CN105085134A - Method for direct production of aromatic hydrocarbon raw material from Inferior heavy aromatics - Google Patents
Method for direct production of aromatic hydrocarbon raw material from Inferior heavy aromatics Download PDFInfo
- Publication number
- CN105085134A CN105085134A CN201410202025.XA CN201410202025A CN105085134A CN 105085134 A CN105085134 A CN 105085134A CN 201410202025 A CN201410202025 A CN 201410202025A CN 105085134 A CN105085134 A CN 105085134A
- Authority
- CN
- China
- Prior art keywords
- raw material
- inferior heavy
- aromatics
- aromatic hydrocarbons
- hydrocarbon raw
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a method for direct production of an aromatic hydrocarbon raw material from 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 direct production of the aromatic hydrocarbon raw material. The method comprises the following steps: a) sulfur and nitrogen impurities in the inferior heavy aromatic raw material rich in mixed condensed ring aromatic hydrocarbons are removed; b) a reaction material flow from a hydrofining reactor and hydrogen are mixed, and pass through a selective hydrocracking reactor in series connection with the hydrofining reactor for selective hydrocracking reaction of the condensed ring aromatic hydrocarbons; c) light fractions, intermediate fractions and heavy fractions are obtained by oil and gas separation and fractionation according to the boiling points of the selective hydrocracking reaction product; d) the intermediate fractions, and hydrogen are mixed and enter a non-aromatic hydrocarbon conversion reactor for deep hydrocracking reaction of alkanes and cycloalkanes; and e) monocylic aromatics and light hydrocarbons can be obtained by oil and gas separation and fractionation of the reaction product, by the technical scheme, the problem is well solved, and the method can be used in the industrial production for production of high purity monocylic aromatics from the inferior heavy aromatic raw material rich in mixed condensed ring aromatic hydrocarbons.
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 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 tune diesel 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 hydrogenation open loop also takes off alkyl, 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 non-aromatic conversion, technical scheme comprises 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 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 is through gas-oil separation, by obtaining lighting end, middle runnings and last running after boiling point fractionation, and wherein last running partly or entirely loops back selective hydrogenation cracking case, and lighting end drains into out-of-bounds; D) middle runnings enters non-aromatics conversion reactor after mixing with hydrogen, alkane and the reaction of naphthenic hydrocarbon generation deep pyrolytic; E) resultant of reaction obtains high purity mononuclear aromatics and light hydrocarbons after gas-oil separation, fractionation.
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 60-98%, and Bicyclic aryl rings content is between 35-80%, sulphur content is between 0-3%, and nitrogen content is between 0-3%; The high purity mononuclear aromatics produced in non-aromatic conversion reactor, obtains comprising benzene,toluene,xylene, C9 aromatic and C10 aromartic after fractionation; The light hydrocarbons produced in non-aromatic conversion reactor, comprises C3, C4 and C5 alkane after fractionation; The purity of benzaldehyde product is greater than 99.90%, and the purity of toluene product is greater than 99.50%, and C8 aronmatic purity is greater than 99.30%; 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 non-aromatic conversion reactor is between 2.5 ~ 3.0MPa, and temperature in is at 360 ~ 460 DEG C, and hydrogen to oil volume ratio is between 600 ~ 1000 (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 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.Deep pyrolytic reaction is there is in benzene to the non-aromatics in C10 aromartic cut on non-aromatic conversion catalyst, be converted into the light ends fractionation of LPG class, thus after simple fractionation, directly obtain high purity mononuclear aromatics raw material, the important basic organic chemical industry raw materials such as benzene, toluene and dimethylbenzene can be obtained after separation.
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, isocrackate gets final product production high purity mononuclear aromatics without extracting, have that aroamtic hydrocarbon raw material utilization ratio is high, mononuclear aromatics product yield is high and the features such as good product purity, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is according to the schematic diagram by the technique of inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material 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 31 is incorporated in pipeline 9 through pipeline 34, and low pressure hydrogen is incorporated in pipeline 25 through pipeline 33.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 15, heavy constituent at the bottom of tower delivers to separation column 17 by pipeline 16, boiling point drains into out-of-bounds higher than 200 DEG C of components by pipeline 19 part, and part returns selective hydrogenation cracking case 4 as charging.Boiling range 70-200 DEG C of component is by pipeline 18, non-aromatic conversion reactor 20 is entered after mixing with the hydrogen in pipeline 25, reaction effluent delivers to gas-liquid separator 22 through pipeline 21, and hydrogen gas-phase product enters circulating hydrogen compressor 24 through pipeline 23, and part drains into out-of-bounds.Liquid product in gas-liquid separator 22 delivers to separation column 27 by pipeline 26, and lighting end drains into out-of-bounds by pipeline 28, can obtain mononuclear aromatics product from pipeline 29.
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 range.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 cracking reaction resultant through gas-oil separation, cut into lower than 70 DEG C of lighting ends, 70-200 DEG C middle runnings by boiling point and be greater than 200 DEG C of last running.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; 70-200 DEG C of middle runnings fed downstream.
Table 3
[embodiment 3]
After 70-200 DEG C of middle runnings being mixed with 3.0MPa hydrogen, enter non-aromatic conversion reactor, at benzene to non-aromatics generation deep pyrolytic reactions such as the alkane in C10 aromartic boiling spread, naphthenic hydrocarbon.Table 4 lists catalyzer used and reaction conditions.Non-aromatic conversion reaction resultant, through gas-oil separation, cuts into lighter hydrocarbons by boiling point and BTX aromatics drains into out-of-bounds, and BTX aromatics can be sent to Aromatic Hydrocarbon United Plant and produce benzene,toluene,xylene further.The raw material of non-aromatic conversion reaction and product analytical data are in table 5, and the purity of aromatic hydrocarbon product is higher, can directly as the raw material of Aromatic Hydrocarbon United Plant.
Table 4
Table 5
Claims (10)
1., by a method for inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material, 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 the logistics come from hydrofining reactor mixes with 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 is through gas-oil separation, by obtaining lighting end, middle runnings and last running after boiling point fractionation, and wherein last running partly or entirely loops back selective hydrogenation cracking case, and lighting end drains into out-of-bounds;
D) after middle runnings mixes with hydrogen, non-aromatics conversion reactor is entered, alkane and the reaction of naphthenic hydrocarbon generation deep pyrolytic;
E) resultant of reaction obtains mononuclear aromatics and light hydrocarbons after gas-oil separation, fractionation.
2. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material 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 60 ~ 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 by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, is characterized in that the mononuclear aromatics produced in non-aromatic conversion reactor, obtains comprising benzene,toluene,xylene, C9 aromatic and C10 aromartic after fractionation.
4. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, is characterized in that the light hydrocarbons produced in non-aromatic conversion reactor, after fractionation, obtains comprising C
3, C
4and C
5alkane.
5. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, is characterized in that the purity of benzaldehyde product is greater than 99.90%.
6. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, is characterized in that the purity of toluene product is greater than 99.50%.
7. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, is characterized in that C8 aronmatic purity is greater than 99.30%
8. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material 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 by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, it is characterized in that hydrotreated product directly enters selective hydrogenation cracking case, pressure is consistent with hydrofining reactor, temperature in is between 350-420 DEG C, and hydrogen to oil volume ratio is between 600 ~ 1200.
