CN103540357A - Heavy oil treatment process - Google Patents
Heavy oil treatment process Download PDFInfo
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- CN103540357A CN103540357A CN201210244803.2A CN201210244803A CN103540357A CN 103540357 A CN103540357 A CN 103540357A CN 201210244803 A CN201210244803 A CN 201210244803A CN 103540357 A CN103540357 A CN 103540357A
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Abstract
The invention discloses a heavy oil treatment method which overcomes the defects of resource wasting and high energy consumption in the prior art. One part of heavy oil enters a first vacuum tower after being heated by a first heating furnace and is subjected to reduced pressure distillation, the distillate oil of less than 350 DEG C in the first vacuum tower enters a refining device, the wax oil in the first vacuum tower enters a wax oil treatment device, the heavy wax oil in the first vacuum tower enters a residual oil hydrotreating device, the residual oil in the first vacuum tower enters a delayed coking device, the other part of the heavy oil enters a second vacuum tower after being heated by a second heating furnace and is subjected to reduced pressure distillation, the distillate oil of less than 350 DEG C in the second vacuum tower enters a refining device, the wax oil in the second vacuum tower enters a wax oil treatment device, and the residual oil in the second vacuum tower enters a residual oil hydrotreating device.
Description
Technical field
The present invention relates to hydrocarbon ils manufacture field, particularly a kind of heavy oil treatment process.
Background technology
Along with the develop rapidly of national economy, the demand of oils is increased fast, and crude oil becomes gradually heavy, becomes bad, yield of light oil reduces gradually, and this just forces refining of petroleum industry to utilize heavy oil to produce lightweight oil.Residual oil processing is the key that improves crude oil yield of light oil, is also a kind of embodiment of oil Refining Technologies level.In residual oil complete processing, having hydrogenation and de-charcoal two schemes, is that de-charcoal technology or its object of hydrogen addition technology are all the hydrocarbon ratios in change residual oil, makes hydrocarbon reconfiguring, the lower residual oil of hydrogen richness is processed into the light-end products that hydrogen richness is higher, meets the needs of national economy.
Residual hydrocracking (RHT) is the method upgrading residual oil that utilizes hydrogenation, comprise the techniques such as fixed bed hydrogenation, boiling bed hydrogenation, floating bed hydrogenation, relatively more conventional is fixed bed hydrogenation at present, as Vacuum Residue Desulfurization (VRDS), atmospheric resid desulphurization (ARDS), hydrodemetallation (HDM) (HDM) etc.Fixed bed hydrogenation is that hydrogenation catalyst is seated in reactor, after hydrogen mixes with residual oil, under 300～450 ℃ of high temperature, 4.0～20.0MPa condition of high voltage, the form with trickle flows through beds, carry out hydrogenation reaction simultaneously, remove metal and carbon residue in residual oil, improved the hydrogen richness in hydrocarbon, made residual oil obtain upgrading.
Residual hydrogenation technology comprises vacuum residuum desulfurization (VRDS) [< < refining of petroleum and chemical industry > > 1998 (6), P17～21; < < petrochemical equipment technology > > 1995 (1), P10～12] and atmospheric resid desulphurization (ARDS) [< < oil refining design > > 1994 (2) P31～34].VRDS adopts multi-stage fixed-bed residuum hydrodesulfurization technology, under higher hydrogen partial pressure, operation removes metal and impurity, hydrogen dividing potential drop is at least 15.0MPa, processing sulphur and the higher raw material of metal content, advantage is that demetalization and sweetening power are stronger, apply more extensive, but VRDS technology is to take vacuum residuum as raw material, at present in order to improve wax oil yield, adopt deep drawing technology, make in subtracting slag amount worse and worse, to VRDS, bring the many difficulties such as charging and demetalization, solution is to divide 515～565 ℃ of wax oils of part of having extracted to mix with vacuum residuum underpressure distillation at present, composition mixture is as VRDS raw material, to reduce the viscosity that enters residual hydrocracking device raw material, though this scheme can meet the requirement of residual hydrogenation equipment to charging, but but cause larger energy wastage.
