CN1382766A - Process for viscosity breaking of deoiled asphalt - Google Patents
Process for viscosity breaking of deoiled asphalt Download PDFInfo
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- CN1382766A CN1382766A CN 01115495 CN01115495A CN1382766A CN 1382766 A CN1382766 A CN 1382766A CN 01115495 CN01115495 CN 01115495 CN 01115495 A CN01115495 A CN 01115495A CN 1382766 A CN1382766 A CN 1382766A
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- viscosity breaking
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Abstract
A process for viscosity breaking of deoiled asphalt produced by the apparatus using solvent to remove oil from asphalt features that said deoiled asphalt and the catalytic cracking clean oil (1-50%) are fed in the flow-up viscosity breaking apparatus and a low-temp long-stay operation manner is used. It has high effect on reducing viscosity.
Description
The invention belongs to a kind of under the situation that does not have hydrogen the method for the thermal non-catalytic cracking of hydrocarbon ils, more particularly, the present invention is a kind of heavy oil residue carries out viscosity breaking through the de-oiled asphalt of solvent deasphalting unit production a method.
Viscosity breaking technology is one of heavy oil lighting means, is a kind of special applications of heavy oil residue thermal cracking process, and its main purpose is to reduce to greatest extent the viscosity of residual oil, reduces the consumption of dilution light oil in the merchantable fuels oil.The heavy oil residue viscosity breaking is the heavy oil residue complete processing that cracking and condensation two class different directions thermal responses take place at a certain temperature.The reduction of viscosity mainly causes owing to non-asphaltene carries out thermo-cracking.
Solvent deasphalting technology is a kind of heavy oil residue deep processing technology of existing six more than ten years industrialization history, this technology is mainly used in the production heavy grease in early days, widespread usage along with residual oil deep processing technology, utilize this explained hereafter catalytically cracked material to provide residual oil reasonable utilization ratio, when improving the deasphalted oil yield, the obvious variation of de-oiled asphalt quality of coproduction, this gilsonite inferior can not be as petroleum pitch, the oil if act as a fuel, because viscosity height, need call in Macrodilution light oil, very uneconomical.
De-oiled asphalt is a kind of special colloidal solution, in this system, the aromatic nucleus that has different side chains interconnects in flakes, interconnect nucleation between sheet and the sheet again, the various higher hydrocabons of these nuclear absorption, the disperse phase of constitution system, the external phase of various small molecules aromatic compounds and alkane constitution system.Because de-oiled asphalt is enrichment bituminous matter and the heavy gelationus component that obtains behind solvent extraction from heavy oil residue.Under thermal rection condition, de-oiled asphalt is compared with heavy oil residue, and the heavy constituent among the former are easier separates out, and the coking tendency is bigger.
In recent years, in order to solve the problem of outlet of de-oiled asphalt, bituminous transforms and more and more comes into one's own.For example:
USP4,428,824 disclose solvent deasphalting technology and viscosity breaking technology anabolic process, be that heavy oil residue is after solvent deasphalting is handled, the viscosity breaking process is carried out in the deasphalted oil that obtains, and then the de-oiled asphalt of solvent deasphalting explained hereafter and deasphalted oil after the viscosity breaking process are reconciled into again the oil fuel of low viscosity and pour point, this technology is for the prolongation cycle, having avoided heavy component is the thermal transition of de-oiled asphalt, and be the light constituent that high quality can be used for downstream cracking (as catalytic cracking and hydrocracking etc.) device processing that viscosity breaking is carried out in deasphalted oil, tooling cost is increased.
EP0133774 discloses a kind of method of viscosity breaking, and this method adds hydrogen supply agent catalytically cracked oil and light cycle oil in the viscosity breaking process, to improve the severity of viscosity breaking, reaches the purpose that reduces heavy oil residue.But, therefore, will shorten on-stream time greatly, and system is resulted in blockage, weares and teares, and influence quality product owing to contain catalyst fines in catalytically cracked oil and the light cycle oil.
USP4,298,455 disclose a kind of reduction method of viscosity, and this method is to add radical initiator and chain-transfer agent in heavy oil residue, carries out viscosity breaking under the mitigation condition, reduces the reaction severity and reaches the purpose that reduces viscosity.Though can prolong on-stream time under the mitigation condition, the radical initiator and the chain-transfer agent that add are organic compound, have increased cost and expense.
The viscosity breaking method that the purpose of this invention is to provide a kind of de-oiled asphalt is to reduce the viscosity of de-oiled asphalt.
The objective of the invention is to realize by following proposal: heavy feed stock enters solvent deasphalting unit, obtains deasphalted oil and de-oiled asphalt through low molecule alkane solvent extracting; Catalytically cracked oil enters the sedimentation tower, removes wherein the last fluid catalytic cracking decant oil that obtains of catalyst powder through sedimentation; De-oiled asphalt is with after fluid catalytic cracking decant oil mixes, enter the process furnace heating of upflow visbreaking cracking unit, enter the reactor of viscosity breaking plant then, in reactor, carry out the viscosity breaking reaction, reactant flow enters the separation column of viscosity breaking plant, fractionate out visbreaking gas, visbreaking gasoline and visbreaking residue, visbreaking residue can be used as heavy fuel oil (HFO).
Detail operations process of the present invention comprises:
(1), heavy feed stock enters solvent deasphalting unit, solvent be propane, butane, pentane or above-mentioned two or three with arbitrary proportion blended solvent, extraction temperature is 60～280 ℃, pressure is 1.0～6.0MPa, solvent ratio is 1.0～15.0v/v, and gained de-oiled asphalt yield is 10～90m%;
(2), catalytically cracked oil enters the sedimentation tower at the bottom of catalytic cracking fractionating tower, sedimentation tower temperature is 70 ℃～250 ℃, the settling time is 1～120 hour, removes the last fluid catalytic cracking decant oil that obtains of catalyst powder wherein;
(3), fluid catalytic cracking decant oil and de-oiled asphalt are according to part by weight 0.01～1.0: 1 mixes, mixture enters upflow visbreaking cracking unit process furnace, the furnace outlet temperature is 370 ℃～480 ℃, water injection rate is 1.0～10.0% (accounting for parallel feeding), the mixture that heated enters reactor from the reactor bottom of upflow visbreaking cracking unit, the reactor bottom temperature is 350 ℃～470 ℃, head temperature is 340 ℃～460 ℃, the residence time is 10～120 minutes, working pressure is 0.1～1.5MPa, reactant flow is overflowed from the reactor head of upflow visbreaking cracking unit, enter the separation column of upflow visbreaking cracking unit, separate obtaining visbreaking gas, visbreaking gasoline and visbreaking residue.
The used heavy feed stock of solvent deasphalting is that long residuum, vacuum residuum, visbreaking residue, catalytically cracked oil, hydrocracking tail oil, ethylene residue and the lubricating oil of any crude oil is extracted oil and two or more mixing oil thereof out.
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction, but the present invention is not limited thereto.
Accompanying drawing is the schematic flow sheet of process for viscosity breaking of deoiled asphalt provided by the present invention.
Heavy oil residue and low molecule alkane solvent enter solvent deasphalting unit 3 through pipeline 1 and 2 respectively, and the deasphalted oil behind solvent extraction can be sent into downstream unit processing through pipeline 4, produces simultaneously de-oiled asphalt.
Catalytic cracked oil pulp (not marking the figure) at the bottom of the catalytic cracking fractionating tower out enters sedimentation tower 7 through pipeline 6, through heating sedimentation Removal of catalyst powder, then out mix with de-oiled asphalt from pipeline 5 through pipeline 8 from sedimentation tower, mixed logistics enters heating furnace 10 heating of upflow visbreaking cracking unit through pipeline 9, the logistics that heated enters reactor through pipeline 11 from reactor 12 bottoms of upflow visbreaking cracking unit, overflow from reactor head through the logistics that visbreaking was reacted, enter the fractionating column 14 of upflow visbreaking cracking unit through pipeline 13, separate the visbreaking gas, visbreaking gasoline and the visbreaking residue that obtain and go out device through pipeline 15,16 and 17 respectively.
Advantage of the present invention:
(1), owing to removed the catalyst fines of catalytic cracked oil pulp, avoided coking, obstruction and the wearing and tearing of device, the reactor product quality can satisfy the requirement of fuel oil.
(2) although de-oiled asphalt viscosity is very high, by method of the present invention, after the visbreaking reaction, can be used as fuel oil, for its outlet provides effective processing approach.
(3), because the mixing of fluid catalytic cracking decant oil more tended towards stability the de-oiled asphalt colloid systems, in being subjected to thermal process, greatly reduce the coking tendency, prolong the on-stream time of visbreaking unit.
Further describe characteristics of the present invention below in conjunction with embodiment.
Embodiment 1
The solvent deasphalting raw material that present embodiment adopts is vacuum residuum A, and vacuum residuum A obtains de-oiled asphalt behind propane deasphalting, and the de-oiled asphalt yield is 50m%.The character of vacuum residuum A and de-oiled asphalt sees Table 1 and table 2 respectively.As can be seen from Table 2, the kinematic viscosity of de-oiled asphalt under 100 ℃ is 5 times of vacuum residuum A, but as cracked component stable hydrocarbon 15.4m% is only arranged, and colloid is up to nearly 50m%.
150 ℃ of following sedimentations after 48 hours, ash has reduced by 75% to catalytically cracked oil in slurry tank, and metallic aluminium content has reduced more than 80%.Fluid catalytic cracking decant oil with carry out viscosity breaking after above-mentioned de-oiled asphalt mixes according to weight ratio at 0.042: 1, the viscosity breaking test is to carry out on treatment capacity is 5 kilograms/hour medium-sized viscosity breaking plant.Table 3 is the mixture character of fluid catalytic cracking decant oil and de-oiled asphalt, and table 4 is the viscosity breaking technology condition and the material balance of mixture.Table 5 is the character of visbreaking residue.As can be seen from Table 5, the viscosity of de-oiled asphalt (100 ℃) has dropped to 123mm
2/ s, the visbreaking effect is obvious.
Embodiment 2
With the fluid catalytic cracking decant oil among the embodiment 1 with carry out the viscosity breaking test after de-oiled asphalt mixes according to weight ratio at 0.087: 1.The mixture character of fluid catalytic cracking decant oil and de-oiled asphalt is as shown in table 3, and table 4 is the viscosity breaking technology condition and the material balance of mixture.Table 5 is the character of visbreaking residue.As can be seen from Table 5, the viscosity of de-oiled asphalt (100 ℃) has dropped to 118.3mm
2/ s, the visbreaking effect is obvious.
Embodiment 3
With the fluid catalytic cracking decant oil among the embodiment 1 with carry out the viscosity breaking test after de-oiled asphalt mixes according to weight ratio at 0.111: 1.The mixture character of fluid catalytic cracking decant oil and de-oiled asphalt is as shown in table 3, and table 4 is the viscosity breaking technology condition and the material balance of mixture.Table 5 is the character of visbreaking residue.As can be seen from Table 5, the viscosity of de-oiled asphalt (100 ℃) has dropped to 105.8mm
2/ s, the visbreaking effect is obvious.
Embodiment 4
The solvent deasphalting raw material that present embodiment adopts is vacuum residuum B, and vacuum residuum B obtains de-oiled asphalt behind butane deasphalting, and the de-oiled asphalt yield is 63m%.The character of vacuum residuum A and de-oiled asphalt sees Table 1 and table 2 respectively.As can be seen from Table 2, the kinematic viscosity of de-oiled asphalt under 100 ℃ is 10 times of vacuum residuum B approximately, but as cracked component stable hydrocarbon 5.2m% is only arranged, and colloid is up to 52m%.
With the fluid catalytic cracking decant oil among the embodiment 1 with carry out the viscosity breaking test after above-mentioned de-oiled asphalt mixes according to weight ratio at 0.053: 1.The mixture character of fluid catalytic cracking decant oil and de-oiled asphalt is as shown in table 6, and table 7 is the viscosity breaking technology condition and the material balance of mixture.Table 8 is the character of visbreaking residue.As can be seen from Table 8, the viscosity of de-oiled asphalt (100 ℃) has dropped to 962.6mm
2/ s, the visbreaking effect is obvious.
Embodiment 5
With the fluid catalytic cracking decant oil among the embodiment 1 with carry out the viscosity breaking test after above-mentioned de-oiled asphalt among the embodiment 4 mixes according to weight ratio at 0.111: 1.The mixture character of fluid catalytic cracking decant oil and de-oiled asphalt is as shown in table 6, and table 7 is the viscosity breaking technology condition and the material balance of mixture.Table 8 is the character of visbreaking residue.As can be seen from Table 8, the viscosity of de-oiled asphalt (100 ℃) has dropped to 954.56mm
2/ s, the visbreaking effect is obvious.
Table 1
| Vacuum residuum A | Vacuum residuum B | Clarified oil | |
| Density (20 ℃), g/cm 3 | ????0.9207 | ????0.9709 | ????1.027 |
| Kinematic viscosity (100 ℃), mm 2/s | ????122 | ????765.4 | ????11.43 |
| Condensation point, ℃ | ????38 | ????35 | ????27 |
| Hydrocarbon system forms, m% | |||
| Stable hydrocarbon | ????31.7 | ????27.00 | ????29.8 |
| Aromatic hydrocarbons | ????35.1 | ????35.20 | ????59.0 |
| Colloid | ????33.0 | ????35.50 | ????10.6 |
| Bituminous matter | ????0.20 | ????2.30 | ????0.6 |
Table 2
| The solvent deoiling asphalt stock | Vacuum residuum A | Vacuum residuum B |
| Solvent | Propane | Butane |
| Processing condition | ||
| Extraction temperature, ℃ | ????65 | ????82 |
| Pressure, MPa | ????3.8 | ????3.5 |
| Solvent ratio, v/v | ????6/1 | ????6/1 |
| The de-oiled asphalt yield, m% | ????50 | ????37 |
| De-oiled asphalt character | ||
| Density (20 ℃), g/cm 3 | ????0.9528 | ????1.037 |
| Kinematic viscosity (100 ℃), mm 2/s | ????620.4 | ????7334 |
| Condensation point, ℃ | ????740 | ????740 |
| Hydrocarbon system forms, m% | ||
| Stable hydrocarbon | ????15.4 | ????5.2 |
| Aromatic hydrocarbons | ????35.2 | ????39.04 |
| Colloid | ????49.2 | ????52.3 |
| Bituminous matter | ????0.2 | ????3.46 |
Table 3
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| The clarified oil mixed ratio, m% | ????4.2 | ????8.7 | ????11.1 |
| Density (20 ℃), g/cm 3 | ????0.9683 | ????0.9874 | ????0.9989 |
| Kinematic viscosity (100 ℃), mm 2/s | ????589.6 | ????568.8 | ????548.9 |
| Condensation point, ℃ | ????38 | ????35 | ????34 |
| Hydrocarbon system forms, m% | |||
| Stable hydrocarbon | ????16.5 | ????17.1 | ????17.9 |
| Aromatic hydrocarbons | ????35.8 | ????37.3 | ????36.7 |
| Colloid | ????47.3 | ????45.2 | ????44.9 |
| Bituminous matter | ????0.4 | ????0.4 | ????0.5 |
Table 4
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| The clarified oil mixed ratio, m% | ????4.2 | ????8.7 | ????11.1 |
| Processing condition | |||
| Temperature of reaction, ℃ | ????420 | ????420 | ????420 |
| Reaction pressure, MPa | ????0.40 | ????0.40 | ????0.40 |
| The residence time, minute | ????40 | ????40 | ????40 |
| Material balance, m% | |||
| Visbreaking gas | ????1.52 | ????1.61 | ????1.83 |
| Visbreaking gasoline | ????2.40 | ????2.48 | ????2.51 |
| Visbreaking residue | ????96.08 | ????95.91 | ????95.66 |
Table 5
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| The clarified oil mixed ratio, m% | ????4.2 | ????8.7 | ????11.1 |
| Density (20 ℃), g/cm 3 | ????0.9605 | ????0.9677 | ????0.9752 |
| Kinematic viscosity (100 ℃), mm 2/s | ????123.0 | ????118.3 | ????105.8 |
| Condensation point, ℃ | ????26 | ????27 | ????29 |
| Stability, level | ????1.5 | ????1.5 | ????1.5 |
| Compatibleness, level | ????1.5 | ????1.5 | ????1.5 |
Table 6
| Embodiment 4 | Embodiment 5 | |
| The clarified oil mixed ratio, m% | ????5.3 | ????11.1 |
| Density (20 ℃), g/cm 3 | ????1.0284 | ????1.0298 |
| Kinematic viscosity (100 ℃), mm 2/s | ????6987 | ????6681 |
| Condensation point, ℃ | ????39 | ????38 |
| Hydrocarbon system forms, m% | ||
| Stable hydrocarbon | ????5.9 | ????6.2 |
| Aromatic hydrocarbons | ????39.4 | ????40.1 |
| Colloid | ????51.4 | ????50.6 |
| Bituminous matter | ????3.3 | ????3.1 |
Table 7
| Embodiment 4 | Embodiment 5 | |
| The clarified oil mixed ratio, m% | ????5.3 | ????11.1 |
| Processing condition | ||
| Temperature of reaction, ℃ | ????415 | ????415 |
| Reaction pressure, MPa | ????0.40 | ????0.40 |
| The residence time, minute | ????50 | ????50 |
| Material balance, m% | ||
| Visbreaking gas | ????1.06 | ????1.53 |
| Visbreaking gasoline | ????2.43 | ????2.89 |
| Visbreaking residue | ????96.51 | ????95.58 |
Table 8
| Embodiment 4 | Embodiment 5 | |
| The clarified oil mixed ratio, m% | ????5 | ????10 |
| Density (20 ℃), g/cm 3 | ????0.9984 | ????0.9899 |
| Kinematic viscosity (100 ℃), mm 2/s | ????962.6 | ????954.5 |
| Condensation point, ℃ | ????35 | ????34 |
| Stability, level | ????1.0 | ????1.0 |
| Compatibleness, level | ????1.5 | ????1.0 |
Claims (8)
1, a kind of process for viscosity breaking of deoiled asphalt comprises:
(1), heavy feed stock enters solvent deasphalting unit, obtains deasphalted oil and de-oiled asphalt through low molecule alkane solvent extracting;
(2), catalytically cracked oil enters the sedimentation tower, removes wherein the last fluid catalytic cracking decant oil that obtains of catalyst powder through sedimentation;
(3), de-oiled asphalt is with after fluid catalytic cracking decant oil mixes, enter the process furnace heating of upflow visbreaking cracking unit, enter the reactor of viscosity breaking plant then, in reactor, carry out the viscosity breaking reaction, reactant flow enters the separation column of viscosity breaking plant, fractionates out visbreaking gas, visbreaking gasoline and visbreaking residue.
2,, it is characterized in that the described heavy feed stock of step (1) is long residuum, vacuum residuum, visbreaking residue, catalytically cracked oil, hydrocracking tail oil, ethylene residue and the lubricating oil extraction oil and two or more the mixing oil thereof of any crude oil according to the method for claim 1.
3,, it is characterized in that the described solvent of step (1) is that propane, butane, pentane or above-mentioned two or three are with arbitrary proportion blended mixture according to the method for claim 1.
4, according to the method for claim 1, it is characterized in that the operational condition of solvent deasphalting in the step (1) is as follows: extraction temperature is 60～280 ℃, and pressure is 1.0～6.0MPa, and solvent ratio is 1.0～15.0v/v.
5, according to the method for claim 1, it is characterized in that settling temperature is 70 ℃～250 ℃ in the step (2), the settling time is 1～120 hour.
6, according to the method for claim 1, it is characterized in that fluid catalytic cracking decant oil in the step (3) and de-oiled asphalt are according to part by weight 0.01～1.0: 1 mixes.
7, according to the method for claim 1, it is characterized in that the furnace outlet temperature in the step (3) is 370 ℃～480 ℃, water injection rate is 1.0～10.0m%.
8, according to the method for claim 1, it is characterized in that the reactor bottom temperature in the step (3) is 350 ℃～470 ℃, head temperature is 340 ℃～460 ℃, and the residence time is 10～120 minutes, and working pressure is 0.1～1.5MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01115495 CN1195822C (en) | 2001-04-28 | 2001-04-28 | Process for viscosity breaking of deoiled asphalt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01115495 CN1195822C (en) | 2001-04-28 | 2001-04-28 | Process for viscosity breaking of deoiled asphalt |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1382766A true CN1382766A (en) | 2002-12-04 |
| CN1195822C CN1195822C (en) | 2005-04-06 |
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ID=4662009
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01115495 Expired - Lifetime CN1195822C (en) | 2001-04-28 | 2001-04-28 | Process for viscosity breaking of deoiled asphalt |
Country Status (1)
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| CN (1) | CN1195822C (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103788969A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Combined process for co-pyrolysis of coal and petroleum refining by-product |
| CN104327879A (en) * | 2014-09-19 | 2015-02-04 | 佛山高富中石油燃料沥青有限责任公司 | Fuel oil, aromatic hydrocarbon oil and asphalt combined production process |
| CN104650952A (en) * | 2013-11-21 | 2015-05-27 | 中国石油天然气股份有限公司 | Tower visbreaking thermal residence time estimation method and reaction device |
| CN104650954A (en) * | 2013-11-21 | 2015-05-27 | 中国石油天然气股份有限公司 | Visbreaking thermal residence time estimation method and reaction device |
| CN105400543A (en) * | 2015-12-18 | 2016-03-16 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN106164224A (en) * | 2014-02-25 | 2016-11-23 | 沙特基础工业公司 | Preparation is for the method for the raw material of hydrotreating unit |
| CN116410786A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Method for improving viscosity reduction cracking efficiency and product distribution of heavy oil |
-
2001
- 2001-04-28 CN CN 01115495 patent/CN1195822C/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103788969A (en) * | 2012-11-01 | 2014-05-14 | 中国石油化工股份有限公司 | Combined process for co-pyrolysis of coal and petroleum refining by-product |
| CN104650952A (en) * | 2013-11-21 | 2015-05-27 | 中国石油天然气股份有限公司 | Tower visbreaking thermal residence time estimation method and reaction device |
| CN104650954A (en) * | 2013-11-21 | 2015-05-27 | 中国石油天然气股份有限公司 | Visbreaking thermal residence time estimation method and reaction device |
| CN104650952B (en) * | 2013-11-21 | 2016-06-08 | 中国石油天然气股份有限公司 | Tower visbreaking thermal residence time estimation method and reaction device |
| CN104650954B (en) * | 2013-11-21 | 2016-11-23 | 中国石油天然气股份有限公司 | Visbreaking thermal residence time estimation method and reaction device |
| CN106164224A (en) * | 2014-02-25 | 2016-11-23 | 沙特基础工业公司 | Preparation is for the method for the raw material of hydrotreating unit |
| CN106164224B (en) * | 2014-02-25 | 2018-09-14 | 沙特基础工业公司 | The method for preparing the raw material for hydrotreating unit |
| US10125329B2 (en) | 2014-02-25 | 2018-11-13 | Saudi Basic Industries Corporation | Process for the preparation of a feedstock for a hydroprocessing unit |
| CN104327879A (en) * | 2014-09-19 | 2015-02-04 | 佛山高富中石油燃料沥青有限责任公司 | Fuel oil, aromatic hydrocarbon oil and asphalt combined production process |
| CN105400543A (en) * | 2015-12-18 | 2016-03-16 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN105400543B (en) * | 2015-12-18 | 2017-02-01 | 广东石油化工学院 | Blend oil product and preparation method thereof |
| CN116410786A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Method for improving viscosity reduction cracking efficiency and product distribution of heavy oil |
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|---|---|
| CN1195822C (en) | 2005-04-06 |
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