CN103100409B - Preparation method of hydrogenation catalyst - Google Patents
Preparation method of hydrogenation catalyst Download PDFInfo
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- CN103100409B CN103100409B CN201110355829.XA CN201110355829A CN103100409B CN 103100409 B CN103100409 B CN 103100409B CN 201110355829 A CN201110355829 A CN 201110355829A CN 103100409 B CN103100409 B CN 103100409B
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Abstract
The invention discloses a preparation method of a hydrogenation catalyst. 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. A preparation method of the catalyst carrier material comprises the following steps of adding a mixture of a molecular sieve and an organic amine into amorphous silica-alumina in gelling, after amorphous silica-alumina gelling, carrying out aging, and then carrying out filtration, washing and drying to obtain the catalyst carrier material. The preparation method realizes ordered arrangement and uniform deposition of the silica-alumina on the surface of the molecular sieve, improves the binding strength of the molecular sieve and the silica-alumina, avoids agglomeration of the amorphous silica-alumina and the molecular sieve and channel blocking caused by the agglomeration, realizes mutual communication of channels of the silica-alumina and the molecular sieve, fully develops synergism of the silica-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 method preparing hydrogenation catalyst, especially for the preparation method of the hydrogenation catalyst containing molecular sieve and amorphous aluminum silicide.
Background technology
Developing rapidly and crude oil heaviness progressively and in poor quality of World Economics, makes market increase year by year light-end products (aeroamphibious hand over oil universal, agricultural oils and heating oil etc.) and the demand of industrial chemicals (light aromatics, alkene and ethylene cracking material etc.); In order to protect the living environment of mankind itself, the progressively appearance of all kinds of environmental regulation, cleans to all kinds of oil product the requirement that it is also proposed increasingly stringent.Hydrocracking technology is one of the important means of crude oil secondary operations, heavy oil lighting.Due to it have that adaptability to raw material is strong, production operation and products scheme flexibly and the feature such as good product quality, therefore become production high-quality lightweight clear gusoline and solved the important channel in industrial chemicals source.Hydrocracking technology have also been obtained increasingly extensive application.
The key of hydrocracking technology develops the various hydrocracking catalysts of meeting the need of market.Hydrocracking catalyst is generally bifunctional catalyst, and its lytic activity and hydrogenation activity are provided respectively by the acidic components in catalyst and hydrogenation active component.Acidic components in catalyst are generally provided by molecular sieve contained in catalyst and/or the refractory inorganic oxides that forms carrier.Refractory inorganic oxides generally comprise in amorphous aluminum silicide, amorphous alumina one or more.Molecular sieve in carrier has inseparable relation with the conjugation between refractory inorganic oxides with between decentralization and its reactivity worth, affects the activity of catalyst and selective to various object product to a great extent.
Hydrocracking catalyst disclosed in the patents such as CN201010197869.1, CN200810117102.6, CN00105235.7 is all prepared after mechanical mixture by raw material single to molecular sieve, aluminium oxide etc.Catalyst prepared by the method can be uneven because of various raw material mixing, affects the performance of each component property.
CN1060976A discloses a kind of preparation method of the ultrastable containing amorphous alumina.The method is that in aluminum sulfate solution, add ammoniacal liquor adjust ph be 3.5 ~ 7.5, then NaY zeolite or HNaY zeolite is added, 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 the ultrastable containing amorphous alumina.The method is after aluminium oxide plastic, adds zeolite materials, then the composite of modification gained according to a conventional method.There is amorphous alumina and easily occur agglomeration in the method, make amorphous alumina skewness over a molecular sieve, even block the duct of molecular sieve, the specific area of catalyst and pore volume are significantly reduced, and the patency in molecular sieve and aluminium oxide duct is poor, affect the performance of catalyst.The method carries out hydrothermal treatment consists and ammonium exchange process by NaY zeolite again with after amorphous alumina compound, increases treating capacity, reduces the efficiency of process, and in processing procedure, amorphous alumina can be processed together, easily produces ill effect to aluminium oxide.
