CN104357083B - A kind of C10+heavy aromatics hydrogenation lightening method - Google Patents
A kind of C10+heavy aromatics hydrogenation lightening method Download PDFInfo
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- CN104357083B CN104357083B CN201410642474.6A CN201410642474A CN104357083B CN 104357083 B CN104357083 B CN 104357083B CN 201410642474 A CN201410642474 A CN 201410642474A CN 104357083 B CN104357083 B CN 104357083B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of C10 +Heavy aromatics hydrogenation lightening method.It is characterized in that: heavy aromatics raw material, after heating furnace preheating carries out air-fuel mixture with hydrogen, passes sequentially through two tandem reactors and carries out that pre-hydrogenation is saturated to react with hydrocracking respectively；Product isolates benzene, toluene and low-carbon alkanes mixture through a step rectifying, and materials at bottom of tower isolates C through rectifying again8～C9Before the thick product of aromatic hydrocarbons or 205 DEG C, light ends is for high-knock rating gasoline blend component, heavy distillat circular response at the bottom of tower.The method can be used for processing refinery's reformer or the C of steam cracking device by-product10 +Heavy aromatics, the light aromatics of volume increase high added value or high-knock rating gasoline blend component.It is high that the method that the present invention provides has heavy aromatics activity of conversion in technique, and catalyst stability is good, product feature flexibly.
Description
Technical field
The invention belongs to petrochemical industry, be specifically related to a kind of C10 +Heavy aromatics hydrogenation lightening method.
Background technology
Plant catalytic reformation, ethylene cracker and the coal high-temperature coking substantial amounts of C of device by-product9、C10And above heavy aromatics.At present, except C9Aromatic hydrocarbons (a small amount of C10Aromatic hydrocarbons) can be used for transalkylation reaction and prepare outside Mixed XYLENE, C10And the component that in above heavy aromatics, economic worth is bigger only accounts for about 8%.Typically through simple distillation operation, isolating the higher durol of value, naphthalene, methyl naphthalene etc., remaining small part is for producing solvent naphtha or the blending component as gasoline, and major part is used as fuel at a low price, has the C of 20%～30% simultaneously10Heavy aromatics is converted into heavy oil residue.According to existing C10 +The production management planning of heavy aromatics, raw material availability is low, has both wasted resource, and also serious environment pollution is difficult to play the due economic benefit of Heavy Aromatic Hydrocarbons.
Patent CN102746093 discloses a kind of heavy aromatics hydrocracking volume increase BTX aromatic hydrocarbons and the method for trimethylbenzene, use the Hydrogen binder free ten-ring zeolite catalyst filling reactor of Supported Pt Nanoparticles or palladium, in reaction temperature 320～420, DEG C pressure 2.4～3.5MPa, weight (hourly) space velocity (WHSV) 1.0～3.0h-1, hydrogen hydrocarbon mol ratio 4～8:1 reaction condition under selective hydrogenation cracking C in addition to trimethylbenzene9Aromatic hydrocarbons, increases production BTX, and separates trimethylbenzene product from product.This technique is for C9The heavy aromatics being main has good conversion activity and increment meaning, but is limited by molecular sieve pore passage size used, inapplicable and C10The hydrotreating of above heavy aromatics, it is impossible to realize C10The higher value application of above heavy aromatics.
Patent CN101885663 discloses a kind of heavy aromatics lighting and the method for transalkylation, uses ZSM-5/ beta nuclear shell-shaped molecular sieve catalyst, processes C9And C10 +Aromatic hydrocarbons mixed proportion is the heavy aromatics of 80:20, C9Above aromatics conversion rate reaches more than 40%, BTX selective about 55%.Catalyst and technique that the method is provided have preferable heavy aromatics activity of conversion and BTX selectivity, but it can process C in raw material10 +Ratio is the most relatively low, less to the adverse effect of catalyst activity and stability, and technique range of application is limited.
From prior art it can be seen that more cheap C10 +Heavy aromatics realizes, by lighting technique, the developing direction that higher value application is this technology.
Patent CN103551187 discloses a kind of catalyst producing toluene and C8 aronmatic and its preparation method and application, uses the catalyst of MOR zeolite and ZSM-5 zeolite carried noble metal realize the lighting of heavy aromatics by the transalkylation reaction of benzene Yu heavy aromatics under facing hydrogen state and produce toluene.Use this technique to C10 +Heavy aromatics raw material carries out lighting reaction, C10 +Conversion ratio and C8The yield of aromatic hydrocarbons is the highest, demonstrates good activity and selectivity, but this technique uses benzene to feed intake close to 1:1 with heavy aromatics, benzene consumption is big, and because benzene is carcinogen, when using in a large number as raw material, once occur leakage environment and people can be caused bigger infringement；On the other hand, owing to ZSM-5 zeolite acidity is relatively strong, when in raw material, condensed-nuclei aromatics content is higher, catalyst easily carbon distribution coking, cause catalyst activity rapid decrease.
Summary of the invention
For the deficiencies in the prior art, the present invention provides a kind of C10 +Heavy aromatics hydrogenation lightening method, by the hydrogenation lighting of heavy aromatics is increased production light aromatics or high-knock rating gasoline blend component, improves C10 +The value of heavy aromatics, and solve in existing technique C in handled raw material10 +Heavy aromatics content is low and the problem of catalyst activity poor stability.
One C of the present invention10 +Heavy aromatics hydrogenation lightening method, comprises the following steps:
a.C10 +After heavy aromatics raw material and hydrogen carry out air-fuel mixture, enter pre-hydrogenator, contact the pre-hydrogenation saturated reaction carrying out polycyclic aromatic hydrocarbon with catalyst for pre-hydrogenation；Wherein pre-hydrotreating reaction condition is: hydrogen dividing potential drop 1.0～6.0MPa, bed middle portion temperature 280～420, DEG C volume space velocity 0.1～3.0h-1, hydrogen hydrocarbon volume ratio 200～1500；
B. the effluent of step a is directly entered hydrocracking reactor, contacts saturated, the open loop of tetrahydrochysene naphthalene and its derivative of hydrogenation and the cleavage reaction of branched mononuclear aromatics side chain carrying out single multi-PAH with hydrocracking catalyst；Hydrocracking reaction condition is: hydrogen dividing potential drop 1.0～6.0MPa, bed middle portion temperature 300～450, DEG C volume space velocity 0.1～3.0h-1, hydrogen hydrocarbon volume ratio be 200～1500；
C. the effluent of step b is after gas-liquid separation, enters a rectifying column and separates, obtains the mixture of low-carbon alkanes, benzene and toluene, described mixture further isolated benzene and toluene after separation from tower top；Materials at bottom of tower enters No. two rectifying columns and separates, and tower top obtains C8～C9Before the thick product of aromatic hydrocarbons or 205 DEG C, light ends is as high-knock rating gasoline blend component, and tower bottom divides heavy distillat to loop back reaction system to continue reaction, and part heavy distillat is discharged.
The above-mentioned C of the present invention10 +Heavy aromatics hydrogenation lightening method, described catalyst for pre-hydrogenation is preferably by macropore γ-Al2O3Making as one or more in carrier loaded VIII, group vib and VIIB race base metal, wherein tenor is 1～20wt%, and remaining is γ-Al2O3；The preferred Ni of described group VIII metal, group vib metal preferred Cr, Mo, W, the preferred Mn of VIIB race metal；Described hydrocracking catalyst by one or more in beta-molecular sieve, Y molecular sieve and modenite as carrier loaded VIII precious metals pt or/and Pd makes, wherein tenor is 0.05～2.0wt%, molecular sieve content is 5～95wt%, and remaining is adhesive.
The above-mentioned C of the present invention10 +Heavy aromatics hydrogenation lightening method, described C10 +Heavy aromatics is from the heavy aromatics cut of refinery's reformer or steam cracking device by-product；C10 +20 DEG C of density of heavy aromatics raw material are 0.90～0.99g/cm3, arene content is not less than 95%, and wherein dicyclo and above arene content are not less than 40%.
The above-mentioned C of the present invention10 +Heavy aromatics hydrogenation lightening method, described pre-hydrotreating reaction condition is preferably: hydrogen dividing potential drop 2.0～5.0MPa, bed middle portion temperature 300～360, DEG C volume space velocity 0.5～2.0h-1, hydrogen hydrocarbon volume ratio be 500～1000.Described hydrocracking reaction condition is preferably: hydrogen dividing potential drop 2.0～5.0MPa, bed middle portion temperature 320～380, DEG C volume space velocity 0.5～2.0h-1, hydrogen hydrocarbon volume ratio be 500～1000.
Compared with prior art, the heavy aromatics hydrogenation lightening method that the present invention provides has a characteristic that
1, C can be processed10 +Content heavy aromatics raw material more than 95%, and without mixing lightweight material.
2, introduce pre-hydrotreating section, use hydrogenation catalyst part C in low middle pressure counterweight aroamtic hydrocarbon raw material of alumina support load base metal active component10And above polycyclic aromatic hydrocarbon to carry out pre-hydrogenation saturated, reduce polycyclic aromatic hydrocarbon ratio, improve mononuclear aromatics ratio, the charging of more high-quality is provided for cracking section catalyst, reduces the speed of hydrocracking catalyst carbon distribution coking, improve catalyst activity and stability.
3, use base metal to be hydrogenated with saturated-noble metal hydrogenation catalyst for cracking combination in advance, improve C10And the selectivity of the light aromatics such as the high conversion of above component and BTX.
4, product can separate low temperature fraction (comprising the products such as liquefied gas, benzene and toluene) by follow-up separation process, isolates C from midbarrel8～C9Aromatic hydrocarbon product or cut out 205 DEG C of front-end volatiles as high-knock rating gasoline blend component, product is flexible.
The C that the present invention provides10 +The heavy aromatics hydrogenation accessible technique effect of lightening method is as follows:
It is hydrogenated with saturated-hydrocracking single hop tandem process and two follow-up step separating technologies designs by pre-in this method, the most preferably with base metal catalyst for pre-hydrogenation and noble metal hydrogenation catalyst for cracking with the use of, with refinery's reformer or the C of steam cracking device by-product10 +Heavy aromatics cut is raw material, carries out lighting reaction, can make C under mesolow10 +Conversion per pass reaches 55%～60%, and total conversion can reach 77%～84%；Wherein C8～C9Arenes selectivity is 47%～56%, and before 205 DEG C, high-knock rating gasoline blend component yield can reach more than 68%.
Accompanying drawing explanation
Fig. 1 is C10 +The process flow diagram of heavy aromatics hydrogenation lightening method；
Fig. 2 is C10 +Heavy aromatics hydrogenation lighting reactivity stability data figure.
Wherein: 1 is C10 +Heavy aromatics and new hydrogen mixing raw material, 2 is pre-hydrogenator, and 3 is hydrocracking reactor, 4 lighting products, and 5 is high-pressure separator, and 6 is circulating hydrogen, and 7 is product liquid, and 8 is a rectifying column, and 9 is the mixture of low-carbon alkanes, benzene and toluene, and 10 is C8And above aromatic hydrocarbons, 11 is No. two rectifying columns, and 12 is 205 DEG C of front-end volatiles or C8～C9Aromatic hydrocarbons, 13 is for heavy distillat at the bottom of the part tower of circular response, and 14 is heavy distillat at the bottom of the part tower discharged.
