CN106753612B - A kind of jet fuel high density composite oil - Google Patents
A kind of jet fuel high density composite oil Download PDFInfo
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- CN106753612B CN106753612B CN201611228384.8A CN201611228384A CN106753612B CN 106753612 B CN106753612 B CN 106753612B CN 201611228384 A CN201611228384 A CN 201611228384A CN 106753612 B CN106753612 B CN 106753612B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2270/00—Specifically adapted fuels
- C10L2270/04—Specifically adapted fuels for turbines, planes, power generation
Abstract
A kind of jet fuel high density composite oil, including high-density propellant blend component, the high-density propellant blend component is the cycloalkane and aromatic hydrocarbons that are 300 DEG C of 180 ﹣ as raw material, by the boiling range that hydrofinishing obtains using inferior heavy oil and tail oil part, the physicochemical property of high-density propellant blend component meets the standard of RP-3 jet fuel, and its density is 960 ﹣ 980kg/m3, the base oil that can be used as high density liquid jet fuel also can be used as the dense additive use of jet fuel, and production cost is low.
Description
Technical field
The invention belongs to field of aviation fuel, and in particular to a kind of jet fuel high density composite oil, the compound oil was both
The base oil that can be used as high density liquid jet fuel is used but also as the dense additive of jet fuel.
Background technique
Jet fuel, that is, jet fuel, also known as aviation turbine fuel are a kind of oils, are widely used in
Various jet airplane.Jet fuel is mainly processed by the kerosene distillate of crude distillation through purification, is additionally added additive sometimes and is made,
It can also be produced by the hydrogenated cracking of heavy distillate of crude distillation.Divide long distillate type (280 DEG C of 60 ﹣ of boiling point) and kerosene type (boiling
315 DEG C of 150 ﹣ of point) two major classes.There are strict requirements for the quality of jet fuel, primary quality measure are as follows: 1. volume calorific value refers to list
The net heat discharged when the volumetric fuei completely burned of position is the product of quality of fuel calorific value and its density.Strictly speaking, it
It is just marginal to the petroleum fuel for guided missile (Ramjet Missile and cruise missile).Voyage of the volume calorific value to aircraft
Significant, the big expression voyage of value can also be remote.Improving fuel density is to increase the most effective approach of its volume calorific value.
2. freezing point, one of the important indicator of fuel cryogenic property refer to that fuel forms hydro carbons crystallization while cooling and disappears when heated
Temperature.Jet fuel require freezing point it is low, to the fuel of high-altitude flying for long time should lower than -50 DEG C (short flight can
Not higher than -40 DEG C).3. density, the higher the better for density, the big fuel of volume calorific value is traditionally also known as high-density propellant.4. virtue
Hydrocarbon content is not more than 25% (quality).5. fuel wants clean, thermal stability will be got well.
Currently, High-Density Jet is the hot spot of various countries' research.With the military service successively of China's high performance airplane, to height
Density, the demand of high performance jet fuel are also more and more urgent, and jet fuel used in China is main or RP-3, close
Degree (20 DEG C) highest only reaches 830kg/m3, therefore, develop high density, low cost jet fuel and have a very important significance.
Summary of the invention
The purpose of the present invention is overcoming the problems, such as that the density of existing jet fuel is lower, providing one kind can not only be used for high density
The base oil of liquid jet, the jet fuel high density composite that uses of dense additive but also as jet fuel
Oil.
In order to achieve the above object, the present invention provides following technical schemes:
A kind of jet fuel high density composite oil, raw material composition includes high-density propellant blend component, the high density
Fuel blend component is the cycloalkane and virtue for being 300 DEG C of 180 ﹣ as raw material, by the boiling range that hydrofinishing obtains using inferior heavy oil
Hydrocarbon and tail oil part, the physicochemical property of high-density propellant blend component meets the standard of RP-3 jet fuel, and its density is
960 ﹣ 980kg/m3。
The high density distiller liquor component is successively prepared using following technique:
One, first inferior heavy oil is put into No.1 atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil and catalyst are mixed to get mixture；
Two, first the mixture is mixed with hydrogen, then is heated to be placed in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in No.1 thermal high knockout drum, then
Bottom product in bottom product and No.1 thermal high knockout drum in catalytic hydroprocessing cracking reactor is put into togerther No.1 heat
Heat low separation is carried out in low pressure separation pot；
Three, heat low separation after the completion of, first by the bottom product in No.1 heat low knockout drum be placed in vacuum fractionation tower into
Row vacuum fractionation, then distillate, No.1 atmospheric fractional tower top and the side line product that vacuum fractionation tower side line obtains are placed in admittedly
It is reacted in fixed bed finishing reactor, after the reaction was completed, the bottom product in fixed bed finishing reactor is put into No. two heat
It is separated in high pressure knockout drum；
Four, after the completion of separating, the gas being discharged at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and is carried out
Separation, and the bottom product in No. two thermal high knockout drums is put into No. two heat low knockout drums, then cold anticyclone is separated
The bottom of tank, which condenses oil product and is placed in cold low separator, to be separated, then the bottom of cold low separator is condensed oil product and is placed in
Stripper；
Five, the bottom product in the bottom product and No. two heat low knockout drums in stripper is put into No. two normal pressure fractionation
Tower carries out normal pressure fractionation, and the side line lower part product of No. two atmospheric fractional towers is high-density propellant blend component.
The inferior heavy oil is at least one of coal tar, ethylene bottom oil, catalytic slurry.
In technique one, the catalyst is the molybdenum nickel oil solvent catalyst that molybdenum nickel mass ratio is 1: 4 ﹣ 4: 1, and the molybdenum nickel oil is molten
The dosage of agent catalyst is 0.01% ﹣ 0.05% of hydrogen.
The reaction condition for facing hydrogen cracking reactor are as follows:
10 ﹣ 23MPa of reaction pressure, 470 DEG C of 430 ﹣ of reaction temperature, 0.3 ﹣ 1.5h of combined feed volume space velocity-1, hydrogen to oil volume ratio
800 ﹣ 1200；
The reaction condition of the fixed bed finishing reactor are as follows:
10 ﹣ 20MPa of reaction pressure, reaction temperature are 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen oil body
Product 500 ﹣ 1200 of ratio.
In the fixed bed finishing reactor contain hydro-upgrading catalyst converter, the hydro-upgrading catalyst converter be by Co, Mo,
2 kinds in Ni, W metal or 3 kinds of Metal Supporteds are in Al2O3On catalyst, total metal mass be the total matter of catalyst for hydro-upgrading
20% ﹣ 40% of amount.
Bottoms material in the vacuum fractionation tower is outer whipping oil solid fuel, the top product gas in the stripper
State and liquid hydrocarbon, for the top product in No. two atmospheric fractional towers as reformer feed, side line top product is aviation kerosine,
Bottom product is catalytically cracked material.
In technique four, the gas being discharged by the cold anticyclone knockout drum top is successively after desulfurization process, circulation hydrogen compressed
It mixes with hydrogen, is then mixed with mixture.
The compound oil raw material composition further include in 2,6-di-tert-butyl p-cresol BHT, dimethyl carbonate DMC at least
It is a kind of.
Compared with prior art, the invention has the benefit that
1, a kind of raw material composition of jet fuel high density composite oil of the present invention includes high-density propellant blend component, should
High-density propellant blend component is the cycloalkanes for being 300 DEG C of 180 ﹣ as raw material, by the boiling range that hydrofinishing obtains using inferior heavy oil
Hydrocarbon and aromatic hydrocarbons and tail oil part, density are 960 ﹣ 980kg/m3, on the one hand, the high-density propellant blend component can be used as
The dense additive of high density liquid jet fuel base oil or jet fuel uses, and application range is wider, and its sulphur contains
Amount is no more than 5ppm, very environmentally friendly, and on the other hand, the production cost of compound oil is far below existing jet fuel production cost.
Therefore, the present invention can be used as high density liquid jet fuel base oil or the dense additive of jet fuel uses, and
And environmental protection, production cost it is low.
2, a kind of preparation process of jet fuel high density composite oil middle-high density fuel blend component of the present invention passes through
The reaction condition of catalytic hydroprocessing cracking is controlled, so that entire preparation process conversion ratio with higher, by limiting catalytic hydroprocessing
The catalyst of cracking reaction can inhibit feedstock oil green coke during the reaction, guarantee the long-term operation of device, the original of this method
Expect adaptable, byproduct passes through hydrofinishing, and property is excellent, use value with higher.Therefore, the present invention prepares work
Not only yield and product use value are high for skill, but also make the service life of device long.
Detailed description of the invention
Fig. 1 is the preparation technology flow chart of middle-high density fuel blend component of the present invention.
Specific embodiment
The invention will be further described With reference to embodiment.
A kind of jet fuel high density composite oil, raw material composition includes high-density propellant blend component, the high density
Fuel blend component is the cycloalkane and virtue for being 300 DEG C of 180 ﹣ as raw material, by the boiling range that hydrofinishing obtains using inferior heavy oil
Hydrocarbon and tail oil part, the physicochemical property of high-density propellant blend component meets the standard of RP-3 jet fuel, and its density is
960 ﹣ 980kg/m3。
Referring to Fig. 1, the high density distiller liquor is successively prepared using following technique:
One, first inferior heavy oil is put into No.1 atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil and catalyst are mixed to get mixture；
Two, first the mixture is mixed with hydrogen, then is heated to be placed in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in No.1 thermal high knockout drum, then
Bottom product in bottom product and No.1 thermal high knockout drum in catalytic hydroprocessing cracking reactor is put into togerther No.1 heat
Heat low separation is carried out in low pressure separation pot；
Three, heat low separation after the completion of, first by the bottom product in No.1 heat low knockout drum be placed in vacuum fractionation tower into
Row vacuum fractionation, then distillate, No.1 atmospheric fractional tower top and the side line product that vacuum fractionation tower side line obtains are placed in admittedly
It is reacted in fixed bed finishing reactor, after the reaction was completed, the bottom product in fixed bed finishing reactor is put into No. two heat
It is separated in high pressure knockout drum；
Four, after the completion of separating, the gas being discharged at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and is carried out
Separation, and the bottom product in No. two thermal high knockout drums is put into No. two heat low knockout drums, then cold anticyclone is separated
The bottom of tank, which condenses oil product and is placed in cold low separator, to be separated, then the bottom of cold low separator is condensed oil product and is placed in
Stripper；
Five, the bottom product in the bottom product and No. two heat low knockout drums in stripper is put into No. two normal pressure fractionation
Tower carries out normal pressure fractionation, and the side line lower part product of No. two atmospheric fractional towers is high-density propellant blend component.
The inferior heavy oil is at least one of coal tar, ethylene bottom oil, catalytic slurry.
In technique one, the catalyst is the molybdenum nickel oil solvent catalyst that molybdenum nickel mass ratio is 1: 4 ﹣ 4: 1, and the molybdenum nickel oil is molten
The dosage of agent catalyst is 0.01% ﹣ 0.05% of hydrogen.
The reaction condition for facing hydrogen cracking reactor are as follows:
10 ﹣ 23MPa of reaction pressure, 470 DEG C of 430 ﹣ of reaction temperature, 0.3 ﹣ 1.5h of combined feed volume space velocity-1, hydrogen to oil volume ratio
800 ﹣ 1200；
The reaction condition of the fixed bed finishing reactor are as follows:
10 ﹣ 20MPa of reaction pressure, reaction temperature are 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen oil body
Product 500 ﹣ 1200 of ratio.
In the fixed bed finishing reactor contain hydro-upgrading catalyst converter, the hydro-upgrading catalyst converter be by Co, Mo,
2 kinds in Ni, W metal or 3 kinds of Metal Supporteds are in Al2O3On catalyst, total metal mass be the total matter of catalyst for hydro-upgrading
20% ﹣ 40% of amount.
Bottoms material in the vacuum fractionation tower is outer whipping oil solid fuel, the top product gas in the stripper
State and liquid hydrocarbon, for the top product in No. two atmospheric fractional towers as reformer feed, side line top product is aviation kerosine,
Bottom product is catalytically cracked material.
In technique four, the gas being discharged by the cold anticyclone knockout drum top is successively after desulfurization process, circulation hydrogen compressed
It mixes with hydrogen, is then mixed with mixture.
The compound oil raw material composition further include in 2,6-di-tert-butyl p-cresol BHT, dimethyl carbonate DMC at least
It is a kind of.
The principle of the present invention is described as follows:
The present invention provides a kind of jet fuel high density composite oil, when the compound oil is fired as high density liquid jet
The base oil of material, can will be close in use, add a certain amount of more highdensity artificial synthesized solid or liquid additive again
Degree increases to 1.1 ﹣ 1.3kg/m3, become for hypersonic plane, cruise missile, rocket High-Density Jet.When this
Compound oil as jet fuel dense additive in use, such as compounded with RP-3 jet fuel, density can be from
830kg/m3Increase to 950kg/m3More than, coal oil compounding is synthesized with F-T, density can be from 746kg/m3Increase to 940kg/
m3More than.Meanwhile BHT and/or DMC can be also added in the compound oil, the thermal oxidation stability and ring of fuel can be effectively improved
Guaranteed cost.
The all technical of high density composite oil of the present invention
In preparation process of the present invention, contain catalyst for hydro-upgrading in fixed bed finishing reactor, the hydro-upgrading
Catalyst can promote the fraction not less than 370 DEG C that cracking reaction occurs, and reduce the fraction less than 370 DEG C and cracking reaction occurs.
Inferior heavy oil of the present invention originates from the Inner Mongol, and related physicochemical property is shown in Table 1:
The physicochemical property of 1 inferior heavy oil of table
| Project | Coal tar | Ethylene bottom oil | Catalytic slurry |
| Density (20 DEG C), gcm-3 | 1.2150 | 1.0500 | 1.0800 |
| Kinematic viscosity (40 DEG C), mm2·s-1 | 115.0 | 44.2 | 127.0 |
| S content, w% | 0.33 | 0.40 | 0.70 |
| N content, w% | 0.93 | 0.07 | 1.20 |
| C content, w% | 88.36 | 91.64 | 91.20 |
| H content, w% | 5.92 | 7.47 | 6.90 |
| Carbon residue, w% | 20.50 | 12.00 | 9.60 |
| Ash content, w% | 0.12 | 0.0005 | 0.21 |
| 350 DEG C of < | 42.01 | 66.50 | 10.20 |
| 350 DEG C of > | 57.99 | 33.50 | 89.80 |
| Saturation point | 25.03 | 17.24 | 27.60 |
| Fragrance point | 28.42 | 53.25 | 66.20 |
| Colloid | 18.01 | 10.82 | 5.60 |
| Asphalitine | 28.54 | 18.69 | 0.60 |
Embodiment 1:
Referring to Fig. 1, a kind of High-Density Jet compound oil presses 98.8 by high-density propellant blend component, BHT, DMC:
0.2: 1 mass ratio mixes, wherein the high-density propellant blend component is using inferior heavy oil as raw material, by adding hydrogen
The cycloalkane and aromatic hydrocarbons and tail oil part that the boiling range being refining to obtain is 300 DEG C of 180 ﹣, density is 960 ﹣ 980kg/m3, specific to make
Standby technique are as follows:
One, first inferior heavy oil is put into No.1 atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil and catalyst are mixed to get mixture, wherein the inferior heavy oil is coal tar, and the catalyst is molybdenum nickel mass ratio
It is 1: 4 molybdenum nickel oil solvent catalyst, the dosage of the molybdenum nickel oil solvent catalyst is the 0.015% of hydrogen；
Two, first the mixture is mixed with hydrogen, then is heated to be placed in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in No.1 thermal high knockout drum, then
Bottom product in bottom product and No.1 thermal high knockout drum in catalytic hydroprocessing cracking reactor is put into togerther No.1 heat
Heat low separation is carried out in low pressure separation pot, wherein the reaction condition for facing hydrogen cracking reactor are as follows:
Reaction pressure 10MPa, 430 DEG C of reaction temperature, combined feed volume space velocity 0.3h-1, hydrogen to oil volume ratio 1000；
Three, heat low separation after the completion of, first by the bottom product in No.1 heat low knockout drum be placed in vacuum fractionation tower into
Row vacuum fractionation, then distillate, No.1 atmospheric fractional tower top and the side line product that vacuum fractionation tower side line obtains are placed in admittedly
It is reacted in fixed bed finishing reactor, after the reaction was completed, the bottom product in fixed bed finishing reactor is put into No. two heat
It is separated in high pressure knockout drum, wherein the bottoms material in the vacuum fractionation tower is outer whipping oil solid fuel, described solid
Contain hydro-upgrading catalyst converter in fixed bed finishing reactor, which is Mo-Ni/Al2O3Hydro-upgrading catalysis
Agent, active metal quality is the 25% of catalyst for hydro-upgrading gross mass, and the reaction condition of fixed bed finishing reactor are as follows:
Reaction pressure 10MPa, reaction temperature are 280 DEG C, and combined feed volume space velocity is 1.0h-1, hydrogen to oil volume ratio 500；
Four, after the completion of separating, the gas being discharged at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and is carried out
Separation, and the bottom product in No. two thermal high knockout drums is put into No. two heat low knockout drums, then cold anticyclone is separated
The bottom of tank, which condenses oil product and is placed in cold low separator, to be separated, then the bottom of cold low separator is condensed oil product and is placed in
Stripper, wherein by the gas that is discharged at the top of the cold anticyclone knockout drum successively after desulfurization process, circulation hydrogen compressed with hydrogen
Mixing, then mixes with mixture；
Five, the bottom product in the bottom product and No. two heat low knockout drums in stripper is put into No. two normal pressure fractionation
Tower carries out normal pressure fractionation, and the side line lower part product of No. two atmospheric fractional towers is high-density propellant blend component, wherein described
Top product gaseous state and liquid hydrocarbon in stripper, the top product in No. two atmospheric fractional towers is as reformer feed, side
Line top product is aviation kerosine, and bottom product is catalytically cracked material.
Embodiment 2:
Step with embodiment 1, the difference is that:
In the technique one, inferior heavy oil is ethylene bottom oil, and catalyst is urged for the molybdenum nickel oil solvent that molybdenum nickel mass ratio is 1: 1
Agent, the dosage of the molybdenum nickel oil solvent catalyst are the 0.02% of hydrogen；
In the technique two, face the reaction condition of hydrogen cracking reactor are as follows:
Reaction pressure 16MPa, 445 DEG C of reaction temperature, combined feed volume space velocity 1.0h-1, hydrogen to oil volume ratio 800；
In the technique three, hydro-upgrading catalyst converter is Co-Ni/Al2O3Catalyst for hydro-upgrading, active metal quality
It is the 30% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor are as follows:
Reaction pressure 15MPa, reaction temperature are 330 DEG C, and combined feed volume space velocity is 0.6h-1, hydrogen to oil volume ratio 800.
Embodiment 3:
In the technique one, inferior heavy oil is catalytic slurry, and catalyst is urged for the molybdenum nickel oil solvent that molybdenum nickel mass ratio is 4: 1
Agent, the dosage of the molybdenum nickel oil solvent catalyst are the 0.04% of hydrogen；
In the technique two, face the reaction condition of hydrogen cracking reactor are as follows:
Reaction pressure 23MPa, 470 DEG C of reaction temperature, combined feed volume space velocity 1.5h-1, hydrogen to oil volume ratio 1200；
In the technique three, hydro-upgrading catalyst converter is Co-W/Al2O3Catalyst for hydro-upgrading, active metal quality are
The 40% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor are as follows:
Reaction pressure 20MPa, reaction temperature are 400 DEG C, and combined feed volume space velocity is 2.0h-1, hydrogen to oil volume ratio 800.
Embodiment 4:
Step with embodiment 1, the difference is that:
In the technique one, inferior heavy oil is catalytic slurry, and catalyst is urged for the molybdenum nickel oil solvent that molybdenum nickel mass ratio is 2 ﹕ 1
Agent, the dosage of the molybdenum nickel oil solvent catalyst are the 0.035% of hydrogen；
In the technique two, face the reaction condition of hydrogen cracking reactor are as follows:
Reaction pressure 14MPa, 440 DEG C of reaction temperature, combined feed volume space velocity 0.6h-1, hydrogen to oil volume ratio 1100；
In the technique three, hydro-upgrading catalyst converter is Co-Ni-W/Al2O3Catalyst for hydro-upgrading, active metal matter
Amount is the 23% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor are as follows:
Reaction pressure 13MPa, reaction temperature are 300 DEG C, and combined feed volume space velocity is 0.8h-1, hydrogen to oil volume ratio 1000.
Embodiment 5:
Step with embodiment 1, the difference is that:
In the technique one, inferior heavy oil is ethylene bottom oil, and catalyst is urged for the molybdenum nickel oil solvent that molybdenum nickel mass ratio is 1: 2
Agent, the dosage of the molybdenum nickel oil solvent catalyst are the 0.05% of hydrogen；
In the technique two, face the reaction condition of hydrogen cracking reactor are as follows:
Reaction pressure 20MPa, 460 DEG C of reaction temperature, combined feed volume space velocity 1.2h-1, hydrogen to oil volume ratio 900；
In the technique three, hydro-upgrading catalyst converter is Mo-Ni-W/Al2O3Catalyst for hydro-upgrading, active metal matter
Amount is the 20% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor are as follows:
Reaction pressure 17MPa, reaction temperature are 360 DEG C, and combined feed volume space velocity is 1.5h-1, hydrogen to oil volume ratio 700.
The density and net heating value data of the high-density propellant blend component obtained using above-described embodiment are referring to table 3:
The density and net heating value of 3 high-density propellant blend component of table
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Density kg/m3 | 967 | 978 | 960 | 971 | 980 |
| Net heating value MJ/kg | 44.3 | 44.6 | 44.0 | 43.8 | 44.8 |
Claims (8)
1. a kind of jet fuel high density composite oil, it is characterised in that:
The raw material composition of the compound oil includes high-density propellant blend component, which is with inferior heavy
Oil be raw material, be 300 DEG C of 180 ﹣ by the boiling range that hydrofinishing obtains cycloalkane and aromatic hydrocarbons and tail oil part, high-density propellant
The physicochemical property of blend component meets the standard of RP-3 jet fuel, and its density is 960 ﹣ 980kg/m3；
The high-density propellant blend component is successively prepared using following technique:
One, first inferior heavy oil is put into No.1 atmospheric fractional tower to obtain light fraction and reduced crude, then by the normal pressure slag
Oil is mixed to get mixture with catalyst；
Two, first the mixture is mixed with hydrogen, then is heated to be placed in catalytic hydroprocessing cracking reactor and reacts, then
Top product in catalytic hydroprocessing cracking reactor is placed in progress thermal high separation in No.1 thermal high knockout drum, will then be faced
The bottom product in bottom product and No.1 thermal high knockout drum in hydrogen catalysis cracking reactor is put into togerther No.1 heat low
Heat low separation is carried out in knockout drum；
Three, after the completion of heat low separation, the bottom product in No.1 heat low knockout drum is first placed in vacuum fractionation tower and is subtracted
Pressure fractionating, then distillate, No.1 atmospheric fractional tower top and the side line product that vacuum fractionation tower side line obtains are placed in fixed bed
It is reacted in finishing reactor, after the reaction was completed, the bottom product in fixed bed finishing reactor is put into No. two thermal highs
It is separated in knockout drum；
Four, after the completion of separating, the gas being discharged at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and is separated,
And the bottom product in No. two thermal high knockout drums is put into No. two heat low knockout drums, then by the bottom of cold anticyclone knockout drum
Portion, which condenses oil product and is placed in cold low separator, to be separated, then the bottom of cold low separator is condensed oil product and is placed in stripping
Tower；
Five, the bottom product of bottom product and No. two heat low knockout drums in stripper No. two atmospheric fractional towers are put into carry out
Normal pressure fractionation, the side line lower part product of No. two atmospheric fractional towers is high-density propellant blend component.
2. a kind of jet fuel according to claim 1 high density composite oil, it is characterised in that: the inferior heavy oil is
At least one of coal tar, ethylene bottom oil, catalytic slurry.
3. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that: in technique one, institute
Stating catalyst is the molybdenum nickel oil solvent catalyst that molybdenum nickel mass ratio is 1: 4 ﹣ 4: 1, and the dosage of the molybdenum nickel oil solvent catalyst is hydrogen
0.01% ﹣ 0.05% of gas.
4. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that:
The reaction condition of the catalytic hydroprocessing cracking reactor are as follows:
10 ﹣ 23MPa of reaction pressure, 470 DEG C of 430 ﹣ of reaction temperature, 0.3 ﹣ 1.5h of combined feed volume space velocity-1, 800 ﹣ of hydrogen to oil volume ratio
1200；
The reaction condition of the fixed bed finishing reactor are as follows:
10 ﹣ 20MPa of reaction pressure, reaction temperature are 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen to oil volume ratio
500 ﹣ 1200.
5. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that: the fixed bed
Contain hydro-upgrading catalyst converter in finishing reactor, which is by 2 kinds or 3 kinds in Co, Mo, Ni, W metal
Metal Supported is in Al2O3On catalyst, total metal mass be catalyst for hydro-upgrading gross mass 20% ﹣ 40%.
6. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that: the decompression point
Evaporating bottoms material in tower is outer whipping oil solid fuel, top product gaseous state and liquid hydrocarbon in the stripper, described two
For top product in number atmospheric fractional tower as reformer feed, side line top product is aviation kerosine, and bottom product is that catalysis is split
Change raw material.
7. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that: in technique four, by
The gas being discharged at the top of the cold anticyclone knockout drum successively mix after desulfurization process, circulation hydrogen compressed with hydrogen, then with mix
Close material mixing.
8. a kind of jet fuel according to claim 1 or 2 high density composite oil, it is characterised in that: the compound oil
Raw material composition further include at least one of 2,6-di-tert-butyl p-cresol BHT, dimethyl carbonate DMC.
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