CN200610134152.6 discloses a kind of preparation method of hydrogenation catalyst, and the method adopts a kind of carrier material containing molecular sieve and amorphous aluminum silicide, adopts infusion process or coprecipitation to prepare final catalyst.Wherein carrier material is prepared by the method directly adding molecular sieve in amorphous aluminum silicide plastic process.In the method easily there is agglomeration in amorphous aluminum silicide, also easily enter the duct of the other side or the aperture of blocking molecular sieve, affect amorphous aluminum silicide distribution over a molecular sieve, the connectivity in molecular sieve and amorphous aluminum silicide duct is poor, the specific area of catalyst and pore volume are reduced, catalyst activity Metal Distribution is uneven, 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 of hydrogenation catalyst.Molecular sieve and amorphous aluminum silicide can combine by the catalyst prepared by the method, there is good conjugation and decentralization, can avoid occurs between molecular sieve and amorphous aluminum silicide reuniting blocks the phenomenon in duct even mutually, improves the serviceability of catalyst.
The preparation method of hydrogenation catalyst of the present invention, comprise: preparation contains the catalyst carrier material of molecular sieve and amorphous aluminum silicide, adopt infusion process or coprecipitation to introduce hydrogenation active component, obtain final hydrogenation catalyst, wherein the preparation process of catalyst carrier material comprises:
(1) mixed with organic amine by molecular sieve, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve;
(2) in amorphous aluminum silicide plastic process, add the mixture that step (1) obtains, with the weight of final carrier material for benchmark, molecular sieve addition is 5wt% ~ 90wt%;
(3) carry out aging after the amorphous aluminum silicide cemented into bundles described in step (2), then after filtration, washing, dry, obtain catalyst carrier dry gel powder.
In step of the present invention (1), described organic amine is fatty amine, aromatic amine, one or more in hydramine that carbon number is less than 20.Better suited is the amine containing chain, is preferably containing one or more in the fatty amines of 2 ~ 10 carbon numbers.Such as: propylamine, tert-butylamine; Decyl amine, dimethylamine, di-n-propylamine, butylamine, hexylamine, ethamine, 2 ethyl hexylamine, diethylamine, diisopropylamine, hexamethylene diamine, 1,2-dimethyl propylamine, sec-butylamine, 1,5-dimethylhexylamine, ethylenediamine, 1, one or more in 2-propane diamine, Putriscine, monoethanolamine, diethanol amine, triethanolamine, 3-Propanolamine, monoisopropanolamine, diisopropanolamine (DIPA), triisopropanolamine, aniline.Organic amine mixes with molecular sieve, organic amine directly can be added in molecular sieve, also organic amine can be dissolved in solvent and add again in molecular sieve, solvent is wherein water, one or more in low-carbon alcohols (namely carbon number is one or more in the monohydric alcohol of 1 ~ 5).If the addition of organic amine is comparatively large, needs to filter and carry out step (2) again after drying.
