CN1351114A - Process for treating heavy arylhydrocarbon oil - Google Patents
Process for treating heavy arylhydrocarbon oil Download PDFInfo
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- CN1351114A CN1351114A CN 00123142 CN00123142A CN1351114A CN 1351114 A CN1351114 A CN 1351114A CN 00123142 CN00123142 CN 00123142 CN 00123142 A CN00123142 A CN 00123142A CN 1351114 A CN1351114 A CN 1351114A
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Abstract
A process for processing heavy arylhydrocarbon oil features the combination of hydrogenating and refining with solvent. It can effectively remove inpurities (S, N and metals) from heavy arylhydrocarbon oil and convert the macro-molecular condensed-ring arylhydrocarbon (colloid and asphalt) to micro-molecular one, improving the output rate of ideal arylhydrocarbon.
Description
The present invention relates to the processing and treating method of heavy aromatic oil.
At present, the main source of heavy aromatic oil has: the residual oil of technologies such as the extraction oil of the slurry oil of catalytic cracking process (clarified oil), lube oil finishing technology and viscosity breaking, thermally splitting, Pintsch process and coking recycle oil etc.Along with the heaviness and the poor qualityization of crude resources, the quantity of heavy aromatic oil is also more and more.Document (" refining of petroleum and chemical industry ", 4,1994,20～25) points out that heavy aromatic oil can be used for optimizing oil refining process, can make road bitumen blend component and heavy gas oil blend component; Can produce the leading raw material of needle coke and asphalt base carbon fiber; Also can make PVC in rubber filling oil, rubber processing oil and the plastics industry with aromatic plasticizer etc.But owing to contain undesirable components such as more sulphur, nitrogen, metal impurities and colloid, bituminous matter in the heavy aromatic oil in above-mentioned source, and most heavy aromatic oils are still mixed act as a fuel in the vacuum residuum oil to use, effectively do not utilized.The CN87107146A patent has proposed the solvent pairs extraction process and has carried out the processing of catalytically cracked oil, and the desirable catalytic cracking component in the catalytically cracked oil is extracted, and proceed catalytic cracking, and remaining heavy arene removes to do bituminous blend component etc.This patent only uses physical method to make the parallel feeding character of catalytic cracking unit that improvement arranged, and has reduced the coke and the gas yield of catalytic cracking unit, but the character of heavy arene do not change, so the heavy aromatic oil utilization in full force and effect of failing.
The object of the present invention is to provide a kind of working method of heavy aromatic oil, sulphur, nitrogen, metal impurities in can the effective elimination heavy aromatic oil, macromole condensed-nuclei aromaticss such as colloid contained in the heavy aromatic oil, bituminous matter can be converted into micromolecular aromatic hydrocarbons again, increase the yield of desirable aromatic hydrocarbons in the heavy aromatic oil, make full use of limited petroleum resources.
Characteristics of the present invention are: heavy aromatic oil is carried out hydrotreatment and solvent treatment processing, and two processes are organically combined, reach the purpose that the present invention improves heavy arene and stable hydrocarbon raw materials quality in the raw material,, make full use of petroleum resources for the downstream unit high quality raw material.
Specifically, the present invention includes following two kinds of schemes:
Scheme one: heavy aromatic oil raw material (can be one or more mixture of above-mentioned heavy aromatic oil) at first mixes with hydrogen, enters in the charging process furnace and heats.After material is heated to the required temperature of hydrogenation reaction, enter hydrogenator, and contact with hydrogenation catalyst and to carry out hydrogenation reaction.In hydrogenator, the heavy aromatic oil raw material mainly carries out hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and colloid, bituminous matter hydroconversion reactions, and the cracking reaction of stable hydrocarbon is side reaction.Purpose is effectively to reduce the content of undesirable components such as heavy aromatic oil raw material S, N, metal impurities and colloid, bituminous matter, rather than for it being hydrocracking into low boiler cuts such as gasoline, diesel oil, therefore, the chemical hydrogen consumption of this hydrogenation reaction is very low.After hydrogenation reaction finishes, the hydrogenation resultant flows out from reactor, enter gas-liquid separator and carry out gas-liquid separation, the hydrogen-containing gas of wherein telling capable of circulation time reactor after washing, purifying continues to use, and oily the entering after step-down, cooling of liquid phase generation carried out solvent treatment in the solvent refining unit.Solvent and hydrocarbons hydrogenation generate oily countercurrent flow and contact and carry out mass transfer, extract oil out and raffinate oil and flow out from the bottom and the top for the treatment of tower respectively, the flash separator that enters separately carries out separating of solvent and hydrocarbon oil, extracts oil out and returns solvent treatment tower continuation use after isolated solvent converges again with raffinating oil.The heavy arene class oil of extracting out can return hydrogenator again and continue hydro-upgrading, also can go out the raw material that device removes to do industrial chemicals or produces needle coke, asphalt base carbon fiber etc., can go out device and make catalytically cracked material or lube stock etc. and take out surplus saturated hydrocarbons oil.