ARDS adopts fixed bed residuum hydrodesulfurization technology, and feature is that demetalization and desulfurization are carried out respectively on two kinds of catalyzer, is that with the difference of VRDS stock oil is long residuum, and boiling point is greater than 350 ℃.Adopt this technical process, the quality of residual hydrogenation raw material can meet charging requirement.But, owing to containing the diesel oil of 3% left and right in long residuum and can be used as in a large number catalytic cracking or the wax oil of hydroeracking unit raw material, adopt long residuum directly as residual oil, to add and process hydrogen production device raw material, not only reduced catalytic cracking or hydroeracking unit raw material sources, also cause the waste of diesel oil and wax oil resource, also cause residual hydrogenation equipment scale large, process cost is high.
Generally, petrochemical enterprise configures the delayed coking unit of fairly large heavy-oil hydrogenation treatment unit and small-scale or the whole economic efficiency that other heavy oil conversion devices improve enterprise and the trend that adapts to crude oil kind heaviness.
For better utilised resource, general petrochemical enterprise reconfiguration latency coker, the vacuum residuum that Disposal quality is poor, for improving whole economic efficiency, the general decompression deep drawing scheme that adopts, the yield of raising decompressed wax oil as much as possible, conventionally vacuum residuum cut point temperature is brought up to and is equal to, or greater than 565 ℃, using a vacuum residuum part as delayed coking unit charging, another part is as the raw material of residual hydrocracking device, but in being greater than the vacuum residue fraction of 565 ℃, metal content no matter, carbon residue content, or viscosity is all higher, be difficult to the raw material as residual hydrocracking device, and the decompression wax slop of 515～565 ℃ of cuts that the division that prior art solves this contradiction has been extracted for decompression is blended in vacuum residuum again, to reduce the viscosity that enters residual hydrocracking device raw material, though this scheme can meet the requirement of residual hydrogenation equipment to charging, but but cause larger energy wastage.
De-charcoal technology comprises the techniques such as FCC, delayed coking, solvent deasphalting, utilization removes the charcoal in residual oil by the mode of the higher macromole condensation coking of carbon content in residual oil, remove the impurity such as metal in residual oil, sulfide simultaneously, improve the content of hydrogen in fuel and produce high-quality oil fuel, the advantage of de-charcoal technology is that investment and process cost are low, and shortcoming is that a part of residual oil has been changed into inferior coke.
Fluid catalytic cracking FCC technique, to belong to de-charcoal technique, at riser reactor Raw oil with catalyzer at 0.1～0.3MPa, under 450～530 ℃ of conditions, contact, through cracking, generate gas, gasoline, diesel oil, mink cell focus and coke, the raw material of FCC be take decompressed wax oil conventionally as main.
All these secondary processing technology all, on normal pressure or underpressure distillation basis, go out gasoline, diesel oil by crude separation, normal slag, decompressed wax oil and vacuum residuum, and usually said heavy oil, except heavy crude, refers generally to long residuum or vacuum residuum.The common cut of long residuum is 360 ℃ of >, the general raw material as underpressure distillation, catalytic cracking or long residuum hydrotreater, the common cut of decompressed wax oil is 360～565 ℃, generally make catalytic cracking or hydroeracking unit raw material, the common cut of vacuum residuum is 565 ℃ of >, generally does the charging of residual hydrogenation equipment, delayed coking unit or solvent deasphalting unit.
Summary of the invention
The present invention has proposed a kind of combination heavy oil treatment processes in order to overcome the waste resource of VRDS in prior art, ARDS existence and the defect of the energy, can solve the raw materials quality problem of residual hydrocracking device, can make full use of again decompressed wax oil and recovery part diesel oil, reduce the energy expenditure of enterprise.
A kind of heavy oil treatment processes, it is characterized in that: a part of heavy oil enters the first vacuum distillation tower through the first process furnace heating and carries out underpressure distillation, the first 350 ℃ of vacuum distillation tower < distillate enters refining plant, the first vacuum distillation tower wax oil enters wax oil treatment unit, the first vacuum distillation tower wax slop enters residual hydrocracking device, the first vacuum distillation tower residual oil enters delayed coking unit, another part heavy oil enters the second vacuum distillation tower through the second process furnace heating and distills, the second 350 ℃ of vacuum distillation tower < distillate enters refining plant, the second vacuum distillation tower wax oil enters wax oil treatment unit, the second vacuum distillation tower residual oil enters residual hydrocracking device.
Described wax oil treatment unit is catalytic cracking or hydroeracking unit.
Described refining plant is at least in hydro-refining unit, acid-alkali refining device, Clay Refining Unit a kind of.
Described heavy oil is at least the extraction oil of long residuum, heavy crude, deasphalted oil, thermally splitting heavy oil, lube oil finishing, the tar of the turning oil of catalytic cracking and clarified oil, cracking of ethylene, sump oil, coal tar, shale oil, oil-sand heavy oil, rock asphalt a kind of.
Described vacuum distillation tower service temperature is 80～440 ℃, and preferably 80～440 ℃, flash zone pressure is that 10～300mmHg is exhausted, and preferably 15～30mmHg is exhausted.
Described catalytic cracking unit operational condition is: riser reactor temperature is 450～580 ℃, pressure is 0.03～0.30MPa, the weight ratio of water vapor and stock oil is 0.01～1.00, be preferably 0.05～0.10, the weight ratio of catalyzer and stock oil is 2～20, be preferably 6～15, the reaction times is 0.1～2s, is preferably 0.5～1.5s.
Described hydroeracking unit operational condition is: reactor gauge pressure pressure is 70～21000kPa, 150～500 ℃ of temperature, hydrogen-oil ratio 100～3000, air speed 0.1～500.0hr-1.
Described residual hydrocracking device operational condition is: reactor gauge pressure pressure 10～20MPa, 340～450 ℃ of temperature, hydrogen-oil ratio 100～3000, air speed 0.1～5.0hr-1.
Described delayed coker operation condition is: the gauge pressure of coking tower tower top is 0.103～1.0Mpa, preferred 0.103～0.25Mpa, and filling the burnt time is 3～48hr, preferably 6～20hr.
Compared with prior art, a kind of heavy oil treatment processes of the present invention, has:
1) flexible operation, can be according to the needs of each Downstream processing device to raw material, the flow process of modulation fractionation;
2) can increase the diesel yield of 2～5 % by weight, in crude oil gross weight;
3) improve decompressed wax oil yield 1～6%, in crude oil gross weight;
4) improve the quality of residual hydrogenation equipment raw material, can extend its operational cycle;
5) reduce oil fuel consumption, reduce energy expenditure.
Accompanying drawing explanation:
Fig. 1 is a kind of heavy oil treatment processes schematic flow sheet of the present invention.
Wherein:
1. heavy oil, 2. process furnace, 3. vacuum distillation tower 4 chargings, 4. vacuum distillation tower, 5. vacuum distillation tower 4 top oil gas, 6. process furnace 2 chargings, 7. 350 ℃ of distillates of vacuum distillation tower 4 <, 8. wax slop, 9. vacuum distillation tower 4 residual oil, 10. process furnace 22 chargings, 11 vacuum distillation towers, 12. vacuum distillation tower 11 chargings, 13 vacuum distillation tower 4 wax oils, 14. 350 ℃ of < distillates, 350 ℃ of distillate treatment unit of 15. vacuum distillation tower 11 <, 16. vacuum distillation tower 11 wax oils, 17. wax oil treatment unit, 18. vacuum distillation tower 11 residual oil, 19. delayed coking units, 20. mixed residue oils, 21, residual hydrocracking device, 22. process furnace.
Embodiment
As shown in Figure 1, a kind of heavy oil treatment processes, 25 % by weight heavy oil 1 enter vacuum distillation tower 4 through process furnace 2 heating, in heavy oil 1 gross weight, 350 ℃ of distillates 7 of vacuum distillation tower 4 < enter refining plant 15, vacuum distillation tower 4 wax oils 13 enter wax oil treatment unit 17, vacuum distillation tower 4 wax slops 8 enter residual hydrocracking device 21, vacuum distillation tower 4 residual oil 9 enter delayed coking unit 19, 75 % by weight heavy oil 1 enter vacuum distillation tower 11 as process furnace 22 chargings 10 through process furnace 22 heating and distill, in heavy oil 1 gross weight, 350 ℃ of distillates 14 of vacuum distillation tower 11 < enter refining plant 15, vacuum distillation tower 11 wax oils 16 enter wax oil treatment unit 17, vacuum distillation tower 11 residual oil 17 enter residual hydrocracking device 21.
A kind of heavy oil treatment processes, it is characterized in that: 25 % by weight heavy oil enter the first vacuum distillation tower through the first process furnace heating, in heavy oil 1 gross weight, the first 350 ℃ of vacuum distillation tower < distillate enters refining plant, the first vacuum distillation tower wax oil enters wax oil treatment unit, the first vacuum distillation tower wax slop enters residual hydrocracking device, the first vacuum distillation tower residual oil enters delayed coking unit, 75 % by weight heavy oil enter the second vacuum distillation tower through the second process furnace heating and distill, in heavy oil 1 gross weight, the second 350 ℃ of vacuum distillation tower < distillate enters refining plant, the second vacuum distillation tower wax oil enters wax oil treatment unit, the second vacuum distillation tower residual oil enters residual hydrocracking device.
Claims (12)
1. a heavy oil treatment processes, it is characterized in that: part heavy oil enters the first vacuum distillation tower through the first process furnace heating and carries out underpressure distillation, the first 350 ℃ of vacuum distillation tower < distillate enters refining plant, the first vacuum distillation tower wax oil enters wax oil treatment unit, the first vacuum distillation tower wax slop enters residual hydrocracking device, the first vacuum distillation tower residual oil enters delayed coking unit, another part heavy oil enters the second vacuum distillation tower through the second process furnace heating and carries out underpressure distillation, the second 350 ℃ of vacuum distillation tower < distillate enters refining plant, the second vacuum distillation tower wax oil enters wax oil treatment unit, the second vacuum distillation tower residual oil enters residual hydrocracking device.
2. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described wax oil treatment unit is catalytic cracking or hydroeracking unit.
3. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described refining plant is at least in hydro-refining unit, acid-alkali refining device, Clay Refining Unit a kind of.
4. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described heavy oil is at least the extraction oil of long residuum, heavy crude, deasphalted oil, thermally splitting heavy oil, lube oil finishing, the tar of the turning oil of catalytic cracking and clarified oil, cracking of ethylene, sump oil, coal tar, shale oil, oil-sand heavy oil, rock asphalt a kind of.
5. according to a kind of heavy oil treatment process claimed in claim 1, it is characterized in that: described vacuum distillation tower service temperature is 80～440 ℃, flash zone pressure is that 10～300mmHg is exhausted.
6. according to a kind of heavy oil treatment process claimed in claim 1, it is characterized in that: described vacuum distillation tower service temperature is 80～440 ℃, flash zone pressure is that 15～30mmHg is exhausted.
7. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described catalytic cracking unit operational condition is: riser reactor temperature is 450～580 ℃, pressure is 0.03～0.30MPa, the weight ratio of water vapor and stock oil is 0.01～1.00, the weight ratio of catalyzer and stock oil is 2～20, and the reaction times is 0.1～2s.
8. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described hydroeracking unit operational condition is: reactor gauge pressure pressure is 70～21000kPa 150～500 ℃ of temperature, hydrogen-oil ratio 100～3000, air speed 0.1～500.0hr
-1.
9. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described residual hydrocracking device operational condition is: reactor gauge pressure pressure 10～20MPa, 340～450 ℃ of temperature, hydrogen-oil ratio 100～3000, air speed 0.1～5.0hr
-1.
10. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described delayed coker operation condition is: the gauge pressure of coking tower tower top is 0.103～1.0Mpa, filling the burnt time is 3～48hr.
11. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described delayed coker operation condition is: the gauge pressure of coking tower tower top is 0.103～0.25Mpa, and filling the burnt time is 6～20hr.
12. according to a kind of heavy oil treatment processes claimed in claim 1, it is characterized in that: described delayed coker operation condition is: the gauge pressure of coking tower tower top is 0.103～0.25Mpa, fills the burnt time to be～20hr.
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