Amorphous aluminum silicide plastic process described in step of the present invention (2) can be undertaken by process well known to those skilled in the art.Amorphous aluminum silicide plastic process is generally the neutralization reaction process of acid material and alkaline material, and plastic process generally adopts two kinds of materials and flows plastic mode of operation, or a kind of material is placed on another kind of material in plastic cans and adds the mode of operation of plastic continuously.Plastic material generally comprises aluminium source (Al
2(SO
4)
3, AlCl
3, Al (NO
3)
3and NaAlO
2deng in one or more), silicon source (in waterglass, Ludox and organic silicon-containing compound etc. one or more), precipitating reagent (NaOH, NH
4oH or CO
2deng), the different choice according to plastic process uses, and conventional mode of operation mainly contains: (1) acid aluminium salt (Al
2(SO
4)
3, AlCl
3, Al (NO
3)
3) and basic aluminium salt (NaAlO
2) or alkaline precipitating agent (NaOH, NH
4oH) in and plastic, (2) basic aluminium salt (NaAlO
2) and acidic precipitation agent (CO
2) in and plastic.Plastic cans is generally introduced in silicon source in plastic process, also can with aluminium source or precipitant mix after again in and plastic, as waterglass add carry out in basic aluminium salt or alkaline precipitating agent in and plastic, Ludox add carry out in acid aluminium salt in and plastic etc.Silicon source also can add after the precipitation of aluminium source in material, also can two or more is combined by aforesaid way.Said method is all well-known to those skilled in the art.Described plastic process is generally carried out at room temperature ~ 85 DEG C, is comparatively suitably for 40 ~ 80 DEG C, is preferably 50 ~ 70 DEG C.Described plastic process is generally carried out under certain pH value condition, and typical pH is 6.0 ~ 10.0, is comparatively suitably for 7.0 ~ 9.5, is preferably 7.5 ~ 9.0.Aging described in step (3), condition is as follows: pH is 6.0 ~ 10.0, and be preferably 7.0 ~ 9.5, ageing time 0.25 ~ 8 hour, is comparatively adapted at 0.5 ~ 5 hour, and be preferably 1 ~ 3 hour, aging temperature is room temperature ~ 85 DEG C, is preferably 40 ~ 80 DEG C.Temperature time aging and pH with in time temperature preferably identical with pH.
In step of the present invention (1), described molecular sieve is known any one or several molecular sieve, one or several in best modified molecular screen.In hydrogenation catalyst, conventional molecular sieve as Y zeolite, β zeolite, ZSM Series Molecules sieve, SAPO Series Molecules sieve, MCM Series Molecules sieve etc. one or more, these molecular sieves are that those skilled in that art are known.In order to obtain the catalytic performance of hope, various molecular sieve can carry out suitable modifying process, the process that method of modifying is well known to those skilled in the art, as one or more method modifications in hydrothermal treatment consists, acid treatment, ion-exchange, various solvent process etc.In step of the present invention (1), the state that adds of described molecular sieve can be that dry powder-shaped adds, and also can be add with slurries form.
In step of the present invention (2), the incorporation way of the mixture of step (1) gained adopts the one or more combination of following manner: this mixture, in plastic neutralization reaction process, adds in plastic cans by (1) continuously; (2) this mixture is first joined in plastic cans, then will prepare in the acid material of amorphous aluminum silicide and alkaline material and plastic; (3) one or more with plastic material of this mixture are mixed, then in plastic material and plastic.
In step of the present invention (3), the mode of washing of described material is known in those skilled in the art, can select to add the mode such as water washing, lower alcohols washing when making beating washing, filtration, the temperature of washing should in the scope of room temperature ~ 90 DEG C temperature, preferably 50 ~ 70 DEG C.The washing of described material is generally carried out in the scope that pH is 1.0 ~ 9.0, and preferred pH is 4.0 ~ 8.5.Material described in step of the present invention (3) should not contain or contain the heteroion of seldom amount after washing, filtration, and 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 drying mode can adopt natural drying, oven drying, spraying dry, microwave drying or infra-red drying, and general drying condition is as follows: drying 1 ~ 15 hour at 50 ~ 150 DEG C.
Carrier material of the present invention also can add other auxiliary agent as required, as one or more in phosphorus, boron, titanium, zirconium etc.
Carrier dry gel powder prepared by the inventive method is a kind of raw material of Kaolinite Preparation of Catalyst carrier, through 450 ~ 650 DEG C of roastings after 2 ~ 10 hours, with the weight of carrier after roasting for benchmark, the content of molecular sieve is 5 wt% ~ 90wt%, the content of amorphous aluminum silicide at 10 wt% ~ 95wt%, in amorphous aluminum silicide, SiO
2content is generally 10wt% ~ 50wt%, and after roasting, the character of carrier is as follows: specific area is 200 ~ 1000m
2/ g, pore volume is 0.3 ~ 1.8cm
3/ g, meleic acid amount is 0.1 ~ 2.0mmol/g.
