CN102744098A - Catalyst for yield increases of BTX (benzene, toluene and xylol) aromatic hydrocarbons and trimethylbenzene through hydrocracking heavy aromatic hydrocarbons - Google Patents
Catalyst for yield increases of BTX (benzene, toluene and xylol) aromatic hydrocarbons and trimethylbenzene through hydrocracking heavy aromatic hydrocarbons Download PDFInfo
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Abstract
The invention relates to a catalyst for the yield increases of BTX aromatic hydrocarbons and trimethylbenzene through hydrocracking heavy aromatic hydrocarbons to mainly solve technical problems of insufficient capability of present hydrotreatment catalysts for removing C9 aromatic hydrocarbons except the trimethylbenzene from the heavy aromatic hydrocarbons with low added values, and long flow, difficult separation and high cost in rectification separation of trimethylbenzene monomers from products. According to the invention, hydrogen type binder-free ten-membered ring zeolite loading 0.005-0.5 parts by mass of Pt or Pd is adopted as the catalyst, so the catalyst well solves the problems, and can be used for the industrial production for the yield increases of the BTX aromatic hydrocarbons and the trimethylbenzene with a high added value through hydrocracking the heavy aromatic hydrocarbons.
Description
Technical field
The present invention relates to the catalyst of a kind of heavy aromatics hydrocracking raising the output BTX aromatic hydrocarbons and trimethylbenzene.
Background technology
Heavy arene comprises the carbon nine above aromatic hydrocarbons of steam cracking device and oil plant continuous reformer by-product, is valuable petrochemical industry resource, the heavy arene of particularly reforming.Along with China's operation in succession of large-scale petrochemical enterprise continuous reformer in recent years; The increase of production amplitude of reformation heavy arene is very fast; C9 aromatic in the continuous reformer heavy aromatics generally is used for producing with the toluene transalkylation production of paraxylene (PX); Also have considerable part to get into heavy aromatics comprehensive utilization process units and handle application, be used to extract components such as wherein mesitylene, pseudocumene, 1,2,3-trimethylbenzene, first and second benzene.
After from the reformation C9 aromatic, isolating pseudocumene the 1950's, just begun to utilize on a large scale this part resource to produce fine chemical product abroad; Its application broadened has formed relatively rounded system, comprises every field such as plastics, coating, plasticizer, medicine, synthetic fibers.This partly heavy aromatics have its unique serviceability in producing fine chemicals such as high-temperature resin, sapecial coating, plasticizer, curing agent particularly in some goods of specific molecular structure characteristics exploitation, improved economic benefit.And the research of domestic reformation C9 aromatic and production scale are all smaller, and some enterprise is owing to reasons such as technology and equipment successively stop production, and some devices do not reach the large production equipment scale as yet.The utilization rate of China's reformation C9 aromatic is also lower at present, and a considerable amount of heavy aromatics are blended in the gasoline have been burnt, and this is the waste on a reward for writing or painting source utilizes.
C9 aromatic has nine kinds of isomers, after separating, can as product mesitylene, pseudocumene, m-methyl ethylbenzene and p-methyl-ethylbenzene be arranged industrial.Wherein maximum with pseudocumene and mesitylene added value.See that from prior art the difficult point of produce separating trimethylbenzene is to have many materials such as C9 aromatic isomers such as first and second benzene, propyl benzene and butylbenzene in the raw material, the boiling point and the trimethylbenzene of part carbon nine and above aromatic hydrocarbons (first and second benzene, butylbenzene) are very approaching.CN1139095A has invented a kind of from C
9Separate the method produce mesitylene in the BTX aromatics, the first and second benzene weight contents are greater than 22% C
9The BTX aromatics raw material is through after the first rectifying; Contain mesitylene, pseudocumene and neighbour,, the blending fraction section of p-methyl-ethylbenzene is used as reaction raw materials; Add the tert-butyl alcohol, the concentrated sulfuric acid, alchlor and hydrochloric acid as the reaction additive, handle, first and second benzene are converted into high-boiling components through alkylated reaction and sedimentation; Then reactant is carried out rectifying separation, finally obtain purity greater than 98% mesitylene product.The heavy aromatics of reformer generally contains the C except that trimethylbenzene of high level
9Aromatic hydrocarbons, its content are generally greater than 30%, and CN1313269A will need carry out continuous rectification through two packed towers from the heavy aromatics of oil plant reformer and isolate the higher pseudocumene fraction of purity, but can not obtain the higher degree mesitylene.CN1974500A adopts three tower serial flow process counterweight bulk wight aromatic hydrocarbons to separate, but the higher pseudocumene of production purity and the enriched mesitylene of coproduction 35% above purity, and mesitylene purity is lower.Therefore, in the prior art technological process of separation of produced mesitylene and pseudocumene longer, complex process, and yield is lower, production cost is higher, the commercial Application difficulty is big.
Zeolite powder particularly nano zeolite powder can form dust in practical application; Inconvenient operation; There is difficult recovery, is prone to weakness such as inactivation and gathering, also can jeopardize operator's health, because too high pressure drop zeolite powder is not suitable for fixed bed reactors in catalytic reaction yet.Therefore must the zeolite molecular sieve powder be processed the particle with certain mechanical strength and shape; This process often need add binding agent; The binding agent that often adopts 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, causes adsorbance to descend, and effective surface area is reduced.Because binding agent part component can get into zeolite cavity or blocking portion zeolite aperture; Therefore introduced diffusion restriction; Cause adsorption capacity to weaken; The adsorptive selectivity variation; Absorption and desorption rate descend; In catalytic reaction, then cause active the reduction, selectivity descends, and the binding agent composition also may cause some and do not expect the side reaction that takes place.The binder free zeolite molecular sieve is meant and does not contain inert binder in the zeolite molecular sieve particle, the zeolite block of material with definite shape and size that mainly relies 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 bigger, in catalytic reaction, has more performance.
Summary of the invention
Technical problem to be solved by this invention is that hydrotreating catalyst removes scarce capacity to the C9 aromatic except that trimethylbenzene in the low value-added heavy aromatics in the prior art; Rectifying separation trimethylbenzene monomer long flow path from product; Separation difficulty, the cost technical problems of high provides a kind of heavy aromatics hydrocracking to increase production the catalyst of BTX aromatic hydrocarbons and trimethylbenzene; This invention catalyst activity is high; Can the C9 aromatic of effective elimination except that trimethylbenzene, can be from product separating high-purity trimethylbenzene monomer and increase production BTX aromatic hydrocarbons, solved this problem preferably.
For solving the problems of the technologies described above, the technical scheme that the present invention adopts is following: the catalyst of a kind of heavy aromatics hydrocracking raising the output BTX aromatic hydrocarbons and trimethylbenzene comprises by weight percentage:
A) 0.005～0.5 part is selected from noble metal at least a among Pt or the 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 the zeolite weight content is greater than 95%;
Heavy aromatics is carbon nine and above aromatic hydrocarbons, and B is a benzene in the BTX aromatic hydrocarbons, and T is a toluene, and X is an xylenes.
In the technique scheme, the consumption of selecting at least a noble metal among Pt or the Pd in the catalyst for use preferable range by weight percentage is 0.01～0.5 part; The ten-ring zeolite of selecting for use in the catalyst is at least a in ZSM-5 or the ZSM-11 zeolite, the SiO of binder free ten-ring zeolite
2/ Al
2O
3Mol ratio is 20～200; Also contain in the catalyst and be selected from least a among Zn, La, Sn, Pb or the Bi, its consumption is＞0～1 part by weight percentage; Heavy aromatics is from reformate, drippolene, naphtha and catalytically cracked gasoline, the heavy aromatics raw material of preferably reforming.
The binder free zeolite is synthetic with the preparation of sodium type, carries out ion-exchange with acid solutions such as ammonium salt solution or hydrochloric acid then, carries out roasting after the exchange and is converted into h-type zeolite; Introduce at least a metal of Pt or Pd then through ion-exchange or dipping method, use palladium bichloride, palladium nitrate; Ammonium chloropalladate, ammonium chloropalladite, platinum nitrate; Chloroplatinic acid, ammonium chloroplatinate, ammonium chloroplatinite, dichloro four ammoniums close at least a aqueous solution of platinum as precursor.The binder free h-type zeolite is introduced after Pt or the Pd, under less than 200 ℃, carries out drying, at 300-600 ℃ dried catalyst is calcined then.
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 of separating trimethylbenzene is the many materials that have C9 aromatic isomers such as comprising first and second benzene, propyl benzene and butylbenzene in the raw material, and the boiling point and the trimethylbenzene of part carbon nine and above aromatic hydrocarbons (first and second benzene, butylbenzene) are very approaching; The flow process of therefore separating the trimethylbenzene monomer is longer, and complex process is invested big energy consumption height; Product yield is low, and therefore problems such as economic indicator difference are difficult to be used; Separate the purification new technology so develop aromatic hydrocarbons as early as possible, improve and development trimethylbenzene production technology, reduce production costs; Improve the technological competitiveness of homemade trimethylbenzene industry, satisfy 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 the hydrocracking reaction, and many carbon of alkylbenzene carbochain is at first carried out protonated on the B acid site, removes many carbon carbochain through cracking, reacts more or less freely; And on the L acid site, many carbon of alkylbenzene carbochain then be form free radical therefrom between chain rupture, reaction is difficulty comparatively.Binder free Zeolites Zeolites content is high, contains highdensity B acid site, and it is more easy therefore to remove for many carbon carbochain of alkylbenzene.The pore passage structure of zeolite also is vital for the influence of taking off alkyl; Different zeolites has different pore passage structures; Wherein the ten-ring structural zeolite has the very high activity that removes to the ethyl and the propyl group of heavy arene, but only has the conversion ratio of medium trimethylbenzene.In above-mentioned hydrocracking reaction; Can produce such as alkene intermediates such as ethene, propylene, promptly hydrogenation is saturated to prevent that olefinic polymerization from impelling coke to form and causing catalysqt deactivation perhaps to cause the character variation of aromatic component in the product with light aromatics generation alkylated reaction.Therefore, have the hydrogenating function that acid centre is complementary in the catalyst, should contain the metallic element of group VIII in the periodic table of elements with hydrogenation.Metal component Pt or Pd all have good hydrogenation effect, the problem that considered acidity of catalyst center and hydrogenation metal center are complementary and raw material is adapted in Preparation of Catalyst.Acid centre can perhaps be mediated through modification through the silica/alumina mole ratio of adjustment zeolite molecular sieve, and the hydrogenation activity of metal center can be adjusted through the decentralization of content of metal, carried metal.Possibly contain the raw material that suppresses metal hydrogenation performance component for raw material is comparatively complicated; Drippolene raw material such as sulfur compound; Can consider Pt, two kinds of metal composite of Pd together, thereby this all can have good sulfur resistance and keep good hydrogenation performance than independent use Pt, any one metal of Pd.Pt, two kinds of metal composite of Pd can produce electro ultrafiltration or chemical action mutually, rather than separately exist in the catalyst, thereby good hydrogenation and sulfur resistance is provided.Catalyst of the present invention adopts binder free ten-ring zeolite as acidic components; It is big to have sour density, and the characteristics that the aperture is unobstructed, metal hydrogenation component have the characteristics of hydrogenation moderate performance; Can effective elimination first and second benzene, heavy aromatics such as propyl benzene and butylbenzene; Thereby the rectifying separation that helps the trimethylbenzene monomer can be separated obtaining highly purified trimethylbenzene monomer, and can be increased 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 is used for the reaction of heavy aromatics hydrocracking raising the output BTX aromatic hydrocarbons and trimethylbenzene; Mixture with heavy aromatics and hydrogen in fixed bed reactors is a raw material; At Hydrogen Vapor Pressure 2.8MPa, H
2/ oil volume is reacted 360 ℃ of inlet temperatures, weight (hourly) space velocity (WHSV) WHSV=2.0 hour than 400
-1Situation under; In the reaction effluent in the C9 aromatic arene content except that trimethylbenzene less than 0.5%; BTX aromatic hydrocarbons yield reaches 59.2%; Therefore product is separated behind the lighter hydrocarbons to separate through the BTX tower and is obtained the BTX aromatic hydrocarbon product, and the bottoms material only need get into mesitylene tower and pseudocumene tower successively to carry out rectifying and just can isolate purity greater than 98% trimethylbenzene monomer, has obtained better technical effect.
Through embodiment the present invention is done further elaboration below.
The specific embodiment
[embodiment 1～2]
Adhesiveless ZSM-5 zeolite (SiO
2/ Al
2O
3Mol ratio is 60) prepare with reference to Chinese patent CN100384735C; 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 after the exchange and is converted into h-type zeolite.The Pt of dip loading weight ratio meter 0.05% and 0.25% Zn on Hydrogen adhesiveless ZSM-5 zeolite, calcining obtained catalyst a in 4 hours under 450 ℃; The Pd of dip loading weight ratio meter 0.3% and 0.05% Pb on Hydrogen adhesiveless ZSM-5 zeolite, calcining obtained catalyst b in 4 hours under 450 ℃.
[embodiment 3～5]
Adhesiveless ZSM-5 zeolite (SiO
2/ Al
2O
3Mol ratio is 20) prepare with reference to Chinese patent CN100384735C; 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 after the exchange and is converted into h-type zeolite.The Pt of dip loading weight ratio meter 0.005% and 0.01% Sn on Hydrogen adhesiveless ZSM-5 zeolite, calcining obtained catalyst c in 4 hours under 450 ℃; The Pd of dip loading weight ratio meter 0.5%, 0.01% Zn and 1.0% La on Hydrogen adhesiveless ZSM-5 zeolite, 450 ℃ down calcining obtained catalyst d in 4 hours; The Pt of dip loading weight ratio meter 0.03%, 0.02% Bi and 0.2% Sn on Hydrogen adhesiveless ZSM-5 zeolite, 450 ℃ down calcining obtained catalyst e in 4 hours.
[embodiment 6～7]
Binderless ZSM-5-11 zeolite (SiO
2/ Al
2O
3Mol ratio is 45) prepare with reference to Chinese patent CN101348261A; Binderless ZSM-5-11 zeolite the 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 after the exchange and is converted into h-type zeolite.The Pt of dip loading weight ratio meter 0.06% and 0.2% Zn on Hydrogen binderless ZSM-5-11 zeolite, calcining obtained catalyst f in 4 hours under 450 ℃; The Pt of dip loading weight ratio meter 0.2% and 0.20% Bi on Hydrogen binderless ZSM-5-11 zeolite, calcining obtained catalyst g in 4 hours under 450 ℃.
[embodiment 8]
Take by weighing the white carbon black of 250 grams, 100 gram ZSM-5 zeolite (SiO
2/ Al
2O
3Mol ratio is 125), add 12 gram sesbania powder, 16 gram aluminum sulfate [Al
2(SO
4)
318H
2O], 10 gram NaOH mix with the Ludox (percentage by weight 40%) that adds 500 grams again and pinch into cylindric shape and carry out drying.Be that 8% TBAH (TBAOH) solution mixes and places crystallizing kettle under 160 ℃, to carry out hydrothermal treatment consists 4 days with cylindric presoma and the 80 gram mass percentage concentrations of the above-mentioned preparation of 40 grams respectively.Product with the distilled water washing and drying after in air atmosphere in 550 ℃ of roastings.The XRD figure spectrum of product shows that all crystalline phase is a ZSM-5/ZSM-11 cocrystallization zeolite, baseline straightening, the SiO of preparation 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 carries out ion-exchange with preparation product and ammonium nitrate solution, carries out roasting after the exchange and is converted into h-type zeolite.The Pt of dip loading weight ratio meter 0.001% and 0.1% Pd on Hydrogen adhesiveless ZSM-5/ZSM-11 zeolite, calcining obtained catalyst h in 4 hours under 450 ℃.
