CN101338220B - A kind of hydrogenation method for hydrocarbon oils - Google Patents
A kind of hydrogenation method for hydrocarbon oils Download PDFInfo
- Publication number
- CN101338220B CN101338220B CN200810140991.8A CN200810140991A CN101338220B CN 101338220 B CN101338220 B CN 101338220B CN 200810140991 A CN200810140991 A CN 200810140991A CN 101338220 B CN101338220 B CN 101338220B
- Authority
- CN
- China
- Prior art keywords
- reactor
- hydrogen
- hydrocarbon oils
- oil
- hydrogenation method
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of hydrogenation method for hydrocarbon oils, the method eliminates recycle hydrogen and circulating hydrogen compressor, hydrogen is mixed to form mixes logistics with fresh feed oil and part recycle oil in the presence of solvent or diluent, mixture stream enters reactor and contacts with catalyst, another part or all recycle oil mix with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
Description
Technical field
The present invention relates to hydrocarbon oil hydrogenation technology, particularly to liquid-solid two-phase hydrocarbon oil hydrogenation technology.
Background technology
In hydrocarbon ils process technology, hydrogen addition technology is to improve one of conventional technology of hydrocarbon ils quality, along with global crude oil market supply tends to the crude oil of higher sulfur content, refinery need to process the hydrocarbon ils inferior that sulfur-bearing is higher, sulfur, nitrogen, oxygen and metal impurities are removed in refining process, its quality is changed, so that various product meets code requirement by changing the molecular structure of hydrocarbon ils.Hydrocarbon oil hydrogenation process actually participates in the hydrogen hydrogen only for chemical hydrogen consumption of reaction, and tradition trickle bed reactor hydrogen addition technology, need excessive hydrogen to exist so that the volume ratio of reactor is relatively big, and maintains the exess of H2 gas to need to use circulating hydrogen compressor.
In traditional hydrogenation technique, hydrogen needs to be delivered to liquid phase from gas phase, and then co-absorbed is on the surface of catalyst, reacts under the effect of catalyst active center.Owing to hydrogenation reaction is a strong exothermal reaction, in order to maintain reaction temperature, substantial amounts of hydrogen and raw oil is utilized to take away, by beds, the heat that reaction produces, and the hydrogen being actually needed in hydrogenation process (chemical hydrogen consumption) is fewer, do not participate in the hydrogen of reaction, be recycled to hydrogenation reactor and continue to participate in reaction；Tradition hydrocarbon ils hydrogen addition technology uses another main cause of excessive hydrogen to be the hydrogen dividing potential drop maintaining hydrocarbon oil hydrogenation reaction, and the hydrogen dividing potential drop remaining higher is thermodynamically conducive to hydrofinishing and hydrocracking reaction, and suppression generates the condensation reaction of coke.
Do not participate in the hydrogen of reaction by separator and liquid phase separation and after removing impurity, by circulating hydrogen compressor, its pressure is increased to react required pressure and delivers to reactor and continue to participate in hydrogenation reaction.The hydrogen being not engaged in hydrogenation reaction is improved pressure by the effect of circulating hydrogen compressor exactly makes it recycle, and therefore circulating hydrogen compressor becomes requisite equipment in existing hydrogen addition technology, is called in the industry the heart of hydrogenation plant.
Being gas, liquid, solid three-phase in traditional fixed bed hydrogenation reactor and deposit, gas phase is the steam of hydrogen and hydrocarbon raw material, and liquid phase is unboiled hydrocarbon raw material, and solid phase is catalyst.Gas-liquid two-phase is that the form with drip is by beds, the most also referred to as trickle bed reactor.
In trickle bed reactor, in order to strengthen mass transfer dynamics, hydrogen is generally 50～2000: 1 with the volume ratio of raw oil, therefore hydrogenation reactor design is bigger, and the raw oil of reality participation reaction is relevant with liquid hourly space velocity (LHSV), air speed reflects the disposal ability of device, and industrial hope uses bigger air speed operation, but air speed is restricted by response speed.Air speed according to catalyst activity, feedstock property, reaction depth unusual 0.5～10h-1Between fluctuate.The unifining process of commercial Application reduces air speed under the conditions of certain reaction temperature and can improve alkene saturation factor, hydrodesulfurization rate and hydrodenitrogeneration rate at present.Under hydrocracking condition, improve air speed little on total conversion ratio impact, but the light constituent content in product declines more.