In the inventive method, hydrogenation active component is generally one or more in group vib and group VIII metal, as one or more in molybdenum, tungsten, nickel, cobalt etc., hydrogenation active component content is in the catalyst generally 5% ~ 80%(with oxide basis, lower same), suitable content is 10% ~ 50%, specifically can determine according to the requirement used.The introducing method of hydrogenation active component is generally infusion process, coprecipitation etc., and concrete introducing method is content well known to those skilled in the art.During as adopted infusion process, first by shaping for carrier material, dry, roasting, the carrier after then shaping by the solution impregnation containing Active hydrogenation component, then drying, roasting, obtain final hydrogenation catalyst.When adopting coprecipitation, pulled an oar by carrier material, hydrogenation active metals is deposited in carrier material slurries, then through washing, shaping, dry, roasting, obtains final hydrogenation catalyst.Above-mentioned catalyst preparation process and condition are all well known to those skilled in the art.In carrier forming process, other carrier material or auxiliary agent can be added, 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 aperture place of molecular sieve in advance, the pore passage structure of molecular sieve is protected in advance, fragment in amorphous aluminum silicide plastic process can be avoided like this to enter duct, blocking aperture or direct plastic in duct, organic amine has the guide effect to sial duct in sial plastic process simultaneously, long-chain end group directly extends in solvent from the duct of molecular sieve, there is hydrophilic sial in molecular sieve surface arrangement in order, be deposited on the surface of molecular sieve equably, and enhance the adhesion of molecular sieve and sial, avoid sial and even block the phenomenon in duct with occurring between molecular sieve reuniting, and make the duct of sial and molecular sieve mutually through, sial and molecular sieve is made to give full play to synergy, the aging amorphous silicon Alumina gel that contributes to is assembled gradually, even pore-forming, be conducive to the utilization rate with metal that is uniformly distributed of active metal, improve the serviceability of catalyst.。Molecular sieve can adopt various suitable method to process before being introduced according to requirements, and the modification process of molecular sieve can not produce adverse influence to composite carrier.
Detailed description of the invention
The preparation process of hydrogenation catalyst of the present invention is described for infusion process, specific as follows: catalyst carrier material and other components such as adhesive and auxiliary agent through mixing, rolling, the means such as extrusion are shaping, then drying, roasting is carried out, obtain catalyst carrier, then adopt conventional impregnation methods 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 catalyst carrier material is shaping, drying condition is generally at 80 ~ 200 DEG C, and dry 1 ~ 15 hour, sintering temperature was generally 450 ~ 700 DEG C, and roasting time is generally 1 ~ 10 hour.After impregnation of catalyst carriers supported active metals, the drying condition of catalyst is as follows: be generally at 80 ~ 200 DEG C, dry 1 ~ 15 hour, and the roasting condition of catalyst is roasting 1 ~ 8 hour at 350 ~ 550 DEG C.
In the inventive method, described containing molybdenum and/or tungsten, nickel and/or cobalt compound, can be by be selected from the soluble compound of nickeliferous and/or cobalt metal one or more, as their nitrate, acetate, soluble carbonate salt, chloride, one or more solution prepared in soluble complexes; Can be by being selected from containing one or more in the soluble compound of molybdenum and/or tungsten metal, as one or more solution prepared in molybdate, tungstates, ethyl metatungstate, it can be the mixed solution prepared by the nickeliferous and/or soluble compound of cobalt metal and the solubility platform thing of molybdenum and/or tungsten metal; Can also be the aqueous solution prepared by the heteropoly acid of nickeliferous and/or cobalt metal and molybdenum and/or tungsten metal or salt.According to method provided by the invention, not limiting the solvent in solution, can be organic solvent, as alcohol, ether and acid, can be inorganic solvent, as water and their mixture, and preferred water.