Scheme two: heavy aromatic oil raw material (can be one or more mixture of above-mentioned heavy aromatic oil) at first enters and carries out solvent treatment in the solvent refining unit.Solvent and hydrocarbons hydrogenation generate oily countercurrent flow and contact and carry out mass transfer, extract oil out and raffinate oil and flow out from the bottom and the top for the treatment of tower respectively, the flash separator that enters separately carries out separating of solvent and hydrocarbon oil, can return the solvent treatment tower again after the extraction oil and the isolated solvent of raffinating oil are joined and continue use.Take out surplus saturated hydrocarbons oil and can go out device, make catalytically cracked material or lube stock etc.And the heavy arene class of extracting out oil mixes with hydrogen, enters in the charging process furnace and heats.After material is heated to the required temperature of hydrogenation reaction, enter hydrogenator, and contact with hydrogenation catalyst and to carry out hydrogenation reaction.In hydrogenator, heavy aromatic oil mainly carries out hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and colloid, bituminous matter hydroconversion reactions, and the cracking reaction of stable hydrocarbon is side reaction.Purpose is effectively to reduce the content of undesirable components such as heavy aromatic oil raw material S, N, metal impurities and colloid, bituminous matter, rather than for it being hydrocracking into low boiler cuts such as gasoline, diesel oil.Therefore, the chemical hydrogen consumption of this hydrogenation reaction is very low.After hydrogenation reaction finishes, the hydrogenation resultant flows out from reactor, enter gas-liquid separator and carry out gas-liquid separation, the hydrogen-containing gas of wherein telling capable of circulation time reactor after washing, purification continues to use, and liquid phase generation oil can return solvent treatment tower continuation solvent upgrading again, also can go out the raw material that device goes to make industrial chemicals or produces needle coke, asphalt base carbon fiber etc.
Comprehensive more above-described two kinds of schemes, wherein first kind of scheme is particularly suitable for the more bad situation of heavy arene stock oil character, and promptly the amount of its contained S, N, metal impurities and colloid, bituminous matter etc. is more; And that second kind of scheme is particularly suitable for heavy arene stock oil character is better, i.e. its contained S, N, metal impurities and less situation such as colloid, bituminous matter.Certainly, also can select a kind of in above two kinds of schemes according to other particular cases such as device, investments.
Hydrotreatment described in the above-mentioned two kinds of schemes of the present invention can be any appropriate process technology that can reach the object of the invention, for example moving-bed hydrogenation technique technology, boiling bed hydrogenation technique technology, its processing condition can be according to required hydrorefined degree of depth decision, with present industrial more sophisticated fixed bed hydrogenation technology is example, when being used for concrete scheme of the present invention, its operational condition is generally: temperature of reaction 340-427 ℃, and preferably 350-400 ℃; Reaction pressure is 6-16MPa, and that best is 8-15MPa; Hydrogen to oil volume ratio is 500-2000, and that best is 700-1500; Volume space velocity is 0.1-5.0h during liquid
-1, that best is 0.2-4.5h
-1
The hydrogenation catalyst that is adopted be meant have hydrodemetallation (HDM), the single catalyst or the combination catalyst of function such as hydrogenating desulfurization, hydrodenitrification and hydrocracking.These catalyzer generally all are to be carrier with porous refractory inorganic oxides such as aluminum oxide, the oxide compound of group vib and/or VIII family metal such as W, Mo, Co, Ni etc. is an active ingredient, optionally adds the catalyzer of other various auxiliary agents such as P, Si, elements such as F, B.And the pore distribution situation of catalyzer preferably can satisfy following requirement: the catalyzer of (1) aperture maximum: diameter accounts for 5% (better be 5%～10%, preferably 10%～15%) of pore volume at least greater than the macropore of 100nm; Surface-area (BET, nitrogen adsorption method) is at 50m
2/ g～200m
2Between/the g, be preferably at 80m
2/ g～200m
2/ g, best is at 100m
2/ g～180m
