CN105712822A - Method for preparation of ethylene by ethanol dehydration - Google Patents
Method for preparation of ethylene by ethanol dehydration Download PDFInfo
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Abstract
The invention discloses a method for preparation of ethylene by ethanol dehydration. The method involves at least two catalyst beds, i.e. a catalyst A and a catalyst B. The catalyst A is composed of: an active component heteropoly acid, an assistant boron oxide, and a carrier silicon dioxide coated alumina, and the catalyst B consists of: an active component heteropoly acid ammonium salt, an assistant nickel oxide, and a carrier silicon oxide. According to the invention, the two catalysts are employed for mutual cooperation to give full play to respective advantages, so that the reaction system has improved comprehensive reaction performance, and has higher activity, selectivity and stability.
Description
Technical field
The present invention relates to a kind of by the method for preparing ethylene by dehydrating ethanol, particularly relate to a kind of use combination catalyst for the method for preparing ethylene by dehydrating ethanol.
Background technology
Ethylene is as the flagship product of basic Organic Chemicals and petro chemical industry, and the chemical products of about 75% prepare with ethylene for raw material, and therefore the size of ethylene yield has become as the important symbol weighing a national oil development of chemical industry level.Traditional ethylene obtains mainly by light petroleum fraction cracking, heavy dependence petroleum resources.Along with the day of international energy situation is becoming tight, petroleum resources are increasingly exhausted, and developing new renewable alternative energy source has been the task of top priority.
Many-sided advantages such as recently, ethanol particularly recyclable organism preparing ethylene by dehydrating ethanol is increasingly subject to people's attention, and it has green, sustainable, reaction condition is gentle and product ethylene purity is high.Bio-ethanol is mainly derived from the fermentation of agricultural byproducts, can avoid the dependence to petroleum resources, continues to use this method in the country that some petroleum resources such as Brazil, India, Pakistan are deficient always and produces ethylene, and more there is realistic meaning in the country of oil-poor and few oil by this point.Preparing ethylene by dehydrating ethanol has the great potential partly or entirely replacing obtaining ethylene from oil.Therefore, research producing ethylene from dehydration of ethanol has great economic worth and strategic importance.
Catalyst for ethanol delydration to ethylene report is a lot, mainly activated alumina, molecular sieve and heteropoly acid etc..Activated alumina is as catalyst low price, and activity and selectivity is better, but reaction temperature is high, and reaction velocity is low, and energy consumption is high, and utilization rate of equipment and installations is low.The catalysis activity and selectivity of molecular sieve is high, stable；Reaction temperature is low, and reaction velocity is big, but catalyst life is short, and amplification is little, limits its industrialized production.Heteropoly acid is with certain structure oxygen-containing polyprotic acid by oxygen atom ligand bridging by central atom and coordination atom, has the advantages such as highly acid.In producing ethylene from dehydration of ethanol reacts, it is low that heteropolyacid catalyst has reaction temperature, the feature that selectivity is high and yield is high.
Li Benxiang etc. [Chemical Engineering Technology and exploitation, 2010,5 (39): 7-9] report the article being entitled as MCM-41 load Catalyzed by Silicotungstic Acid producing ethylene from dehydration of ethanol, and catalyst adopts infusion process to prepare.CN200910057539.X discloses the catalyst of a kind of producing ethylene from dehydration of ethanol.This catalyst is with aluminium oxide for carrier, and active component is heteropoly acid, adopts kneading method to prepare.Above-mentioned catalyst, when with high concentration ethanol for raw material, shows higher catalysis activity and selectivity, but when with low-concentration ethanol for raw material, catalyst activity is decreased obviously, and stability is bad.
Producing ethylene from dehydration of ethanol is the endothermic reaction, primary response is that a part alcohol catalysis is obtained by reacting a part ethylene and a part water, carrying out along with reaction, axial along reactor, ethanol generation dehydration content in raw material is gradually lowered, the content of water gradually rises, catalyst bed interlayer also there will be the bigger temperature difference, the catalyst contact of bottom bed is the low-concentration ethanol raw material containing a large amount of water all the time, and catalyst bottom bed temperature substantially reduces, this can directly influence the performance of lower catalytic agent, the catalyst activity causing reactor lower part substantially reduces, thus affecting the activity of integer catalyzer, selectivity and stability.
Summary of the invention
In order to overcome weak point of the prior art, a kind of method that the invention provides preparing ethylene by dehydrating ethanol.The method has the advantages such as ethanol conversion height, selectivity and good stability.
The method of preparing ethylene by dehydrating ethanol of the present invention, including at least two beds and catalyst A and catalyst B, wherein ethanol raw material first contacts with catalyst A, then contacts with catalyst B again；
Catalyst A's is composed as follows: adopt alumina support, with heteropoly acid for active component, auxiliary agent is boron oxide, wherein alumina carrier surface coated silica, the weight of silicon dioxide accounts for the 5% ~ 20% of the carrying alumina body weight of coated with silica, it is preferably 8% ~ 18%, with the weight of catalyst for benchmark, the content of heteropoly acid is 3% ~ 25%, being preferably 5% ~ 20%, more preferably 10% ~ 18%, the content that auxiliary agent is counted with oxide is for 2% ~ 8%, the content of the alumina support of coated with silica is 67% ~ 95%, it is preferred to 72% ~ 93%；
Catalyst B's is composed as follows:
Active component is that ammonium heteropoly acids is shown in formula (1), and auxiliary agent is nickel oxide, and carrier is silicon oxide；With the weight of catalyst for benchmark, the content of ammonium heteropoly acids is 8% ~ 35%, it is preferred to 12% ~ 30%, more preferably 18% ~ 30%, the content that auxiliary agent is counted with oxide is for 3% ~ 18%, it is preferred to 5% ~ 15%, the content of carrier is 47% ~ 89%, it is preferred to 55% ~ 83%, more preferably 55% ~ 77%；
Hm(NH4)nYX12O40(1)
Wherein X represents W or Mo, Y and represents Si or P；When Y represents Si, m+n=4, n value is 0.1 ~ 0.5；When Y represents P, m+n=3, n value is 0.1 ~ 0.5.
The character of described silica support is as follows: specific surface area is 500 ~ 820m2/ g, pore volume is 0.62 ~ 0.92mL/g, and average pore diameter is 4.6 ~ 6.6nm.
In catalyst A of the present invention, heteropoly acid is the distribution in uniform type on the alumina support of coated with silica, and namely heteropoly acid is evenly distributed on the surfaces externally and internally of the alumina support of coated with silica.In catalyst B of the present invention, ammonium heteropoly acids is distributed on silica support and is distributed in eggshell type, say, that ammonium heteropoly acids is distributed on the outer surface of silica support, and is substantially free of ammonium heteropoly acids in catalyst duct.
In the inventive method, in catalyst B, the weight content of ammonium heteropoly acids is not less than in catalyst A the weight content of heteropoly acid.
In the present invention, the preparation method of catalyst A, including:
I, prepare alumina support；
II, preparation coated with silica alumina support；
III, the carrier that step II prepares is joined in the mixed solution of heteropoly acid and auxiliary agent presoma, stir at 50 DEG C ~ 90 DEG C to solution and be evaporated；
IV, the solid obtained by step III, at 90 DEG C ~ 120 DEG C dry 5h ~ 12h, then at 300 DEG C ~ 450 DEG C roasting 2h ~ 6h, obtain catalyst A.
In step I, described alumina support is to be obtained through molding, dry and roasting by boehmite.Described boehmite can adopt conventional method to prepare, such as: Alchlor process, aluminum sulfate method, carbonizatin method etc..Described roasting condition: sintering temperature is 400 DEG C ~ 700 DEG C, and roasting time is 2h ~ 10h.
In step II, the method of the alumina support of preparation coated with silica is as follows: organic acid, dispersion aids is mixed with water and is made into mixed solution, silicon source is joined in mixed solution, after mix homogeneously, adds alumina support, 2h ~ 6h is stirred at 50 DEG C ~ 90 DEG C, then stir to becoming gel at 50 DEG C ~ 90 DEG C, aging 5h ~ 12h at 20 DEG C ~ 50 DEG C, at 90 DEG C ~ 120 DEG C dry 5h ~ 12h, at 300 DEG C ~ 600 DEG C roasting 2h ~ 6h, obtain the alumina support of coated with silica.Described organic acid is one or more in citric acid, tartaric acid and malic acid, and the mol ratio that organic acid and silicon source are counted with silicon dioxide is for 0.05 ~ 0.25；Dispersion aids is molecular weight is one or more in the Polyethylene Glycol of 200 ~ 2000, and the mol ratio that Polyethylene Glycol and silicon source are counted with silicon dioxide is for 0.05 ~ 0.20.Silicon source is one or more in tetraethyl orthosilicate, Ludox.Adopt the silica particles that said method can make carrier surface be coated with suitable and uniform, be uniformly dispersed.
In step III, described heteropoly acid is one or more in phosphotungstic acid, silico-tungstic acid, phosphomolybdic acid；Auxiliary agent presoma is boric acid.
In the present invention, the preparation method of catalyst B, including:
(1) auxiliary agent precursor water solution is joined in silica support, stir at 60 DEG C ~ 90 DEG C to solution and be evaporated；
(2) solid step (1) obtained is at 90 DEG C ~ 120 DEG C dry 3h ~ 12h, then at 300 DEG C ~ 500 DEG C roasting 2h ~ 6h, prepares catalyst precarsor A；
(3) catalyst precarsor A is joined in autoclave, adopt hydrogen that it is carried out reduction treatment；
(4) polyhydric alcohol solutions is driven in autoclave, then regulates Hydrogen Vapor Pressure to 2～4MPa, at 200～300 DEG C, react 0.5～5.0h；
(5) catalyst precarsor A reacted in step (4) is filtered out, at 20 DEG C ~ 50 DEG C, it is preferred to be dried at 30 DEG C ~ 50 DEG C, until sample surfaces is without liquid phase, obtain catalyst precarsor B；
(6) the catalyst precarsor B that step (5) obtains is joined in aqueous solutions of organic acids, stir at 60 DEG C ~ 90 DEG C and be evaporated to solution, obtain catalyst precarsor C；
(7) the catalyst precarsor C that step (6) obtains is joined in the alkaline solution containing ammonium, through filtering, dry at 50 DEG C ~ 90 DEG C；Or material step (6) obtained adsorbs ammonia at 50 DEG C ~ 90 DEG C, obtains catalyst precarsor D；
(8) aqueous solution of heteropoly acid is joined in the catalyst precarsor D that step (7) obtains, stir at 60 DEG C ~ 90 DEG C to solution and be evaporated；
(9) solid step (8) obtained is at 90 DEG C ~ 120 DEG C dry 3h ~ 12h, then at 300 DEG C ~ 550 DEG C roasting 2h ~ 6h, obtains catalyst.
Silica support described in step (1) is adopted and is prepared with the following method:
A, template is joined containing in organic acid aqueous solution, obtain solution I；
B, silicon source is joined in solution I, obtain solution II, then stir to becoming gel at 60 DEG C ~ 90 DEG C；
C, by gel aging 8h ~ 24h, drying at 20 DEG C ~ 50 DEG C, make silica support.
In step A, described template is cetyl trimethylammonium bromide, hexadecyltrimethylammonium chloride, sodium lauryl sulphate, triblock polymer P123, triblock polymer F127, triblock polymer F108, molecular weight be 1000 ~ 10000 Polyethylene Glycol in one or more, described template and SiO in carrier2Mol ratio be 0.01 ~ 1.2；Described organic acid is one or more in citric acid, tartaric acid, malic acid, SiO in described organic acid and carrier2Mol ratio be 0.1 ~ 1.2.
In step B, described silicon source is one or more in tetraethyl orthosilicate, Ludox.
In step C, described silica support can make the silica support of molding, it is also possible to being the silica support not needing molding, those skilled in the art determine according to selected technique.The silica support of molding, it is possible to adopt existing conventional molding techniques to carry out molding, such as extruded moulding, compression molding etc., shape can be bar shaped, spherical, lamellar etc..In forming process, it is possible to adding binding agent and shaping assistant as required, binding agent is generally adopted little porous aluminum oxide.Shaping assistant is peptizer, extrusion aid etc. such as.After step C dries, it is possible to through molding or without molding, obtain silica support then through high-temperature roasting.
