary operations, heavy oil lighting.Due to it has that adaptability to raw material is strong, production operation and product solution flexibly and the characteristics such as good product quality, therefore become production high-quality lightweight clear gusoline and solved the important channel in industrial chemicals source.Hydrocracking technology has also obtained increasingly extensive application.
The key of hydrocracking technology is to develop the various hydrocracking catalysts that use the market demand.Hydrocracking catalyst is generally a kind of bifunctional catalyst, and its lytic activity and hydrogenation activity are to be provided respectively by the acidic components in catalyst and hydrogenation activity component.Acidic components in catalyst are generally to be provided by molecular sieve contained in catalyst and/or the refractory inorganic oxides that consists of carrier.Refractory inorganic oxides generally comprises one or more in amorphous aluminum silicide, amorphous alumina.Between conjugation between molecular sieve in carrier and refractory inorganic oxides and decentralization and its reactivity worth, inseparable relation is arranged, affect to a great extent the active of catalyst and selective to various purpose products.
In the patents such as CN201010197869.1, CN200810117102.6, CN00105235.7, disclosed hydrocracking catalyst is all that the raw material that molecular sieve, aluminium oxide etc. are single prepares through after mechanical mixture.The prepared catalyst of the method can be inhomogeneous because of various raw materials mixing, affects the performance of each component property.
CN1060976A discloses a kind of preparation method who contains the ultrastable of amorphous alumina.The method is that to add ammoniacal liquor to regulate the pH value in aluminum sulfate solution be 3.5～7.5, then add NaY zeolite or HNaY zeolite, mix, then prepare USY zeolite process by hydro-thermal method and carry out the subsequent treatment such as ammonium ion exchange and hydrothermal treatment consists, obtain containing the ultrastable of amorphous alumina.The method is after the aluminium oxide plastic, adds the zeolite raw material, then the composite of modification gained according to a conventional method.The method exists amorphous alumina agglomeration easily to occur, make the skewness of amorphous alumina on molecular sieve, even stop up the duct of molecular sieve, specific area and the pore volume of catalyst are significantly reduced, and the patency in molecular sieve and aluminium oxide duct is relatively poor, affects the performance of catalyst.Carry out hydrothermal treatment consists and ammonium exchange process after the method is compound with amorphous alumina by the NaY zeolite again, strengthened treating capacity, reduced the efficient of processing, in processing procedure, amorphous alumina can be processed together, easily aluminium oxide produced ill effect.
CN200610134152.6 discloses a kind of preparation method of hydrogenation catalyst, and the method is to adopt a kind of carrier material that contains molecular sieve and amorphous aluminum silicide, adopts infusion process or coprecipitation to prepare final catalyst.Wherein carrier material is directly to add the method for molecular sieve to prepare in amorphous aluminum silicide plastic process.In the method, agglomeration easily appears in amorphous aluminum silicide, also easily enter the other side's duct or the aperture of obstruction molecular sieve, affect the distribution of amorphous aluminum silicide on molecular sieve, the connectivity in molecular sieve and amorphous aluminum silicide duct is relatively poor, specific area and the pore volume of catalyst are reduced, the catalyst activity Metal Distribution is inhomogeneous, affects the performance of catalyst.
Summary of the invention
In order to overcome the deficiencies in the prior art, the invention provides a kind of preparation method who contains the hydrogenation catalyst of molecular sieve.Catalyst by the method preparation can combine molecular sieve and aluminium oxide, has good conjugation and decentralization, can avoid molecular sieve and and amorphous alumina between the even clogging that occurs reuniting, improve the serviceability of catalyst.
The present invention contains the preparation method of the hydrogenation catalyst of molecular sieve, comprise: preparation contains the catalyst carrier material of molecular sieve and aluminium oxide, adopt infusion process or coprecipitation to introduce the hydrogenation activity component, obtain final hydrogenation catalyst, wherein the preparation process of catalyst carrier material comprises:
(1) molecular sieve is mixed with organic amine, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve weight;
(2) the mixture thing that adds step (1) to obtain in amorphous alumina plastic process, take the weight of final carrier material as benchmark, the molecular sieve addition is 5wt% ~ 90wt%;
(3) carry out agingly after the described amorphous alumina cemented into bundles of step (2), then carry out hydrothermal treatment consists, after filtration, washing, drying, obtain catalyst carrier material.
In step of the present invention (1), described organic amine be carbon number greater than the fatty amine of 10, aromatic amine, in one or more.Better suited for containing the amine of chain, be preferably one or more in the fatty amines that contains 10 ~ 20 carbon numbers.For example: decyl amine, lauryl amine, cetylamine, octadecylamine, 1,10-decamethylene diamine, to one or more in butylaniline.Organic amine mixes with molecular sieve, can directly add organic amine in molecular sieve, also organic amine can be dissolved in and add in solvent in molecular sieve again, solvent wherein is one or more in water, low-carbon alcohols (being that carbon number is one or more in 1 ~ 5 monohydric alcohol).If the addition of organic amine is larger, needs to filter also and carry out again step (2) after drying.
The plastic process of the amorphous alumina described in step of the present invention (2) can be undertaken by process well known to those skilled in the art.The plastic process of amorphous alumina is generally the neutralization reaction process of acid material and alkaline material.The plastic process can adopt the mode of the continuous acid-base titration of soda acid, also can adopt the mode of two kinds of materials and stream neutralization.
In step of the present invention (2), the aluminium oxide plastic is to adopt aluminum soluble salt and acidic precipitation agent or alkaline precipitating agent to carry out the process of neutralization reaction, wherein aluminum soluble salt used is one or more in aluminium chloride, aluminum sulfate, aluminum nitrate, acidic precipitation agent used is generally one or several in hydrochloric acid, sulfuric acid, nitric acid, oxalic acid, carbon dioxide etc., and alkaline precipitating agent used is generally one or several in sodium carbonate, sodium acid carbonate, NaOH, potassium hydroxide, ammoniacal liquor etc.The aluminium oxide plastic also can adopt meta-aluminate (such as sodium metaaluminate and/or potassium metaaluminate) and acid aluminium salt (such as one or more in aluminium chloride, aluminum nitrate, aluminum sulfate) carry out in and the method for plastic.Described plastic process is generally carried out under room temperature ~ 85 ℃, is suitably for 40 ~ 80 ℃, is preferably 50 ~ 70 ℃.Described plastic process is generally carried out under certain pH value condition, and typical pH is 6.0 ~ 10.0, is suitably for 7.0 ~ 9.5, is preferably 7.5 ~ 9.0.Step (3) is described aging, and condition is as follows: pH is 6.0 ~ 10.0, is preferably 7.0 ~ 9.5, and ageing time 0.25 ~ 8 hour is adapted at 0.5 ~ 5 hour, is preferably 1 ~ 3 hour, and aging temperature is room temperature ~ 85 ℃, is preferably 40 ~ 80 ℃.Temperature when aging and pH with in and the time temperature and pH preferably identical.
In step of the present invention (1), described molecular sieve is known any or several molecular sieves, preferably one or several in modified molecular screen.In hydrogenation catalyst, molecular sieve commonly used such as Y zeolite, β zeolite, ZSM Series Molecules sieve, SAPO Series Molecules sieve, MCM Series Molecules sieve etc. one or more, for the catalytic performance that obtains to wish, various molecular sieves can carry out suitable modifying process, the process that method of modifying is well known to those skilled in the art is as one or more method modifications in hydrothermal treatment consists, acid treatment, ion-exchange, various solvent processing etc.In step of the present invention (1), the state that adds of described molecular sieve can be that dry powder-shaped adds, and can be also to add with the slurries form.
In step of the present invention (2), the introducing mode of the mixture of step (1) gained adopts the one or more combination of following manner: (1) adds this mixture in plastic cans in plastic neutralization reaction process continuously; (2) this mixture is first joined in plastic cans, then will prepare in the acid material of amorphous alumina and alkaline material and plastic; (3) one or more with the plastic material of this mixture are mixed, then in the plastic material and plastic.
In step of the present invention (3), before hydrothermal treatment consists, preferably after filtration or the heating concentration, remove excessive moisture and organic matter.Wherein said heating simmer down to is at 90 ~ 110 ℃ of lower heating stepses (2) products obtained therefrom, and temperature is 95 ~ 105 ℃ preferably, preferably 98 ~ 100 ℃, is heated to immobilising paste shape.
