CN109266390B - Method for increasing yield of aviation kerosene through hydrocracking - Google Patents

Method for increasing yield of aviation kerosene through hydrocracking Download PDF

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CN109266390B
CN109266390B CN201710585785.7A CN201710585785A CN109266390B CN 109266390 B CN109266390 B CN 109266390B CN 201710585785 A CN201710585785 A CN 201710585785A CN 109266390 B CN109266390 B CN 109266390B
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reactor
hydrocracking
aviation kerosene
oil
pressure separator
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CN109266390A (en
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袁晓亮
张占全
张志华
王燕
王延飞
余颖龙
谢斌
张雅琳
付凯妹
翟绪丽
庄梦琪
王晶晶
王嘉祎
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Petrochina Co Ltd
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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
    • C10G2300/1037—Hydrocarbon fractions
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

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Abstract

The invention discloses a method for producing aviation kerosene in a high yield by hydrocracking, which comprises the following steps: raw oil S1 and fresh hydrogen are fed into a high-pressure separator after being hydrofined by a first reactor; s2, the liquid phase material flow of the high-pressure separator enters a low-pressure separator and a fractionating tower in sequence, and naphtha and aviation kerosene fractions are cut out through the fractionating tower; compressing the gas-phase product of the S3 high-pressure separator, and then feeding the compressed gas-phase product and the bottom material of the fractionating tower into a second reactor for hydrocracking reaction; the reaction effluent of the second reactor S4 was recycled back to the first reactor. The method of the invention arranges the fractionating tower between the hydrofining reactor and the hydrocracking reactor, avoids the influence of overcracking on the yield of the aviation kerosene, and simultaneously improves the properties of the aviation kerosene fraction by carrying out aromatic saturation on the aviation kerosene fraction after cracking.

Description

Method for increasing yield of aviation kerosene through hydrocracking
Technical Field
The invention belongs to a method for hydrocracking aviation kerosene with high yield, wherein a hydrofining reactor is used as raw material pretreatment for desulfurization and denitrification, and aviation kerosene aromatic hydrocarbon hydrogenation saturation is carried out at the same time, and a fractionating tower is arranged between the hydrofining reactor and the hydrocracking reactor for cutting hydrocracking products and cutting aviation kerosene fractions in the raw materials in time so as to avoid excessive cracking.
Background
The hydrocracking technology is used as an important processing means for integrating heavy oil lightening, inferior oil quality modification and refining, and has the advantages of flexible production scheme, strong raw material adaptability, high target product selectivity, good quality, high tail oil added value and the like. In recent years, the diesel-gasoline ratio is continuously reduced, the demand of diesel oil is slowly increased, and the self-sufficient rate of aviation kerosene, chemical engineering and aromatic hydrocarbon raw materials is seriously insufficient. Therefore, hydrocracking technology is shifting from the medium oil type to the aviation kerosene or chemical feedstock type. Compared with the traditional high-pressure hydrocracking, the medium-pressure hydrocracking has the advantages of low investment, low operation cost and the like. However, when the process is operated at medium pressure, the quality of the middle distillate product is slightly poorer than that of the high-pressure operation, particularly the aviation kerosene fraction has high aromatic hydrocarbon content and low smoke point, and needs to be further hydrotreated or blended with other products.
CN98121079.1 discloses a medium pressure hydrocracking process capable of producing qualified aviation kerosene products. The raw oil is subjected to hydrocracking reaction, gas-liquid two phases are subjected to high-resolution separation, and a gas-phase product is used as recycle hydrogen and circulated to a hydrocracking unit; and the liquid phase product enters a fractionating tower to separate naphtha, aviation kerosene, diesel oil and tail oil, one part of aviation kerosene fraction enters an aviation kerosene hydrogenation saturation unit to be subjected to aromatic saturation, and gas serving as make-up hydrogen continues to enter a hydrocracking unit.
CN200410068935.X discloses a medium-pressure hydrocracking method for producing jet fuel, wherein raw oil and hydrogen are mixed and firstly subjected to hydrotreating, a gas-phase material flow of a hydrotreating effluent subjected to thermal high-pressure separation directly enters a second hydrotreating reactor for aromatic saturation, and a liquid-phase material flow of a thermal high-pressure separator is subjected to pressure reduction and then sequentially enters a thermal low-pressure separator, a cold low-pressure separator and a fractionating tower; the effluent of the second hydrotreating reactor is subjected to cold high-pressure separation to obtain a liquid phase material flow and a gas phase material flow, wherein the gas phase material flow is recycled, and the liquid phase material flow enters a cold low-pressure separator and a fractionating tower in sequence after being subjected to pressure reduction; and separating the liquid phase material flow in the fractionating tower to obtain naphtha fraction, jet fuel fraction, diesel oil fraction and tail oil.
CN201410594510.6 discloses a method for producing aviation kerosene by medium-pressure hydrocracking, wherein raw oil sequentially passes through a hydrofining zone and a hydrocracking zone for reaction, effluent is sequentially subjected to gas-liquid separation and fractionation, and light naphtha fraction, heavy naphtha fraction, diesel fraction, tail oil fraction and kerosene fraction are fractionated; at least part of the kerosene fraction is fed into the post-refining catalyst bed of the hydrocracking reaction zone for recycling.
The reason is that the medium-pressure hydrocracking is limited by thermodynamic equilibrium, the aromatic hydrocarbon saturation depth is low, the product quality, especially the smoke point of the aviation kerosene, is unqualified, and the heavy wax oil and the catalytic diesel oil are not suitable for being used as raw materials for producing aviation kerosene by the medium-pressure hydrocracking due to the high aromatic hydrocarbon content. The light wax oil, straight-run diesel oil or mixed raw materials thereof are usually subjected to hydrofining and hydrocracking, and the aviation kerosene fraction is subjected to aftertreatment and aromatic saturation to meet the standard requirement of aviation kerosene.
Therefore, how to solve the problem of producing qualified aviation kerosene products by a medium-pressure and low-pressure hydrocracking unit is a key problem which needs to be solved urgently by the technology.
Disclosure of Invention
The invention aims to realize that light wax oil and straight-run diesel oil are used as raw materials in a medium-pressure range by reasonably adjusting a process flow on the basis of the prior art, so that aviation kerosene can be produced to the maximum extent, and meanwhile, naphtha and tail oil can be used as ethylene raw materials.
According to the invention, hydrofining and hydrocracking reactors are connected in series in an inverted manner, the first reactor is used as a hydrofining pretreatment section to remove sulfur, nitrogen and aromatic hydrocarbons of the raw material, and is used as a supplementary refining section to carry out aromatic saturation, the fractionating tower is arranged between the first reactor and the second reactor to cut the aviation kerosene fraction in the raw material while cutting the hydrocracking product, so that excessive cracking is avoided, and the aviation kerosene smoke point is ensured to be qualified while the aviation kerosene is produced to the maximum extent.
The invention provides a method for hydrocracking aviation kerosene with high yield, which comprises the following steps:
raw oil S1 and fresh hydrogen are fed into a high-pressure separator after being hydrofined by a first reactor;
s2, the liquid phase material flow of the high-pressure separator enters a low-pressure separator and a fractionating tower in sequence, and naphtha and aviation kerosene fractions are cut out through the fractionating tower;
compressing the gas-phase product of the S3 high-pressure separator, and then feeding the compressed gas-phase product and the bottom material of the fractionating tower into a second reactor for hydrocracking reaction;
the reaction effluent of the second reactor S4 was recycled back to the first reactor.
The hydrocracking method for increasing the yield of aviation kerosene, provided by the invention, is characterized in that the reaction conditions of the first reactor are preferably as follows: the pressure is 5-16 MPa, the temperature is 260-420 ℃, and the volume space velocity is 0.5-3.0 h-1Hydrogen to oil volume ratio of 500 to 2000Nm3/m3。
The hydrocracking method for increasing the yield of aviation kerosene, provided by the invention, is characterized in that the reaction conditions of the second reactor are preferably as follows: the pressure is 5-14 MPa, the temperature is 260-420 ℃, and the volume space velocity is 0.3-3.0 h-1Hydrogen to oil volume ratio of 500 to 2000Nm3/m3。
The method for hydrocracking and producing aviation kerosene in high yield preferably comprises the step of selecting the raw oil from at least one of light wax oil, straight-run diesel oil and coker diesel oil.
The method for hydrocracking and producing aviation kerosene in high yield, disclosed by the invention, is characterized in that the weight percentage of the coking diesel oil in the raw oil is preferably 0-15%.
The hydrocracking method for producing aviation kerosene in a high yield, provided by the invention, has the distillation range of the raw oil preferably ranging from 200 ℃ to 500 ℃.
The method for hydrocracking aviation kerosene with high yield, disclosed by the invention, is characterized in that the first reactor is preferably filled with hydrofining catalyst.
The method for hydrocracking and producing aviation kerosene in high yield is characterized in that the upper layer of the first reactor is filled with a hydrofining catalyst, the lower layer of the first reactor is filled with a hydrocracking catalyst, and the height ratio of the upper layer to the lower layer is 1: 10-10: 1, and more preferably 1: 5-5: 1.
The method for hydrocracking the high-yield aviation kerosene, disclosed by the invention, is characterized in that the second reactor is preferably filled with a hydrocracking catalyst.
The hydrocracking method for producing aviation kerosene in a high yield is characterized in that the upper layer of the second reactor is preferably filled with a hydrocracking catalyst, the lower layer of the second reactor is filled with a hydrofining catalyst, and the height ratio of the upper layer to the lower layer is 1: 10-10: 1, and more preferably 1: 5-5: 1.
The hydrocracking method disclosed by the invention is operated under a medium-pressure condition, and the reaction pressure of the first reactor and the reaction pressure of the second reactor are both 5-16 MPa. The raw oil is preferably selected from lighter fractions such as wax oil, diesel oil and the like, the distillation range is 200-500 ℃, the raw oil can be light wax oil, straight-run diesel oil or a mixed raw material thereof, and can also be mixed with partial coking diesel oil, and the mixing proportion of the coking diesel oil is not more than 15%.
The invention produces the aviation kerosene with low aromatic hydrocarbon content and high smoke point under the medium pressure, has the characteristics of low investment, low operation cost, simple operation, high yield and the like, and can produce naphtha as the ethylene raw material.
According to the invention, a fractionating tower is arranged between a first reactor and a second reactor, the tail oil fraction after naphtha and aviation kerosene fraction are fractionated is subjected to hydrocracking, the hydrocracked product enters the first reactor again for aromatic saturation, and then enters the fractionating tower for fractionating the naphtha and aviation kerosene fraction. The first reactor is used as raw material pretreatment for desulfurization and denitrification and simultaneously for aviation kerosene aromatic hydrocarbon hydrogenation saturation, and the fractionating tower is arranged between the first reactor and the second reactor to cut the aviation kerosene fraction in the raw material while cutting the hydrocracking product, so that excessive cracking is avoided.
Drawings
FIG. 1 is a schematic flow diagram of a process for hydrocracking high-yield aviation kerosene according to the present invention, in which some conventional devices such as a heating furnace and a pump are omitted;
in the figure, 1, a first reactor; 2. a high pressure separator; 3. a low pressure separator; 4. a fractionating column; 5. a second reactor; 6. a recycle compressor; 7. a reaction effluent; 8. a gas phase product; 9. a liquid phase stream; 10. a naphtha fraction; 11. aviation kerosene fraction; 12 bottom material.
Raw oil, new hydrogen and reaction effluent 7 are mixed, the mixture enters a high-pressure separator 2 after desulfurization and denitrification and aromatic saturation in a first reactor 1, liquid phase material flow 9 of the high-pressure separator passes through a low-pressure separator 3 and then is cut into naphtha fraction 10 and aviation kerosene fraction 11 through a fractionating tower 4, a gas phase product 8 of the high-pressure separator 2 is compressed by a recycle hydrogen compressor and then is mixed with a bottom material 12, the mixture enters a second reactor 5 for hydrocracking reaction, and the reaction effluent 7 is mixed with the raw oil and the new hydrogen and then returns to the first reactor.
Detailed Description
Example 1
The mixed raw material of 65 wt% of straight-run diesel oil, 28 wt% of vacuum wax oil and 7 wt% of coking wax oil is adopted.
S1, firstly, raw oil and new hydrogen are hydrofined in a first reactor 1 and then enter a high-pressure separator 2;
s2, the liquid phase material flow 9 of the high-pressure separator 2 enters the low-pressure separator 3 and the fractionating tower 4 in sequence, and naphtha 10 and aviation kerosene fraction 11 are cut out through the fractionating tower 4;
s3, compressing the gas-phase product 8 of the high-pressure separator 2 by a circulating compressor 6, and then entering the gas-phase product and the bottom material 12 of the fractionating tower 4 into a second reactor 5 for hydrocracking reaction;
s4 finally, the reaction effluent 7 of the second reactor 5 is recycled back to the first reactor 1.
Wherein, the reaction conditions of the first reactor 1 are as follows: the pressure is 13MPa, the temperature is 375 ℃, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 700Nm3/m3；
The reaction conditions of the second reactor were: the pressure is 13MPa, the temperature is 386 ℃, and the volume space velocity is 0.8h-1Hydrogen to oil volume ratio 1000Nm3/m3。
The first reactor is filled with industrial hydrofining catalyst GHT-01, and the specific surface area is 150.6m2The pore volume is 0.33 ml/g; the second reactor is filled with hydrocracking catalyst GHC-01, and the specific surface area is 229.8m2The pore volume is 0.34 ml/g.
The properties of the feedstock, the specific operating conditions and product distribution of the process, and the product results of this example are shown in Table 1.
TABLE 1 example 1 raw oil, operating conditions and product distribution
Figure BDA0001353490690000051
As can be seen from Table 1, the yield of aviation kerosene was 63.8% and the smoke point was 28.8 mm.
Example 2
Straight-run diesel oil from an atmospheric distillation device is used as a raw material, and the distillation range is 230-352 ℃.
S1, firstly, raw oil and new hydrogen are hydrofined in a first reactor 1 and then enter a high-pressure separator 2;
s2, the liquid phase material flow 9 of the high-pressure separator 2 enters the low-pressure separator 3 and the fractionating tower 4 in sequence, and naphtha 10 and aviation kerosene fraction 11 are cut out through the fractionating tower 4;
s3, compressing the gas-phase product 8 of the high-pressure separator 2 by a circulating compressor 6, and then entering the gas-phase product and the bottom material 12 of the fractionating tower 4 into a second reactor 5 for hydrocracking reaction;
s4 finally, the reaction effluent 7 of the second reactor 5 is recycled back to the first reactor 1.
Wherein, the reaction conditions of the first reactor 1 are as follows: the pressure is 6.4MPa, the temperature is 350 ℃, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 800Nm3/m3；
The reaction conditions of the second reactor were: the pressure is 6.4MPa, the temperature is 363 ℃, and the volume space velocity is 0.8h-1Hydrogen to oil volume ratio of 800Nm3/m3。
The first reactor was packed with a hydrofining catalyst GHT-02 having a specific surface area of 157.9m2The pore volume is 0.36 ml/g; the upper layer of the second reactor is filled with a hydrocracking catalyst GHC-02, and the specific surface area is 245.4m2The pore volume is 0.35ml/g, the lower layer is filled with hydrofining catalyst GHT-02, and the height ratio of the upper layer to the lower layer is 4: 1.
The properties of the feedstock, the specific operating conditions and product distribution of the process, and the product results of this example are shown in Table 2.
Table 2 example 2 feed oil, operating conditions and product distribution
Figure BDA0001353490690000061
Figure BDA0001353490690000071
As can be seen from Table 2, the yield of aviation kerosene was 64.5% and the smoke point was 26.9 mm.
Example 3
The mixed raw material of 50 wt% of straight-run diesel oil, 25 wt% of vacuum wax oil and 15 wt% of coking wax oil is adopted.
S1, firstly, raw oil and new hydrogen are hydrofined in a first reactor 1 and then enter a high-pressure separator 2;
s2, the liquid phase material flow 9 of the high-pressure separator 2 enters the low-pressure separator 3 and the fractionating tower 4 in sequence, and naphtha 10 and aviation kerosene fraction 11 are cut out through the fractionating tower 4;
s3, compressing the gas-phase product 8 of the high-pressure separator 2 by a circulating compressor 6, and then entering the gas-phase product and the bottom material 12 of the fractionating tower 4 into a second reactor 5 for hydrocracking reaction;
s4 finally, the reaction effluent 7 of the second reactor 5 is recycled back to the first reactor 1.
Wherein, the reaction conditions of the first reactor 1 are as follows: the pressure is 10MPa, the temperature is 375 ℃, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 800Nm3/m3；
The reaction conditions of the second reactor were: the pressure is 10MPa, the temperature is 383 ℃, and the volume space velocity is 0.8h-1Hydrogen to oil volume ratio of 800Nm3/m3。
The upper layer of the first reactor is filled with hydrofining catalyst GHT-03, the lower layer is filled with hydrocracking catalyst GHC-03, and the height ratio of the upper layer to the lower layer is 3: 1; the upper layer of the second reactor is filled with a hydrocracking catalyst GHC-03, the lower layer is filled with a hydrofining catalyst GHT-03, and the height ratio of the upper layer to the lower layer is 3: 1. Wherein the GHT-03 catalyst specific surface is 207.6m2G, pore volume 0.36ml/g(ii) a The specific surface area of the GHC-03 catalyst is 219.5m2The pore volume is 0.34 ml/g.
The properties of the feedstock, the specific process conditions and product distribution, and the product results of this example are shown in Table 3.
TABLE 3 example 3 feed oil, operating conditions and product distribution
Figure BDA0001353490690000081
As can be seen from Table 3, the yield of aviation kerosene was 67.7% and the smoke point was 27.6 mm.
Example 4
The mixed raw material of 50 wt% of straight-run diesel oil and 50 wt% of vacuum wax oil is adopted.
S1, firstly, raw oil and new hydrogen are hydrofined in a first reactor 1 and then enter a high-pressure separator 2;
s2, the liquid phase material flow 9 of the high-pressure separator 2 enters the low-pressure separator 3 and the fractionating tower 4 in sequence, and naphtha 10 and aviation kerosene fraction 11 are cut out through the fractionating tower 4;
s3, compressing the gas-phase product 8 of the high-pressure separator 2 by a circulating compressor 6, and then entering the gas-phase product and the bottom material 12 of the fractionating tower 4 into a second reactor 5 for hydrocracking reaction;
s4 finally, the reaction effluent 7 of the second reactor 5 is recycled back to the first reactor 1.
Wherein, the reaction conditions of the first reactor 1 are as follows: the pressure is 13MPa, the temperature is 380 ℃, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 800Nm3/m3；
The reaction conditions of the second reactor were: the pressure is 13MPa, the temperature is 388 ℃ and the volume space velocity is 0.6h-1Hydrogen to oil volume ratio 1000Nm3/m3。
The first reactor is filled with industrial hydrofining catalyst GHT-01, and the specific surface area is 150.6m2The pore volume is 0.33 ml/g; the second reactor is filled with hydrocracking catalyst GHC-01, and the specific surface area is 229.8m2The pore volume is 0.34 ml/g.
The properties of the feedstock, the specific operating conditions and product distribution of the process, and the product results of this example are shown in Table 4.
Table 4 example 4 feed oil, operating conditions and product distribution
Figure BDA0001353490690000091
As can be seen from Table 4, the yield of aviation kerosene was 55.4% and the smoke point was 25.6 mm.
Comparative example 1
Using the same feedstock as in example 4, 50 wt% straight-run diesel was mixed with 50 wt% vacuum wax oil.
S1, firstly, raw oil and new hydrogen enter a hydrocracking reactor after being subjected to hydrofining reaction;
s2, feeding the product from the hydrocracking reactor into a fractionating tower through a high-pressure separator and a low-pressure separator, cutting naphtha and aviation kerosene fractions, and circulating the rest as tail oil to the inlet of the hydrocracking reactor;
s3, the aviation kerosene fraction enters a third reactor to be hydrorefined to obtain an aviation kerosene product.
Wherein, the reaction conditions of the first reactor 1 are as follows: the pressure is 13MPa, the temperature is 380 ℃, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 800Nm3/m3；
The reaction conditions of the second reactor were: the pressure is 13MPa, the temperature is 388 ℃ and the volume space velocity is 0.6h-1Hydrogen to oil volume ratio 1000Nm3/m3；
The reaction conditions of the third reactor were: the pressure is 6MPa, the temperature is 350 ℃, the volume space velocity is 1.5h < -1 >, and the volume ratio of hydrogen to oil is 600Nm3/m3。
The first reactor is filled with industrial hydrofining catalyst GHT-01, and the specific surface area is 150.6m2The pore volume is 0.33 ml/g; the second reactor is filled with hydrocracking catalyst GHC-01, and the specific surface area is 229.8m2The pore volume is 0.34 ml/g; the third reactor is filled with an industrial hydrofining catalyst GHT-01.
The properties of the feedstock, the specific operating conditions and product distribution of the process, and the product results of this comparative example are shown in Table 5.
TABLE 5 crude oil, operating conditions and product distribution for comparative example 1
Figure BDA0001353490690000101
Figure BDA0001353490690000111
As can be seen from Table 5, the yield of aviation kerosene was 55.4% and the smoke point was 25.6 mm.
Compared with the comparative example, the embodiment of the invention can save a section of flow compared with the prior art, and has the characteristics of high yield and low smoke point of the aviation kerosene.
The present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore intended that all such changes and modifications as fall within the true spirit and scope of the invention be considered as within the following claims.

Claims (10)

1. The hydrocracking method for producing aviation kerosene in high yield is characterized by comprising the following steps:
raw oil S1 and fresh hydrogen are fed into a high-pressure separator after being hydrofined by a first reactor;
s2, the liquid phase material flow of the high-pressure separator enters a low-pressure separator and a fractionating tower in sequence, and naphtha and aviation kerosene fractions are cut out through the fractionating tower;
compressing the gas-phase product of the S3 high-pressure separator, and then feeding the compressed gas-phase product and the bottom material of the fractionating tower into a second reactor for hydrocracking reaction;
the reaction effluent of the second reactor is recycled to the first reactor S4.
2. The method for hydrocracking high-yield aviation kerosene according to claim 1, wherein the reaction conditions of said first reactor are: the pressure is 5-16 MPa, the temperature is 260-420 ℃, and the volume isThe airspeed is 0.5-3.0 h-1Hydrogen to oil volume ratio of 500 to 2000Nm3/m3。
3. The method for hydrocracking high-yield aviation kerosene according to claim 1, wherein the reaction conditions of said second reactor are: the pressure is 5-14 MPa, the temperature is 260-420 ℃, and the volume space velocity is 0.3-3.0 h-1Hydrogen to oil volume ratio of 500 to 2000Nm3/m3。
4. The method for hydrocracking aviation kerosene of claim 1, wherein said feedstock oil is at least one selected from the group consisting of light wax oil, straight-run diesel oil and coker diesel oil.
5. The method for hydrocracking aviation kerosene with high yield as claimed in claim 4, wherein the weight percentage of coking diesel oil in the raw oil is 0% -15%.
6. The method for hydrocracking aviation kerosene of claim 1, wherein the distillation range of said feedstock oil is 200 to 500 ℃.
7. The method of hydrocracking productive aviation kerosene of claim 1 wherein said first reactor is packed with a hydrofinishing catalyst.
8. The method of claim 1, wherein the upper layer of the first reactor is loaded with hydrofinishing catalyst and the lower layer is loaded with hydrocracking catalyst; the height ratio of the upper layer to the lower layer in the first reactor is 1: 10-10: 1.
9. The method of hydrocracking productive aviation kerosene of claim 1 wherein said second reactor is packed with a hydrocracking catalyst.
10. The method for hydrocracking aviation kerosene of claim 1, wherein the upper layer of the second reactor is filled with hydrocracking catalyst, the lower layer of the second reactor is filled with hydrofining catalyst, and the height ratio of the upper layer to the lower layer in the second reactor is 1: 10-10: 1.
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CN115637172A (en) * 2021-07-20 2023-01-24 中国石油天然气股份有限公司 Preparation method of military aviation kerosene

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