CN104353487A - C8 aromatics isomerization catalyst and application thereof - Google Patents
C8 aromatics isomerization catalyst and application thereof Download PDFInfo
- Publication number
- CN104353487A CN104353487A CN201410667408.4A CN201410667408A CN104353487A CN 104353487 A CN104353487 A CN 104353487A CN 201410667408 A CN201410667408 A CN 201410667408A CN 104353487 A CN104353487 A CN 104353487A
- Authority
- CN
- China
- Prior art keywords
- molecular sieve
- catalyst
- zsm
- carrier
- isomerization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention discloses a C8 aromatics isomerization catalyst which comprises a carrier and platinum supported on the carrier, wherein the mass of platinum is 0.25% of that of the carrier; the carrier comprises 50wt% of aluminum oxide, 6wt%-9wt% of an EU-1 molecular sieve and 41wt%-44wt% of a ZSM-5 molecular sieve; the mole ratio of SiO2 to Al2O3 in the EU-1 molecular sieve is 45, and the mole ratio of SiO2 to Al2O3 of the ZSM-5 molecular sieve is 260. In addition, the invention also discloses application of the catalyst to C8 aromatics isomerization reaction. When the catalyst is used for catalyzing the C8 aromatics isomerization reaction, the concentration of p-xylene in a product is close to thermodynamic equilibrium concentration, and the catalyst has high ethylbenzene conversion rate and high p-xylene selectivity, and can maintain low loss of C8 aromatics.
Description
Technical field
The invention belongs to petrochemical catalyst technical field, be specifically related to a kind of C8 arene isomerization catalyst and application thereof.
Background technology
C8 aromatic hydrocarbons refers to the mixture of paraxylene (PX), meta-xylene (MX), ortho-xylene (OX) and ethylo benzene (EB) four kinds of isomers, the main source of C8 aromatic hydrocarbons is the accessory substance of catalytic reforming in oil secondary operations and naphtha thermal cracking, or toluene disproportionation or transalkylation etc.Due to the boiling point of ethylbenzene and dimethylbenzene boiling point closely, according to the ethylbenzene in highly efficient distilling or the direct separating dimethyl benzene of adsorbing separation, cost is very high.Separation due to ethylbenzene is very difficult and cost is high, under normal circumstances, is dimethylbenzene by ethylbenzene conversion while oil company's multiselect is used in C8 aromatics isomerization.
In order to make the reaction of ethylbenzene conversion and C8 aromatics isomerization complete simultaneously, be dimethylbenzene with the solid acid catalyst containing hydrogenation component by ethylbenzene conversion, and method xylene isomerization being turned to thermodynamical equilibrium mixture draw attention day by day.
The patent of present ethylbenzene conversion aspect is a lot, catalyst metal constituent element used is all noble metal platinum substantially, although on content and mode of loading on different, but too not large difference, each catalyst acidic zeolite component used is then had any different: be the technique of dimethylbenzene for ethylbenzene conversion, molecular sieve in the I-400 catalyst of Uop Inc. is UZM series, molecular sieve in the OPARIS catalyst of IFP is EUO series, and the molecular sieve in the SKI-400 catalyst of Shi Keyuan is MOR series.
Ethylbenzene isomery becomes dimethylbenzene to need VIII noble metal to exist, and is inclined to use modenite and ZSM-5 zeolite traditionally.A kind of isomerization catalyst for C8 aromatic fraction is described in patent US150292, silica alumina ratio is selected to be the modenite of 5 ~ 10 and a kind of binding agent, and containing one or both in the elements platinum of group VIII and palladium, simultaneously in catalyst containing one or both in indium and tin.Patent US4482773 selects ZSM-5 zeolite, patent EP458378 describes a kind of C8 arene isomerization catalyst, 2wt% ~ 3wt% alkali-metal H type modenite is contained containing platinum active component and one, it is relatively low generally all to there is target product selectivity in existing catalyst, the serious problems such as conversion of ethylbenzene is relatively low, disproportionated reaction.
Summary of the invention
Technical problem to be solved by this invention is, for above-mentioned deficiency of the prior art, to provide a kind of C8 arene isomerization catalyst.When this catalyst is used for the reaction of catalysis C8 aromatics isomerization, in product, the concentration of paraxylene is close to thermodynamical equilibrium concentration, and reaction has higher conversion of ethylbenzene and Selectivity for paraxylene, and can maintain lower C8 aromatic hydrocarbons loss amount.
For solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of C8 arene isomerization catalyst, comprise carrier and be carried on the platinum on described carrier, the quality of described platinum is 0.25% of described carrier quality, and described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 6wt% ~ 9wt% and 41wt% ~ 44wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and the crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
Above-mentioned a kind of C8 arene isomerization catalyst, is characterized in that, described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7wt% ~ 8wt% and 42wt% ~ 43wt%.
Above-mentioned a kind of C8 arene isomerization catalyst, is characterized in that, described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7.6wt% and 42.4wt%.
Further, present invention also offers the application of a kind of above-mentioned catalyst in the reaction of C8 aromatics isomerization, it is characterized in that, the method of described isomerization reaction is: loaded by catalyst in fixed bed reactors, it is 340 DEG C ~ 350 DEG C in reaction temperature, 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
-1condition under, catalysis C8 aromatics isomerization react.
Above-mentioned application, is characterized in that, described reaction temperature is 350 DEG C, and reaction pressure is 0.7MPa, and the mol ratio of hydrogen and C8 aromatic hydrocarbons 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: obtain mixture after EU-1 molecular sieve, ZSM-5 molecular sieve and aluminium oxide being mixed, carries out kneading by described mixture and dust technology, and dry after extruded moulding, then roasting 4h ~ 5h under 540 DEG C ~ 560 DEG C conditions, obtains carrier; The mass ratio of described mixture and dust technology is 100:(55 ~ 65), the mass concentration of described dust technology is 0.4% ~ 0.6%;
Step 2, carrier described in step one is placed in ammonium nitrate solution and carries out 3 ~ 4 secondary ions and exchange, the temperature of each ion-exchange is 80 DEG C ~ 90 DEG C, and the time is 1.5h ~ 2.5h; The molar concentration of described ammonium nitrate solution is 0.8mol/L ~ 1.2mol/L;
Step 3, the carrier in step 2 after ion-exchange is placed in the medium volume impregnation 12h ~ 14h of chloroplatinic acid, obtains catalyst precursor;
Step 4, catalyst precursor described in step 3 is carried out drying, by dried catalyst precursor roasting 2.5h ~ 3.5h under 480 DEG C ~ 520 DEG C conditions, then by the catalyst precursor after roasting in hydrogen atmosphere, reduce 4h ~ 5h under the condition of 380 DEG C ~ 420 DEG C, after cooling, obtain C8 arene isomerization catalyst.
The present invention compared with prior art has the following advantages:
1, when catalyst of the present invention is used for the reaction of catalysis C8 aromatics isomerization, in product, the concentration of paraxylene is close to thermodynamical equilibrium concentration, and reaction has higher conversion of ethylbenzene and Selectivity for paraxylene, and can maintain lower C8 aromatic hydrocarbons loss amount.
2, catalyst of the present invention has quite high commercial significance when being used in the reaction of C8 aromatics isomerization, paraxylene is important isomers, and paraxylene can be obtained by meta-xylene isomerization, in C8 aromatic hydrocarbons, because the boiling point of the boiling point of ethylbenzene and dimethylbenzene is closely difficult to ethylbenzene to separate, adopt catalyst of the present invention can solve this problem, the production paraxylene of high selectivity simultaneously, this is because ethylbenzene can react on the acidic site of EU-1 molecular sieve generate dimethylbenzene, then dimethylbenzene generates paraxylene to greatest extent through the ZSM-5 molecular sieve of high selectivity, because ZSM-5 molecular sieve has higher SiO
2/ Al
2o
3mol ratio and Nano Particle, dimethylbenzene can be made to avoid secondary response occurs in isomerization process, while keeping ethylbenzene high conversion, there is again high Selectivity for paraxylene, and product generation secondary response can be avoided, maintain high C8 aromatics yield, obtain desirable technique effect.
3, the EU-1 molecular sieve SiO of the present invention's use
2/ Al
2o
3mol ratio is 45, and mild acidity, thus not easily coking occurs in catalytic reaction process, and cracking side reaction is few, and isomerization reaction is effective; ZSM-5 molecular sieve is nano crystals, SiO
2/ Al
2o
3mol ratio is 260, there is higher Bronst acid amount relatively, conversion of ethylbenzene is high, the crystallite dimension of ZSM-5 molecular sieve is not more than 100nm, ethylbenzene conversion is caused to be can rapid diffusion after dimethylbenzene, also not easily coking and cracking side reaction occur, so catalyst of the present invention is selective good, the life-span is long.
Below by drawings and Examples, technical scheme of the present invention is described in further detail.
Accompanying drawing explanation
The XRD spectra of the EU-1 molecular sieve that Fig. 1 prepares for the conventional method provided in the specific embodiment of the invention.
The SEM photo of the EU-1 molecular sieve that Fig. 2 prepares for the conventional method provided in the specific embodiment of the invention.
The XRD spectra of the ZSM-5 molecular sieve that Fig. 3 prepares for the conventional method provided in the specific embodiment of the invention.
The SEM photo of the ZSM-5 molecular sieve that Fig. 4 prepares for the conventional method provided in the specific embodiment of the invention.
Detailed description of the invention
SiO used in the present invention
2/ Al
2o
3mol ratio is EU-1 molecular sieve and the SiO of 45
2/ Al
2o
3mol ratio is 260 and the ZSM-5 molecular sieve that crystallite dimension is not more than 100nm all can adopt customary preparation methods to obtain.
EU-1 molecular sieve used in the present invention can adopt following conventional method to prepare:
Step one, get Ludox 203.9g, sodium metaaluminate 6.2g, distilled water 38g, obtains mixed liquor after mixing; SiO in described Ludox
2mass concentration be 26.17%, Na in described sodium metaaluminate
2the mass concentration of O is 304.9565g/L, Al
2o
3mass concentration be 370.1874g/L;
Step 2, get NaOH 9.4g, 1,6-dibromo-hexane 70.6g, trimethylamine solution 106.1g, distilled water 20g, obtains emulsion after mix and blend; The quality purity of described NaOH is 96%, and the quality purity of described 1,6-dibromo-hexane is 98.5%, and the mass concentration of described trimethylamine solution is 33.0%;
Step 3, emulsion described in step 2 is joined in mixed liquor described in step one, vigorous stirring evenly obtains mixture, described mixture is loaded in autoclave, crystallization 48 hours under temperature is 180 DEG C of conditions, naturally crystallization liquid is taken out after cooling, described crystallization liquid is carried out successively be separated, filter and carrying out washing treatment, obtain product;
Step 4, product described in step 3 is placed in baking oven, under the condition of 110 DEG C, dry 12h, obtains EU-1 molecular sieve, and the sodium content in described EU-1 molecular sieve is the SiO of 2.1%, EU-1 molecular sieve of its butt weight
2/ Al
2o
3mol ratio is 45 (x-ray fluorescence elementary analyses), and pore volume is 0.19m
3, specific area is 347m
2/ g.
Fig. 1 is the XRD spectra of the EU-1 molecular sieve that above-mentioned preparation method obtains, and Fig. 2 is the SEM photo of the EU-1 molecular sieve that above-mentioned preparation method obtains, and can find out that EU-1 molecular sieve has that degree of crystallinity is high, crystallite dimension is little and uniform feature from Fig. 1 and Fig. 2.
ZSM-5 molecular sieve used in the present invention can adopt following customary preparation methods to obtain:
Step one, get silochrom 181.39g, sodium metaaluminate 4.2g, tetraethyl ammonium hydroxide 36.82g, NaOH 1.3g, distilled water 90g, obtains mixture after mixing; SiO in described silochrom
2mass concentration be 99.3%, Na in described sodium metaaluminate
2the mass concentration of O is 304.9565g/L, Al
2o
3mass concentration be 370.1874g/L, the mass concentration of described tetraethyl ammonium hydroxide is 40%, and the quality purity of described NaOH is 96%;
Step 2, mixture described in step one to be loaded in autoclave, crystallization 48 hours under temperature 150 DEG C of conditions, naturally takes out crystallization liquid after cooling, by described crystallization liquid successively through being separated, filtration and carrying out washing treatment, obtain product;
Step 3, product described in step 2 is placed in baking oven, dry 12h under 110 DEG C of conditions, obtain ZSM-5 molecular sieve, sodium content in this ZSM-5 molecular sieve is 1.8% of its butt weight, the silica alumina ratio of ZSM-5 molecular sieve is 260 (x-ray fluorescence elementary analyses), and pore volume is 0.28m
3, specific area is 567m
2/ g.
Fig. 3 is the XRD spectra of the ZSM-5 molecular sieve that above-mentioned preparation method obtains, Fig. 4 is the SEM photo of the ZSM-5 molecular sieve that above-mentioned preparation method obtains, and can find out that ZSM-5 molecular sieve has that degree of crystallinity is high, crystallite dimension is little (being not more than 100nm) and uniform feature from Fig. 3 and Fig. 4.
C8 arene isomerization catalyst of the present invention is described according to embodiment 1 ~ embodiment 5:
Embodiment 1
The catalyst of the present embodiment comprises carrier and is carried on the platinum on carrier, and the quality of described platinum is 0.25% of carrier quality, and described carrier comprises the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7.6wt% and the ZSM-5 molecular sieve of 42.4wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and 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: obtain mixture after EU-1 molecular sieve, ZSM-5 molecular sieve and aluminium oxide being mixed, carries out kneading by described mixture and dust technology, and dry after extruded moulding, then roasting 4.5h under 550 DEG C of conditions, obtains carrier; The mass ratio of described mixture and dust technology is 100:60, and the mass concentration of described dust technology is 0.5%;
Step 2, carrier described in step one is placed in ammonium nitrate solution carries out 4 secondary ion exchanges, the temperature of each ion-exchange is 85 DEG C, and the time is 2h; The molar concentration of described ammonium nitrate solution is 1.0mol/L;
Step 3, the carrier after ion-exchange is placed in the medium volume impregnation 13h of chloroplatinic acid, obtains catalyst precursor;
Step 4, catalyst precursor described in step 3 is carried out drying, by dried catalyst precursor roasting 3h under 500 DEG C of conditions, then by the catalyst precursor after roasting in hydrogen atmosphere, reduce 4.5h under the condition of 400 DEG C, after cooling, obtain C8 arene isomerization catalyst.
Embodiment 2
The catalyst of the present embodiment comprises carrier and is carried on the platinum on carrier, and the quality of described platinum is 0.25% of carrier quality, and described carrier comprises the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7wt% and the ZSM-5 molecular sieve of 43wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and the crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
The preparation method of the present embodiment catalyst is with embodiment 1.
Embodiment 3
The catalyst of the present embodiment comprises carrier and is carried on the platinum on carrier, and the quality of described platinum is 0.25% of carrier quality, and described carrier comprises the aluminium oxide of 50wt%, the EU-1 molecular sieve of 8wt% and the ZSM-5 molecular sieve of 42wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and 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: obtain mixture after EU-1 molecular sieve, ZSM-5 molecular sieve and aluminium oxide being mixed, carries out kneading by described mixture and dust technology, and dry after extruded moulding, then roasting 4h under 560 DEG C of conditions, obtains carrier; The mass ratio of described mixture and dust technology is 100:65, and the mass concentration of described dust technology is 0.4%;
Step 2, carrier described in step one is placed in ammonium nitrate solution carries out 3 secondary ion exchanges, the temperature of each ion-exchange is 90 DEG C, and the time is 2.5h; The molar concentration of described ammonium nitrate solution is 1.2mol/L;
Step 3, the carrier after ion-exchange is placed in the medium volume impregnation 14h of chloroplatinic acid, obtains catalyst precursor;
Step 4, catalyst precursor described in step 3 is carried out drying, by dried catalyst precursor roasting 3.5h under 480 DEG C of conditions, then by the catalyst precursor after roasting in hydrogen atmosphere, reduce 5h under the condition of 380 DEG C, after cooling, obtain C8 arene isomerization catalyst.
Embodiment 4
The catalyst of the present embodiment comprises carrier and is carried on the platinum on carrier, and the quality of described platinum is 0.25% of carrier quality, and described carrier comprises the aluminium oxide of 50wt%, the EU-1 molecular sieve of 6wt% and the ZSM-5 molecular sieve of 44wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and the crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
The preparation method of the present embodiment catalyst is with embodiment 3.
Embodiment 5
The catalyst of the present embodiment comprises carrier and is carried on the platinum on carrier, and the quality of described platinum is 0.25% of carrier quality, and described carrier comprises the aluminium oxide of 50wt%, the EU-1 molecular sieve of 9wt% and the ZSM-5 molecular sieve of 41wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and 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: obtain mixture after EU-1 molecular sieve, ZSM-5 molecular sieve and aluminium oxide being mixed, carries out kneading by described mixture and dust technology, and dry after extruded moulding, then roasting 5h under 540 DEG C of conditions, obtains carrier; The mass ratio of described mixture and dust technology is 100:55, and the mass concentration of described dust technology is 0.6%;
Step 2, carrier described in step one is placed in ammonium nitrate solution carries out 4 secondary ion exchanges, the temperature of each ion-exchange is 80 DEG C, and the time is 1.5h; The molar concentration of described ammonium nitrate solution is 0.8mol/L;
Step 3, the carrier after ion-exchange is placed in the medium volume impregnation 12h of chloroplatinic acid, obtains catalyst precursor;
Step 4, catalyst precursor described in step 3 is carried out drying, by dried catalyst precursor roasting 2.5h under 520 DEG C of conditions, then by the catalyst precursor after roasting in hydrogen atmosphere, reduce 4h under the condition of 420 DEG C, after cooling, obtain C8 arene isomerization catalyst.
The application of C8 arene isomerization catalyst of the present invention is described according to embodiment 6 ~ embodiment 8:
Embodiment 6
The application of catalyst in the reaction of C8 aromatics isomerization of embodiment 1 ~ embodiment 5, the method of described isomerization reaction is: loaded by catalyst in fixed bed reactors, is 350 DEG C in reaction temperature, and reaction pressure is 0.7MPa, the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.5, and mass space velocity is 4h
-1condition under, catalysis C8 aromatics isomerization react; In described C8 aromatic hydrocarbons, containing carbon eight alkane, carbon eight cycloalkane, meta-xylene, ortho-xylene and ethylbenzene, (wherein the mass percentage sum of carbon eight alkane and carbon eight cycloalkane is 7.8733%, the mass percentage of meta-xylene is 53.0043%, the mass percentage of ortho-xylene is 20.4355%, and the mass percentage of ethylbenzene is 18.6869%).
The reaction result adopting catalyst C8 aromatics isomerization of the present invention to react is as shown in table 1.
The reaction result that table 1 adopts catalyst C8 aromatics isomerization of the present invention to react
In table 1, the computational methods of paraxylene equilibrium concentration, conversion of ethylbenzene and C8 hydrocarbon yield are respectively:
In above formula, w (EB)
ffor the mass fraction of ethylbenzene in raw material C8 aromatic hydrocarbons, w (X)
ffor the mass fraction of dimethylbenzene in raw material C8 aromatic hydrocarbons, w (PX)
pfor the mass fraction of paraxylene in product,
for the mass fraction sum of carbon eight alkane and carbon eight cycloalkane in raw material C8 aromatic hydrocarbons; W (MX)
pfor the mass fraction of meta-xylene in product, w (OX)
pfor the mass fraction of ortho-xylene in product, 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 carbon in product eight alkane and carbon eight cycloalkane.
Embodiment 7
The application of catalyst in the reaction of catalysis C8 aromatics isomerization of embodiment 1, the method of described isomerization reaction is: loaded by catalyst in fixed bed reactors, is 340 DEG C in reaction temperature, and reaction pressure is 0.8MPa, the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.3, and mass space velocity is 6h
-1condition under, catalysis C8 aromatics isomerization react; Composition and the content of described C8 aromatic hydrocarbons are identical with enforcement 6.
Embodiment 8
Adopt the application of the catalyst of embodiment 1 in the reaction of catalysis C8 aromatics isomerization, the method of described isomerization reaction is: loaded by catalyst in fixed bed reactors, is 345 DEG C in reaction temperature, and reaction pressure is 0.75MPa, the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.4, and mass space velocity is 5h
-1condition under, catalysis C8 aromatics isomerization react; Composition and the content of described C8 aromatic hydrocarbons are identical with enforcement 6.
The reaction result of embodiment 7 ~ embodiment 8 is as shown in table 2.
The reaction result of table 2 embodiment 7 ~ embodiment 8
The computational methods of paraxylene equilibrium concentration in table 2, conversion of ethylbenzene and C8 hydrocarbon yield and paraxylene equilibrium concentration in embodiment 6 table 1, conversion of ethylbenzene are identical with the computational methods of C8 hydrocarbon yield.
As can be seen from Table 1 and Table 2, when catalyst of the present invention is used for the reaction of catalysis C8 aromatics isomerization, in product, the concentration of paraxylene is close to thermodynamical equilibrium concentration, there is higher conversion of ethylbenzene and Selectivity for paraxylene, C8 hydrocarbon yield very high showing there occurs few side reaction in isomerization reaction, so catalyst of the present invention has active high, selective good and feature that the life-span is long.
The above; it is only preferred embodiment of the present invention; not the present invention is imposed any restrictions, every above embodiment is done according to the technology of the present invention essence any simple modification, change and equivalent structure change, all still belong in the protection domain of technical solution of the present invention.
Claims (5)
1. a C8 arene isomerization catalyst, comprise carrier and be carried on the platinum on described carrier, the quality of described platinum is 0.25% of described carrier quality, and described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 6wt% ~ 9wt% and 41wt% ~ 44wt%; The SiO of described EU-1 molecular sieve
2/ Al
2o
3mol ratio is 45, the SiO of described ZSM-5 molecular sieve
2/ Al
2o
3mol ratio is 260, and the crystallite dimension of ZSM-5 molecular sieve is not more than 100nm.
2. according to a kind of C8 arene isomerization catalyst according to claim 1, it is characterized in that, described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7wt% ~ 8wt% and 42wt% ~ 43wt%.
3. according to a kind of C8 arene isomerization catalyst according to claim 2, it is characterized in that, described carrier comprises the ZSM-5 molecular sieve of the aluminium oxide of 50wt%, the EU-1 molecular sieve of 7.6wt% and 42.4wt%.
4. the application of catalyst in the reaction of C8 aromatics isomerization as described in claim 1,2 or 3, it is characterized in that, the method of described isomerization reaction is: loaded by catalyst in fixed bed reactors, it 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
-1condition under, catalysis C8 aromatics isomerization react.
5. according to application according to claim 4, it is characterized in that, described reaction temperature is 350 DEG C, and reaction pressure is 0.7MPa, and the mol ratio of hydrogen and C8 aromatic hydrocarbons is 2.5, and mass space velocity is 4h
-1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410667408.4A CN104353487B (en) | 2014-11-20 | 2014-11-20 | A kind of C8 arene isomerization catalysts and its application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410667408.4A CN104353487B (en) | 2014-11-20 | 2014-11-20 | A kind of C8 arene isomerization catalysts and its application |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104353487A true CN104353487A (en) | 2015-02-18 |
| CN104353487B CN104353487B (en) | 2017-08-29 |
Family
ID=52520848
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410667408.4A Active CN104353487B (en) | 2014-11-20 | 2014-11-20 | A kind of C8 arene isomerization catalysts and its application |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104353487B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN108349836A (en) * | 2015-10-28 | 2018-07-31 | Bp北美公司 | Improvement catalyst for ethylbenzene conversion in Xylene isomerization process |
| CN111514928A (en) * | 2020-04-29 | 2020-08-11 | 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 |
| CN112028730A (en) * | 2019-06-04 | 2020-12-04 | 中国石油化工股份有限公司 | Xylene isomerization method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2014
- 2014-11-20 CN CN201410667408.4A patent/CN104353487B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108349836A (en) * | 2015-10-28 | 2018-07-31 | Bp北美公司 | Improvement catalyst for ethylbenzene conversion in Xylene isomerization process |
| US10799852B2 (en) | 2015-10-28 | 2020-10-13 | Bp Corporation North America Inc. | Catalyst for ethylbenzene conversion in a xylene isomerization process |
| CN108349836B (en) * | 2015-10-28 | 2021-04-20 | Bp北美公司 | Improved catalyst for ethylbenzene conversion in xylene isomerization 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 |
| CN112028730A (en) * | 2019-06-04 | 2020-12-04 | 中国石油化工股份有限公司 | Xylene isomerization method |
| CN112028730B (en) * | 2019-06-04 | 2023-06-09 | 中国石油化工股份有限公司 | Xylene isomerization method |
| CN111514928A (en) * | 2020-04-29 | 2020-08-11 | 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 |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104353487B (en) | 2017-08-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2491268C2 (en) | Transalkylation method | |
| EP2931686B1 (en) | Aromatic transalkylation using uzm-44 aluminosilicate zeolite | |
| US8242321B2 (en) | Processes for transalkylating aromatic hydrocarbons | |
| JP6005878B2 (en) | Aromatic transalkylation reaction using UZM-39 aluminosilicate zeolite | |
| US8633344B2 (en) | Aromatic transformation using UZM-39 aluminosilicate zeolite | |
| EP2773603B1 (en) | Catalyst and process for hydrocarbon conversion | |
| CN102553639A (en) | Catalysts, processes for preparing the catalysts, and processes for transalkylating aromatic hydrocarbon compounds | |
| US20130066123A1 (en) | Process for transalkylating aromatic hydrocarbons | |
| US8748685B1 (en) | Aromatic transformation using UZM-44 aluminosilicate zeolite | |
| CN104353487A (en) | C8 aromatics isomerization catalyst and application thereof | |
| KR20180069909A (en) | Improved catalyst for ethylbenzene conversion in xylene isomerization process | |
| TWI749489B (en) | Catalysts and processes for converting aromatics | |
| KR20220117338A (en) | UZM-54 and transalkylation method using same | |
| KR20220130831A (en) | Toluene disproportionation using reinforced UZM-39 aluminosilicate zeolite |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20160422 Address after: 710600 No. 1 Railway Station Street, Lintong District, Shaanxi, Xi'an Applicant after: The Northwest Research Institute of Chemical Industry Applicant after: Shaanxi extends refinery company of oil (group) limited liability company Address before: 710061 Shaanxi province Xi'an Yanta District Yan Cheung Road No. 99 Applicant before: Xi'an Origin Chemical Technologies Co., Ltd. Applicant before: The Northwest Research Institute of Chemical Industry Applicant before: Shaanxi extends refinery company of oil (group) limited liability company |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |