CN104549471A - Catalyst for converting C10<+> heavy aromatics into mononuclear aromatics and preparation method of catalyst - Google Patents
Catalyst for converting C10<+> heavy aromatics into mononuclear aromatics and preparation method of catalyst Download PDFInfo
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- CN104549471A CN104549471A CN201310512609.2A CN201310512609A CN104549471A CN 104549471 A CN104549471 A CN 104549471A CN 201310512609 A CN201310512609 A CN 201310512609A CN 104549471 A CN104549471 A CN 104549471A
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- 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
Abstract
The invention relates to a catalyst for converting C10<+> heavy aromatics into mononuclear aromatics and a preparation method of the catalyst, and mainly aims to solve the problems of low heavy conversion level of heavy aromatics, low yield and selectivity of mononuclear aromatics and high deactivation rate of catalyst in the prior art. The problems can be solved by adopting a technical scheme that the catalyst is prepared from the following components in percentage by weight: 30-60 percent of mixture of BEA-type zeolite and ZSM-12 molecular sieve, 39.5-69.9 percent of at least one of gamma-alumina, eta-alumina and pseudo-boehmite serving as adhesive and 0.1-0.5 part of at least one metal or metal oxide of Pt, Pd and Ir. The catalyst can be used in industrial production for converting C10<+> heavy polycyclic aromatic hydrocarbon into mononuclear aromatics.
Description
Technical field
The present invention relates to a kind of C
10 +heavy aromatics is converted into the Catalysts and its preparation method of mononuclear aromatics.
Background technology
Heavy aromatics refers to the C of by-product in oil and the coal course of processing
9above aromatic hydrocarbons, its main source has following 5 kinds: refinery catalytic reforming unit by-product C
9heavy aromatics; Polyester raw material factory wide fraction catalytic reforming unit by-product C
10heavy aromatics; Ethylene unit by-product C
9or C
10heavy aromatics: ethylene unit by-product ethylene bottom oil; Coal high-temperature coking by-product heavy aromatics-coal tar.The composition of heavy aromatics is very complicated, wherein C
10heavy aromatics about has 100 various ingredients altogether.Current heavy aromatics is through simple distillation operation, isolate the higher durol of value, isodurene, naphthalene, methylnaphthalene etc., all the other small parts are for the production of solvent oil or the blending component as gasoline, major part is used as fuel at a low price, raw material availability is low, both wastes resource, also serious environment pollution, infringement HUMAN HEALTH, is difficult to play the due economic benefit of Heavy Aromatic Hydrocarbons.Along with the continuous intensification of oil product degree of heaviness and the finiteness of world petroleum resource, for meeting the growth of the petroleum demand that Economic development brings, by development heavy oil deep conversion technology, the light-end products of volume increase high added value will be the significant development strategies of 21 century oil refining industry.Domestic and international industrialized technique at present, actual treatment heavy aromatics, particularly C
10and the ability of above heavy aromatics still is apparent not enough, following technique research and development should as emphasis.Through development for many years, as the important technology hydrotreatment by heavy aromatic hydrocarbon light, although at present there is the advantages such as adaptability to raw materials is wide, depth of conversion is large, but also there is temperature of reaction and pressure is high, air speed is low, consumption hydrogen is large, catalyst life is short etc. weak point, these also become the emphasis that domestic and international research institution breaks through.
USP4,341,622 disclose a kind of method utilizing heavy reformate to produce BTX.The method employing restricted index is 1 ~ 12, silica/alumina molar ratio (silica alumina ratio) is more than 12, the zeolite of low acid activity is catalyzer, reformate is reacted under the condition of 427 ~ 540 DEG C, then resultant fractionation by distillation is obtained benzene, toluene and dimethylbenzene.Described catalyzer contains the VIII precious metal of hydro-dealkylation function, preferred platinum, and the silica alumina ratio of zeolite used is preferably greater than 200, and more preferably greater than 500, preferred zeolite is ZSM-5.Selecting the zeolite of high silica alumina ratio for reducing zeolite acidity, retaining dimethylbenzene as far as possible and not being converted in the reaction.
