CN108085059A - A kind of method that heavy benzene hydrogenation refines fuel oil - Google Patents

A kind of method that heavy benzene hydrogenation refines fuel oil Download PDF

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Publication number
CN108085059A
CN108085059A CN201711361513.5A CN201711361513A CN108085059A CN 108085059 A CN108085059 A CN 108085059A CN 201711361513 A CN201711361513 A CN 201711361513A CN 108085059 A CN108085059 A CN 108085059A
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hydrogenation
benzene
hydrogenation reactor
hydrogen
reactor
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金冬梅
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1096—Aromatics or polyaromatics
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention relates to a kind of methods that heavy benzene hydrogenation refines fuel oil, this method is that heavy benzol and hydrogen are separately added into the first hydrogenation reactor to carry out pre-hydrotreating reaction, reaction product enters de- benzene unit, isolate benzene, toluene and dimethylbenzene, remaining ingredient is sent into evaporator and is vaporized, after the boil-off gas of evaporator outlet is mixed with hydrogen, preliminary hydrofining reaction is carried out into the second hydrogenation reactor, reaction product is sent into the 3rd hydrogenation reactor and carries out further hydrofining reaction, reaction product carries out rectifying separation again, respectively obtain gasoline fraction and diesel oil distillate.The method of the present invention directly can carry out hydrotreating by counterweight benzene raw materials, promote the further utilization of coal tar, and capacity usage ratio is high, superior product quality, and catalyst life is long.

Description

A kind of method that heavy benzene hydrogenation refines fuel oil
Technical field
The present invention relates to a kind of methods that technical field of petrochemical industry more particularly to heavy benzene hydrogenation refine fuel oil.
Background technology
Heavy benzol is the by-product of generation during crude benzole hydrogenation, is colourless to pale yellow oily liquid, there is similar chloroform Smell, density 0.960-0.990g/cm3 is not soluble in water, volatile, inflammable, toxic, can be most organic with benzene, ketone, ester, alcohol etc. Solvent is miscible.In crude benzole hydrogenation technical process, raw material crude benzol is separated in multi-stage evaporation device, high boiling component such as front three Benzene, naphthalene, indane, coumarone etc. are discharged as Residual oil from multi-stage evaporation device bottom, this part Residual oil is heavy benzol.
All using heavy benzol as raw fuel stock or solvent oil processing, only only a few enterprise is used for for most domestic producer at present Coumarone-indene resin is produced, because Petropols are more more competitive than coumarone indene resin in price and performance etc., and it is ancient The grand resin toxic of horse, is progressively substituted by Petropols.Further, since contain the heterocyclic compounds such as a certain amount of O, S, N in heavy benzol Object also has penetrating odor as solvent naphtha except stability difference is outer, and not only quality is not high during directly as fuel oil and pollution Environment, i.e., at present there is poor product quality, lack competitiveness or pollute environment in these purposes.Therefore, it is necessary to plus Strong heavy benzene hydrogenation purification techniques, the new utilization ways of exploitation heavy benzol, extends coal-coking-Fine Chemical Industry chain, and it is attached to increase product It is value added.
The content of the invention
For the above problem of the prior art, it is an object of the present invention to provide a kind of heavy benzene hydrogenations to refine fuel oil Method directly can carry out hydrotreating by counterweight benzene raw materials, promote the further utilization of coal tar, capacity usage ratio is high, product product Matter is good.
To solve the above-mentioned problems, technical scheme is as follows：
A kind of method that heavy benzene hydrogenation refines fuel oil, this method are that heavy benzol and hydrogen are separately added into the first hydrogenation reactor Pre-hydrotreating reaction is carried out, reaction product isolates benzene, toluene and dimethylbenzene, remaining ingredient is sent into evaporator into de- benzene unit In be vaporized, after the boil-off gas of evaporator outlet is mixed with hydrogen, preliminary hydrogenation is carried out into the second hydrogenation reactor Refining reaction, reaction product are sent into the 3rd hydrogenation reactor and carry out further hydrofining reaction, and reaction product carries out again Rectifying separates, and respectively obtains gasoline fraction and diesel oil distillate, wherein,
The operating condition of first hydrogenation reactor is：Pressure 4-5MPa, 120-150 DEG C of temperature, volume space velocity degree 0.5-3/ H, hydrogen to oil volume ratio 300-500:1；
The operating condition of second hydrogenation reactor is：Pressure 6-9MPa, 200-280 DEG C of temperature, volume space velocity 0.3-0.8/ H, hydrogen to oil volume ratio 300-800:1；
The operating condition of 3rd hydrogenation reactor is：Pressure 6-9MPa, 200-280 DEG C of temperature, volume space velocity 0.3-0.8/ H, hydrogen to oil volume ratio 300-800:1.
Further, the first catalyst bed is equipped in first hydrogenation reactor, first catalyst bed Catalyst is using Pd as active component, and Mo is auxiliary agent, γ-Al2O3For carrier, wherein, the load capacity of active component Pd is 3%-8%, Mo Load capacity for 1%-3%, and the weight ratio of Pd and Mo is 2:1~4:1.
Further, the second catalyst bed is equipped in second hydrogenation reactor, in the 3rd hydrogenation reactor Equipped with the 3rd catalyst bed, the catalyst of second catalyst bed and the 3rd catalyst bed is identical, the catalyst For with W2N active components, Fe are auxiliary agent, γ-Al2O3For carrier, wherein, active component W2The load capacity of N is 6% ~ 13%, auxiliary agent The load capacity of Fe is 0.5% ~ 5%, and W2The weight ratio of N and Fe is 1.5:1~5:1.
Further, the gasoline that the benzene,toluene,xylene that the de- benzene unit is isolated is isolated with the rectifying is evaporated Gasoline products are used as after split-phase mixing.
Further, recuperation of heat range site, the diesel oil that the rectifying is isolated are equipped with before first hydrogenation reactor Fraction heats the heavy benzol into first hydrogenation reactor in the recuperation of heat range site.
The method that a kind of heavy benzene hydrogenation of the present invention refines fuel oil, has the advantages that：
（1）The present invention directly carries out hydrogenation reaction by raw material of heavy benzol, simple for process without carrying out separating treatment to raw material, easily In control.
（2）The first hydrogenation reactor of the present invention carries out hydrotreating to the alkene in heavy benzol, can prevent subsequent process The polymerism of middle generation extends the service life of catalyst.
（3）The present invention by benzene, toluene and dimethylbenzene, was reacted in de- benzene unit so as to reduce the second hydrogenation reactor Hydrogen consumption in journey adds the octane number of gasoline fraction.
（4）The remaining ingredient of de- benzene unit is first sent into evaporator vaporization by the present invention, and after boil-off gas is mixed with hydrogen The second hydrogenation reactor is re-fed into, due to being homogeneous reaction in the second hydrogenation reactor（It is gas phase）, so as to greatly improve The yield of product, reduces reaction temperature.Further, since the boil-off gas temperature of evaporator outlet has reached the second hydrogenation reaction Reaction temperature in device the step of so as to save to being heated into the raw material of the second hydrogenation reactor, reduces and is The whole energy consumption of system, capacity usage ratio is high, and superior product quality simplifies technique.
（5）The present invention is equipped with recuperation of heat range site before the first hydrogenation reactor, sufficiently rectifying make use of to isolate Diesel oil distillate heat, improve capacity usage ratio.
（6）The present invention uses three sections of hydrogenation reactions on the whole so that the liquid phase pre-hydrotreating reaction in the first hydrogenation reactor Can the alkene in heavy benzol be subjected to saturated process, subsequent preliminary hydrofining reaction and hydrofinishing at a lower temperature Reaction extends hydrogenation process, not only ensure that sour gas field reacts at a lower temperature, but also product Quality greatly improves.
Description of the drawings
It, below will be to required in embodiment or description of the prior art in order to illustrate more clearly of technical scheme The attached drawing used is briefly described.It should be evident that the accompanying drawings in the following description is only some embodiments of the present invention, it is right For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings Its attached drawing.
Fig. 1 is the FB(flow block) for the method that a kind of heavy benzene hydrogenation provided by the invention refines fuel oil；
In figure：The first hydrogenation reactors of 1-, 2- take off benzene unit, and 3- evaporators, the second hydrogenation reactors of 4-, 5- recuperations of heat utilize single Member, the 3rd hydrogenation reactors of 6-.
Specific embodiment
Below in conjunction with the attached drawing in the embodiment of the present invention, the technical solution in the embodiment of the present invention is carried out clear, complete Site preparation describes, it is clear that described embodiment is only part of the embodiment of the present invention, instead of all the embodiments.It is based on Embodiment in the present invention, those of ordinary skill in the art obtained on the premise of creative work is not made it is all its His embodiment, belongs to the scope of protection of the invention.
The present invention provides a kind of method that heavy benzene hydrogenation refines fuel oil, as shown in Figure 1, this method is by heavy benzol and hydrogen Be separately added into the first hydrogenation reactor 1 and carry out pre-hydrotreating reaction, reaction product into de- benzene unit 2, isolate benzene, toluene and Dimethylbenzene, remaining ingredient are sent into evaporator 3 and are vaporized, after the boil-off gas that evaporator 3 exports is mixed with hydrogen, into second Preliminary hydrofining reaction is carried out in hydrogenation reactor 4, reaction product is sent into the 3rd hydrogenation reactor 6 and is carried out further Hydrofining reaction, reaction product carry out rectifying separation, respectively obtain gasoline fraction and diesel oil distillate again.The gasoline fraction with from As gasoline products after the benzene,toluene,xylene mixing that de- benzene unit 2 is isolated.Heat is equipped with before the first hydrogenation reactor 1 to return Range site 5 is received, the diesel oil distillate that the rectifying is isolated is in the recuperation of heat range site 5 to anti-into the described first hydrogenation The heavy benzol of device 1 is answered to be heated.
Wherein, the operating condition of first hydrogenation reactor is：Pressure 4-5MPa, 120-150 DEG C of temperature, volume space velocity Spend 0.5-3/h, hydrogen to oil volume ratio 300-500:1；The operating condition of second hydrogenation reactor is：Pressure 6-9MPa, temperature 200-280 DEG C, volume space velocity 0.3-0.8/h, hydrogen to oil volume ratio 300-800:1；The operating condition of 3rd hydrogenation reactor For：Pressure 6-9MPa, 200-280 DEG C of temperature, volume space velocity 0.3-0.8/h, hydrogen to oil volume ratio 300-800:1.Described first adds The first catalyst bed is equipped in hydrogen reactor, for the catalyst of first catalyst bed using Pd as active component, Mo is to help Agent, γ-Al2O3For carrier, wherein, the load capacity of active component Pd is 3%-8%, and the load capacity of Mo is 1%-3%, and Pd and Mo Weight ratio is 2:1~4:1.The second catalyst bed is equipped in second hydrogenation reactor, is set in the 3rd hydrogenation reactor There is the 3rd catalyst bed, the catalyst of second catalyst bed and the 3rd catalyst bed is identical, and the catalyst is With W2N active components, Fe are auxiliary agent, γ-Al2O3For carrier, wherein, active component W2The load capacity of N is 6% ~ 13%, auxiliary agent Fe Load capacity for 0.5% ~ 5%, and W2The weight ratio of N and Fe is 1.5:1~5:1.
In order to further illustrate the heavy benzene hydrogenation process for refining of the present invention, illustrated below with specific embodiment, certainly The present invention and from the limitation of the following example.
Embodiment 1
First catalyst bed is set in the first hydrogenation reactor, and the catalyst of first catalyst bed is：3%Pd-1%Mo/ γ-Al2O3.Second catalyst bed is set in the second hydrogenation reactor, and the catalyst of second catalyst bed is：6%W2N- 2%Fe/γ-Al2O3.3rd catalyst bed is set in the 3rd hydrogenation reactor, and the catalyst of the 3rd catalyst bed is：6% W2N-2%Fe/γ-Al2O3。
The operating condition of first hydrogenation reactor is：Pressure 4MPa, 120 DEG C of temperature, volume space velocity degree 1/h, hydrogen oil volume Than 300:1.The operating condition of second hydrogenation reactor is：Pressure 6MPa, 200 DEG C, volume space velocity 0.3/h of temperature, hydrogen oil volume Than 300:1.The operating condition of 3rd hydrogenation reactor is：Pressure 6MPa, 200 DEG C, volume space velocity 0.3/h of temperature, hydrogen oil volume Than 300:1.Evaporator outlet temperature is 150 DEG C.Evaporator outlet temperature is 220 DEG C.
After testing, after hydrogenation reaction, the sulfur contents of gasoline products is 19ppm, nitrogen content 20ppm, and oxygen content is 15ppm, the octane number of gasoline products reach 98.2.The sulfur content of diesel product is 52ppm, nitrogen content 82ppm, and oxygen content is 15ppm, the Cetane number of diesel product reach 53.
Embodiment 2
First catalyst bed is set in the first hydrogenation reactor, and the catalyst of first catalyst bed is：4%Pd-1%Mo/ γ-Al2O3.Second catalyst bed is set in the second hydrogenation reactor, and the catalyst of second catalyst bed is：8%W2N- 4%Fe/γ-Al2O3.3rd catalyst bed is set in the 3rd hydrogenation reactor, and the catalyst of the 3rd catalyst bed is：8% W2N-4%Fe/γ-Al2O3。
The operating condition of first hydrogenation reactor is：Pressure 4MPa, 140 DEG C of temperature, volume space velocity degree 2/h, hydrogen oil volume Than 400:1.The operating condition of second hydrogenation reactor is：Pressure 8MPa, 250 DEG C, volume space velocity 0.5/h of temperature, hydrogen oil volume Than 500:1.The operating condition of 3rd hydrogenation reactor is：Pressure 8MPa, 250 DEG C, volume space velocity 0.5/h of temperature, hydrogen oil volume Than 500:1.Evaporator outlet temperature is 250 DEG C.
After testing, after hydrogenation reaction, the sulfur contents of gasoline products is 17ppm, nitrogen content 18ppm, and oxygen content is 13ppm, the octane number of gasoline products reach 99.1.The sulfur content of diesel product is 48ppm, nitrogen content 79ppm, and oxygen content is 13ppm, the Cetane number of diesel product reach 56.
Embodiment 3
First catalyst bed is set in the first hydrogenation reactor, and the catalyst of first catalyst bed is：8%Pd-3%Mo/ γ-Al2O3.Second catalyst bed is set in the second hydrogenation reactor, and the catalyst of second catalyst bed is：10%W2N- 5%Fe/γ-Al2O3.3rd catalyst bed is set in the 3rd hydrogenation reactor, and the catalyst of the 3rd catalyst bed is： 10%W2N-5%Fe/γ-Al2O3。
The operating condition of first hydrogenation reactor is：Pressure 5MPa, 150 DEG C of temperature, volume space velocity degree 3/h, hydrogen oil volume Than 500:1.The operating condition of second hydrogenation reactor is：Pressure 9MPa, 280 DEG C, volume space velocity 0.8/h of temperature, hydrogen oil volume Than 800:1.The operating condition of 3rd hydrogenation reactor is：Pressure 9MPa, 280 DEG C, volume space velocity 0.8/h of temperature, hydrogen oil volume Than 800:1.Evaporator outlet temperature is 290 DEG C.
After testing, after hydrogenation reaction, the sulfur contents of gasoline products is 20ppm, nitrogen content 22ppm, and oxygen content is 17ppm, the octane number of gasoline products reach 97.The sulfur content of diesel product is 54ppm, nitrogen content 86ppm, and oxygen content is 17ppm, the Cetane number of diesel product reach 52.
In summary, a kind of heavy benzene hydrogenation process for refining of the invention, has the advantages that：
（1）The present invention directly carries out hydrogenation reaction by raw material of heavy benzol, simple for process without carrying out separating treatment to raw material, easily In control.
（2）The first hydrogenation reactor of the present invention carries out hydrotreating to the alkene in heavy benzol, can prevent subsequent process The polymerism of middle generation extends the service life of catalyst.
（3）The present invention by benzene, toluene and dimethylbenzene, was reacted in de- benzene unit so as to reduce the second hydrogenation reactor Hydrogen consumption in journey adds the octane number of gasoline fraction.
（4）The remaining ingredient of de- benzene unit is first sent into evaporator vaporization by the present invention, and after boil-off gas is mixed with hydrogen The second hydrogenation reactor is re-fed into, due to being homogeneous reaction in the second hydrogenation reactor（It is gas phase）, so as to greatly improve The yield of product, reduces reaction temperature.Further, since the boil-off gas temperature of evaporator outlet has reached the second hydrogenation reaction Reaction temperature in device the step of so as to save to being heated into the raw material of the second hydrogenation reactor, reduces and is The whole energy consumption of system, capacity usage ratio is high, and superior product quality simplifies technique.
（5）The present invention is equipped with recuperation of heat range site before the first hydrogenation reactor, sufficiently rectifying make use of to isolate Diesel oil distillate heat, improve capacity usage ratio.
（6）The present invention uses three sections of hydrogenation reactions on the whole so that the liquid phase pre-hydrotreating reaction in the first hydrogenation reactor Can the alkene in heavy benzol be subjected to saturated process, subsequent preliminary hydrofining reaction and hydrofinishing at a lower temperature Reaction extends hydrogenation process, not only ensure that sour gas field reacts at a lower temperature, but also product Quality greatly improves.
Above description has fully disclosed the specific embodiment of the present invention.It is pointed out that it is familiar with the field Technical staff is to any change that the specific embodiment of the present invention is done all without departing from the scope of claims of the present invention. Correspondingly, the scope of claim of the invention is also not limited only to previous embodiment.

Claims (5)

1. a kind of method that heavy benzene hydrogenation refines fuel oil, which is characterized in that this method is that heavy benzol and hydrogen are separately added into Pre-hydrotreating reaction is carried out in one hydrogenation reactor, reaction product isolates benzene, toluene and dimethylbenzene, residue into de- benzene unit Component is sent into evaporator and is vaporized, after the boil-off gas of evaporator outlet is mixed with hydrogen, into the second hydrogenation reactor Preliminary hydrofining reaction is carried out, reaction product is sent into the 3rd hydrogenation reactor and carries out further hydrofining reaction, Reaction product carries out rectifying separation again, respectively obtains gasoline fraction and diesel oil distillate, wherein,
The operating condition of first hydrogenation reactor is：Pressure 4-5MPa, 120-150 DEG C of temperature, volume space velocity degree 0.5-3/ H, hydrogen to oil volume ratio 300-500:1；
The operating condition of second hydrogenation reactor is：Pressure 6-9MPa, 200-280 DEG C of temperature, volume space velocity 0.3-0.8/ H, hydrogen to oil volume ratio 300-800:1；
The operating condition of 3rd hydrogenation reactor is：Pressure 6-9MPa, 200-280 DEG C of temperature, volume space velocity 0.3-0.8/ H, hydrogen to oil volume ratio 300-800:1.
2. the method that a kind of heavy benzene hydrogenation according to claim 1 refines fuel oil, which is characterized in that first hydrogenation The first catalyst bed is equipped in reactor, for the catalyst of first catalyst bed using Pd as active component, Mo is auxiliary agent, γ-Al2O3For carrier, wherein, the load capacity of active component Pd is 3%-8%, and the load capacity of Mo is 1%-3%, and the weight of Pd and Mo Than for 2:1~4:1.
3. the method that a kind of heavy benzene hydrogenation according to claim 1 refines fuel oil, which is characterized in that second hydrogenation The second catalyst bed is equipped in reactor, is equipped with the 3rd catalyst bed in the 3rd hydrogenation reactor, described second urges The catalyst of agent bed and the 3rd catalyst bed is identical, and the catalyst is with W2N active components, Fe are auxiliary agent, γ- Al2O3For carrier, wherein, active component W2The load capacity of N is 6% ~ 13%, and the load capacity of auxiliary agent Fe is 0.5% ~ 5%, and W2N and Fe Weight ratio be 1.5:1~5:1.
4. the method that a kind of heavy benzene hydrogenation according to claim 1 refines fuel oil, which is characterized in that by the de- benzene list The benzene,toluene,xylene that member is isolated is used as gasoline products after being mixed with the gasoline fraction that the rectifying is isolated.
5. the method that a kind of heavy benzene hydrogenation according to claim 1 refines fuel oil, which is characterized in that first hydrogenation Recuperation of heat range site is equipped with before reactor, the diesel oil distillate that the rectifying is isolated is in the recuperation of heat range site to entering The heavy benzol of first hydrogenation reactor is heated.
CN201711361513.5A 2017-12-18 2017-12-18 A kind of method that heavy benzene hydrogenation refines fuel oil Pending CN108085059A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108659882A (en) * 2018-05-16 2018-10-16 煤炭科学技术研究院有限公司 A kind of Heavy oil hydrogenation method and its hydrogenation system

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104774648A (en) * 2015-03-18 2015-07-15 大连理工大学 Heavy benzol hydrofining method of clean fuel oil
CN107365241A (en) * 2017-06-28 2017-11-21 徐州东兴能源有限公司 A kind of crude benzole hydrogenation process for refining

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104774648A (en) * 2015-03-18 2015-07-15 大连理工大学 Heavy benzol hydrofining method of clean fuel oil
CN107365241A (en) * 2017-06-28 2017-11-21 徐州东兴能源有限公司 A kind of crude benzole hydrogenation process for refining

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108659882A (en) * 2018-05-16 2018-10-16 煤炭科学技术研究院有限公司 A kind of Heavy oil hydrogenation method and its hydrogenation system
CN108659882B (en) * 2018-05-16 2020-05-12 煤炭科学技术研究院有限公司 Heavy oil hydrogenation method and hydrogenation system thereof

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Application publication date: 20180529