In step of the present invention (3), described hydrothermal treatment consists is carried out in closed container, and the temperature of hydrothermal treatment consists is 90 ~ 300 ℃, preferably 100 ~ 250 ℃, be preferably 150 ~ 210 ℃, described hydrothermal treatment consists is for carrying out under self the pressure condition that produces when the material treatment temperature.The described hydrothermal treatment consists time is 0.5 ~ 48h, is 1 ~ 36h, preferably 2 ~ 24h preferably.
In step of the present invention (3), the mode of washing of described material is known in those skilled in the art, can select the making beating washing, add the modes such as water washing, lower alcohols washing when filtering, the temperature of washing should be in the scope of room temperature ~ 90 ℃ temperature, preferred 50 ~ 70 ℃.The washing of described material is generally carried out in pH is 1.0 ~ 9.0 scope, and preferred pH is 4.0 ~ 8.5.Material described in step of the present invention (3) should not contain or contain the seldom heteroion of amount after washing, filtration, heteroion comprises Na
+, Cl
-, SO
4 2-, NO
3 -, K
+Deng in one or more.
In step of the present invention (3), described material is after washing, filtering, filter cake carries out drying, and that drying mode can adopt is natural drying, oven drying, spray-drying, microwave drying or infra-red drying, and general drying condition is as follows: under 50 ~ 150 ℃ dry 1 ~ 15 hour.
Carrier material of the present invention also can add other auxiliary agent as required, as one or more in phosphorus, boron, titanium, zirconium etc.
The carrier material of the inventive method preparation is a kind of raw material of Kaolinite Preparation of Catalyst carrier, this carrier material is through 450 ~ 650 ℃ of roastings after 2 ~ 10 hours, the character of gained is as follows: the weight of carrier material is as benchmark after the roasting, the content of molecular sieve is 5wt% ~ 90wt%, the content of aluminium oxide is at 10 wt% ~ 95wt%, and specific area is 200 ~ 800m
2/ g, pore volume are 0.3 ~ 1.8cm
3/ g, the meleic acid amount is 0.1 ~ 2.0 mmol/g.
In the inventive method, the hydrogenation activity component is generally one or more in group vib and group VIII metal, as one or more in molybdenum, tungsten, nickel, cobalt etc., the content of hydrogenation activity component in catalyst is generally 5% ~ 80%(in oxide, lower same), suitable content is 10% ~ 50%, can specifically determine according to the requirement of using.The introducing method of hydrogenation activity component is generally infusion process, coprecipitation etc., and concrete introducing method is content well known to those skilled in the art.As when adopting infusion process, first with carrier material moulding, drying, roasting, then with the carrier after the solution impregnation moulding that contains active hydrogenation component, then drying, roasting, obtain final hydrogenation catalyst.When adopting coprecipitation, with the carrier material making beating, hydrogenation active metals is deposited in the carrier material slurries, then through washing, moulding, drying, roasting, obtains final hydrogenation catalyst.Above-mentioned catalyst preparation process and condition are all well known to those skilled in the art.In the carrier forming process, can add other carrier material or auxiliary agent, as one or more in boron oxide, titanium oxide, zirconia etc.
in the preparation process of hydrogenation catalyst of the present invention, molecular sieve mixes with organic amine in advance, organic amine can be adsorbed onto duct and the place, aperture of molecular sieve in advance, the pore passage structure of molecular sieve is protected in advance, can avoid like this that in aluminium oxide plastic process, fragment enters the duct, stop up aperture or direct plastic in the duct, organic amine has the guide effect to the aluminium oxide duct in aluminium oxide plastic process simultaneously, organic amine part chain end extends in the outside, duct of molecular sieve, the aluminium oxide that can lead plastic is outside in the duct of molecular sieve, the direction that stretches along chain be wrapped in the chain extended end around, avoided amorphous alumina staggered with duct between molecular sieve, the phenomenon in duct is even stopped up in reunion mutually, the duct of aluminium oxide and molecular sieve is connected mutually, aluminium oxide and molecular sieve are given full play to synergy, the aging amorphous alumina colloidal sol that helps is assembled gradually, even pore-forming, hydrothermal treatment consists helps the mesopore of aluminium oxide formation rule.Be conducive to the diffusion of reaction mass between catalyst inner surface and outer surface, be conducive to the even distribution of reactive metal, improve the utilization rate of reactive metal, thereby improved the serviceability of catalyst.Preferably according to requirements adopted suitable method to carry out modification before molecular sieve is introduced, the modification process of molecular sieve can not produce adverse influence to composite carrier like this.
