CN107057779A - A kind of High-Density Jet - Google Patents
A kind of High-Density Jet Download PDFInfo
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- CN107057779A CN107057779A CN201611227458.6A CN201611227458A CN107057779A CN 107057779 A CN107057779 A CN 107057779A CN 201611227458 A CN201611227458 A CN 201611227458A CN 107057779 A CN107057779 A CN 107057779A
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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
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
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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
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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
- C10L1/10—Liquid carbonaceous fuels containing additives
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
- C10G2300/1092—C2-C4 olefins
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A kind of High-Density Jet, its raw material composition includes the jet fuels of RP 3, high-density propellant blend component, wherein, high-density propellant blend component is the cycloalkane and aromatic hydrocarbons and tail oil part that the boiling range obtained using inferior heavy oil as raw material, by hydrofinishing is 300 DEG C of 180 ﹣, the physicochemical property of the high-density propellant blend component meets the standard of the jet fuels of RP 3, and its density is 960 ﹣ 980kg/m3.The design not only increases the density and calorific value of jet fuel, and reduces production cost.
Description
Technical field
The invention belongs to field of aviation fuel, and in particular to a kind of High-Density Jet, it is adaptable to improve jet fuel
Density and calorific value, reduce production cost.
Background technology
Jet fuel is jet fuel, also known as aviation turbine fuel, is a kind of oils, is widely used in
Various jet airplane.The main kerosene distillate by crude distillation of jet fuel is additionally added additive and is made sometimes through refined processing,
Also it can 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, and primary quality measure is：1. volume calorific value, refers to list
The net heat that position volumetric fuei discharges when burning completely, is the product of quality of fuel caloric 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, its value is big to represent that voyage is more remote.It is the increase maximally effective approach of its volume calorific value to improve fuel density.2. ice
One of point, the important indicator of fuel cryogenic property, refer to the temperature that fuel forms hydro carbons crystallization in cooling and disappeared in heating
Degree.Jet fuel requires that freezing point is low, to the fuel of high-altitude flying for long time should less than -50 DEG C (hop can not be high
In -40 DEG C).3. density, the higher the better for density, and the big fuel of volume calorific value is traditionally also known as high-density propellant.4. aromatic hydrocarbons contains
Amount, no more than 20% (quality).5. fuel is clean, and heat endurance will get well.
High-Density Jet is that a class has high density, high volume calorific value and high performance liquid hydrocarbon fuel, and common
Jet fuel is compared, and it effectively increases the calorific value of units of fuel volume.By this fuel applications on aircraft, it can be effectively increased
Aircraft takes the unit volume heat of fuel, so as to meet the requirement of the high speed of a ship or plane of aircraft and oceangoing voyage journey.As China's high-performance flies
The military service successively of machine, it is also more and more urgent to high density, the demand of high performance jet fuel, and the jet fuel used in China
Main or RP-3, its density (20 DEG C) highest is only capable of reaching 830kg/m3, therefore, develop high density, the jet of low cost
Fuel tool is of great significance.
The content of the invention
The purpose of the present invention be overcome existing RP-3 jet fuels density it is relatively low the problem of there is provided a kind of high density, height
The jet fuel of calorific value, low cost.
To realize object above, the invention provides following technical scheme：
A kind of High-Density Jet, its raw material composition includes RP-3 jet fuels, high-density propellant blend component, its
In, the high-density propellant blend component is that the boiling range obtained using inferior heavy oil as raw material, by hydrofinishing is 300 DEG C of 180 ﹣
Cycloalkane and aromatic hydrocarbons and tail oil part, the physicochemical property of the high-density propellant blend component meets the mark of RP-3 jet fuels
Standard, and its density is 960 ﹣ 980kg/m3。
The high-density propellant blend component is prepared from using following technique successively：
First, first inferior heavy oil is put into an atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil is mixed to get compound with catalyst；
2nd, first the compound is mixed with hydrogen, then is placed in after being heated in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in a thermal high knockout drum, then
Bottom product in catalytic hydroprocessing cracking reactor is put into a heat together with the bottom product in a thermal high knockout drum
Heat low separation is carried out in low pressure separation pot；
3rd, after the completion of heat low separation, the bottom product in a heat low knockout drum is first placed in vacuum fractionation tower and entered
Row vacuum fractionation, then distillate, the light fraction obtained in technique one, the atmospheric fractional tower that vacuum fractionation tower side line is obtained
Top and side line product, which are placed in fixed bed finishing reactor, to be reacted, after the completion of reaction, by fixed bed finishing reactor
Bottom product be put into No. two thermal high knockout drums and separated；
4th, after the completion of separating, the gas of discharge at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and 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 condensation oily product of tank, which is placed in cold low separator, to be separated, then the bottom condensation oily product of cold low separator is placed in
Stripper；
5th, the bottom product in the bottom product in stripper and No. two normal pressure knockout towers is put into No. two atmospheric fractional towers
Normal pressure fractionation is carried out, the side line bottom 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 consumption of agent catalyst is 0.01% ﹣ 0.05% of hydrogen.
It is described face hydrogen cracking reactor reaction condition be：
The ﹣ 23MPa of reaction pressure 10,470 DEG C of 430 ﹣ of reaction temperature, the ﹣ 1.5h of combined feed volume space velocity 0.3-1, hydrogen to oil volume ratio
800 ﹣ 1200；
The reaction condition of the fixed bed finishing reactor is：
The ﹣ 20MPa of reaction pressure 10, reaction temperature is 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen oil body
500 ﹣ 1200 of product 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 proprietary catalyst, its total metal mass be catalyst for hydro-upgrading
20% ﹣ 40% of gross mass.
Bottoms material in the vacuum fractionation tower is the top product gas in the oily solid fuel of outer whipping, the stripper
Top product in state and liquid hydrocarbon, No. two atmospheric fractional towers is as reformer feed, and side line top product is aviation kerosine,
Bottom product is catalytically cracked material.
In technique four, the gas discharged at the top of the cold anticyclone knockout drum is successively after desulfurization process, circulation hydrogen compressed
Mix, then mixed with compound with hydrogen.
The raw material composition of the fuel also includes at least one in BHT BHT, dimethyl carbonate DMC
Kind.
Compared with prior art, beneficial effects of the present invention are：
1st, a kind of raw material composition of High-Density Jet of the invention includes RP-3 jet fuels, high-density propellant mediation group
Point, wherein, high-density propellant blend component is that the boiling range obtained using inferior heavy oil as raw material, by hydrofinishing is 180 ﹣ 300
DEG C cycloalkane and aromatic hydrocarbons and tail oil part, on the one hand, the density of the high-density propellant blend component be 960 ﹣ 980kg/m3, its
, can be by the density of RP-3 jet fuels from 830kg/m after being mixed with RP-3 jet fuels3It is promoted to 950kg/m3More than, and heat
Value significantly increases the endurance of jet engine up to more than 44MJ/kg, meanwhile, its total sulfur content is only 0.004%,
Very environmentally friendly, on the other hand, the production cost of the jet fuel is far below the production cost of RP-3 jet fuels.Therefore, this hair
The density and calorific value of bright fuel are high, environmentally friendly and cost is low.
2nd, a kind of preparation technology of High-Density Jet middle-high density blend component of the invention is by controlling catalytic hydroprocessing
The reaction condition of cracking so that whole preparation technology has higher conversion ratio, by limiting urging for catalytic hydroprocessing cracking reaction
Agent can suppress feedstock oil green coke during the course of the reaction, it is ensured that the long-term operation of device, and the adaptability to raw material of this method is strong, secondary
Product passes through hydrofinishing, and its property is excellent, with higher use value.Therefore, preparation technology of the present invention not only yield and
Product use value is high, and make it that the usage cycles of device are long.
Brief description of the drawings
Fig. 1 is the preparation technology flow chart of middle-high density fuel blend component of the present invention.
Embodiment
With reference to embodiment, the invention will be further described.
A kind of High-Density Jet, its raw material composition includes RP-3 jet fuels, high-density propellant blend component, its
In, the high-density propellant blend component is that the boiling range obtained using inferior heavy oil as raw material, by hydrofinishing is 300 DEG C of 180 ﹣
Cycloalkane and aromatic hydrocarbons and tail oil part, the physicochemical property of the high-density propellant blend component meets the mark of RP-3 jet fuels
Standard, and its density is 960 ﹣ 980kg/m3。
Referring to Fig. 1, the high-density propellant blend component is prepared from using following technique successively：
First, first inferior heavy oil is put into an atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil is mixed to get compound with catalyst；
2nd, first the compound is mixed with hydrogen, then is placed in after being heated in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in a thermal high knockout drum, then
Bottom product in catalytic hydroprocessing cracking reactor is put into a heat together with the bottom product in a thermal high knockout drum
Heat low separation is carried out in low pressure separation pot；
3rd, after the completion of heat low separation, the bottom product in a heat low knockout drum is first placed in vacuum fractionation tower and entered
Row vacuum fractionation, then distillate, the light fraction obtained in technique one, the atmospheric fractional tower that vacuum fractionation tower side line is obtained
Top and side line product, which are placed in fixed bed finishing reactor, to be reacted, after the completion of reaction, by fixed bed finishing reactor
Bottom product be put into No. two thermal high knockout drums and separated；
4th, after the completion of separating, the gas of discharge at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and 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 condensation oily product of tank, which is placed in cold low separator, to be separated, then the bottom condensation oily product of cold low separator is placed in
Stripper；
5th, the bottom product in the bottom product in stripper and No. two normal pressure knockout towers is put into No. two atmospheric fractional towers
Normal pressure fractionation is carried out, the side line bottom 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 consumption of agent catalyst is 0.01% ﹣ 0.05% of hydrogen.
It is described face hydrogen cracking reactor reaction condition be：
The ﹣ 23MPa of reaction pressure 10,470 DEG C of 430 ﹣ of reaction temperature, the ﹣ 1.5h of combined feed volume space velocity 0.3-1, hydrogen to oil volume ratio
800 ﹣ 1200；
The reaction condition of the fixed bed finishing reactor is：
The ﹣ 20MPa of reaction pressure 10, reaction temperature is 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen oil body
500 ﹣ 1200 of product 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 proprietary catalyst, its total metal mass be catalyst for hydro-upgrading
20% ﹣ 40% of gross mass.
Bottoms material in the vacuum fractionation tower is the top product gas in the oily solid fuel of outer whipping, the stripper
Top product in state and liquid hydrocarbon, No. two atmospheric fractional towers is as reformer feed, and side line top product is aviation kerosine,
Bottom product is catalytically cracked material.
In technique four, the gas discharged at the top of the cold anticyclone knockout drum is successively after desulfurization process, circulation hydrogen compressed
Mix, then mixed with compound with hydrogen.
The raw material composition of the fuel also includes at least one in BHT BHT, dimethyl carbonate DMC
Kind.
The principle of the present invention is described as follows：
The invention provides a kind of High-Density Jet, the jet fuel middle-high density fuel blend component can not only
Play a part of dense additive, by its RP-3 jet fuels density from 830kg/m3Increase to 950kg/m3More than, but also
Its calorific value can be adjusted to more than 44MJ/kg, so as to significantly increase the endurance of fuel.Simultaneously as high-density propellant is adjusted
Production cost with component is under the production cost of RP-3 jet fuels, therefore, and the production cost of fuel of the present invention is less than
The production cost of RP-3 jet fuels.
In addition, the preparation technology of jet fuel of the present invention is simply, conveniently, only need to be according to high-density propellant blend component, RP-
The proportioning of 3 jet fuels, is directly mixed using measure control method and round-robin method.
The all technical of high density blend component and High-Density Jet of the present invention is shown in Table 1
The indices of the jet fuel of the present invention of table 1, high-density propellant blend component (boiling range 180 ﹣ 300 DEG C)
In preparation technology of the present invention, contain catalyst for hydro-upgrading in fixed bed finishing reactor, the hydro-upgrading
Catalyst can promote the cut not less than 370 DEG C to occur cracking reaction, reduce the cut less than 370 DEG C and occur cracking reaction.
Inferior heavy oil of the present invention originates from the Inner Mongol, and its related physicochemical property is shown in Table 2：
The physicochemical property of the inferior heavy oil of table 2
| 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 contents, 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：
A kind of High-Density Jet, 49.4 are pressed by RP-3 jet fuels, high-density propellant blend component, BHT, DMC:
49.4: 0.2: 1 mass ratio is mixed, wherein, the high density blend component is using inferior heavy oil as raw material, by hydrogenation
The boiling range being refining to obtain is 180-300 DEG C of cycloalkane and aromatic hydrocarbons and tail oil part, and specific preparation technology is：
First, first inferior heavy oil is put into an atmospheric fractional tower to obtain light fraction and reduced crude, then will be described normal
Pressure residual oil is mixed to get compound with catalyst, wherein, the inferior heavy oil is coal tar, and the catalyst is molybdenum nickel mass ratio
Be 1: 4 molybdenum nickel oil solvent catalyst, the consumption of the molybdenum nickel oil solvent catalyst is the 0.015% of hydrogen；
2nd, first the compound is mixed with hydrogen, then is placed in after being heated in catalytic hydroprocessing cracking reactor and reacts,
The top product in catalytic hydroprocessing cracking reactor is then placed in progress thermal high separation in a thermal high knockout drum, then
Bottom product in catalytic hydroprocessing cracking reactor is put into a heat together with the bottom product in a thermal high knockout drum
In low pressure separation pot carry out heat low separation, wherein, it is described face hydrogen cracking reactor reaction condition be：
Reaction pressure 10MPa, 430 DEG C of reaction temperature, combined feed volume space velocity 0.3h-1, hydrogen to oil volume ratio 1000；
3rd, after the completion of heat low separation, the bottom product in a heat low knockout drum is first placed in vacuum fractionation tower and entered
Row vacuum fractionation, then distillate, the light fraction obtained in technique one, the atmospheric fractional tower that vacuum fractionation tower side line is obtained
Top and side line product, which are placed in fixed bed finishing reactor, to be reacted, after the completion of reaction, by fixed bed finishing reactor
Bottom product be put into No. two thermal high knockout drums and separated, wherein, the bottoms material in the vacuum fractionation tower is outer
Contain hydro-upgrading catalyst converter in whipping oil solid fuel, the fixed bed finishing reactor, the hydro-upgrading catalyst converter is Mo-
Ni/Al2O3Catalyst for hydro-upgrading, its active metal quality is the 25% of catalyst for hydro-upgrading gross mass, and fixed bed is refined
The reaction condition of reactor is：
Reaction pressure 10MPa, reaction temperature is 280 DEG C, and combined feed volume space velocity is 1.0h-1, hydrogen to oil volume ratio 500；
4th, after the completion of separating, the gas of discharge at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and 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 condensation oily product of tank, which is placed in cold low separator, to be separated, then the bottom condensation oily product of cold low separator is placed in
Stripper, wherein, at the top of the cold anticyclone knockout drum gas of discharge successively after desulfurization process, circulation hydrogen compressed with hydrogen
Mixing, is then mixed with compound；
5th, the bottom product in the bottom product in stripper and No. two normal pressure knockout towers is put into No. two normal pressure fractionation
Tower, after No. two atmospheric fractional tower fractionation, the as high density blend component flowed out by its side line, wherein, in the stripper
Top product gaseous state and liquid hydrocarbon, the top product in No. two atmospheric fractional towers is as reformer feed, and side line product is
Aviation kerosine, bottom product is catalytically cracked material.
Embodiment 2：
Step be the same as Example 1, difference is：
In the jet fuel, RP-3 jet fuels, the mass ratio of high-density propellant blend component are 9: 1；
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 consumption of the molybdenum nickel oil solvent catalyst is the 0.02% of hydrogen；
In the technique two, the reaction condition for facing hydrogen cracking reactor is：
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, its active metal quality
For the 30% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor is：
Reaction pressure 15MPa, reaction temperature is 330 DEG C, and combined feed volume space velocity is 0.6h-1, hydrogen to oil volume ratio 800.
Embodiment 3：
Step be the same as Example 1, difference is：
In the jet fuel, RP-3 jet fuels, the mass ratio of high-density propellant blend component are 7: 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 consumption of the molybdenum nickel oil solvent catalyst is the 0.04% of hydrogen；
In the technique two, the reaction condition for facing hydrogen cracking reactor is：
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, its active metal quality is
The 40% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor is：
Reaction pressure 20MPa, reaction temperature is 400 DEG C, and combined feed volume space velocity is 2.0h-1, hydrogen to oil volume ratio 800.
Embodiment 4：
Step be the same as Example 1, difference is：
In the jet fuel, RP-3 jet fuels, the mass ratio of high-density propellant blend component are 3: 7；
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 consumption of the molybdenum nickel oil solvent catalyst is the 0.035% of hydrogen；
In the technique two, the reaction condition for facing hydrogen cracking reactor is：
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, its active metal matter
Measure as the 23% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor is：
Reaction pressure 13MPa, reaction temperature is 300 DEG C, and combined feed volume space velocity is 0.8h-1, hydrogen to oil volume ratio 1000.
Embodiment 5：
Step be the same as Example 1, difference is：
In the jet fuel, RP-3 jet fuels, the mass ratio of high-density propellant blend component are 1: 9；
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 consumption of the molybdenum nickel oil solvent catalyst is the 0.05% of hydrogen；
In the technique two, the reaction condition for facing hydrogen cracking reactor is：
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, its active metal matter
Measure as the 20% of catalyst for hydro-upgrading gross mass, the reaction condition of fixed bed finishing reactor is：
Reaction pressure 17MPa, reaction temperature is 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 the high-density propellant blend component of table 3
Claims (9)
1. a kind of High-Density Jet, it is characterised in that：
The raw material composition of the fuel includes RP-3 jet fuels, high-density propellant blend component, wherein, the high-density propellant
Blend component be the cycloalkane and aromatic hydrocarbons that the boiling range that is obtained using inferior heavy oil as raw material, by hydrofinishing is 300 DEG C of 180 ﹣ and
Tail oil part, the physicochemical property of the high-density propellant blend component meets the standard of RP-3 jet fuels, and its density is 960 ﹣
980kg/m3。
2. a kind of High-Density Jet according to claim 1, it is characterised in that：
The high-density propellant blend component is prepared from using following technique successively：
First, first inferior heavy oil is put into an atmospheric fractional tower to obtain light fraction and reduced crude, then by the normal pressure slag
Oil is mixed to get compound with catalyst；
2nd, first the compound is mixed with hydrogen, then is placed in after being heated in catalytic hydroprocessing cracking reactor and reacts, then
Top product in catalytic hydroprocessing cracking reactor is placed in progress thermal high separation in a thermal high knockout drum, will then be faced
Bottom product in hydrogen catalysis cracking reactor is put into a heat low together with the bottom product in a thermal high knockout drum
Heat low separation is carried out in knockout drum；
3rd, after the completion of heat low separation, the bottom product in a heat low knockout drum is first placed in vacuum fractionation tower and subtracted
Pressure fractionating, then the distillate that vacuum fractionation tower side line is obtained, the light fraction obtained in technique one, at the top of an atmospheric fractional tower
And side line product is placed in fixed bed finishing reactor and reacted, after the completion of reaction, by the bottom in fixed bed finishing reactor
Portion's product is put into No. two thermal high knockout drums and separated；
4th, after the completion of separating, the gas of discharge at the top of No. two thermal high knockout drums is first passed through cold anticyclone knockout drum and 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's condensation oily product, which is placed in cold low separator, to be separated, then the bottom condensation oily product of cold low separator is placed in into stripping
Tower；
5th, the bottom product in the bottom product in stripper and No. two normal pressure knockout towers is put into No. two atmospheric fractional tower progress
Normal pressure is fractionated, and the side line bottom product of No. two atmospheric fractional towers is high-density propellant blend component.
3. a kind of High-Density Jet according to claim 2, it is characterised in that：The inferior heavy oil be coal tar,
At least one of ethylene bottom oil, catalytic slurry.
4. a kind of High-Density Jet according to Claims 2 or 3, it is characterised in that：In technique one, the catalyst
It is 1: 4 ﹣ 4: 1 molybdenum nickel oil solvent catalyst for molybdenum nickel mass ratio, the consumption of the molybdenum nickel oil solvent catalyst is hydrogen
0.01% ﹣ 0.05%.
5. a kind of High-Density Jet according to Claims 2 or 3, it is characterised in that：
It is described face hydrogen cracking reactor reaction condition be：
The ﹣ 23MPa of reaction pressure 10,470 DEG C of 430 ﹣ of reaction temperature, the ﹣ 1.5h of combined feed volume space velocity 0.3-1, the ﹣ of hydrogen to oil volume ratio 800
1200；
The reaction condition of the fixed bed finishing reactor is：
The ﹣ 20MPa of reaction pressure 10, reaction temperature is 400 DEG C of 280 ﹣, and combined feed volume space velocity is 0.6 ﹣ 2.0h-1, hydrogen to oil volume ratio
500 ﹣ 1200.
6. a kind of High-Density Jet according to Claims 2 or 3, it is characterised in that：The fixed bed refining reaction
Contain hydro-upgrading catalyst converter in device, the hydro-upgrading catalyst converter is by 2 kinds in Co, Mo, Ni, W metal or 3 kinds of Metal Supporteds
In Al2O3On proprietary catalyst, its total metal mass be catalyst for hydro-upgrading gross mass 20% ﹣ 40%.
7. a kind of High-Density Jet according to Claims 2 or 3, it is characterised in that：In the vacuum fractionation tower
Bottoms material is the top product gaseous state and liquid hydrocarbon in the oily solid fuel of outer whipping, the stripper, No. two normal pressures point
The top product in tower is evaporated as reformer feed, and side line top product is aviation kerosine, and bottom product is catalytically cracked material.
8. a kind of High-Density Jet according to Claims 2 or 3, it is characterised in that：In technique four, by the cold height
The gas of discharge is mixed after desulfurization process, circulation hydrogen compressed with hydrogen successively at the top of pressure knockout drum, is then mixed with compound.
9. a kind of High-Density Jet according to any one of claim 1 ﹣ 3, it is characterised in that：The original of the fuel
Material composition also includes at least one of 2.6- BHTs BHT, dimethyl carbonate DMC.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4398978A (en) * | 1982-04-26 | 1983-08-16 | The United States Of America As Represented By The Secretary Of The Navy | High density, low viscosity airbreather fuel (RJ-4-I) |
| GB2234518A (en) * | 1989-07-27 | 1991-02-06 | Exxon Research Engineering Co | Process for the production of high density jet fuel from fused multi-ring aromatics and hydroaromatics |
| CN101506337A (en) * | 2006-06-28 | 2009-08-12 | 国际壳牌研究有限公司 | Fuel compositions |
| CN105062579A (en) * | 2015-09-08 | 2015-11-18 | 天津大学 | Method for preparing high-density mixed hydrocarbon liquid jet fuel from dicyclopentadiene |
-
2016
- 2016-12-27 CN CN201611227458.6A patent/CN107057779B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4398978A (en) * | 1982-04-26 | 1983-08-16 | The United States Of America As Represented By The Secretary Of The Navy | High density, low viscosity airbreather fuel (RJ-4-I) |
| GB2234518A (en) * | 1989-07-27 | 1991-02-06 | Exxon Research Engineering Co | Process for the production of high density jet fuel from fused multi-ring aromatics and hydroaromatics |
| CN101506337A (en) * | 2006-06-28 | 2009-08-12 | 国际壳牌研究有限公司 | Fuel compositions |
| CN105062579A (en) * | 2015-09-08 | 2015-11-18 | 天津大学 | Method for preparing high-density mixed hydrocarbon liquid jet fuel from dicyclopentadiene |
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