CN104353487B - A kind of C8 arene isomerization catalysts and its application - Google Patents
A kind of C8 arene isomerization catalysts and its application Download PDFInfo
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Abstract
The invention discloses a kind of C8 arene isomerization catalysts, including carrier and the platinum being carried on the carrier, the quality of the platinum is the 0.25% of carrier quality, and the carrier includes 50wt% aluminum oxide, the 6wt%~9wt% molecular sieves of the EU 1 and 41wt%~44wt% molecular sieves of ZSM 5；The SiO of the molecular sieves of EU 12/Al2O3Mol ratio is 45, the SiO of the molecular sieves of ZSM 52/Al2O3Mol ratio is 260；In addition, the application present invention also offers the catalyst in the reaction of C8 aromatics isomerizations.When the catalyst of the present invention is used to be catalyzed the reaction of C8 aromatics isomerizations, the concentration of paraxylene with higher conversion of ethylbenzene and Selectivity for paraxylene, and is able to maintain that relatively low C8 aromatic hydrocarbons loss amounts close to thermodynamical equilibrium concentration in product.
Description
Technical field
The invention belongs to petrochemical catalyst technical field, and in particular to a kind of C8 arene isomerization catalysts and its should
With.
Background technology
It is different with dividing that C8 aromatic hydrocarbons refers to four kinds of paraxylene (PX), meta-xylene (MX), ortho-xylene (OX) and ethylo benzene (EB)
The mixture of structure body, the main source of C8 aromatic hydrocarbons is catalytic reforming in oil secondary operation and the by-product of naphtha thermal cracking
Thing, or toluene disproportionation or transalkylation etc..Due to ethylbenzene boiling point and dimethylbenzene boiling point closely, according to efficient
Rectifying or adsorbing separation are directly separated the ethylbenzene in dimethylbenzene, and cost is very high.Because the separation of ethylbenzene is extremely difficult and cost is high,
Under normal circumstances, dimethylbenzene is converted the ethylbenzene into while oil company's multiselect is used in C8 aromatics isomerizations.
In order that ethylbenzene conversion and the reaction of C8 aromatics isomerizations are completed, with the solid acid catalysis containing hydrogenation component simultaneously
Agent converts the ethylbenzene into dimethylbenzene, and the method that xylene isomerization is turned into thermodynamical equilibrium mixture increasingly draws attention.
The patent of present ethylbenzene conversion aspect is a lot, and the metal constituent element used in catalyst is essentially all noble metal platinum, though
It is so different in content and on mode of loading, but do not have too big difference, and the molecular sieve used in each catalyst is sour
Property component is then had any different：The molecular sieve being converted into for ethylbenzene in the technique of dimethylbenzene, the I-400 catalyst of Uop Inc. is UZM
Molecular sieve in series, the OPARIS catalyst of IFP is serial for EUO, in Shi Keyuan SKI-400 catalyst
Molecular sieve for MOR series.
Ethylbenzene isomery needs VIII noble metal to exist into dimethylbenzene, is traditionally inclined to use modenite and ZSM-5 boilings
Stone.A kind of isomerization catalyst for C8 aromatic fractions is described in patent US150292, is 5~10 from silica alumina ratio
Modenite and a kind of binding agent, and one or both of elements platinum and palladium containing group VIII, while in catalyst
Contain one or both of indium and tin.Patent US4482773 selects ZSM-5 zeolite, and patent EP458378 describes a kind of C8
Arene isomerization catalyst, it is existing containing platinum active component and a kind of H type modenites containing 2wt%~3wt% alkali metal
Catalyst generally all have that target product selectivity is relatively low, conversion of ethylbenzene is relatively low, and disproportionated reaction etc. is seriously asked
Topic.
The content of the invention
In view of the above-mentioned deficiencies in the prior art, the technical problem to be solved by the present invention is that it is different to provide a kind of C8 aromatic hydrocarbons
Structure catalyst.When the catalyst is used to be catalyzed the reaction of C8 aromatics isomerizations, the concentration of paraxylene is close to heating power in product
Equilibrium concentration is learned, reaction has higher conversion of ethylbenzene and Selectivity for paraxylene, and is able to maintain that relatively low C8 aromatic hydrocarbons is damaged
Vector.
