CN102585894B - Hydrocarbon oil hydrogenation method - Google Patents
Hydrocarbon oil hydrogenation method Download PDFInfo
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- CN102585894B CN102585894B CN201210032397.3A CN201210032397A CN102585894B CN 102585894 B CN102585894 B CN 102585894B CN 201210032397 A CN201210032397 A CN 201210032397A CN 102585894 B CN102585894 B CN 102585894B
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Abstract
The invention discloses a hydrocarbon oil hydrogenation method, which cancels recycle hydrogen and a recycle hydrogen compressor. Hydrogen is mixed with fresh raw oil and recycle oil in the presence of solvent or diluent to form the mixture flow which enters into a reactor to be contacted with a catalyst. The other part of the recycle oil is mixed with the hydrogen and subjected to gas exhausting, and the mixture enters the reactor from between reactor catalyst beds in a one-path mode or divided-path mode. The solvent or the diluent is mixed with the hydrogen and subjected to gas exhausting, and the mixture enters the reactor from between reactor catalyst beds in a one-path mode or divided-path mode. Gas-liquid separation is performed on the reaction effluent, the solvent or the diluent is further separated from the liquid phase for recycle use, parts of separated-out liquid products serve as products, and parts of the separated-out liquid products serve as recycle oil.
Description
The application is that application number is: 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 processing technology, hydrogen addition technology is to improve 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 hydrocarbon ils inferior that sulfur-bearing is higher, sulphur, nitrogen, oxygen and metal impurities are removed in refining process, change its quality by the molecular structure that changes hydrocarbon ils, thereby make various products meet code requirement.The hydrogen that in fact hydrocarbon oil hydrogenation process participates in reaction only has the hydrogen for chemical hydrogen consumption, and traditional trickle-bed reactor hydrogen addition technology, need to there is excessive hydrogen to exist, make the volume ratio of reactor larger, and maintain the exess of H2 gas and need to use circulating hydrogen compressor.
In traditional hydrogenation technique, hydrogen need to be delivered to liquid phase from gas phase, and then co-absorbed, on the surface of catalyzer, is reacted under the effect of catalyst active center.Because hydrogenation reaction is a strong exothermal reaction, in order to maintain temperature of reaction, utilize a large amount of hydrogen and stock oil to take away by beds the heat that reaction produces, and the hydrogen of actual needs (chemical hydrogen consumption) is fewer in hydrogenation process, do not participate in the hydrogen of reaction, be recycled to hydrogenator and continue to participate in reaction; It is the hydrogen dividing potential drop that maintains hydrocarbon oil hydrogenation reaction that tradition hydrocarbon oil hydrogenation technology adopts another major cause of excessive hydrogen, maintains higher hydrogen and divides to be pressed on thermodynamics and be conducive to hydrofining and hydrocracking reaction, suppresses to generate the condensation reaction of coke.
The hydrogen of not participating in reaction is by separator and liquid phase separation and remove after impurity, by circulating hydrogen compressor, its pressure is elevated to the required pressure of reaction and delivers to reactor and continue to participate in hydrogenation reaction.The effect of circulating hydrogen compressor is exactly the hydrogen that does not participate in hydrogenation reaction to be improved to pressure it is recycled, and therefore circulating hydrogen compressor becomes requisite equipment in existing hydrogen addition technology, is called in the industry the heart of hydrogenation unit.
In traditional fixed bed hydrogenation reactor, be gas, liquid, solid three-phase 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 catalyzer.Gas-liquid two-phase is to pass through beds with the form of drip, therefore also claims trickle-bed reactor.
In trickle-bed reactor, in order to strengthen mass transfer dynamics, the volume ratio of hydrogen and stock oil is generally 50～2000: 1, therefore hydrogenator design is larger, and the actual stock oil reacting of participating in is relevant with liquid hourly space velocity, air speed has reflected the processing power of device, and industrial hope adopts larger air speed operation, but air speed is subject to the restriction of speed of response.Air speed is unusual at 0.5～10h according to catalyst activity, feedstock property, reaction depth
-1between fluctuation.The unifining process of industrial application can improve olefin saturated rate, hydrogenating desulfurization rate and hydrodenitrification rate at certain temperature of reaction condition decline low-speed at present.Under hydrocracking condition, improve air speed little on the impact of total transformation efficiency, but light constituent content in reaction product declines more.
The object that adopts the exess of H2 gas is strengthen mass transfer and take away the amount of heat producing because of hydrogenation reaction, circulating hydrogen compressor is as the heart of hydrogenation process, investment and process cost are all higher, in order to cancel circulating hydrogen compressor, people start to consider to utilize hydrogen supply agent to provide hydrogen source for hydrocarbon oil hydrogenation process, USP4698147 discloses and has utilized hydrogen supply agent to reduce the residence time, and after reaction, hydrogen supply agent utilizes hydrogen to regenerate, and after regeneration, recycles.In order to strengthen cracking reaction, USP4857168 discloses and has utilized hydrogen supply agent and hydrogen to provide the heavy-oil hydrogenation cracking method of hydrogen source for heavy-oil hydrogenation, and hydrogen supply agent mainly works to suppress to generate the condensation reaction of coke.
Above-mentioned improvement still needs recycle hydrogen and circulating hydrogen compressor, US6428686 has proposed a kind of two-phase hydrogenation method, hydrogen is dissolved in stock oil before reactor, recycle hydrogen and circulating hydrogen compressor are cancelled, investment and the process cost of hydrogenation unit are reduced, this technology adopts the liquid phase circulation of reaction product, improve the meltage of hydrogen, to meet the requirement to hydrogen in hydrogenation process, and take reaction heat out of, this technology is to enter hydrogenator after turning oil is mixed with stock oil and hydrogen, its shortcoming is the speed of response that the existence of a large amount of turning oil can affect fresh feed and hydrogen, because fresh feed is fiercer with hydrogen reaction in the time starting to contact with catalyzer, the existence of turning oil has suppressed the touch opportunity of fresh feed oil and hydrogen and catalyzer, mass transfer and the speed of response of fresh feed oil and hydrogen are reduced.
Summary of the invention
The present invention proposes a kind of two-phase hydrogenation method, cancelled recycle hydrogen and circulating hydrogen compressor, strengthen the touch opportunity of fresh feed oil and hydrogen and catalyzer, improve mass transfer and speed of response.
A kind of two-phase hydrogenation method of the present invention is: hydrogen is mixed to form mixture flow with fresh feed oil and turning oil under the existence of solvent or thinner, mixture flow enters reactor and contacts with catalyzer, solvent or thinner are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase further isolates solvent or thinner recycles, isolated product liquid part is as product, part is as turning oil, hydrogen solubleness in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
The described turning oil mixing with fresh feed oil and hydrogen is part turning oil, and another part turning oil is with after hydrogen mixing Exhaust Gas, and a road or shunt enter reactor between reactor catalyst bed.
Described mixture flow enters reactor from reactor head, and reaction effluent flows out and carries out gas-liquid separation from reactor bottom.
Described mixture flow enters reactor from reactor bottom, and reaction effluent flows out and carries out gas-liquid separation from reactor head.
Described mixture flow enters reactor after isolating gas.
Described mixture flow is mixed in mixing tank, from gas is isolated at mixing tank top, enters reactor.
Described a kind of two-phase hydrogenation method, is further characterized in that: from gas is isolated at mixing tank top, enter the mixture flow of reactor, liquid contacts with catalyzer, and gas is got rid of from reactor head.
The present invention proposes another kind of two-phase hydrogenation method, it is characterized in that: after fresh feed oil mixes with turning oil, under the existence of solvent or thinner, be mixed to form mixture flow with hydrogen again, mixture flow enters reactor and contacts with catalyzer, solvent or thinner are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase further isolates solvent or thinner recycles, isolated product liquid part is as product, part is as turning oil, the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
The described turning oil mixing with fresh feed oil is part turning oil, and another part turning 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, is further characterized in that: mixture flow enters reactor from reactor head, and reaction effluent flows out and carries out gas-liquid separation from reactor bottom.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor from reactor bottom, and reaction effluent flows out and carries out gas-liquid separation from reactor head.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor after isolating gas.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow is mixed in mixing tank, from gas is isolated at mixing tank top, enters reactor.
Described another kind of two-phase hydrogenation method, is further characterized in that: from isolating gas, mixing tank top enters the mixture flow of reactor, and liquid and catalyzer contact reacts, gas is got rid of from reactor head.
The present invention proposes another kind of two-phase hydrogenation method, it is characterized in that: after fresh feed oil and turning oil and solvent or mixing diluents, be mixed to form mixture flow with hydrogen, mixture flow enters reactor and contacts with catalyzer, solvent or thinner are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase further isolates solvent or thinner recycles, isolated product liquid part is as product, part is as turning oil, the solubleness of hydrogen in solvent or thinner is greater than the solubleness of hydrogen in fresh feed oil and solvent or diluent mixture.
The described turning oil mixing with fresh feed oil is part turning oil, and another part turning 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, is further characterized in that: mixture flow enters reactor from reactor head, and reaction effluent flows out and carries out gas-liquid separation from reactor bottom.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor from reactor bottom, and reaction effluent flows out and carries out gas-liquid separation from reactor head.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor after isolating gas.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow is mixed in mixing tank, from gas is isolated at mixing tank top, enters reactor.
Described another kind of two-phase hydrogenation method, is further characterized in that: from isolating gas, mixing tank top enters the mixture flow of reactor, and liquid and catalyzer contact reacts, gas is got rid of from reactor head.
The another kind of two-phase hydrogenation method of the present invention, it is characterized in that: after fresh feed oil and solvent or mixing diluents, be mixed to form mixture flow with turning oil and hydrogen, mixture flow enters reactor and contacts with catalyzer, solvent or thinner are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase further isolates solvent or thinner recycles, isolated product liquid part is as product, and part is as turning oil.
The described turning oil mixing with fresh feed oil is part turning oil, and another part turning 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, is further characterized in that: mixture flow enters reactor from reactor head, and reaction effluent flows out and carries out gas-liquid separation from reactor bottom.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor from reactor bottom, and reaction effluent flows out and carries out gas-liquid separation from reactor head.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow enters reactor after isolating gas.
Described another kind of two-phase hydrogenation method, is further characterized in that: mixture flow is mixed in mixing tank, from gas is isolated at mixing tank top, enters reactor.
Described another kind of two-phase hydrogenation method, is further characterized in that: from isolating gas, mixing tank top enters the mixture flow of reactor, and liquid and catalyzer contact reacts, gas is got rid of from reactor head.
In hydrogenator of the present invention, catalyzer at least divides two sections of bed fillings, form at least two-stage catalytic agent bed, be mixed into second segment beds from effluent out of first paragraph beds and the turning oil of introducing, contact with catalyzer and proceed reaction, from mixing with the turning oil of introducing, second segment beds effluent out enters the 3rd section of beds, the rest may be inferred, and reaction effluent is drawn from reactor bottom.
Solvent of the present invention or thinner are at least one in the hydrocarbon ils after heavy naphtha, petroleum naphtha, lighter hydrocarbons, benzoline, diesel oil, VGO and hydrogenation.
The fresh feed oil of two-phase hydrogenation method of the present invention is the distillate of hydrocarbon ils or hydrocarbon ils, as petroleum fractions, distillate, diesel oil, deasphalted oil, residual oil, lubricating oil, liquefied coal coil and shale oil or its product.
Two-phase hydrogenation method of the present invention, at least removes a kind of pollutent in its sulphur, nitrogen, oxygen, metallic impurity, and saturated aromatic hydrocarbons, changes the molecular structure of hydrocarbon ils.
Two-phase hydrogenation method of the present invention has been cancelled recycle hydrogen and circulating hydrogen compressor, utilize hydrocarbon ils, solvent or thinner that hydrogen is dissolved in wherein, for hydrocarbon oil hydrogenation provides hydrogen source, wherein solvent or thinner are greater than hydrocarbon ils to the dissolving power of hydrogen, the addition of solvent or thinner is according to the amount of the required hydrogen of hydrocarbon oil hydrogenation process reaction, i.e. chemical hydrogen consumption and regulating.
Two-phase hydrogenation method of the present invention: the temperature of utilizing the ratio of mixture control mixture flow of turning oil and solvent or thinner and fresh feed oil to enter reactor, utilize to enter between beds, to be dissolved with the turning oil of hydrogen and the amount control temperature of reactor of solvent or thinner.
Maximum problem of hydrogenation process is beds coking, under reaction conditions, can there is coking reaction, if there is no enough hydrogen, cracking reaction meeting causes coke to form, and is deposited on catalyst surface, and the present invention is owing to adopting turning oil circulation, it is saturated that turning oil obtains much aromatic hydrocarbons through hydrogenation, there is the function of hydrogen supply, can suppress coke and form, the life-span of extending catalyst.
Two-phase hydrogenation method of the present invention can be used for straight run, FCC turning oil, coker gas oil CGO, or it mixes kerosene and diesel oil hydrogenation processing, also can be used for FCC raw materials pretreatment, for new device and mild hydrocracking transformation, for the production of ULSD, for the pre-treatment of raw material or the aftertreatment of product.
Two-phase hydrogenation method of the present invention has following advantage:
1) catalyst levels is few;
2) hydrogen loss is less;
3) lower process cost;
4) liquid yield is higher;
5) larger flexibility of operation;
6) the sulphur nitrogen content of product is very low;
7) lower investment;
8) for producing ultra-low-sulphur diesel, improvement expenses is very low.
Compared with the prior art of trickle bed hydrogenator, advantage of the present invention is: can desulfurization 90%～98%, and hydrogen consumption is only 70%～90% of trickle bed hydrogenator, the total consumption of catalyzer is only 15%～30%.
Brief description of the drawings
Fig. 1 is two-phase hydrogenation processing flow chart of the present invention.
Fig. 2 is the another kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 3 is the third two-phase hydrogenation processing flow chart of the present invention.
Fig. 4 is the 4th kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 5 is the 5th kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 6 is the 6th kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 7 is the 7th kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 8 is the 8th kind of two-phase hydrogenation processing flow chart of the present invention.
Fig. 9 is the 9th kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 10 is the tenth kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 11 is the 11 kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 12 is the 12 kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 13 is the 13 kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 14 is the 14 kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 15 is the 15 kind of two-phase hydrogenation processing flow chart of the present invention.
Figure 16 is the 16 kind of two-phase hydrogenation processing flow chart of the present invention.
In figure: 1-fresh feed oil, 2-hydrogen, 3-the first mixing tank, 4-separating tank, 5-reactor, 6-the second mixing tank, 7-reactor feed, 8-the first separator, 9-the second separator, 10-the 3rd mixing tank; 11-the first separator waste gas, the molten hydrogen solvent of 12-or thinner; 13-solvent or thinner, 14-separating tank waste gas, the molten hydrogen turning oil of 15-, 16-the first separator separated product, 17-turning oil, 18-the 3rd mixing tank waste gas, 19-the second mixing tank waste gas.
Embodiment
As shown in Figure 1, reactor shown in figure is four sections of beds.Fresh feed oil 1 mixes in the first mixing tank 3 with hydrogen 2 and turning oil 17 under partial solvent or thinner 13 existence, mixture flow enters separating tank 4, after isolating separating tank waste gas 14, become reactor feed 7, reactor feed 7 enters reactor first paragraph beds and catalyzer contact reacts from reactor 5 tops, another part solvent or thinner 13 mix in the 3rd mixing tank 10 with hydrogen 2 and discharge the 3rd mixing tank waste gas 18, molten hydrogen solvent or thinner 12 are respectively from first paragraph and the second segment beds of reactor 5, between second segment and the 3rd section of beds and the 3rd section and the 4th section of beds, enter reactor 5, entering the first separator 8 from reactor 5 bottoms reaction effluent out separates, isolate the first separator waste gas 11, be divided into two portions from the first separator 8 bottoms separated product out, a part is as the first separator separated product 16, another part is as turning oil 17, the first separator separated product 16 enters the second separator 9 again and separates, from the second separator 9 tops logistics out as solvent or thinner 13, go out device from the second separator 9 bottoms separated product out as product.
Fig. 2, the difference of itself and Fig. 1 is: reactor feed 7 enters reactor 5 from reactor 5 bottoms, 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: turning oil 17 is divided into two portions, part turning oil 17 enters the first mixing tank 3, another part turning oil 17 mixes in the second mixing tank 6 with hydrogen 2 discharges the second mixing tank waste gas 19 and becomes molten hydrogen turning oil 15, enters reactor 5 respectively between the first paragraph of reactor 5 and second segment beds, second segment and the 3rd section of beds and 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 from reactor 5 bottoms, 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: after fresh feed oil 1 mixes with turning oil 17, be mixed to form mixture flow again under the existence of partial solvent or thinner 13 with hydrogen 2 in the first mixing tank 3.
Fig. 6, the difference of itself and Fig. 5 is: reactor feed 7 enters reactor 5 from reactor 5 bottoms, 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: turning oil 17 is divided into two portions, part turning oil 17 enters the first mixing tank 3, another part turning oil 17 mixes in the second mixing tank 6 with hydrogen 2 discharges the second mixing tank waste gas 19 and becomes molten hydrogen turning oil 15, enters reactor 5 respectively between the first paragraph of reactor 5 and second segment beds, second segment and the 3rd section of beds and 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 from reactor 5 bottoms, and reactor exhausts 4 are discharged at reactor 5 tops, and reactor 5 tops reaction effluent out enters the first separator 8 and separates.
Fig. 9, it is with the difference of Fig. 1: after fresh feed oil 1 and partial solvent or thinner 13 mix, be mixed to form mixture flow again with turning oil 17 and hydrogen 2 in the first mixing tank.
Figure 10, the difference of itself and Fig. 9 is: reactor feed 7 enters reactor 5 from reactor 5 bottoms, and reactor exhausts 4 are discharged at reactor 5 tops, and reactor 5 tops reaction effluent out enters the first separator 8 and separates.
Figure 11, the difference of itself and Fig. 9 is: turning oil 17 is divided into two portions, part turning oil 17 enters the first mixing tank 3, another part turning oil 17 mixes in the second mixing tank 6 with hydrogen 2 discharges the second mixing tank waste gas 19 and becomes molten hydrogen turning oil 15, enters reactor 5 respectively between the first paragraph of reactor 5 and second segment beds, second segment and the 3rd section of beds and 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 from reactor 5 bottoms, and reactor exhausts 4 are discharged at reactor 5 tops, and reactor 5 tops reaction effluent out enters the first separator 8 and separates.
Figure 13, it is with the difference of Fig. 1: fresh feed oil 1, turning oil are mixed to form mixture flow with hydrogen 2 after mixing with partial solvent or thinner 13 again in the first mixing tank 3.
Figure 14, the difference of itself and Figure 13 is: reactor feed 7 enters reactor 5 from reactor 5 bottoms, and reactor exhausts 4 are discharged at reactor 5 tops, and reactor 5 tops reaction effluent out enters the first separator 8 and separates.
Figure 15, the difference of itself and Figure 13 is: turning oil 17 is divided into two portions, part turning oil 17 enters the first mixing tank 3, another part turning oil 17 mixes in the second mixing tank 6 with hydrogen 2 discharges the second mixing tank waste gas 19 and becomes molten hydrogen turning oil 15, enters reactor 5 respectively between the first paragraph of reactor 5 and second segment beds, second segment and the 3rd section of beds and 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 from reactor 5 bottoms, and reactor exhausts 4 are discharged at reactor 5 tops, and reactor 5 tops reaction effluent out enters the first separator 8 and separates.
Claims (4)
1. a hydrogenation method for hydrocarbon oils, it is characterized in that: after fresh feed oil mixes with turning oil, under the existence of solvent or thinner, be mixed to form mixture flow with hydrogen again, mixture flow is liquid and catalyzer contact reacts from gas is isolated at mixing tank top, gas is got rid of from reactor head, solvent or thinner are with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, reaction effluent carries out gas-liquid separation, liquid phase further isolates solvent or thinner recycles, isolated product liquid part is as product, part is as turning oil, the turning oil mixing with fresh feed oil is part turning oil, another part turning oil is with after hydrogen mixing Exhaust Gas, one tunnel or shunt enter reactor between reactor catalyst bed, catalyzer in reactor at least divides two sections of fillings.
2. according to a kind of hydrogenation method for hydrocarbon oils claimed in claim 1, it is characterized in that: mixture flow enters reactor from reactor head, reaction effluent flows out and carries out gas-liquid separation from reactor bottom; Or mixture flow enters reactor from reactor bottom, reaction effluent flows out and carries out gas-liquid separation from reactor head.
3. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2, it is characterized in that: solvent or thinner are at least one in petroleum naphtha, lighter hydrocarbons, benzoline, diesel oil and VGO.
4. according to a kind of hydrogenation method for hydrocarbon oils described in claim 1 or 2, it is characterized in that: the temperature of utilizing the ratio of mixture control mixture flow of turning oil and solvent or thinner and fresh feed oil to enter reactor, utilize to enter between beds, to be dissolved with the turning oil of hydrogen and the amount control temperature of reactor of solvent or thinner.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4698147A (en) * | 1985-05-02 | 1987-10-06 | Conoco Inc. | Short residence time hydrogen donor diluent cracking process |
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN101210195A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrocracking method for more producing chemical industry light oil from poor heavy raw material |
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2008
- 2008-08-11 CN CN201210032397.3A patent/CN102585894B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4698147A (en) * | 1985-05-02 | 1987-10-06 | Conoco Inc. | Short residence time hydrogen donor diluent cracking process |
| US6428686B1 (en) * | 1997-06-24 | 2002-08-06 | Process Dynamics, Inc. | Two phase hydroprocessing |
| CN101210195A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrocracking method for more producing chemical industry light oil from poor heavy raw material |
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