The purpose using the exess of H2 gas is to strengthen mass transfer and take away the amount of heat produced because of hydrogenation reaction, circulating hydrogen compressor is as the heart of hydrogenation process, investment and operating cost are the highest, in order to cancel circulating hydrogen compressor, people start consideration and utilize hydrogen supply agent to provide hydrogen source for hydrocarbon oil hydrogenation process, USP4698147 i.e. discloses and utilizes hydrogen supply agent to reduce the time of staying, and after reaction, hydrogen supply agent utilizes hydrogen to regenerate, and regeneration Posterior circle uses.In order to strengthen cracking reaction, USP4857168 discloses and utilizes hydrogen supply agent and hydrogen to provide the hydrocracking heavy oil method of hydrogen source for heavy-oil hydrogenation, and hydrogen supply agent acts primarily as the effect that suppression generates the condensation reaction of coke.
Above-mentioned improvement need nonetheless remain for recycle hydrogen and circulating hydrogen compressor, US6428686 proposes a kind of two-phase hydrogenation method, hydrogen is dissolved in raw oil before reactor, eliminate recycle hydrogen and circulating hydrogen compressor, reduce investment and the operating cost of hydrogenation plant, this technology uses the liquid phase circulation of product, improve the meltage of hydrogen, to meet in hydrogenation process the requirement to hydrogen, and take reaction heat out of, this technology be recycle oil is mixed with raw oil and hydrogen after enter hydrogenation reactor, its shortcoming is the response speed that the existence of substantial amounts of recycle oil can affect fresh feed and hydrogen, because fresh feed reacts fiercer with hydrogen when starting and contacting with catalyst, the existence of recycle oil inhibits the touch opportunity of fresh feed oil and hydrogen and catalyst, reduce fresh feed oil and the mass transfer of hydrogen and response speed.
Summary of the invention
The present invention proposes a kind of hydrogenation method for hydrocarbon oils, eliminates recycle hydrogen and circulating hydrogen compressor, strengthens the touch opportunity of fresh feed oil and hydrogen and catalyst, improves mass transfer and response speed, reduce reactor volume.
One hydrogenation method for hydrocarbon oils of the present invention is: hydrogen is mixed to form mixes logistics with fresh feed oil and part recycle oil in the presence of solvent or diluent, mixture stream enters reactor and contacts with catalyst, another part or all recycle oil mix with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
Described mixing logistics enters reactor from reactor head, and reaction effluent flows out from reactor bottom and carries out gas-liquid separation.
Described mixing logistics enters reactor from reactor bottom, and reaction effluent flows out from reactor head and carries out gas-liquid separation.
Described another part or all recycle oil mix with hydrogen in the presence of solvent or diluent.
Described mixture flow separation go out gas laggard enter reactor.
Described mixing logistics mixes in blender, enters reactor after gas is isolated at blender top.
Described a kind of hydrogenation method for hydrocarbon oils, is further characterized in that: entering the mixing logistics of reactor after gas is isolated at blender top, liquid contacts with catalyst, and gas is got rid of from reactor head.
Described a kind of hydrogenation method for hydrocarbon oils, it is characterized in that: after gas is isolated at blender top, enter the mixing logistics of reactor, liquid and catalyst haptoreaction, gas is got rid of from reactor head, after another part or all recycle oil mix eliminating gas with hydrogen, a road or branch enter reactor between reactor catalyst bed.
Described a kind of hydrogenation method for hydrocarbon oils, is further characterized in that: hydrogen is mixed to form mixes logistics with fresh feed oil and part recycle oil.
The present invention proposes another kind of hydrogenation method for hydrocarbon oils, it is characterized in that: fresh feed oil is mixed to form with hydrogen in the presence of solvent or diluent after mixing with part recycle oil again and mixes logistics, mixture stream enters reactor and contacts with catalyst, another part or all recycle oil mix with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: mixing logistics enters reactor from reactor head, and reaction effluent flows out from reactor bottom and carries out gas-liquid separation.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: mixing logistics enters reactor from reactor bottom, and reaction effluent flows out from reactor head and carries out gas-liquid separation.
Described another part or all recycle oil mix with hydrogen in the presence of solvent or diluent.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: mixture flow separation go out gas laggard enter reactor.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: mixing logistics mixes in blender, enters reactor after gas is isolated at blender top.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: enter the mixing logistics of reactor, liquid and catalyst haptoreaction after gas is isolated at blender top, and gas is got rid of from reactor head.
Described a kind of hydrogenation method for hydrocarbon oils, it is characterized in that: after gas is isolated at blender top, enter the mixing logistics of reactor, liquid and catalyst haptoreaction, gas is got rid of from reactor head, after another part or all recycle oil mix eliminating gas with hydrogen, a road or branch enter reactor between reactor catalyst bed.
Described another kind of hydrogenation method for hydrocarbon oils, is further characterized in that: hydrogen is mixed to form mixes logistics with fresh feed oil and recycle oil.
In hydrogenation reactor of the present invention, catalyst at least divides two sections of bed fillings, form at least two-stage catalytic agent bed, it is mixed into second segment beds from the recycle oil of first paragraph beds effluent out Yu introducing, contact with catalyst and proceed reaction, the 3rd section of beds is entered with the recycle oil of introducing after second segment beds effluent out mixes, the rest may be inferred, and reaction effluent is drawn from reactor bottom.
Solvent of the present invention or diluent are at least one in the hydrocarbon ils after heavy naphtha, Petroleum, lighter hydrocarbons, light distillate, diesel oil, VGO and hydrogenation.
A kind of hydrogenation method for hydrocarbon oils of the present invention and the distillate that fresh feed oil is hydrocarbon ils or hydrocarbon ils of another kind of hydrogenation method for hydrocarbon oils, such as petroleum distillate, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
The present invention provides another kind of hydrogenation method for hydrocarbon oils, fresh feed oil, it is mixed to form with hydrogen after part recycle oil and solvent or diluent mixing and mixes logistics, mixture stream enters reactor and contacts with catalyst, another part or all recycle oil mix with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
The present invention proposes another kind of hydrogenation method for hydrocarbon oils, it is characterized in that: fresh feed oil is mixed to form with part recycle oil and hydrogen after mixing with solvent or diluent again and mixes logistics, mixture stream enters reactor and contacts with catalyst, another part or all recycle oil mix with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
A kind of hydrogenation method for hydrocarbon oils of the present invention and another kind of hydrogenation method for hydrocarbon oils, at least remove a kind of pollutant in its sulfur, nitrogen, oxygen, metal impurities, and saturated aromatic hydrocarbons, change the molecular structure of hydrocarbon ils.
One hydrogenation method for hydrocarbon oils of the present invention and another kind of hydrogenation method for hydrocarbon oils eliminate recycle hydrogen and circulating hydrogen compressor, hydrocarbon ils, solvent or diluent is utilized to be dissolved in wherein by hydrogen, hydrogen source is provided for hydrocarbon oil hydrogenation, wherein solvent or diluent are more than hydrocarbon ils to the solvability of hydrogen, the addition of solvent or diluent is adjusted according to the amount of hydrogen, i.e. chemical hydrogen consumption needed for hydrocarbon oil hydrogenation process reaction.
One hydrogenation method for hydrocarbon oils of the present invention and another kind of hydrogenation method for hydrocarbon oils: the mixing ratio utilizing recycle oil and fresh feed oily controls mixture stream and enters the temperature of reactor, utilizes the circulation fuel-flow control temperature of reactor entered between beds.
One maximum problem of hydrogenation process is beds coking, coking can be occurred under reaction condition to react, without enough hydrogen, cracking reaction can cause coke to be formed, and is deposited on catalyst surface, due to the fact that employing recycle oil circulation, recycle oil makes much aromatic hydrocarbons obtain saturated through hydrogenation, there is the function of hydrogen supply, coke can be suppressed to be formed, extend the life-span of catalyst.
One hydrogenation method for hydrocarbon oils of the present invention and another kind of hydrogenation method for hydrocarbon oils can be used for straight-run, FCC recycle oil, coker gas oil CGO, or its mixing kerosene and diesel oil hydrogenation process, can be additionally used in FCC feedstock pretreatment, transform for new device and mild hydrocracking, for producing ULSD, for pretreatment or the post processing of product of raw material.
Hydrogenation method for hydrocarbon oils of the present invention has the advantage that
1) catalyst amount is few；
2) hydrogen loss is less；
3) relatively low operating cost；
4) liquid yield is higher；
5) bigger operating flexibility；
6) the sulfur nitrogen content of product is the lowest；
7) relatively low investment；
8) reactor volume is reduced；
9) for producing ultra-low-sulphur diesel, improvement expenses is the lowest.
Compared with the prior art of trickle bed hydrogenation reactor, the present invention: can desulfurization 90%～98%, and hydrogen consumption be only the 70%～90% of trickle bed hydrogenation reactor, the total consumption of catalyst is only 15%～30%.
Accompanying drawing explanation
Fig. 1 is hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 2 is another kind hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 3 is the third hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 4 is the 4th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 5 is the 5th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 6 is the 6th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 7 is the 7th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 8 is the 8th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Fig. 9 is the 9th kind of hydrocarbon oil hydrogenation process chart of the present invention.
Figure 10 is the tenth kind of hydrocarbon oil hydrogenation process chart of the present invention.
Figure 11 is the 11st kind of hydrocarbon oil hydrogenation process chart of the present invention.
Figure 12 is diesel oil hydrogenation process chart of the present invention.
In figure: 1-fresh feed oil, 2-hydrogen, 3-the first blender, 4-knockout drum, 5-reactor, 6-the second blender, 7-reactor feed, 8-the first separator, 9-the second separator, 11-the first separator exhaust, 13-solvent or diluent, 14-knockout drum waste gas, 15-molten hydrogen recycle oil, 16-the first separator separation product, 17-recycle oil, 20-the second blender waste gas.
Detailed description of the invention
As it is shown in figure 1, reactor shown in figure is four sections of beds.nullFresh feed oil 1 mixes in the first blender 3 with hydrogen 2 and part recycle oil in the presence of solvent or diluent 13，Mixture stream enters knockout drum 4，Reactor feed 7 is become after isolating knockout drum waste gas 14，Reactor feed 7 enters reactor first paragraph beds and catalyst haptoreaction from reactor 5 top，Another part or all recycle oil are mixed into molten hydrogen recycle oil 15 in the second blender 6 with hydrogen 2，Molten hydrogen recycle oil 15 is respectively from the first paragraph of reactor 5 and second segment beds、Reactor 5 is entered between second segment and the 3rd section of beds and the 3rd section and the 4th section of beds，Bottom reactor 5, reaction effluent out enters the first separator 8 and separates，Isolate the first separator exhaust 11，Bottom the first separator 8, separation product out is divided into two parts，A part is as the first separator separation product 16，Another part is as recycle oil 17，First separator separation product 16 enters back into the second separator 9 and separates，From the logistics out of the second separator 9 top as solvent or diluent 13，Bottom the second separator 9, separation product out goes out device as product.17 times the first blenders 3 of a part of recycle oil, another part or all recycle oil 17 enter the second blender 6 and are mixed into molten hydrogen recycle oil 15 with hydrogen 2.
Fig. 2, it is with the difference of Fig. 1: reactor feed 7 enters reactor 5 bottom reactor 5, and the reaction effluent of reactor 5 out enters the first separator 8 from the top of reactor 5.
Fig. 3, it is with the difference of Fig. 1: from the second separator 9 top, logistics out is divided into two bursts of recyclings as solvent or diluent 13, and one enters the first blender 3, and another stock enters the second blender 6.
Fig. 4, it is with the difference of Fig. 3: reactor feed 7 enters reactor 5 bottom reactor 5, and the reaction effluent of reactor 5 out enters the first separator 8 from the top of reactor 5.
Fig. 5, it is with the difference of Fig. 3: the mixing logistics mixed in the first blender 3 becomes reactor feed 7 after discharging the first blender waste gas 12 from the first blender 3, and reactor feed 7 enters reactor 5 from reactor 5 top.
Fig. 6, it is with the difference of Fig. 5: reactor feed 7 enters reactor 5 bottom reactor 5, and the reaction effluent of reactor 5 out enters the first separator 8 from the top of reactor 5.
Fig. 7, it is with the difference of Fig. 5: reactor feed 7 enters reactor 5 from reactor 5 top, and reactor exhaust 4 is discharged at reactor 5 top, and bottom reactor 5, reaction effluent out enters the first separator 8 and separates.
Fig. 8, it is with the difference of Fig. 7: reactor feed 7 enters reactor 5 bottom reactor 5, enters the first separator 8 from reactor 5 top reaction effluent out and separates.
Fig. 9, it is with the difference of Fig. 3: the mixing logistics mixed in the first blender 3 becomes reactor feed 7 after discharging the first blender waste gas 12 from the first blender 3, reactor feed 7 enters reactor 5 from reactor 5 top, reactor exhaust 4 is discharged at reactor 5 top, bottom reactor 5, reaction effluent out enters the first separator 8 and separates, bottom the first separator 8, separation product out is divided into two parts, a part is as the first separator separation product 16, another part is as recycle oil 17, first separator separation product 16 enters back into the second separator 9 and separates, from the second separator 9 top, logistics out is divided into two bursts of recyclings as solvent or diluent 13, bottom the second separator 9, separation product out goes out device as product.17 times the first blenders 3 of a part of recycle oil, another part or all recycle oil 17 enter the second blender 6 and hydrogen 2 and another strand of solvent or diluent 13 mixes in 6, become molten hydrogen recycle oil 15 after getting rid of the second blender waste gas 20.
Figure 10, it is with the difference of Fig. 9: reactor feed 7 enters reactor 5 bottom reactor 5, enters the first separator 8 from reactor 5 top reaction effluent out and separates.
Figure 11, it is with the difference of Fig. 1: fresh feed oil 1 is mixed to form with hydrogen 2 in the presence of solvent or diluent 13 after mixing with part recycle oil 17 again and mixes logistics.
Figure 12, as shown in figure 12, reactor shown in Figure 12 is four sections of beds.nullFresh feed oil 1 mixes in the first blender 3 with hydrogen 2 and part recycle oil，Mixture stream enters knockout drum 4，Reactor feed 7 is become after isolating knockout drum waste gas 14，Reactor 5 and catalyst haptoreaction is entered from reactor 5 top，Another part or all recycle oil mix with hydrogen 2，Molten hydrogen recycle oil 15 is respectively from the first paragraph of reactor 5 and second segment beds、Reactor 5 is entered between second segment and the 3rd section of beds and the 3rd section and the 4th section of beds，Bottom reactor 5, reaction effluent out enters the first separator 8 and separates，Isolate the first separator exhaust 11，Bottom the first separator 8, separation product out is divided into two parts，A part goes out device as product，Another part is as recycle oil 17，A part of recycle oil 17 loops back the first blender 3，Another part or all recycle oil 17 enter the second blender 6 and are mixed into molten hydrogen recycle oil 15 with hydrogen 2.
Claims (30)
1. a hydrogenation method for hydrocarbon oils, it is characterized in that: hydrogen is mixed to form mixes logistics with fresh feed oil and part recycle oil in the presence of solvent or diluent, mixture stream enters reactor and contacts with catalyst, another part recycle oil mixes with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
2. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1, it is characterised in that: mixing logistics enters reactor from reactor head, and reaction effluent flows out from reactor bottom and carries out gas-liquid separation.
3. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1, it is characterised in that: mixing logistics enters reactor from reactor bottom, and reaction effluent flows out from reactor head and carries out gas-liquid separation.
4. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1, it is characterised in that: another part recycle oil mixes with hydrogen in the presence of solvent or diluent.
5. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: mixture flow separation go out gas laggard enter reactor.
6. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: mixing logistics mixes in blender, enters reactor after gas is isolated at blender top.
7. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: entering the mixing logistics of reactor after gas is isolated at blender top, liquid contacts with catalyst, and gas is got rid of from reactor head.
8. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterized in that: after gas is isolated at blender top, enter the mixing logistics of reactor, liquid and catalyst haptoreaction, gas is got rid of from reactor head, after another part recycle oil mixes eliminating gas with hydrogen, a road or branch enter reactor between reactor catalyst bed.
9. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: solvent or diluent are at least one in the hydrocarbon ils after light distillate, VGO and hydrogenation.
10. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterized in that: utilize the temperature of recycle oil and the mixing ratio control mixture stream entrance reactor of fresh feed oil, utilize the circulation fuel-flow control temperature of reactor entered between beds.
11. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: the catalyst in reactor at least divides two sections of fillings.
12. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: fresh feed oil is the distillate of hydrocarbon ils or hydrocarbon ils.
13. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: fresh feed oil is distillate, lubricating oil, liquefied coal coil, shale oil or its product.
14. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2 or 3 or 4, it is characterised in that: fresh feed oil, in hydrogenation reactor, at least deviates from the one of sulfur, nitrogen, oxygen and metal impurities, and saturated aromatic hydrocarbons.
15. 1 kinds of hydrogenation method for hydrocarbon oils, it is characterized in that: fresh feed oil is mixed to form with hydrogen in the presence of solvent or diluent after mixing with part recycle oil again and mixes logistics, mixture stream enters reactor and contacts with catalyst, another part recycle oil mixes with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
16. according to a kind of hydrogenation method for hydrocarbon oils described in claim 15, it is characterised in that: mixing logistics enters reactor from reactor head, and reaction effluent flows out from reactor bottom and carries out gas-liquid separation.
17. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16, it is characterised in that: mixing logistics enters reactor from reactor bottom, and reaction effluent flows out from reactor head and carries out gas-liquid separation.
18. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16, it is characterised in that: another part recycle oil mixes with hydrogen in the presence of solvent or diluent.
19. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: mixture flow separation go out gas laggard enter reactor.
20. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: mixing logistics mixes in blender, enters reactor after gas is isolated at blender top.
21. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: entering the mixing logistics of reactor after gas is isolated at blender top, liquid contacts with catalyst, and gas is got rid of from reactor head.
22. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterized in that: after gas is isolated at blender top, enter the mixing logistics of reactor, liquid and catalyst haptoreaction, gas is got rid of from reactor head, after another part recycle oil mixes eliminating gas with hydrogen, a road or branch enter reactor between reactor catalyst bed.
23. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: solvent or diluent are at least one in the hydrocarbon ils after light distillate, VGO and hydrogenation.
24. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterized in that: utilize the temperature of recycle oil and the mixing ratio control mixture stream entrance reactor of fresh feed oil, utilize the circulation fuel-flow control temperature of reactor entered between beds.
25. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: the catalyst in reactor at least divides two sections of fillings.
26. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: fresh feed oil is the distillate of hydrocarbon ils or hydrocarbon ils.
27. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: fresh feed oil is distillate, lubricating oil, liquefied coal coil, shale oil or its product.
28. according to a kind of hydrogenation method for hydrocarbon oils described in claim 16 or 17 or 18 or 19, it is characterised in that: fresh feed oil, in hydrogenation reactor, at least deviates from the one of sulfur, nitrogen, oxygen and metal impurities, and saturated aromatic hydrocarbons.
29. 1 kinds of hydrogenation method for hydrocarbon oils, it is characterized in that: fresh feed oil, it is mixed to form with hydrogen after part recycle oil and solvent or diluent mixing and mixes logistics, mixture stream enters reactor and contacts with catalyst, another part recycle oil mixes with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
30. 1 kinds of hydrogenation method for hydrocarbon oils, it is characterized in that: fresh feed oil is mixed to form with part recycle oil and hydrogen after mixing with solvent or diluent again and mixes logistics, mixture stream enters reactor and contacts with catalyst, another recycle oil divides and mixes with hydrogen, one tunnel or branch enter reactor between reactor catalyst bed, reaction effluent is drawn from reactor bottom and is carried out gas-liquid separation, liquid phase is further separated out solvent or diluent recycles, isolated product liquid part is as product, part is as recycle oil, hydrogen dissolubility in solvent or diluent is more than hydrogen dissolubility in fresh feed oil and solvent or diluent mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810140991.8A CN101338220B (en) | 2008-08-11 | 2008-08-11 | A kind of hydrogenation method for hydrocarbon oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810140991.8A CN101338220B (en) | 2008-08-11 | 2008-08-11 | A kind of hydrogenation method for hydrocarbon oils |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101338220A CN101338220A (en) | 2009-01-07 |
| CN101338220B true CN101338220B (en) | 2016-08-03 |
Family
ID=40212392
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200810140991.8A Active CN101338220B (en) | 2008-08-11 | 2008-08-11 | A kind of hydrogenation method for hydrocarbon oils |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101338220B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8926826B2 (en) | 2011-04-28 | 2015-01-06 | E I Du Pont De Nemours And Company | Liquid-full hydroprocessing to improve sulfur removal using one or more liquid recycle streams |
| US9365781B2 (en) | 2012-05-25 | 2016-06-14 | E I Du Pont De Nemours And Company | Process for direct hydrogen injection in liquid full hydroprocessing reactors |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1464034A (en) * | 2002-06-17 | 2003-12-31 | 中国石油化工股份有限公司安庆分公司 | Process for catalyzed gasoline hydrogenation desulfurization |
| CN101194001A (en) * | 2005-03-24 | 2008-06-04 | 过程动力学公司 | Control system method and apparatus for continuous liquid phase hydroprocessing |
-
2008
- 2008-08-11 CN CN200810140991.8A patent/CN101338220B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1464034A (en) * | 2002-06-17 | 2003-12-31 | 中国石油化工股份有限公司安庆分公司 | Process for catalyzed gasoline hydrogenation desulfurization |
| CN101194001A (en) * | 2005-03-24 | 2008-06-04 | 过程动力学公司 | Control system method and apparatus for continuous liquid phase hydroprocessing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101338220A (en) | 2009-01-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10597591B2 (en) | Conversion process comprising permutable hydrodemetallization guard beds, a fixed-bed hydrotreatment step and a hydrocracking step in permutable reactors | |
| CN201644076U (en) | Liquid-phase hydrogenated reactor | |
| CN101280217A (en) | Liquid-solid two-phase hydrogenation method for hydrocarbon oil | |
| CN104560132B (en) | A kind of Continuous Liquid Phase wax oil hydrogenation processing method | |
| CN101875855B (en) | Method for hydrogenation and catalytic cracking of residual oil | |
| KR102529349B1 (en) | Method for converting feedstocks comprising a hydrotreatment step, a hydrocracking step, a precipitation step and a sediment separation step, in order to produce fuel oils | |
| KR102558074B1 (en) | Process integrating two-stage hydrocracking and a hydrotreating process | |
| US8951406B2 (en) | Hydrogen-enriched feedstock for fluidized catalytic cracking process | |
| CN101992048A (en) | Reactor and application thereof to hydrocarbon oil liquid-solid two-phase hydrogenation | |
| CN102732298A (en) | Liquid phase hydrogenation method | |
| CN102041095B (en) | Resid hydrotreating and catalytic cracking combined processing method | |
| CN101993720A (en) | Liquid phase hydrogenating method of hydrocarbon oil | |
| CN101381623B (en) | Liquid-solid two-phase hydrogenation method | |
| CN101338219A (en) | Two-phase hydrogenation process | |
| CN101275083A (en) | Hydrogenation method for hydrocarbon oils | |
| CN101338220B (en) | A kind of hydrogenation method for hydrocarbon oils | |
| CN101280219A (en) | Two-phase hydrogenation method for hydrocarbon oil | |
| CN101280218A (en) | Two-phase hydrogenation method for hydrocarbon oil | |
| CN102453544B (en) | Residual oil hydrogenation treatment and catalytic cracking combination method | |
| CN202063881U (en) | Liquid-phase hydrogenation reactor | |
| CN102311801B (en) | Residual oil hydrogenation treatment and catalytic cracking combined method | |
| CN101358146B (en) | Hydrocarbon oil hydrogenation technique | |
| CN102618320B (en) | Method for biphase hydrogenation of hydrocarbon oil | |
| CN102634367A (en) | Double-phase hydrogenating method | |
| CN102732299A (en) | Hydrocarbon oil two-phase hydrogenation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |