CN105085154A - Method for increase production of aromatic hydrocarbon raw material by use of inferior heavy aromatics - Google Patents
Method for increase production of aromatic hydrocarbon raw material by use of inferior heavy aromatics Download PDFInfo
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Abstract
The present invention relates to a method for increase production of an aromatic hydrocarbon raw material by use of inferior heavy aromatics, and mainly solves the problem that in the prior art inferior heavy aromatics containing condensed ring aromatic hydrocarbons cannot be used for increase production of a monocylic aromatic hydrocarbon raw material. The method comprises the following steps: a) sulfur and nitrogen impurities in an inferior heavy aromatic raw material rich in mixed condensed ring aromatic hydrocarbons are removed; b) selective hydrocracking reaction of the condensed ring aromatic hydrocarbons is performed; c) light fractions, light aromatic fractions, heavy aromatic fractions and heavy fractions are obtained by oil and gas separation, and fractionation in a fractionation system according to boiling points of the selective hydrocracking reaction product; d) heavy aromatic fractions and hydrogen are mixed, and enter into a heavy aromatic lightening reactor for occurrence of transalkylation and dealkylation reaction, and the reaction product is returned to the fractionation system; and e) the light aromatic fractions are discharged to the outside world as a product, by the technical scheme, the problem is well solved, and the method can be used in the industrial production for production of benzene, toluene and xylene.
Description
Technical field
The present invention relates to a kind of by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material method, particularly about a kind of method that the mixture through catalytic containing hydrocarbon with condensed rings can be converted into high purity benzene,toluene,xylene, carbon nine mononuclear aromatics and carbon ten mononuclear aromatics mixture.
Background technology
Benzene and p-Xylol (PX) are important basic organic chemical industry raw materials, are widely used in and produce the product such as polyester, chemical fibre, closely related with the clothing, food, lodging and transportion--basic necessities of life of the national economic development and people, in recent years sought-after, increment is rapid.The source of aroamtic hydrocarbon raw material mainly contains two operational paths: a raw material route is that petroleum naphtha obtains aroamtic hydrocarbon raw material through catalytic reforming, Aromatics Extractive Project; Another raw material route is that the byproduct of ethylene unit-cracking of ethylene gasoline is obtained aroamtic hydrocarbon raw material through hydrogenation, Aromatics Extractive Project, thus is high added value aromatic hydrocarbon product low value-added feedstock conversion.In petrochemical factory, Aromatic Hydrocarbon United Plant is product for the purpose of p-Xylol (coproduction o-Xylol) usually, for downstream PTA device is supplied raw materials.Will the p-Xylol of production maximum, except the dimethylbenzene in catalytic reforming and cracking of ethylene gasoline, mainly adopt the processing method of disproportionation and transalkylation toluene and C
9aromatic hydrocarbons (also comprises part monocycle C
10aromatic hydrocarbons) under molecular sieve catalyst effect, carry out disproportionation and transalkylation reaction generate xylol and benzene, xylol is converted into p-Xylol by dimethylbenzene hydro-isomerization metallization processes again.
Ethylene unit and Aromatic Hydrocarbon United Plant are all raw material with petroleum naphtha, and limited naphtha resource also will meet the motor spirit demand of domestic quick growth.Reduce the degree of dependence to raw material petroleum naphtha, expand aroamtic hydrocarbon raw material resource, be the important topic of current development petrochemical complex, catalytic cracking light cycle oil (LCO), Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil, coal tar or DCL/Direct coal liquefaction wet goods enter the visual field of people containing the inferior heavy aromatic hydrocarbon resource of condensed-nuclei aromatics.Wherein mainly containing naphthalene system double ring arene, anthracene, phenanthrene system thrcylic aromatic hydrocarbon etc. hydrocarbon polymer, cut is wide, complicated components and cannot isolate pure component, and utility value is not high.Coal tar and coal direct liquefaction oil, by after hydrotreatment, can be used for producing oil fuel and automobile-used petrol and diesel oil, but not yet for the production of high added value aromatic hydrocarbon product.Aromatic Hydrocarbon United Plant heavy aromatics tail oil is after isolating the products such as durene, and the value utilized further is little, can only as hydrogenation unit raw material or oil fuel.
