CN103801362B - Prepare the method for hydrogenating catalyst composition - Google Patents
Prepare the method for hydrogenating catalyst composition Download PDFInfo
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- CN103801362B CN103801362B CN201210450405.6A CN201210450405A CN103801362B CN 103801362 B CN103801362 B CN 103801362B CN 201210450405 A CN201210450405 A CN 201210450405A CN 103801362 B CN103801362 B CN 103801362B
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Abstract
The invention discloses a kind of method preparing hydrogenating catalyst composition.The method comprises: before coprecipitation prepares amorphous aluminum silicide and hydrogenation active metals oxide composite oxides or add the mixture of molecular sieve and organic amine in process, carry out aging after cemented into bundles, then after filtration, washing, drying, again through shaping, drying and roasting, obtain hydrogenating catalyst composition.Molecular sieve and amorphous aluminum silicide can combine by the catalyst prepared by the method, there is good conjugation and decentralization, can avoid occurring reuniting between molecular sieve and amorphous aluminum silicide even clogging, the distribution of effective control hydrogenation component on each acidic components simultaneously, improves the serviceability of catalyst.Hydrogenating catalyst composition prepared by the inventive method is specially adapted to acid requirement relatively high, and Hydrogenation requires relatively low hydrogenation catalyst.
Description
Technical field
The present invention relates to a kind of method preparing hydrogenating catalyst composition, especially for the preparation method of the hydrogenating catalyst composition containing molecular sieve and amorphous aluminum silicide.
Background technology
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 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.
For hydrocracking catalyst, the difference of mating between cracking function and hydrogenating function can produce different reaction effects, that is for different object products, needs the cracking function and the hydrogenating function that regulate catalyst.
Hydrocracking catalyst disclosed in the patents such as CN200810117102.6, CN200710012770.8, CN00109747.4 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 load hydrogenation active metals component to obtain final catalyst.Wherein carrier material is prepared by the method directly adding molecular sieve in amorphous aluminum silicide plastic process, easily there is agglomeration in such 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, active metal distribution is not easy to control, and then the hydrogenating function of catalyst is not mated with cracking function, affect 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 hydrogenating catalyst composition.Molecular sieve and amorphous aluminum silicide can combine by the catalyst prepared by the method, there is good conjugation and decentralization, can avoid occurring reuniting between molecular sieve and amorphous aluminum silicide even clogging, the distribution of effective control hydrogenation component on each acidic components simultaneously, the quantity at adjustment of acidity center and ratio, improve the serviceability of catalyst.
The preparation method of hydrogenating catalyst composition of the present invention, hydrogenation active metals component is selected from least one in group vib metal and group VIII metal, comprising:
(1) mixed with organic amine by molecular sieve, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve, is preferably 7wt% ~ 40wt%;
(2) adopt coprecipitation prepare amorphous aluminum silicide and hydrogenation active metals oxide composite oxides before or add the mixture that step (1) obtains in process, make the weight ratio of amorphous aluminum silicide and molecular sieve be 1:19 ~ 19:1, hydrogenation active metals accounts for 3% ~ 50% of amorphous aluminum silicide weight with the addition of oxide basis;
(3) carry out aging after step (2) coprecipitation reaction terminates, then after filtration, washing, dry, obtain catalyst intermediate;
(4) catalyst intermediate of step (3) gained is through shaping, and dry and roasting, obtains hydrogenating catalyst composition.
In step of the present invention (1), described organic amine is the fatty amine of carbon number more than 10, one or more in aromatic amine.Better suited for containing the amine of chain, be preferably containing one or more in the fatty amines of 10 ~ 20 carbon numbers, such as: decyl amine, lauryl amine, cetylamine, octadecylamine, 1,10-decamethylene diamine, to one or more in butylaniline.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).After molecular sieve being mixed with organic amine in step (1), can after filtration, after filtration and after drying, then step (2) can also be carried out.
In step of the present invention (2), described group VIII metal is one or more in Fe, Co, Ni.Group vib metal is Mo and/or W.
In step of the present invention (2), employing coprecipitation prepares amorphous aluminum silicide and hydrogenation active metals oxide composite oxides can be undertaken by process well known to those skilled in the art.Generally in acid material and alkaline material and plastic process.Plastic process can adopt the mode of the continuous acid-base titration of soda acid, also can adopt two kinds of materials and the mode of stream neutralization.
In step of the present invention (2), coprecipitation adopts aluminium source and hydrogenation active metals source (to be preferably molybdenum source, tungsten source, cobalt source, in nickel source one or more) react carry out plastic with precipitating reagent, aluminum soluble salt wherein used is aluminium chloride, aluminum sulfate, one or more in aluminum nitrate, molybdenum source is molybdenum trioxide, the form of molybdenum trioxide slurries can be adopted to add, tungsten source is sodium tungstate, ammonium metatungstate or wolframic acid, nickel source is nickel nitrate, nickel chloride, one or more in basic nickel carbonate, cobalt source is cobalt nitrate, cobalt chloride, one or more in basic cobaltous carbonate.Precipitating reagent used is generally one or several in sodium carbonate, sodium acid carbonate, NaOH, potassium hydroxide, ammoniacal liquor etc., preferred ammoniacal liquor.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 aluminium salt or precipitating reagent in and plastic etc., silicon source also can to add after the precipitation of aluminium source in material.Also can two or more be combined by aforesaid way.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 (4), 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 hydrogenating catalyst composition, 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 (2), the incorporation way of the mixture of step (1) gained adopts the one or more combination of following manner: this mixture, in coprecipitation reaction process, adds in plastic cans by (1) continuously; (2) this mixture is first joined in plastic cans, then carry out coprecipitation reaction; (3) one or more with coprecipitate material of this mixture are mixed, then carry out coprecipitation reaction.
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, drying condition: general at 50 ~ 150 DEG C dry 1 ~ 15 hour.
In step (4) catalyst intermediate forming process, shaping assistant can be added as required as one or more in adhesive, peptization acid, extrusion aid etc.
In step (4), after catalyst intermediate 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.
Hydrogenating catalyst composition prepared by the inventive method also can add other auxiliary agent, as required as one or more in phosphorus, boron, titanium, zirconium etc.The mode introduced in hydrogenating catalyst composition can adopt conventional method, such as can introduce in step (2) plastic process, can introduce, infusion process also can be adopted to introduce in step (5) forming process.
Hydrogenating catalyst composition prepared by the inventive method, with the weight of hydrogenating catalyst composition for benchmark, hydrogenation active metals content take oxide basis as 3wt% ~ 40wt%.In catalyst of the present invention, the weight ratio of group vib metal and group VIII metal is 2 ~ 8:1.
In the preparation process of hydrogenating catalyst composition 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 directly plastic in duct, organic amine has the guide effect to amorphous aluminum silicide duct in amorphous aluminum silicide plastic process simultaneously, make to there is hydrophilic amorphous aluminum silicide in molecular sieve surface arrangement in order, be deposited on the surface of molecular sieve equably, and enhance the adhesion of molecular sieve and amorphous aluminum silicide, avoid amorphous aluminum silicide and even block the phenomenon in duct with occurring between molecular sieve reuniting, and make the duct of amorphous aluminum silicide and molecular sieve mutually through, amorphous aluminum silicide and molecular sieve is made to give full play to synergy, improve the serviceability of catalyst.Hydrogenating catalyst composition prepared by the inventive method, part or all of hydrogenation active metals component deposition is on amorphous aluminum silicide, the acid centre of hydrogenation active metals and molecular sieve is fully isolated, regulate hydrogenating function and acid function, control reactant and carry out deep pyrolytic, amorphous aluminum silicide growth surrounds molecular sieve in the outside of molecular sieve on the other hand, for product provides unobstructed diffusion admittance, making product can be diffused into reaction center outside timely, providing good reaction environment for reaching desirable object product.Hydrogenating catalyst composition prepared by the inventive method is specially adapted to acid requirement relatively high, and Hydrogenation requires relatively low hydrogenation catalyst, is applicable to drastic cracking, in the hydrocracking process of either shallow hydrogenation, and such as light oil type hydrogen cracking etc.
Detailed description of the invention
Hydrogenating catalyst composition obtained by the inventive method can directly use as hydrogenation catalyst, also can supplement part hydrogenation active metals component as required, to meet the needs of differential responses.Amount according to the performance of catalyst and supplementary hydrogenation active metals component selects suitable method, such as can to adopt in infusion process, physical mixed method, coprecipitation method one or more, preferably adopt infusion process.Supplement after dip loading hydrogenation active metals, after drying and roasting, obtain hydrogenating catalyst composition.Wherein drying condition is as follows: be generally at 80 ~ 200 DEG C, dry 1 ~ 15 hour, and roasting condition is roasting 1 ~ 8 hour at 350 ~ 550 DEG C.
In the inventive method, preparation adopts conventional method preparation containing the maceration extract of hydrogenation active metals, such as nickel source, cobalt source are selected from one or more in nitrate, acetate, chloride, soluble complexes, molybdenum source is selected from one or more in molybdate, molybdenum trioxide, tungsten source is selected from one or more in tungstates, ethyl metatungstate, also can adopt solution prepared by heteropoly acid or its salt containing hydrogenation active metals component.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.
Catalyst preparation process of the present invention is simple, convenient, is easy to operation, is applicable to industrial production.
The inventive method is particularly useful for preparing hydrocracking catalyst, select suitable molecular sieve (Y molecular sieve and/or beta-molecular sieve), the cracking function of adjustment catalyst and hydrogenating function, improve the activity of catalyst and the selective of object product, can obtain good result of use.This hydrocracking catalyst 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, deasphalted 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.
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
By 291g solid aluminum chloride, 15g sodium tungstate, 14g nickel nitrate joins in 2 liters of distilled water, heats simultaneously and is stirred to dissolving, obtaining solution (a).Concentrated ammonia liquor is added appropriate distilled water diluting and be dissolved in 120ml absolute ethyl alcohol into about 10wt% weak aqua ammonia (b), 9.6g cetylamine, under stirring, add 24.7gY type molecular sieve 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 plastic cans, (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 50/50 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 intermediate J-1.
Get catalyst intermediate J-1100 gram, form paste, extruded moulding with the peptization liquid comes into contact containing nitric acid, 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
By 268g Solid aluminum sulfate, 180g sodium tungstate, 160g nickel nitrate joins in 2 liters of distilled water, heats simultaneously and is stirred to dissolving, obtaining solution (a).Concentrated ammonia liquor is added appropriate distilled water diluting to be dissolved in 200ml absolute ethyl alcohol into about 10wt% weak aqua ammonia (b), 42.3g octadecylamine, add 211.6gY type molecular sieve 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 plastic cans, (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 50/50 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 intermediate J-2.
Get catalyst intermediate J-2100 gram, form paste, extruded moulding with the peptization liquid comes into contact containing nitric acid, 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
By 187g Solid aluminum sulfate, 327g sodium tungstate, 288.3g nickel nitrate joins in 5 liters of distilled water, heats simultaneously and is stirred to dissolving, obtaining solution (a).Solid sodium metaaluminate being mixed with concentration is 20gAl
2o
3/ l sodium aluminate solution (b), 158g lauryl amine is dissolved in 2.5L absolute ethyl alcohol, adds 1580gY type molecular sieve 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 plastic cans, 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 50/50 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 intermediate J-3.
Get catalyst intermediate J-3100 gram, form paste, extruded moulding with the peptization liquid comes into contact containing nitric acid, 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
By 4246g solid aluminum chloride, 2481g sodium tungstate, 2187g nickel nitrate joins in 80 liters of distilled water, heats simultaneously and is stirred to dissolving, obtaining solution (a).Concentrated ammonia liquor is added appropriate distilled water diluting to be dissolved in 600ml absolute ethyl alcohol into about 10wt% weak aqua ammonia (b), 66.7g cetylamine, add 171g Hydrogen β zeolite (SiO
2/ Al
2o
3=30.0, lattice constant is 12.00, and relative crystallinity is 90%) making beating, form slurries (c).Get 1000L waterglass (technical grade, modulus is 3.0) to be diluted in 2000L deionized water, be configured to solution (d).Get a plastic cans, (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 50/50 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 intermediate J-4.
Get catalyst intermediate J-4100 gram, form paste, extruded moulding with the peptization liquid comes into contact containing nitric acid, 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's intermediate DF-1.
The process of catalyst intermediate 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 4, do not add organic amine, obtained comparative catalyst's intermediate DF-2.
The process of catalyst intermediate 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 2, in coprecipitation process, do not add active metal component, obtained comparative composite DF-3.Get product DF-3 carrier material 100 grams, paste is formed with the peptization liquid comes into contact containing nitric acid, extruded moulding, after drying roasting, the same maceration extract containing W-Ni metal component contacts 3 hours, then at 120 DEG C after dry 180 minutes, by dried catalyst 500 DEG C of roastings 4 hours, obtain catalyst 3DC, its composition is in table 2.
Table 1 raw molecule sieve main character
| Y-1 | B-1 | |
| Specific area, m 2/g | 786 | 553 |
| Pore volume, ml/g | 0.37 | 0.40 |
The composition of table 2 catalyst and character
| Catalyst is numbered | A | B | C | D | DA | DB | DC |
| WO 3，wt％ | 3.78 | 21.93 | 9.08 | 28.74 | 21.8 | 29.6 | 21.2 |
| NiO，wt％ | 1.22 | 7.07 | 2.92 | 9.26 | 5.6 | 9.6 | 7.3 |
| Specific area, m 2/g | 348 | 393 | 550 | 187 | 345 | 182 | 296 |
| Pore volume, ml/g | 0.69 | 0.36 | 0.34 | 0.40 | 0.31 | 0.40 | 0.31 |
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 1.5h 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 | DC |
| Reaction temperature, DEG C | 358 | 360 | 358 |
| Conversion ratio, wt% | 63 | 62 | 63 |
| Naphtha yield, wt% | 49.05 | 46.55 | 48.58 |
| Heavy naphtha virtue is dived, wt% | 52 | 47 | 50 |
As can be seen from evaluation result, the catalyst using the inventive method to prepare has active and product selectivity preferably.
Claims (13)
1. a preparation method for hydrogenating catalyst composition, hydrogenation active metals component is selected from least one in group vib metal and group VIII metal, comprising:
(1) mixed with organic amine by molecular sieve, wherein the addition of organic amine accounts for the 1wt% ~ 40wt% of molecular sieve, and described organic amine is containing one or more in the fatty amines of 10 ~ 20 carbon numbers;
(2) adopt coprecipitation prepare amorphous aluminum silicide and hydrogenation active metals oxide composite oxides before or add the mixture that step (1) obtains in process, make the weight ratio of amorphous aluminum silicide and molecular sieve be 1:19 ~ 19:1, hydrogenation active metals accounts for 3% ~ 50% of amorphous aluminum silicide weight with the addition of oxide basis;
(3) carry out aging after step (2) coprecipitation reaction terminates, then after filtration, washing, dry, obtain catalyst intermediate;
(4) catalyst intermediate of step (3) gained is through shaping, and dry and roasting, obtains hydrogenating catalyst composition.
2. in accordance with the method for claim 1, it is characterized in that described group VIII metal is one or more in Fe, Co, Ni, group vib metal is Mo and/or W.
3. in accordance with the method for claim 1, it is characterized in that described hydrogenation active metals is group vib metal and group VIII metal, wherein the weight ratio of group vib metal and group VIII metal is 2 ~ 8:1.
4. in accordance with the method for claim 1, it is characterized in that, in step (1), the addition of organic amine accounts for the 7wt% ~ 40wt% of molecular sieve.
5. in accordance with the method for claim 1, it is characterized in that in step (1), described organic amine is containing one or more in the fatty amines of 16 ~ 20 carbon numbers.
6. 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.
7. in accordance with the method for claim 1, after it is characterized in that step (1) molecular sieve mixes with organic amine, after filtration or after filtration and after drying, then carry out step (2).
8. 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.
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 coprecipitation reaction process, adds in plastic cans by (1) continuously; (2) this mixture is first joined in plastic cans, then carry out coprecipitation reaction; (3) one or more with coprecipitate material of this mixture are mixed, then carry out coprecipitation reaction.
10. in accordance with the method for claim 1, it is characterized in that in step (4), after catalyst intermediate is shaping, drying condition is at 80 ~ 200 DEG C, and dry 1 ~ 15 hour, sintering temperature was 450 ~ 700 DEG C, and roasting time is 1 ~ 10 hour.
11. in accordance with the method for claim 1, it is characterized in that the hydrogenation catalyst of gained supplements part hydrogenation active metals component as required.
12. in accordance with the method for claim 11, it is characterized in that: adopt infusion process to supplement load hydrogenation active metals component, again after drying and roasting, obtain hydrogenation catalyst, wherein drying condition is as follows: at 80 ~ 200 DEG C, dry 1 ~ 15 hour, roasting condition was roasting 1 ~ 8 hour at 350 ~ 550 DEG C.
13. according to the method described in claim 1 or 11, it is characterized in that described hydrogenation catalyst, and with the weight of hydrogenation catalyst for benchmark, hydrogenation active metals content take oxide basis as 3wt% ~ 40wt%.
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| CN101167451A (en) * | 2007-09-17 | 2008-04-30 | 苏州科技学院 | Zeolite base composite antibiotic material and its preparation method |
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