CN1160441C - Technological route for treating s-contained crude oil - Google Patents
Technological route for treating s-contained crude oil Download PDFInfo
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- CN1160441C CN1160441C CNB001231553A CN00123155A CN1160441C CN 1160441 C CN1160441 C CN 1160441C CN B001231553 A CNB001231553 A CN B001231553A CN 00123155 A CN00123155 A CN 00123155A CN 1160441 C CN1160441 C CN 1160441C
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Abstract
The present invention discloses a processing flow of sulfur bearing crude oil, which is characterized in that technologies, such as normal-pressure and reduced-pressure distillation, coking or solvent deasphalting, medium pressure hydrocracking, catalytic cracking, etc., are organically combined so that a refinery can treat high sulfur raw oil having a sulfur content of 1.8 to 2.8%. Due to the adoption of the medium pressure hydrocracking technology, the requirement of the market for higher and higher diesel oil/gasoline ratio can also be met while material feeding by catalytic cracking is improved, and a low sulfur light fraction conforming to product indexes and environmental protection specifications can be finally produced to reasonably utilize petroleum resources.
Description
The present invention relates to the processing scheme of a kind of processing scheme of sulphur-bearing crude, particularly high-sulfur crude oil.
Along with the national economy fast development, the oil consumption amount is in rapid rising.And domestic crude production rate descends day by day, and oil quality also worse and worse, thereby each refinery a large amount of imported crude oil of will having to consider to process.And the imported crude oil major part is a sulphur-bearing crude, and as middle-eastern crude, it will be sulphur-bearing crude that this crude oil that will cause processing from now on will have greatly.In the face of existing situation, press for how rationally this new problem of Sulfur-Containing Crude, particularly high-sulfur crude oil of solution.The complete processing of how rationally to arrange the work flow of sulphur-bearing crude and developing new sulphur-bearing crude is oil refining scientific worker's a top priority.The processing treatment of crude oil will not be lower boiling, utilizable product with its cracking still, as intermediate oils such as liquefied gas, petroleum naphtha, steam coal diesel oil, but also will improve their hydrogen-carbon ratio, and generally the method by decarburization or hydrogenation realizes.Wherein decarbonization process comprises coking, solvent deasphalting, heavy oil fluid catalytic cracking etc.; Hydrogenation technique comprises residual hydrogenation, hydrocracking, hydrofining etc.At present, in the technology of process residual oils still based on decarbonization process, as coking process, this technology is compared with other technology, and it is simple to have technology, flexible operation, less investment, advantages such as the character that do not processed raw material restriction have become the main means of heavy oil upgrading in the refinery.
The processing of high-sulfur distillate generally is to carry out hydrogenating desulfurization earlier, and then carries out catalytic cracking.USP4780193 has described a kind of work flow of sulphur-bearing crude, and in this patent, crude oil is through behind the atmospheric and vacuum distillation, and vacuum residuum goes delayed coking, wax tailings with carry out hydrotreatment after VGO mixes with certain proportion, the tail oil after the processing carries out catalytic cracking.In this flow process, VGO and wax oil all carry out hydrotreatment, because its transformation efficiency low (＜20%), tail oil all enters catalytic cracking unit after the hydrotreatment, can increase the burden of catalytic cracking, in addition, the diesel and gasoline ratio of catalytic cracking is low, can not satisfy more and more higher diesel and gasoline ratio needs.
The objective of the invention is to develop a kind of work flow of sulphur-bearing crude.Use work flow of the present invention, can under the situation that guarantees desulfurization, denitrogenation, metal removal effect, improve transformation efficiency.When alleviating catalytic cracking unit load, can also satisfy market, and hydrocracking product and catalytic cracking product can both reach the requirement as clean fuel oil to more and more higher diesel and gasoline ratio needs.
Specific embodiments of the present invention comprises the steps:
(1) in atmospheric and vacuum distillation unit, carries out crude distillation, obtain light ends oil, VGO, vacuum residuum;
(2) will deliver to coker or solvent deasphalting unit from the vacuum residuum of step (1), obtain wax tailings and coking gasoline and diesel etc. or deasphalted oil and de-oiled asphalt;
(3) VGO that obtains of wax tailings that will obtain in step (2) or deasphalted oil and step (1) mixes with certain proportion and delivers to middle pressure hydrocracking device (MPHC) and obtain light ends oil and hydrogenation tail oil;
(4) hydrogenation tail oil that step (3) is obtained is delivered to catalytic cracking unit and is carried out lighting with mixing with certain proportion from the part of V GO of step (1).