Total aromaticity content of LCO is up to 80%, and naphthalene system double ring arene accounts for about 70%, and mononuclear aromatics and thrcylic aromatic hydrocarbon about respectively account for about 15%, and other is alkane, naphthenic hydrocarbon and alkene etc.Sulphur content 0.2 ~ the 1.5wt% of LCO, nitrogen content 100 ~ 750ppm, cetane value only has 15 ~ 25, and ignition characteristic is poor, and the Technical Economy of processing derv fuel oil is not good.LCO usually used as a kind of second-rate diesel oil blending component and straight-run diesel oil used in combination, or directly to use as oil fuel.In recent years, the MIP technique of domestic catalytic cracking unit many employings maximizing iso-paraffins carries out technology upgrading, and a large amount of by-product MIP solar oil (i.e. LCO) exists the utilization of resources and an increment difficult problem.China's catalytic cracking (FCC) device year, amount of finish was close to 100,000,000 tons, and the year output of LCO is more than 1,000 ten thousand tons.
Poor quality catalytic cracking diesel (mainly LCO) the upgrading means that Present Domestic generally adopts outward are hydrofining, hydro-upgrading and light oil type hydrogen cracking.Catalytic diesel oil hydrofining, be in, under the condition of low pressure, carry out olefins hydrogenation, desulfurization, denitrogenation and aromatic moiety saturated reaction, its color and stability can be improved, and cetane value increase rate is less, especially process the catalytic unit of inferior raw material, its catalytic diesel oil also far can not meet the requirement of product to cetane value by hydrofining.Hydrogenation modifying process, as the Unicracking technique (USP5026472) of Uop Inc., there is the saturated performance of good aromatic hydrogenation and selectivity of ring-opening, the aromatic conversion degree of depth is very high, ensure larger cetane value increase rate and have higher diesel yield, but the hydrogen of this technique consumption is very large, and high-tension unit is invested and running cost is all higher.Light oil type hydrogen cracking be then by solar oil component after refining, violent saturated hydrogenation, obtain reforming material or the gasoline fraction of naphtha fraction, this process has aromatic hydrocarbons supersaturation too and hydrogen consumes too high problem, and the naphthenic hydrocarbon generated after supersaturation and chain hydrocarbon also will be converted into aromatic hydrocarbons in reformer, it not an economic route.As the light oil type hydrogen cracking method that CN101684415 patent proposes, directly do not produce aromatic hydrocarbons, the virtue of heavy naphtha is dived also lower.
In order to light cycle oil being converted into the higher mononuclear aromatics of industrial added value, patent CN102227490 describes a kind of method being prepared clean fuel and aromatics by light cycle oil, light cycle oil raw material is cut into 170-220 DEG C and 220-360 DEG C of cut by this processing method, wherein light oil distillate is by after hydrofining and hydrocracking reaction, again through special catalyst bed, mainly will be cracked into liquid petroleum gas cut containing the non-aromatics in the reaction effluent of aromatic hydrocarbons and non-aromatics, thus obtain the aromatic hydrocarbon product of higher degree.But only have the light oil distillate Partial Conversion of 170-220 DEG C of cut in order to aromatic hydrocarbon product, the utilization ratio of raw material is not high.Patent USP7265252 describes the method that dimethylbenzene is produced in a kind of fuels from FCC LCO hydrocracking-alkylation selectivity transfer.This processing method is the impurity such as sulphur, nitrogen in first pre-hydrotreating removing stock oil, then carry out catalytic hydrocracking reaction double ring arene is partially converted into mononuclear aromatics, finally by the transalkylation reaction of mononuclear aromatics, generate target product dimethylbenzene and benzene, go back a by-product part liquefied gas, light naphthar and ultra-low-sulphur diesel component simultaneously.But because hydrofining and isocrackate directly enter transalkylation reaction, the existence of a large amount of by-product non-aromatics brings disadvantageous effect by the long-term operation of transalkylation catalyst, the purity of aromatic hydrocarbon product is not high yet.
Summary of the invention
Technical problem to be solved by this invention is the problems such as inferior heavy aroamtic hydrocarbon raw material utilization ratio is not high, mononuclear aromatics productive rate is low, aromatic hydrocarbon product purity is not high, provide a kind of newly with the method for inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material.The method is used for inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material, has that aroamtic hydrocarbon raw material utilization ratio is high, mononuclear aromatics product yield is high and the features such as good product purity.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method combined by hydrofining, selective hydrogenation cracking and heavy aromatic hydrocarbon light, comprise the following steps: a) be rich in mixing condensed-nuclei aromatics inferior heavy raw material mix with hydrogen after by hydrofining reactor, remove sulphur wherein, nitrogen impurity; B) after the logistics come from hydrofining reactor mixes with appropriate amount of hydrogen again, by the selective hydrogenation cracking case of connecting with hydrofining reactor, condensed-nuclei aromatics generation selective hydrogenation cracking reaction; C) selective hydrogenation cracking reaction resultant through gas-oil separation, after fractionating system is by boiling point fractionation, obtain lighting end, light aromatics cut, heavy arene cut and last running, wherein last running partly or entirely loops back selective hydrogenation cracking case, and lighting end drains into out-of-bounds; D) heavy arene cut enters heavy aromatic hydrocarbon light reactor after mixing with hydrogen, and transalkylation and dealkylation occur, and resultant of reaction turns back to fractionating system; E) light aromatics cut drains into out-of-bounds as product.
In technique scheme, raw material carrys out at least one of catalytic cracking light cycle oil, Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil or coal direct liquefaction oil, boiling spread 180 ~ 370 DEG C, when 20 DEG C, density is not less than 0.85g/ml, by weight percentage, total aromatic ring content is between 50-98%, and Bicyclic aryl rings content is between 35-80%, sulphur content is between 0 ~ 3%, and nitrogen content is between 0 ~ 3%; The light aromatics cut that fractionating system obtains is benzene, toluene, ethylbenzene and dimethylbenzene, also comprises naphthenic hydrocarbon and alkane, and by weight percentage, aromaticity content is between 65-95%, and total sulfur content is less than 0.5ppm, and total nitrogen content is less than 0.5ppm; The boiling spread of heavy arene cut is 145 ~ 200 DEG C; The boiling spread of unconverted last running is 200 ~ 350 DEG C; The working pressure of hydrofining reactor is between 3.5 ~ 10.0MPa, and temperature in is between 330 ~ 400 DEG C, and hydrogen to oil volume ratio is between 400 ~ 1000 (V/V); Hydrotreated product directly enters selective hydrogenation cracking case, and pressure is consistent with hydrofining reactor, and temperature in is between 350-420 DEG C, and hydrogen to oil volume ratio is between 600 ~ 1200 (V/V); The working pressure of heavy aromatic hydrocarbon light reactor is between 2.5 ~ 3.5MPa, and temperature in is at 360 ~ 450 DEG C, and hydrogen to oil volume ratio is between 500 ~ 1200 (V/V).
Using the mixture containing condensed-nuclei aromatics as raw material, by hydrofining unit, selective hydrogenation Cracking Unit and non-aromatic conversion unit, mononuclear aromatics raw materials such as comprising benzene,toluene,xylene, C9 aromatic and monocycle C10 aromartic efficiently can be generated.The impurity such as hydrofining unit efficient removal sulphur, nitrogen, fractional saturation condensed-nuclei aromatics component.After imurity-removal, mixture is under the effect of selective hydrogenation cracking catalyst, is selectively converted to mononuclear aromatics product and a small amount of non-aromatics.Benzene directly can enter Aromatic Hydrocarbon United Plant to carbon eight light aromatics cut, there is de-alkyl and transalkylation reaction in the heavy arene cut comprising carbon nine and carbon ten, thus maximize the important basic organic chemical industry raw materials such as volume increase benzene, toluene and dimethylbenzene in heavy aromatic hydrocarbon light reactor.
Can find out, such operational path, the mixture containing condensed-nuclei aromatics lower for the added value of industry can be converted into the mononuclear aromatics mixture of high added value, the heavy arene cut of hydrocracking by-product is further converted to benzene, toluene and dimethylbenzene, have and maximize volume increase benzene, toluene and dimethylbenzene, the features such as product value-added effect is good, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is according to the schematic diagram being increased production the technique of aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons of the present invention.This figure is intended to schematically illustrate the present invention but not is limited.
By the raw material containing inferior heavy aromatic hydrocarbons by entering hydrofining reactor 2 after the hydrogen mixing of pipeline 1 and pipeline 9, reaction effluent mixes laggard selectable hydrocracking reactor 4 with the hydrogen partial in pipeline 9 again through pipeline 3, and reaction effluent sends into high-pressure separator 6 through pipeline 5.Hydrogen gas-phase product enters circulating hydrogen compressor 8 through pipeline 7, and part drains into out-of-bounds.High pressure hydrogen from hydrogen make-up compressor 29 is incorporated in pipeline 9 through pipeline 32, and low pressure hydrogen is incorporated in pipeline 27 through pipeline 31.Liquid product in high-pressure separator 6 sends into light pressure separator 11 through pipeline 10, light hydrocarbon component drains into out-of-bounds from pipeline 12, liquid phase component sends into separation column 14 through pipeline 13, drain into out-of-bounds lower than 70 DEG C of light constituents through pipeline 16, heavy constituent at the bottom of tower delivers to separation column 17 by pipeline 15, and boiling point is drained into out-of-bounds as product by pipeline 19 between 70-145 DEG C of light aromatics cut.Boiling point at the bottom of tower is greater than 200 DEG C of ends fraction and returns selective hydrogenation cracking case 4 as charging, and part is outer to be drained into out-of-bounds.Heavy aromatic hydrocarbon light reactor 21 is entered after boiling range 145-200 DEG C of component of side take-off is mixed with the hydrogen in pipeline 27 by pipeline 20, reaction effluent delivers to gas-liquid separator 23 through pipeline 22, hydrogen gas-phase product enters circulating hydrogen compressor 26 through pipeline 25, and part drains into out-of-bounds.Liquid product in gas-liquid separator 23 is back to pipeline 13 by pipeline 24, enters fractionating system.