For hydrocracking catalyst, hydrogenation active component is molybdenum and/or tungsten and nickel and/or cobalt, with the weight of catalyst for benchmark, with oxide basis, 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, is easy to operation, is applicable to industrial production.When selecting suitable molecular sieve (modified Y molecular sieve and modified beta molecular sieve), catalyst is used for hydrocracking process, effectively can improve the mass transfer of reaction mass at catalyst, improve the activity of catalyst and the selective of object product, good result of use can be obtained.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 DEG C, general at 300 ~ 550 DEG C, there is the feedstock oil of These characteristics as gas oil, vacuum distillate, de-pitch prill oil, catalytic cracking recycle oil, shale oil, coal tar wet goods.Reaction condition generally under hydrogen existence condition, reaction pressure 5 ~ 30MPa, hydrogen to oil volume ratio 100 ~ 5000, volume space velocity 0.1 ~ 5.0h during liquid
-1, reaction temperature 340 ~ 420 DEG C.Catalyst of the present invention process common VGO time, reaction condition generally under 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, reaction temperature 370 ~ 410 DEG C.
The specific area of product of the present invention and pore volume adopt 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 embodiments.
embodiment 1
200g solid aluminum chloride is joined in 2 liters of distilled water, heat simultaneously and be stirred to dissolving, obtaining liquor alumini chloridi (a).Concentrated ammonia liquor is added appropriate distilled water diluting into about 10% weak aqua ammonia (b), 10g cetylamine is dissolved in 120ml absolute ethyl alcohol, under stirring, add 25g Modified Zeolite Y Y-1 (SiO to the inside
2/ Al
2o
3=11.0, lattice constant is 24.42, and relative crystallinity is 95%) in, form solution (c).Get 10L waterglass (technical grade, modulus is 3.0) to be diluted in 20L deionized water, be configured to solution (d).Get a stainless steel reaction tank, (a) is added and after being heated with stirring to 65 DEG C in tank, open the valve of the container having (b), control, within 10 minutes, system in tank is added drop-wise to pH=4.5, now in tank, add 250ml solution (c), continue to drip (b), control, in 30 minutes, system in tank is added drop-wise to pH=8.0.Keep temperature to be 65 DEG C, pH=8.0, stops after 20 minutes, in system, adds solution (d), and the amount of the waterglass that the part by weight being 45/55 according to silica/alumina in amorphous aluminum silicide calculates added in 10 minutes.Aging 1 hour, filtered by material in tank, washing to without chlorion, is filtered, and by filter cake drying 10 hours at 110 DEG C, pulverizes and sieves and obtains catalyst carrier dry gel powder J-1.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
Get product J-1 carrier dry gel powder 80 grams, the mixing of 20 grams, adhesive, extruded moulding after rolling, dry also 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 and flood 3 hours, then dry at 120 DEG C, after dry 180 minutes, by dried catalyst 500 DEG C of roastings 4 hours, obtain catalyst A, its composition is in table 2.
embodiment 2
200g Solid aluminum sulfate is joined in 2 liters of distilled water, heat simultaneously and be stirred to dissolving, obtaining aluminum sulfate solution (a).Concentrated ammonia liquor is added appropriate distilled water diluting into about 10% weak aqua ammonia (b), 18g octadecylamine is dissolved in 200ml absolute ethyl alcohol, adds 88g Modified Zeolite Y Y-1 (SiO
2/ Al
2o
3=11.0, lattice constant is 24.42, and relative crystallinity is 95%) making beating formation slurries (c).Get 10L waterglass (technical grade, modulus is 3.0) to be diluted in 20L deionized water, be configured to solution (d).Get a stainless steel reaction tank, (a) is added and after being heated with stirring to 65 DEG C in tank, open the valve of the container having (b), control, within 10 minutes, system in tank is added drop-wise to pH=4.5, open the valve of the container having (c), continue to drip (b), control, in 30 minutes, system in tank is added drop-wise to pH=8.0, control the valve of the container of (c), ensure now to be added dropwise to complete.Keep temperature to be 65 DEG C, pH=8.0, stops after 20 minutes, in system, adds solution (d), and the amount of the waterglass that the part by weight being 45/55 according to silica/alumina in amorphous aluminum silicide calculates added in 10 minutes.Aging 1 hour, material in tank is filtered, wash to sulfate radical-free ion, filter, by filter cake at 110 DEG C dry 10 hours, pulverize and sieve and obtain catalyst carrier dry gel powder J-2.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
Get product J-2 carrier dry gel powder 80 grams, the mixing of 20 grams, adhesive, extruded moulding after rolling, dry also 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 and flood 3 hours, then dry at 120 DEG C, after dry 180 minutes, by dried catalyst 500 DEG C of roastings 4 hours, obtain catalyst B, its composition is in table 2.
embodiment 3
200g Solid aluminum sulfate is joined in 2 liters of distilled water, heat simultaneously and be stirred to dissolving, obtaining aluminum sulfate solution (a).Solid sodium metaaluminate being mixed with concentration is 20g Al
2o
3/ l sodium aluminate solution (b), 65g lauryl amine is dissolved in 2.5L absolute ethyl alcohol, adds 645g Modified Zeolite Y Y-1 (SiO wherein
2/ Al
2o
3=11.0, lattice constant is 24.42, and relative crystallinity is 95%) making beating, obtained slurries (c).Get 10L waterglass (technical grade, modulus is 3.0) to be diluted in 20L deionized water, be configured to solution (d).Get a stainless steel reaction tank, insert after 2l deionized water and stirring is heated to 65 DEG C, open the valve having (a), (b) and (c) container simultaneously, the pH=8.0 of the hierarchy of control, controls (a) (c) and (d) to be dripped off in 45 minutes.Keep temperature to be 65 DEG C, pH=8.0, stops after 20 minutes, in system, adds solution (d), and the amount of the waterglass that the part by weight being 45/55 according to silica/alumina in amorphous aluminum silicide calculates added in 10 minutes.Aging 1 hour, material in tank is filtered, wash to sulfate radical-free ion, filter, by filter cake at 110 DEG C dry 10 hours, pulverize and sieve and obtain catalyst carrier dry gel powder J-3.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
Get product J-3 carrier dry gel powder 80 grams, the mixing of 20 grams, adhesive, extruded moulding after rolling, dry also 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 and flood 3 hours, then dry at 120 DEG C, after dry 180 minutes, by dried catalyst 500 DEG C of roastings 4 hours, obtain catalyst C, its composition is in table 2.
embodiment 4
500g solid aluminum chloride is joined in 2 liters of distilled water, heat simultaneously and be stirred to dissolving, obtaining liquor alumini chloridi (a).Concentrated ammonia liquor is added appropriate distilled water diluting to be dissolved in 60ml absolute ethyl alcohol into about 10wt% weak aqua ammonia (b), 10g cetylamine, add the Hydrogen β zeolite (SiO of 26g modification
2/ Al
2o
3=30.0, lattice constant is 12.00, and relative crystallinity is 90%) making beating, form slurries (c).Get 10L waterglass (technical grade, modulus is 3.0) to be diluted in 20L deionized water, be configured to solution (d).Get a stainless steel reaction tank, (a) is added and after being heated with stirring to 65 DEG C in tank, open the valve of the container having (b), control, within 10 minutes, system in tank is added drop-wise to pH=4.0, continue to drip (b), open the valve of the container having (c), control, in 30 minutes, system in tank is added drop-wise to pH=8.0, control the valve of the container of (c), ensure now to be added dropwise to complete.Keep temperature to be 65 DEG C, pH=8.0, stops after 20 minutes, in system, adds solution (d), and the amount of the waterglass that the part by weight being 45/55 according to silica/alumina in amorphous aluminum silicide calculates added in 10 minutes.Aging 1 hour, filtered by material in tank, washing to without chlorion, is filtered, and by filter cake drying 10 hours at 110 DEG C, pulverizes and sieves and obtains catalyst carrier dry gel powder J-4.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
Get product J-4 carrier dry gel powder 80 grams, the mixing of 20 grams, adhesive, extruded moulding after rolling, dry also 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 and flood 3 hours, then dry at 120 DEG C, after dry 180 minutes, by dried catalyst 500 DEG C of roastings 4 hours, obtain catalyst D, its composition is in table 2.
comparative example 1
Repeat the synthesis of embodiment 2, do not add organic amine, obtained comparative catalyst carrier dry gel powder DF-1.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
The process of carrier material DF-1 synthetic catalyst, with embodiment 2, obtains catalyst DA, and its composition is in table 2.
comparative example 2
Repeat the synthesis of embodiment 2, do not add Y zeolite and organic amine, obtained comparative catalyst carrier dry gel powder DF-2.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
The process of carrier material DF-2 synthetic catalyst, with embodiment 2, obtains catalyst DB, and its composition is in table 2.
comparative example 3
Repeat the synthesis of embodiment 4, do not add modified hydrogen beta-zeolite molecular sieve B-1 and organic amine, obtained comparative catalyst carrier dry gel powder DF-3.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
The process of carrier material DF-3 synthetic catalyst, with embodiment 4, obtains catalyst DC, and its composition is in table 2.
comparative example 4
Repeat the synthesis of embodiment 4, do not add organic amine, obtained comparative catalyst carrier dry gel powder DF-4.Roasting 5 hours at 550 DEG C, the Main physical chemical property of gained is in table 1.
The process of carrier material DF-4 synthetic catalyst, with embodiment 4, obtains catalyst DD, and its composition is in table 2.
Table 1 composite carrier main character
| Bearer number | J-1 | J-2 | J-3 | DF-1 | DF-2 | Y-1 |
| Specific area, m 2/g | 390 | 513 | 636 | 410 | 346 | 777 |
| Pore volume, ml/g | 0.73 | 0.58 | 0.45 | 0.49 | 0.82 | 0.36 |
Table 1 continues composite carrier main character
| Bearer number | J-4 | DF-3 | DF-4 | B-1 |
| Specific area, m 2/g | 342 | 352 | 274 | 550 |
| Pore volume, ml/g | 0.75 | 0.78 | 0.64 | 0.40 |
Found out by table 1 Data Comparison, use the inventive method saturated absorption organic amine in advance when amorphous aluminum silicide plastic, obtained molecular sieve-amorphous aluminum silicide carrier dry gel powder with do not add compared with organic amine, specific area and pore volume are greatly improved, and effectively can solve the problem that the amorphous aluminum silicide that causes when plastic even blocks with the reunion between molecular sieve.
The composition of table 2 catalyst and character
| Catalyst is numbered | A | B | C | D | DA | DB | DC | DD |
| WO 3，wt％ | 21.02 | 20.79 | 21.87 | 22.27 | 23.04 | 22.72 | 21.54 | 21.49 |
| NiO，wt％ | 6.58 | 6.69 | 5.82 | 5.13 | 5.03 | 6.67 | 6.12 | 5.32 |
| Face more long-pending than table, m 2/g | 241 | 308 | 373 | 216 | 250 | 212 | 221 | 181 |
| Pore volume, ml/g | 0.45 | 0.37 | 0.30 | 0.47 | 0.32 | 0.49 | 0.48 | 0.41 |
The invention described above catalyst and comparative catalyst thereof are evaluated.Evaluation feedstock oil is Iranian VGO, and character is in 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
-1.Main character is in table 4.