In order to solve the above technical problems, the technical solution adopted by the present invention is：A kind of C8 arene isomerization catalysts, including
Carrier and the platinum being carried on the carrier, the quality of the platinum are the 0.25% of the carrier quality, and the carrier includes
50wt% aluminum oxide, 6wt%~9wt% EU-1 molecular sieves and 41wt%~44wt% ZSM-5 molecular sieve；The EU-1
The SiO of molecular sieve2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260, ZSM-5 molecular sieve
Crystallite dimension be not more than 100nm.
A kind of above-mentioned C8 arene isomerization catalysts, it is characterised in that aluminum oxide of the carrier including 50wt%,
7wt%~8wt% EU-1 molecular sieves and 42wt%~43wt% ZSM-5 molecular sieve.
A kind of above-mentioned C8 arene isomerization catalysts, it is characterised in that aluminum oxide of the carrier including 50wt%,
7.6wt% EU-1 molecular sieves and 42.4wt% ZSM-5 molecular sieve.
Further, the application present invention also offers a kind of above-mentioned catalyst in the reaction of C8 aromatics isomerizations, it is special
Levy and be, the method for the isomerization reaction is：By catalyst load fixed bed reactors in, reaction temperature be 340 DEG C~
350 DEG C, reaction pressure is 0.7MPa~0.8MPa, and the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.3~2.5, and mass space velocity is 4h-1~
6h-1Under conditions of, catalysis C8 aromatics isomerization reactions.
Above-mentioned application, it is characterised in that the reaction temperature is 350 DEG C, reaction pressure is 0.7MPa, hydrogen and C8 virtues
The mol ratio of hydrocarbon is 2.5, and mass space velocity is 4h-1。
The preparation method of catalyst of the present invention comprises the following steps：
Step one：Mixture is obtained after EU-1 molecular sieves, ZSM-5 molecular sieve and aluminum oxide are well mixed, will be described mixed
Compound and dust technology dried after kneading, extruded moulding, and 4h~5h is then calcined under the conditions of 540 DEG C~560 DEG C, is carried
Body；The mass ratio of the mixture and dust technology is 100：(55~65), the mass concentration of the dust technology for 0.4%~
0.6%；
Exchanged Step 2: carrier described in step one is placed in ammonium nitrate solution and carries out 3~4 secondary ions, per secondary ion
The temperature of exchange is 80 DEG C~90 DEG C, and the time is 1.5h~2.5h；The molar concentration of the ammonium nitrate solution be 0.8mol/L~
1.2mol/L；
Step 3: the carrier in step 2 after ion exchange is placed in into the medium volume impregnation 12h~14h of chloroplatinic acid, obtain
To catalyst precursor；
Step 4: catalyst precursor described in step 3 is dried, by dried catalyst precursor 480
DEG C~520 DEG C under the conditions of be calcined 2.5h~3.5h, then by the catalyst precursor after roasting in hydrogen atmosphere, 380 DEG C~
4h~5h is reduced under conditions of 420 DEG C, C8 arene isomerization catalysts are obtained after cooling.
The present invention has advantages below compared with prior art：
1st, when catalyst of the invention is used to be catalyzed the reaction of C8 aromatics isomerizations, in product the concentration of paraxylene close to
Thermodynamical equilibrium concentration, reaction has higher conversion of ethylbenzene and Selectivity for paraxylene, and is able to maintain that relatively low C8 virtues
Hydrocarbon loss amount.
2nd, there is at a relatively high commercial significance when catalyst of the invention is used in the reaction of C8 aromatics isomerizations, to diformazan
Benzene is important isomers, and paraxylene can be made by meta-xylene isomerization, in C8 aromatic hydrocarbons, because the boiling of ethylbenzene
The boiling point of point and dimethylbenzene is difficult closely to separate ethylbenzene, can solve the problem that this is asked using the catalyst of the present invention
Topic, while the production paraxylene of high selectivity, because ethylbenzene can react generation on the acidic site of EU-1 molecular sieves
Dimethylbenzene, then ZSM-5 molecular sieve of the dimethylbenzene Jing Guo high selectivity generate paraxylene to greatest extent, due to ZSM-5 point
Sub- sifter device has higher SiO2/Al2O3Mol ratio and Nano Particle, can make dimethylbenzene avoid generation two in isomerization process
Secondary response, keeps having high Selectivity for paraxylene while ethylbenzene high conversion again, and product can be avoided to occur two
Secondary response, maintains high C8 aromatics yields, obtains preferable technique effect.
3rd, the EU-1 molecular sieves SiO that the present invention is used2/Al2O3Mol ratio is 45, mild acidity, thus in catalytic reaction mistake
Coking is not susceptible in journey, and cracking side reaction is few, isomerization reaction effect is good；ZSM-5 molecular sieve is nano crystals,
SiO2/Al2O3Mol ratio is 260, and relative with higher Bronst acid amounts, conversion of ethylbenzene is high, the crystal grain of ZSM-5 molecular sieve
Size is not more than 100nm, and causing ethylbenzene to be converted into after dimethylbenzene can quickly spread, and is not easy to occur coking and cracking is secondary anti-
Should, so the selectivity of catalyst of the present invention is good, long lifespan.
Below by drawings and examples, technical scheme is described in further detail.
Brief description of the drawings
Fig. 1 is the XRD spectra of the EU-1 molecular sieves that the conventional method that provides is prepared in the specific embodiment of the invention.
Fig. 2 is the SEM photograph of the EU-1 molecular sieves that the conventional method that provides is prepared in the specific embodiment of the invention.
Fig. 3 is the XRD spectrums of the ZSM-5 molecular sieve that the conventional method that provides is prepared in the specific embodiment of the invention
Figure.
Fig. 4 is that the SEM of the ZSM-5 molecular sieve that the conventional method that provides is prepared in the specific embodiment of the invention shines
Piece.
Embodiment
SiO used in the present invention2/Al2O3EU-1 molecular sieve and SiO of the mol ratio for 452/Al2O3Mol ratio be 260 and
The ZSM-5 molecular sieve that crystallite dimension is not more than 100nm can be obtained using customary preparation methods.
EU-1 molecular sieves used can be prepared using following conventional method in the present invention：
Step 1: taking Ludox 203.9g, sodium metaaluminate 6.2g, distilled water 38g obtain mixed liquor after being well mixed；Institute
State SiO in Ludox2Mass concentration be 26.17%, Na in the sodium metaaluminate2O mass concentration is 304.9565g/L,
Al2O3Mass concentration be 370.1874g/L；
Step 2: taking sodium hydroxide 9.4g, 1,6- dibromo-hexane 70.6g, trimethylamine solution 106.1g, distilled water 20g, mix
Emulsion is obtained after closing stirring；The quality purity of the sodium hydroxide is 96%, and the quality purity of 1, the 6- dibromo-hexanes is
98.5%, the mass concentration of the trimethylamine solution is 33.0%；
Step 3: emulsion described in step 2 is added to described in step one in mixed liquor, it is stirred vigorously and uniformly obtains
Mixture, the mixture is fitted into autoclave, and crystallization 48 hours, takes out after natural cooling under the conditions of temperature is 180 DEG C
Crystallization liquid, the crystallization liquid is separated successively, filtered and carrying out washing treatment, product is obtained；
Step 4: product described in step 3 is placed in baking oven, 12h is dried under conditions of 110 DEG C, EU-1 points are obtained
Sodium content in son sieve, the EU-1 molecular sieves is the SiO of 2.1%, the EU-1 molecular sieves of its butt weight2/Al2O3Mol ratio
For 45 (x-ray fluorescence elementary analyses), pore volume is 0.19m3, specific surface area is 347m2/g。
Fig. 1 is the XRD spectra for the EU-1 molecular sieves that above-mentioned preparation method is obtained, and Fig. 2 is the EU- that above-mentioned preparation method is obtained
The SEM photograph of 1 molecular sieve, can be seen that EU-1 molecular sieves have crystallinity height, crystallite dimension small and uniform from Fig. 1 and Fig. 2
Feature.
ZSM-5 molecular sieve used can be obtained using following customary preparation methods in the present invention：
Step 1: taking silochrom 181.39g, sodium metaaluminate 4.2g, tetraethyl ammonium hydroxide 36.82g, sodium hydroxide
1.3g, distilled water 90g, mixture is obtained after being well mixed；SiO in the silochrom2Mass concentration be 99.3%, it is described
Na in sodium metaaluminate2O mass concentration is 304.9565g/L, Al2O3Mass concentration be 370.1874g/L, the tetraethyl
The mass concentration of ammonium hydroxide is 40%, and the quality purity of the sodium hydroxide is 96%；
Step 2: mixture described in step one is fitted into autoclave, the crystallization 48 hours under the conditions of 150 DEG C of temperature,
Crystallization liquid is taken out after natural cooling, the crystallization liquid is sequentially passed through into separation, filtering and carrying out washing treatment, product is obtained；
Step 3: product described in step 2 is placed in baking oven, 12h is dried under the conditions of 110 DEG C, ZSM-5 points are obtained
Sodium content in son sieve, the ZSM-5 molecular sieve is the 1.8% of its butt weight, and the silica alumina ratio of ZSM-5 molecular sieve is 260
(x-ray fluorescence elementary analysis), pore volume is 0.28m3, specific surface area is 567m2/g。
Fig. 3 is the XRD spectra for the ZSM-5 molecular sieve that above-mentioned preparation method is obtained, and the above-mentioned preparation methods of Fig. 4 are obtained
The SEM photograph of ZSM-5 molecular sieve, can be seen that ZSM-5 molecular sieve has crystallinity height, crystallite dimension small (no from Fig. 3 and Fig. 4
More than 100nm) and it is uniform the characteristics of.
C8 arene isomerization catalysts of the present invention are described according to 1~embodiment of embodiment 5：
Embodiment 1
The catalyst of the present embodiment includes carrier and the platinum being carried on carrier, and the quality of the platinum is carrier quality
0.25%, the carrier includes 50wt% aluminum oxide, 7.6wt% EU-1 molecular sieves and 42.4wt% ZSM-5 molecular sieve；
The SiO of the EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260,
The crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
The preparation method of the present embodiment catalyst comprises the following steps：
Step one：Mixture is obtained after EU-1 molecular sieves, ZSM-5 molecular sieve and aluminum oxide are well mixed, will be described mixed
Compound and dust technology dried after kneading, extruded moulding, are then calcined 4.5h under the conditions of 550 DEG C, are obtained carrier；It is described mixed
The mass ratio of compound and dust technology is 100：60, the mass concentration of the dust technology is 0.5%；
4 secondary ion exchanges, each ion exchange are carried out Step 2: carrier described in step one is placed in ammonium nitrate solution
Temperature be 85 DEG C, the time is 2h；The molar concentration of the ammonium nitrate solution is 1.0mol/L；
Step 3: carrier after ion exchange is placed in into the medium volume impregnation 13h of chloroplatinic acid, complex catalyst precursor is obtained
Body；
Step 4: catalyst precursor described in step 3 is dried, by dried catalyst precursor 500
3h is calcined under the conditions of DEG C, then by the catalyst precursor after roasting in hydrogen atmosphere, 4.5h is reduced under conditions of 400 DEG C,
C8 arene isomerization catalysts are obtained after cooling.
Embodiment 2
The catalyst of the present embodiment includes carrier and the platinum being carried on carrier, and the quality of the platinum is carrier quality
0.25%, the carrier includes 50wt% aluminum oxide, 7wt% EU-1 molecular sieves and 43wt% ZSM-5 molecular sieve；It is described
The SiO of EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260, ZSM-5 points
The crystallite dimension of son sieve is not more than 100nm.
The preparation method be the same as Example 1 of the present embodiment catalyst.
Embodiment 3
The catalyst of the present embodiment includes carrier and the platinum being carried on carrier, and the quality of the platinum is carrier quality
0.25%, the carrier includes 50wt% aluminum oxide, 8wt% EU-1 molecular sieves and 42wt% ZSM-5 molecular sieve；It is described
The SiO of EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260, ZSM-5 points
The crystallite dimension of son sieve is not more than 100nm.
The preparation method of the present embodiment catalyst comprises the following steps：
Step one：Mixture is obtained after EU-1 molecular sieves, ZSM-5 molecular sieve and aluminum oxide are well mixed, will be described mixed
Compound and dust technology dried after kneading, extruded moulding, are then calcined 4h under the conditions of 560 DEG C, are obtained carrier；The mixing
The mass ratio of thing and dust technology is 100：65, the mass concentration of the dust technology is 0.4%；
3 secondary ion exchanges, each ion exchange are carried out Step 2: carrier described in step one is placed in ammonium nitrate solution
Temperature be 90 DEG C, the time is 2.5h；The molar concentration of the ammonium nitrate solution is 1.2mol/L；
Step 3: carrier after ion exchange is placed in into the medium volume impregnation 14h of chloroplatinic acid, complex catalyst precursor is obtained
Body；
Step 4: catalyst precursor described in step 3 is dried, by dried catalyst precursor 480
3.5h is calcined under the conditions of DEG C, then by the catalyst precursor after roasting in hydrogen atmosphere, 5h is reduced under conditions of 380 DEG C,
C8 arene isomerization catalysts are obtained after cooling.
Embodiment 4
The catalyst of the present embodiment includes carrier and the platinum being carried on carrier, and the quality of the platinum is carrier quality
0.25%, the carrier includes 50wt% aluminum oxide, 6wt% EU-1 molecular sieves and 44wt% ZSM-5 molecular sieve；It is described
The SiO of EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260, ZSM-5 points
The crystallite dimension of son sieve is not more than 100nm.
The preparation method be the same as Example 3 of the present embodiment catalyst.
Embodiment 5
The catalyst of the present embodiment includes carrier and the platinum being carried on carrier, and the quality of the platinum is carrier quality
0.25%, the carrier includes 50wt% aluminum oxide, 9wt% EU-1 molecular sieves and 41wt% ZSM-5 molecular sieve；It is described
The SiO of EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260, ZSM-5 points
The crystallite dimension of son sieve is not more than 100nm.
The preparation method of the present embodiment catalyst comprises the following steps：
Step one：Mixture is obtained after EU-1 molecular sieves, ZSM-5 molecular sieve and aluminum oxide are well mixed, will be described mixed
Compound and dust technology dried after kneading, extruded moulding, are then calcined 5h under the conditions of 540 DEG C, are obtained carrier；The mixing
The mass ratio of thing and dust technology is 100：55, the mass concentration of the dust technology is 0.6%；
4 secondary ion exchanges, each ion exchange are carried out Step 2: carrier described in step one is placed in ammonium nitrate solution
Temperature be 80 DEG C, the time is 1.5h；The molar concentration of the ammonium nitrate solution is 0.8mol/L；
Step 3: carrier after ion exchange is placed in into the medium volume impregnation 12h of chloroplatinic acid, complex catalyst precursor is obtained
Body；
Step 4: catalyst precursor described in step 3 is dried, by dried catalyst precursor 520
2.5h is calcined under the conditions of DEG C, then by the catalyst precursor after roasting in hydrogen atmosphere, 4h is reduced under conditions of 420 DEG C,
C8 arene isomerization catalysts are obtained after cooling.
The application of C8 arene isomerization catalysts of the present invention is described according to 6~embodiment of embodiment 8：
Embodiment 6
Application of the catalyst of 1~embodiment of embodiment 5 in the reaction of C8 aromatics isomerizations, the side of the isomerization reaction
Method is：Catalyst is loaded in fixed bed reactors, is 350 DEG C in reaction temperature, reaction pressure is 0.7MPa, hydrogen and C8 virtues
The mol ratio of hydrocarbon is 2.5, and mass space velocity is 4h-1Under conditions of, catalysis C8 aromatics isomerization reactions；Contain carbon in the C8 aromatic hydrocarbons
Eight alkanes, the cycloalkane of carbon eight, meta-xylene, ortho-xylene and ethylbenzene (the wherein quality of the alkane of carbon eight and the cycloalkane of carbon eight
Percentage composition sum is 7.8733%, and the weight/mass percentage composition of meta-xylene is 53.0043%, and the quality percentage of ortho-xylene contains
Measure as 20.4355%, 18.6869%) weight/mass percentage composition of ethylbenzene is.
The reaction result reacted using catalyst C8 aromatics isomerizations of the present invention is as shown in table 1.
The reaction result that table 1 is reacted using catalyst C8 aromatics isomerizations of the present invention
The computational methods of paraxylene equilibrium concentration, conversion of ethylbenzene and C8 hydrocarbon yields are respectively in table 1：
In above formula, w (EB)FFor the mass fraction of ethylbenzene in raw material C8 aromatic hydrocarbons, w (X)FFor dimethylbenzene in raw material C8 aromatic hydrocarbons
Mass fraction, w (PX)pFor the mass fraction of paraxylene in product,For the alkane of carbon eight in raw material C8 aromatic hydrocarbons
With the mass fraction sum of the cycloalkane of carbon eight；w(MX)pFor the mass fraction of meta-xylene in product, w (OX)pFor neighbour two in product
The mass fraction of toluene, w (EB)pFor the mass fraction of ethylbenzene in product, w (X)pFor the mass fraction of dimethylbenzene in product,For the mass fraction sum of the alkane of carbon in product eight and the cycloalkane of carbon eight.
