CN108913203B - Production process of No. 10 military diesel oil and No. 5 industrial white oil - Google Patents
Production process of No. 10 military diesel oil and No. 5 industrial white oil Download PDFInfo
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- CN108913203B CN108913203B CN201810616793.8A CN201810616793A CN108913203B CN 108913203 B CN108913203 B CN 108913203B CN 201810616793 A CN201810616793 A CN 201810616793A CN 108913203 B CN108913203 B CN 108913203B
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes 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
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/14—White oil, eating oil
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Abstract
The invention discloses a production process of No. 10 military diesel oil and No. 5 industrial white oil, which comprises the following steps: (1) the extraction port of a diesel side stripper T3 is moved upwards, and after being treated by a diesel side stripper T3, the military diesel oil of No. 10 is obtained after heat exchange and cooling; (2) adding an industrial white oil side line extraction outlet and a return outlet in a product fractionating tower T1, enabling an industrial white oil material extracted from a fractionating tower T1 to automatically flow into a newly-added industrial white oil material side line stripping tower T4, after being stripped by a white oil material side line stripping tower T4, returning the gas at the top of the white oil material side line stripping tower T4 to the fractionating tower T1, extracting a product at the bottom of the white oil material side line stripping tower T4, then entering a dewatering tank V1 for vacuum dewatering, and then carrying out pressurization, heat exchange and cooling treatment to obtain the 5# industrial white oil. The process can produce military-10 diesel oil and industrial 5# white oil simultaneously, and the obtained military-10 diesel oil and high-quality industrial 5# white oil have high initial boiling point, high yield and high quality reaching the high-grade product.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a production process of No. 10 military diesel oil and No. 5 industrial white oil.
Background
As shown in fig. 1, in the prior art, a process for preparing industrial white oil is adopted in which a raw material is cut by a device fractionation system, the raw material is usually the produced oil obtained by processing vacuum wax oil from an atmospheric and vacuum device by a hydrocracking device system, the process is to cut the produced oil from a reactor of the hydrocracking device by a fractionating tower T1, heavy naphtha is discharged from the top of T1, aviation kerosene is discharged from a aviation kerosene side stripper T2, aviation kerosene is discharged from a diesel oil side stripper T3, and tail oil is discharged from a diesel oil side stripper T1. The original diesel oil is extracted from the 28 th layer of the diesel oil side stripper T3, so the position of the extraction port is far away from the bottom of the tower, the extraction temperature is low, 5# industrial white oil with the initial boiling point reaching about 250 ℃ is produced, the appearance is still kerosene-flavored, and the appearance is not bright and has a large difference from high-quality industrial white oil. Therefore, the hydrocracking unit in the prior art does not have a side line for specially producing the 5# industrial white oil, and can only produce the white oil by utilizing a diesel side stripping tower T3. In addition, the diesel oil produced by the existing diesel oil side stripper T3 has high colloid content, and can not be used as-10 # military diesel oil.
Therefore, in order to improve the quality of the industrial white oil and the diesel oil and enable the device to simultaneously produce the-10 # military diesel oil and the high-quality 5# industrial white oil, the prior hydrocracking process needs to be improved so as to simultaneously produce the-10 # military diesel oil and the high-quality 5# industrial white oil.
Disclosure of Invention
The invention aims to provide a production process of No. 10 military diesel oil and high-quality industrial white oil, which can simultaneously produce No. 10 military diesel oil and No. 5 high-quality industrial white oil, and the obtained No. 10 military diesel oil and No. 5 industrial white oil have high initial boiling point, high yield and high quality reaching the top grade.
The above purpose of the invention is realized by the following technical scheme: a production process of No. 10 military diesel oil and No. 5 industrial white oil comprises the following steps:
(1) pretreating the hydrocracking produced oil, then feeding the pretreated produced oil into a fractionating tower T1 with 50-60 layers of trays for fractionation, forming a diesel oil extraction port at the 16 th-18 th layer of tray of the fractionating tower T1, wherein a diesel oil extraction pipeline is arranged at the diesel oil extraction port, the diesel oil extraction pipeline is connected with a diesel oil side-draw stripper T3, the diesel oil extracted from the diesel oil extraction port flows into a diesel oil side-draw stripper T3 through the diesel oil extraction pipeline, after the diesel oil side-draw stripper T3 is stripped, oil gas at the top of the diesel oil side-draw stripper T3 returns to the 14 th-15 th layer of tray of the fractionating tower T1, and after the product at the bottom of the diesel oil side-draw stripper T3 is extracted, heat exchange and cooling treatment are carried out to obtain No. 10 military diesel oil;
(2) adding a white oil material extraction port at the 34 th-36 th layer tray of the fractionating tower T1, wherein a white oil material extraction pipeline is arranged at the white oil material extraction port, the white oil material extraction pipeline is connected with a white oil material side-line stripping tower T4, the white oil material extracted from the white oil material extraction port flows into the white oil material side-line stripping tower T4 through the white oil material extraction pipeline, after being stripped by the white oil material side-line stripping tower T4, the gas at the top of the white oil material side-line stripping tower T4 returns to the 32 th-33 th layer tray of the fractionating tower T1, the product at the bottom of the white oil material side-line stripping tower T4 is extracted and then enters a dehydrating tank V1 for vacuum dehydration, and then the 5# industrial white oil is obtained through pressurization, heat exchange and cooling treatment.
In the production process of the No. 10 military diesel oil and the No. 5 industrial white oil:
the pretreatment in the step (1) is hydrogen sulfide removal treatment; the number of trays of the diesel side stripper T3 is preferably 14-20.
And (2) pumping a product at the bottom of the diesel side stripper T3 in the step (1) by using a centrifugal pump, and then carrying out heat exchange and cooling treatment to obtain No. 10 military diesel, wherein the heat exchange treatment comprises the steps of recovering heat in the product by using the product pumped by the centrifugal pump through a steam generator, a heat exchanger and an air cooler, and carrying out heat exchange, cooling and cooling treatment to obtain No. 10 military diesel, wherein self-produced steam generated by the steam generator is used as superheated steam of a fractionating tower T1, a diesel side stripper T3 and a white oil side stripper T4.
The superheated steam used in the diesel side stripper T3 in the step (1) and used in the white oil side stripper in the step (2) is superheated low-pressure steam with the temperature of 380-400 ℃ and the pressure of 0.3-0.6 MPa, the superheated low-pressure steam is derived from self-generated steam generated by the steam generator, and the heat source of the steam generator is derived from heat of products at the bottom of the diesel side stripper T3 and heat generated by middle-stage reflux.
Wherein the low-pressure steam is self-produced by the steam generator, then can be preferably heated into superheated steam by a convection section of the fractionating furnace, the preselection of a heat source of the steam generator is the heat of diesel oil in the device and a heat exchanger reflowing from the middle section, and the deaerated water of the steam generator is desalted water from an external device, deaerated by a deaerator in the device and then sent into the steam generator by a feed water pump.
The distillation range of the No. 10 military diesel oil produced in the step (1) of the invention is 214-302 ℃.
The diesel oil which is extracted from the side line extraction position of a fractionating tower T1 and moved upwards is treated by a diesel oil side line stripping tower T3, light components in the diesel oil can be removed, the flash point of the diesel oil is improved, the diesel oil which is treated by the diesel oil side line stripping tower T3 is extracted from the bottom of the diesel oil side line stripping tower T3 through a centrifugal pump, then the heat in the diesel oil is recovered through a steam generator, a heat exchanger and an air cooler, and after heat exchange and temperature reduction, the No. 10 military diesel oil is obtained.
The number of trays of the white oil side stripper T4 in the step (2) is preferably 14-20.
And (3) preferably pumping a product at the bottom of the white oil side-line stripping tower T4 in the step (2) by adopting a centrifugal pump, then feeding the product into a dewatering tank V1 for vacuum dewatering, wherein a steam jet vacuum-pumping system is arranged at the top of the dewatering tank V1, the vacuum-pumped oil gas at the top of the dewatering tank V1 returns to the white oil side-line stripping tower T4, the white oil which is subjected to flash evaporation and dewatering by the steam jet vacuum-pumping system at the bottom of the dewatering tank V1 is subjected to pressurization, heat exchange and cooling treatment to obtain the industrial white oil, and the vacuum degree in the vacuum dewatering tank V1 is-0.08 to-0.03 MPa.
The heat exchange in the step (2) of the invention adopts twice heat exchange, wherein the first heat exchange is heat exchange with desalted water (desalted water is out of the boundary area of the device and can be low-temperature desalted water in other processes), the temperature of a product before heat exchange is 220-250 ℃, the temperature of a product after heat exchange is 140-160 ℃, the temperature before heat exchange of desalted water is 60-80 ℃, the temperature after heat exchange is 100-104 ℃, the temperature of a product after heat exchange is ensured to be not higher than 160 ℃ after heat exchange, the second heat exchange is heat exchange with a lean solvent (lean solvent is out of the boundary area of the device and can be low-temperature lean solvent in other processes), the temperature before heat exchange of the product is 140-160 ℃, the temperature after heat exchange is 80-100 ℃, the temperature before heat exchange of the lean solvent is 45-50 ℃, and the temperature after heat exchange is 50-60 ℃.
After heat exchange, firstly, the temperature of the industrial white oil before entering the air cooler can be guaranteed to be not higher than 160 ℃, energy-saving effect is achieved, secondly, after heat exchange with desalted water, the temperature of the desalted water reaches the deoxygenation temperature, and the deoxygenation steam consumption of the device can be reduced (the deoxygenation steam is steam of 1.0MPa of the system, and is used for deoxygenation of the desalted water).
In addition, the second heat exchange and the lean solvent heat exchange are carried out, the temperature of the industrial white oil before heat exchange is 140-160 ℃, and the temperature of the industrial white oil after heat exchange is 80-100 ℃. The lean solvent can come from an amine liquid main pipe of an external system, the temperature before heat exchange is about 45-50 ℃, the temperature after heat exchange is about 50-60 ℃, and the method mainly improves the temperature of the lean solvent entering the circulating hydrogen desulfurization tower, ensures that the temperature difference between the lean solvent and the circulating hydrogen of the device exists, and prevents hydrocarbons in the circulating hydrogen from being largely condensed in the lean liquid to cause the amine liquid of the circulating hydrogen desulfurization tower to foam.
In the step (2), a booster pump is preferably adopted for pressurizing, an air cooler is preferably adopted for cooling in the step (2), and the temperature of the 5# industrial white oil after being cooled by the air cooler is 50-60 ℃.
The distillation range of the 5# industrial white oil obtained in the step (2) of the invention is 280-345 ℃.
The industrial white oil material which is extracted from the side line of the fractionating tower T1 and is discharged from the side line close to the bottom of the fractionating tower T1 after moving downwards is treated by a white oil side line stripping tower T4, so that light components in the industrial white oil material can be removed, the flash point of the industrial white oil material is improved, meanwhile, the industrial white oil material is dehydrated by a dehydration tank V1 arranged at the bottom outlet of the white oil material side line stripping tower T4, the obtained product is extracted by a centrifugal pump, heat in the industrial white oil is recovered by a heat exchanger and an air cooler, and the high-quality industrial white oil is obtained after heat exchange and temperature reduction.
The invention has the following advantages:
(1) the initial boiling point of the 5# industrial white oil produced by the process can reach about 280 ℃, while the initial boiling point of the 5# industrial white oil produced by the prior art is about 250 ℃, the problems that the 5# industrial white oil has kerosene smell and the appearance is not bright enough can be solved, and the 5# industrial white oil with high quality can be produced;
(2) the initial boiling point of military diesel oil No. 10 produced by the process is about 217 ℃, the final boiling point is about 300 ℃, while the initial boiling point of military diesel oil No. 10 produced by the conventional method is only about 160 ℃, and the final boiling point is about 290 ℃, the process can effectively solve the problems that the yield is low and most of diesel oil components move down to the tail oil during the production of military diesel oil No. 10, and can greatly reduce the colloid in the diesel oil, and the military diesel oil can be used as military diesel oil No. 10.
Drawings
FIG. 1 is a flow diagram of a prior art process for producing diesel and technical white oil using a fractionator;
FIG. 2 is a diagram of the production process of military No. 10 diesel fuel and high quality No. 5 industrial white oil in an embodiment of the present invention.
Detailed Description
Example 1
As shown in figure 2, the production process of No. 10 military diesel oil and high-quality industrial white oil comprises the following steps:
(1) pretreating hydrocracking produced oil, then, introducing the pretreated produced oil into a fractionating tower T1 with 54 layers of trays for fractionation, forming a diesel oil extraction port at the 17 th layer tray of the fractionating tower T1, arranging a diesel oil extraction pipeline at the diesel oil extraction port, connecting the diesel oil extraction pipeline with a diesel oil side stripper T3, allowing diesel oil extracted from the diesel oil extraction port to flow into a diesel oil side stripper T3 through the diesel oil extraction pipeline, stripping the diesel oil by the diesel oil side stripper T3, returning oil gas at the top of the diesel oil side stripper T3 to a 15 th layer tray of the fractionating tower T1, extracting a product at the bottom of the diesel oil side stripper T3, and then, carrying out heat exchange and cooling treatment to obtain No. 10 military diesel oil;
(2) a white oil material extraction port is additionally arranged at the 35 th tray of the fractionating tower T1, a white oil material extraction pipeline is arranged at the white oil material extraction port, the white oil material extraction pipeline is connected with a white oil material side-line stripping tower T4, white oil material extracted from the white oil material extraction port flows into the white oil material side-line stripping tower T4 through the white oil material extraction pipeline, after being stripped by the white oil material side-line stripping tower T4, the gas at the top of the white oil material side-line stripping tower T4 returns to the 33 th tray of the fractionating tower T1, and the product at the bottom of the white oil material side-line stripping tower T4 is extracted and then enters a dehydrating tank V1 for vacuum dehydration, and then the 5# industrial white oil is obtained through pressurization, heat exchange and cooling treatment.
Wherein the pretreatment is hydrogen sulfide removal treatment; the number of trays of the diesel side stripper T3 was specifically 16.
And (2) pumping a product at the bottom of the diesel side-line stripper T3 in the step (1) by using a centrifugal pump, and then carrying out heat exchange and cooling treatment to obtain No. 10 military diesel, wherein the heat exchange treatment comprises the steps of recovering heat in the product pumped by the centrifugal pump through a steam generator, a heat exchanger and an air cooler, and carrying out heat exchange, cooling and cooling treatment to obtain No. 10 military diesel, wherein self-produced steam generated by the steam generator is used as superheated steam of a fractionating tower T1, a diesel side-line stripper T3 and a white oil side-line stripper T4.
The superheated steam used in the diesel side stripper T3 in the step (1) and the superheated low-pressure steam used in the white oil side stripper in the step (2) is superheated low-pressure steam with the temperature of 400 ℃ and the pressure of 0.35MPa, the superheated low-pressure steam is derived from self-produced steam generated by a steam generator, and the heat source of the steam generator is derived from the heat of products at the bottom of the diesel side stripper T3 and the heat generated by middle-stage reflux.
Wherein low pressure steam is from producing through steam generator, later can become superheated steam through fractional distillation furnace convection current section heating, and steam generator's heat source preselection is the heat of the diesel oil in the device and the heat exchanger of middle section backward flow, and wherein steam generator's deoxidization water is that the demineralized water that comes from the external device is after the deoxidization of the oxygen-eliminating device in the device, sends into steam generator through the feed-water pump.
The distillation range of the produced military-10 diesel oil is 214-300 ℃.
The diesel oil which is extracted from the side extraction position of a fractionating tower T1 and moved upwards is treated by a diesel oil side stripper T3, so that light components in the diesel oil can be removed, the flash point of the diesel oil is improved, the diesel oil which is treated by the diesel oil side stripper T3 is extracted from the bottom of a diesel oil side stripper T3 through a centrifugal pump, then the heat in the diesel oil is recovered through a steam generator, a heat exchanger and an air cooler, and after heat exchange and temperature reduction, the No. 10 military diesel oil is obtained.
The number of trays in the white oil side stripper T4 in step (2) is preferably 16.
And (3) preferably pumping a product at the bottom of the white oil side line stripping tower T4 in the step (2) by adopting a centrifugal pump, then feeding the product into a dewatering tank V1 for vacuum dewatering, wherein a steam jet vacuum-pumping system is arranged at the top of the dewatering tank V1, the vacuum-pumped oil gas at the top of the dewatering tank V1 returns to the white oil side line stripping tower T4, and the white oil flashed and dewatered by the steam jet vacuum-pumping system at the bottom of the dewatering tank V1 is subjected to pressurization, heat exchange and cooling treatment to obtain industrial white oil, wherein the vacuum degree in the vacuum dewatering tank V1 is-0.03 MPa.
In the step (2), two heat exchanges are adopted for heat exchange, wherein the first heat exchange is heat exchange with desalted water (desalted water is out of a device boundary area and can be low-temperature desalted water in other processes), the temperature of a product before heat exchange is 220-250 ℃, the temperature of the product after heat exchange is 140-160 ℃, the temperature of the product before heat exchange is 60-80 ℃, the temperature after heat exchange is 100-104 ℃, the temperature of the product after heat exchange is not higher than 160 ℃ after heat exchange, the second heat exchange is heat exchange with a lean solvent (the lean solvent is out of the device boundary area and can be a low-temperature lean solvent in other processes), the temperature of the product before heat exchange is 140-160 ℃, the temperature after heat exchange is 80-100 ℃, the temperature of the lean solvent before heat exchange is 45-50 ℃, and the temperature after heat exchange is 50-60 ℃.
After heat exchange, firstly, the temperature of the industrial white oil before entering the air cooler can be guaranteed to be not higher than 160 ℃, energy-saving effect is achieved, secondly, after heat exchange with desalted water, the temperature of the desalted water reaches the deoxygenation temperature, and the deoxygenation steam consumption of the device can be reduced (the deoxygenation steam is steam of 1.0MPa of the system, and is used for deoxygenation of the desalted water).
In addition, the second heat exchange and the lean solvent heat exchange are carried out, the temperature of the industrial white oil before the heat exchange is 140-160 ℃, and the temperature of the industrial white oil after the heat exchange is 80-100 ℃. The lean solvent can come from an amine liquid main pipe of an external system, the temperature before heat exchange is about 45-50 ℃, the temperature after heat exchange is about 50-60 ℃, and the method mainly improves the temperature of the lean solvent entering a recycle hydrogen desulfurization tower, ensures that the lean solvent and the recycle hydrogen of the device have temperature difference, and prevents hydrocarbons in the recycle hydrogen from being largely condensed in the lean solution to cause amine liquid foaming of the recycle hydrogen desulfurization tower.
Pressurizing in the step (2) by using a booster pump, cooling in the step (2) by using an air cooler, and cooling the 5# industrial white oil by using the air cooler to reach the temperature of 50-60 ℃.
The distillation range of the 5# industrial white oil obtained in the step (2) of the invention is 280-345 ℃.
The industrial white oil material which is extracted from the side line of the fractionating tower T1 and is discharged from the side line close to the bottom of the fractionating tower T1 after moving downwards is treated by a white oil side line stripping tower T4, so that light components in the industrial white oil material can be removed, the flash point of the industrial white oil material is improved, meanwhile, the industrial white oil material is dehydrated by a dehydration tank V1 arranged at the bottom outlet of the white oil material side line stripping tower T4, the obtained product is extracted by a centrifugal pump, heat in the industrial white oil is recovered by a heat exchanger and an air cooler, and the high-quality No. 5 industrial white oil is obtained after heat exchange and temperature reduction.
To sum up, the key points of the production process of the military diesel oil No. 10 and the industrial white oil No. 5 can be summarized as follows:
(1) the diesel side stripper T3 withdrawal was located at the tray of the 17 th stage of the fractionation column T1.
(2) An industrial white oil side line is additionally arranged at the 35 th layer of a tower tray of a product fractionating tower T1 for extraction, and a corresponding T41 base of an industrial white oil side line stripping tower, flash dehydration tanks (namely V11 dehydration tanks), 2 pumps (centrifugal pumps) (one for one use) and 2 heat exchangers are additionally arranged.
The invention relates to a production process of No. 10 military diesel oil and No. 5 industrial white oil, which comprises the following main processes:
(1) moving an extraction port of a diesel side stripper T3 upwards, treating the diesel side stripper T3, exchanging heat through a steam generator, a heat exchanger and an air cooler, and cooling to obtain No. 10 military diesel;
(2) and a side line extraction outlet and a return outlet of the industrial white oil are added to the product fractionating tower T1. The industrial white oil extracted from the fractionating tower T1 automatically flows into a newly added industrial white oil side stripper T4, 0.35MPa of superheated steam at 400 ℃ is introduced into the bottom of the industrial white oil side stripper T4 for stripping;
(3) the overhead gas of the industrial white oil side-line stripping tower T4 returns to the product fractionating tower T1, the liquid phase at the bottom of the industrial white oil side-line stripping tower T4 enters a flash evaporation (vacuum) dehydration tank V1, and the top of the flash evaporation dehydration tank is provided with a 1.0MPa steam injection vacuumizing system;
(4) the flash evaporated and dehydrated industrial white oil material is pressurized by a newly-added industrial white oil material centrifugal pump (one is prepared), enters a newly-added desalted water/industrial white oil material heat exchanger to exchange heat with desalted water, then passes through a newly-added lean solvent/white oil heat exchanger to exchange heat with a lean solvent, and finally is cooled by an original diesel air cooler and is discharged to a product tank.
The application conditions of the process of the invention in the hydrocracking device 2# of the Ministry of maoming of the China petrochemical industry Limited company are as follows in the following table 1:
TABLE 1 Main product specifications obtained by the Process according to the invention
| Serial number | Product(s) | Distillation Range D86, deg.C | Density kg/m 3 ，(20℃) | Flash point, DEG C |
| 1 | No. 10 military diesel fuel | 214～300 | 816 | 100 |
| 2 | 5# Industrial white oil | 280～345 | 821 | 140 |
The following table 2 shows the application of the process of fig. 2 of the present invention and the process of fig. 1 of the background art in a 2# hydrocracking apparatus, a maxmarker division company, a petrochemical company, ltd, in china:
TABLE 2 comparison of products using the inventive process and processes before and after the inventive revamping
As can be seen from Table 1, the distillation range of the light diesel oil component of the product fractionating tower of the device after implementation is 214-300 ℃, and the distillation range of the industrial white oil component is 280-345 ℃, wherein the industrial white oil component has good property and can be used as high-quality No. 5 industrial white oil, and the light diesel oil component has good property and low colloid content and can be used as No. 10 military diesel oil.
Example 2
The difference from the embodiment 1 is that the number of layers of the fractionating tower T1 is 60, a diesel oil extraction port is arranged at the 16 th tray of the fractionating tower T1, and oil gas at the top of the diesel oil side stripper T3 returns to the 14 th tray of the fractionating tower T1 after being stripped by the diesel oil side stripper T3.
A white oil extraction port is additionally arranged at the 34 th tray of the fractionating tower T1, and after being stripped by a white oil side line stripping tower T4, the overhead gas of the white oil side line stripping tower T4 returns to the 32 th tray of the fractionating tower T1.
Example 3
Unlike example 1, the number of trays in the diesel side stripper T3 was 18, and the number of trays in the white oil side stripper was 18.
The superheated steam used in the diesel side stripper T3 and in the white oil side stripper T4 was superheated low pressure steam at a temperature of 380 ℃ and a pressure of 0.45 MPa.
Finally, it should be noted that the above-mentioned embodiments are only preferred embodiments of the present invention, and should not be construed as limiting the scope of the present invention, and those skilled in the art should make various simple modifications and equivalent substitutions without departing from the spirit of the technical solution of the present invention.
Claims (7)
1. A production process of No. 10 military diesel oil and No. 5 industrial white oil is characterized by comprising the following steps:
(1) pretreating the hydrocracking produced oil, then feeding the pretreated produced oil into a fractionating tower T1 with 50-60 layers of trays for fractionation, forming a diesel oil extraction port at the 16 th-18 th layer of tray of the fractionating tower T1, wherein a diesel oil extraction pipeline is arranged at the diesel oil extraction port, the diesel oil extraction pipeline is connected with a diesel oil side-draw stripper T3, the diesel oil extracted from the diesel oil extraction port flows into a diesel oil side-draw stripper T3 through the diesel oil extraction pipeline, after the diesel oil side-draw stripper T3 is stripped, oil gas at the top of the diesel oil side-draw stripper T3 returns to the 14 th-15 th layer of tray of the fractionating tower T1, and after the product at the bottom of the diesel oil side-draw stripper T3 is extracted, heat exchange and cooling treatment are carried out to obtain No. 10 military diesel oil;
(2) adding a white oil material extraction port at the 34 th to 36 th layers of trays of a fractionating tower T1, wherein a white oil material extraction pipeline is arranged at the white oil material extraction port, the white oil material extraction pipeline is connected with a white oil material side-line stripping tower T4, white oil material extracted from the white oil material extraction port flows into the white oil material side-line stripping tower T4 through the white oil material extraction pipeline, after being stripped by the white oil material side-line stripping tower T4, gas at the top of the white oil material side-line stripping tower T4 returns to the 32 th to 33 th layers of trays of the fractionating tower T1, and a product at the bottom of the white oil material side-line stripping tower T4 is extracted and then enters a dehydration tank V1 for vacuum dehydration, and then is subjected to pressurization, heat exchange and cooling treatment to obtain 5# industrial white oil;
pumping a product at the bottom of the diesel side-line stripper T3 in the step (1) by using a centrifugal pump, and then carrying out heat exchange and cooling treatment to obtain No. 10 military diesel, wherein the heat exchange treatment comprises the steps of recovering heat in the product from the product pumped by the centrifugal pump through a steam generator, a heat exchanger and an air cooler, and carrying out heat exchange, cooling and cooling treatment to obtain No. 10 military diesel, wherein self-produced steam generated by the steam generator is used as superheated steam of a fractionating tower T1, a diesel side-line stripper T3 and a white oil side-line stripper T4;
the superheated steam used for the diesel side stripper T3 in the step (1) and the superheated steam used for the white oil side stripper in the step (2) is superheated low-pressure steam with the temperature of 380-400 ℃ and the pressure of 0.3-0.6 MPa, the superheated low-pressure steam is derived from self-generated steam generated by the steam generator, and the heat source of the steam generator is derived from heat of a product at the bottom of the diesel side stripper T3 and heat generated by middle-stage reflux;
and (3) performing heat exchange twice in the step (2), wherein the first heat exchange is heat exchange with desalted water, the temperature of a product before heat exchange is 220-250 ℃, the temperature of the product after heat exchange is 140-160 ℃, the temperature of desalted water before heat exchange is 60-80 ℃, the temperature after heat exchange is 100-104 ℃, the temperature of the product after heat exchange is ensured not to be higher than 160 ℃, the second heat exchange is heat exchange with a poor solvent, the temperature of the product before heat exchange is 140-160 ℃, the temperature after heat exchange is 80-100 ℃, the temperature of the poor solvent before heat exchange is 45-50 ℃, and the temperature after heat exchange is 50-60 ℃.
2. The process for producing military diesel No. 10 and industrial white oil No. 5 as claimed in claim 1, wherein the process comprises the following steps: the pretreatment in the step (1) is hydrogen sulfide removal treatment; the number of the trays of the diesel side stripper T3 is 14-20.
3. The process for producing military diesel-10 and industrial white oil 5# according to claim 1, wherein the process comprises the following steps: the distillation range of the military diesel oil No. 10 generated in the step (1) is 214-302 ℃.
4. The process for producing military diesel No. 10 and industrial white oil No. 5 as claimed in claim 1, wherein the process comprises the following steps: the number of the trays of the white oil material side stripper T4 in the step (2) is 14-20.
5. The process for producing military diesel No. 10 and industrial white oil No. 5 as claimed in claim 1, wherein the process comprises the following steps: and (3) pumping a product at the bottom of the white oil material side-line stripping tower T4 in the step (2) by adopting a centrifugal pump, then feeding the product into a dewatering tank V1 for vacuum dewatering, wherein a steam jet vacuum pumping system is arranged at the top of the dewatering tank V1, the vacuum pumping oil gas at the top of the dewatering tank V1 returns to the white oil material side-line stripping tower T4, and the white oil material which is subjected to flash evaporation dewatering by the steam jet vacuum pumping system at the bottom of the dewatering tank V1 is subjected to pressurization, heat exchange and cooling treatment to obtain industrial white oil, wherein the vacuum degree in the vacuum dewatering tank V1 is-0.08 to-0.03 MPa.
6. The process for producing military diesel No. 10 and industrial white oil No. 5 as claimed in claim 1, wherein the process comprises the following steps: and (3) pressurizing in the step (2) by using a booster pump, cooling in the step (2) by using an air cooler, and cooling by using the air cooler to obtain the industrial white oil with the temperature of 50-60 ℃.
7. The process for producing military diesel-10 and industrial white oil 5# according to claim 1, wherein the process comprises the following steps: the distillation range of the 5# industrial white oil obtained in the step (2) is 280-345 ℃.
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| CN105233518A (en) * | 2015-10-16 | 2016-01-13 | 海南汉地阳光石油化工有限公司 | Fractionating tower, fractionating system and method for producing heat conducting oil |
| CN205528608U (en) * | 2016-02-25 | 2016-08-31 | 中国石油化工股份有限公司 | White oil initial boiling point lift system |
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| CN105233518A (en) * | 2015-10-16 | 2016-01-13 | 海南汉地阳光石油化工有限公司 | Fractionating tower, fractionating system and method for producing heat conducting oil |
| CN205528608U (en) * | 2016-02-25 | 2016-08-31 | 中国石油化工股份有限公司 | White oil initial boiling point lift system |
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