2/ g, can several apertures in the scope of about 30～90nm, pore volume (mercury penetration method) is at 0.7～1.2cm
3Between/the g, average particulate diameter 0.5～4.5mm is preferably at 0.8～4.5mm, and best is at 1.0～4.5mm.(2) catalyzer of aperture minimum: diameter accounts for 5% (better be 5%～10%, preferably 10%～15%) of pore volume at least greater than the hole of 30nm; Surface-area (BET, nitrogen adsorption method) is at 50m
2/ g～250m
2Between/the g, be preferably at 100m
2/ g～250m
2/ g, best is at 120m
2/ g～250m
2/ g, can several apertures in the scope of about 14～20nm, pore volume (mercury penetration method) is at 0.5～1.1cm
3Between/the g, average particulate diameter 0.5～3.5mm is preferably at 0.8～3.0mm, and best is at 1.0～2.5mm.Aperture, specific surface, the particle diameter of the catalyzer that hydrogenation technique of the present invention uses preferably can meet the index of above-mentioned catalyzer or be between above-mentioned two kinds of catalyzer indexs.Alumina supporter can prepare with any method in common.For example, preparing the method for catalyst oxidation alumina supporter of the present invention can be referring to the United States Patent (USP) the 4179408th (date of publication on December 18th, 1979) of the United States Patent (USP) of Laine etc. No. 4392987 (12 days July nineteen eighty-three of date of publication) and Sanchez etc.After this, can be by pickling process or kneading method commonly used in any suitable method, particularly catalyst preparation technology, the catalyst component that the catalyzer of this beds is required joins on the alumina supporter.Be applicable to that catalyst component of the present invention has vib metal (especially molybdenum and tungsten) and/or VIII family metal (especially cobalt and nickel).The amount of metal active constituent (by the metal oxide compound) is preferably between 4.0～35% (in the catalyst weights), and particle shape can be shapes such as cylindrical, bar shaped, sphere, elliposoidal, trifolium and Herba Galii Bungei.The present invention requires to decide according to the purpose of the heavy arene oil properties of institute's hydrotreatment and/or product and uses a kind of or multiple in the above-mentioned difference in functionality catalyzer.If need to adopt multiple catalyzer, the filling of difference in functionality catalyzer meets the principle of catalyzer grading loading so, and promptly raw material at first contacts with Hydrodemetalation catalyst, and then contacts with hydrogenating desulfurization, hydrodenitrification, hydrogenation conversion catalyst.According to the sequencing meter that contacts with stock oil, the catalyzer of adorning generally is that the aperture is descending in the reactor, and specific surface is ascending, and is active ascending.The scheme that can certainly adopt other to be fit to, as mixed packing, or according to the sequencing meter that contacts with stock oil, the aperture of the catalyzer of adorning is little again to bigger by being up in the reactor, specific surface by minimum to greatly again to less, active by minimum to greatly again to less etc.
Described solvent treatment technology can be any appropriate technology that can reach the object of the invention, for example can use rotating disk contact tower or tray column, hydrocarbon oil feed enters from the bottom, and refining solvent enters from top, carrying out the condition that solvent takes off heavy arene is generally: total extraction solvent and heavy aromatic oil weight ratio are 1.0～5, column bottom temperature is 30～100 ℃, and tower top temperature is higher about 20～50 ℃ than column bottom temperature, and the tower internal pressure is 3～6 normal atmosphere.By the change of solvent ratio and temperature, can control the aromatic hydrocarbons sucrose extraction of heavy oil.Refining solvent is C normally
3～C
8Alkane, phenol, furfural, N-methyl-2 pyrrolidone etc., C wherein
3～C
8Alkane comprise propane, butane, Trimethylmethane, pentane, iso-pentane, hexane or two or more mixture wherein.The preferred furfural of the present invention is made refining solvent.
Concrete when implementing the above-mentioned two kinds of schemes of the present invention, can be according to the difference of raw material oil properties or product purpose, the device operating parameters of arbitrarily adjusting hydrogenation technique and solvent process is fit to industrial requirement, as the catalyzer in the hydrogenation technique, air speed, pressure, hydrogen-oil ratio; Temperature in the solvent treatment technology, agent-oil ratio, solvent etc.
The present invention is applicable to the processing treatment of the residual oil of technologies such as the extraction oil of slurry oil (clarified oil), lube oil finishing technology of catalytic cracking process and viscosity breaking, thermally splitting, Pintsch process and coking recycle oil etc., is particularly useful for the processing treatment of the slurry oil (clarified oil) of catalytic cracking process.
Compared with prior art, the present invention is owing to adopted hydrogenation, solvent-refined process integration, saturated hydrocarbons content in the present heavy aromatic oil is improved, enlarge the material quantity of devices such as catalytic cracking and lubricating oil processing, and the aromatic hydrocarbons in the heavy aromatic oil also obtains upgrading, reduced the content of undesirable components such as S wherein, N, metal impurities and colloid, bituminous matter, make its main raw material that can be used as spinning asphalt, needle coke, synthetic rubber, plastics or auxiliary material, realized that the real of petroleum resources effectively utilizes.
Fig. 1 is the present invention program one a schematic flow sheet, and Fig. 2 is the present invention program two a schematic flow sheet.
Below in conjunction with accompanying drawing and specific embodiment the present invention is elaborated.
As shown in Figure 1, heavy arene stock oil 1 enters 3 heating of charging process furnace with the charging that hydrogen 2 is formed, after being heated to the required temperature of hydrogenator, reaction feed 4 enters fixed bed hydrogenation treatment unit 5, carry out hydrogenation reaction, the resultant of reaction 6 of gained enters resultant separator 8, the hydrogen-rich gas 7 that obtains, can return hydrogenation unit after purifying recycles, 9 of product liquids that obtains enter solvent treatment tower 10 by the bottom of tower after step-down, cooling, refining solvent 11 enters from top.Discharge the bottom that is dissolved in heavy arene class 16 slave units in the refining solvent, tell refining solvent 18 and heavy arene 19 through separator 17, refining solvent 18 returns solvent treatment tower 10, heavy arene 19 then can return hydrogenator again and continue hydro-upgrading, also can go out the raw material that device goes to make industrial chemicals or produces needle coke, asphalt base carbon fiber etc.The saturated hydrocarbons 12 that is insoluble to refining solvent is discharged from solvent treatment tower 10 tops, tell refining solvent 15 and saturated hydrocarbons oil 14 through separator 13, refining solvent 15 returns solvent treatment tower 10, makes catalytically cracked material or lube stock etc. and the saturated hydrocarbons oil that obtains can go out device.
As shown in Figure 2, heavy arene stock oil 1 enters solvent treatment tower 10 by the bottom of tower, and refining solvent 11 enters from top.The saturated hydrocarbons 12 that is insoluble to refining solvent is discharged from solvent treatment tower 10 tops, tell refining solvent 15 and saturated hydrocarbons oil 14 through separator 13, refining solvent 15 returns solvent treatment tower 10, makes catalytically cracked material or lube stock etc. and the saturated hydrocarbons oil that obtains can go out device.Discharge the bottom that is dissolved in heavy arene class 16 slave units in the refining solvent, tell refining solvent 18 and heavy arene 19 through separator 17, refining solvent 18 returns solvent treatment tower 10, heavy arene 19 then enters 3 heating of charging process furnace with the charging that hydrogen 2 is formed, after being heated to the required temperature of hydrogenator, reaction feed 4 enters fixed bed hydrogenation treatment unit 5, carry out hydrogenation reaction, the resultant of reaction 6 of gained enters resultant separator 8, the hydrogen-rich gas 7 that obtains, can return hydrogenation unit after purifying recycles, 9 of the product liquids that obtains can return solvent treatment tower 10 again, also can go out device and remove to do industrial chemicals or produce needle coke, the raw material of asphalt base carbon fiber etc.
This test is carried out with scheme one, and running is carried out on hydrotreatment pilot plant and solvent refining unit.The fixed bed hydrogenation catalyzer physico-chemical property that uses in following test sees Table-1, and the solvent that solvent refining unit uses is furfural.
The stock oil character that this test is used sees Table-2, and test-results sees Table-3.
Table-1 catalyzer physico-chemical property
| Project | Catalyst A | Analytical procedure |
| Shape | Bar shaped | Range estimation |
| Diameter, mm | ???0.9 | Slide calliper rule |
| Pore volume, ml/g | ???1.0 | The nitrogen cryogenic absorption |
| Specific surface area, m 2/g | ???130 | The nitrogen cryogenic absorption |
| ??Nio???????w％ | ???3.0 | |
| ??MoO 3?????w％ | ???9.5 | |
| The hole of＞100nm | ???8％ | |
| Can several apertures, nm | ???30 |
Table-2 stock oil main character
| Project | Stock oil |
| Elementary composition | |
| S，w％ | ????1.04 |
| N，μg/g | ????2300 |
| Carbon residue, w% | ????9.75 |
| Saturated part, w% | ????28.0 |
| Fragrance part, w% | ????49.0 |
| Colloid, w% | ????21.8 |
| Bituminous matter, w% | ????0.14 |
Table-3 combination process processing treatment results
| Embodiment | ????1 | ????2 | ????3 | ????4 | ????5 |
| Fixed bed hydrogenation is handled | |||||
| Temperature, ℃ | ????370 | ????375 | ????380 | ????380 | ????385 |
| Pressure, MPa | ????10.0 | ????12.0 | ????14.0 | ????14.0 | ????15.0 |
| Hydrogen-oil ratio, (V/V) | ????800 | ????1000 | ????1000 | ????1000 | ????1000 |
| Air speed, h -1 | ????0.5 | ????0.5 | ????1.0 | ????1.5 | ????1.5 |
| Hydrogenated oil character | |||||
| S，w％ | ????0.20 | ????0.14 | ????0.13 | ????0.25 | ????0.16 |
| N，μg/g | ????1663 | ????1441 | ????1240 | ????1860 | ????1532 |
| Carbon residue, w% | ????2.30 | ????2.23 | ????2.20 | ????2.54 | ????2.26 |
| Saturated part, w% | ????38.2 | ????39.2 | ????41.2 | ????37.2 | ????40.1 |
| Fragrance part, w% | ????53.8 | ????54.8 | ????55.5 | ????54.4 | ????55.3 |
| Colloid+bituminous matter, w% | ????8.0 | ????6.0 | ????3.3 | ????8.4 | ????4.6 |
| Solvent treatment | |||||
| Column bottom temperature, ℃ | ????40 | ????40 | ????40 | ????50 | ????60 |
| Tower top temperature, ℃ | ????80 | ????80 | ????80 | ????90 | ????85 |
| Pressure, MPa | ????0.5 | ????0.5 | ????0.5 | ????0.5 | ????0.5 |
| Solvent ratio, (V/V) | ????3 | ????2 | ????1 | ????3 | ????2 |
| Extract oil nature out | |||||
| Yield, % | ????38 | ????33 | ????30 | ????40 | ????36 |
| S，w％ | ????0.45 | ????0.33 | ????0.29 | ????0.49 | ????0.37 |
| N，μg/g | ????4290 | ????3738 | ????3550 | ????4507 | ????4122 |
| Carbon residue, w% | ????7.3 | ????6.4 | ????5.1 | ????7.5 | ????5.9 |
| Fragrance part, w% | ????81.1 | ????84.2 | ????89.8 | ????80.1 | ????88.9 |
| Colloid+bituminous matter, w% | ????18.9 | ????15.8 | ????10.2 | ????19.9 | ????11.1 |
| The character of raffinating oil | |||||
| Yield, % | ????62 | ????67 | ????70 | ????60 | ????64 |
| S，w％ | ????0.04 | ????0.04 | ????0.05 | ????0.08 | ????0.05 |
| N，μg/g | ????68 | ????323 | ????264 | ????112 | ????92 |
| Saturated part, w% | ????61.3 | ????58.2 | ????58.6 | ????61.7 | ????62.5 |
| Fragrance part, w% | ????38.7 | ????41.8 | ????41.4 | ????38.3 | ????37.5 |
This test is carried out with scheme two, and running is carried out on hydrotreatment pilot plant and solvent refining unit.The fixed bed hydrogenation catalyzer physico-chemical property that uses in following test sees Table-1, and the solvent that solvent refining unit uses is furfural.
The stock oil character that this test is used sees Table-4, and test-results sees Table-5.
Table-4 stock oil main character
| Project | Stock oil |
| Elementary composition | |
| S，w％ | ????0.27 |
| ?N，μg/g | ????6546 |
| Carbon residue, w% | ????0.14 |
| Saturated part, w% | ????58.4 |
| Fragrance part, w% | ????32.3 |
| Colloid+bituminous matter, w% | ????9.3 |
Table-5 combination process processing treatment results
| Embodiment | ????6 | ????7 | ????8 | ????9 | ????10 |
| Solvent treatment | |||||
| Column bottom temperature, ℃ | ????40 | ????40 | ????40 | ????50 | ????50 |
| Tower top temperature, ℃ | ????80 | ????80 | ????80 | ????90 | ????90 |
| Pressure, MPa | ????0.5 | ????0.5 | ????0.5 | ????0.5 | ????0.5 |
| Solvent ratio, (V/V) | ????3 | ????2 | ????1 | ????3 | ????2 |
| The character of raffinating oil | |||||
| Yield, % | ????68 | ????72 | ????75 | ????65 | ????70 |
| S，w％ | ????0.08 | ????0.12 | ????0.14 | ????0.05 | ????0.10 |
| N，μg/g | ????1193 | ????1287 | ????1339 | ????1011 | ????1232 |
| Saturated part, w% | ????84.8 | ????80.4 | ????77.3 | ????87.4 | ????81.8 |
| Fragrance part, w% | ????15.2 | ????19.6 | ????12.7 | ????12.6 | ????18.2 |
| Extract oil nature out | |||||
| Yield, % | ????32 | ????28 | ????25 | ????35 | ????30 |
| S，w％ | ????0.61 | ????0.58 | ????0.56 | ????0.62 | ????0.59 |
| N，μg/g | ????17921 | ????20069 | ????25020 | ????16825 | ????18945 |
| Carbon residue, w% | ????8.33 | ????8.39 | ????8.21 | ????8.31 | ????8.36 |
| Saturated part, w% | ????1.1 | ????0.5 | ????0 | ????3.4 | ????2.5 |
| Fragrance part, w% | ????70.8 | ????67.4 | ????93.9 | ????70.9 | ????67.5 |
| Colloid+bituminous matter, w% | ????28.1 | ????32.1 | ????6.1 | ????25.7 | ????30.0 |
| Extracting oily fixed bed hydrogenation out handles | |||||
| Temperature, ℃ | ????370 | ????375 | ????380 | ????380 | ????385 |
| Pressure, MPa | ????10.0 | ????12.0 | ????14.0 | ????14.0 | ????15.0 |
| Hydrogen-oil ratio, (V/V) | ????800 | ????1000 | ????1000 | ????1000 | ????1000 |
| Air speed, h -1 | ????0.5 | ????0.5 | ????1.0 | ????1.5 | ????1.5 |
| Hydrogenated oil character | |||||
| S，w％ | ????0.12 | ????0.08 | ????0.07 | ????0.15 | ????0.09 |
| N，μg/g | ????12956 | ????12583 | ????13485 | ????13611 | ????12617 |
| Carbon residue, w% | ????1.96 | ????1.92 | ????1.85 | ????2.16 | ????1.94 |
| Saturated part, w% | ????10.1 | ????11.7 | ????13.2 | ????9.6 | ????14.6 |
| Fragrance part, w% | ????75.6 | ????73.2 | ????85.0 | ????76.3 | ????74.0 |
| Colloid+bituminous matter, w% | ????14.3 | ????15.1 | ????1.8 | ????14.1 | ????11.4 |
Claims (14)
1, a kind of working method of heavy aromatic oil, comprise: raw material at first mixes with hydrogen, enter in the charging process furnace and heat, after being heated to the required temperature of hydrogenation reaction, material enters hydrogenator, and contact with hydrogenation catalyst and to carry out hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and colloid, bitum hydroconversion reactions, after hydrogenation reaction finishes, the hydrogenation resultant flows out from reactor, enter gas-liquid separator and carry out gas-liquid separation, the liquid phase generation oil of telling enters and carries out solvent treatment in the solvent refining unit, solvent and hydrocarbons hydrogenation generate oily countercurrent flow and contact and carry out mass transfer, extract oil out and raffinate oil and flow out from described solvent refining unit bottom and top respectively, the flash separator that enters separately carries out separating of solvent and hydrocarbon oil, tells solvent, heavy arene class oil and saturated hydrocarbons oil.
2, according to the working method of the described heavy aromatic oil of claim 1, the operational condition that it is characterized in that described hydrogenation reaction is: temperature of reaction 340-427 ℃, reaction pressure is 6-16MPa, and hydrogen to oil volume ratio is 500-2000, and volume space velocity is 0.1-5.0h during liquid
-1
3, according to the working method of the described heavy aromatic oil of claim 1, the operational condition that it is characterized in that described hydrogenation reaction is: temperature of reaction 350-400 ℃, reaction pressure is 8-15MPa, and hydrogen to oil volume ratio is 700-1500, and volume space velocity is 0.2-4.5h during liquid
-1
4, according to the working method of the described heavy aromatic oil of claim 1, it is characterized in that described catalyst carrier for hydrgenating is porous refractory inorganic oxides and/or molecular sieve, active ingredient is group vib and/or VIII family metal component.
5, according to the working method of the described heavy aromatic oil of claim 1, it is characterized in that described solvent refining unit is rotating disk contact tower or tray column, described hydrocarbon oil feed enters from the bottom, refining solvent enters from top, carrying out the condition that solvent takes off heavy arene is: total extraction solvent and heavy aromatic oil weight ratio are 1.0～5, column bottom temperature is 30～100 ℃, and tower top temperature is higher about 20～50 ℃ than column bottom temperature, and the tower internal pressure is 3～6 normal atmosphere.
6,, it is characterized in that described refining solvent is to be selected from C according to the working method of the described heavy aromatic oil of claim 1
3～C
8Alkane, phenol, furfural, N-methyl-2 pyrrolidone in one or more.
7,, it is characterized in that described refining solvent is a furfural according to the working method of the described heavy aromatic oil of claim 1.
8, a kind of working method of heavy aromatic oil, comprise: the heavy aromatic oil raw material at first enters and carries out solvent treatment in the solvent refining unit, solvent and hydrocarbons hydrogenation generate oily countercurrent flow and contact and carry out mass transfer, extract oil out and raffinate oil and flow out from the bottom and the top for the treatment of tower respectively, the flash separator that enters separately carries out separating of solvent and hydrocarbon oil, isolates solvent, takes out surplus saturated hydrocarbons oil and the heavy arene class oil of extracting out; The heavy arene class oil of described extraction mixes with hydrogen, enter in the charging process furnace and heat, after being heated to the required temperature of hydrogenation reaction, material enters hydrogenator, and contact with hydrogenation catalyst and to carry out hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and colloid, bituminous matter hydroconversion reactions, after hydrogenation reaction finishes, the hydrogenation resultant flows out from reactor, enters gas-liquid separator and carries out gas-liquid separation, tells gas and liquid-phase product.
9, according to the working method of the described heavy aromatic oil of claim 8, it is characterized in that described solvent refining unit is rotating disk contact tower or tray column, described hydrocarbon oil feed enters from the bottom, refining solvent enters from top, carrying out the condition that solvent takes off heavy arene is: total extraction solvent and heavy aromatic oil weight ratio are 1.0～5, column bottom temperature is 30～100 ℃, and tower top temperature is higher about 20～50 ℃ than column bottom temperature, and the tower internal pressure is 3～6 normal atmosphere.
10,, it is characterized in that described refining solvent is to be selected from C according to the working method of the described heavy aromatic oil of claim 8
3～C
8Alkane, phenol, furfural, N-methyl-2 pyrrolidone in one or more.
11,, it is characterized in that described refining solvent is a furfural according to the working method of the described heavy aromatic oil of claim 8.
12, according to the working method of the described heavy aromatic oil of claim 8, the operational condition that it is characterized in that described hydrogenation reaction is: temperature of reaction 340-427 ℃, reaction pressure is 6-16MPa, and hydrogen to oil volume ratio is 500-2000, and volume space velocity is 0.1-5.0h during liquid
-1
13, according to the working method of the described heavy aromatic oil of claim 8, the operational condition that it is characterized in that described hydrogenation reaction is: temperature of reaction 350-400 ℃, reaction pressure is 8-15MPa, and hydrogen to oil volume ratio is 700-1500, and volume space velocity is 0.2-4.5h during liquid
-1
14, according to the working method of the described heavy aromatic oil of claim 8, it is characterized in that described catalyst carrier for hydrgenating is porous refractory inorganic oxides and/or molecular sieve, active ingredient is group vib and/or VIII family metal component.
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