Detailed description of the invention
C of the present invention is further illustrated below in conjunction with the accompanying drawings with embodiment10 +The detailed process of heavy aromatics hydrogenation lightening method and technique effect.
As it is shown in figure 1, heavy aromatics raw material and new hydrogen mixture material 1 enter pre-hydrogenator 2, contact with catalyst for pre-hydrogenation, at the macropore γ-Al being loaded with activity non-noble metal components2O3The pre-hydrogenation saturated reaction of dicyclo and above aromatic hydrocarbons is carried out in duct, reaction effluent is directly entered hydrocracking reactor 3, contact with the noble metal hydrogenation decomposition agent of acidic molecular sieve load, occur the aromatic ring without side chain of double ring arene to be hydrogenated with saturated, the open loop of tetrahydrochysene naphthalene and its derivative and mononuclear aromatics props up the reactions such as chain break；Lighting product 4 enters after high-pressure separator 5 carries out gas-liquid separation, circulating hydrogen 6 circular response, product liquid 7 enters a rectifying column 8 and carries out rectifying separation, the mixture 9 of overhead extraction low-carbon alkanes, benzene and toluene, this mixture can be through products such as further isolated benzene, toluene and liquefied gas, this portioned product is less because of content, therefore separation scheme is not described in detail in detail in this programme；C at the bottom of tower8And above aromatic hydrocarbons 10 enters No. two rectifying columns 11, after separation, obtain C from tower top8～C9Light ends 12 before the thick product of aromatic hydrocarbons or 205 DEG C, loops back reaction system for heavy distillat 13 at the bottom of the part tower of circular response and continues reaction, and part heavy end 14 is discharged, and can sell as fuel oil.
The following examples illustrate the present invention further.
Experiment catalyst for pre-hydrogenation used and hydrocracking catalyst are prepared by conventional catalyst preparation method, and concrete preparation process and catalyst composition are as follows:
The preparation of catalyst for pre-hydrogenation: take macropore boehmite 400g, adds dilute nitric acid solution 360mL, the sesbania powder 12g of 3%, and through mediating, being molded, 120 DEG C of dry 8h, 550 DEG C of roasting 4h prepare γ-Al2O3Carrier 320g；Take nickel acetate 72g and citric acid 20g to be dissolved in deionized water, be made into maceration extract 360mL；By saturated infusion process, maceration extract is carried on carrier, then prepares catalyst for pre-hydrogenation 356g through 120 DEG C of dry 8h, 600 DEG C of roasting 3h；Wherein active metal Ni content in the catalyst is 10wt%.
The preparation of hydrocracking catalyst: take modified Y molecular sieve 280g, adds adhesive kaolin 40g, sesbania powder 16g, the dilute nitric acid solution 400mL of 3%, and through mediating, being molded, 120 DEG C of dry 8h, 600 DEG C of roasting 4h prepare molecular sieve carrier；The nitrate 3g addition deionized water taking Pt metal is made into maceration extract 290mL, is placed in Rotary Evaporators by molecular sieve carrier, adds metal impregnation liquid, and rotary dipping 3h is evaporated to moisture.Finally the catalyst semi-finished product after dipping are prepared hydrocracking catalyst finished product 302g at 650 DEG C of roasting 4h；Wherein Pt metal content in the catalyst is 0.5wt%, and modified Y molecular sieve content is 93wt%.
In experiment, the loadings of catalyst for pre-hydrogenation and hydrocracking catalyst is 200g.
Embodiment 1
To take from the C of certain refinery's reformer by-product10 +Heavy aromatics cut is raw material, and feedstock property is shown in Table 1.Raw material passes sequentially through pre-hydrogenator and hydrocracking reactor, feed volume air speed 1.0h with hydrogen after mixing-1Hydrogen hydrocarbon volume ratio 1000:1, in the middle part of two reactor bed, reaction temperature is respectively 350 DEG C and 360 DEG C, reaction pressure is 2.5MPa, product is after a rectifying column separates, and materials at bottom of tower enters No. two rectifying columns, from 205 DEG C of front-end volatiles of overhead extraction, materials at bottom of tower loops back reaction system, and product analytical data is shown in Table 2.
Embodiment 2
Test with embodiment 1 same materials.Raw material passes sequentially through pre-hydrogenator and hydrocracking reactor, feed volume air speed 1.0h with hydrogen after mixing-1Hydrogen hydrocarbon volume ratio 1000:1, in the middle part of two reactor bed, reaction temperature is respectively 340 DEG C and 355 DEG C, reaction pressure is 3.0MPa, product is after a rectifying column separates, and materials at bottom of tower enters No. two rectifying columns, from 205 DEG C of front-end volatiles of overhead extraction, materials at bottom of tower loops back reaction system, and product analytical data is shown in Table 2.
Embodiment 3
Test with embodiment 1 same materials.Raw material passes sequentially through pre-hydrogenator and hydrocracking reactor, feed volume air speed 1.0h with hydrogen after mixing-1Hydrogen hydrocarbon volume ratio 1000:1, in the middle part of two reactor bed, reaction temperature is respectively 330 DEG C and 350 DEG C, reaction pressure is 3.8MPa, product is after a rectifying column separates, and materials at bottom of tower enters No. two rectifying columns, from 205 DEG C of front-end volatiles of overhead extraction, materials at bottom of tower loops back reaction system, and product analytical data is shown in Table 2.
Embodiment 4
To take from the C of certain refinery's ethylene cracker by-product10 +Heavy aromatics cut is raw material, and feedstock property is shown in Table 1.Raw material passes sequentially through pre-hydrogenator and hydrocracking reactor, feed volume air speed 1.0h with hydrogen after mixing-1Hydrogen hydrocarbon volume ratio 1000:1, in the middle part of two reactor bed, reaction temperature is respectively 340 DEG C and 355 DEG C, reaction pressure is 3.0MPa, product is after a rectifying column separates, and materials at bottom of tower enters No. two rectifying columns, from 205 DEG C of front-end volatiles of overhead extraction, materials at bottom of tower loops back reaction system, and product analytical data is shown in Table 2.
Embodiment 5
Testing with embodiment 1 same materials and technological process, two reactor operating conditions use the operating condition of embodiment 2, run 30 days continuously, and every day, product was analyzed by sampling, showed that periodic data is as shown in Figure 2.
As shown in Figure 2, this hydrogenation lighting technique and supporting catalyst thereof have long period activity stability.
Table 1
| Project | Embodiment 1～3 | Embodiment 4 |
| C10 +Content, % | 99 | 97 |
| Boiling range, DEG C | 210～320 | 208～335 |
| Density (20 DEG C), g/cm3 | 0.946 | 0.968 |
| Dicyclo and above arene content, % | 51 | 62 |
Table 2
| Project | C10 +Total conversion | C8～C9 arenes selectivity | 205 DEG C of front-end volatiles yields |
| Embodiment 1 | 77 | 56 | 74.6 |
| Embodiment 2 | 82 | 52 | 72.5 |
| Embodiment 3 | 84 | 47 | 68.6 |
| Embodiment 4 | 78 | 49 | 70.2 |
Claims (4)
1. a C10 +Heavy aromatics hydrogenation lightening method, comprises the steps:
a.C10 +After heavy aromatics raw material and hydrogen carry out air-fuel mixture, enter pre-hydrogenator, contact with catalyst for pre-hydrogenation
Carry out the pre-hydrogenation saturated reaction of polycyclic aromatic hydrocarbon；Wherein pre-hydrotreating reaction condition is: in hydrogen dividing potential drop 1.0～6.0MPa, bed
Portion's temperature 280～420 DEG C, volume space velocity 0.1～3.0h-1, hydrogen hydrocarbon volume ratio 200～1500；
B. the effluent of step a is directly entered hydrocracking reactor, contacts with hydrocracking catalyst and carries out single multi-PAH
Be hydrogenated with saturated, the open loop of tetrahydrochysene naphthalene and its derivative and the cleavage reaction of branched mononuclear aromatics side chain；Hydrocracking
