CN106140319A - A kind of preparation method of middle oil type hydrocracking catalyst carrier - Google Patents
A kind of preparation method of middle oil type hydrocracking catalyst carrier Download PDFInfo
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Abstract
The invention discloses the preparation method of a kind of middle oil type hydrocracking catalyst carrier.The method includes: beta-molecular sieve, Y molecular sieve, amorphous silica-alumina and binding agent is mixed, molding, drying and roasting, makes carrier；Wherein beta-molecular sieve is to use specific acid-base precipitation method to prepare amorphous silica-alumina predecessor, is subsequently adding water, silicon source and template, obtains silica-alumina gel；Through two step dynamic crystallizations, then process through ammonium salt exchange and Template removal, prepare beta-molecular sieve.Beta-molecular sieve prepared by the inventive method has the feature of high-crystallinity, high silica alumina ratio, good stability, acidic components as carrier of hydrocracking catalyst, hydrocracking catalyst prepared therefrom is active good, and middle distillates oil selectivity is high, the advantage of good product quality.
Description
Technical field
The present invention relates to the preparation method of a kind of carrier of hydrocracking catalyst, be predominant cracking component especially with beta-molecular sieve and Y type molecular sieve, it is adaptable to preparation produces the hydrocracking catalyst of high-quality intermediate oil.
Background technology
The problems such as the market demand it have been not suitable with for being faced with petroleum resources shortage, environmental requirement increasingly stringent and oil product structure at present, the application of hydrocracking technology improves petroleum product-quality, reduction environmental pollution, the effective technology measure of increase market adaptability to changes by becoming, it has also become the of paramount importance process unit in modernization refinery.The problem that the strictest automotive fuel discharge standard makes processing inferior heavy oil be directly produced high-quality cleaning fuel becomes increasingly conspicuous, and hydrocracking technology and the supporting middle oil type catalyst development thereof of maximum production intermediate oil are the most active.
Hydrocracking technology core is hydrocracking catalyst, and the progress of its technology depends on the raising of levels of catalysts, and molecular sieve, as the main acidic components of hydrocracking catalyst, plays conclusive effect to activity, selectivity and the product quality of catalyst.The most industrialized molecular sieve type hydrocracking catalyst is generally based on Modified Zeolite Y at present, hydrocracking catalyst containing Y type molecular sieve is active good, open-loop performance is high, to the heavy constituent selective splitting performance advantages of higher rich in cyclic hydrocarbon, but it is the highest to there is intermediate oil yield, the weak points such as diesel product low temperature flow difference, especially in diesel oil deep drawing or time back-end crop oil does not produces wide cut diesel fuel, this problem is more prominent.Relative to Y type molecular sieve, beta-molecular sieve has three-dimensional twelve-ring pore structure, but not supercage structure as Y type molecular sieve, it is mainly characterized by double 6 ring unit bug hole structures of two 4 rings and four 5 rings, main channel diameter is at 0.56-0.75nm, the duct feature of beta-molecular sieve makes it in cracking reaction, the fracture of chain hydrocarbon-selective be had well effect, and there is the strongest isomery performance, can be used for Low Freezing Point middle oil fraction as cracking component, be industrially widely used.
US4847055 discloses the method for the synthesis beta-molecular sieve of a kind of improvement, wherein uses a kind of special silicon source, with TEABr as template, prepares beta-molecular sieve under conditions of crystal seed exists.This silicon source is to be added precipitant under certain condition by soluble silicon solution to prepare.The large usage quantity of the method template, and easily produce modenite and ZSM-5 stray crystal.Only as (TEA)2O/SiO2> 0.14, i.e. TEA+/SiO2> 0.28 time, the growing amount of stray crystal could be reduced.
Above-mentioned water heat transfer β zeolite needs a large amount of expensive organic formwork agent tetraethyl ammonium hydroxide, the cost major part of beta-molecular sieve synthesis to come from template, typically constitute from about 70%.Reduce template consumption, thus reduce β zeolite synthesis cost, always the focus of this area research.
Furthermore, the organic formwork agent being blocked in zeolite cavity removing must be fallen just can make it have before beta-molecular sieve uses as catalyst catalysis activity.The method of conventional removing organic formwork agent is high-temperature roasting, and owing to high-temperature roasting will destroy the structure of beta-molecular sieve so that it is degree of crystallinity declines, heat stability and hydrothermal stability are deteriorated, and consumption of template agent is the biggest, and this destructiveness is the most serious.And using the beta-molecular sieve adding a small amount of template synthesizing high-silicon aluminum ratio, the degree of crystallinity of products obtained therefrom can be the lowest, and heat stability and hydrothermal stability are poor.
CN1351959A relates to the synthetic method of a kind of molecular sieve.First Al is pressed2O3: (30-150) SiO2: (5-20) (TEA)2O:(1-8.5) Na2O:(650-1200) H2The mol ratio of O prepares Alusil A, by Al2O3: (20-80) SiO2: (5-15) Na2O:(350-1000) H2The mol ratio of O prepares Alusil B, then Alusil A and Alusil B is pressed the weight ratio mixing of 1:10, proceed to after stirring in autoclave pressure, after sealing at a temperature of 100-200 DEG C, stir crystallization 15-150 hour under static or 10-150rpm rotating speed, end product through sucking filtration, wash and be dried to obtain beta-molecular sieve.Although the consumption of organic formwork can be reduced to TEAOH/SiO by this synthetic method2=0.05, but beta-molecular sieve silica alumina ratio prepared by the method is relatively low, and also the characteristic peak of beta-molecular sieve has a small amount of miscellaneous peak, has stray crystal to generate.
CN 1198404A proposes a kind of method synthesizing beta-molecular sieve, uses the composite mould plate agent formed in the basic conditions by halogenide, tetraethyl ammonium hydroxide and the fluoride of tetraethyl ammonium, makes silicon source, aluminum source and crystal seed reaction crystallization produce beta-molecular sieve.Although the method reduces template consumption, adding the productivity of beta-molecular sieve, however it is necessary that addition composite mould plate agent and crystal seed, and after silica alumina ratio is more than 30, degree of crystallinity is relatively low, heat stability and hydrothermal stability are poor.
CN101578353A describes a kind of method utilizing beta-molecular sieve to be optionally hydrocracked.Beta-molecular sieve does not carry out the mol ratio of hydrothermal treatment consists or hydrothermal treatment consists, silicon dioxide and aluminium oxide at relatively low temperatures less than 30:1 and the SF of at least 28wt%6Adsorbance, the catalyst that this beta-molecular sieve obtained by modification is prepared as cracking component, the selectivity of intermediate oil is the highest.
Summary of the invention
For weak point of the prior art, the invention provides the preparation method of the good carrier of hydrocracking catalyst of a kind of catalytic performance.This carrier of hydrocracking catalyst uses a kind of high silica alumina ratio, high-crystallinity, bigger serface, the beta-molecular sieve of good stability and Y molecular sieve jointly to do as acidic components, hydrocracking catalyst prepared by carrier of the present invention has higher activity and middle distillates oil selectivity, and product is of fine quality.
The preparation method of carrier of hydrocracking catalyst of the present invention, including: beta-molecular sieve, Y molecular sieve, amorphous silica-alumina and binding agent are mixed, molding, drying and roasting, make carrier；On the basis of the weight of carrier, carrier composition includes: the content of beta-molecular sieve is 2～20wt%, and the content of Y molecular sieve is 10～30wt%, and the content of amorphous silica-alumina is 20～60wt%, and the content of binding agent is 15～40 wt%；Wherein said beta-molecular sieve, including following preparation process:
(1), using acid-base precipitation method to prepare amorphous silica-alumina predecessor, described amorphous silica-alumina predecessor is on the basis of the gross weight of silicon dioxide and aluminium oxide, and the content that silicon is counted with silicon dioxide is as 40wt%～75wt%, preferably 55wt%～70wt%；Its preparation process includes acid-base neutralization plastic, aging, wherein silicon introduce reaction system method be in aluminum contained compound and plastic before and/or plastic during introducing portion silicon-containing compound, remainder silicon-containing compound be in aluminum contained compound and plastic after and introduce before ageing；
(2), by Al2O3: SiO2: Na2O:H2O=1:(62 ~ 130): (0.5～3.0): (100～500), TEAOH/SiO2It is total molar ratio of 0.010 ~ 0.095, preferably SiO2/Al2O3Be 70 ~ 110, TEAOH/SiO2=0.020 ~ 0.080, under conditions of 0～40 DEG C of quick stirring, in the amorphous silica-alumina predecessor of step (1) gained, add water, silicon source and template, and control ph is 9.5 ~ 12.0, stirs, obtaining silica-alumina gel, TEA is the quaternary amine alkali cation in template；
(3), the silica-alumina gel of step (2) gained through two step dynamic crystallizations, then through filtering, washing, prepare Na beta molecular sieve；
(4), described Na beta molecular sieve carries out ammonium salt exchange and Template removal processes, and prepares beta-molecular sieve.
Preferably, the preparation method of the amorphous silica-alumina predecessor of step (1) uses conventional acid-base precipitation method, including acid-base neutralization plastic, aging, and wherein acid-base neutralization plastic process is acid material and the neutralization course of reaction of alkaline material.
Preferably, neutralization plastic process in the way of using acid material or the continuous acid-base titration of alkaline material, or can use acid material and alkaline material and flow the mode of neutralization.
Preferably, described in aluminum contained compound with precipitant and before plastic and/or during plastic the mode of introducing portion silicon-containing compound be: part silicon-containing compound carries out premixing with described aluminum contained compound and/or precipitant, silicon-containing compound and can also be individually added in reaction system during plastic in aluminum contained compound, it is also possible to be the combination of said method.
When carrying out premixing, first can mix with acid material or alkaline material according to the character of different silicon-containing compounds, then (when such as using sodium silicate containing silicon materials, sodium silicate can mix with alkaline material to carry out acid-base neutralization plastic；When using Ludox containing silicon materials, add in acid aluminiferous material).
The mode that silicon-containing compound is individually added in aluminum contained compound and during plastic reaction system is: described aluminum contained compound and precipitant first mix, then it is individually added into silicon-containing compound, or described part silicon-containing compound, described aluminum contained compound and precipitant are separately added in reactor simultaneously；Or described part silicon-containing compound and aluminum contained compound are added separately in described precipitant simultaneously；Or described part silicon-containing compound and precipitant are added separately in described aluminum contained compound simultaneously.The mode being individually added into reaction system is not affected by the character containing silicon materials, and silicon-containing compound can be directly added into.
Preferably, in step (1), the silicon-containing compound and after plastic and introduced before ageing in described aluminum contained compound accounts for the 5wt% ~ 85wt% in terms of silicon dioxide of the silicon in amorphous silica-alumina predecessor, preferably 30wt% ~ 70wt% in terms of silicon dioxide.
Preferably, described aluminum contained compound is selected from Al2(SO4)3、AlCl3、Al(NO3)3One or more in solution, the concentration of described aluminum contained compound solution is 30～150g A12O3/L；One or more in sodium hydroxide solution, ammonia, sodium carbonate liquor, sodium bicarbonate solution, sodium aluminate solution of precipitant.
Preferably, described aluminum contained compound is sodium aluminate solution, and the concentration of described sodium aluminate solution is 40～100 g A12O3/ L, described acidic precipitation agent is nitric acid.
Described silicon-containing compound can be one or more in waterglass, Ludox and organo-silicon compound etc., and described organo-silicon compound are preferably one or more in silanol, silicon ether and siloxanes, with SiO2Quality meter, the concentration of described silicon-containing compound is 40～200 g SiO2/L。
In step (2), described silicon source uses silicon source for conventional during preparing beta molecular sieve, and described silicon source is one or more in White Carbon black, silica gel, Ludox, waterglass.Described template is preferably tetraethyl ammonium hydroxide.
In described step (1), the condition of described plastic is: temperature is 20～85 DEG C, and pH value is 7.0～10.0, is preferably, and temperature is 40～80 DEG C, and pH value is 7.5～9.0；
Described aging condition is: temperature is 20～85 DEG C, and pH is 7.0～10.0, time 0.2～8.0 hours, is preferably, and temperature is 40～80 DEG C, and pH is 7.0～9.5, and the time is 0.5～5.0 hour.
In step (2), generating the reaction temperature 0 of described silica-alumina gel～40 DEG C, pH value is 9.5～12.0, is preferably, and the reaction temperature generating described silica-alumina gel is 10～30 DEG C, and pH value is 10～11.
In described step (3), the silica-alumina gel of step (2) gained includes through the concrete steps of two step dynamic crystallizations: the condition of first step dynamic crystallization is: carry out crystallization under agitation, and temperature is 50～90 DEG C, and the time is 0.5～18 hour；The condition of second step dynamic crystallization is: carry out crystallization under agitation, and temperature is 100～200 DEG C, and the time is 40～120 hours.
In described step (3), the condition of described first step dynamic crystallization is: carry out crystallization under agitation, and temperature is 60～80 DEG C, and the time is 1～10 hour；The condition of described second step dynamic crystallization is: carry out crystallization under agitation, and temperature is 120～170 DEG C, and the time is 50～100 hours.
In described step (3), in the silica-alumina gel of step (2) gained through two step dynamic crystallizations, then through filtering, after washing, through being dried or moist can obtain Na beta molecular sieve.
Preferably, in step (4), ammonium salt exchange uses conventional method to carry out, as one or many ammonium salt exchanges, and Na in the beta-molecular sieve after ammonium salt exchange2O weight content is less than 0.3%；Can be through washing and the step being dried after ammonium salt exchange, the condition being wherein dried is as follows: be dried 3～6 hours at 80 DEG C ~ 150 DEG C.
Preferably, in step (4), described Template removal processes and uses aerobic high-temperature process, and treatment temperature is 400～800 DEG C, and the process time is 5～20 hours, is preferably, and treatment temperature is 500～700 DEG C, and the process time is 10～15 hours.
In carrier of hydrocracking catalyst of the present invention, the character of beta-molecular sieve used is as follows: SiO2/Al2O3Mol ratio is 60～120, and specific surface area is 505～850m2/ g, pore volume is 0.35～0.60mL/g, and relative crystallinity is 100%～135%；This beta-molecular sieve relative crystallinity after water vapour hydrothermal treatment consists is more than 95%.
Beta-molecular sieve preferred property used is, SiO2/Al2O3Mol ratio is 65～100, and specific surface area is 550～800m2/ g, pore volume is 0.40～0.60mL/g, and relative crystallinity is 110%～130%, and this beta-molecular sieve relative crystallinity after water vapour hydrothermal treatment consists is 95%～125%.
Beta-molecular sieve character used is more preferably: SiO2/Al2O3Mol ratio is 65～100, and specific surface area is 600～750 m2/ g, pore volume 0.45～0.55mL/g, relative crystallinity is 115%～130%；This beta-molecular sieve relative crystallinity after water vapour hydrothermal treatment consists is 110%～125%.
In the present invention, this beta-molecular sieve was as follows through the condition of water vapour hydrothermal treatment consists: through 750 DEG C of water vapour hydrothermal treatment consists 2 hours.
In the preparation method of carrier of hydrocracking catalyst of the present invention, it is 0.3～0.5 mL/g that adhesive therefor is preferably the pore volume of the little porous aluminum oxide used by little porous aluminum oxide, and specific surface area is 200～400m2/g。
In catalyst carrier of the present invention, amorphous silica-alumina used can be prepared by coprecipitation or grafting copolymerization process, prepares by conventional method in document.SiO in described amorphous silica-alumina2Weight content be 20%～60%, preferably 25%～40%, the pore volume of amorphous silica-alumina is 0.6～1.1mL/g, preferably 0.8～1.0 mL/g, and specific surface area is 300～500 m2/ g, preferably 350～500 m2/g。
Y molecular sieve of the present invention, its character is as follows: specific surface area 700～1000 m2/ g, total pore volume 0.45～0.90 mL/g, relative crystallinity 95%～130%, SiO2/Al2O3Mol ratio 30～100, cell parameter 2.426～2.433nm, meleic acid amount 0.1～0.4mmol/g.This Y molecular sieve can use prior art to prepare.
Catalyst carrier of the present invention can be shaped according to actual needs, and shape can be cylindrical bars, Herba Trifolii Pratentis etc..In catalyst carrier forming process, it is also possible to adding shaping assistant, such as peptization acid, extrusion aid etc., peptizer typically can use mineral acid and/or organic acid, extrusion aid such as sesbania powder.Catalyst carrier of the present invention used conventional method to be dried and roasting, specific as follows: be dried 3～10 hours at a temperature of 80～150 DEG C, 400～800 DEG C of roastings 3～12 hours.
When catalyst carrier of the present invention is used for preparing hydrocracking catalyst, carrying method conventional in prior art can be used, preferably infusion process, can be saturated leaching, excess leaching or complexation leaching, i.e. with the solution impregnated catalyst carrier containing required active component, carrier after dipping, through being dried, after roasting, prepares final hydrocracking catalyst.
Carrier of hydrocracking catalyst character of the present invention is as follows: specific surface area is 400～600 m2/ g, pore volume is 0.50～1.0 mL/g.
Part silicon-containing compound, in the preparation process of beta-molecular sieve, is first added in reaction system before plastic and/or during plastic by the present invention, forms stable colloidal state and sial integrated structure.Owing to this colloid surface has a lot of hydroxyl structures, can be combined with the remainder silicon-containing compound added below well, so that amorphous silica-alumina predecessor has more stable structure.Afterwards, amorphous silica-alumina predecessor, template are mixed and made into silica-alumina gel with another part silicon source etc., so can form more nucleus in synthetic system, it is evenly dispersed in synthetic system, there is good crystallization guide effect, again through two step dynamic crystallizations, easily form complete framing structure, the beta-molecular sieve that degree of crystallinity is high.The inventive method not only can reduce the usage amount of organic formwork agent, it is also possible to synthesizes the beta-molecular sieve of high-crystallinity, high silica alumina ratio, and has more preferable heat stability and hydrothermal stability, and the beta-molecular sieve purity of the present invention is high, does not has stray crystal.And, the beta-molecular sieve of the present invention is through the exchange of simple ammonium salt and Template removal by Na beta molecular sieve, just can obtain, it is not necessary to carry out the dual-spectrum process such as dealuminzation or dealumination complement silicon again.
Beta-molecular sieve of the present invention and Y molecular sieve are collectively as cracking center, both its respective performance characteristics had been given full play to, the concerted catalysis effect that two kinds of molecular sieves produce can be made again, i.e. beta molecular sieve has good isomerization to the long side chain on alkane or aromatic hydrocarbons, can effectively reduce the condensation point of product, Y type molecular sieve has the highest selectivity of ring-opening to aromatic hydrocarbons simultaneously, improves the product property of purpose product.The active height of hydrocracking catalyst prepared by carrier of the present invention, can high-output qulified midbarrel oil product (boat coal+diesel oil), can hold concurrently simultaneously and produce the hydrogenation tail oil of high-quality.
Detailed description of the invention
In order to the present invention is better described, further illustrate the present invention below in conjunction with embodiment and comparative example.But the scope of the present invention is not limited solely to the scope of these embodiments.The present invention analyzes method: specific surface area, pore volume use low temperature liquid nitrogen physisorphtion, relative crystallinity and cell parameter to use x-ray diffraction method, and silica alumina ratio uses chemical method.In the present invention, wt% is mass fraction.
Embodiment 1
(1) preparation of amorphous silica-alumina predecessor
It is 80g A1 that Solid aluminum sulfate is configured to 100mL concentration2O3/ L aluminum sulfate working solution (a).Strong aqua ammonia is added appropriate distilled water diluting and becomes about 10wt% weak ammonia (b).Take with SiO2The sodium silicate solution of quality meter 28wt%, then to be diluted to 80mL concentration be 150g SiO2/ L sodium silicate working solution (c).Take the steel retort of 5 liters, after retort adding 0.2 liter of distilled water and being heated with stirring to 70 DEG C, open the valve having (a) and (b) and (c) container respectively simultaneously, control the flow of (a) and (c) so that neutralizing the response time at 40 minutes, and the flow adjusting rapidly (b) makes the pH value of system be maintained at 7～8, and control the temperature of system at about 60 DEG C.After reacting aluminum sulfate completes, stopping adding (b), the addition of (c) is 40mL, after the silicon-aluminum sol generated stablizes 20 minutes, continuously add (c) 40mL, add in 10 minutes, start the ageing process of system, keep pH value 8.0, temperature 60 C, aging 30 minutes, obtains amorphous silica-alumina predecessor, amorphous silica-alumina predecessor is on the basis of the wgt dry basis by total of silicon dioxide and aluminium oxide, and the content counted with silicon dioxide is as 60wt%.
(2) preparation of gel
According to Al2O3: SiO2: Na2O:H2O=1:80: 1.6: 240, TEAOH/SiO2Each material is mixed by total molar ratio of=0.075, adding water, sodium silicate solution and tetraethyl ammonium hydroxide in the amorphous silica-alumina predecessor of step (1) gained, and control ph is 11, reaction temperature is 25 DEG C, uniform stirring 30 minutes, obtains silica-alumina gel.
(3) crystallization
Silica-alumina gel obtained by step (2) is poured in stainless steel cauldron, stirs crystallization 5 hours at 80 DEG C, then heat to 150 DEG C, stirring crystallization 30 hours, then filters, and washs and is dried at 120 DEG C to neutrality, obtain Na beta-molecular sieve product N β-1, record relative crystallinity；N β-1, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；N β-1 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete N β-1 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Adding appropriate water purification in Na beta-molecular sieve N β-1, and add a certain amount of ammonium nitrate, making liquid-solid ratio (weight) is 10:1, the concentration of ammonium nitrate is 2mol/L, stirring, is warmed up to 95～100 DEG C, and constant temperature stirs 2 hours, then filter, filter cake secondary again carries out ammonium salt exchange, and the condition of exchange is identical with first time, till finally washing molecule is sieved to pH value neutrality, put in dry zone and be dried, be dried 8 hours at 100～120 DEG C.Taking dried beta-molecular sieve to carry out deviating from template process, use open kiln to process, 570 DEG C of constant temperature process 15 hours, make beta-molecular sieve S β-1, XRD determining S β-1 relative crystallinity；S β-1 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
Embodiment 2
(1) preparation of amorphous silica-alumina predecessor
It is 100g A1 that solid aluminum chloride is configured to 100mL concentration2O3
/ L aluminum chloride working solution (a).Strong aqua ammonia is added appropriate distilled water diluting and becomes about 10wt% weak ammonia (b).Take with SiO2The sodium silicate solution of quality meter 28wt%, then to be diluted to 100mL concentration be 100g SiO2/ L sodium silicate working solution (c).Take the steel retort of 2 liters, after adding 0.3 liter of distilled water in retort and being heated with stirring to 70 DEG C, open the valve having (a) and (b) and (c) container respectively simultaneously, control the flow of (a) and (c) so that neutralizing the response time at 40 minutes, and the flow adjusting rapidly (b) makes the pH value of system be maintained at 7～8, and control the temperature of system at about 60 DEG C.After aluminium reaction completes, stopping adding (b), the addition of (c) is 60mL, after the silicon-aluminum sol generated stablizes 20 minutes, continuously add (c) 40mL, add in 10 minutes, start the ageing process of system, keep pH value 8.0, temperature 60 C, aging 30 minutes, obtains amorphous silica-alumina predecessor, amorphous silica-alumina predecessor is on the basis of the wgt dry basis by total of silicon dioxide and aluminium oxide, and the content counted with silicon dioxide is as 50wt%.
(2) preparation of gel
According to Al2O3: SiO2: Na2O:H2O=1:90: 1.8: 260, TEAOH/SiO2Each material is mixed by total molar ratio of=0.062, adding water, sodium silicate solution and tetraethyl ammonium hydroxide in the amorphous silica-alumina predecessor of step (1) gained, and control ph is 11, reaction temperature is 25 DEG C, uniform stirring 30 minutes, obtains silica-alumina gel.
(3) crystallization
Silica-alumina gel obtained by step (2) is poured in stainless steel cauldron, stirs crystallization 5 hours at 90 DEG C, then heat to 160 DEG C, stirring crystallization 30 hours, then filters, and washs and is dried at 120 DEG C to neutrality, obtain Na beta-molecular sieve product N β-2, record relative crystallinity；N β-2, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；N β-2 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete N β-2 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Adding appropriate water purification in Na beta-molecular sieve N β-2, and add a certain amount of ammonium nitrate, making liquid-solid ratio (weight) is 10:1, the concentration of ammonium nitrate is 2mol/L, stirring, is warmed up to 95～100 DEG C, and constant temperature stirs 2 hours, then filter, filter cake secondary again carries out ammonium salt exchange, and the condition of exchange is identical with first time, till finally washing molecule is sieved to pH value neutrality, put in dry zone and be dried, be dried 8 hours at 100～120 DEG C.Taking dried beta-molecular sieve to carry out deviating from template process, use open kiln to process, 570 DEG C of constant temperature process 15 hours, make beta-molecular sieve S β-2, XRD determining S β-2 relative crystallinity；S β-2 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
Embodiment 3
(1) preparation of amorphous silica-alumina predecessor.
It is 100g A1 that solid aluminum chloride is configured to 120mL concentration2O3 / L aluminum chloride working solution (a).Strong aqua ammonia is added appropriate distilled water diluting and becomes about 10wt% weak ammonia (b).Take with SiO2The sodium silicate solution of quality meter 28wt%, then to be diluted to 100mL concentration be 80g SiO2/ L sodium silicate working solution (c).nullTake the steel retort of one 2 liters，0.3 liter of distilled water is added in retort，Open the valve having (a) container，(a) joined in retort and stir，Then the valve having (c) container is opened，About 30 minutes by 40ml(c) join in retort，After being heated to 70 DEG C，Open the valve having (b) container，Control the flow of (b) so that neutralizing the response time at 40 minutes，When system pH reaches about 7 ~ 8，Close valve，After the silicon-aluminum sol generated stablizes 20 minutes，Continuously add (c) 50ml，Add in 10 minutes，The ageing process of beginning system，Keep pH value 8.5，Temperature 60 C，Aging 30 minutes，Obtain amorphous silica-alumina predecessor，Amorphous silica-alumina predecessor is on the basis of the wgt dry basis by total of silicon dioxide and aluminium oxide，The content counted with silicon dioxide is as 40wt%.
(2) preparation method of gel is the most identical with embodiment 1.Difference is: according to Al2O3: SiO2: Na2O:H2O=1:70: 1.8: 260, TEAOH/SiO2Each material is mixed by total molar ratio of=0.064.
(3) crystallization is with embodiment 1, obtains Na beta-molecular sieve product N β-3, records relative crystallinity；N β-3, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；N β-3 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete N β-3 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Na beta-molecular sieve N β-3, with embodiment 1, is made beta-molecular sieve S β-3, XRD determining S β-3 relative crystallinity by the method for ammonium salt exchange and Template removal；S β-3 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
Embodiment 4
By 7.8 grams of S β-1 molecular sieves, 20 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 80 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, carrier TCAT-1 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CAT-3, carrier and corresponding catalyst character and are shown in Table 3.
Embodiment 5
By 8.9 grams of S β-2 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, carrier TCAT-2 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CAT-2, carrier and corresponding catalyst character and are shown in Table 3.
Embodiment 6
By 8.9 grams of S β-3 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, carrier TCAT-3 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CAT-3, carrier and corresponding catalyst character and are shown in Table 3.
Comparative example 1 (with reference to CN1351959A)
By 20.5g White Carbon black, 2mL sodium aluminate solution, 59g tetraethyl ammonium hydroxide and 0.9g sodium hydroxide, mix under room temperature and mechanical agitation, and continue stirring to raw material mix homogeneously: mixture is proceeded in autoclave pressure, after static state is aged 5 hours at a temperature of 130 DEG C after sealing, takes out and quick cooling pressure still, obtain Alusil A.120g Ludox, 6.3mL sodium metaaluminate, 6g sodium hydroxide and 17mL distilled water are mixed under room temperature and mechanical agitation, and stirs to raw material mix homogeneously, obtain Alusil B.5g Alusil A and 50g Alusil B is mixed under room temperature and mechanical agitation, and stirs and proceed in autoclave pressure to raw material mix homogeneously, after sealing at a temperature of 130 DEG C, to stir crystallization 48 hours under 60rpm rotating speed, take out and quick cooling pressure still.Product, through sucking filtration, washing, washs and is dried at 120 DEG C to neutrality, obtain Na beta-molecular sieve products C N β-1, and characterization result shows, product is the characteristic peak possessing beta-molecular sieve, but has a small amount of miscellaneous peak, i.e. has a small amount of stray crystal.And record the relative crystallinity of CN β-1；CN β-1, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；CN β-1 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete CN β-1 character is shown in Table 1.
Carry out ammonium salt exchange and Template removal according to the method for embodiment 1, Na beta-molecular sieve CN β-1 is made H beta molecular sieve products C S β-1, XRD determining CS β-1 relative crystallinity；CS β-1 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
By 8.9 grams of CS β-1 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, carrier TCCAT-1 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CCAT-1, carrier and corresponding catalyst character and are shown in Table 3.
Comparative example 2(is with reference to CN1198404A)
16g tetraethylammonium bromide and 1.6g sodium fluoride D are dissolved in 30g deionized water, it is sequentially added under stirring and is dissolved in 20g deionized water gained solution, 53.7g Ludox and 0.72g crystal seed by 1.67g sodium aluminate B, continue stirring 60 minutes, proceed in stainless steel cauldron, crystallization 4 days at 160 DEG C.Then filter, wash, be dried to obtain Na beta-molecular sieve products C N β-2, record the relative crystallinity of CN β-2；CN β-2, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；CN β-2 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete CN β-2 character is shown in Table 1.
Carry out ammonium salt exchange and Template removal according to the method for embodiment 1, Na beta-molecular sieve CN β-2 is made H beta molecular sieve products C S β-2, XRD determining CS β-2 relative crystallinity；CS β-2 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
By 8.9 grams of CS β-2 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, support C TCAT-2 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CCAT-2, carrier and corresponding catalyst character and are shown in Table 3.
Comparative example 3
(1) preparation of amorphous silica-alumina predecessor
It is 80g A1 that Solid aluminum sulfate is configured to 100mL concentration2O3/ L aluminum sulfate working solution (a).Strong aqua ammonia is added appropriate distilled water diluting and becomes about 10wt% weak ammonia (b).Take with SiO2The sodium silicate solution of quality meter 28wt%, then to be diluted to 80mL concentration be 150g SiO2/ L sodium silicate working solution (c).Take the steel retort of 5 liters, after retort adding 0.2 liter of distilled water and being heated with stirring to 70 DEG C, open the valve having (a) and (b) and (c) container respectively simultaneously, control the flow of (a) and (c) so that neutralizing the response time at 40 minutes, and the flow adjusting rapidly (b) makes the pH value of system be maintained at 7～8, and control the temperature of system at about 60 DEG C.After having reacted, stopping adding (b), the silicon-aluminum sol of generation stablizes 20 minutes.The ageing process of beginning system, keep pH value 8.0, temperature 60 C, aging 30 minutes, obtain amorphous silica-alumina predecessor, amorphous silica-alumina predecessor is on the basis of the wgt dry basis by total of silicon dioxide and aluminium oxide, and the content counted with silicon dioxide is as 60wt%.
(2) preparation of gel is with embodiment 1.
(3) crystallization is with embodiment 1, records relative crystallinity after obtaining Na beta-molecular sieve products C N β-3；CN β-3, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；CN β-3 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete CN β-3 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Na beta-molecular sieve CN β-3, with embodiment 1, is made H beta molecular sieve CS β-3, XRD determining CS β-3 relative crystallinity by the method for ammonium salt exchange and Template removal；CS β-3 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
By 8.9 grams of CS β-3 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, support C TCAT-3 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CCAT-3, carrier and corresponding catalyst character and are shown in Table 3.
Comparative example 4
(1) preparation of amorphous silica-alumina predecessor
It is 80g A1 that Solid aluminum sulfate is configured to 100mL concentration2O3 / L aluminum sulfate working solution (a).Strong aqua ammonia is added appropriate distilled water diluting and becomes about 10wt% weak ammonia (b).Take with SiO2The sodium silicate solution of quality meter 28wt%, then to be diluted to 80mL concentration be 150g SiO2/ L sodium silicate working solution (c).Take the steel retort of one 5 liters, after tank adding 0.2 liter of distilled water and being heated with stirring to 70 DEG C, open the valve having (a) and (b) container respectively simultaneously, control the flow of (a) so that neutralizing the response time at 40 minutes, and the flow adjusting rapidly (b) makes the pH value of system be maintained at 7～8, and control the temperature of system at about 60 DEG C.After reacting aluminum sulfate completes, stop adding (b), after stablizing 20 minutes, add (c) 80mL, add in 10 minutes, the ageing process of beginning system, keep pH value 8.0, temperature 60 C, aging 30 minutes, obtaining amorphous silica-alumina predecessor, amorphous silica-alumina predecessor is on the basis of the wgt dry basis by total of silicon dioxide and aluminium oxide, and the content counted with silicon dioxide is as 60wt%.
(2) preparation of gel is with embodiment 1.
(3) crystallization is with embodiment 1, records relative crystallinity after obtaining Na beta-molecular sieve products C N β-4；CN β-4, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；CN β-4 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete CN β-4 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Na beta-molecular sieve CN β-4, with embodiment 1, is made H beta molecular sieve CS β-4, XRD determining CS β-4 relative crystallinity by the method for ammonium salt exchange and Template removal；CS β-4 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
By 8.9 grams of CS β-4 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, support C TCAT-4 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CCAT-4, carrier and corresponding catalyst character and are shown in Table 3.
Comparative example 5
(1) preparation of amorphous silica-alumina predecessor is with embodiment 1；
(2) preparation of gel is the most same as in Example 1, and difference is: amorphous silica-alumina predecessor, sodium silicate, tetraethyl ammonium hydroxide and water are according to Al2O3: SiO2: Na2O:H2O=1:80: 1.6: 240, TEAOH/SiO2Total molar ratio of=0.2.
(3) crystallization is with embodiment 1, final prepared Na beta-molecular sieve CN β-5, records relative crystallinity；CN β-5, after roasting in 550 DEG C of air 3 hours, records the relative crystallinity after roasting；CN β-5 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, and concrete CN β-5 character is shown in Table 1.
(4) ammonium salt exchange and Template removal
Na beta-molecular sieve CN β-5, with embodiment 1, is made H beta molecular sieve CS β-5, XRD determining CS β-5 relative crystallinity by the method for ammonium salt exchange and Template removal；CS β-5 is after 750 DEG C of water vapour hydrothermal treatment consists 2 hours, then records the relative crystallinity after hydrothermal treatment consists, the results are shown in Table 2.
By 8.9 grams of CS β-5 molecular sieves, 25.6 grams of Y molecular sieve (specific surface areas 740m2/ g, total pore volume 0.75mL/g, relative crystallinity 101%, SiO2/Al2O3Mol ratio 48, cell parameter 2.430nm, meleic acid amount 0.2mmol/g), 90 grams of amorphous silica-aluminas (pore volume 0.9mL/g, specific surface areas 350m2/ g, silicon oxide weight content 30%), 75 grams of little porous aluminum oxides, mixed grind in chaser is put into dust technology (nitric acid is 0.25 with the mol ratio of little porous aluminum oxide), add water, being rolled into paste, extrusion, extrusion bar is dried 4 hours at 110 DEG C, then 550 DEG C of roastings 4 hours, support C TCAT-5 is obtained.
The impregnation liquid room temperature immersion of carrier tungstenic and nickel 2 hours, 120 DEG C are dried 4 hours, and 500 DEG C of roastings of temperature programming 4 hours obtain catalyst CCAT-5, carrier and corresponding catalyst character and are shown in Table 3.
Table 1
| Feed intake SiO2/Al2O3Mol ratio | Specific surface area, m2/g | Pore volume, mL/g | SiO2/Al2O3Mol ratio | Relative crystallinity, % | The reservation degree of crystallization relatively after hydrothermal treatment consists, % | |
| Nβ-1 | 80 | 659 | 0.52 | 72 | 121 | 118 |
| Nβ-2 | 90 | 675 | 0.54 | 80 | 120 | 110 |
| Nβ-3 | 70 | 625 | 0.50 | 63 | 126 | 118 |
| CNβ-1 | 86 | 581 | 0.46 | 28 | 102 | 93 |
| CNβ-2 | 43 | 570 | 0.44 | 33 | 98 | 78 |
| CNβ-3 | 80 | 601 | 0.48 | 60 | 103 | 94 |
| CNβ-4 | 80 | 590 | 0.47 | 54 | 105 | 97 |
| CNβ-5 | 80 | 603 | 0.49 | 63 | 105 | 96 |
Table 2
| Relative crystallinity, % | The reservation degree of crystallization relatively after hydrothermal treatment consists, % | |
| Sβ-1 | 120 | 115 |
| Sβ-2 | 115 | 108 |
| Sβ-3 | 120 | 115 |
| CSβ-1 | 94 | 83 |
| CSβ-2 | 80 | 57 |
| CSβ-3 | 93 | 86 |
| CSβ-4 | 98 | 87 |
| CSβ-5 | 97 | 88 |
Table 3 carrier and the physico-chemical property of catalyst
| Bearer number | TCAT-1 | TCAT-2 | TCAT-3 | CTCAT-1 | CTCAT-2 | CTCAT-3 | CTCAT-4 | CTCAT-5 |
| Beta-molecular sieve, wt% | 7 | 8 | 8 | 8 | 8 | 8 | 8 | 8 |
| Y molecular sieve, wt% | 16 | 23 | 23 | 23 | 23 | 23 | 23 | 23 |
| Amorphous silica-alumina, wt% | 57 | 49 | 49 | 49 | 49 | 49 | 49 | 49 |
| Aluminium oxide, wt% | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus | Surplus |
| Specific surface area, m2/g | 501 | 512 | 518 | 474 | 483 | 480 | 486 | 488 |
| Pore volume, mL/g | 0.74 | 0.76 | 0.78 | 0.70 | 0.71 | 0.72 | 0.73 | 0.72 |
| Catalyst is numbered | CAT-1 | CAT-2 | CAT-3 | CCAT-1 | CCAT-2 | CCAT-3 | CCAT-4 | CCAT-5 |
| WO3, wt% | 22.0 | 21.8 | 22.1 | 22.1 | 22.2 | 22.1 | 22.1 | 22.2 |
| NiO, wt% | 5.9 | 5.8 | 6.0 | 6.0 | 5.9 | 6.0 | 6.1 | 6.0 |
| Specific surface area, m2/g | 410 | 415 | 427 | 385 | 383 | 386 | 397 | 395 |
| Pore volume, mL/g | 0.55 | 0.56 | 0.57 | 0.51 | 0.52 | 0.53 | 0.54 | 0.53 |
The invention described above catalyst CAT-1, CAT-2, CAT-3 and comparative example catalyst CCAT-1, CCAT-2, CCAT-3, CCAT-4, CCAT-5 are carried out active evaluation test.Test is carried out on 200mL small hydrogenation device, uses the raw materials used oil nature of one-stage serial technique to be shown in Table 4.Operating condition is as follows: hydrogen dividing potential drop 14.7MPa, hydrogen to oil volume ratio 1200:1, volume space velocity 1.5h during liquid- 1, control cracking zone nitrogen content 5～10 g/g.Catalyst Activating Test the results are shown in Table 5.
Table 4 raw oil character
| Raw oil | Iran VGO |
| Density (20 DEG C), g/cm3 | 0.9082 |
| Boiling range, DEG C | 308～560 |
| Condensation point, DEG C | 30 |
| Acid number, mgKOH/g | 0.53 |
| Carbon residue, wt% | 0.2 |
| S, wt% | 2.11 |
| N, wt% | 0.1475 |
| C, wt% | 84.93 |
| H, wt% | 12.52 |
| Aromatic hydrocarbons, wt% | 39.2 |
| BMCI value | 47.5 |
| Refractive power/nD 70 | 1.48570 |
Table 5 catalyst activity evaluation result
| Catalyst is numbered | CAT-1 | CAT-2 | CAT-3 | CCAT-1 | CCAT-2 | CCAT-3 | CCAT-4 | CCAT-5 |
| Reaction temperature, DEG C | 372 | 370 | 369 | 376 | 377 | 380 | 381 | 379 |
| < 370 DEG C of conversion ratios, wt% | 66.1 | 66.3 | 66.4 | 65.4 | 65.4 | 65.5 | 65.7 | 65.6 |
| Middle distillates oil selectivity, %(132～370 DEG C) | 89.4 | 88.4 | 87.5 | 81.9 | 82.1 | 83.8 | 84.5 | 84.8 |
| Major product character | ||||||||
| Heavy naphtha (82 ~ 132 DEG C) | ||||||||
| Virtue is latent, wt% | 66.2 | 66.7 | 66.4 | 59.4 | 59.6 | 61.2 | 61.2 | 61.5 |
| Jet fuel (132 ~ 282 DEG C) | ||||||||
| Freezing point, DEG C | <-60 | <-60 | <-60 | -52 | -54 | -58 | <-60 | <-60 |
| Aromatic hydrocarbons, wt% | 3.2 | 3.4 | 3.1 | 7.0 | 7.1 | 6.0 | 5.6 | 5.0 |
| Smoke point, mm | 27 | 27 | 27 | 21 | 22 | 23 | 24 | 24 |
| Diesel oil (282 ~ 370 DEG C) | ||||||||
| Cetane number | 71 | 70 | 72 | 54 | 56 | 57 | 58 | 59 |
| Condensation point, DEG C | -20 | -19 | -22 | -6 | -7 | -8 | -9 | -10 |
| Tail oil (> 370 DEG C) | ||||||||
| BMCI | 10.8 | 11.0 | 11.2 | 17.6 | 17.1 | 14.5 | 14.6 | 14.3 |
Be can be seen that by the evaluation result of table 5 catalyst, the catalyst prepared by the present invention, on the basis of greater activity, has good selectivity, and product property is good, and especially condensation point of diesel oil and tail oil BMCI value is relatively low.
Claims (17)
1. a preparation method for carrier of hydrocracking catalyst, including: beta-molecular sieve, Y molecular sieve, amorphous silica-alumina and binding agent are mixed, molding, drying and roasting, make carrier；On the basis of the weight of carrier, carrier composition includes: the content of beta-molecular sieve is 2～20wt%, and the content of Y molecular sieve is 10～30wt%, and the content of amorphous silica-alumina is 20～60wt%, and the content of binding agent is 15～40wt%；It is characterized in that: beta-molecular sieve is adopted and prepared with the following method:
(1), using acid-base precipitation method to prepare amorphous silica-alumina predecessor, described amorphous silica-alumina predecessor is on the basis of the gross weight of silicon dioxide and aluminium oxide, and the content that silicon is counted with silicon dioxide is as 40wt%～75wt%, preferably 55wt%～70wt%；Its preparation process includes acid-base neutralization plastic, aging, wherein silicon introduces the method for reaction system is introducing portion silicon-containing compound in aluminum contained compound and precipitant and before plastic and/or during plastic, and remainder silicon-containing compound is in aluminum contained compound with precipitant and after plastic and to introduce before ageing；
(2), by Al2O3: SiO2: Na2O:H2O=1:(62 ~ 130): (0.5～3.0): (100～500), TEAOH/SiO2Total molar ratio of=0.010 ~ 0.095, preferably SiO2/Al2O3Be 70 ~ 110, TEAOH/SiO2=0.020 ~ 0.080, under conditions of 0～40 DEG C of quick stirring, in the amorphous silica-alumina predecessor of step (1) gained, add water, silicon source and template, and control ph is 9.5 ~ 12.0, stirs, obtaining silica-alumina gel, TEA represents the quaternary amine alkali cation in template；
(3), the silica-alumina gel of step (2) gained through two step dynamic crystallizations, then through filtering, washing, prepare Na beta molecular sieve；
(4) the Na beta molecular sieve of step (3) gained is carried out ammonium salt exchange and Template removal processes, prepare beta-molecular sieve.
Preparation method the most according to claim 1, it is characterized in that: described in aluminum contained compound with precipitant and before plastic and/or during plastic the mode of introducing portion silicon-containing compound be: described part silicon-containing compound carries out premixing with described aluminum contained compound and/or precipitant, or silicon-containing compound and is individually added in reaction system during plastic in aluminum contained compound, or the combination of said method.
Preparation method the most according to claim 1, it is characterized in that: in step (1), the silicon-containing compound and after plastic and introduced before ageing in described aluminum contained compound accounts for the 5wt% ~ 85wt% in terms of silicon dioxide of the silicon in amorphous silica-alumina predecessor, preferably 30wt% ~ 70wt% in terms of silicon dioxide.
4. according to the preparation method described in any one in claim 1-3, it is characterised in that: described aluminum contained compound is selected from Al2(SO4)3、AlCl3、Al(NO3)3One or more in solution, with A12O3Quality meter, the concentration of described aluminum contained compound is 30～150g A12O3/L；One or more in sodium hydroxide solution, ammonia, sodium carbonate liquor, sodium bicarbonate solution, sodium aluminate solution of precipitant.
5. according to the preparation method described in any one in claim 1-3, it is characterised in that: described aluminum contained compound is sodium aluminate solution, with A12O3Quality meter, the concentration of described sodium aluminate solution is 40～100g A12O3/ L, described acidic precipitation agent is nitric acid.
6. according to the preparation method described in any one in claim 1-3, it is characterized in that: one or more in waterglass, Ludox and organo-silicon compound of described silicon-containing compound, described organo-silicon compound are preferably one or more in silanol, silicon ether and siloxanes, with SiO2Quality meter, the concentration of described silicon-containing compound is 40～200g SiO2/L。
7. according to the preparation method described in any one in claim 1-3, it is characterised in that: in step (2), one or more in White Carbon black, silica gel, Ludox, waterglass of described silicon source, described template is tetraethyl ammonium hydroxide.
8. according to the preparation method described in any one in claim 1-3, it is characterised in that: in step (1), the condition of described plastic is: temperature is 20～85 DEG C, and pH value is 7.0～10.0, is preferably, and temperature is 40～80 DEG C, and pH value is 7.5～9.0；Described aging condition is: temperature is 20～85 DEG C, and pH is 7.0～10.0, time 0.2～8.0 hours, is preferably, and temperature is 40～80 DEG C, and pH is 7.0～9.5, and the time is 0.5～5.0 hour.
9. according to the preparation method described in any one in claim 1-3, it is characterised in that: in step (2), generate the reaction temperature 0 of described silica-alumina gel～40 DEG C, pH value is 9.5～12.0, being preferably, the reaction temperature generating described silica-alumina gel is 10～30 DEG C, and pH value is 10～11.
10. according to the preparation method described in any one in claim 1-3, it is characterized in that: in step (3), the silica-alumina gel of step (2) gained includes through the concrete steps of two step dynamic crystallizations: the condition of first step dynamic crystallization is: carry out crystallization under agitation, temperature is 50～90 DEG C, and the time is 0.5～18.0 hour；The condition of second step dynamic crystallization is: carry out crystallization under agitation, and temperature is 100～200 DEG C, and the time is 40～120 hours.
11. preparation methoies according to claim 10, it is characterised in that: in step (3), the condition of described first step dynamic crystallization is: carry out crystallization under agitation, and temperature is 60～80 DEG C, and the time is 1～10 hour；The condition of described second step dynamic crystallization is: carry out crystallization under agitation, and temperature is 120～170 DEG C, and the time is 50～100 hours.
12. according to the preparation method described in claim 1, it is characterised in that Na in beta-molecular sieve after the exchange of ammonium salt described in step (4)2O weight content is less than 0.3%.
13. according to the preparation method described in claim 1, it is characterised in that the Template removal described in step (4) processes and uses aerobic high-temperature process, treatment temperature is 400～800 DEG C, and the process time is 5～20 hours, is preferably, treatment temperature is 500～700 DEG C, and the process time is 10～15 hours.
14. preparation methoies according to claim 1, it is characterised in that: SiO in described amorphous silica-alumina2Weight content be 20%～60%, the character of amorphous silica-alumina is as follows: pore volume is 0.6～1.1mL/g, and specific surface area is 300～500 m2/g；It is preferably as follows: SiO in described amorphous silica-alumina2Weight content be 25%～40%, character is as follows: pore volume is 0.8～1.0 mL/g, and specific surface area is 350～500 m2/g。
15. preparation methoies according to claim 1, it is characterised in that: described Y molecular sieve, its character is as follows: specific surface area 700～1000 m2/ g, total pore volume 0.45～0.90 mL/g, relative crystallinity 95%～130%, SiO2/Al2O3Mol ratio 30～100, cell parameter 2.426～2.433nm, meleic acid amount 0.1～0.4mmol/g.
16. preparation methoies according to claim 1, it is characterised in that: adhesive therefor is little porous aluminum oxide, and the pore volume of little porous aluminum oxide used is 0.3～0.5 mL/g, and specific surface area is 200～400m2/g。
17. preparation methoies according to claim 1, it is characterised in that what described carrier used be dried and roasting condition is as follows: is dried 3～10 hours at a temperature of 80～150 DEG C, 400～800 DEG C of roastings 3～12 hours.
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| CN1096295C (en) * | 1998-11-18 | 2002-12-18 | 中国石油化工集团公司 | Beta-zeolite |
| CN1221637C (en) * | 2002-04-04 | 2005-10-05 | 中国石油化工股份有限公司 | Hydro-conversion catalyst for heavy oil and residual oil and its preparing process |
| CN1290976C (en) * | 2004-06-21 | 2006-12-20 | 中国石油化工股份有限公司 | Diesel production from hydrogenation upgrading isomerizing pour-point reduction |
| CN101632938B (en) * | 2008-07-24 | 2011-12-07 | 中国石油天然气股份有限公司 | Middle fraction oil type hydrocracking catalyst |
| JP5492431B2 (en) * | 2009-03-13 | 2014-05-14 | 出光興産株式会社 | Hydrocracking catalyst, method for hydrocracking, and method for producing hydrocracking catalyst |
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| CN112221535A (en) * | 2020-10-27 | 2021-01-15 | 中化泉州石化有限公司 | Medium oil type hydrocracking catalyst and preparation method thereof |
| CN114160191A (en) * | 2021-12-02 | 2022-03-11 | 万华化学集团股份有限公司 | Catalytic cracking catalyst, preparation method and application thereof |
| CN114160191B (en) * | 2021-12-02 | 2023-07-14 | 万华化学集团股份有限公司 | Catalytic cracking catalyst and preparation method and application thereof |
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