CN108913203A - A kind of production technology of-No. 10 military diesels and 5# technical white oil - Google Patents
A kind of production technology of-No. 10 military diesels and 5# technical white oil Download PDFInfo
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- CN108913203A CN108913203A CN201810616793.8A CN201810616793A CN108913203A CN 108913203 A CN108913203 A CN 108913203A CN 201810616793 A CN201810616793 A CN 201810616793A CN 108913203 A CN108913203 A CN 108913203A
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- white oil
- side stripper
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- heat exchange
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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
-
- 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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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses the production technologies of a kind of-No. 10 military diesels and 5# technical white oil, include the following steps：(1) outlet port diesel oil side stripper T3 is moved up, after diesel oil side stripper T3 processing, then obtains-No. 10 military diesels after heat exchange and cooling；(2) increase technical white oil material lateral line withdrawal function mouth and return port in product fractionating column T1, the technical white oil material extracted out from fractionating column T1 flows into newly-increased technical white oil material side stripper T4 certainly, after white oil material side stripper T4 stripping, white oil material side stripper T4 overhead gas returns to fractionating column T1, enter drain sump V1 vacuum dehydration after the product extraction of white oil material side stripper T4 tower bottom, pressurized again, heat exchange and cooling treatment, obtain 5# technical white oil.The technique can be produced at the same time-No. 10 military diesels and 5# technical white oil, and-No. 10 military diesels of acquisition and high-quality 5# technical white oil initial boiling point are high, and high income, quality reaches top grade product.
Description
Technical field
The invention belongs to technical field of petrochemical industry, and in particular to a kind of life of-No. 10 military diesels and 5# technical white oil
Production. art.
Background technique
As shown in fig. 1, the generation oil after the hydrogenated cracking reaction of raw material is used in prior art is through device fractionating system
The technique that technical white oil is prepared after cutting, the hydrogenated cracking unit system of decompressed wax oil that raw material comes usually from atmospheric and vacuum distillation unit
Treated generates oil, which will be after coming out from REACTION SYSTEM IN HYDROCRACKING UNIT and reacting and generate the fractionated tower T1 cutting of oil,
Go out heavy naphtha at the top of T1, T2 is that boat coal side stripper sails coal, and T3 is that diesel oil side stripper is gone abroad five diesel oil, the bottom T1
For tail oil.Since what is utilized into diesel oil side stripper T3 is original diesel oil draw out mouth (the 28th layer extraction), so outlet port
Farther out, extraction temperature is relatively low for positional distance tower bottom, produces initial boiling point and reaches 250 DEG C or so of 5# technical white oil, and still has coal
Oily taste, appearance unclarity, from high-quality technical white oil, there are also larger gaps.Therefore, hydrocracking unit in the prior art does not have
The side line of special production 5# technical white oil, can only be produced using diesel oil side stripper T3.In addition, using existing diesel oil side line
The diesel oil of stripper T3 production, gum level is high, and cannot function as the use of -10# military diesel.
Therefore, in order to improve the quality of technical white oil and diesel oil, enable device output -10# military diesel and high-quality simultaneously
5# technical white oil needs to improve existing hydrocracking process, so as to produce-No. 10 military diesels and excellent simultaneously
The production technology of matter 5# technical white oil.
Summary of the invention
The purpose of the present invention is to provide the production technology of a kind of-No. 10 military diesels and high-quality technical white oil, the techniques
It can be produced at the same time-No. 10 military diesels and the high-quality technical white oil of 5# ,-No. 10 military diesels of acquisition and 5# technical white oil fore-running
Point is high, and high income, quality reaches top grade product.
Above-mentioned purpose of the invention is achieved through the following technical solutions：- No. 10 military diesels of one kind and 5# industry
The production technology of white oil, includes the following steps：
(1) after pretreatment by the generation oil being hydrocracked, it is carried out in the fractionating column T1 for being 50~60 layers into tower tray number
Fractionation opens up diesel oil draw out mouth at the 16th~18 layer of tower tray of fractionating column T1, is equipped with diesel oil draw out at the diesel oil draw out mouth
Pipeline, the diesel oil draw out pipeline are connected with diesel oil side stripper T3, and the diesel oil extracted out from diesel oil draw out mouth is through diesel oil draw out
Pipeline flows into diesel oil side stripper T3, after diesel oil side stripper T3 stripping, the oil gas of diesel oil side stripper T3 tower top
The 14th~15 layer of tower tray of fractionating column T1 is returned to, through heat exchange and cooling treatment after the product extraction of diesel oil side stripper T3 tower bottom
Obtain-No. 10 military diesels；
(2) white oil material outlet port is added at the 34th~36 layer of tower tray of fractionating column T1, the white oil material is set at outlet port
There is white oil material to extract pipeline out, the white oil material extraction pipeline is connected with white oil material side stripper T4, takes out from white oil material outlet port
White oil material out flows into white oil material side stripper T4 through white oil material extraction pipeline, after white oil material side stripper T4 stripping,
White oil material side stripper T4 overhead gas returns to the 32nd~33 layer of tower tray of fractionating column T1, white oil material side stripper T4 tower bottom
Product extraction after enter drain sump V1 vacuum dehydration, then it is pressurized, heat exchange and cooling treatment, obtain 5# technical white oil.
In the production technology of above-mentioned-No. 10 military diesels and 5# technical white oil：
Pretreatment described in step (1) is depriving hydrogen sulphide processing；The tower tray number of the diesel oil side stripper T3 is preferred
It is 14~20 layers.
The product of diesel oil side stripper T3 tower bottom is obtained using after centrifugal pump extraction through heat exchange and cooling treatment in step (1)
- No. 10 military diesels are obtained, wherein heat exchange processing includes the product by centrifugal pump extraction through steam generator, heat exchanger and sky
Cooler is by the heat recovery in product, and heat exchange cools down and obtains-No. 10 military diesels after cooling treatment, and wherein steam generator produces
Raw self-produced steam is used as the superheated steam of fractionating column T1, diesel oil side stripper T3 and white oil material side stripper T4.
For being used for the mistake of white oil material side stripper in the diesel oil side stripper T3 and step (2) in step (1)
Hot steam is that temperature is 380~400 DEG C, and pressure is the superheated low pressure vapor of 0.3~0.6MPa, the superheated low pressure vapor source
In the self-produced steam that the steam generator generates, the heat source of the steam generator is from diesel oil side stripper T3 tower bottom
Product heat and middle section reflux generate heat.
Its low pressure steam comes out by the way that steam generator is self-produced, can be heated into later preferably through fractionation furnace convection section
Superheated steam, the heat source pre-selection of steam generator are the heats of the heat exchanger of the diesel oil and middle section reflux in device, wherein steam
The deaerated water of generator is the desalted water from outer device after the oxygen-eliminating device deoxygenation in device, is pumped into steam generation through water supply
Device.
The boiling range of-No. 10 military diesels generated in step (1) of the present invention is 214~302 DEG C.
The present invention moves up the diesel oil released from fractionating column T1 lateral line withdrawal function position and handles by diesel oil side stripper T3
Afterwards, it can remove the light component in diesel oil, improve the flash-point of diesel oil, pass through by the processed diesel oil of diesel oil side stripper T3
Centrifugal pump is extracted out from the bottom of diesel oil side stripper T3, then will be in diesel oil through steam generator, heat exchanger and air cooler
Heat recovery obtains-No. 10 military diesels after heat exchange cooling.
The tower tray number of white oil material side stripper T4 is preferably 14~20 layers described in step (2) of the present invention.
Enter drain sump V1 after the product of white oil material side stripper T4 tower bottom preferably uses centrifugal pump to extract out in step (2)
Vacuum dehydration, the top drain sump V1 are equipped with vapor injection vacuum pumping system, vacuumize oil gas return at the top of drain sump V1
The white oil material through vapor injection vacuum pumping system flash-evaporation dehydration of the bottom white oil material side stripper T4, drain sump V1 is pressurized,
Heat exchange and cooling treatment, obtain technical white oil, and wherein the vacuum degree in vacuum dehydration can V1 is -0.08~-0.03MPa.
