CN102618320B - Method for biphase hydrogenation of hydrocarbon oil - Google Patents
Method for biphase hydrogenation of hydrocarbon oil Download PDFInfo
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- CN102618320B CN102618320B CN201210032299.XA CN201210032299A CN102618320B CN 102618320 B CN102618320 B CN 102618320B CN 201210032299 A CN201210032299 A CN 201210032299A CN 102618320 B CN102618320 B CN 102618320B
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Abstract
The present invention discloses a method for biphase hydrogenation of hydrocarbon oil. According to the method, recycle hydrogen and a recycle hydrogen compressor are cancelled; hydrogen is mixed with fresh raw oil and one part of recycle oil in the presence of a solvent or a diluent to form a mixture flow, and the mixture flow enters a reactor to contact with a catalyst; after the other part of the recycle oil is mixed with the hydrogen and the gas is discharged, an obtained mixture enters the reactor by a path or branches from spaces between catalyst bed layers of the reactor; after the solvent or the diluent is mixed with the hydrogen and the gas is discharged, an obtained mixture enters the reactor by a path or branches from spaces between catalyst bed layers of the reactor; the reaction effluent is subjected to gas-liquid separation, and the liquid phase is further separated to obtain the solvent or the diluent, wherein the separated solvent or the separated diluent is used for recycle use; and the partial separated liquid product is used as the product, and the partial separated liquid product is used as the recycle oil.
Description
The application is application number: 200810140990.3, and the applying date is: on 08 11st, 2008, name was called: a kind of divisional application of two-phase hydrogenation method
Technical field
The present invention relates to hydrocarbon oil hydrogenation technology, particularly liquid-solid two-phase hydrocarbon oil hydrogenation technology.
Background technology
In hydrocarbon ils process technology, hydrogen addition technology improves one of conventional technology of hydrocarbon ils quality, along with global crude oil market supply is tending towards the crude oil of higher sulfur content, refinery need process the higher hydrocarbon ils inferior of sulfur-bearing, sulphur, nitrogen, oxygen and metal impurities are removed in refining process, change its quality by the molecular structure changing hydrocarbon ils, thus make various product meet code requirement.The hydrogen that in fact hydrocarbon oil hydrogenation process participates in reacting only has the hydrogen for chemical hydrogen consumption, and traditional trickle bed reactor hydrogen addition technology, need excessive hydrogen to exist, make the volume ratio of reactor comparatively large, and maintain the exess of H2 gas and need to use circulating hydrogen compressor.
In traditional hydrogenation technique, hydrogen needs to be delivered to liquid phase from gas phase, is then jointly adsorbed on the surface of catalyst, reacts under the effect of catalyst active center.Because hydrogenation reaction is a strong exothermal reaction, in order to maintain reaction temperature, a large amount of hydrogen and feedstock oil is utilized to take away the heat of reaction generation by beds, and the hydrogen (chemical hydrogen consumption) of actual needs is fewer in hydrogenation process, do not participate in the hydrogen of reaction, be recycled to hydrogenation reactor and continue to participate in reaction; Tradition hydrocarbon oil hydrogenation technology adopts another main cause of excessive hydrogen to be the hydrogen dividing potential drop maintaining hydrocarbon oil hydrogenation reaction, maintains higher hydrogen dividing potential drop and is thermodynamically conducive to hydrofinishing and hydrocracking reaction, suppresses the condensation reaction generating coke.
The hydrogen not participating in reaction is by separator and liquid phase separation and after removing impurity, by circulating hydrogen compressor, its pressure pressure be elevated to needed for reaction is delivered to reactor and continue to participate in hydrogenation reaction.The effect of circulating hydrogen compressor is exactly the hydrogen not participating in hydrogenation reaction is improved pressure make 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.
Be 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 the hydrocarbon raw material of not vaporizing, and solid phase is catalyst.Gas-liquid two-phase be with the form of drip by beds, therefore also claim trickle bed reactor.
In trickle bed reactor, in order to strengthen mass transfer dynamics, the volume ratio of hydrogen and feedstock oil is generally 50 ~ 2000: 1, therefore hydrogenation reactor design is larger, and the actual feedstock oil reacted of participating in is relevant with liquid hourly space velocity (LHSV), air speed reflects the disposal ability of device, and industrial hope adopts larger air speed operation, but air speed is subject to the restriction of reaction speed.Air speed according to catalyst activity, feedstock property, reaction depth unusual at 0.5 ~ 10h
-1between fluctuation.The unifining process of current commercial Application can improve olefin saturated rate, hydrodesulfurization rate and hydrodenitrogeneration rate at certain reaction temperature condition decline low-speed.Under hydrocracking condition, improve air speed little on the impact of total conversion ratio, but the light component content in product declines more.
The object of the exess of H2 gas is adopted to be 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 all higher, in order to cancel circulating hydrogen compressor, people start consideration and utilize hydrogen supply agent to provide hydrogen source for hydrocarbon oil hydrogenation process, namely USP4698147 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 mainly works the condensation reaction suppressing to generate coke.
Above-mentioned improvement still needs recycle hydrogen and circulating hydrogen compressor, US6428686 proposes a kind of two-phase hydrogenation method, hydrogen is dissolved in feedstock oil before reactor, eliminate recycle hydrogen and circulating hydrogen compressor, reduce investment and the operating cost of hydrogenation plant, this technology adopts the liquid phase circulation of product, improve the meltage of hydrogen, to meet the requirement to hydrogen in hydrogenation process, and take reaction heat out of, this technology enters hydrogenation reactor after being mixed with feedstock oil and hydrogen by recycle oil, its shortcoming is the reaction speed that the existence of a large amount of recycle oil can affect fresh feed and hydrogen, because fresh feed and hydrogen are in beginning and react fiercer during catalyst exposure, the existence of recycle oil inhibits the touch opportunity of fresh feed oil and hydrogen and catalyst, reduce mass transfer and the reaction speed of fresh feed oil and hydrogen.
Summary of the invention
The present invention proposes a kind of two-phase hydrogenation method for hydrocarbon oil, eliminate recycle hydrogen and circulating hydrogen compressor, strengthen the touch opportunity of fresh feed oil and hydrogen and catalyst, improve mass transfer and reaction speed.
A kind of two-phase hydrogenation method for hydrocarbon oil of the present invention is: hydrogen is mixed to form with fresh feed oil and recycle oil and mixes logistics under the existence of solvent or diluent, mixture flows to into reactor and catalyst exposure, solvent or diluent are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent part carries out gas-liquid separation, liquid phase isolates solvent further or diluent recycles, isolated product liquid is as product, hydrogen solubility in solvent or diluent is greater than the solubility of hydrogen in fresh feed oil and solvent or diluent mixture.
The described recycle oil mixed with fresh feed oil and hydrogen is component loops oil, and another part recycle oil is with after hydrogen mixing Exhaust Gas, and a road or shunt enter reactor between reactor catalyst bed.
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 mixture flow point from go out gas laggard enter reactor.
Described mixing logistics mixes in blender, from blender top portion from go out gas laggard enter reactor.
Described a kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: from blender top portion from go out gas laggard enter the mixing logistics of reactor, liquid and catalyst exposure, gas is got rid of from reactor head.
The present invention proposes another kind of two-phase hydrogenation method for hydrocarbon oil, it is characterized in that: be mixed to form with hydrogen under the existence of solvent or diluent again after fresh feed oil mixes with recycle oil and mix logistics, mixture flows to into reactor and catalyst exposure, solvent or diluent are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent part carries out gas-liquid separation, liquid phase isolates solvent further or diluent recycles, isolated product liquid is as product, part is as recycle oil, the solubility of hydrogen in solvent or diluent is greater than the solubility of hydrogen in fresh feed oil and solvent or diluent mixture.
The described recycle oil mixed with fresh feed oil is component loops oil, and another part recycle oil is with after hydrogen mixing Exhaust Gas, and a road or shunt enter reactor between reactor catalyst bed.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, 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 two-phase hydrogenation method for hydrocarbon oil, 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 kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixture flow point from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixing logistics mix in blender, from blender top portion from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: from blender top portion from go out gas laggard enter the mixing logistics of reactor, liquid and catalyst exposure react, and gas is got rid of from reactor head.
The present invention proposes another kind of two-phase hydrogenation method for hydrocarbon oil, it is characterized in that: fresh feed oil mixes logistics with being mixed to form with hydrogen after recycle oil and solvent or mixing diluents, mixture flows to into reactor and catalyst exposure, solvent or diluent are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent part carries out gas-liquid separation, liquid phase isolates solvent further or diluent recycles, isolated product liquid is as product, part is as recycle oil, the solubility of hydrogen in solvent or diluent is greater than the solubility of hydrogen in fresh feed oil and solvent or diluent mixture.
The described recycle oil mixed with fresh feed oil is component loops oil, and another part recycle oil is with after hydrogen mixing Exhaust Gas, and a road or shunt enter reactor between reactor catalyst bed.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, 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 two-phase hydrogenation method for hydrocarbon oil, 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 kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixture flow point from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixing logistics mix in blender, from blender top portion from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: from blender top portion from go out gas laggard enter the mixing logistics of reactor, liquid and catalyst exposure react, and gas is got rid of from reactor head.
The another kind of two-phase hydrogenation method for hydrocarbon oil of the present invention, it is characterized in that: fresh feed oil mixes logistics with being mixed to form with recycle oil and hydrogen after solvent or mixing diluents, mixture flows to into reactor and catalyst exposure, solvent or diluent are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent part carries out gas-liquid separation, liquid phase isolates solvent further or diluent recycles, isolated product liquid is as product, and part is as recycle oil.
The described recycle oil mixed with fresh feed oil is component loops oil, and another part recycle oil is with after hydrogen mixing Exhaust Gas, and a road or shunt enter reactor between reactor catalyst bed.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, 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 two-phase hydrogenation method for hydrocarbon oil, 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 kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixture flow point from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: mixing logistics mix in blender, from blender top portion from go out gas laggard enter reactor.
Described another kind of two-phase hydrogenation method for hydrocarbon oil, is further characterized in that: from blender top portion from go out gas laggard enter the mixing logistics of reactor, liquid and catalyst exposure react, and gas is got rid of from reactor head.
In hydrogenation reactor of the present invention, catalyst at least divides two sections of bed fillings, form at least two-stage catalytic agent bed, second segment beds is mixed into from the recycle oil of first paragraph beds effluent out and introducing, proceed to react with catalyst exposure, the 3rd section of beds is entered after second segment beds effluent out mixes with the recycle oil of introducing, 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, naphtha, lighter hydrocarbons, light distillate, diesel oil, VGO and hydrogenation.
The fresh feed oil of two-phase hydrogenation method for hydrocarbon oil of the present invention is the distillate of hydrocarbon ils or hydrocarbon ils, as petroleum distillate, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
Two-phase hydrogenation method for hydrocarbon oil of the present invention, at least removes a kind of pollutant in its sulphur, nitrogen, oxygen, metal impurities, and saturated aromatic hydrocarbons, change the molecular structure of hydrocarbon ils.
Two-phase hydrogenation method for hydrocarbon oil of the present invention eliminates recycle hydrogen and circulating hydrogen compressor, hydrocarbon ils, solvent or diluent is utilized to be dissolved in wherein by hydrogen, for hydrocarbon oil hydrogenation provides hydrogen source, wherein solvent or the solvability of diluent to hydrogen are greater than hydrocarbon ils, the amount of addition hydrogen needed for hydrocarbon oil hydrogenation process reaction of solvent or diluent, i.e. chemical hydrogen consumption and regulating.
Two-phase hydrogenation method for hydrocarbon oil of the present invention: utilize the mixing ratio of recycle oil and solvent or diluent and fresh feed oil to control mixture and flow to temperature into reactor, utilizes the amount entering recycle oil and solvent or the diluent being dissolved with hydrogen between beds to control temperature of reactor.
The maximum problem of hydrogenation process one is beds coking, coking reaction can be there is under reaction condition, if there is no enough hydrogen, cracking reaction can cause coke to be formed, and is deposited on catalyst surface, and the present invention is owing to adopting recycle oil circulation, it is saturated that recycle oil makes much aromatic hydrocarbons obtain through hydrogenation, there is the function of hydrogen supply, coke can be suppressed to be formed, the life-span of extending catalyst.
Two-phase hydrogenation method for hydrocarbon oil of the present invention can be used for straight-run, FCC recycle oil, coker gas oil CGO, or its mixing kerosene and diesel oil hydrogenation process, also can be used for FCC pretreatment of raw material, for new device and mild hydrocracking transformation, for the production of ULSD, for the pretreatment of raw material or the post processing of product.
Two-phase hydrogenation method for hydrocarbon oil of the present invention has following advantage:
1) catalyst amount is few;
2) hydrogen loss is less;
3) lower operating cost;
4) liquid yield is higher;
5) larger operating flexibility;
6) the sulphur nitrogen content of product is very low;
7) lower investment;
8) for production ultra-low-sulphur diesel, improvement expenses is very low.
Compared with the prior art of trickle bed hydrogenation reactor, advantage of the present invention is: can desulfurization 90% ~ 98%, and hydrogen consumption is only 70% ~ 90% of trickle bed hydrogenation reactor, and the total consumption of catalyst is only 15% ~ 30%.
Accompanying drawing explanation
Fig. 1 is hydrocarbon ils two-phase hydrogenation process chart of the present invention.
Fig. 2 is the present invention's another kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 3 is the third hydrocarbon ils two-phase hydrogenation process chart of the present invention.
Fig. 4 is the present invention's the 4th kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 5 is the present invention's the 5th kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 6 is the present invention's the 6th kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 7 is the present invention's the 7th kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 8 is the present invention's the 8th kind of hydrocarbon ils two-phase hydrogenation process chart.
Fig. 9 is the present invention's the 9th kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 10 is the present invention's the tenth kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 11 is the present invention's the 11 kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 12 is the present invention's the 12 kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 13 is the present invention's the 13 kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 14 is the present invention's the 14 kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 15 is the present invention's the 15 kind of hydrocarbon ils two-phase hydrogenation process chart.
Figure 16 is the present invention's the 16 kind of hydrocarbon ils two-phase hydrogenation process chart.
In figure: 1-fresh feed oil, 2-hydrogen, 3-first blender, 4-knockout drum, 5-reactor, 6-second blender, 7-reactor feed, 8-first separator, 9-second separator, 10-the 3rd blender; 11-first separator waste gas, the molten hydrogen solvent of 12-or diluent; 13-solvent or diluent, 14-knockout drum waste gas, the molten hydrogen recycle oil of 15-, 16-first separator separated product, 17-recycle oil, 18-the 3rd blender waste gas, 19-second blender waste gas.
Detailed description of the invention
As shown in Figure 1, reactor shown in figure is four sections of beds.Fresh feed oil 1 mixes in the first blender 3 with hydrogen 2 and recycle oil 17 under partial solvent or diluent 13 exist, mixture flows to into knockout drum 4, reactor feed 7 is become after isolating knockout drum waste gas 14, reactor feed 7 enters reactor first paragraph beds from reactor 5 top and catalyst exposure reacts, another part solvent or diluent 13 mix with hydrogen 2 and discharge the 3rd blender waste gas 18 in the 3rd blender 10, molten hydrogen solvent or diluent 12 are respectively from first paragraph and the second segment beds of reactor 5, second segment and the 3rd section of beds and enter reactor 5 between the 3rd section and the 4th section of beds, bottom reactor 5, reaction effluent out enters the first separator 8 and is separated, isolate the first separator waste gas 11, bottom the first separator 8, separated product is out divided into two parts, a part is as the first separator separated product 16, another part is as recycle oil 17, first separator separated product 16 enters the second separator 9 again and is separated, from the second separator 9 top logistics out as solvent or diluent 13, bottom the second separator 9, separated product out goes out device as product.
Fig. 2, the difference of itself and Fig. 1 is: 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, the difference of itself and Fig. 1 is: recycle oil 17 is divided into two parts, part recycle oil 17 enters the first blender 3, another part recycle oil 17 and hydrogen 2 mix discharge second blender waste gas 19 in the second blender 6 becomes molten hydrogen recycle oil 15, respectively from first paragraph and second segment beds, second segment and the 3rd section of beds of reactor 5 with enter reactor 5 between the 3rd section and the 4th section of beds.
Fig. 4, the difference of itself and Fig. 3 is: 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. 1: be mixed to form in the first blender 3 with hydrogen 2 under the existence of partial solvent or diluent 13 after fresh feed oil 1 mixes with recycle oil 17 again and mix logistics.
Fig. 6, the difference of itself and Fig. 5 is: 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, the difference of itself and Fig. 5 is: recycle oil 17 is divided into two parts, part recycle oil 17 enters the first blender 3, another part recycle oil 17 and hydrogen 2 mix discharge second blender waste gas 19 in the second blender 6 becomes molten hydrogen recycle oil 15, respectively from first paragraph and second segment beds, second segment and the 3rd section of beds of reactor 5 with enter reactor 5 between the 3rd section and the 4th section of beds.
Fig. 8, the difference of itself and Fig. 7 is: reactor feed 7 enters reactor 5 bottom reactor 5, and reactor exhaust 4 is discharged at reactor 5 top, and reactor 5 top reaction effluent out enters the first separator 8 and is separated.
Fig. 9, it is with the difference of Fig. 1: be mixed to form in the first blender with recycle oil 17 and hydrogen 2 after fresh feed oil 1 and partial solvent or diluent 13 mix again and mix logistics.
Figure 10, the difference of itself and Fig. 9 is: reactor feed 7 enters reactor 5 bottom reactor 5, and reactor exhaust 4 is discharged at reactor 5 top, and reactor 5 top reaction effluent out enters the first separator 8 and is separated.
Figure 11, the difference of itself and Fig. 9 is: recycle oil 17 is divided into two parts, part recycle oil 17 enters the first blender 3, another part recycle oil 17 and hydrogen 2 mix discharge second blender waste gas 19 in the second blender 6 becomes molten hydrogen recycle oil 15, respectively from first paragraph and second segment beds, second segment and the 3rd section of beds of reactor 5 with enter reactor 5 between the 3rd section and the 4th section of beds.
Figure 12, the difference of itself and Figure 11 is: reactor feed 7 enters reactor 5 bottom reactor 5, and reactor exhaust 4 is discharged at reactor 5 top, and reactor 5 top reaction effluent out enters the first separator 8 and is separated.
Figure 13, it is with the difference of Fig. 1: fresh feed oil 1, recycle oil are mixed to form with hydrogen 2 after mixing with partial solvent or diluent 13 again and mix logistics in the first blender 3.
Figure 14, the difference of itself and Figure 13 is: reactor feed 7 enters reactor 5 bottom reactor 5, and reactor exhaust 4 is discharged at reactor 5 top, and reactor 5 top reaction effluent out enters the first separator 8 and is separated.
Figure 15, the difference of itself and Figure 13 is: recycle oil 17 is divided into two parts, part recycle oil 17 enters the first blender 3, another part recycle oil 17 and hydrogen 2 mix discharge second blender waste gas 19 in the second blender 6 becomes molten hydrogen recycle oil 15, respectively from first paragraph and second segment beds, second segment and the 3rd section of beds of reactor 5 with enter reactor 5 between the 3rd section and the 4th section of beds.
Figure 16, the difference of itself and Figure 15 is: reactor feed 7 enters reactor 5 bottom reactor 5, and reactor exhaust 4 is discharged at reactor 5 top, and reactor 5 top reaction effluent out enters the first separator 8 and is separated.
Claims (2)
1. a two-phase hydrogenation method for hydrocarbon oil, it is characterized in that: be mixed to form with hydrogen after fresh feed oil and solvent oily with component loops or mixing diluents and mix logistics, another part recycle oil is with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reactor and catalyst exposure is entered from liquid reactor top after mixing logistics hybrid separation in blender goes out gas, gas is got rid of from reactor head, solvent or diluent are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent flows out from reactor bottom and carries out gas-liquid separation, or mixing logistics enters reactor from reactor bottom, reaction effluent flows out from reactor head and carries out gas-liquid separation, liquid phase isolates solvent further or diluent recycles, isolated product liquid is as product, part is as recycle oil, catalyst in reactor at least divides two sections of fillings, utilize the mixing ratio of recycle oil and solvent or diluent and fresh feed oil to control mixture and flow to temperature into reactor, utilize the amount entering recycle oil and solvent or the diluent being dissolved with hydrogen between beds to control temperature of reactor.
2. according to a kind of two-phase hydrogenation method for hydrocarbon oil according to claim 1, it is characterized in that: solvent or diluent are at least one in the hydrocarbon ils after heavy naphtha, naphtha, lighter hydrocarbons, light distillate, diesel oil, VGO and hydrogenation.
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| CN103131461A (en) * | 2013-03-11 | 2013-06-05 | 中国寰球工程公司辽宁分公司 | Hydrocarbon oil hydrogenation method |
| CN104560132B (en) * | 2013-10-29 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of Continuous Liquid Phase wax oil hydrogenation processing method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU658130B2 (en) * | 1990-11-07 | 1995-04-06 | Davy Process Technology Limited | Hydrodesulphurization process |
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1746266A (en) * | 2004-09-07 | 2006-03-15 | 白跃华 | Energy-saving process with hydrotreatment |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU658130B2 (en) * | 1990-11-07 | 1995-04-06 | Davy Process Technology Limited | Hydrodesulphurization process |
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN1746266A (en) * | 2004-09-07 | 2006-03-15 | 白跃华 | Energy-saving process with hydrotreatment |
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