Embodiment 7
Application of the catalyst of embodiment 1 in catalysis C8 aromatics isomerizations reaction, the method for the isomerization reaction is：
Catalyst is loaded in fixed bed reactors, is 340 DEG C in reaction temperature, reaction pressure is 0.8MPa, hydrogen and C8 aromatic hydrocarbons
Mol ratio is 2.3, and mass space velocity is 6h-1Under conditions of, catalysis C8 aromatics isomerization reactions；The composition and content of the C8 aromatic hydrocarbons
It is identical with implementing 6.
Embodiment 8
Using application of the catalyst of embodiment 1 in catalysis C8 aromatics isomerizations reaction, the side of the isomerization reaction
Method is：Catalyst is loaded in fixed bed reactors, is 345 DEG C in reaction temperature, reaction pressure is 0.75MPa, hydrogen and C8
The mol ratio of aromatic hydrocarbons is 2.4, and mass space velocity is 5h-1Under conditions of, catalysis C8 aromatics isomerization reactions；The composition of the C8 aromatic hydrocarbons
And content is identical with implementing 6.
The reaction result of 7~embodiment of embodiment 8 is as shown in table 2.
The reaction result of the 7~embodiment of embodiment 8 of table 2
It is right in paraxylene equilibrium concentration, the computational methods of conversion of ethylbenzene and C8 hydrocarbon yields and the table 1 of embodiment 6 in table 2
Xylene equilibrium concentration, conversion of ethylbenzene are identical with the computational methods of C8 hydrocarbon yields.
As can be seen from Table 1 and Table 2, when catalyst of the invention is used to be catalyzed the reaction of C8 aromatics isomerizations, in product
The concentration of paraxylene is close to thermodynamical equilibrium concentration, with higher conversion of ethylbenzene and Selectivity for paraxylene, C8 hydrocarbon
Yield is very high to be shown to there occurs few side reaction in isomerization reaction, so the active height of the catalyst of the present invention,
The characteristics of selective good and long lifespan.
It is described above, only it is presently preferred embodiments of the present invention, not the present invention is imposed any restrictions, it is every according to the present invention
Any simple modification, change and equivalent structure change that technical spirit is made to above example, still fall within skill of the present invention
In the protection domain of art scheme.
Claims (3)
1. a kind of C8 arene isomerization catalysts, including carrier and the platinum being carried on carrier, the quality of the platinum is carrier matter
The 0.25% of amount, the carrier includes 50wt% aluminum oxide, 7.6wt% EU-1 molecular sieves and 42.4% ZSM-5 molecules
Sieve；The SiO of the EU-1 molecular sieves2/Al2O3Mol ratio is 45, the SiO of the ZSM-5 molecular sieve2/Al2O3Mol ratio is 260,
The crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
2. a kind of application of catalyst as claimed in claim 1 in the reaction of C8 aromatics isomerizations, it is characterised in that the isomery
Changing the method reacted is：Catalyst is loaded in fixed bed reactors, is 340 DEG C~350 DEG C in reaction temperature, reaction pressure is
0.7MPa~0.8MPa, the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.3~2.5, and mass space velocity is 4h-1~6h-1Under conditions of, urge
Change the reaction of C8 aromatics isomerizations.
3. according to the application described in claim 2, it is characterised in that the reaction temperature is 350 DEG C, reaction pressure is
0.7MPa, the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.5, and mass space velocity is 4h-1。
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| SG11201802653RA (en) * | 2015-10-28 | 2018-05-30 | Bp Corp Nurth America Inc | Improved catalyst for ethylbenzene conversion in a xylene isomerrization process |
| CN106669809A (en) * | 2015-11-09 | 2017-05-17 | 中国石油化工股份有限公司 | C8 aromatic hydrocarbon isomerization catalyst, and preparation method and application thereof |
| CN112028730B (en) * | 2019-06-04 | 2023-06-09 | 中国石油化工股份有限公司 | Xylene isomerization method |
| CN111514928B (en) * | 2020-04-29 | 2022-09-20 | 陕西延长石油（集团）有限责任公司 | Catalyst and method for preparing ethylbenzene from synthesis gas and benzene by one-step method |
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| CN101722020A (en) * | 2008-10-15 | 2010-06-09 | 中国石油天然气股份有限公司 | Eutectic zeolite catalyst containing EUO structure and preparation and application thereof |
| CN101898145A (en) * | 2009-05-27 | 2010-12-01 | 中国石油化工股份有限公司 | Alkyl aromatic hydrocarbon isomerization catalyst and preparation method thereof |
| CN102039161A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | C8 arene isomerization catalyst and application thereof |
| CN103120954A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Catalyst for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons |
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