CN1235873A - Silicon dioxide carried heteropoly acid catalyst, its preparation and use - Google Patents
Silicon dioxide carried heteropoly acid catalyst, its preparation and use Download PDFInfo
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Abstract
The catalyst has grain size of 1-100 nm and is constituted by carrying heteropoly acid in 5-80 wt% on superfine SiO2 carrier. Its preparation includes the steps of mixing heteropoly acid solution and superfine SiO2, kneading sufficiently to form homogenaeous sol, stopping kneading to make the sol form homogeneous gel automatically owing to the thixotropy of SiO2, and then drying gel, roasting and crushing. With the features of high activity, high selectivity and long service life, the catalyst is suitable for alkylation reaction of arene and C2-C20 olefines.
Description
The invention relates to a kind of solid acid catalyst, its preparation and application, specifically about a kind of be carrier loaded heteropolyacid catalyst with silica, its preparation method and the application of this catalyst in aromatic hydrocarbons and olefin alkylation reaction.
As everyone knows, in aromatic hydrocarbons and olefin alkylation reaction.Traditional acidic catalyst is inorganic liquid acid, as AlCl
3, BF
3, HF, H
2SO
4Deng.Though these inorganic liquid acid catalysts are active high, selectivity is good, but all have strong corrosivity and toxicity, can cause a series of problems such as equipment corrosion, product post processing difficulty and environmental pollution, so these inorganic acid catalysts are eliminated by solid acid catalyst just gradually.
A kind of as in the solid acid catalyst, molecular sieve catalyst has catalytic performance preferably, and has overcome shortcomings such as the corrosivity of liquid acid catalyst and contaminated environment, but its activity is than AlCl
3, HF is poor, and reaction needed is carried out under higher temperature, and then side reaction takes place easily, makes the selectivity variation, and pyroreaction also makes catalysqt deactivation, the one way lost of life easily in addition.
Heteropoly acid and salt compounds thereof are class novel solid acid catalysts of developing in recent years.Heteropoly acid is to be contained the oxygen polyacid by hetero atom (as P, Si, Fe, Go etc.) and polyatom (mainly containing Mo, W and V atom) by what the coordination of oxygen atom bridging formed, as phosphotungstic acid, and phosphomolybdic acid, silico-tungstic acid and silicomolybdic acid etc.The heteropllyacids compound has superpower acidity, low temperature high activity, and false liquid phase behavior is with advantages such as acid catalysis performance and oxidation catalytic properties.
Generally require catalyst to have higher specific surface area in actual applications, but the specific area of heteropoly acid is very little, only less than 10m
2Therefore/g need load on it on carrier of various high-ratio surfaces, and the carrier of normal employing is a silica.To the existing lot of documents report of the research of silicon dioxide carried heteropoly acid catalyst, as: Catal Rev Sci Eng, 1995,37 (2), 311; New Frontiers in Catalysis (GusziL, etal, eds.), Elsevier, Amsterdam, 1993,19; Perspectives in Catalysis (Thomas JM, Iamaraev KI.Eds.), Black, London, 1992,421.
Silicon dioxide carried heteropoly acid catalyst is also shown in following patent literature:
Having described a kind of among the WO95/13869 is the composition of porous carrier carried heteropoly acid salt (or acid salt) catalyst with titanium dioxide, silica and zirconia, preparation method and the application in aromatic hydrocarbons and olefin alkylation reaction thereof.Its preparation process divided for three steps: (1) uses the solution impregnating carrier of heteropoly acid; (2) soaked carrier is dried under 90-150 ℃; (3) after the 200-350X roasting, feed ammonia down at 100-150 ℃ again, and then heat treatment.
Having described a kind of among the USP4827048 is the process of the tert-butyl alcohol of carried heteropoly acid catalyst and the synthetic MTBE of one step of methyl alcohol reaction of carrier with titanium dioxide, silica, aluminium oxide, zirconia etc.Wherein catalyst system therefor with moulding after the aqueous solution of carrier impregnation heteropoly acid make.The shape of carrier can be powdery, sheet, spherical or strip.
A kind of method of gas-phase olefin hydration and the composition of catalyst have been described among the CN1130103.The composition of catalyst comprises the heteropoly acid that is carried on the siliceous supports, it is characterized in that siliceous supports is a strip or granular, and its particle diameter is 2-10mm, and pore volume is 0.3～1.2ml/g, and average pore size is 10～500A, and crushing strength is at least 2Kg.
A kind of synthetic method of alkylphenol of the continuous flow reactor of fixed bed that adopts heteropolyacid catalyst has been described among the USP5300703.The catalyst that is adopted to be to contain the oxide of III and IV family element, as aluminium oxide, silica, titanium dioxide, zirconia, and carbon, ion exchange resin, comprises that the sial clay that covers holder soil is that the aqueous solution of carrier impregnation heteropoly acid gets.
Having described a kind of preparation method of alkylbenzene among the JP0525063, is to be catalyst with heteropoly acid or heteropolyacid salt, makes aromatic hydrocarbons and C2-5 alkene carry out liquid-phase alkylation system kind monoalkyl benzene and dialkyl benzene.
In sum, in the prior art up to now, with silica be the carried heteropoly acid catalyst of carrier all to adopt particle size be that millimetre-sized silica is carrier, catalyst all is prepared into oven dry roasting behind the aqueous solution of silica supports dipping heteropoly acid.
The objective of the invention is to provide on the basis of existing technology a kind of prior art that is different from, the active and higher silicon dioxide carried heteropoly acid catalyst of selectivity.
Second purpose of the present invention promptly provides the specific preparation method who is used for above-mentioned catalyst.
The 3rd purpose of the present invention then provides the application of this catalyst in alkylated reaction.
The particle diameter of silicon dioxide carried heteropoly acid catalyst provided by the invention is 1～100 nanometer, is to be carrier with the superfine silicon dioxide, load 5～80 heavy %, and the heteropoly acid of best 15～50 heavy % constitutes.
Wherein said superfine silicon dioxide is selected from the silica of the pore-free that comprises white carbon, fumed silica, precipitated silica.Said heteropoly acid is to be contained the oxygen polyacid by the hetero atom that comprises P, Si, Fe, Co and the polyatom that comprises Mo, W, V by what the coordination of oxygen atom bridging constituted, as 12 phosphotungstic acids, 12 silico-tungstic acids, 12 phosphomolybdate, 12 silicomolybdic acid etc.
Above-mentioned Preparation of catalysts method provided by the invention is: heteropoly acid solution is mixed with superfine silicon dioxide, fully kneading is to forming uniform sol, will be owing to stopping to mediate the uniform frozen glue that forms of transition at room temperature dry drying, roasting, pulverizing then.
Wherein selected heteropoly acid is to be contained the oxygen polyacid by the hetero atom that comprises P, Si, Fe, Co and the polyatom that comprises Mo, W, V by what the coordination of oxygen atom bridging constituted, as 12 phosphotungstic acids, 12 silico-tungstic acids, 12 phosphomolybdate, 12 silicomolybdic acid etc.
Said heteropoly acid solution is that above-mentioned heteropoly acid is dissolved in formed solution in the water that can dissolve heteropoly acid, alcohol, ketone, ether, the ester isopolarity solvent, preferably is dissolved in formed solution in the little easy volatile solvent of surface tension such as ethanol, acetone, ether.
The concentration of this solution is 0.005g/ml～0.5g/ml, and its consumption is every gram silica supports 2～10ml, best 3～6ml.In this addition scope, the even colloidal sol that heteropoly acid solution and silica form can automatic transition form uniform frozen glue when stopping to mediate, and promptly silica demonstrates its thixotropic property.The concentration of heteropoly acid solution and addition thereof should be regulated simultaneously, and making the load capacity of heteropoly acid on the final catalyst is 5～80%, is preferably 15～50%.
Employed superfine silicon dioxide carrier is the silica of the simple particle diameter that makes of the whole bag of tricks less than the pore-free of 100 nanometers, for example white carbon black, fumed silica, precipitated silica etc.
The baking temperature that is adopted is 60 ℃～150 ℃, is preferably 100 ℃～120 ℃, and be 1～10 hour drying time, is preferably 3～5 hours.
The sintering temperature that is adopted is 150 ℃～450 ℃, is preferably 200 ℃～300 ℃, and roasting time is 1～10 hour, is preferably 3～5 hours.Roasting can be carried out in air atmosphere, also can carry out in inert gas atmosphere such as nitrogen, can also carry out in a vacuum.
Because the material after the roasting is very easily pulverized, thereby grinding mode is not subjected to any restriction, as long as be crushed to powdery.
Superfine silicon dioxide carried heteropoly acid catalyst provided by the invention be suspended in the reaction mass easily, and the activated centre is dispersed in the outer surface of catalyst fully because catalyst granules is little, eliminated inside and outside diffusion influence, do not exist because of carbon distribution stops up the catalysqt deactivation problem that the duct causes yet, therefore, the activity of such catalysts height, the selectivity height, catalyst life is long, can be used for aromatic hydrocarbons (benzene, toluene, dimethylbenzene, phenol etc.) and C
2～C
20The various alkylated reactions of alkene prepare corresponding alkylbenzene, as benzene and ethylene reaction synthesizing ethyl benzene; Benzene and propylene reaction synthesizing iso-propylbenzene; Benzene and long chain olefin alkylation reaction synthesize long-chain linear alkylbenzene; The first benzene alkylation with propylene generates cymene; Phenol and isobutene alkylation generate t-butyl phenol etc.
The specific preparation method of this catalyst provided by the invention has adopted the little easy volatile solvent of surface tension when carried heteropoly acid, and utilize the thixotropic property of superfine silicon dioxide, thereby guaranteed that heteropoly acid can high degree of dispersion can not assembled at the outer surface and the carrier of carrier in preparation process, made pore-free, bulk density is little (only to be 0.1～0.3g/ml) ultrafine particle catalyst.
When catalyst provided by the present invention is used for above-mentioned aromatic hydrocarbons and makes preparations for sowing the alkylated reaction of alkene, can in reactor, carry out with mode of operation intermittently, or the catalyst fluidised formization is carried out in the fluidized bed process mode, also can carry out in a continuous manner, this catalyst fines and binding agent can also be applied to together the distillation element surface and make and be fixed in the destilling tower mode after " catalyst structure " again and carry out with catalytic distillation with being loaded in the fixed bed reactors after this catalyst and the adhesive moulding.General adoptable alkylated reaction temperature is room temperature～300 ℃, is preferably room temperature～100 ℃, and the pressure of reaction should be able to guarantee that reaction mass is in or partly be in liquid phase state that benzene alkene mol ratio is 2～50: 1, is preferably 5～10: 1.
Accompanying drawing demonstrates the situation of change of the catalytic activity of catalyst provided by the present invention and contrast medium with access times.
Following example will be further specified the present invention, but therefore scope of the present invention not limited to some extent.
Example 1
The preparation of superfine silicon dioxide load phosphotungstic acid catalyst.
Compound concentration is that (analyze purely, molecular formula is H for the phosphotungstic acid of 0.0235M
3PW
1220H
2O) acetone soln, get this solution 600ml join the superfine silicon dioxide support powder that the 100g vapor phase method produces (AEROSIL 200, the DEGUSSA product, pore-free, specific area is 200m
2/ g, simple particle mean size is 12nm) in, fully mediate,, stop to mediate until forming uniform sol, because silica has thixotropic property, stop to mediate back colloidal sol and become uniform frozen glue, this frozen glue is at room temperature dried, drying is 3 hours under 120 ℃, again 200 ℃ of following roastings 5 hours, again the gained solid is pulverized with pulverizer that to make the phosphotungstic acid load capacity be 28% superfine silicon dioxide supported catalyst at last.Its bulk density is 0.25g/cm after measured
3, the BET specific area is 134m
2/ g, the TEM method records its simple average particle diameter and is about 15nm.
Example 2
The preparation of superfine silicon dioxide load silicotungstic acid catalyst.
Compound concentration is that (analyze purely, molecular formula is H for the silico-tungstic acid of 0.0235M
3SiW
1224H
2O) acetone soln, getting this solution 600ml joins in the superfine silicon dioxide support powder of 100g specification with example 1, fully mediate,, stop to mediate until forming uniform sol, because silica has thixotropic property, stop to mediate back colloidal sol and become uniform frozen glue, this frozen glue is at room temperature dried, drying is 5 hours under 100 ℃, 300 ℃ of following roastings 3 hours, making the silico-tungstic acid load capacity after the gained solid being pulverized at last was 28% superfine silicon dioxide supported catalyst again again.Its bulk density is 0.3g/cm after measured
3, the BET specific area is 137m
2/ g, it is 20nm that the TEM method records its average simple particle diameter.
Comparative example 1
The preparation of common silica gel load phosphotungstic acid catalyst.
Compound concentration is the aqueous solution of the phosphotungstic acid (specification is with example 1) of 0.094M, gets this solution 600ml and joins 100g silica-gel carrier powder (Haiyang Chemical Plant, Qingdao produces, and particle size is 105～125 μ m, and specific area is 450m
2/ g) in, this solution amount just in time can suppressed by vector institute all absorb, with its 110 ℃ dry 3 hours down, again 225 ℃ of following roastings 3 hours, make the phosphotungstic acid load capacity and be 28% silica supported catalyst.Its BET specific area is 350m after measured
2/ g, bulk density are 1.5g/cm
3
Comparative example 2
The preparation of pure phosphotungstic acid catalyst.
With commercially available phosphotungstic acid (specification is with example 1),, at 250 ℃ of roastings porphyrize after 3 hours, make phosphotungstic acid catalyst again 100 ℃ of dryings 3 hours.Its bulk density is 3.8g/cm after measured
3, the BET specific area is 6m
2/ g.
Comparative example 3
The preparation of pure silicon tungstic acid catalyst.
With commercially available silico-tungstic acid (specification is with example 2),, at 250 ℃ of roastings porphyrize after 3 hours, make silicotungstic acid catalyst again 100 ℃ of dryings 3 hours.Its bulk density is 3.5g/cm after measured
3, the BET specific area is 5m
2/ g.
Comparative example 4
H beta-molecular sieve Preparation of catalysts.
With Na beta-molecular sieve (industrial goods, SiO
2/ Al
2O
3=25) through NH
4NO
3Exchange for several times, washing, 120 ℃ of dryings 3 hours, 550 ℃ of roastings obtained the H beta catalyst in 5 hours, and its sodium content is less than 0.5% after measured.
Comparative example 5
The preparation of HY molecular sieve catalyst.
With NaY molecular sieve (industrial goods, SiO
2/ Al
2O
3=5) through NH
4NO
3Exchange for several times, washing, 120 ℃ of dryings 3 hours, 550 ℃ of roastings obtained the HY catalyst in 5 hours, and its sodium content is less than 0.5% after measured.
Example 3
Various catalyst are to the catalytic activity of benzene～propylene reaction.
Its catalytic activity to benzene～propylene reaction is estimated in relatively agent of the common silica gel load phosphotungstic acid that superfine silicon dioxide load phosphotungstic acid provided by the invention that example 1 and 2 is prepared and superfine silicon dioxide load silicotungstic acid catalyst and comparative example 1～4 are prepared, pure phosphotungstic acid, pure silicon wolframic acid and H β as follows respectively.
Adding 25ml benzene in having the 100ml four-hole boiling flask of thermostatted water chuck, magnetic agitation and reflux condensing tube (analyzes pure, through the 4A molecular sieve drying) and a certain amount of catalyst, opening magnetic stirring apparatus stirs fast, feed thermostatted water, behind the constant temperature to 80 ℃, speed with 200ml/min. fed propylene 20 minutes, and products therefrom is analyzed on gas chromatograph (GC8000 that CE company produces).Chromatographic column is that diameter is 0.25mm, the OV of long 30m～1 capillary column, fid detector.The reaction result of various catalyst is listed in table 1.
Table 1
| Example | Example 1 | Example 2 | Comparative example 1 | Comparative example 2 | Comparative example 3 | Comparative example 4 | |
| Catalyst | PW/SiO 2(ultra-fine) | SiW/SiO 2(ultra-fine) | PW/SiO 2(common) | Pure PW acid | Pure SiW acid | ??Hβ | |
| Catalyst amount g | ?0.15 | ?0.15 | ?0.15 | ?0.15 | ?0.15 | ?1.25 | |
| Product distributes | Benzene isopropylbenzene diisopropylbenzene (DIPB) polyisopropylbenzene | ?64.43 ?24.21 ?8.89 ?2.47 | ?69.75 ?21.95 ?6.73 ?1.57 | ?82.89 ?13.09 ?3.25 ?0.77 | ?70.0 ?21.14 ?7.01 ?1.85 | ?76.07 ?18.32 ?4.76 ?0.85 | ?80.5 ?18.45 ?1.04 ?0.01 |
| Benzene conversion ratio % | ?35.57 | ?30.25 | ?17.11 | ?30.0 | ?23.93 | ?19.05 | |
As can be known from Table 1, superfine silicon dioxide load phosphotungstic acid provided by the present invention and silicotungstic acid catalyst have high activity to the alkylated reaction of benzene～propylene, its loaded by heteropoly acid amount has only 28%, but the pure heteropolyacid catalyst of specific activity same amount is much higher, and adopts the heteropolyacid catalyst activity of common silica gel load minimum.H β is considered to best molecular sieve catalyst usually, but under low temperature (80 ℃) and normal pressure, activity is also very low.As known from Table 1, the consumption of superfine silicon dioxide load phosphotungstic acid catalyst is 1/8 of H β, but the conversion ratio of benzene exceeds nearly one times, illustrates that the specific activity H β of superfine silicon dioxide load phosphotungstic acid catalyst under the same amount situation wants at least 10 times of height.
Example 4
Various catalyst are to the catalytic activity of toluene～propylene reaction.
Its catalytic activity to toluene～propylene reaction is estimated in relatively agent of the common silica gel load phosphotungstic acid that superfine silicon dioxide load phosphotungstic acid catalyst provided by the invention that example 1 is prepared and comparative example 1,2 and 4 are prepared, pure phosphotungstic acid and H β as follows respectively.
Adding 25ml toluene in having the 100ml four-hole boiling flask of thermostatted water chuck, magnetic agitation and reflux condensing tube (analyzes pure, through the 4A molecular sieve drying) and a certain amount of catalyst, opening magnetic stirring apparatus stirs fast, feed thermostatted water, behind constant temperature to the 80 ℃ C, speed with 200ml/min. fed propylene 20 minutes, and products therefrom is analyzed on gas chromatograph (GC8000 that CE company produces).Chromatographic column is that diameter is 0.25mm, the OV of long 30m～1 capillary column, fid detector.The reaction result of various catalyst is listed in table 2.
Table 2
| Example | Example 1 | Comparative example 1 | Comparative example 2 | Comparative example 4 |
| Catalyst | PW acid/SiO 2(ultra-fine) | PW acid/SiO 2(common) | Pure PW 12 | ?Hβ |
| Catalyst amount, g | ?0.25 | ?0.25 | ?0.25 | ?1.0 |
| Toluene conversion % | ?54.15 | ?40.7 | ?52.43 | ?30.2 |
| The selectivity of cymene, wt.% | ?61.54 | ?64.4 | ?63.04 | ?92.9 |
| The cymene isomeric distribution is to ortho position, interdigit position | ?26.04 ?41.51 ?32.45 | ?26.6 ?41.3 ?32.1 | ?26.17 ?41.7 ?32.13 | ?28.74 ?40.94 ?30.32 |
As can be known from Table 2, superfine silicon dioxide load phosphotungstic acid catalyst provided by the present invention has than common silica gel load phosphotungstic acid, pure phosphotungstic acid, the activity that H β is higher the alkylated reaction of toluene～propylene.
Example 5
Various catalyst are to the catalytic activity of benzene and laurylene-1 alkylated reaction
Common silica gel load phosphotungstic acid, pure phosphotungstic acid and five kinds of catalyst of HY that superfine silicon dioxide load phosphotungstic acid provided by the invention that example 1 and 2 is prepared and superfine silicon dioxide load silicotungstic acid catalyst and comparative example 1,2 and 5 are prepared are estimated its catalytic activity to benzene～laurylene～1 reaction as follows respectively.
Having the thermostatted water chuck, adding 20ml benzene in the 100ml four-hole boiling flask of magnetic agitation and reflux condensing tube (analyzes pure, through the 4A molecular sieve drying) and 5ml laurylene～1 (analyze pure, through silica dehydrator), mixture benzene alkene mol ratio is 10: 1, opens magnetic stirring apparatus and stirs fast, feed thermostatted water, add a certain amount of catalyst behind the constant temperature, and open timer simultaneously, regularly on gas chromatograph (GC8000 that CE company produces), analyze with syringe sampling.Chromatographic column is that diameter is 0.25mm, the OV of long 30m～1 capillary column, fid detector.
Press above-mentioned evaluation method at 80 ℃, benzene alkene is under 10: 1 the rigid condition than (mol ratio), minimum catalyst amount (g) when being determined at laurylene in 30 minutes～1 and can transforming fully, and calculate selectivity S, 2～Φ selectivity S according to the product analysis result after laurylene～1 complete reaction
The position, linearity D, gained the results are shown in table 3.
In the table:
Molal quantity * 100 of laurylene in the molal quantity/charging of laurylene conversion ratio X=reaction consumes laurylene
Molal quantity * 100 of the molal quantity of selectivity S=product monoalkyl benzene/reaction consumes laurylene
2～Φ selectivity S
The positionThe molal quantity of the molal quantity/monoalkyl benzene of=2～phenyl dodecane * 100
The molal quantity of the molal quantity/monoalkyl benzene of linearity D=linear alkyl benzene * 100
Table 3
| Example | Example 1 | Example 2 | Comparative example 1 | Comparative example 2 | Comparative example 5 |
| Catalyst | PW/SiO 2(ultra-fine) | ?SiW/SiO 2(ultra-fine) | ???PW/SiO 2(common) | Pure PW acid | ?????HY |
| Minimum catalytic amount g) | ?0.25 | ????0.5 | ????2.5 | ????1.25 | ????1.25 |
| Selectivity S | ?99.0 | ????99.1 | ????99.0 | ????97.0 | ????96.0 |
| 2～Φ selectivity S The position | ?39.8 | ????37.5 | ????42.7 | ????50 | ????26 |
| Linearity D | ?98.5 | ????98.0 | ????98.5 | ????98.0 | ????97.5 |
As can be known from Table 3, superfine silicon dioxide carried heteropoly acid catalyst provided by the present invention shows the highest activity to benzene～laurylene～1 alkylated reaction, wherein the activity with the superfine silicon dioxide phosphotungstic acid catalyst is the highest, its activity is 5 times of pure phosphotungstic acid catalyst, 6 times of HY, 8 times of common silica gel load phosphotungstic acid catalyst.The selectivity of superfine silicon dioxide carried heteropoly acid catalyst is apparently higher than the HY molecular sieve catalyst.The linearity of products therefrom and 2 position isomer content are than high many of HY.
Example 6
The comparison of heteropoly acid and molecular sieve catalyst stability.
Because the easiest catalysqt deactivation that makes of reaction of benzene and long-chain olefin (as laurylene) in the alkylation of benzene and various alkene, thereby the alkylated reaction of this example employing benzene and laurylene～1 has compared the inactivation speed of superfine silicon dioxide load phosphotungstic acid catalyst and pure phosphotungstic acid, HY catalyst.
Relatively agent of pure phosphotungstic acid that superfine silicon dioxide load phosphotungstic acid catalyst provided by the invention that example 1 is prepared and comparative example 2 and 5 are prepared and HY, be 1.25g in catalyst consumption, investigate the variation of the rate of rotation of laurylene with catalyst access times (each 30 minutes) under other condition and the example 5 identical conditions, the result as shown in the figure.
Result's superfine silicon dioxide load phosphotungstic acid catalyst provided by the invention as can be known has the highest stability from figure, and its activity still remains on more than 75% when using 20 times, and other catalyst use has just lost activity 5 times substantially.
Example 7
The catalytic activity of different phosphate wolframic acid load capacity catalyst.
Compound concentration is 0.00587 respectively, 0.00118,0.0235,0.0353,0.0558,0.175M the phosphotungstic acid acetone soln, get each 600ml of above-mentioned solution and join respectively in the superfine silicon dioxide support powder of 100g specification with example 1, fully mediate, until forming uniform sol, stop to mediate,, stop to mediate back colloidal sol and become uniform frozen glue because silica has thixotropic property, this frozen glue is at room temperature dried, drying is 3 hours under 110 ℃, again 225 ℃ of roastings 3 hours, and the last superfine silicon dioxide supported catalyst that again the gained solid is made different phosphate wolframic acid load capacity with the pulverizer pulverizing.Their materialization data separately and the catalytic activity in benzene-propylene alkylated reaction are as shown in table 4.
Benzene alkylation with propylene reaction time catalizer consumption is 0.15g, and the remaining reaction condition is with example 3.
By table 4 data as can be known no matter the phosphotungstic acid load capacity what, superfine silicon dioxide carried heteropoly acid catalyst provided by the invention all has catalytic activity preferably.
Table 4
| Load capacity (weight fraction) | ????SiO 2 | ?0.1 | ?0.175 | ?0.28 | ?0.375 | ????0.5 | ????0.67 |
| Specific surface, m 2/g | ????200 | ?171 | ?156 | ?134 | ?112 | ????97 | ????68 |
| Particle diameter, nm | ????12 | ?13 | ?13 | ?15 | ?16 | ????17 | ????22 |
| The benzene conversion ratio, % | ????0 | ?17.1 | ?30.5 | ?35.6 | ?35.2 | ????34.3 | ????32.0 |
Claims (12)
1. a silicon dioxide carried heteropoly acid catalyst is characterized in that its particle diameter is 1～100 nanometer, is to be carrier with the superfine silicon dioxide, and the heteropoly acid of load 5～80 heavy % constitutes.
2. according to the described catalyst of claim 1, the load capacity that it is characterized in that said heteropoly acid is 15～50 heavy %.
3. according to the described catalyst of claim 1, it is characterized in that said superfine silicon dioxide is the silica of simple particle diameter less than the pore-free that comprises white carbon, fumed silica, precipitated silica of 100 nanometers.
4. according to the described catalyst of claim 1, it is characterized in that said heteropoly acid is to be contained the oxygen polyacid by the hetero atom that comprises P, Si, Fe, Co and the polyatom that comprises Mo, W, V by what the coordination of oxygen atom bridging constituted.
5. the described Preparation of catalysts method of claim 1, it is characterized in that: heteropoly acid solution is mixed with superfine silicon dioxide, fully kneading is to forming uniform sol, and uniform frozen glue that will transition forms owing to stopping to mediate at room temperature dries drying, roasting, pulverizing then.
6. according to the described preparation method of claim 5, it is characterized in that said superfine silicon dioxide is the silica of simple particle diameter less than the pore-free that comprises white carbon, fumed silica, precipitated silica of 100 nanometers.
7. according to the described preparation method of claim 5, it is characterized in that said heteropoly acid is to be contained the oxygen polyacid by the hetero atom that comprises P, Si, Fe, Co and the polyatom that comprises Mo, W, V by what the coordination of oxygen atom bridging constituted.
8. according to the described preparation method of claim 5, it is characterized in that said heteropoly acid solution is that heteropoly acid is dissolved in formed solution in the polar solvent that comprises water, alcohol, ketone, ether, ester.
9. according to the described preparation method of claim 8, it is characterized in that said heteropoly acid solution is that heteropoly acid is dissolved in formed solution in ethanol, acetone, the ether.
10. according to claim 5, one of 8 or 9 described preparation methods, the concentration that it is characterized in that said heteropoly acid solution is 0.005g/ml～0.5g/ml, and its consumption is every gram silica supports 2～10ml.
11. according to the described preparation method of claim 10, the consumption that it is characterized in that said heteropoly acid solution is every gram silica supports 3～6ml.
12. the carried heteropoly acid catalyst of claim 1 is characterized in that being used for aromatic hydrocarbons and C
2～C
20The alkylated reaction of alkene.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4898995A (en) * | 1988-10-24 | 1990-02-06 | Texaco Chemical Company | Method for production of phenol/acetone from cumene hydroperoxide |
| JP2546545B2 (en) * | 1990-02-02 | 1996-10-23 | 株式会社日本触媒 | Method for producing alkylnaphthalene |
| WO1995013869A1 (en) * | 1993-11-19 | 1995-05-26 | Exxon Research & Engineering Company | Heteropoly compounds and use in aromatic alkylation |
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