Heat exchange is using exchanging heat twice in step (2) of the present invention, wherein heat exchange for the first time is that (desalted water is from device with desalted water
Battery limit (BL) is external, can be the low temperature desalted water in other techniques) heat exchange, the temperature of product is 220~250 DEG C before exchanging heat, heat exchange
The temperature of product is 140~160 DEG C afterwards, and temperature is 60~80 DEG C before desalted water exchanges heat, and temperature is 100~104 DEG C after heat exchange, is changed
Guarantee that the temperature of product after exchanging heat is not higher than 160 DEG C after heat, second of heat exchange is that (lean solvent is outside device battery limit (BL) with lean solvent
Come, can be the low temperature lean solvent in other techniques) heat exchange, temperature is 140~160 DEG C before product exchanges heat, and temperature is after heat exchange
80~100 DEG C, temperature is 45~50 DEG C before lean solvent exchanges heat, and temperature is 50~60 DEG C after heat exchange.
After heat exchange, first is that can guarantee that technical white oil, not higher than 160 DEG C, plays energy-conserving action into the temperature before air cooler,
Second is that desalination coolant-temperature gage reaches deoxygenation temperature with after desalted water heat exchange, it is possible to reduce (deoxygenation steam is device deoxygenation steam consumption
System 1.0MPa steam carries out deoxygenation use to desalted water).
In addition, second of heat exchange exchanges heat with lean solvent, temperature is 140~160 DEG C before technical white oil exchanges heat, and is exchanged heat postindustrial
The temperature of white oil is 80~100 DEG C.Lean solvent can come from external system amine liquid general pipeline, and temperature is about 45~50 DEG C before exchanging heat,
Temperature is about 50~60 DEG C after heat exchange, and mainly raising lean solvent guarantees lean solvent and dress into the temperature of desulphurization of recycle hydrogen tower
Recycle hydrogen is set there are temperature difference, prevents the hydro carbons in recycle hydrogen from largely condensing in lean solution, desulphurization of recycle hydrogen tower amine liquid is caused to send out
Bubble.
Pressurization preferably uses booster pump in step (2) of the present invention, and cooling preferably uses air cooler in step (2), through air-cooled
The temperature of 5# technical white oil is 50~60 DEG C after device cooling.
The boiling range range of the 5# technical white oil obtained in step (2) of the present invention is 280~345 DEG C.
The industry that the present invention comes out from the side line that fractionating column T1 lateral line withdrawal function position moves down rear close fractionating column T1 tower bottom is white
Oil plant can remove the light components in technical white oil material after white oil side stripper T4 processing, improve technical white oil material
Flash-point, while through being set to white oil material side stripper T4 outlet at bottom drain sump V1 be carried out dehydrating, the production of acquisition
Product are extracted out via centrifugal pump again, through heat exchanger and air cooler by the heat recovery in technical white oil, up to high-quality after heat exchange cooling
Technical white oil.
The invention has the advantages that：
(1) using the 5# technical white oil of present invention process production, initial boiling point can reach 280 DEG C or so, and the prior art is raw
The initial boiling point of the 5# technical white oil of production is about 250 DEG C or so, moreover it is possible to which solving 5# technical white oil has kerosene taste and appearance not saturating enough
Bright problem is able to produce good 5# technical white oil；
(2) for-No. 10 military diesel initial boiling points for using present invention process to produce for 217 DEG C or so, the end point of distillation is 300 DEG C of left sides
The right side, and-No. 10 military diesel initial boiling points of usual manner production are only 160 DEG C or so, the end point of distillation is about 290 DEG C, the present invention
The problem of yield is low when can effectively solve-No. 10 army's bavins of production, and most of diesel component is displaced downwardly to inside tail oil, while substantially dropping
Colloid in low diesel oil can be used as the use of -10# military diesel.
Detailed description of the invention
Fig. 1 is in the prior art using the flow chart of fractionating column production diesel oil and technical white oil；
Fig. 2 is the production technology figure of-No. 10 military diesels and high-quality 5# technical white oil in the specific embodiment of the invention.
Specific embodiment
Embodiment 1
As shown in Figure 2, a kind of production technology of-No. 10 military diesels and high-quality technical white oil, includes the following steps：
(1) after pretreatment by the generation oil being hydrocracked, it is fractionated in the fractionating column T1 for being 54 layers into tower tray number,
Diesel oil draw out mouth is opened up at the 17th layer of tower tray of fractionating column T1, is equipped with diesel oil draw out pipeline, diesel oil draw out at diesel oil draw out mouth
Pipeline is connected with diesel oil side stripper T3, and the diesel oil extracted out from diesel oil draw out mouth flows into diesel oil side line vapour through diesel oil draw out pipeline
Stripper T3, after diesel oil side stripper T3 stripping, the oil gas of diesel oil side stripper T3 tower top returns to the 15th of fractionating column T1 the
Layer tower tray obtains-No. 10 military diesels through heat exchange and cooling treatment after the product extraction of diesel oil side stripper T3 tower bottom；
(2) white oil material outlet port is added at the 35th layer of tower tray of fractionating column T1, is equipped with white oil material at white oil material outlet port
Extract pipeline out, white oil material extraction pipeline is connected with white oil material side stripper T4, the white oil material warp extracted out from white oil material outlet port
White oil material extracts pipeline out and flows into white oil material side stripper T4, after white oil material side stripper T4 stripping, white oil material side line vapour
Stripper T4 overhead gas returns to the 33rd layer of tower tray of fractionating column T1, enters after the product extraction of white oil material side stripper T4 tower bottom
Drain sump V1 vacuum dehydration, then pressurized, heat exchange and cooling treatment, obtain 5# technical white oil.
Wherein pretreatment is that depriving hydrogen sulphide is handled；The tower tray number of diesel oil side stripper T3 is specially 16 layers.
The product of diesel oil side stripper T3 tower bottom is obtained using after centrifugal pump extraction through heat exchange and cooling treatment in step (1)
- No. 10 military diesels are obtained, wherein heat exchange processing includes the product by centrifugal pump extraction through steam generator, heat exchanger and air cooler
By the heat recovery in product, heat exchange cools down and obtains-No. 10 military diesels after cooling treatment, and wherein steam generator generates
Self-produced steam is used as the superheated steam of fractionating column T1, diesel oil side stripper T3 and white oil material side stripper T4.
For being used for the mistake of white oil material side stripper in the diesel oil side stripper T3 and step (2) in step (1)
Hot steam is that temperature is 400 DEG C, and pressure is the superheated low pressure vapor of 0.35MPa, and superheated low pressure vapor derives from steam generator
The self-produced steam of generation, the heat source of steam generator are returned from the heat of the product of diesel oil side stripper T3 tower bottom and middle section
The raw heat of miscarriage.
Its low pressure steam comes out by the way that steam generator is self-produced, can be heated into overheat by fractionation furnace convection section later
Steam, the heat source pre-selection of steam generator are the heat of the heat exchanger of the diesel oil and middle section reflux in device, wherein steam generation
The deaerated water of device is the desalted water from outer device after the oxygen-eliminating device deoxygenation in device, is pumped into steam generator through water supply.
The boiling range of-No. 10 military diesels generated is 214~300 DEG C.
The present invention moves up the diesel oil released from fractionating column T1 lateral line withdrawal function position and handles by diesel oil side stripper T3
Afterwards, it can remove the light component in diesel oil, improve the flash-point of diesel oil, pass through by the processed diesel oil of diesel oil side stripper T3
Centrifugal pump is extracted out from the bottom of diesel oil side stripper T3, then will be in diesel oil through steam generator, heat exchanger and air cooler
Heat recovery obtains-No. 10 military diesels after heat exchange cooling.
The tower tray number of white oil material side stripper T4 is preferably 16 layers in step (2).
Enter drain sump V1 after the product of white oil material side stripper T4 tower bottom preferably uses centrifugal pump to extract out in step (2)
Vacuum dehydration, the top drain sump V1 are equipped with vapor injection vacuum pumping system, and the oil gas that vacuumizes at the top of drain sump V1 returns to white oil
Expect side stripper T4, the white oil material through vapor injection vacuum pumping system flash-evaporation dehydration of the bottom drain sump V1 is pressurized, exchanges heat
And cooling treatment, technical white oil is obtained, wherein the vacuum degree in vacuum dehydration can V1 is -0.03MPa.
Heat exchange using exchanging heat twice in step (2), wherein heat exchange is that (desalted water is outside device battery limit (BL) with desalted water for the first time
Come, can be the low temperature desalted water in other techniques) heat exchange, the temperature of product is 220~250 DEG C before exchanging heat, product after heat exchange
Temperature be 140~160 DEG C, desalted water exchange heat before temperature be 60~80 DEG C, after heat exchange temperature be 100~104 DEG C, protected after heat exchange
The temperature of product is not higher than 160 DEG C after card heat exchange, and second heat exchange is that (lean solvent is external from device battery limit (BL), can be with lean solvent
It is the low temperature lean solvent in other techniques) heat exchange, temperature is 140~160 DEG C before product exchanges heat, and temperature is 80~100 after heat exchange
DEG C, temperature is 45~50 DEG C before lean solvent exchanges heat, and temperature is 50~60 DEG C after heat exchange.
After heat exchange, first is that can guarantee that technical white oil, not higher than 160 DEG C, plays energy-conserving action into the temperature before air cooler,
Second is that desalination coolant-temperature gage reaches deoxygenation temperature with after desalted water heat exchange, it is possible to reduce (deoxygenation steam is device deoxygenation steam consumption
System 1.0MPa steam carries out deoxygenation use to desalted water).
In addition, second of heat exchange exchanges heat with lean solvent, temperature is 140~160 DEG C before technical white oil exchanges heat, and is exchanged heat postindustrial
The temperature of white oil is 80~100 DEG C.Lean solvent can come from external system amine liquid general pipeline, and temperature is about 45~50 DEG C before exchanging heat,
Temperature is about 50~60 DEG C after heat exchange, and mainly raising lean solvent guarantees lean solvent and dress into the temperature of desulphurization of recycle hydrogen tower
Recycle hydrogen is set there are temperature difference, prevents the hydro carbons in recycle hydrogen from largely condensing in lean solution, desulphurization of recycle hydrogen tower amine liquid is caused to send out
Bubble.
Pressurization uses booster pump, cooling using air cooler, the 5# industry after air cooler cools down in step (2) in step (2)
The temperature of white oil is 50~60 DEG C.
The boiling range range of the 5# technical white oil obtained in step (2) of the present invention is 280~345 DEG C.
The industry that the present invention comes out from the side line that fractionating column T1 lateral line withdrawal function position moves down rear close fractionating column T1 tower bottom is white
Oil plant can remove the light components in technical white oil material after white oil side stripper T4 processing, improve technical white oil material
Flash-point, while through being set to white oil material side stripper T4 outlet at bottom drain sump V1 be carried out dehydrating, the production of acquisition
Product are extracted out via centrifugal pump again, through heat exchanger and air cooler by the heat recovery in technical white oil, up to high-quality after heat exchange cooling
5# technical white oil.
To sum up, it-No. 10 military diesels of the invention and can be summarized as with the main points of the production technology of 5# technical white oil：
(1) outlet port diesel oil side stripper T3 position is at the 17th layer of tower tray of fractionating column T1.
(2) technical white oil material lateral line withdrawal function is added at the 35th layer of tower tray of product fractionating column T1, is additionally arranged corresponding work
Industry white oil material side stripper T41, pump (centrifugal pump) 2 (a preparation and a use), changes flash-evaporation dehydration tank (i.e. drain sump V11)
Hot device 2.
- No. 10 military diesels of the invention and with the main flow of the production technology of 5# technical white oil it is：
(1) outlet port diesel oil side stripper T3 is moved up, after diesel oil side stripper T3 processing, then through steam generation
Device, heat exchanger and air cooler heat exchange, obtain-No. 10 military diesels after cooling；
(2) increase technical white oil material lateral line withdrawal function mouth and return port in product fractionating column T1.The work extracted out from fractionating column T1
From newly-increased technical white oil material side stripper T4 is flowed into, the bottom technical white oil material side stripper T4 is passed through industry white oil material
0.35MPa, 400 DEG C of superheated steam strippings；
(3) technical white oil material side stripper T4 tower overhead gas returns to product fractionating column T1, technical white oil material side stripper
The bottom T4 liquid phase enters flash distillation (vacuum) drain sump V1, and 1.0MPa vapor injection vacuum pumping system is arranged in flash-evaporation dehydration tank deck；
(4) the technical white oil material of flash-evaporation dehydration enters newly-increased after newly-increased technical white oil material centrifugal pump (one one standby) pressure-raising
Desalted water/technical white oil material heat exchanger and desalted water exchange heat, changed using newly-increased lean solvent/white oil heat exchanger with lean solvent
Heat most goes out device to products pot after original diesel oil air cooler is cooling afterwards.
Present invention process is practiced in China Petroleum & Chemical Co., Ltd. Maoming Branch's 2# hydrocracking unit
Situation such as the following table 1：
The major product specification that table 1 is obtained using present invention process
| Serial number | Product | Boiling range D86, DEG C | Density kg/m3, (20 DEG C) | Flash-point, DEG C |
| 1 | - No. 10 military diesels | 214~300 | 816 | 100 |
| 2 | 5# technical white oil | 280~345 | 821 | 140 |
Using the technique in Fig. 2 of the present invention and the technique in background technique Fig. 1 in the limited public affairs of Sinopec's share
Department's Maoming branch company 2# hydrocracking unit practices situation such as the following table 2：
The product control of front and back technique is transformed using present invention process and the present invention for table 2
Seen from table 1, the boiling range range of the light diesel fuel component of the product fractionating column of device is at 214~300 DEG C after implementation, work
Industry white oil component boiling range range is at 280~345 DEG C, and wherein technical white oil constitutive property is preferable, can be used as high-quality 5# technical white oil
Material, and light diesel fuel constitutive property is good, gum level is low, can be used as the use of -10# military diesel.
Embodiment 2
Unlike the first embodiment, the number of plies of fractionating column T1 is 60 layers, opens up bavin at the 16th layer of tower tray of fractionating column T1
Oily outlet port, after diesel oil side stripper T3 stripping, the oil gas of diesel oil side stripper T3 tower top returns to the of fractionating column T1
14 layers of tower tray.
White oil material outlet port is added at the 34th layer of tower tray of fractionating column T1, after white oil material side stripper T4 stripping,
The 32nd layer of tower tray of white oil material side stripper T4 overhead gas return fractionating column T1.
Embodiment 3
Unlike the first embodiment, the tower tray number of diesel oil side stripper T3 is 18 layers, the tower of white oil material side stripper
Disk number is 18 layers.
Superheated steam for diesel oil side stripper T3 and for white oil material side stripper T4 is that temperature is 380 DEG C,
Pressure is the superheated low pressure vapor of 0.45MPa.
Finally, it should be noted that the above content is only the preferred embodiments of the disclosure, should not become to this
The limitation of invention protection scope, those skilled in the art in the case where not departing from the essence of technical solution of the present invention,
Various simple deformations or equivalent replacement, should all fall within the scope of protection of the present invention to made by the present invention.
Claims (10)
1. a kind of production technology of-No. 10 military diesels and 5# technical white oil, it is characterized in that including the following steps：
(1) after pretreatment by the generation oil being hydrocracked, it is fractionated in the fractionating column T1 for being 50~60 layers into tower tray number,
Diesel oil draw out mouth is opened up at the 16th~18 layer of tower tray of fractionating column T1, is equipped with diesel oil draw out pipeline at the diesel oil draw out mouth,
The diesel oil draw out pipeline is connected with diesel oil side stripper T3, and the diesel oil extracted out from diesel oil draw out mouth is through diesel oil draw out pipeline stream
Enter diesel oil side stripper T3, after diesel oil side stripper T3 stripping, the oil gas of diesel oil side stripper T3 tower top, which returns, to be divided
The 14th~15 layer of tower tray of tower T1 is evaporated, through heat exchange and cooling treatment acquisition-after the product extraction of diesel oil side stripper T3 tower bottom
No. 10 military diesels；
(2) white oil material outlet port is added at the 34th~36 layer of tower tray of fractionating column T1, is equipped at white oil material outlet port white
Oil plant extracts pipeline out, and the white oil material extraction pipeline is connected with white oil material side stripper T4, extracts out from white oil material outlet port
White oil material flows into white oil material side stripper T4 through white oil material extraction pipeline, after white oil material side stripper T4 stripping, white oil
Expect that side stripper T4 overhead gas returns to the 32nd~33 layer of tower tray of fractionating column T1, the production of white oil material side stripper T4 tower bottom
Enter drain sump V1 vacuum dehydration, then pressurized, heat exchange and cooling treatment after product extraction, obtains 5# technical white oil.
2.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(1) pretreatment described in is depriving hydrogen sulphide processing；The tower tray number of the diesel oil side stripper T3 is 14~20 layers.
3.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(1) product of diesel oil side stripper T3 tower bottom is using military through heat exchange and cooling treatment acquisition -10 after centrifugal pump extraction in
Diesel oil, wherein heat exchange processing includes through steam generator, heat exchanger and air cooler by the product of centrifugal pump extraction by product
In heat recovery, heat exchange cooling and cooling treatment after obtain-No. 10 military diesels, wherein steam generator generate self-produced steaming
Vapour is used as the superheated steam of fractionating column T1, diesel oil side stripper T3 and white oil material side stripper T4.
4.-No. 10 military diesels according to claim 3 and the production technology with 5# technical white oil, it is characterized in that：Step
(1) superheated steam being used in the diesel oil side stripper T3 and step (2) for white oil material side stripper in is temperature
It is 380~400 DEG C, pressure is the superheated low pressure vapor of 0.3~0.6MPa, and the superheated low pressure vapor is sent out from the steam
The self-produced steam that raw device generates, the heat of the heat source of the steam generator from the product of diesel oil side stripper T3 tower bottom
The heat generated with middle section reflux.
5.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(1) boiling range of-No. 10 military diesels generated in is 214~302 DEG C.
6.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(2) the tower tray number of the side stripper of white oil material described in T4 is 14~20 layers.
7.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(2) enter drain sump V1 vacuum dehydration after the product of white oil material side stripper T4 tower bottom is extracted out using centrifugal pump in, it is described de-
Vapor injection vacuum pumping system is equipped at the top of water pot V1, the oil gas that vacuumizes at the top of drain sump V1 returns to white oil material side stripper
The white oil material through vapor injection vacuum pumping system flash-evaporation dehydration of the bottom T4, drain sump V1 is pressurized, heat exchange and cooling treatment, obtains
Technical white oil, wherein the vacuum degree in vacuum dehydration can V1 is -0.08~-0.03MPa.
8.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(2) heat exchange using exchanging heat twice in, wherein heat exchange for the first time is exchanged heat with desalted water, the temperature of product is 220~250 before exchanging heat
DEG C, after heat exchange the temperature of product be 140~160 DEG C, desalted water exchange heat before temperature be 60~80 DEG C, after heat exchange temperature be 100~
104 DEG C, guarantee that the temperature of product after exchanging heat is not higher than 160 DEG C after heat exchange, second of heat exchange is exchanged heat with lean solvent, and product exchanges heat
Preceding temperature is 140~160 DEG C, and temperature is 80~100 DEG C after heat exchange, and temperature is 45~50 DEG C before lean solvent exchanges heat, warm after heat exchange
Degree is 50~60 DEG C.
9.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(2) pressurization uses booster pump in, cooling in step (2) to use air cooler, is 50 through the cool down temperature of postindustrial white oil of air cooler
~60 DEG C.
10.-No. 10 military diesels according to claim 1 and the production technology with 5# technical white oil, it is characterized in that：Step
(2) the boiling range range of the 5# technical white oil obtained in is 280~345 DEG C.
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| CN112048331A (en) * | 2020-08-21 | 2020-12-08 | 马金山 | Raw oil primary distillation processing device and production process |
| CN114836236A (en) * | 2021-02-01 | 2022-08-02 | 中国石油天然气股份有限公司 | Production process of military diesel oil |
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