US2007062848A1 discloses and a kind ofly first will carry out selective opening and de-alkyl after polycyclic aromatic hydrocarbons fractional saturation again to obtain the method for light aromatics.The method can to meet in feed stream polycyclic aromatic hydrocarbon content at more than 20wt%, saturation stage temperature at 300 ~ 500 DEG C, pressure 2 ~ 10MPa; Open loop phase temperature at 200 ~ 600 DEG C, pressure 1 ~ 12MPa.Because two-stage catalytic agent is contained in same reactor, so require that logistics needs to ensure that certain residence time could obtain good transformation efficiency, therefore air speed is lower.
CN1270989A discloses a kind of containing C
9 +heavy arenes lightening catalyst and product separation method, described catalyzer is made up of group VIII metal, the zeolite with MOR structure of 20 ~ 59 heavy %, the zeolite of the MFI structure of 20 ~ 50 heavy % and the aluminum oxide of 20 ~ 40 heavy % of 0.05 ~ 0.3 % by weight.Described method be by heavy arene 350 ~ 450 DEG C, under 0.5 ~ 3.5MPa condition with above-mentioned catalyst exposure, gained lighting product can obtain the organic raw material such as BTX and sym-trimethylbenzene, unsym-trimethyl benzene, durol through fractionation.
CN1934058A discloses a kind of by indane and C
10deng polycyclic aromatic hydrocarbons transform and transalkylation be C
8the method of aromatic hydrocarbons, the catalyzer that the method uses comprises solid acid carrier (as: mordenite) and metal component (as: rhenium), produces valuable dimethylbenzene by this method.
Summary of the invention
One of technical problem to be solved by this invention is to overcome the catalyzer that exists in prior art for C
10 +heavy aromatics depth of conversion is low, and the low and selectivity of mononuclear aromatics yield is low, the problem that catalyst deactivation rate is fast, provide a kind of newly for C
10 +heavy aromatics is converted into the catalyzer of mononuclear aromatics.This catalyzer is used for C
10 +heavy aromatics is converted into the reaction of mononuclear aromatics, has heavy aromatics depth of conversion high, and yield and the selectivity of mononuclear aromatics are high, the advantage that catalyst deactivation rate is slow.
Two of technical problem to be solved by this invention is to provide a kind of C corresponding with one of technical solution problem
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics.
Three of technical problem to be solved by this invention is to provide a kind of C corresponding with one of technical solution problem
10 +heavy aromatics is converted into the purposes of the catalyzer of mononuclear aromatics.
For one of solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of C
10 +heavy aromatics is converted into the catalyzer of mononuclear aromatics, in catalyst weight percent, comprises following component:
A) mixture of 30 ~ 60% BEA type zeolites and ZSM-12 molecular sieve;
B) 39.5 ~ 69.9% at least one be selected from gama-alumina, η-aluminum oxide or pseudo-boehmite are binding agent;
C) 0.1 ~ 0.5% at least one metal in Pt, Pd or Ir or its oxide compound is selected from.
In technique scheme, in used catalyst composition, BEA type zeolite and ZSM-12 molecular sieve are Hydrogen or ammonium type, and sodium weight content is lower than 2%; In mixture, the amount preferable range of BEA type zeolite is the amount preferable range of 10 ~ 90%, ZSM-12 molecular sieve is by weight percentage 10 ~ 90%.
For solve the problems of the technologies described above two, the technical solution used in the present invention is as follows: a kind of C
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, comprises the following steps:
1., after the binding agent of at least one be selected from gama-alumina, η-aluminum oxide, pseudo-boehmite of the BEA type zeolite of aequum and the mixture of ZSM-12 molecular sieve and aequum being carried out kneading, shaping, drying, support of the catalyst is obtained at 450 ~ 650 DEG C of roasting 0.5 ~ 24h;
2. the precursor solution being selected from least one metal in Pt, Pd or Ir or its oxide compound of aequum is impregnated into 0.5 ~ 24h in support of the catalyst in 30 ~ 50 DEG C, obtains finished catalyst at 300 ~ 450 DEG C of roasting 0.5 ~ 24h after drying.
In technique scheme, in catalyst support preparation process, preferred version is, adds and presses the extrusion aid of carrier dry basis 2 ~ 5%, and extrusion aid is at least one in sesbania powder or tung oil; Add and press the gelatinizing agent of carrier dry basis 3 ~ 6%, gelatinizing agent is selected from least one in hydrochloric acid, nitric acid, acetic acid, tartrate, citric acid or oxalic acid and water volume ratio 1:1 ~ 1:5.
The precursor solution preferred version of Pt metal used in technique scheme is Platinic chloride; The precursor solution preferred version of metal Pd is at least one in Palladous nitrate or Palladous chloride; The precursor solution preferred version of metal Ir is chloro-iridic acid.
For solve the problems of the technologies described above three, the technical solution used in the present invention is as follows: a kind of C
10 +heavy aromatics is converted into the method for mononuclear aromatics, and raw material heavy aromatics mixture mixes with hydrogen, passes through beds, at temperature of reaction 350 ~ 420 DEG C, reaction pressure 4 ~ 7 MPa, weight hourly space velocity degree 1 ~ 8 hr
-1, under hydrogen/hydrocarbon mol ratio 4.0 ~ 8.0 condition with above-mentioned catalyst exposure described in any one, C
10 +heavy aromatics is converted into the mononuclear aromatics comprising benzene,toluene,xylene.
In technique scheme, preferred technical scheme is, temperature of reaction is 350 ~ 400 DEG C, reaction pressure is 5 ~ 6 MPa, weight hourly space velocity degree is 1 ~ 2 hr
-1, hydrogen/hydrocarbon mol ratio is 6.0 ~ 7.0.
Catalyzer provided by the invention is a kind of for C
10 +heavy polycyclic aromatic hydrocarbons is converted into the catalyzer of mononuclear aromatics, can be used for producing in the industrial production of benzene, toluene and dimethylbenzene.
Owing to have selected BEA zeolite containing 12 ring macropores and ZSM-12 molecular sieve as catalyst acid center in the present invention, be conducive to the acid site that heavy arene macromole enters in duct and carry out ring-opening reaction, product molecule after conversion can passing hole channel rapid diffusion, thus has delayed the deactivation rate of catalyzer; Be there is by load the precious metal element of hydrogenating function, control its charge capacity at a zone of reasonableness, not only protect acid site but also effectively improve the degree of unsaturation of heavy Polycyclic Aromatic Hydrocarbon Mixture raw material, help deep conversion heavy aromatics; The rational proportion of catalyst acid center and metallic element makes to remain original mononuclear aromatics component in feedstream in reaction process and to greatest extent polycyclic aromatic hydrocarbons is converted into mononuclear aromatics, maximize with the yield and selectivity that make mononuclear aromatics, achieve good technique effect.
The present invention uses overcritical fixed-bed reactor to carry out C
10 +the reactivity worth that heavy aromatics is converted into mononuclear aromatics is investigated, reactor inside diameter Ф 12 millimeters, length 800 millimeters, stainless steel.Adopt electrically heated, temperature automatic control.It is upholder that reactor bottom fills Ф 2 ~ 3 millimeters of granulated glass spherees, catalyst filling 5 grams in reactor, and Ф 2 ~ 3 millimeters of granulated glass spherees are filled on top, is made for the use of raw material preheating and vaporization.Raw material C
10 +heavy aromatics mixture mixes with hydrogen, passes through beds, at temperature of reaction 350 ~ 420 DEG C, reaction pressure 4 ~ 7 MPa, weight hourly space velocity degree 1 ~ 8 hr
-1, hydrogen/hydrocarbon mol ratio 4.0 ~ 8.0 condition under contact with catalyzer, make heavy aromatics be converted into the mononuclear aromatics such as benzene,toluene,xylene.
Heavy aromatics mixture provides for Plant of Tianjin Petrochemical Company aromatic hydrocarbons factory, and experimental data is calculated as follows.
Below by embodiment, the present invention is further elaborated.
Embodiment
[embodiment 1]
Be 25 g BEA types zeolite (being purchased ammonium type), 25 g ZSM-12 molecular sieves (being purchased Hydrogen) and 50 g γ-Al by butt
2o
3(industrial goods) add mixing tank to evenly, in mixture, then add 3 g sesbania powder, 5 g volume ratio 1:1 HNO
3solution and 40 g deionized waters, the dough being suitable for extruding evenly is made in grinding.It extruded by mould, shape is elongated cylindrical (diameter 1.7 mm), in 550 DEG C of roasting 4 h after 120 DEG C of oven dry, is then cut into the carrier granule (1.7 × 4.0 mm) of consistent size, is designated as Z1.
Flooded carrier granule at 40 DEG C by Platinic chloride wiring solution-forming, the amount containing Pt in steeping fluid is 0.2% of carrier butt weight, and dipping 8h also after drying, at 450 DEG C of roasting 3 h, obtains finished catalyst A.
[embodiment 2 ~ 10]
The preparation method provided according to embodiment 1 and process, by changing the contamination of metal precursor in carrier composition and steeping fluid, prepared a series of finished catalyst, in table 1.
Table 1
[embodiment 11-19]
Catalyst A ~ the J on overcritical fixed-bed reactor (highest response pressure 10MPa, use temperature be room temperature ~ 600 DEG C) obtained by embodiment 1 ~ 10 investigates C
10 +heavy aromatics mixture is converted into the ability of the mononuclear aromatics such as BTX (wherein B is benzene, and T is toluene, and X is dimethylbenzene).Table 2 is Tianjin heavy aromatics raw material composition.Catalyst loading 5 g, at temperature of reaction 350 DEG C, reaction pressure 5.0MPa, weight hourly space velocity degree 2.5hr
-1, contact with catalyzer under hydrogen/hydrocarbon mol ratio 5.5 condition, product to be reclaimed and component detects, conversion results is shown in Table 3.
Table 2
| Raw material forms | Toluene | C 10 | C 11 | C 12 | >C 12 |
| Content (wt%) | 0.01 | 18.61 | 32.18 | 23.34 | 25.87 |
Table 3
| Catalyzer is numbered | Total conversion rate (wt%) | Mononuclear aromatics selectivity (wt%) | BTX selectivity (wt%) |
| A | 68.3 | 70.2 | 45.2 |
| B | 70.5 | 69.4 | 44.9 |
| C | 65.8 | 71.5 | 46.3 |
| D | 74.1 | 70.0 | 45.1 |
| E | 73.5 | 69.1 | 44.5 |
| F | 68.6 | 72.3 | 47.0 |
| G | 75.8 | 68.2 | 44.1 |
| H | 65.4 | 75.3 | 48.6 |
| I | 62.0 | 75.9 | 49.1 |
| J | 76.3 | 67.4 | 43.8 |
[embodiment 20 ~ 24]
Catalyst A ~ the E obtained by embodiment 1 ~ 5 investigates C on overcritical fixed-bed reactor
10 +heavy aromatics mixture is converted into the ability of the mononuclear aromatics such as BTX.Catalyst loading 5 g, at temperature of reaction 380 DEG C, reaction pressure 6MPa, weight hourly space velocity degree 1.5 hr
-1, contact with catalyzer under hydrogen/hydrocarbon mol ratio 6.0 condition, product to be reclaimed and component detects, conversion results is shown in Table 4.
Table 4
| Catalyzer is numbered | Total conversion rate (wt%) | Mononuclear aromatics selectivity (wt%) | BTX selectivity (wt%) |
| A | 71.2 | 73.6 | 44.9 |
| B | 72.9 | 72.0 | 44.5 |
| C | 69.8 | 75.4 | 46.3 |
| D | 77.6 | 69.9 | 42.8 |
| E | 75.4 | 70.1 | 43.7 |
[embodiment 25 ~ 29]
Catalyst A ~ the E obtained by embodiment 1 ~ 5 investigates C on overcritical fixed-bed reactor
10 +heavy aromatics mixture is converted into the ability of the mononuclear aromatics such as BTX.Catalyst loading 5 g, at temperature of reaction 370 DEG C, reaction pressure 5MPa, weight hourly space velocity degree 2.0hr
-1, contact with catalyzer under hydrogen/hydrocarbon mol ratio 6.0 condition, product to be reclaimed and component detects, conversion results is shown in Table 5.
Table 5
| Catalyzer is numbered | Total conversion rate (wt%) | Mononuclear aromatics selectivity (wt%) | BTX selectivity (wt%) |
| A | 68.5 | 73.0 | 46.3 |
| B | 68.9 | 72.5 | 46.0 |
| C | 65.2 | 75.1 | 48.3 |
| D | 71.7 | 72.0 | 45.2 |
| E | 71.0 | 71.2 | 47.1 |
[embodiment 30 ~ 34]
Catalyst A ~ the E obtained by embodiment 1 ~ 5 investigates C on overcritical fixed-bed reactor
10 +heavy aromatics mixture is converted into the ability of the mononuclear aromatics such as BTX.Catalyst loading 5 g, at temperature of reaction 370 DEG C, reaction pressure 6MPa, weight hourly space velocity degree 2.0 hr
-1, contact with catalyzer under hydrogen/hydrocarbon mol ratio 6.0 condition, product to be reclaimed and component detects, conversion results is shown in Table 6.
Table 6
| Catalyzer is numbered | Total conversion rate (wt%) | Mononuclear aromatics selectivity (wt%) | BTX selectivity (wt%) |
| A | 68.0 | 73.2 | 46.0 |
| B | 68.6 | 72.8 | 45.6 |
| C | 65.1 | 75.5 | 47.9 |
| D | 71.3 | 71.3 | 44.1 |
| E | 70.4 | 70.6 | 46.2 |
[embodiment 35 ~ 39]
Catalyst A ~ the E obtained by embodiment 1 ~ 5 investigates C on overcritical fixed-bed reactor
10 +heavy aromatics mixture is converted into the ability of the mononuclear aromatics such as BTX.Catalyst loading 5 g, at temperature of reaction 370 DEG C, reaction pressure 6MPa, weight hourly space velocity degree 1.5 hr
-1, contact with catalyzer under hydrogen/hydrocarbon mol ratio 6.0 condition, product to be reclaimed and component detects, conversion results is shown in Table 7.
Table 7
| Catalyzer is numbered | Total conversion rate (wt%) | Mononuclear aromatics selectivity (wt%) | BTX selectivity (wt%) |
| A | 70.0 | 72.9 | 45.3 |
| B | 71.5 | 71.5 | 45.5 |
| C | 67.7 | 73.8 | 47.1 |
| D | 74.1 | 70.0 | 43.6 |
| E | 72.9 | 69.4 | 45.0 |
Claims (10)
1. a C
10 +heavy aromatics is converted into the catalyzer of mononuclear aromatics, in catalyst weight percent, comprises following component:
A) mixture of 30 ~ 60% BEA type zeolites and ZSM-12 molecular sieve;
B) 39.5 ~ 69.9% at least one be selected from gama-alumina, η-aluminum oxide or pseudo-boehmite are binding agent;
C) 0.1 ~ 0.5% at least one metal in Pt, Pd or Ir or its oxide compound is selected from.
2. C according to claim 1
10 +heavy aromatics is converted into the catalyzer of mononuclear aromatics, and it is characterized in that BEA type zeolite and ZSM-12 molecular sieve are Hydrogen or ammonium type, sodium weight content is lower than 2%.
3. C according to claim 1
10 +heavy aromatics is converted into the catalyzer of mononuclear aromatics, it is characterized in that the amount of BEA type zeolite by weight percentage in mixture be the amount of 10 ~ 90%, ZSM-12 molecular sieve is 10 ~ 90%.
4. C according to claim 1
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, comprises the following steps:
1., after the binding agent of the BEA type zeolite of aequum and the mixture of the ZSM-12 molecular sieve of aequum and at least one be selected from gama-alumina, η-aluminum oxide or pseudo-boehmite of aequum being carried out kneading, shaping, drying, support of the catalyst is obtained at 450 ~ 650 DEG C of roasting 0.5 ~ 24h;
2. the precursor solution being selected from least one metal in Pt, Pd or Ir or its oxide compound of aequum is impregnated into 0.5 ~ 24h in support of the catalyst in 30 ~ 50 DEG C, obtains finished catalyst at 300 ~ 450 DEG C of roasting 0.5 ~ 24h after drying.
5. C according to claim 4
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, it is characterized in that the extrusion aid added in catalyst support preparation process by carrier dry basis 2 ~ 5% weight; Adding at least one acid solution be selected from hydrochloric acid, nitric acid, acetic acid, tartrate, citric acid or oxalic acid in catalyst support preparation process is gelatinizing agent.
6. C according to claim 5
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, it is characterized in that extrusion aid is at least one in sesbania powder or tung oil.
7. C according to claim 5
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, it is characterized in that by carrier dry basis, the gelatinizing agent of add in catalyst support preparation process 3 ~ 6 % by weight, in gelatinizing agent, the volume ratio being selected from least one in hydrochloric acid, nitric acid, acetic acid, tartrate, citric acid or oxalic acid and water is 1:1 ~ 1:5.
8. C according to claim 4
10 +heavy aromatics is converted into the preparation method of the catalyzer of mononuclear aromatics, it is characterized in that the precursor solution of described Pt metal is Platinic chloride; The precursor solution of metal Pd is at least one in Palladous nitrate or Palladous chloride; The precursor solution of metal Ir is chloro-iridic acid.
9. a C
10 +heavy aromatics is converted into the method for mononuclear aromatics, and raw material heavy aromatics mixture mixes with hydrogen, passes through beds, at temperature of reaction 340 ~ 420 DEG C, reaction pressure 4 ~ 7 MPa, weight hourly space velocity degree 1 ~ 8 hr
-1, under hydrogen/hydrocarbon mol ratio 4.0 ~ 8.0 condition with catalyst exposure described in any one in claim 1 ~ 3, C
10 +heavy aromatics is converted into the mononuclear aromatics comprising benzene,toluene,xylene.
10. C according to claim 9
10 +heavy aromatics is converted into the method for mononuclear aromatics, it is characterized in that temperature of reaction 350 ~ 400 DEG C, reaction pressure 5 ~ 6MPa, weight hourly space velocity degree 1 ~ 2 hr
-1, hydrogen/hydrocarbon mol ratio 6.0 ~ 7.0 condition under with catalyst exposure.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106588534A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Method for transalkylation and hydrocracking of aromatic hydrocarbon |
| CN107115887A (en) * | 2017-06-19 | 2017-09-01 | 中国海洋石油总公司 | A kind of method for preparing catalyst for being used to crack heavy aromatics |
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|---|---|---|---|---|
| US5763720A (en) * | 1995-02-10 | 1998-06-09 | Mobil Oil Corporation | Transalkylation process for producing aromatic product using a treated zeolite catalyst |
| CN101045208A (en) * | 2006-03-27 | 2007-10-03 | 中国石油化工股份有限公司 | Dealkylation and alkyl-transfering catalyst for C9 or more heavy aromatic hydrocarbons |
| CN103121912A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing dimethylbenzene through methylation and transalkylation |
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2013
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US5763720A (en) * | 1995-02-10 | 1998-06-09 | Mobil Oil Corporation | Transalkylation process for producing aromatic product using a treated zeolite catalyst |
| CN101045208A (en) * | 2006-03-27 | 2007-10-03 | 中国石油化工股份有限公司 | Dealkylation and alkyl-transfering catalyst for C9 or more heavy aromatic hydrocarbons |
| CN103121912A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing dimethylbenzene through methylation and transalkylation |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106588534A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Method for transalkylation and hydrocracking of aromatic hydrocarbon |
| CN106588534B (en) * | 2015-10-19 | 2021-08-03 | 中国石油化工股份有限公司 | Process for transalkylation and hydrocracking of aromatic hydrocarbons |
| CN107115887A (en) * | 2017-06-19 | 2017-09-01 | 中国海洋石油总公司 | A kind of method for preparing catalyst for being used to crack heavy aromatics |
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Application publication date: 20150429 |