In step C, described dry and roasting adopts usual manner to carry out, and the dry condition being generally adopted is as follows: 90 DEG C ~ 120 DEG C dry 3h ~ 12h, roasting is typically in 300 DEG C ~ 800 DEG C roasting 2h ~ 6h.
In step (1), the described nickel salt that auxiliary agent presoma is solubility, be generally in nickel nitrate, nickel acetate one or more.
In step (3), described reduction treatment process is as follows: catalyst precarsor is warming up under hydrogen atmosphere 300 DEG C～600 DEG C, processes 4h～8h under 0.1MPa～0.5MPa.Wherein reduction treatment can adopt pure hydrogen, it would however also be possible to employ the hydrogen containing noble gas, and hydrogen volume concentration is 30% ~ 100%.
In step (4), described polyhydric alcohol is one or more in C5～C10 polyhydric alcohol, it is preferable that one or more in xylitol, sorbitol, mannitol, arabitol；The mass concentration of polyhydric alcohol solutions is 5%～30%.The mass ratio of the addition of polyhydric alcohol and catalyst precarsor A is 3:1 ~ 10:1.
In step (6), described organic acid is one or more in citric acid, tartaric acid, malic acid.Described organic acid and SiO in carrier2Mol ratio be 0.05 ~ 0.50.
In step (7), being joined in the alkaline solution containing ammonium by the catalyst precarsor C that step (6) obtains and impregnate, dip time is generally 5min ~ 30min.Catalyst precarsor C step (6) obtained adsorbs ammonia, and adsorption time is generally 5min ~ 30min.In step (7), the described alkaline solution containing ammonium is one or more in ammonia, sal volatile, ammonium bicarbonate soln.
In step (7), described ammonia can adopt pure ammonia, it would however also be possible to employ the gaseous mixture containing ammonia, and in mixing gas except ammonia, other is one or more in noble gas such as nitrogen, argon etc..
In step (8), described heteropoly acid is one or more in phosphotungstic acid, silico-tungstic acid, phosphomolybdic acid.
Can also adding mesopore molecular sieve, one or more in such as SBA-15, SBA-3, MCM-41 etc. in described silica support, molecular sieve weight content in the carrier, below 10%, is generally 1% ~ 8%.Mesopore molecular sieve can introduce before silicon oxide plastic, it is also possible to introduces in plastic process, it is also possible to introduces after silicon oxide plastic, it is also possible in silica support forming process, kneading introduces.
Described catalyst A and the admission space of catalyst B are than for 4:1 ~ 1:4.
The method of preparing ethylene by dehydrating ethanol of the present invention, adopts fixed-bed process, and reaction condition is as follows: mass space velocity 0.5h-1~15.0h-1, reaction temperature 260 DEG C ~ 400 DEG C.
Compared with prior art, the invention have the advantages that
In the inventive method, the catalyst B adopted, it is particularly well-suited to low-concentration ethanol raw material dehydration ethylene reaction produced, and low temperature active is high, it is seated in the downstream of catalyst A, the negative effect that bed temperature reduces and in raw material, catalyst system is brought by water content increase can be obviously improved, make catalyst A and catalyst B cooperate and give full play to respective advantage, catalyst entirety is made to have higher activity, while selectivity and coking resistivity, improve the stability of catalyst, the service life of catalyst can be extended, the combined reaction performance making reaction system improves, there is higher product yield.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in detail.In the present invention, wt% is mass fraction.
Embodiment 1
1, catalyst preparing:
Prepared by catalyst A
(1) preparation of carrier:
4.8g citric acid and 15.0g Macrogol 600 are joined in deionized water, it is made into mixed solution, it is subsequently adding 37.8mL tetraethyl orthosilicate, after stirring, join prepare in the aluminium oxide of compression molding, 2h is stirred at 60 DEG C, then stir at 80 DEG C to becoming gel, aging 8h at 40 DEG C, then at 110 DEG C of dry 8h, at 550 DEG C of roasting 3h, obtain the alumina support of coated with silica, wherein silicon oxide accounts for the mol ratio of the 12% of vehicle weight, citric acid and silicon oxide is 0.15, and the mol ratio of Macrogol 600 and silicon oxide is 0.15.