Use a～h catalyst of reduction activation in fixed bed reactors, to react examination, the heavy aromatics raw material is counted xylenes 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%; 10 hydrocarbon 18.22% that carbon is above.At Hydrogen Vapor Pressure 2.8MPa, H
2/ oil volume is than 400,360 ℃ of inlet temperatures, and weight (hourly) space velocity (WHSV) WHSV is 2.0 hours
-1Reaction result list in table 1.Product is separated behind the lighter hydrocarbons to separate through the BTX tower and is obtained the BTX aromatic hydrocarbon product, and the bottoms material only need get into mesitylene tower and pseudocumene tower successively to carry out rectifying and just can isolate purity greater than 98% trimethylbenzene monomer.
Claims (4)
1. the catalyst of heavy aromatics hydrocracking raising the output BTX aromatic hydrocarbons and trimethylbenzene comprises by weight percentage:
A) 0.005～05 part is selected from noble metal at least a among Pt or the 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 the zeolite weight content is greater than 95%;
Heavy aromatics is carbon nine and above aromatic hydrocarbons, and B is a benzene in the BTX aromatic hydrocarbons, and T is a toluene, and X is an xylenes.
2. according to the catalyst of the said heavy aromatics hydrocracking of claim 1 raising the output BTX aromatic hydrocarbons and trimethylbenzene, it is characterized in that ten-ring zeolite that catalyst is selected for use is at least a in ZSM-5 or the ZSM-11 zeolite.
3. according to the catalyst of said heavy aromatics hydrocracking raising the output BTX aromatic hydrocarbons of claim 1 and trimethylbenzene, it is characterized in that the SiO of binder free ten-ring zeolite
2/ Al
2O
3Mol ratio is 20～200.
4. according to the catalyst of the said heavy aromatics hydrocracking of claim 1 raising the output BTX aromatic hydrocarbons and trimethylbenzene, it is characterized in that also containing in the catalyst and be selected from least a among Zn, La, Sn, Pb or the Bi, its consumption is＞0～1 part by weight percentage.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104148104A (en) * | 2013-05-16 | 2014-11-19 | 中国石油化工股份有限公司 | Catalyst and method of cracked gasoline hydrogenation |
| 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 |
| CN104399520A (en) * | 2014-11-11 | 2015-03-11 | 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 |
| CN105233862A (en) * | 2014-07-11 | 2016-01-13 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst and preparation method therefor |
| CN105582988A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Cyclohexylbenzene catalyst |
| CN105582990A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Catalyst for producing cyclohexylbenzene |
| 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 |
| WO2022083526A1 (en) * | 2020-10-19 | 2022-04-28 | 中国石油化工股份有限公司 | Chemical hydrocracking catalyst, preparation method therefor, and application thereof |
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| CN104148104A (en) * | 2013-05-16 | 2014-11-19 | 中国石油化工股份有限公司 | Catalyst and method of cracked gasoline hydrogenation |
| CN105233862A (en) * | 2014-07-11 | 2016-01-13 | 中国石油化工股份有限公司 | Cyclohexyl benzene catalyst and preparation method therefor |
| 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 |
| CN105582990B (en) * | 2014-10-24 | 2018-06-08 | 中国石油化工股份有限公司 | Cyclohexyl benzene production catalyst |
| CN105582988A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Cyclohexylbenzene catalyst |
| CN105582990A (en) * | 2014-10-24 | 2016-05-18 | 中国石油化工股份有限公司 | Catalyst for producing cyclohexylbenzene |
| CN104399520A (en) * | 2014-11-11 | 2015-03-11 | 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 |
| WO2022083526A1 (en) * | 2020-10-19 | 2022-04-28 | 中国石油化工股份有限公司 | Chemical hydrocracking catalyst, preparation method therefor, and application thereof |
| CN114433211A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Chemical hydrocracking catalyst and preparation method and application thereof |
| 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 |
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