Description of drawings
Fig. 1 is the pore size distribution figure of embodiment 2 and Comparative Examples 3 gained carrier materials.
The specific embodiment
The preparation process of explanation hydrogenation catalyst of the present invention as an example of infusion process example, specific as follows: catalyst carrier material and other components such as adhesive and auxiliary agent through mix, roll, the means moulding such as extrusion, then carry out drying, roasting, obtain catalyst carrier, then adopt conventional dipping method with containing active metallic compound (such as molybdenum and/or tungsten, nickel and/or cobalt compound) solution impregnation metal, then carry out drying, roasting obtains catalyst prod.Wherein, after the catalyst carrier material moulding, drying condition is generally at 80 ~ 200 ℃, and dry 1 ~ 15 hour, sintering temperature was generally 450 ~ 700 ℃, and roasting time is generally 1 ~ 10 hour.After impregnation of catalyst carriers supported active metal, the drying condition of catalyst is as follows: be generally at 80 ~ 200 ℃, dry 1 ~ 15 hour, the roasting condition of catalyst was 350 ~ 550 ℃ of lower roastings 1 ~ 8 hour.
In the inventive method, described molybdenum and/or tungsten, nickel and/or the cobalt compound of containing, can be by one or more in the soluble compound that is selected from nickeliferous and/or cobalt metal, as the solution of one or more preparations in their nitrate, acetate, soluble carbonate salt, chloride, soluble complexes; Can be by be selected from the soluble compound that contains molybdenum and/or tungsten metal one or more, as the solution of one or more preparations in molybdate, tungstates, ethyl metatungstate, it can be the mixed solution by the solubility platform thing preparation of the soluble compound of nickeliferous and/or cobalt metal and molybdenum and/or tungsten metal; Can also be by the heteropoly acid of nickeliferous and/or cobalt metal and molybdenum and/or tungsten metal or the aqueous solution of salt preparation.According to method provided by the invention, to not restriction of the solvent in solution, can be organic solvent, as alcohol, ether and acid, can be inorganic solvent, as water and their mixture, preferred water.
For hydrocracking catalyst, the hydrogenation activity component is molybdenum and/or tungsten and nickel and/or cobalt, take the weight of catalyst as benchmark, in oxide, the content of molybdenum and/or tungsten is 5% ~ 40%, is preferably 12% ~ 35%, the content of nickel and/or cobalt is l% ~ 15%, is preferably 5% ~ 13%.
Catalyst preparation process of the present invention is simple, convenient, and easy operating is fit to industrial production.When selecting suitable molecular sieve (modified Y molecular sieve and modified beta molecular sieve), catalyst is used for hydrocracking process, can effectively improve reaction mass at the mass transfer of catalyst, that improves the activity of catalyst and purpose product selectively can obtain good result of use.Catalyst of the present invention is particularly suitable for treatment of heavy hydrocarbon material, the boiling range scope of heavy hydrocarbon material is at 250 ~ 600 ℃, generally at 300 ~ 550 ℃, have These characteristics feedstock oil such as gas oil, vacuum distillate, take off pitch prill oil, catalytic cracking recycle oil, shale oil, coal tar wet goods.Reaction condition generally under the hydrogen existence condition, reaction pressure 5 ~ 30MPa, hydrogen to oil volume ratio 100 ~ 5000, volume space velocity 0.1 ~ 5.0h during liquid
-1, 340 ~ 420 ℃ of reaction temperatures.Catalyst of the present invention when processing common VGO, reaction condition generally under the hydrogen existence condition, the best 10 ~ 20MPa of reaction pressure, hydrogen to oil volume ratio 500 ~ 2000, volume space velocity 0.5 ~ 1.5h during liquid
-1, 370 ~ 410 ℃ of reaction temperatures.
The specific area of product of the present invention and pore volume are to adopt the low temperature liquid nitrogen physisorphtion to measure, and relative crystallinity and cell parameter adopt X-ray diffraction method to measure.Sodium content adopts By Icp-aes.In the present invention, wt% is mass fraction.
Further illustrate preparation method of the present invention below in conjunction with specific embodiment, but scope of the present invention is not only limited to the scope of these embodiment.
Embodiment 1
The 500g solid aluminum chloride is joined in 2.5 liters of distilled water, heat simultaneously and be stirred to dissolving, obtain liquor alumini chloridi (a).Add appropriate distilled water diluting into about 10wt% weak aqua ammonia (b) concentrated ammonia liquor, the 13.5g decyl amine is dissolved in the 300ml absolute ethyl alcohol, is heated to 60 ℃, under stirring, adds 34g Modified Zeolite Y Y-1 (SiO
2/ Al
2O
3Mol ratio is 11.0, and lattice constant is 24.42, and relative crystallinity is 95%), stirred 2 hours, filter, filter cake is dried to get (c) at 100 ℃ of lower 4h.Get a stainless steel reaction tank, after adding (a) in tank and being heated with stirring to 60 ℃, open the valve of the container that has (b), within controlling 10 minutes, system in tank is added drop-wise to pH=4.0, add (c) this moment in tank, continue to drip (b), system in tank is added drop-wise to pH=8.0 in controlling 30 minutes.Keeping temperature is 60 ℃, pH=8.0, aging 1 hour, with material in tank under 100 ℃ at the baking oven inner drying to contents on dry basis 15wt%, material is transferred in autoclave, processed 18h under 165 ℃ of conditions, then material is used ethanol to carry out solvent extraction and remove a part of organic matter, filter, washing was filtered to without chlorion, with filter cake under 110 ℃ dry 10 hours, pulverize and sieve, obtain containing the composite carrier S-1 of modification Y molecular sieve 15wt%.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 550 ℃ of roastings.
Get product S-1 carrier material 80 grams, adhesive 20 grams mix, extruded moulding after rolling, dry and roasting is placed in reaction vessel, takes ammonium metatungstate 50 grams and is dissolved in water into 200 ml solns with nickel nitrate 23 grams, solution is joined reaction vessel dipping 3 hours, then dry under 120 ℃, after dry 180 minutes, with dried catalyst 500 ℃ of roastings 4 hours, obtain catalyst A, its composition sees Table 2.
500g solid sulphuric acid aluminium is joined in 2.5 liters of distilled water, heat simultaneously and be stirred to dissolving, obtain aluminum sulfate solution (a).Add appropriate distilled water diluting into about 10wt% weak aqua ammonia (b) concentrated ammonia liquor, the 45g cetylamine is dissolved in 1L ethanol, is heated to 65 ℃, under stirring, adds 224g Modified Zeolite Y Y-1 (SiO
2/ Al
2O
3Mol ratio is 11.0, and lattice constant is 24.42, and relative crystallinity is 95%), stir 2h, filter, filter cake is got (c) at 110 ℃ of oven dry 12h.Get a stainless steel reaction tank, after adding (a) in tank and being heated with stirring to 60 ℃, open the valve of the container that has (b), within controlling 10 minutes, system in tank is added drop-wise to pH=4.5, add (d) this moment in tank, continue to drip (b), system in tank is added drop-wise to pH=8.0 in controlling 30 minutes.Keeping temperature is 60 ℃, pH=8.0, aging 1 hour, with material in tank under 100 ℃ at the baking oven inner drying to contents on dry basis 15wt%, material is transferred in autoclave, processed 4h under 180 ℃ of conditions, use ethanol to carry out a solvent extraction part organic matter material, filter, wash to the sulfate radical-free ion, filter, with filter cake under 110 ℃ dry 10 hours, pulverize and sieve, obtain containing the composite carrier S-2 of Modified Zeolite Y 60wt%.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 500 ℃ of roastings.Fig. 1 is seen in pore size distribution.
Get product S-2 carrier material 80 grams, adhesive 20 grams mix, extruded moulding after rolling, dry and roasting is placed in reaction vessel, takes ammonium metatungstate 50 grams and is dissolved in water into 200 ml solns with nickel nitrate 23 grams, solution is joined reaction vessel dipping 3 hours, then dry under 120 ℃, after dry 180 minutes, with dried catalyst 500 ℃ of roastings 4 hours, obtain catalyst B, its composition sees Table 2.
Embodiment 3
250g solid sulphuric acid aluminium is joined in 1 liter of distilled water, heat simultaneously and be stirred to dissolving, obtain aluminum sulfate solution (a).It is 20g Al that the solid sodium metaaluminate is mixed with concentration
2O
3/ l sodium aluminate solution (b), the 85g octadecylamine is dissolved in 4L ethanol, is heated to 65 ℃, under stirring, adds 844g Modified Zeolite Y Y-1 (SiO
2/ Al
2O
3Mol ratio is 11.0, and lattice constant is 24.42, and relative crystallinity is 95%), stir 2h, get slurries (c).Get a stainless steel reaction tank, after inserting the 1L deionized water and stirring and being heated to 60 ℃, open simultaneously have (a), the valve of (b) and container (c), the pH=8.0 of the hierarchy of control drips off with (a) with (c) in controlling 45 minutes.Keeping temperature is 60 ℃, PH=8.0, aging 1 hour, with material filtering in tank to contents on dry basis 15wt%, material is transferred in autoclave, process 4h under 180 ℃ of conditions, filter, wash to the sulfate radical-free ion, filter, with filter cake under 110 ℃ dry 10 hours, pulverize and sieve, obtain containing the composite carrier S-3 of Modified Zeolite Y 85wt%.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 500 ℃ of roastings.
Get product S-3 carrier material 80 grams, adhesive 20 grams mix, extruded moulding after rolling, dry and roasting is placed in reaction vessel, takes ammonium metatungstate 50 grams and is dissolved in water into 200 ml solns with nickel nitrate 23 grams, solution is joined reaction vessel dipping 3 hours, then dry under 120 ℃, after dry 180 minutes, with dried catalyst 500 ℃ of roastings 4 hours, obtain catalyst C, its composition sees Table 2.
Embodiment 4
The 500g solid aluminum chloride is joined in 3 liters of distilled water, heat simultaneously and be stirred to dissolving, obtain liquor alumini chloridi (a).Add appropriate distilled water diluting into about 10% weak aqua ammonia (b) concentrated ammonia liquor, the 6g cetylamine is dissolved in 100ml ethanol, is heated to 60 ℃, under stirring, adds the Hydrogen β zeolite B-1 (SiO of 15g modification
2/ Al
2O
3Mol ratio is 30.0, and lattice constant is 12.00, and relative crystallinity is 90%), stir 1h, filter, filter cake (c).Get a stainless steel reaction tank, after adding (a) in tank and being heated with stirring to 60 ℃, open the valve of the container that has (b), within controlling 10 minutes, system in tank is added drop-wise to pH=4.0, add (c) this moment in tank, continue to drip (b), system in tank is added drop-wise to pH=8.0 in controlling 30 minutes.Keeping temperature is 60 ℃, pH=8.0, aging 1 hour, with material in tank under 100 ℃ at the baking oven inner drying to contents on dry basis 15wt%, material is transferred in autoclave, processed 18h under 165 ℃ of conditions, use ethanol to carry out a solvent extraction part organic matter material, filter, washing was filtered to without chlorion, with filter cake under 110 ℃ dry 10 hours, pulverize and sieve, obtain containing the composite carrier S-4 of modified beta zeolite 7wt%.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 500 ℃ of roastings.
Get product S-4 carrier material 80 grams, adhesive 20 grams mix, extruded moulding after rolling, dry and roasting is placed in reaction vessel, takes ammonium metatungstate 50 grams and is dissolved in water into 200 ml solns with nickel nitrate 23 grams, solution is joined reaction vessel dipping 3 hours, then dry under 120 ℃, after dry 180 minutes, with dried catalyst 500 ℃ of roastings 4 hours, obtain catalyst D, its composition sees Table 2.
Comparative Examples 1
Repeat the synthetic of embodiment 2, do not add organic amine, make comparison vehicle material DF-1.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 550 ℃ of roastings.
The process of carrier material DF-1 synthetic catalyst obtains catalyst DA with embodiment 2, and its composition sees Table 2.
Comparative Examples 2
Repeat the synthetic of embodiment 2, do not add Y zeolite Y-1 and organic amine, make comparison vehicle material DF-2.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 550 ℃ of roastings.
The process of carrier material DF-2 synthetic catalyst obtains catalyst DB with embodiment 2, and its composition sees Table 2.
Comparative Examples 3
Repeat the synthetic of embodiment 2, do not carry out hydrothermal treatment consists, make comparative composite DF-3.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 550 ℃ of roastings.Fig. 1 is seen in pore size distribution.
The process of carrier material DF-3 synthetic catalyst obtains catalyst D C with embodiment 2, and its composition sees Table 2.
Comparative Examples 4
Repeat the synthetic of embodiment 4, do not carry out hydrothermal treatment consists, make contrast composite carrier DF-4.After 5 hours, the Main physical chemical property of gained carrier material sees Table 1 through 550 ℃ of roastings.
The process of carrier material DF-4 synthetic catalyst obtains catalyst DD with embodiment 4, and its composition sees Table 2.
Table 1 composite carrier main character
| Bearer number | S-1 | S-2 | S-3 | DF-1 | DF-2 | DF-3 | Y-1 | S-4 | DF-4 | B-1 |
| Specific area, m 2/g | 396 | 586 | 691 | 468 | 351 | 580 | 786 | 346 | 342 | 553 |
| Pore volume, ml/g | 0.80 | 0.57 | 0.43 | 0.48 | 0.87 | 0.56 | 0.37 | 0.85 | 0.84 | 0.40 |
By as seen from Table 1, use the prepared molecular sieve of this method-alumina catalyst carrier material specific area and pore volume to obtain improving greatly, can effectively solve the problem that the amorphous alumina that causes even stops up with the reunion between molecular sieve when plastic; By relatively can finding out of Fig. 1 pore size distribution, the carrier material for preparing by this method has the middle pore size distribution of more concentrating.
The composition of table 2 catalyst and character
| The catalyst numbering | A | B | C | D | DA | DB | DC | DD |
| WO 3，wt％ | 20.68 | 20.64 | 22.17 | 22.48 | 21.81 | 21.61 | 23.22 | 23.32 |
| NiO，wt％ | 5.58 | 5.64 | 6.07 | 6.87 | 6.50 | 5.94 | 6.68 | 6.93 |
| Specific area, m 2/g | 249 | 354 | 400 | 212 | 280 | 220 | 332 | 207 |
| Pore volume, ml/g | 0.50 | 0.38 | 0.29 | 0.51 | 0.32 | 0.53 | 0.35 | 0.49 |
The invention described above catalyst and comparative catalyst thereof are estimated.Estimating is Iranian VGO with feedstock oil, and character sees Table 3, and appreciation condition is as follows: reaction pressure 14MPa, hydrogen to oil volume ratio 1500, volume space velocity 1.5 h during liquid
-1Main character sees Table 4.
Table 3 raw material oil properties
| Density, d 4 20 | 0.9024 | Mass spectral analysis, wt% | ? |
| Boiling range, ℃ | ? | Alkane | 19.7 |
| IBP | 321 | Cycloalkane | 36.7 |
| 10% | 393 | Aromatic hydrocarbons | 41.1 |
| 50% | 443 | Colloid | 25 |
| 90% | 497 | S，wt% | 1.01 |
| EP | 528 | N，μg/g | 1138 |
| Carbon residue, wt% | 0.03 | The BMCI value | 40.3 |
Table 4 evaluation result
| The catalyst numbering | B | DA | DC |
| Conversion ratio, wt% | 55 | 55 | 55 |
| Reaction temperature, ℃ | 352 | 355 | 353 |
| Heavy naphtha is selective, wt% | 82.9 | 78.7 | 80.7 |
| The heavy naphtha virtue is dived, wt% | 55 | 51 | 53 |
Can find out from evaluation result, use the catalyst of the inventive method preparation to have activity and product selectivity preferably.
Claims (16)
1. the preparation method of a hydrogenation catalyst comprises: preparation contains the catalyst carrier material of molecular sieve and aluminium oxide, adopts infusion process or coprecipitation to introduce the hydrogenation activity component, obtains final hydrogenation catalyst, and wherein the preparation process of carrier material comprises:
(1) molecular sieve is mixed with organic amine, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve weight;
(2) mixture that adds step (1) to obtain in amorphous alumina plastic process, take the weight of final carrier material as benchmark, the molecular sieve addition is 5wt% ~ 90wt%;
(3) carry out agingly after the described amorphous alumina cemented into bundles of step (2), then carry out hydrothermal treatment consists, after filtration, washing, drying, obtain catalyst carrier material.
2. in accordance with the method for claim 1, it is characterized in that in step (1), described organic amine is carbon number greater than the fatty amine of 10, one or more in aromatic amine.
3. in accordance with the method for claim 1, it is characterized in that in step (1), described organic amine is for containing one or more in the fatty amines of 10 ~ 20 carbon numbers.
4. in accordance with the method for claim 1, it is characterized in that in step (1), described organic amine and molecular sieve mixed method: directly add organic amine in molecular sieve, perhaps organic amine is dissolved in and adds in solvent in molecular sieve again, solvent wherein is one or more in water, low-carbon alcohols; Described low-carbon alcohols is that carbon number is one or more in 1 ~ 5 monohydric alcohol.
5. in accordance with the method for claim 1, after it is characterized in that step (1) molecular sieve and organic amine mixing, carry out again step (2) after filtration and after drying.
6. in accordance with the method for claim 1, the plastic process that it is characterized in that the amorphous alumina described in step (2) is the neutralization reaction process of acid material and alkaline material, the plastic process adopts the mode of the continuous acid-base titration of soda acid, perhaps adopts the mode of two kinds of materials and stream neutralization.
7. in accordance with the method for claim 1, it is characterized in that in step (2), the aluminium oxide plastic is to adopt aluminum soluble salt and acidic precipitation agent or alkaline precipitating agent to carry out the process of neutralization reaction, wherein aluminum soluble salt used is one or more in aluminium chloride, aluminum sulfate, aluminum nitrate, acidic precipitation agent used is one or several in hydrochloric acid, sulfuric acid, nitric acid, oxalic acid, carbon dioxide, and alkaline precipitating agent used is one or several in sodium carbonate, sodium acid carbonate, NaOH, potassium hydroxide, ammoniacal liquor.
8. in accordance with the method for claim 1, it is characterized in that in step (2), the aluminium oxide plastic adopt meta-aluminate and acid aluminium salt carry out in the method for plastic.
9. in accordance with the method for claim 1, it is characterized in that in step (1), described molecular sieve is one or more in Y zeolite, β zeolite, ZSM Series Molecules sieve, SAPO Series Molecules sieve, MCM Series Molecules sieve and above-mentioned modified molecular screen.
10. in accordance with the method for claim 1, it is characterized in that in step (1), the state that adds of described molecular sieve is that dry powder-shaped adds, or adds with the slurries form.
11. in accordance with the method for claim 1, it is characterized in that in step (2), the introducing mode of the mixture of step (1) gained adopts the one or more combination of following manner: (1) adds this mixture in plastic cans in plastic neutralization reaction process continuously; (2) this mixture is first joined in plastic cans, then will prepare in the acid material of amorphous alumina and alkaline material and plastic; (3) one or more with the plastic material of this mixture are mixed, then in the plastic material and plastic.
12. it is characterized in that in step (3), before hydrothermal treatment consists in accordance with the method for claim 1,, after filtration or the heating concentration, remove excessive moisture and organic matter, described heating simmer down to is heated to immobilising paste shape at 90 ~ 110 ℃ of lower heating stepses (2) products obtained therefrom.
13. in accordance with the method for claim 1, it is characterized in that in step (3), described hydrothermal treatment consists is carried out in closed container, the temperature of hydrothermal treatment consists is 90 ~ 300 ℃, described hydrothermal treatment consists is for carrying out under self the pressure condition that produces when the material treatment temperature, and the described hydrothermal treatment consists time is 0.5 ~ 48h.
14. in accordance with the method for claim 1, it is characterized in that in step (3), described hydrothermal treatment consists is carried out in closed container, the temperature of hydrothermal treatment consists is 100 ~ 250 ℃, described hydrothermal treatment consists is for carrying out under self the pressure condition that produces when the material treatment temperature, and the described hydrothermal treatment consists time is 1 ~ 36h.
15. in accordance with the method for claim 1, it is characterized in that described hydrogenation activity component is one or more in group vib and group VIII metal, the content of hydrogenation activity component in catalyst counts 5% ~ 80% with oxide.
16. according to the described method of claim 1 or 15, it is characterized in that described hydrogenation activity component is one or more in molybdenum, tungsten, nickel, cobalt.
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