(2) preparation of catalyst: catalyst adopts supersaturation infusion process to prepare, and step is as follows:
8.9g boric acid and 12.5g phosphotungstic acid are joined in deionized water, is configured to mixed solution；The carrier prepared is joined in mixed solution, stirs at 60 DEG C to solution and be evaporated；Then solid dry 8h, the roasting 3h at 350 DEG C at 110 DEG C that will obtain, prepares H3PW12O40-B2O3/Al2O3-SiO2Catalyst, wherein B2O3Content is 5wt%, H3PW12O40Content is 12wt%, SiO2Content is the 12wt% of the alumina support of coated with silica.
Prepared by catalyst B
(1) preparation of carrier:
Weigh 145.8g cetyl trimethylammonium bromide and 205g citric acid is made into mixed solution, 302mL tetraethyl orthosilicate is joined in mixed solution, stirring 2h, then stirs to becoming gel, by gel aging 12h at 40 DEG C at 70 DEG C, then dry 8h at 110 DEG C, through compression molding, at 580 DEG C of roasting 3h, obtain silica support, wherein cetyl trimethylammonium bromide is 0.3 with the mol ratio of silicon oxide, and the mol ratio of citric acid and silicon oxide is 0.8.Support is: specific surface area is 525m2/ g, pore volume is 0.64mL/g, and average pore diameter is 4.9nm.
(2) preparation of catalyst:
27.2g nickel nitrate is dissolved in deionized water, join in 81g silica support, stir at 70 DEG C to solution and be evaporated, by the solid that obtains at 110 DEG C of dry 8.0h, then at 400 DEG C of roasting 3.0h, prepare catalyst precarsor A, it is then added in autoclave, 450 DEG C it are warming up under hydrogen atmosphere, 4h is processed under 0.3MPa, it is down to reaction temperature, adding 400g mass concentration is the sorbitol solution of 20%, then Hydrogen Vapor Pressure is regulated to 3MPa, 3h is reacted at 260 DEG C, after reaction terminates, by catalyst filtration out, carrier surface it is dried to without liquid phase at 40 DEG C；It is then added to containing in 38.9g Fructus Citri Limoniae aqueous acid, stirs at 70 DEG C to solution and be evaporated；The material obtained joins dipping 10min in sal volatile, dry at 60 DEG C after filtration；It is then added in the aqueous solution containing 12.4g phosphotungstic acid, stirs at 70 DEG C to solution and be evaporated；By the solid that obtains at 110 DEG C of dry 8.0h, then at 500 DEG C of roasting 3.0h, prepare (NH4)0.5H2.5PW12O40-NiO/SiO2Catalyst, wherein NiO content is 7wt%, (NH4)0.5H2.5PW12O40Content is 12wt%.
2, the evaluation of catalyst:
Evaluating catalyst carries out in atmospheric fixed bed tubular reactor, and raw material is 95wt% ethanol water, first contacts with catalyst A, then contacts with catalyst B again, and wherein the admission space of catalyst A and catalyst B ratio is for 3:1, common 20mL, mass space velocity 3h-1, reaction temperature 360 DEG C.Before reaction, catalyst is at N2Activating 2h in 400 DEG C under protection, be then down to after reaction temperature starts to react 200 hours, product is analyzed by gas chromatogram, calculates ethanol conversion and ethylene selectivity, and result is in Table 1.
Embodiment 2
Select in embodiment 1 catalyst A and B admission space ratio for 1:1, mass space velocity 4h-1, reaction temperature 360 DEG C, other appreciation condition is constant, and ethanol conversion and ethylene selectivity result are in Table 1.
Embodiment 3
The preparation of catalyst A:
(1) preparation of carrier:
7.4g citric acid and 13.9g PEG400 are joined in deionized water, it is made into mixed solution, it is subsequently adding 43.8mL tetraethyl orthosilicate, after stirring, join prepare in the aluminium oxide of compression molding, 2h is stirred at 60 DEG C, then stir at 80 DEG C to becoming gel, aging 8h at 40 DEG C, then at 110 DEG C of dry 8h, at 550 DEG C of roasting 3h, obtain the alumina support of coated with silica, wherein silicon oxide accounts for the mol ratio of the 15% of vehicle weight, citric acid and silicon oxide is 0.2, and the mol ratio of PEG400 and silicon oxide is 0.18.