Reaction condition is: hydrogen dividing potential drop 1.0～6.0MPa, bed middle portion temperature 300～450 DEG C, volume space velocity 0.1～3.0h-1, hydrogen
Hydrocarbon volume ratio is 200～1500；
C. the effluent of step b is after gas-liquid separation, enters rectifying column and separates, after separation from tower top obtain low-carbon alkanes,
Benzene and the mixture of toluene, described mixture further isolated benzene and toluene；Materials at bottom of tower enters No. two rectifying columns and separates,
Tower top obtains C8～C9Before the thick product of aromatic hydrocarbons or 205 DEG C, light ends is as high-knock rating gasoline blend component, and tower bottom divides weight
Cut loops back reaction system and continues reaction, and part heavy distillat is discharged；
Described C10 +Heavy aromatics is from the heavy aromatics cut of refinery's reformer or steam cracking device by-product；C10 +Heavy aromatics is former
20 DEG C of density of material are 0.90～0.99g/cm3, arene content is not less than 95%, and wherein dicyclo and above arene content are not less than
40%.
2. according to the C described in claim 110 +Heavy aromatics hydrogenation lightening method, it is characterised in that:
Described catalyst for pre-hydrogenation is by macropore γ-Al2O3As carrier loaded VIII, group vib and VIIB race non-noble gold
One or more in genus are made, and wherein tenor is 1～20wt%, and remaining is γ-Al2O3；Described hydrocracking catalyst
Agent be by one or more in beta-molecular sieve, Y molecular sieve and modenite as carrier loaded VIII precious metals pt or/
Making with Pd, wherein tenor is 0.05～2.0wt%, and molecular sieve content is 5～95wt%, and remaining is adhesive.
3. according to the C described in claim 210 +Heavy aromatics hydrogenation lightening method, it is characterised in that:
VIII base metal described in catalyst for pre-hydrogenation is Ni, and group vib base metal is Cr, Mo or W, VIIB
Race's base metal is Mn.
4. according to the C described in claim 110 +Heavy aromatics hydrogenation lightening method, it is characterised in that:
Described pre-hydrotreating reaction condition is: hydrogen dividing potential drop 2.0～5.0MPa, bed middle portion temperature 300～360 DEG C, and volume is empty
Speed 0.5～2.0h-1, hydrogen hydrocarbon volume ratio be 500～1000；Described hydrocracking reaction condition be preferably: hydrogen dividing potential drop 2.0～
5.0MPa, bed middle portion temperature 320～380 DEG C, volume space velocity 0.5～2.0h-1, hydrogen hydrocarbon volume ratio be 500～1000.
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| CN103121895A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons |
| CN103121897A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing arene by mixture containing hydrocarbon with condensed rings |
| CN103214332A (en) * | 2012-01-18 | 2013-07-24 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbons and high-quality oil products from catalytically cracked diesel |
| CN103897731A (en) * | 2014-02-24 | 2014-07-02 | 中国海洋石油总公司 | Method for mixed production of light-weight aromatic hydrocarbon by use of catalytic cracking diesel and C10<+> distillate oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103121895A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons |
| CN103121897A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing arene by mixture containing hydrocarbon with condensed rings |
| CN103214332A (en) * | 2012-01-18 | 2013-07-24 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbons and high-quality oil products from catalytically cracked diesel |
| CN103897731A (en) * | 2014-02-24 | 2014-07-02 | 中国海洋石油总公司 | Method for mixed production of light-weight aromatic hydrocarbon by use of catalytic cracking diesel and C10<+> distillate oil |
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