Below by embodiment, the invention will be further elaborated.
Embodiment
[embodiment 1]
Be that after 180-370 DEG C of inferior heavy aromatic hydrocarbons mixes with 6.0MPa hydrogen, enter hydrofining reactor and remove sulphur nitrogen, be saturated to surplus next aromatic ring to part condensed-nuclei aromatics, table 1 lists catalyzer used and reaction conditions by boiling point.Table 2 lists the sulphur nitrogen content of raw material and hydrofining product, density, aromatic content, naphthane system aromaticity content and fractional distribution.The nitrogen content of hydrotreated product is less than 20ppm.
Table 1
Table 2
[embodiment 2]
After being mixed with 6.0MPa hydrogen by hydrotreated product, enter selective hydrogenation cracking case, selective hydrogenation ring-opening reaction and the dealkylation of tetrahydrochysene naphthalene series aromatics and polycyclic aromatic hydrocarbons occur.Table 3 lists catalyzer used and reaction conditions.Selective hydrogenation cracked reaction product cuts into lower than 70 DEG C of lighting ends, 70-145 DEG C light aromatics cut, 145-200 DEG C heavy arene cut by boiling point and is greater than 200 DEG C of last running in the separation column of series connection.Drain into out-of-bounds lower than 70 DEG C of lighting ends; 70% last running loops back selective hydrogenation cracking case, and 30% last running drains into out-of-bounds; 70-145 DEG C of light aromatics cut is arranged outward as product; 145-200 DEG C of cut fed downstream.Table 4 lists the composition of light aromatics component, mainly benzene, toluene, ethylbenzene and dimethylbenzene, also containing a small amount of naphthenic hydrocarbon and alkane.
Table 3
Table 4
| 70-145 DEG C of cut product |
| Below C6 is non-aromatic | 0.32 |
| C6-C8 is non-aromatic | 8.76 |
| Benzene | 13.72 |
| Toluene | 36.13 |
| Ethylbenzene | 7.48 |
| Dimethylbenzene | 33.5 |
| More than C9 hydro carbons | 0.09 |
[embodiment 3]
After being mixed with 3.0MPa hydrogen by 145-200 DEG C of heavy arene cut, enter heavy aromatic hydrocarbon light reactor, C9 aromatic, carbon ten and above aromatic hydrocarbons generation transalkylation and side chain dealkylation.Table 5 lists heavy aromatics lightening catalyst used and reaction conditions.Heavy aromatics lighting product, after gas-oil separation, turns back in fractionating system.
Table 5
Claims (10)
1. increased production a method for aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons, comprise the following steps:
A) be rich in mixing condensed-nuclei aromatics inferior heavy aroamtic hydrocarbon raw material mix with hydrogen after, by hydrofining reactor, remove sulphur wherein, nitrogen impurity;
B) after mixing with hydrogen again from hydrofining reactor logistics out, by the selective hydrogenation cracking case of connecting with hydrofining reactor, condensed-nuclei aromatics generation selective hydrogenation cracking reaction;
C) selective hydrogenation cracking reaction resultant, after gas-oil separation, after fractionating system presses boiling point fractionation, obtain lighting end, light aromatics cut, heavy arene cut and last running, wherein last running partly or entirely loops back selective hydrogenation cracking case, and lighting end drains into out-of-bounds;
D) after heavy arene cut mixes with hydrogen, enter heavy aromatic hydrocarbon light reactor, transalkylation and dealkylation occur, and resultant of reaction turns back to fractionating system;
E) light aromatics cut drains into out-of-bounds as product.
2. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, it is characterized in that raw material carrys out at least one of catalytic cracking light cycle oil, Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil or coal direct liquefaction oil, boiling spread 180 ~ 370 DEG C, when 20 DEG C, density is not less than 0.85g/ml, by weight percentage, total aromatic ring content is between 50-98%, and Bicyclic aryl rings content is between 35-80%, sulphur content is between 0 ~ 3%, and nitrogen content is between 0 ~ 3%.
3. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, is characterized in that the light aromatics cut that fractionating system obtains is benzene, toluene, ethylbenzene and dimethylbenzene, also comprises naphthenic hydrocarbon and alkane.
4. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, is characterized in that in the light aromatics cut that fractionating system obtains, by weight percentage, aromaticity content is between 65-95%.
5. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, it is characterized in that the light aromatics cut that fractionating system obtains, total sulfur content is less than 0.5ppm, and total nitrogen content is less than 0.5ppm.
6. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, is characterized in that the boiling spread of heavy arene cut is 145 ~ 200 DEG C.
7. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, is characterized in that the boiling spread of unconverted last running is 200 ~ 350 DEG C.
8. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, it is characterized in that the working pressure of hydrofining reactor is between 3.5 ~ 10.0MPa, temperature in is between 330 ~ 400 DEG C, and hydrogen to oil volume ratio is between 400 ~ 1000.
9. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, it is characterized in that hydrotreated product directly enters selective hydrogenation cracking case, pressure is consistent with hydrofining reactor, and temperature in is between 350-420 DEG C, and hydrogen to oil volume ratio is between 600 ~ 1200.
10. the method being increased production aroamtic hydrocarbon raw material by inferior heavy aromatic hydrocarbons according to claim 1, it is characterized in that the working pressure of heavy aromatic hydrocarbon light reactor is between 2.5 ~ 3.5MPa, temperature in is at 360 ~ 450 DEG C, and hydrogen to oil volume ratio is between 500 ~ 1200.
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| CN108179026A (en) * | 2018-02-09 | 2018-06-19 | 中国海洋石油集团有限公司 | A kind of heavy aromatic hydrocarbon light prepares the method and device of low-carbon aromatic hydrocarbons |
| CN109718760A (en) * | 2017-10-30 | 2019-05-07 | 中国石油化工股份有限公司 | A method of light aromatics is produced by raw material of catalytic cracking diesel oil |
| CN114437818A (en) * | 2020-10-30 | 2022-05-06 | 宁波中金石化有限公司 | Heavy aromatic oil processing method |
| CN114437811A (en) * | 2020-10-30 | 2022-05-06 | 中国科学院宁波材料技术与工程研究所 | Processing method for lightening heavy aromatic oil |
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| CN101730673B (en) * | 2007-07-06 | 2013-05-01 | 环球油品公司 | Process for xylene production |
| KR101735108B1 (en) * | 2010-09-16 | 2017-05-15 | 에스케이이노베이션 주식회사 | The method for producing valuable aromatics and olefins from hydrocarbonaceous oils derived from coal or wood |
| CN103059917B (en) * | 2011-10-24 | 2015-04-08 | 中国石油化工股份有限公司 | Light cycle oil selective hydrorefining method |
| CN103121897B (en) * | 2011-11-18 | 2015-08-12 | 中国石油化工股份有限公司 | By the method for the mixture preparing aromatic hydrocarbon containing hydrocarbon with condensed rings |
| CN103121895B (en) * | 2011-11-18 | 2015-06-10 | 中国石油化工股份有限公司 | Method for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons |
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| CN109718760A (en) * | 2017-10-30 | 2019-05-07 | 中国石油化工股份有限公司 | A method of light aromatics is produced by raw material of catalytic cracking diesel oil |
| CN108179026A (en) * | 2018-02-09 | 2018-06-19 | 中国海洋石油集团有限公司 | A kind of heavy aromatic hydrocarbon light prepares the method and device of low-carbon aromatic hydrocarbons |
| CN114437818A (en) * | 2020-10-30 | 2022-05-06 | 宁波中金石化有限公司 | Heavy aromatic oil processing method |
| CN114437811A (en) * | 2020-10-30 | 2022-05-06 | 中国科学院宁波材料技术与工程研究所 | Processing method for lightening heavy aromatic oil |
| CN114437818B (en) * | 2020-10-30 | 2023-04-07 | 宁波中金石化有限公司 | Heavy aromatic oil processing method |
| CN114437811B (en) * | 2020-10-30 | 2023-05-16 | 中国科学院宁波材料技术与工程研究所 | Processing method for lightening heavy aromatic oil |
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