Table 3 raw material oil properties
| Density, d 4 20 | 0.9024 | Mass spectral analysis, wt% | ? |
| Boiling range, DEG C | ? | -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 | BMCI value | 40.3 |
Table 4 evaluation result
| Catalyst is numbered | B | DA |
| Reaction temperature, DEG C | 358 | 360 |
| Conversion ratio, wt% | 63 | 62 |
| Naphtha yield, wt% | 48.58 | 46.55 |
| Heavy naphtha virtue is dived, wt% | 50 | 47 |
As can be seen from evaluation result, the catalyst using the inventive method to prepare has active and product selectivity preferably.
Claims (11)
1. the preparation method of a hydrogenation catalyst, comprise: preparation contains the catalyst carrier material of molecular sieve and amorphous aluminum silicide, adopt infusion process or coprecipitation to introduce hydrogenation active component, obtain final hydrogenation catalyst, wherein the preparation process of carrier material comprises:
(1) mixed with organic amine by molecular sieve, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve; Described organic amine is containing one or more in the fatty amines of 10 ~ 20 carbon numbers;
(2) in amorphous aluminum silicide plastic process, add the mixture that step (1) obtains, with the weight of final carrier material for benchmark, molecular sieve addition is 5wt% ~ 90wt%;
(3) carry out aging after the amorphous aluminum silicide cemented into bundles described in step (2), then after filtration, washing, dry, obtain catalyst carrier material.
2. in accordance with the method for claim 1, it is characterized in that in step (1), described organic amine and molecular sieve mixed method: organic amine is directly added in molecular sieve, or be dissolved in by organic amine in solvent and add in molecular sieve again, solvent is wherein one or more in water, low-carbon alcohols; Described low-carbon alcohols to be carbon number be in the monohydric alcohol of 1 ~ 5 one or more.
3. in accordance with the method for claim 1, after it is characterized in that step (1) molecular sieve mixes with organic amine, after filtration and drying after carry out step (2) again.
4. in accordance with the method for claim 1, it is characterized in that the plastic process of the amorphous aluminum silicide described in step (2) is the neutralization reaction process of acid material and alkaline material, plastic process adopts the mode of the continuous acid-base titration of soda acid, or adopts two kinds of materials and the mode of stream neutralization.
5. in accordance with the method for claim 1, it is characterized in that in step (2), amorphous aluminum silicide plastic process is the neutralization reaction process of acid material and alkaline material, plastic process adopts two kinds of materials and flows plastic mode of operation, or a kind of material is placed on another kind of material in plastic cans and adds the mode of operation of plastic continuously.
6. in accordance with the method for claim 5, it is characterized in that, in step (2), it is Al that plastic material comprises aluminium source
2(SO
4)
3, AlCl
3, Al (NO
3)
3and NaAlO
2in one or more, silicon source is waterglass, in Ludox and organic silicon-containing compound one or more, precipitating reagent is NaOH, NH
4oH, CO
2in one or more.
7. 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.
8. according to the method described in claim 1 or 7, 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 slurries form.
9. in accordance with the method for claim 1, it is characterized in that in step (2), the incorporation way of the mixture of step (1) gained adopts the one or more combination of following manner: this mixture, in plastic neutralization reaction process, adds in plastic cans by (1) continuously; (2) this mixture is first joined in plastic cans, then will prepare in the acid material of amorphous aluminum silicide and alkaline material and plastic; (3) one or more with plastic material of this mixture are mixed, then in plastic material and plastic.
10. in accordance with the method for claim 1, it is characterized in that described hydrogenation active component is one or more in group vib and group VIII metal, hydrogenation active component content in the catalyst with oxide basis for 5% ~ 80%.
11. according to the method described in claim 1 or 10, it is characterized in that described hydrogenation active component is one or more in molybdenum, tungsten, nickel, cobalt.
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| Synthesis of high silica zeolites using a mixed quaternary ammonium cation, amine approach: discovery of zeolite SSZ-47;S.I.Zones;《Chem. Mater.》;acs;20011229;第12卷;第313-320页 * |
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