The blending ratio of the described wax tailings of step (3) or deasphalted oil and VGO according to separately oil property and middle pressure hydrocracking under specified condition to the index request decision of charging, the ratio of mixture of wax tailings or deasphalted oil and VG0 is generally 0.25～1.5, be preferably 0.5～1, the blending ratio of hydrogenation tail oil described in the step (4) and VGO should be according to the index request decision of catalytic cracking to charging, the required index of catalytic cracking charging is: sulphur content is not higher than 0.35%～0.5m%, Conradson carbon residue is less than 5%～10m%, and the Ni+V total content is not higher than 20～40 μ g/g.
The operational condition of the middle pressure hydrocracking device that step (3) is mentioned: pressure is 5-14MPa, 8-12MPa preferably, temperature is 300-500 ℃, preferably 350-425 ℃, volume space velocity and hydrogen dividing potential drop are to select according to the characteristic for the treatment of material and the transformation efficiency and the refining depth of requirement during liquid.Volume space velocity is generally at 0.1-2.0h during liquid
-1, 0.15-1.0h preferably
-1Scope in.Hydrogen to oil volume ratio is 100-3000, is preferably 500-1000.
Said middle pressure hydrocracking device comprises two reactors in the step (3): pretreatment reaction device and hydrocracking reactor.Hydrocracking reactor wherein is a big diameter multi-layer catalyst bed reaction device, can adopt the spider shape eddy flow quench zone and the reallocation system of Mobil patented technology.
Said middle pressure hydrocracking device loads two kinds of catalyzer at least in the step (3), and a kind of is pretreatment catalyst, and a kind of is hydrocracking catalyst.Because the metal content of solvent-deasphalted oils and wax tailings, sulphur nitrogen content and carbon residue are all higher, so pretreatment catalyst must have very strong metal removal activity and well desulfurization, denitrification activity, with the activity of the hydrocracking catalyst that guarantees the back.Hydrocracking catalyst must have good hydrogenation cracking activity and high HVGO transforms and the HDS activity.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, the catalyzer that optionally adds other various auxiliary agents such as P, Si, elements such as F, B for example just belongs to this class catalyzer by KF series pretreatment catalyst and the KC series hydrocracking catalyst that AKZO Nobel company produces.The KF catalyst series is a kind of NiCoMo catalyzer, is by CoMo and NiMo organic assembling, and the KC catalyst series is a kind of CoMo molecular sieve catalyst.
Coker in the step (2) or solvent deasphalting unit adopt the processing condition operation that those skilled in the art of the present technique were familiar with, and coking process can be delayed coking, fluid coking, also can be flexicoking etc.Operational condition is generally: pressure is 1～3 * 10
5Pa, commonly used is 1～2 * 10
5Pa; Temperature is 450～550 ℃, and commonly used is 480～520 ℃.Obtain the gas fraction body recovery system of can degassing in the coking, naphtha fraction and gas oil fraction can go the device of re-refining separately to handle respectively, and wax tailings is to carry out carrying out hydrocracking reaction again after the hydrotreatment with the pretreatment reaction device that certain proportion is mixed into middle pressure hydrocracking with VGO among the present invention.High-sulfur Jiao who produces has two kinds to utilize approach, and a kind of is vaporization, for example passes through industrial chemicals such as half oxidation style hydrogen manufacturing and further synthetic ammonia, acetic acid, alcohol; Another kind is to act as a fuel, and for example makes fuel or make fuel in cement kiln in circular fluid bed.
Solvent deasphalting technology is to utilize solvent to remove undesirable components and objectionable impurities in the residual oil, obtains all lower deasphalted oil of a kind of carbon residue, heavy metal, sulphur and nitrogen content and de-oiled asphalt.Solvent can adopt propane or butane, and concrete processing condition are: extraction tower pressure 2～8MPa, 50～150 ℃ of extracting tower top temperatures, 40～70 ℃ of extraction tower middle part temperature, 30～50 ℃ of extraction tower bottom temps; The deasphalted oil of gained can be used as lube stock, catalytically cracked material, hydrocracking raw material, preferably deasphalted oil is delivered to hydrogenation reaction system among the present invention and is carried out pre-treatment, carries out hydrocracking then.De-oiled asphalt can be produced road bitumen or building asphalt.
In the step (4), the catalytic cracking technology that uses those skilled in the art of the present technique to be familiar with carries out hydrocarbon raw material catalytic cracking.The required index of catalytic cracking unit charging is at present: (1) sulphur content is not higher than 0.35%-0.5m%; (2) Conradson carbon residue is less than 5%-10m%; (3) heavy metal nickel and vanadium total content are not higher than 20-40 μ g/g; (4) the total nitrogen content general requirement is less than 0.35m%, or basic n content is less than 0.15m%.If the index of catalytic cracking unit charging surpasses above-mentioned restriction, the then easy inactivation of catalytic cracking catalyst, and gas, coke yield increase in the product; Productive rate such as gasoline, diesel oil reduces.Therefore can be from the hydrogenation tail oil of step (3) and blending ratio by the charging index decision of catalytic cracking unit from the VGO of step (1).The gas that the generates body recovery system of can degassing, gasoline fraction is preferably all delivered to the oil product jar.Gas oil often is sent to the further hydrotreatment of downstream hydrofining section at least in part, and slurry oil can be used as heavy fuel oil (HFO) or gets back to coker of the present invention or solvent deasphalting unit.The operational condition of catalytic cracking unit is generally: temperature is 450～550 ℃, preferably 480～520 ℃; The agent weight of oil is than 2～30, and preferably 2～20; With 0.1～15 second duration of contact of catalyzer, best 0.5～5 second; Pressure 0.1～0.5MPa.The catalytic cracking catalyst that is adopted can adopt conventional catalytic cracking catalyst, as silica-alumina catalyst, silica-magnesia catalyst, acid-treated carclazyte and X type, Y type, ZSM-5, M type, layer post equimolecular sieve cracking catalyst, preferably molecular sieve cracking catalyst.The reactor of described catalytic cracking unit can be the catalyst cracker of various types, and preferably riser reactor or riser tube add the bed reactor.Technical process is generally: stock oil injects from the riser reactor bottom, contact with high temperature catalyst from the fresh regenerated of revivifier, the oil gas that cracking reaction generates and the catalyst mixture of deposit coke move up along riser reactor, finish the catalytic cracking reaction of whole stock oil.
Compared with prior art, method of the present invention not only makes the charging of present catalytic cracking unit improve greatly, but also stock oil treatment capacity and/or the corresponding device operating severity that reduced have been increased, prolonged the work-ing life of catalytic cracking catalyst, increase the total liquid yield of catalytic cracking, coke and reacted gas productive rate have been reduced, realized the lighting rate of heavy feed stock, and can obtain the quite low light ends oil of sulphur content, meet the requirement of environmental protection, realized the reasonable utilization of petroleum resources petroleum products.
Below in conjunction with drawings and Examples the present invention is described in further details.
Fig. 1 is a kind of simple and easy schematic flow sheet of the present invention.
As shown in Figure 1, feedstock oil 1 enters atmospheric and vacuum distillation unit 2 and distills, obtain decompression residuum 5, VGO4 and other straight-run, decompression residuum 5 enters coking plant or solvent deasphalting unit 6, gets deasphalted oil or wax tailings 7 and Behavior of High-sulfur Petroleum Coke or de-oiled asphalt 8 and coking gasoline and diesel after the reaction, and coking gasoline and diesel dispatches from the factory after further processing, de-oiled asphalt can be used as building asphalt or road asphalt, and Behavior of High-sulfur Petroleum Coke can be used for gas making or as cement kiln or circulating fluidized bed boiler fuel. Wax tailings or deasphalted oil 7 mix with VGO4 with enter hydrocracking preprocessor 10 after hydrogen 9 together mixes and process after, product 11 enters hydrocracking reactor 12, after the reaction, get light naphthar 13, heavy naphtha 14, kerosene 15, diesel oil 16 and hydrogenation tail oil 17, light naphthar 13 can be used as the high-quality industrial chemicals with heavy naphtha 14, kerosene 15 and diesel oil 16 can be used as quality product and go out device, hydrogenation tail oil with mix from 2 VGO3 after enter catalytic cracking unit 18, after the reaction, obtain gas 19, liquefied gas 20, gasoline 21, diesel oil 22 and slurry oil 23, these products all can be used as the low-sulfur quality product and dispatch from the factory.
Process Saudi Arabia's crude oil with processing scheme of the present invention, its oil property sees Table 1.
Table 1 Saudi Arabia oil property
| Density d 4 20，kg/m 3 | 861.5 |
| Viscosity, mm 2/s 50 | 5.58 |
| Carbon residue, % | 1.99 |
| Sulphur, % | 2.61 |
| Nitrogen, % | 0.03 |
| Colloid, % | 8.53 |
| Bituminous matter, % | 0.46 |
| Ni+V，wppm | 42.0 |
The catalyzer of middle pressure hydrocracking process using Akzo Nobel N.V. of present embodiment, pretreatment catalyst is KF-843, hydrocracking catalyst is KC-2600.
The stock oil that middle pressure hydrocracking uses adopts wax tailings and VGO parallel feeding, VGO: CGO=50: 50, and character sees Table 2.
Table 2 middle pressure hydrocracking stock oil main character
| VGO，m％ | 50 |
| Wax tailings, m% | 50 |
| Density, d 4 20(Kg/m 3) | 940 |
| Sulphur content, w% | 2.6 |
| Nitrogen content, wppm | 1800 |
| Ni+V，wppm | 2.1 |
| IBP(℃) | 239 |
| 10％ | 338 |
| 50％ | 422 |
| 90％ | 493 |
| FBP | 559 |
The middle pressure hydrocracking process conditions of present embodiment is:
Hydrogen dividing potential drop: 9.4Mpa volume space velocity: 0.9h
-1Average reaction temperature: 380 ℃ of hydrogen internal circulating load: 850Nm
3/ m
3Hydrogen consumption: 176Nm
3/ m
3
Table 3 middle pressure hydrocracking product distributes
| C 5～82℃ LN | 8.9 |
| 82～166℃HN | 18.8 |
| 166～227 ℃ of kerosene | 17.0 |
| 227～343 ℃ of diesel oil | 28.7 |
| The 343+FCC raw material | 36.7 |
Table 4 middle pressure hydrocracking product property
| Cut | LN | HN | Kerosene | Diesel oil | The FCC raw material |
| Boiling range, ℃ | C5～82 | 82～166 | 166～227 | 227～343 | 343+ |
| Density d 4 20，kg/m 3 | 677.4 | 769.4 | 826.5 | 848.8 | 867.0 |
| S，wppm | ＜100 | ＜100 | ＜100 | ＜100 | ＜200 |
| N，wppm | ＜0.5 | ＜0.5 | ＜2 | ＜5 | ＜10 |
| RON | 78 | 61 | |||
| Smoke point, | 18 | ||||
| The cetane value index | 32 | 51 | |||
| Metal Ni+V, wppm | ＜0.2 |
The mixing oil of the hydrogenation tail oil of 80w%+20%VGO oil enters catalytic cracking unit and carries out lighting, and the operational condition of catalytic cracking unit is:
Temperature: 502 ℃ of pressure: the 0.14MPa agent-oil ratio, (W): 5.5
Finish duration of contact: 1 second
The reaction result of catalytic cracking sees Table 5, and product property sees Table 6.
Table 5 catalytic cracking reaction result
| Dry gas, w% | 2.75 |
| Liquefied gas, w% | 10.15 |
| Gasoline, w% | 46.88 |
| Diesel oil, w% | 30.56 |
| Slurry oil, w% | 4.97 |
| Coke, w% | 4.57 |
| Loss, w% | 0.12 |
Table 6 catalytic cracking product property
| Gasoline | |
| FBP | 204 |
| Density d 4 20，kg/m 3 | 742.8 |
| S，wppm | 20 |
| R+M/2 | 88 |
| Diesel oil | |
| FBP | 338 |
| Density d 4 20，kg/m 3 | 872.9 |
| S，％ | ＜0.03 |
| The cetane value index | 42 |
Process Iranian light crude with processing scheme of the present invention, its character sees Table 7.
The Iranian light crude character of table 7
| Density d 4 20，kg/m 3 | 855.1 |
| Viscosity, mm 2/s 50℃ | 4.90 |
| Carbon residue, % | 3.27 |
| Sulphur, % | 1.49 |
| Nitrogen, % | 0.12 |
| Colloid, % | 9.13 |
| Bituminous matter, % | 0.55 |
| Ni+V，wppm | 45.0 |
The catalyzer of middle pressure hydrocracking process using Akzo Nobel N.V. of present embodiment, pretreatment catalyst is KF-843, hydrocracking catalyst is KC-2600.The charging of middle pressure hydrocracking is the mixture of VGO and deasphalted oil, VGO: DAO=70: 30, and stock oil character sees Table 11.
Table 8 middle pressure hydrocracking stock oil main character
| VGO，m％ | 70 |
| Deasphalted oil, m% | 30 |
| Density, d 4 20(Kg/m 3) | 920.6 |
| Sulphur content, w% | 1.72 |
| Nitrogen content, wppm | 1300 |
| Ni+V，wppm | 5.8 |
| IBP(℃) | 284 |
| 10％ | 367 |
| 50％ | 458 |
| 90％ | 633 |
| FBP | 734 |
The middle pressure hydrocracking process conditions of present embodiment is:
Hydrogen dividing potential drop: 10.4Mpa volume space velocity: 1.0h
-1Average reaction temperature: 385 ℃
Hydrogen internal circulating load: 970Nm
3/ m
3Hydrogen consumption: 224Nm
3/ m
3
Table 9 middle pressure hydrocracking product distributes
| C 5～82℃LN | 7.2 |
| 82～166℃HN | 17.0 |
| 166～227 ℃ of kerosene | 17.8 |
| 227～343 ℃ of diesel oil | 22.1 |
| The 343+FCC raw material | 47.5 |
Table 10 middle pressure hydrocracking product property
| Cut | LN | HN | Kerosene | Diesel oil | The FCC raw material |
| Boiling range, ℃ | C5～82 | 82～166 | 166～227 | 227～343 | 343+ |
| Density d 4 20，kg/m 3 | 669.0 | 766.9 | 805.8 | 824.1 | 849.3 |
| S，wppm | ＜100 | ＜100 | ＜100 | ＜200 | ＜200 |
| N，wppm | ＜0.5 | ＜0.5 | ＜0.5 | ＜1 | ＜5 |
| RON | 77 | 60 | |||
| Smoke point, mm | 26 | ||||
| The cetane value index | 40 | 58 | |||
| Metal Ni+V, wppm | 0.01 |
The mixing oil of the hydrogenation tail oil of 80w%+20%VGO oil enters catalytic cracking unit and carries out lighting, and the operational condition of catalytic cracking unit is:
Temperature: 500 ℃ of pressure: the 0.24MPa agent-oil ratio, (W): 5.8
Finish duration of contact: 1.5 seconds
The reaction result of catalytic cracking sees Table 11.
Table 11 catalytic cracking reaction result
| Dry gas, w% | 3.13 |
| Liquefied gas, w% | 11.23 |
| Gasoline, w% | 47.58 |
| Diesel oil, w% | 29.13 |
| Slurry oil, w% | 4.23 |
| Coke, w% | 4.52 |
| Loss, w% | 0.18 |
Table 12 catalytic cracking product property
| Gasoline | |
| FBP | 204 |
| Density d 4 20，kg/m 3 | 750.6 |
| S，wppm | 20 |
| R+M/2 | 89 |
| Diesel oil | |
| FBP | 338 |
| Density d 4 20，kg/m 3 | 868.9 |
| S，％ | ＜0.03 |
| The cetane value index | 45 |
Present embodiment crude oil adopts Saudi Arabia's light crude, and its character sees Table 13.
Table 13 Saudi Arabia light crude character
| Density d 4 20，kg/m 3 | 887.8 |
| Viscosity, mm 2/s 50℃ | 4.67 |
| Carbon residue, % | 1.59 |
| Sulphur, % | 2.15 |
| Nitrogen, % | 0.09 |
| Colloid, % | 5.81 |
| Bituminous matter, % | 0.42 |
| Ni+V，wppm | 23.1 |
The catalyzer of middle pressure hydrocracking process using Akzo Nobel N.V. of present embodiment, pretreatment catalyst is KF-843, hydrocracking catalyst is KC-2300.The charging of middle pressure hydrocracking is the mixture of VGO and deasphalted oil, VGO: CGO=60: 40, and stock oil character sees Table 14.
Table 14 middle pressure hydrocracking stock oil main character
| VGO，m％ | 60 |
| Deasphalted oil, m% | 40 |
| Density, d 4 20(Kg/m 3) | 907.0 |
| Sulphur content, w% | 2.25 |
| Nitrogen content, wppm | 800 |
| Ni+V，wppm | 5.15 |
| IBP(℃) | 250 |
| 10％ | 334 |
| 50％ | 412 |
| 90％ | 608 |
| FBP | 698 |
The middle pressure hydrocracking process conditions of present embodiment is:
Hydrogen dividing potential drop: 8.2Mpa volume space velocity: 0.75h
-1The average response temperature: 391 ℃, hydrogen internal circulating load: 1100Nm
3/ m
3Hydrogen consumption: 133Nm
3/ m
3
Table 15 middle pressure hydrocracking product distributes
| C 5～166℃LN | 11.1 |
| 166～227 ℃ of kerosene | 17.8 |
| 227～343 ℃ of diesel oil | 23.0 |
| The 343+FCC raw material | 53.6 |
Table 16 middle pressure hydrocracking product property
| Cut | Petroleum naphtha | Kerosene | Diesel oil | The FCC raw material |
| Boiling range, ℃ | C5～166 | 166～227 | 227～343 | 343+ |
| Density d 4 20，kg/m 3 | 712.5 | 796.5 | 835.6 | 865.2 |
| S，wppm | ＜100 | ＜100 | ＜200 | ＜200 |
| N，wppm | ＜0.5 | ＜0.5 | ＜1 | ＜5 |
| RON | 65 | |||
| Smoke point, | 21 | |||
| The cetane value index | 41 | 57 | ||
| Metal Ni+V, wppm | 0.01 |
The mixing oil of the hydrogenation tail oil of 70w%+10%VGO oil enters catalytic cracking unit and carries out lighting, and the operational condition of catalytic cracking unit is:
Temperature: 505 ℃ of pressure: the 0.15MPa agent-oil ratio, (W): 4.2
Finish duration of contact: 1.5 seconds
The reaction result of catalytic cracking sees Table 17.
Table 17 catalytic cracking reaction result
| Dry gas, w% | 4.35 |
| Liquefied gas, w% | 8.52 |
| Gasoline, w% | 45.09 |
| Diesel oil, w% | 33.11 |
| Slurry oil, w% | 3.1 |
| Coke, w% | 5.47 |
| Loss, w% | 0.36 |
Table 18 catalytic cracking product property
| Gasoline | |
| FBP | 204 |
| Density d 4 20，kg/m 3 | 726.8 |
| S，wppm | 20 |
| R+M/2 | 89 |
| Diesel oil | |
| FBP | 338 |
| Density d 4 20，kg/m 3 | 858.6 |
| S，％ | ＜0.03 |
| The cetane value index | 46 |
From above three embodiment as can be seen, sulphur content reaches 2.61% in the crude oil of processing, and the sulphur content of the benzoline product of producing is very low, as gasoline S＜100wppm, diesel oil S＜0.03%, other index also can reach requirement, can meet needs and more and more stricter environmental requirement that clean fuel oil is produced.
Claims (7)
1. the processing scheme of a sulphur-bearing crude comprises the steps:
(1) in atmospheric and vacuum distillation unit, carries out crude distillation, obtain light ends oil, VGO, vacuum residuum;
(2) will deliver to coker or solvent deasphalting unit from the vacuum residuum of step (1), obtain wax tailings and coking gasoline and diesel or deasphalted oil and de-oiled asphalt;
(3) wax tailings that will obtain in step (2) or deasphalted oil mix with part of V GO that step (1) obtains and deliver to the middle pressure hydrocracking device and obtain light ends oil and hydrogenation tail oil;
(4) hydrogenation tail oil that step (3) is obtained mixes with part of V GO from step (1) and delivers to catalytic cracking unit and carry out lighting;
Wherein the operational condition of the coker in the step (2) is: pressure 1～3 * 10
5Pa; 450～550 ℃ of temperature; The operational condition of the solvent deasphalting unit in the step (2) is: extraction tower pressure 2～8MPa, 50～150 ℃ of extracting tower top temperatures, 40～70 ℃ of extraction tower middle part temperature, 30～50 ℃ of extraction tower bottom temps; The blending ratio of wax tailings described in the step (3) or deasphalted oil and VGO is 0.25～1.5; The operational condition of the middle pressure hydrocracking device described in the step (3): pressure is 5～14MPa, and temperature is 300～500 ℃, and volume space velocity is 0.1～2.0h during liquid
-1, hydrogen to oil volume ratio is 100～3000; The blending ratio of hydrogenation tail oil described in the step (4) and VGO should make mixed oil product meet following index: sulphur content is smaller or equal to 0.5m%, and Conradson carbon residue is less than 10m%, and the Ni+V total content is smaller or equal to 40 μ g/g; The operational condition of said catalytic cracking unit is in the step (4): 450～550 ℃ of temperature; The agent weight of oil is than 2～30; With 0.1～15 second duration of contact of catalyzer; Pressure 0.1～0.5MPa.
2. according to the described processing scheme of claim 1, the blending ratio that it is characterized in that the wax tailings described in the step (3) or deasphalted oil and VGO is 0.5～1.
3. according to the described processing scheme of claim 1, it is characterized in that the operational condition of the middle pressure hydrocracking device mentioned in the step (3): pressure is 8～12MPa, and temperature is 350～425 ℃, and volume space velocity is 0.15～1.0h during liquid
-1, hydrogen to oil volume ratio is 500～1000.
4. according to the described processing scheme of claim 1, it is characterized in that said middle pressure hydrocracking device comprises two reactors in the step (3): pretreatment reaction device and hydrocracking reactor.
5. according to the described processing scheme of claim 1, it is characterized in that said middle pressure hydrocracking device loads two or more catalyzer in the step (3), wherein a kind of is pretreatment catalyst, and a kind of is hydrocracking catalyst.
6. according to the described processing scheme of claim 1, it is characterized in that the operational condition of the coker in the step (2) is: pressure 1～2 * 10
5Pa; 480～520 ℃ of temperature.
7. according to the described processing scheme of claim 1, it is characterized in that the operational condition of said catalytic cracking unit in the step (4) is: 480～520 ℃ of temperature; The agent weight of oil is than 2～20; With 0.5～5 second duration of contact of catalyzer; Pressure 0.1～0.5MPa.
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| CN100366709C (en) * | 2006-04-17 | 2008-02-06 | 中国石油化工集团公司 | Combined process for processing heavy oil |
| US8932457B2 (en) | 2009-10-22 | 2015-01-13 | China Petroleum & Chemical Corporation | Catalytic conversion method for increasing cetane number barrel of diesel |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100400623C (en) * | 2006-08-01 | 2008-07-09 | 华南理工大学 | Centrifugal molecular distillating process of producing biological diesel for automobile |
| CN101921611B (en) | 2009-06-12 | 2013-07-31 | 中国石油天然气股份有限公司 | Catalytic cracking method and system for reducing sulphur content of petrol |
| CN102337152A (en) * | 2010-07-22 | 2012-02-01 | 中国石油化工股份有限公司 | Processing method of sulfur-containing crude oil |
| CN102660330B (en) * | 2012-04-19 | 2013-07-31 | 陕西延长石油（集团）有限责任公司 | Method for co-producing various chemical products by taking coal, petroleum, natural gas and salt as raw materials |
-
2000
- 2000-10-26 CN CNB001231553A patent/CN1160441C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100366709C (en) * | 2006-04-17 | 2008-02-06 | 中国石油化工集团公司 | Combined process for processing heavy oil |
| US8932457B2 (en) | 2009-10-22 | 2015-01-13 | China Petroleum & Chemical Corporation | Catalytic conversion method for increasing cetane number barrel of diesel |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1351131A (en) | 2002-05-29 |
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