10. the method by inferior heavy aromatic hydrocarbons direct production aroamtic hydrocarbon raw material according to claim 1, it is characterized in that the working pressure of non-aromatic conversion reactor is between 2.5 ~ 3.0MPa, temperature in is at 360 ~ 460 DEG C, and hydrogen to oil volume ratio is between 600 ~ 1000.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410202025.XA CN105085134B (en) | 2014-05-14 | 2014-05-14 | The method that aroamtic hydrocarbon raw material is directly produced by heavy aromatics inferior |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410202025.XA CN105085134B (en) | 2014-05-14 | 2014-05-14 | The method that aroamtic hydrocarbon raw material is directly produced by heavy aromatics inferior |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105085134A true CN105085134A (en) | 2015-11-25 |
| CN105085134B CN105085134B (en) | 2017-08-11 |
Family
ID=54566572
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410202025.XA Active CN105085134B (en) | 2014-05-14 | 2014-05-14 | The method that aroamtic hydrocarbon raw material is directly produced by heavy aromatics inferior |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105085134B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112574782A (en) * | 2019-09-30 | 2021-03-30 | 中国石油化工股份有限公司 | Method and system for preparing light aromatic hydrocarbon |
| CN115141653A (en) * | 2022-06-20 | 2022-10-04 | 中海油天津化工研究设计院有限公司 | Method for producing light aromatic hydrocarbon by lightening aromatic-rich distillate oil |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7265252B1 (en) * | 2003-12-18 | 2007-09-04 | Uop Llc | Process for xylene production |
| CA2541051C (en) * | 2005-09-20 | 2013-04-02 | Nova Chemicals Corporation | Aromatic saturation and ring opening process |
| JP2009235247A (en) * | 2008-03-27 | 2009-10-15 | Toray Ind Inc | Method for producing aromatic hydrocarbon having six to eight carbon atoms |
| CN101684415B (en) * | 2008-09-27 | 2012-07-25 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical materials to maximum with low cost |
| 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 |
-
2014
- 2014-05-14 CN CN201410202025.XA patent/CN105085134B/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112574782A (en) * | 2019-09-30 | 2021-03-30 | 中国石油化工股份有限公司 | Method and system for preparing light aromatic hydrocarbon |
| CN115141653A (en) * | 2022-06-20 | 2022-10-04 | 中海油天津化工研究设计院有限公司 | Method for producing light aromatic hydrocarbon by lightening aromatic-rich distillate oil |
| CN115141653B (en) * | 2022-06-20 | 2024-02-09 | 中海油天津化工研究设计院有限公司 | Method for producing light aromatic hydrocarbon by virtue of light aromatic-rich distillate oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105085134B (en) | 2017-08-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103121897B (en) | By the method for the mixture preparing aromatic hydrocarbon containing hydrocarbon with condensed rings | |
| CN103289740B (en) | Method for preparing clean fuel oil from coal tar | |
| CN102796559B (en) | Method and the device of oil fuel are produced in hydrocracking | |
| CN102604677B (en) | High and low-temperature Fischer-Tropsch synthesis co-production technology | |
| CN101712889B (en) | Method for preparing light aromatics from coal tar | |
| CN106661463A (en) | Processes for converting biomass to btx with low sulfur, nitrogen and olefin content via a catalytic fast pyrolysis process | |
| CA2978647A1 (en) | Diesel oil and jet fuel production system and method utilizing fischer-tropsch synthetic oil | |
| CN104611059A (en) | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products | |
| CN103906725A (en) | Method of producing aromatic hydrocarbons and olefin from hydrocarbonaceous oils comprising large amounts of polycyclic aromatic compounds | |
| CN100389179C (en) | Hydrogenation cracking method of mass production of chemical materials | |
| CN103468314B (en) | DCL/Direct coal liquefaction circulating solvent and its preparation method and application | |
| CN103772123B (en) | Method for increasing yield of BTX aromatics | |
| CN105085154A (en) | Method for increase production of aromatic hydrocarbon raw material by use of inferior heavy aromatics | |
| CN105085135A (en) | Method for direct production of benzene and xylene from inferior heavy aromatics | |
| CN104004541B (en) | A kind of preparation method of coal-based high arene underwater content stock oil | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN103468315B (en) | DCL/Direct coal liquefaction circulating solvent and its preparation method and application | |
| CN109988609B (en) | Flexible shale oil hydrocracking process | |
| CN109988606A (en) | A kind of flexible inverted sequence hydrocracking process | |
| CN105085134A (en) | Method for direct production of aromatic hydrocarbon raw material from Inferior heavy aromatics | |
| CN102807900B (en) | High-value utilization method for oxygen-enriched coal tar | |
| CN106588540B (en) | Method for producing benzene and xylene from catalytic cracking light diesel oil | |
| CN103864563B (en) | Method for preparing aromatic hydrocarbon from hydrocarbon tail oil byproducts produced in coal-based methanol to propylene process | |
| CN105296002A (en) | Method for producing fuel oils by hydrogenation after coal tar cleaning and phenol extraction and system thereof | |
| CN109321273A (en) | The method and apparatus for producing naphthenic base refrigerator oil base oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |