CN102744098B - The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene - Google Patents
The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene Download PDFInfo
- Publication number
- CN102744098B CN102744098B CN201110099958.7A CN201110099958A CN102744098B CN 102744098 B CN102744098 B CN 102744098B CN 201110099958 A CN201110099958 A CN 201110099958A CN 102744098 B CN102744098 B CN 102744098B
- Authority
- CN
- China
- Prior art keywords
- trimethylbenzene
- catalyst
- zeolite
- aromatic hydrocarbons
- heavy aromatics
- 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.)
- Active
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)
Abstract
The present invention relates to the catalyst of a kind of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene, mainly solve existing hydrotreating catalyst and scarce capacity is removed to the C9 aromatic in low value-added heavy aromatics except trimethylbenzene, from product, rectifying is separated trimethylbenzene monomer long flow path, separation difficulty, the technical problem that cost is higher.The present invention to adopt with the Hydrogen binder free ten-ring zeolite of load quality percentage 0.005 ~ 0.5 part of platinum or palladium as catalyst, solves this problem preferably, can be used in the industrial production of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and high added value trimethylbenzene.
Description
Technical field
The present invention relates to the catalyst of a kind of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene.
Background technology
Heavy arene comprises carbon more than nine aromatic hydrocarbons of steam cracking device and oil plant continuous reformer by-product, is valuable petrochemical industry resource, heavy arene of particularly reforming.Along with the operation in succession of China's large petrochemical plant continuous reformer in recent years, the increase of production amplitude of reformation heavy arene is very fast, C9 aromatic in continuous reformer heavy aromatics is generally used for the production of producing paraxylene (PX) with toluene transalkylation, also have considerable part to enter heavy aromatics comprehensive utilization production and carry out process application, for extracting the component such as mesitylene, pseudocumene, 1,2,3-trimethylbenzene, the first and second benzene wherein.
External just starting after isolating pseudocumene the 1950's from reformation C9 aromatic utilizes this part resource to produce fine chemical product on a large scale, its application is day by day widened to define and is compared rounded system, comprises the every field such as plastics, coating, plasticizer, medicine, synthetic fibers.This part heavy aromatics has specific molecular structure feature and develops its serviceability particularly unique in the fine chemicals such as production high-temperature resin, sapecial coating, plasticizer, curing agent in some goods, improves economic benefit.And the R & D and manufacture scale of domestic reformation C9 aromatic is all smaller, some enterprise is due to the reasons such as technology and equipment successively stopping production, and some devices not yet reach large production equipment scale.The utilization rate of current China reformation C9 aromatic is also lower, and a considerable amount of heavy aromatics fusion has been burnt in the oil, and this is the waste in a utilization of resources.
C9 aromatic has nine kinds of isomers, can have mesitylene, pseudocumene, m-methyl ethylbenzene and p-methyl-ethylbenzene after being separated industrially as product.Wherein with pseudocumene and mesitylene added value maximum.From prior art, producing the difficult point being separated trimethylbenzene is there is many materials such as C9 aromatic isomers and butylbenzene such as the first and second benzene, propyl benzene in raw material, and the boiling point of part carbon nine and above aromatic hydrocarbons (the first and second benzene, butylbenzene) and trimethylbenzene are closely.CN1139095A has invented one from C
9the method producing mesitylene is separated, the C that the first and second benzene weight contents are greater than 22% in BTX aromatics
9bTX aromatics raw material is after first rectifying, containing mesitylene, pseudocumene and neighbour, the blending fraction section of p-methyl-ethylbenzene is by as reaction raw materials, add the tert-butyl alcohol, the concentrated sulfuric acid, alchlor and hydrochloric acid as reaction additive, through alkylated reaction and settlement treatment, first and second benzene are converted into high-boiling components, then reactant is carried out rectifying separation, the final mesitylene product obtaining purity and be greater than 98%.Except trimethylbenzene except the C of heavy aromatics generally containing high level of reformer
9aromatic hydrocarbons, its content is generally greater than 30%, CN1313269A and the heavy aromatics from oil plant reformer is needed carry out continuous rectification through two packed towers and isolate the higher pseudocumene fraction of purity, but can not obtain higher degree mesitylene.CN1974500A adopts three tower serial flow process counterweight bulk wight aromatic hydrocarbons to be separated, can the enriched mesitylene of higher pseudocumene co-production more than 35% purity of production purity, and mesitylene purity is lower.Therefore, in prior art, the technological process of separation of produced mesitylene and pseudocumene is longer, complex process, and yield is lower, and production cost is higher, and commercial Application difficulty is large.
Zeolite powder particularly nano zeolite powder can form dust in actual applications, inconvenient operation, there is the weakness such as difficult recovery, easy in inactivation and gathering, also can jeopardize the health of operator, because too high pressure drop zeolite powder is not suitable for fixed bed reactors in catalytic reaction yet.Therefore zeolite molecular sieve powder must be made the particle with certain mechanical strength and shape, this process often needs to add binding agent, the binding agent of frequent employing comprises some oxides and some clay minerals such as aluminium oxide, silica, titanium dioxide, the introducing of binding agent can reduce the content of effective zeolite component, cause adsorbance to decline, effective surface area is reduced.Because binding agent constituent part can enter zeolite cavity or blocking portion zeolite aperture, therefore diffusion restriction is introduced, adsorption capacity is caused to weaken, adsorptive selectivity is deteriorated, sorption and desorption speed declines, in catalytic reaction, then cause active reduction, selective decline, and Binder Composition also may cause some side reactions undesirably occurred.Binder free zeolite molecular sieve refers to not containing inert binder in zeolitic molecular sieve particle, the main zeolite block of material with definite shape and size relying on the interaction self-supporting between zeolite grain to exist.Binder free zeolitic material mesolite weight content is greater than 95%, and crushing strength is greater than 40N/, and available effective surface area is comparatively large, has better performance in catalytic reaction.
Summary of the invention
Technical problem to be solved by this invention is that in prior art, hydrotreating catalyst removes scarce capacity to the C9 aromatic in low value-added heavy aromatics except trimethylbenzene, from product, rectifying is separated trimethylbenzene monomer long flow path, separation difficulty, the technical problem that cost is higher, a kind of heavy aromatics hydrocracking is provided to increase production the catalyst of BTX aromatic hydrocarbons and trimethylbenzene, this invention catalyst activity is high, effectively can remove the C9 aromatic except trimethylbenzene, can from product separating high-purity trimethylbenzene monomer increase production BTX aromatic hydrocarbons, solve this problem preferably.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: the catalyst of a kind of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene, comprises by weight percentage:
A) 0.005 ~ 0.5 part is selected from the noble metal of at least one in Pt or Pd;
B) 99.5 ~ 100 parts is Hydrogen binder free ten-ring zeolite, and the crushing strength of binder free zeolite is greater than 40N/, and zeolite weight content is greater than 95%;
Heavy aromatics is carbon nine and above aromatic hydrocarbons, and in BTX aromatic hydrocarbons, B is benzene, and T is toluene, and X is dimethylbenzene.
In technique scheme, select in catalyst the consumption of at least one noble metal in Pt or Pd by weight percentage preferable range be 0.01 ~ 0.5 part; The ten-ring zeolite selected in catalyst is at least one in ZSM-5 or ZSM-11 zeolite, the SiO of binder free ten-ring zeolite
2/ Al
2o
3mol ratio is 20 ~ 200; Also containing at least one be selected from Zn, La, Sn, Pb or Bi in catalyst, its consumption is > 0 ~ 1 part by weight percentage; Heavy aromatics from reformate, drippolene, naphtha and catalytically cracked gasoline, preferred reformation heavy aromatics raw material.
Binder free zeolite is with sodium form preparation synthesis, then carry out ion-exchange with the acid solution such as ammonium salt solution or hydrochloric acid, carry out roasting after exchange and be converted into h-type zeolite, then introduced at least one metal of Pt or Pd by ion-exchange or dipping method, use palladium bichloride, palladium nitrate, ammonium chloropalladate, ammonium chloropalladite, platinum nitrate, chloroplatinic acid, ammonium chloroplatinate, ammonium chloroplatinite, dichloro four ammonium closes the aqueous solution of platinum at least one as precursor.Binder free h-type zeolite is introduced after Pt or Pd, carries out drying being less than at 200 DEG C, then calcines dried catalyst at 300-600 DEG C.
Along with the progress of Petroleum Processing Technology, the heavy aromatics output of catalytic reforming unit and the output of drippolene improve constantly.From prior art, producing the difficult point being separated trimethylbenzene is exist in raw material to comprise the first and second benzene, the C9 aromatic isomers such as propyl benzene and butylbenzene are at interior many materials, part carbon nine and above aromatic hydrocarbons (the first and second benzene, butylbenzene) boiling point and trimethylbenzene closely, therefore the flow process being separated trimethylbenzene monomer is longer, complex process, invest large energy consumption high, product yield is low, the problems such as economic indicator difference, therefore be difficult to be used, so develop aromatics seperation purification new technology as early as possible, improve and development trimethylbenzene production technology, reduce production cost, improve the technological competitiveness of domestic trimethylbenzene industry, meet the demand of domestic and international market.
According to the present invention, the acid carrier of catalyst uses with the form of binder free ten-ring duct zeolite.The acidity of Zeolite support is most important in hydrocracking reaction, and first alkylbenzene many carbon carbochain carries out protonated on B acid site, removes many carbon carbochain through cracking, and it is comparatively easy to react; And on L acid site, many carbon carbochain of alkylbenzene be then formed free radical therefrom between chain rupture, reaction is difficulty comparatively.Binder free Zeolites Zeolites content is high, and containing highdensity B acid site, it is more easy therefore to remove for many carbon carbochain of alkylbenzene.The pore passage structure of zeolite is also vital for the impact of de-alkyl, different zeolites has different pore passage structures, wherein ten-ring structural zeolite has very high removal activity to the ethyl of heavy arene and propyl group, but only has the conversion ratio of medium trimethylbenzene.In above-mentioned hydrocracking reaction, the such as alkene intermediates such as ethene, propylene can be produced, should promptly cause catalysqt deactivation to prevent olefinic polymerization from impelling coke to be formed or cause the character of aromatic component in product to be deteriorated with light aromatics generation alkylated reaction by hydrotreated lube base oil.Therefore, there is the hydrogenating function that acid centre matches in catalyst, should metallic element containing group VIII in the periodic table of elements with hydrogenation.Metal component Pt or Pd all has good hydrogenation effect, should consider the problem that acidity of catalyst center and hydrogenation metal center match and adapt to raw material in catalyst preparing.Acid centre by the silica/alumina mole ratio of adjustment zeolite molecular sieve or can be mediated by modification, and the hydrogenation activity of metal center can be adjusted by the decentralization of content of metal, carried metal.The raw material suppressing metal hydrogenation performance component may be contained for raw material is comparatively complicated, the drippolene raw material of such as sulfur compound, can consider Pt, Pd two kinds of metal composite together, this all can have good sulfur resistance than being used alone any one metal of Pt, Pd thus keeping good Hydrogenation.Pt, Pd two kinds of metal composite can produce mutually electro ultrafiltration or chemical action, instead of separately exist in catalyst, thus provide excellent hydrogenation and sulfur resistance.Catalyst of the present invention adopts binder free ten-ring zeolite as acidic components, there is sour density large, the feature that aperture is unobstructed, metal hydrogenation component has the moderate feature of Hydrogenation, can effectively remove the heavy aromatics such as the first and second benzene, propyl benzene and butylbenzene, thus the rectifying being conducive to trimethylbenzene monomer is separated, and can be separated and obtain highly purified trimethylbenzene monomer, and can increase production BTX aromatic hydrocarbons from reaction effluent.
The efficient bifunctional catalyst that the invention provides a kind of binder free Zeolite support carried noble metal increases production the reaction of BTX aromatic hydrocarbons and trimethylbenzene for heavy aromatics hydrocracking, in fixed bed reactors with the mixture of heavy aromatics and hydrogen for raw material, at Hydrogen Vapor Pressure 2.8MPa, H
2/ oil volume, than 400, reacts inlet temperature 360 DEG C, weight (hourly) space velocity (WHSV) WHSV=2.0 hour
-1when, arene content in reaction effluent in C9 aromatic except trimethylbenzene is less than 0.5%, BTX aromatic hydrocarbons yield reaches 59.2%, therefore be separated by BTX tower after product is separated lighter hydrocarbons and obtain BTX aromatic hydrocarbon product, materials at bottom of tower only need enter mesitylene tower and pseudocumene tower successively to carry out rectifying and just can isolate the trimethylbenzene monomer that purity is greater than 98%, achieves good technique effect.
Below by embodiment, the present invention is further elaborated.
Detailed description of the invention
[embodiment 1 ~ 2]
Adhesiveless ZSM-5 zeolite (SiO
2/ Al
2o
3mol ratio is 60) with reference to Chinese patent CN100384735C preparation, the adhesiveless ZSM-5 zeolite crushing strength of preparation is greater than 75N/, ZSM-5 zeolite weight content is 98.5%, and product and ammonium nitrate solution carry out ion-exchange, carries out roasting and be converted into h-type zeolite after exchange.The Pt of dip loading the mass ratio range 0.05% and Zn of 0.25% on Hydrogen adhesiveless ZSM-5 zeolite, at 450 DEG C, calcining obtains catalyst a in 4 hours; The Pd of dip loading the mass ratio range 0.3% and Pb of 0.05% on Hydrogen adhesiveless ZSM-5 zeolite, at 450 DEG C, calcining obtains catalyst b in 4 hours.
[embodiment 3 ~ 5]
Adhesiveless ZSM-5 zeolite (SiO
2/ Al
2o
3mol ratio is 20) with reference to Chinese patent CN100384735C preparation, the adhesiveless ZSM-5 zeolite crushing strength of preparation is greater than 65N/, ZSM-5 zeolite weight content is 99.6%, and product and ammonium nitrate solution carry out ion-exchange, carries out roasting and be converted into h-type zeolite after exchange.The Pt of dip loading the mass ratio range 0.005% and Sn of 0.01% on Hydrogen adhesiveless ZSM-5 zeolite, at 450 DEG C, calcining obtains catalyst c in 4 hours; The La of the Pd of dip loading mass ratio range 0.5%, the Zn of 0.01% and 1.0% on Hydrogen adhesiveless ZSM-5 zeolite, at 450 DEG C, calcining obtains catalyst d in 4 hours; The Sn of the Pt of dip loading mass ratio range 0.03%, the Bi of 0.02% and 0.2% on Hydrogen adhesiveless ZSM-5 zeolite, at 450 DEG C, calcining obtains catalyst e in 4 hours.
[embodiment 6 ~ 7]
Binderless ZSM-5-11 zeolite (SiO
2/ Al
2o
3mol ratio is 45) with reference to Chinese patent CN101348261A preparation, binderless ZSM-5-11 zeolite crushing strength of preparation is greater than 80N/, ZSM-11 zeolite weight content is 97.9%, and product and ammonium nitrate solution carry out ion-exchange, carries out roasting and be converted into h-type zeolite after exchange.The Pt of dip loading the mass ratio range 0.06% and Zn of 0.2% on Hydrogen binderless ZSM-5-11 zeolite, at 450 DEG C, calcining obtains catalyst f in 4 hours; The Pt of dip loading the mass ratio range 0.2% and Bi of 0.20% on Hydrogen binderless ZSM-5-11 zeolite, at 450 DEG C, calcining obtains catalyst g in 4 hours.
[embodiment 8]
Take 250 grams of White Carbon blacks, 100 grams of ZSM-5 zeolite (SiO
2/ Al
2o
3mol ratio is 125), add 12 grams of sesbania powder, 16 grams of aluminum sulfate [Al
2(SO
4)
318H
2o], 10 grams of NaOH carry out kneading with the Ludox (percentage by weight 40%) adding 500 grams again and become cylindric shape to carry out drying.TBAH (TBAOH) solution being 8% by the cylindric presoma of 40 grams of above-mentioned preparations and 80 gram mass percentage concentrations respectively mixes and is placed in crystallizing kettle and at 160 DEG C, carries out hydrothermal treatment consists 4 days.Product with after distilled water washing and drying in air atmosphere in 550 DEG C of roastings.The XRD collection of illustrative plates of product all shows that crystalline phase is ZSM-5/ZSM-11 cocrystallization zeolite, and baseline straightening, prepares the SiO of product
2/ Al
2o
3mol ratio is determined as 185.Adhesiveless ZSM-5/ZSM-11 cocrystallization zeolite the crushing strength of preparation is greater than 40N/, ZSM-5/ZSM-11 cocrystallization zeolite weight content is 98.1%, product with prepare product and ammonium nitrate solution carries out ion-exchange, carry out roasting after exchange and be converted into h-type zeolite.The Pt of dip loading the mass ratio range 0.001% and Pd of 0.1% on Hydrogen adhesiveless ZSM-5/ZSM-11 zeolite, at 450 DEG C, calcining obtains catalyst h in 4 hours.
Use a ~ h catalyst of reduction activation in fixed bed reactors, carry out reaction examination, heavy aromatics raw material counts dimethylbenzene 7.49% with weight percent; Isopropylbenzene 2.39%; N-proplbenzene 4.00%; M-methyl ethylbenzene 15.40%; P-methyl-ethylbenzene 4.07%; Mesitylene 5.03%; O-methylethylbenzene 6.82%; Pseudocumene 26.86%; 1,2,3-trimethylbenzene 8.43%; Indane 0.94%; Hydrocarbon 18.22% more than 10 carbon.At Hydrogen Vapor Pressure 2.8MPa, H
2/ oil volume is than 400, and inlet temperature 360 DEG C, weight (hourly) space velocity (WHSV) WHSV is 2.0 hours
-1reaction result list in table 1.Product is separated to be separated by BTX tower after lighter hydrocarbons and obtains BTX aromatic hydrocarbon product, and materials at bottom of tower only need enter mesitylene tower and pseudocumene tower successively to carry out rectifying and just can isolate the trimethylbenzene monomer that purity is greater than 98%.
Claims (3)
1. a catalyst for heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene, comprises with parts by weight:
A) 0.005 ~ 0.5 part is selected from the noble metal of at least one in Pt or Pd;
B) 99.5 ~ 100 parts is Hydrogen binder free ten-ring zeolite, and the crushing strength of binder free zeolite is greater than 40N/, and zeolite weight content is greater than 95%;
Heavy aromatics is carbon nine and above aromatic hydrocarbons, and in BTX aromatic hydrocarbons, B is benzene, and T is toluene, and X is dimethylbenzene;
Also containing at least one be selected from La or Bi in catalyst, its consumption take parts by weight as > 0 ~ 1 part.
2. heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and the catalyst of trimethylbenzene according to claim 1, is characterized in that ten-ring zeolite that catalyst is selected is at least one in ZSM-5 or ZSM-11 zeolite.
3. the catalyst of BTX aromatic hydrocarbons and trimethylbenzene is increased production in heavy aromatics hydrocracking according to claim 1, it is characterized in that the SiO of binder free ten-ring zeolite
2/ Al
2o
3mol ratio is 20 ~ 200.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110099958.7A CN102744098B (en) | 2011-04-20 | 2011-04-20 | The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110099958.7A CN102744098B (en) | 2011-04-20 | 2011-04-20 | The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102744098A CN102744098A (en) | 2012-10-24 |
| CN102744098B true CN102744098B (en) | 2016-04-13 |
Family
ID=47024794
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110099958.7A Active CN102744098B (en) | 2011-04-20 | 2011-04-20 | The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102744098B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104148104B (en) * | 2013-05-16 | 2016-09-07 | 中国石油化工股份有限公司 | Pyrolysis gasoline hydrogenation processes catalyst and method |
| CN105233862B (en) * | 2014-07-11 | 2018-10-23 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst and preparation method thereof |
| CN105582988B (en) * | 2014-10-24 | 2019-05-14 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst |
| CN105582990B (en) * | 2014-10-24 | 2018-06-08 | 中国石油化工股份有限公司 | Cyclohexyl benzene production catalyst |
| CN104399520B (en) * | 2014-11-11 | 2017-02-08 | 中国海洋石油总公司 | Catalyst for producing high-octane-number gasoline composition from heavy aromatic hydrocarbons and preparation method of catalyst |
| CN104383961A (en) * | 2014-11-11 | 2015-03-04 | 中国海洋石油总公司 | Catalyst for hydrocracking heavy aromatics for producing high-purity BTX aromatics and preparing method of catalyst |
| CN109351366A (en) * | 2018-10-16 | 2019-02-19 | 江苏华伦化工有限公司 | The method for reducing high boiling aromatic hydrocarbon solvent bromine index |
| CN112745945A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method and system for treating catalytic pyrolysis gasoline, catalytic pyrolysis process and device for producing more dimethylbenzene |
| CN114433211B (en) * | 2020-10-19 | 2024-05-31 | 中国石油化工股份有限公司 | Chemical hydrocracking catalyst and its prepn and application |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101348405A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for preparing light arene and light alkane from hydrocarbon raw material |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI478768B (en) * | 2007-07-18 | 2015-04-01 | China Petro Chemical Technologydevelopment Company | Catalysts and methods for the production of light aromatics and light alkanes from hydrocarbon feedstocks |
| JP5498720B2 (en) * | 2009-03-30 | 2014-05-21 | 一般財団法人石油エネルギー技術センター | Method for producing monocyclic aromatic hydrocarbons |
-
2011
- 2011-04-20 CN CN201110099958.7A patent/CN102744098B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101348405A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for preparing light arene and light alkane from hydrocarbon raw material |
Non-Patent Citations (2)
| Title |
|---|
| "汽相转化法制备无粘结剂小晶粒ZSM-5沸石";王德举等;《无机材料学报》;20080531;第23卷(第3期);第592-596页 * |
| "重整重芳烃催化加氢裂解反应工艺条件的探究";唐之勤等;《化学反应工程与工艺》;20110228;第27卷(第1期);第1-2页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102744098A (en) | 2012-10-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102744098B (en) | The catalyst of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and trimethylbenzene | |
| CN101348733B (en) | Method for producing light arene and light alkane from hydrocarbon raw material | |
| KR101539613B1 (en) | Catalyst and process for preparing light aromatic hydrocarbons and light alkanes from hydrocarbonaceous feedstock using the catalyst | |
| CN102746092B (en) | Method for separating and producing 1,3,5-trimethylbenzene through hydrocracking heavy aromatic hydrocarbons | |
| CN105272803B (en) | The method that toluene is disproportionated transalkylation with heavy aromatics | |
| JP2009516015A (en) | Process for producing aromatic hydrocarbons and liquefied petroleum gas from hydrocarbon mixtures | |
| CN101348405B (en) | Method for preparing light arene and light alkane from hydrocarbon raw material | |
| JP3988847B2 (en) | Catalysts and processes for the conversion of aromatic hydrocarbons and their use in the production of aromatic hydrocarbons | |
| CN100998950A (en) | Catalyst used for heavy arene lightenation and alkyl transfer and its preparation method | |
| CN102688771A (en) | Catalyst for alkylation of benzene and methanol, preparation and application thereof | |
| CN102746091B (en) | Method for producing BTX (benzene, toluene and xylol) aromatic hydrocarbons and trimethylbenzene from heavy aromatic hydrocarbons | |
| CN106925339B (en) | Preparation method of hierarchical pore molecular sieve catalyst for xylene isomerization reaction in carbon octaarene | |
| CN103153923B (en) | Produce the method for isopropyl benzene | |
| CN102909058B (en) | Catalyst containing modified EUO type molecular sieve, and preparation method and application thereof | |
| CN102451750A (en) | Selective dealkylation catalyst for alkyl aromatics | |
| CN103285912B (en) | Preparation method of ethylbenzene dealkylation catalyst in carbon octaaromatic hydrocarbon | |
| WO2014093467A1 (en) | Conversion of methane to aromatic compounds using a catalytic composite | |
| CN105289704A (en) | Preparation method of C8 aromatic isomerization catalyst | |
| CN102039161A (en) | C8 arene isomerization catalyst and application thereof | |
| CN102746093B (en) | Heavy aromatics hydrocracking is utilized to increase production the method for BTX aromatic hydrocarbons and trimethylbenzene | |
| CN104549472A (en) | Aromatic alkyl transferring and deolefination catalyst and application thereof | |
| CN102372537A (en) | Method for preparing propylene and aromatic hydrocarbon through methanol conversion | |
| CN102309978B (en) | Ethyl benzene dealkylation catalyst and preparation method and application thereof | |
| CN102909057A (en) | Catalyst comprising EUO type zeolite, preparation method and applications thereof | |
| CN102309979B (en) | Catalyst for isomerizing ethyl benzene into dimethyl benzene and preparation method and application thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |