CN115637172A - Preparation method of military aviation kerosene - Google Patents
Preparation method of military aviation kerosene Download PDFInfo
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Abstract
The invention provides a preparation method of military aviation kerosene. The preparation method comprises the following steps: step S1, carrying out hydrogenation reaction on the normal line oil of the atmospheric and vacuum distillation device to obtain a hydrogenated system; s2, carrying out gas-liquid separation on the hydrogenated system to obtain a gas phase, an oil phase and a water phase; s3, fractionating the oil phase to obtain the military aviation kerosene, wherein the distillation range of the atmospheric and vacuum distillation device constant line oil is 140-260 ℃, and the density range is 780-790 kg/m 3 The fractionation treatment is carried out by adopting a single tower, and the gas-liquid separation process is completed in a cooler and a high-pressure three-phase separator. The reaction process is simple, the whole process can be directly carried out in some diesel hydrogenation devices, additional investment on equipment for producing military aviation kerosene is not needed, and the problems of complex preparation device and high operation cost of the military aviation kerosene are fundamentally solved.
Description
Technical Field
The invention relates to the technical field of military aviation kerosene preparation, in particular to a preparation method of military aviation kerosene.
Background
The aviation kerosene has the advantages of proper density, high heat value, good combustion performance, rapid, stable, continuous and complete combustion, small combustion area, less carbon deposition and difficult coking. The low-temperature fluidity is good, and the requirements of cold low-temperature areas and high-altitude flight on the fluidity of oil products can be met; the heat stability and the anti-oxidation stability are good; high cleanliness, no harmful substances such as mechanical impurities and water, low sulfur content, especially low mercaptan sulfur content, and less corrosion to machine parts.
With the rapid development of social economy and aviation technology, the demand of aviation kerosene is increasing day by day, and the requirements on product quality are also becoming stricter. Aviation kerosene is mainly used as a fuel for jet engines, and due to its special application places and environments, the requirements on the performance of aviation kerosene are very strict, and especially for military aviation kerosene, the requirements are more strict. It is required not only to have good low-temperature flow properties, higher net heat value and density, faster burning rate and higher burning degree, but also to have good stability (including storage stability and thermal oxidation stability).
At present, when aviation kerosene is prepared, a stripping tower is required to strip and remove corrosive components (mainly hydrogen sulfide) after hydrogenation, and then a fractionating tower is adopted to fractionate the bottom of the stripping tower, and the stripping tower has a complex structure and is difficult to control the operation conditions.
Disclosure of Invention
The invention mainly aims to provide a preparation method of military aviation kerosene, which aims to solve the problems of complicated device and difficult control of operation caused by stripping and removing hydrogen sulfide of the military aviation kerosene in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a preparation method of military aviation kerosene, the preparation method comprising: step S1, carrying out hydrogenation reaction on the normal line oil of the atmospheric and vacuum distillation device to obtain a hydrogenated system; s2, carrying out gas-liquid separation on the hydrogenated system to obtain a gas phase, an oil phase and a water phase; s3, fractionating the oil phase to obtain the military aviation kerosene, wherein the distillation range of the atmospheric and vacuum distillation device constant line oil is 140-260 ℃, and the density range is 780-790 kg/m 3 The fractionation treatment is carried out by adopting a single tower, and the gas-liquid separation process is completed in a cooler and a high-pressure three-phase separator.
Further, the temperature of the top of the fractionating tower in the fractionation treatment is maintained at 102 to 112 ℃, and the pressure of the top of the fractionating tower in the fractionation treatment is controlled at 60 to 100kPa.
Further, the bottom temperature of the fractionating tower in the fractionation treatment is controlled to 212 to 218 ℃.
Further, the cooler is an air cooler, and the gas-liquid separation process comprises the following steps: cooling the hydrogenated system in an air cooler to obtain a cooled system; and (3) carrying out three-phase separation on the cooled system in a high-pressure three-phase separator to obtain a gas phase, an oil phase and a water phase, wherein the outlet temperature of the air cooler is controlled to be 35-38 ℃, and the pressure in the high-pressure three-phase separator is controlled to be 7.2-7.3 MPa.
Further, the hydrogenation reaction is carried out in a hydrorefining reactor, the inlet temperature of the hydrorefining reactor is 240 to 260 ℃, the outlet temperature of the hydrorefining reactor is preferably 245 to 265 ℃, and the hydrogen partial pressure is preferably 6.7 to 7.59MPa, the hydrogen-oil volume ratio is 10.0 to 13.0 3 /m 3 And the liquid hourly space velocity is 0.9～1.2h -1 。
Further, the hydrorefining reactor is a fixed bed reactor.
Further, the pressure of the hydrogenation reaction is 6.7 to 7.5MPa.
Furthermore, the hydrogenation catalyst for the hydrogenation reaction is an RS-2100 type diesel oil hydrogenation catalyst.
Further, the preparation method further comprises the following steps: and returning at least part of the gas phase to the step S1 for recycling after desulfurization treatment.
Further, 20 to 40wt% of the above gas phase is subjected to desulfurization treatment.
By applying the technical scheme of the invention, the atmospheric and vacuum distillation device normal line oil with the distillation range and the density range in the range is used as the raw material to prepare the military aviation kerosene, and the atmospheric and vacuum distillation device normal line oil has the characteristics of direct material supply, low cost, moderate hydrocarbon composition and the like compared with the conventional preparation military aviation kerosene raw material (a straight distillation component obtained by directly cutting from an atmospheric distillation device and a fraction obtained by catalytically cracking and hydrocracking heavy oil), so that the aviation kerosene component can be obtained only by carrying out hydrogenation reaction on the atmospheric and vacuum distillation device normal line oil. Then, the process of gas-liquid separation is completed in the cooler and the high-pressure three-phase separator, and the hydrogen sulfide is separated out along with the gas phase in the process, so that the use of an additional stripping tower is avoided, and the equipment construction and operation cost is saved. The reaction process is simple, the whole process can be directly carried out in some diesel hydrogenation devices, and extra investment on equipment for producing military aviation kerosene is not needed, so that the problems of complex preparation device and high operation cost of the military aviation kerosene are fundamentally solved.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
As analyzed by the background technology, the problems of complicated device and difficult control of operation caused by hydrogen sulfide removal by steam stripping of military aviation kerosene exist in the prior art, and in order to solve the problems, the invention provides a preparation method of the military aviation kerosene.
In one exemplary embodiment of the present application, there is provided a process for preparing military aviation kerosene, the process comprising: step S1, performing hydrogenation reaction on normal line oil of an atmospheric and vacuum distillation unit to obtain a hydrogenated system; s2, carrying out gas-liquid separation on the hydrogenated system to obtain a gas phase, an oil phase and a water phase; s3, fractionating the oil phase to obtain military aviation kerosene, wherein the distillation range of the atmospheric and vacuum distillation device normal line oil is 140-260 ℃, and the density range is 780-790 kg/m 3 The fractionation treatment is carried out by adopting a single tower, and the gas-liquid separation process is completed in a cooler and a high-pressure three-phase separator.
The atmospheric and vacuum distillation device normal line oil with the distillation range and the density range in the range is used as a raw material for preparing military aviation kerosene, and compared with the conventional preparation method of the military aviation kerosene raw material (a direct distillation component obtained by directly cutting from an atmospheric distillation device and a fraction obtained by carrying out catalytic cracking and hydrocracking on heavy oil), the atmospheric and vacuum distillation device normal line oil has the characteristics of direct material supply, low cost, moderate hydrocarbon composition and the like, so that the aviation kerosene component can be obtained only by carrying out hydrogenation reaction on the atmospheric and vacuum distillation device normal line oil. Then through the process of accomplishing gas-liquid separation in cooler and high pressure three-phase separator, hydrogen sulfide goes out along with gas phase separation in this process to avoid the use of extra stripper, practiced thrift equipment construction and running cost. The reaction process is simple, the whole process can be directly carried out in some diesel hydrogenation devices, and extra investment on equipment for producing military aviation kerosene is not needed, so that the problems of complex preparation device and high operation cost of the military aviation kerosene are fundamentally solved.
In one embodiment of the present application, the overhead temperature of the fractionating tower is maintained at 102 to 112 ℃, and the overhead pressure of the fractionating tower is controlled to be in the range of 60 to 100kPa.
Controlling the top temperature and the top pressure of the fractionating tower within the above ranges helps to separate each component belonging to the military aviation kerosene from other components in the oil phase as much as possible, thereby obtaining the military aviation kerosene meeting the use requirements. In addition, naphtha is preferably temporarily reserved in an oil phase in the fractionation treatment process, so that part of gas stripping effect can be achieved in the fractionating tower by utilizing the naphtha, and the improvement of the quality of the military aviation kerosene is further facilitated.
In order to improve the yield of military aviation kerosene, the bottom temperature of the fractionating tower of the fractionating treatment is preferably controlled to be 212-218 ℃.
In an embodiment of the present application, the cooler is an air cooler, and the gas-liquid separation process includes: cooling the hydrogenated system in an air cooler to obtain a cooled system; and (3) carrying out three-phase separation on the cooled system in a high-pressure three-phase separator to obtain a gas phase, an oil phase and a water phase, wherein the outlet temperature of the air cooler is controlled to be 35-38 ℃, and the pressure in the high-pressure three-phase separator is controlled to be 7.2-7.3 MPa.
This application can make gaseous phase, oil phase and aqueous phase obtain fully separating through the outlet temperature of control air cooler and the pressure in the high-pressure three-phase separator to can avoid the use of extra strip tower, and then simplify the device, reduce equipment cost and cost of labor, wherein, the outlet temperature of control air cooler is 35 ~ 38 ℃, is favorable to follow-up separation of gaseous phase (hydrogen and hydrogen sulfide etc.) and liquid phase (oil phase and aqueous phase) in the high-pressure three-phase separator. Controlling the pressure in the high-pressure three-phase separator within the above range facilitates separation of hydrogen sulfide in the high-pressure three-phase separator as much as possible with the gas phase.
In order to improve the efficiency and effect of the hydrogenation reaction, the hydrogenation reaction is preferably carried out in a hydrofining reactor, the inlet temperature of the hydrofining reactor is 240-260 ℃, the outlet temperature of the hydrofining reactor is 245-265 ℃, the hydrogen partial pressure is 6.7-7.5 MPa, the volume ratio of hydrogen to oil is 10.0-13.0 3 /m 3 The liquid hourly space velocity is 0.9 to 1.2h -1 。
The fixed bed reactor has the advantages of simplicity and full contact between fluid and a catalyst, and the fixed bed reactor is preferably used as the hydrofining reactor in order to improve the hydrogenation reaction efficiency of the normal-line oil of the atmospheric and vacuum device.
In one embodiment of the present application, the pressure of the hydrogenation reaction is 6.7 to 7.5MPa.
The hydrogenation reaction is carried out at a certain temperature and pressure, and the pressure of the hydrogenation reaction is controlled within the range, so that the hydrogenation reaction can be better cooperated with the temperature in the hydrofining reactor, and the efficiency of the hydrogenation reaction is integrally improved.
In order to improve the efficiency of the hydrogenation reaction, the hydrogenation catalyst for the hydrogenation reaction is preferably an RS-2100 type diesel hydrogenation catalyst. Of course, other suitable catalysts can be added by those skilled in the art according to actual needs, and will not be described herein.
In order to make the hydrogenation process more economical, the preparation method preferably further comprises the following steps: and returning at least part of the gas phase to the step S1 for recycling after desulfurization treatment.
The percentage of the gas phase subjected to desulfurization treatment in the gas phase determines the purity of recycled recycle hydrogen, and the desulfurization treatment is preferably performed on 20-40 wt% of the gas phase, so that the purity of the recycle hydrogen is high, the complete hydrogenation reaction is promoted as much as possible, the gas-liquid separation process can be completed even if the hydrogenated system is subjected to simple separation in an air cooler and a high-pressure three-phase separator, and the defect of gas-liquid separation caused by gas stripping deficiency can be overcome.
The following description will explain advantageous effects of the present application with reference to specific examples.
Example 1
The distillation range is 145.0-247.0 deg.c, and the density is 785.5kg/m 3 The atmospheric and vacuum distillation unit of Liaoyang petrochemical company, inc. usually uses linear oil as raw material. The raw material is kept at a stable feeding amount of 80 mL/h and enters a fixed bed reactor (comprising 75g of RS-2100 type diesel hydrogenation catalyst), and the hydrogen partial pressure is controlled to be 6.8MPa, and the volume ratio of hydrogen to oil is controlled to be 10.5 Nm 1Nm 3 /m 3 The liquid hourly space velocity is 0.95h -1 The raw material components are lightened, and the reaction conditions are relatively mild, so that the high hydrogenation depth is not needed, the operation conditions of the circulating hydrogen compressor and the supplementary hydrogen compressor are observed and adjusted in time, the inlet temperature of the fixed bed reactor is controlled to be 246 ℃, the inlet temperature of the fixed bed reactor is controlled to be 260 ℃, the operation pressure of the reaction system is 6.8Mpa, and the outlet temperature of the fixed bed reactor is controlled to be 256 ℃ to carry out hydrogenation reaction for 0.6h, thereby obtaining a hydrogenated system.
And (3) passing the hydrogenated system through certain heat exchange equipment, then cooling the hydrogenated system in an air cooler, and controlling the outlet temperature of the air cooler to be 35 ℃ to obtain a cooled system. And (3) the cooled system enters a high-pressure three-phase separator, and the pressure in the high-pressure three-phase separator is controlled to be 7.2MPa, so that a gas phase, an oil phase and a water phase are obtained. And desulfurizing 20wt% of the gas phase in a recycle hydrogen desulfurization tower, and returning to the hydrogenation reaction for continuing the hydrogenation reaction. And (3) the oil phase enters a single fractionating tower to be fractionated for 0.5h, the bottom temperature of the fractionating tower is controlled to be 216.19 ℃, the top temperature of the fractionating tower is controlled to be 106.97 ℃, and the top pressure of the fractionating tower is controlled to be 89.27kPa, so that the military aviation kerosene product is obtained, wherein the quality parameters are shown in Table 1.
Example 2
The distillation range is 147.1-248.4 ℃, and the density is 784.7kg/m 3 The atmospheric and vacuum distillation unit of Liaoyang petrochemical company, inc. usually uses linear oil as raw material. The feed was maintained at a steady feed rate of 80 mL/hour. And (2) feeding the mixture into a fixed bed reactor (comprising 75g of RS-2100 diesel hydrogenation catalyst), and controlling the hydrogen partial pressure to be 6.9MPa and the hydrogen-oil volume ratio to be 11.0 3 /m 3 The liquid hourly space velocity is 0.95h -1 And because the components of the raw materials become light and the reaction conditions are mild, the operation conditions of the recycle hydrogen compressor and the make-up hydrogen compressor can be observed and adjusted in time without too high hydrogenation depth. And controlling the inlet temperature of the fixed bed reactor to be 246 ℃, the inlet temperature of the fixed bed reactor to be 260 ℃, the operating pressure of a reaction system to be 6.8Mpa and the outlet temperature of the fixed bed reactor to be 256 ℃ to carry out hydrogenation reaction for 0.6h, thus obtaining a hydrogenated system.
And (3) after hydrogenation, the temperature of the system reaches about 100 ℃ after passing through certain heat exchange equipment, and then the system is cooled in an air cooler, and the outlet temperature of the air cooler is controlled to be 35 ℃ to obtain a cooled system. And (3) the cooled system enters a high-pressure three-phase separator, and the pressure in the high-pressure three-phase separator is controlled to be 7.2MPa, so that a gas phase, an oil phase and a water phase are obtained. And desulfurizing 20wt% of the gas phase in a recycle hydrogen desulfurization tower, and returning to the hydrogenation reaction for continuing the hydrogenation reaction. And (3) the oil phase enters a single fractionating tower to be fractionated for 0.5h, the bottom temperature of the fractionating tower is controlled to be 216.34 ℃, the top temperature of the fractionating tower is controlled to be 107.12 ℃, and the top pressure of the fractionating tower is controlled to be 88.46kPa, so that the military aviation kerosene product is obtained, wherein the quality parameters are shown in Table 1.
Example 3
The distillation range is 144.5-243.2 ℃, and the density is 783.7kg/m 3 The atmospheric and vacuum distillation unit of Liaoyang petrochemical company, inc. usually uses linear oil as raw material. The raw material is kept at a stable feeding amount of 80 mL/h and enters a fixed bed reactor (comprising 75g of RS-2100 type diesel hydrogenation catalyst), and the hydrogen partial pressure is controlled to be 6.8MPa, and the volume ratio of hydrogen to oil is controlled to be 11.5 Nm 1Nm 3 /m 3 The liquid hourly space velocity is 1.0h -1 And because the components of the raw materials become light and the reaction conditions are mild, the operation conditions of the recycle hydrogen compressor and the make-up hydrogen compressor can be observed and adjusted in time without too high hydrogenation depth. And (3) controlling the inlet temperature of the fixed bed reactor to be 246 ℃, the inlet temperature of the fixed bed reactor to be 260 ℃, the operating pressure of a reaction system to be 6.8Mpa and the outlet temperature of the fixed bed reactor to be 256 ℃ to carry out hydrogenation reaction for 0.7h to obtain a hydrogenated system.
And (3) passing the hydrogenated system through certain heat exchange equipment, then cooling the hydrogenated system in an air cooler, and controlling the outlet temperature of the air cooler to be 35 ℃ to obtain a cooled system. And (3) the cooled system enters a high-pressure three-phase separator, and the pressure in the high-pressure three-phase separator is controlled to be 7.2MPa, so that a gas phase, an oil phase and a water phase are obtained. And desulfurizing 20wt% of the gas phase in a recycle hydrogen desulfurization tower, and returning to the hydrogenation reaction for continuing the hydrogenation reaction. And (3) the oil phase enters a single fractionating tower to be fractionated for 0.5h, the temperature of the bottom of the fractionating tower is controlled to be 216.13 ℃, the temperature of the top of the fractionating tower is controlled to be 109.02 ℃, and the pressure of the top of the fractionating tower is controlled to be 88.91kPa, so that the military aviation kerosene product is obtained, and the quality parameters are shown in the table 1.
Example 4
The distillation range is 145.4-248.0 ℃, and the density is 784.2kg/m 3 The atmospheric and vacuum distillation device of Liaoyang petrochemical company usually uses linear oil as raw material. The raw material is kept at a stable feeding amount of 80 mL/h and enters a fixed bed reactor (comprising 75g of RS-2100 type diesel hydrogenation catalyst), and the hydrogen partial pressure is controlled to be 6.9MPa, and the hydrogen-oil volume ratio is controlled to be 11.5 Nm 1Nm 3 /m 3 The liquid hourly space velocity is 1.0h -1 And because the components of the raw materials become light and the reaction conditions are mild, the operation conditions of the recycle hydrogen compressor and the make-up hydrogen compressor can be observed and adjusted in time without too high hydrogenation depth. And controlling the inlet temperature of the fixed bed reactor to be 246 ℃, the inlet temperature of the fixed bed reactor to be 260 ℃, the operating pressure of a reaction system to be 6.8Mpa and the outlet temperature of the fixed bed reactor to be 256 ℃ to carry out hydrogenation reaction for 0.6h to obtain a hydrogenated system.
And (3) after hydrogenation, the temperature of the system reaches about 100 ℃ after passing through certain heat exchange equipment, and then the system is cooled in an air cooler, and the outlet temperature of the air cooler is controlled to be 35 ℃ to obtain a cooled system. And (3) the cooled system enters a high-pressure three-phase separator, and the pressure in the high-pressure three-phase separator is controlled to be 7.2MPa, so that a gas phase, an oil phase and a water phase are obtained. And desulfurizing 20wt% of the gas phase in a recycle hydrogen desulfurization tower, and returning to the hydrogenation reaction for continuing the hydrogenation reaction. And (3) the oil phase enters a single fractionating tower to be fractionated for 0.5h, the temperature of the bottom of the fractionating tower is controlled to be 216.32 ℃, the temperature of the top of the fractionating tower is controlled to be 107.74 ℃, and the pressure of the top of the fractionating tower is controlled to be 89.14kPa, so that the military aviation kerosene product is obtained, and the quality parameters of the military aviation kerosene product are shown in the table 1.
Example 5
Example 5 differs from example 1 in that the distillation range is 145.0 to 260.0 ℃ and the density is 790kg/m 3 The atmospheric and vacuum distillation unit of Liaoyang petrochemical company takes constant linear oil as raw material to finally obtain military aviation kerosene products, and the quality parameters are shown in Table 1.
Example 6
Example 6 differs from example 1 in that,
the hydrogen partial pressure in the hydrogenation reaction is 6.7MPa, and the military aviation kerosene product is finally obtained, wherein the quality parameters are shown in Table 1.
Example 7
Example 7 differs from example 1 in that,
the hydrogen partial pressure in the hydrogenation reaction is 7.5MPa, and the military aviation kerosene product is finally obtained, wherein the quality parameters are shown in Table 1.
Example 8
Example 8 differs from example 1 in that,
the hydrogen partial pressure in the hydrogenation reaction is 6.5MPa, and the military aviation kerosene product is finally obtained, wherein the quality parameters are shown in Table 1.
Example 9
Example 9 differs from example 1 in that,
the volume ratio of hydrogen to oil in the hydrogenation reaction is 10 Nm 3 /m 3 Finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in table 1.
Example 10
Example 10 differs from example 1 in that,
the volume ratio of hydrogen to oil in the hydrogenation reaction is 13.0 3 /m 3 Finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in the table 1.
Example 11
Example 11 differs from example 1 in that,
the volume ratio of hydrogen to oil in the hydrogenation reaction is 9.0 3 /m 3 Finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in the table 2.
Example 12
Example 12 differs from example 1 in that,
the liquid hourly space velocity in the hydrogenation reaction is 0.9h -1 Finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in a table 2.
Example 13
Example 13 differs from example 1 in that,
the liquid hourly space velocity in the hydrogenation reaction is 1.2h -1 Finally obtaining the military aviation kerosene product with the qualityThe parameters are shown in Table 2.
Example 14
Example 14 differs from example 1 in that,
the liquid hourly space velocity in the hydrogenation reaction is 1.25h -1 Finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in a table 2.
Example 15
Example 15 differs from example 1 in that,
and controlling the tower bottom temperature of the fractionating tower to be 212 ℃, the tower top temperature of the fractionating tower to be 112 ℃, and the tower top pressure of the fractionating tower to be 100Pa, and finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in Table 2.
Example 16
Example 16 differs from example 1 in that,
and controlling the tower bottom temperature of the fractionating tower to be 218 ℃, the tower top temperature of the fractionating tower to be 102 ℃ and the tower top pressure of the fractionating tower to be 60Pa, and finally obtaining the military aviation kerosene product, wherein the quality parameters are shown in Table 2.
Example 17
Example 17 differs from example 1 in that,
the inlet temperature range of the hydrofining reactor is 240 ℃, the outlet temperature range of the hydrofining reactor is 245 ℃, and the military aviation kerosene product is finally obtained, wherein the quality parameters are shown in Table 2.
Example 18
Example 18 differs from example 1 in that,
the inlet temperature range of the hydrofining reactor is 260 ℃, the outlet temperature range of the hydrofining reactor is 265 ℃, and the military aviation kerosene product is finally obtained, and the quality parameters of the military aviation kerosene product are shown in table 2.
Example 19
Example 19 differs from example 1 in that,
and (3) carrying out desulfurization treatment on 30wt% of gas phase to finally obtain a military aviation kerosene product, wherein the quality parameters are shown in Table 2.
Example 20
Example 20 differs from example 1 in that,
and (3) carrying out desulfurization treatment on 40wt% of gas phase to finally obtain a military aviation kerosene product, wherein the quality parameters are shown in Table 2.
Example 21
Example 21 differs from example 1 in that,
and (3) carrying out desulfurization treatment on 10wt% of gas phase to finally obtain a military aviation kerosene product, wherein the quality parameters are shown in Table 2.
TABLE 1
TABLE 2
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the atmospheric and vacuum distillation device normal line oil with the distillation range and the density range in the range is used as a raw material for preparing military aviation kerosene, and compared with the conventional preparation military aviation kerosene raw material (a straight-run component obtained by directly cutting from an atmospheric distillation device and a fraction obtained by carrying out catalytic cracking and hydrocracking on heavy oil), the atmospheric and vacuum distillation device normal line oil has the characteristics of direct material supply, low cost, moderate hydrocarbon composition and the like, so that the aviation kerosene component can be obtained only by carrying out hydrogenation reaction on the atmospheric and vacuum distillation device normal line oil. Then, the process of gas-liquid separation is completed in the cooler and the high-pressure three-phase separator, and the hydrogen sulfide is separated out along with the gas phase in the process, so that the use of an additional stripping tower is avoided, and the equipment construction and operation cost is saved. The reaction process is simple, the whole process can be directly carried out in some diesel hydrogenation devices, and extra investment on equipment for producing military aviation kerosene is not needed, so that the problems of complex preparation device and high operation cost of the military aviation kerosene are fundamentally solved.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A preparation method of military aviation kerosene is characterized by comprising the following steps:
step S1, carrying out hydrogenation reaction on the normal line oil of the atmospheric and vacuum distillation device to obtain a hydrogenated system;
s2, carrying out gas-liquid separation on the hydrogenated system to obtain a gas phase, an oil phase and a water phase;
s3, fractionating the oil phase to obtain the military aviation kerosene,
wherein the distillation range of the normal linear oil of the atmospheric and vacuum distillation device is 140-260 ℃, and the density range is 780-790 kg/m 3 The fractionation treatment is carried out by adopting a single tower, and the gas-liquid separation process is completed in a cooler and a high-pressure three-phase separator.
2. The production method according to claim 1, wherein the overhead temperature of the fractionating tower is maintained at 102 to 112 ℃ and the overhead pressure of the fractionating tower is controlled at 60 to 100kPa.
3. The method according to claim 1, wherein the bottom temperature of the fractionating tower in the fractionating treatment is controlled to 212 to 218 ℃.
4. The method as claimed in claim 1, wherein the cooler is an air cooler, and the gas-liquid separation process comprises:
cooling the hydrogenated system in an air cooler to obtain a cooled system;
carrying out three-phase separation on the cooled system in a high-pressure three-phase separator to obtain the gas phase, the oil phase and the water phase,
wherein the outlet temperature of the air cooler is controlled to be 35-38 ℃, and the pressure in the high-pressure three-phase separator is controlled to be 7.2-7.3 MPa.
5. The production method according to claim 1, wherein the hydrogenation reaction is carried out in a hydrofining reactor, the inlet temperature of the hydrofining reactor is in a range of 240 to 260 ℃, preferably the outlet temperature of the hydrofining reactor is in a range of 245 to 265 ℃, preferably the hydrogenation reaction has a hydrogen partial pressure of 6.7 to 7.5MPa, a hydrogen-oil volume ratio of 10.0 to 13.0 nm 1nm 3 /m 3 The liquid hourly space velocity is 0.9 to 1.2h -1 。
6. The production method according to claim 5, wherein the hydrofinishing reactor is a fixed bed reactor.
7. The production method according to claim 1, wherein the pressure of the hydrogenation reaction is 6.7 to 7.5MPa.
8. The method of claim 1, wherein the hydrogenation catalyst for the hydrogenation reaction is a diesel hydrogenation catalyst of RS-2100 type.
9. The method of claim 1, further comprising: and returning at least part of the gas phase to the step S1 for recycling after desulfurization treatment.
10. The production method according to claim 9, wherein 20 to 40wt% of the gas phase is subjected to the desulfurization treatment.
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| 吕娜: "航空煤油加氢精制装置工艺设计", CNKI优秀硕士学位论文全文库 工程科技II辑, no. 8, pages 18 - 25 * |
| 崔小琴等: "常一线油管式固定床选择性液相加氢生产喷气燃料的研究", 石油炼制与化工, vol. 49, no. 8, pages 66 - 69 * |
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