(2) preparation of catalyst: catalyst adopts supersaturation infusion process to prepare, and step is as follows:
10.6g boric acid and 15.6g phosphotungstic acid are joined in deionized water, is configured to mixed solution；The carrier prepared is joined in mixed solution, 60oStir under C to solution and be evaporated；Then by the solid that obtains 110oDry 8h under C, 350oRoasting 3h under C, prepares H3PW12O40-B2O3/Al2O3-SiO2Catalyst, wherein B2O3Content is 6wt%, H3PW12O40Content is 15wt%, SiO2Content is the 15wt% of the alumina support of coated with silica.
The preparation of catalyst B:
(1) preparation of carrier:
Weigh 200g cetyl trimethylammonium bromide and 105.7g citric acid is made into mixed solution, 250mL tetraethyl orthosilicate is joined in mixed solution, stirring 2h, then stirs to becoming gel, by gel aging 12h at 40 DEG C at 70 DEG C, then dry 8h at 110 DEG C, through compression molding, at 600 DEG C of roasting 3h, obtain silica support, wherein cetyl trimethylammonium bromide is 0.5 with the mol ratio of silicon oxide, and the mol ratio of citric acid and silicon oxide is 0.5.Support is: specific surface area is 570m2/ g, pore volume is 0.72mL/g, and average pore diameter is 5.1nm.
(2) preparation of catalyst:
35.0g nickel nitrate is dissolved in deionized water, join in 73g silica support, stir at 70 DEG C to solution and be evaporated, by the solid that obtains at 110 DEG C of dry 8.0h, then at 400 DEG C of roasting 3.0h, prepare catalyst precarsor A, it is then added in autoclave, 450 DEG C it are warming up under hydrogen atmosphere, 4h is processed under 0.3MPa, it is down to reaction temperature, adding 400g mass concentration is the sorbitol solution of 20%, then Hydrogen Vapor Pressure is regulated to 3MPa, 2h is reacted at 300 DEG C, after reaction terminates, by catalyst filtration out, carrier surface it is dried to without liquid phase at 40 DEG C；It is then added to containing in 58.4g Fructus Citri Limoniae aqueous acid, stirs at 70 DEG C to solution and be evaporated；The material obtained joins dipping 10min in sal volatile, dry at 60 DEG C after filtration；It is then added in the aqueous solution containing 18.7g phosphotungstic acid, stirs at 70 DEG C to solution and be evaporated；By the solid that obtains at 110 DEG C of dry 8.0h, then at 500 DEG C of roasting 3.0h, prepare (NH4)0.5H2.5PW12O40-NiO/SiO2Catalyst, wherein NiO content is 9wt%, (NH4)0.5H2.5PW12O40Content is 18wt%.
Catalyst A and B admission space are than for 1:2, mass space velocity 6h-1, reaction temperature 350 DEG C, other appreciation condition is constant, and ethanol conversion and ethylene selectivity result are in Table 1.
Embodiment 4
In embodiment 1, changing phosphotungstic acid into silico-tungstic acid, all the other are with embodiment 1, and gained catalyst A is H4SiW12O40-B2O3/Al2O3-SiO2Catalyst, wherein B2O3Content is 5wt%, H4SiW12O40Content is 10wt%.Catalyst B is (NH4)0.5H3.5SiW12O40-NiO/SiO2Catalyst, wherein NiO content is 7wt%, (NH4)0.5H3.5SiW12O40Content is 12wt%.
The evaluation of catalyst with embodiment 1, ethanol conversion and ethylene selectivity result in Table 1.
Comparative example 1
Be used alone in embodiment 1 catalyst A, the evaluation of catalyst with embodiment 1, ethanol conversion and ethylene selectivity result in Table 1.
The evaluation result of each example of table 1
Claims (11)
1. a method for preparing ethylene by dehydrating ethanol, including at least two beds and catalyst A and catalyst B, wherein ethanol raw material first contacts with catalyst A, then contacts with catalyst B again；
Catalyst A's is composed as follows: active component is heteropoly acid, auxiliary agent is boron oxide, wherein alumina carrier surface coated silica, the weight of silicon dioxide accounts for the 5% ~ 20% of the carrying alumina body weight of coated with silica, with the weight of catalyst for benchmark, the content of heteropoly acid is 3% ~ 25%, and the content that auxiliary agent is counted with oxide is for 2% ~ 8%, and the content of the alumina support of coated with silica is 67% ~ 95%；
Catalyst B's is composed as follows:
Active component is that ammonium heteropoly acids is shown in formula (1), and auxiliary agent is nickel oxide, and carrier is silicon oxide；With the weight of catalyst for benchmark, the content of ammonium heteropoly acids is 8% ~ 35%, and the content that auxiliary agent is counted with oxide is for 3% ~ 18%, and the content of carrier is 47% ~ 89%；
Hm(NH4)nYX12O40(1)
Wherein X represents W or Mo, Y and represents Si or P；When Y represents Si, m+n=4, n value is 0.1 ~ 0.5；When Y represents P, m+n=3, n value is 0.1 ~ 0.5.
2. in accordance with the method for claim 1, it is characterized in that: described catalyst A, with the weight of catalyst for benchmark, the content of heteropoly acid is 5% ~ 20%, the content that auxiliary agent is counted with oxide is for 2% ~ 8%, and the content of the alumina support of coated with silica is 72% ~ 93%.
3. in accordance with the method for claim 1, it is characterised in that: described catalyst B, with the weight of catalyst for benchmark, the content of ammonium heteropoly acids is 12% ~ 30%, and the content that auxiliary agent is counted with oxide is for 5% ~ 15%, and the content of carrier is 55% ~ 83%.
4. in accordance with the method for claim 1, it is characterised in that: described catalyst B, with the weight of catalyst for benchmark, the content of ammonium heteropoly acids is 18% ~ 30%, and the content that auxiliary agent is counted with oxide is for 5% ~ 15%, and the content of carrier is 55% ~ 77%.
5. in accordance with the method for claim 1, it is characterised in that: in described catalyst A, the weight of silicon dioxide accounts for the 8% ~ 18% of the carrying alumina body weight of coated with silica.
6. in accordance with the method for claim 1, it is characterised in that: in described catalyst B, the character of silica support is as follows: specific surface area is 500 ~ 820m2/ g, pore volume is 0.62 ~ 0.92mL/g, and average pore diameter is 4.6 ~ 6.6nm.
7. according to the arbitrary described method of claim 1 ~ 6, it is characterized in that: in described catalyst A, heteropoly acid is the distribution in uniform type on the alumina support of coated with silica, and in described catalyst B, ammonium heteropoly acids is distributed on silica support and is distributed in eggshell type.
8. according to the arbitrary described method of claim 1 ~ 6, it is characterised in that: in catalyst B, the weight content of ammonium heteropoly acids is not less than in catalyst A the weight content of heteropoly acid.
9. in accordance with the method for claim 1, it is characterised in that: in described catalyst B, adding one or more in mesoporous molecular sieve SBA-15, SBA-3, MCM-41 in silica support, molecular sieve weight content in the carrier is below 10%.
10. in accordance with the method for claim 1, it is characterised in that: described catalyst A and the admission space of catalyst B are than for 4:1 ~ 1:4.
11. in accordance with the method for claim 1, it is characterised in that: adopting fixed-bed process, the reaction condition of preparing ethylene by dehydrating ethanol is as follows: mass space velocity 0.5h-1~15.0h-1, reaction temperature 260 DEG C ~ 400 DEG C.
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| CN109926074A (en) * | 2017-12-15 | 2019-06-25 | 中国石油化工股份有限公司 | Hydrocracking catalyst and preparation method thereof |
| CN109926074B (en) * | 2017-12-15 | 2021-08-06 | 中国石油化工股份有限公司 | Hydrocracking catalyst and preparation method thereof |
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| CN105712822B (en) | 2018-01-16 |
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