CN107541245A - A kind of hydrocracked product fractionating system and fractional method - Google Patents
A kind of hydrocracked product fractionating system and fractional method Download PDFInfo
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- CN107541245A CN107541245A CN201610480503.2A CN201610480503A CN107541245A CN 107541245 A CN107541245 A CN 107541245A CN 201610480503 A CN201610480503 A CN 201610480503A CN 107541245 A CN107541245 A CN 107541245A
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Abstract
The invention discloses a kind of hydrocracked product fractionating system, the system includes：Hydrogen sulfide stripping tower (1), charging relief valve (2), one-level preheater (3), two level preheater (4), primary flash tank (5), three-level preheater (6), two-stage flash tank (7), product fractionating column charging heating furnace (8) and product fractionating column (9)；The invention also discloses a kind of hydrocracked product fractional method, and the load of product fractionating column charging heating furnace can be effectively reduced compared with conventional method, realizes the energy-saving of system entirety.
Description
Technical field
The present invention relates to petrochemical industry to be hydrocracked field, in particular it relates to a kind of hydrocracked product fractionating system and
Fractional method.
Background technology
Be hydrocracked be both heavy oil lighting effective way, and production clean fuel important means.It is hydrocracked
It is under higher temperature, pressure, hydrogen makes mink cell focus that hydrogenation, cracking and isomerization reaction, conversion occur under catalyst action
For light oil such as：Gasoline, kerosene, diesel oil or catalytic cracking, the process of cracking olefin feedstock, there is yield of light oil
Outstanding advantages of height, good product quality.
The parts such as hydrocracking unit is typically by reacting, being fractionated, Vapor recovery unit form.In fractionating section, low point of oil is in sulphur
Change hydrogen stripper and remove H by steam stripping2S gases.Hydrogen sulfide stripping tower base oil is after preheating, pressure release, flash distillation, flashed vapour
Product fractionating column is mutually directly entered, flash distillation liquid phase is heated to suitable temperature by product fractionating column charging heating furnace again and enters product
Fractionating column.
In recent years, go deep into energy conservation, how further to reduce hydrocracking unit energy consumption, cause refinery work
The common concern of author.Wherein, by optimizing the heat exchange process of product fractionating column feeding preheating, flash temperature is lifted, increase is dodged
Steam Phase Proportion, reduce flash liquid Phase Proportion and improve its temperature, and then reduce product fractionating column charging heating furnace load, be drop
One of effective means of low hydrocracking unit energy consumption.
It is difficult to excavate the heat for arriving and can be used for the charging of pre- hot product fractionating column because Temperature Matching limits, in hydrocracking unit
Source.Simultaneously as temperature typically can reach 190 DEG C or so after the preheating of product fractionating column feed stream, other devices of refinery are also very
Hardly possible is excavated to the logistics that thermal source is provided for product fractionating column feeding preheating so that is born by reducing product fractionating column charging heating furnace
Lotus and reduce that hydrocracking unit energy consumption is almost infeasible, constrain the further drop of hydrocracking unit energy consumption to a certain extent
It is low.
The content of the invention
It is an object of the invention to provide a kind of hydrocracked product fractionating system and fractional method, solve in the prior art
The problem of high energy consumption.
To achieve these goals, first aspect present invention：A kind of hydrocracked product fractionating system is provided, the system bag
Include：Hydrogen sulfide stripping tower, charging relief valve, one-level preheater, two level preheater, primary flash tank, three-level preheater, two level are dodged
Steaming pot, product fractionating column charging heating furnace and product fractionating column；Wherein, the tower base stream outlet of hydrogen sulfide stripping tower is let out with charging
The material inlet of pressure valve is connected, and the material outlet for feeding relief valve is connected with the material inlet of one-level preheater, and the one-level is pre-
The material outlet of hot device is connected with the material inlet of two level preheater, material outlet and the primary flash tank of the two level preheater
Material inlet be connected, the primary flash tank has primary flash gaseous phase outlet and primary flash liquid-phase outlet, the one-level
The primary flash liquid-phase outlet of flash tank is connected with the material inlet of three-level preheater, the material outlet of the three-level preheater with
The material inlet of two-stage flash tank is connected, and there is the two-stage flash tank two-stage flash gaseous phase outlet and two-stage flash liquid phase to go out
Mouthful, the two-stage flash liquid-phase outlet of the two-stage flash tank is connected with the material inlet of product fractionating column charging heating furnace, described
Product fractionating column has a flash distillation gas phase entrance and heating furnace product inlet, the primary flash gaseous phase outlet of the primary flash tank and
The two-stage flash gaseous phase outlet of two-stage flash tank is connected with the flash distillation gas phase entrance of product fractionating column, the product fractionating column charging
The material outlet of heating furnace is connected with the heating furnace product inlet of product fractionating column.
Preferably, the one-level preheater also has one-level preheater heat transferring medium entrance and one-level preheater heat transferring medium
Outlet, the one-level preheater heat transferring medium entrance are connected with circulating stream outlet in two on product fractionating column；The two level
Also there is preheater two level preheater heat transferring medium entrance and two level preheater heat transferring medium to export, the two level preheater heat exchange
Medium inlet is connected with the bottom product outlet on product fractionating column；Also there is the three-level preheater heat exchange of three-level preheater to be situated between
Matter entrance and the outlet of three-level preheater heat transferring medium, the three-level preheater heat transferring medium entrance and two level preheater heat transferring medium
Outlet is connected.
Second aspect of the present invention, there is provided a kind of fractional method of hydrocracked product, this method include：A, make to split from hydrogenation
Change the hydrocracked product in reactor out to be stripped in hydrogen sulfide stripping tower, obtained stripper bottom product logistics
First passing through charging relief valve and carry out pressure release, the logistics after pressure release is preheated into one-level preheater, obtains the pre- hot of one-level,
Then make the pre- hot of one-level continue to preheat into two level preheater, obtain the pre- hot of two level；B, make what step a was obtained
The pre- hot of two level enters primary flash tank and carries out primary flash, obtains primary flash gas phase and primary flash liquid phase；C, step is made
The primary flash liquid phase that rapid b is obtained is preheated into three-level preheater, obtains the pre- hot of three-level；D, make what step c was obtained
The pre- hot of three-level enters two-stage flash tank and carries out two-stage flash, obtains two-stage flash gas phase and two-stage flash liquid phase；E, step is made
The two-stage flash liquid phase that rapid d is obtained enters product fractionating column charging heating furnace and heated, and obtains heating furnace product, makes the heating
Stove product carries out fractionation processing from the bottom of product fractionating column；Obtain primary flash gas phase that step b is obtained and step d
Two-stage flash gas phase carry out fractionation processing from the middle part of the product fractionating column.
Preferably, using temperature be 210-250 DEG C process-stream as the one-level preheater heat exchange thermal source.
Preferably, using the bottom of towe fractionated products that the temperature in the product fractionating column is 250-330 DEG C as the two level
The heat exchange thermal source of preheater.
Preferably, it is 210-250 DEG C of bottom of towe fractionated products logistics as institute using the temperature after the heat exchange of two level preheater
State the heat exchange thermal source of three-level preheater.
Preferably, the bottom product logistics of the hydrogen sulfide stripping tower is 0.8- through the pressure before feeding relief valve pressure release
1.2MPa and temperature are 190-210 DEG C, and the Stress control after feeding relief valve pressure release is 0.5-0.7MPa and temperature is 180-
205℃。
Preferably, the temperature control of the primary flash is 190-220 DEG C, Stress control 0.4-0.6MPa, described one
The control of gas phase ratio is 15-30 mass % after level flash distillation, and the control of liquid phase ratio is 70-85 mass %.
Preferably, the temperature control of the two-stage flash is 200-220 DEG C, Stress control 0.4-0.6MPa, described two
The control of gas phase ratio is 5-10 mass % after level flash distillation, and the control of liquid phase ratio is 90-95 mass %.
Preferably, control into the temperature of the two-stage flash liquid phase in product fractionating column charging heating furnace and be
200-220℃。
Traditional preheating-pressure release-flash distillation-heating stove heat is hydrocracked production by Pass through above-mentioned technical proposal, the present invention
The fractional method of product is improved to pressure release-one-level preheating-two level preheating-primary flash-three-level preheating-two-stage flash-heating furnace and added
The method of heat, the logistics of stripper bottom product is after feed relief valve pressure release, stream temperature reduction, then preheat through one-level, two
Higher flash temperature is can reach without higher heat exchange heat source temperature during level preheating, then is dodged by three-level preheating and two level
Steam, the increase of flashed vapour Phase Proportion can be made, flash liquid Phase Proportion reduces, and effectively reduces the negative of product fractionating column charging heating furnace
Lotus, realize the energy-saving of system entirety.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is hydrocracked product fractionating system schematic flow sheet provided by the invention；
Fig. 2 is the schematic flow sheet of conventional hydrocracking product fractionating system.
Description of reference numerals
1 hydrogen sulfide stripping tower 2 feeds relief valve
The two level preheater of 3 one-level preheater 4
The three-level preheater of 5 primary flash tank 6
The product fractionating column of 7 two-stage flash tank 8 feeds heating furnace
The stripper bottom product logistics of 9 product fractionating column 10
The pre- hot of the one-level of logistics 12 after 11 pressure releases
The pre- primary flash gas phase of hot 14 of 13 two levels
The pre- hot of the three-level of 15 primary flash liquid phase 16
17 two-stage flash gas phases 18 flash gas phase mixture stream
The heating furnace product of 19 two-stage flash liquid phase 20
Process-stream after the heat exchange of 21 process-streams 22
The bottom of towe fractionated products of 23 product fractionating columns
24 once exchange heat after bottom of towe fractionated products logistics
Bottom of towe fractionated products logistics after 25 secondary heat exchanges
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
First aspect present invention, there is provided a kind of hydrocracked product fractionating system, the system include：Hydrogen sulfide stripping tower 1,
Feed relief valve 2, one-level preheater 3, two level preheater 4, primary flash tank 5, three-level preheater 6, two-stage flash tank 7, product
Fractionating column feeds heating furnace 8 and product fractionating column 9；Wherein, the tower base stream outlet of hydrogen sulfide stripping tower 1 and charging relief valve 2
Material inlet be connected, the material outlet of charging relief valve 2 is connected with the material inlet of one-level preheater 3, and the one-level preheats
The material outlet of device 3 is connected with the material inlet of two level preheater 4, the material outlet and primary flash of the two level preheater 4
The material inlet of tank 5 is connected, and the primary flash tank 5 has primary flash gaseous phase outlet and primary flash liquid-phase outlet, described
The primary flash liquid-phase outlet of primary flash tank 5 is connected with the material inlet of three-level preheater 6, the thing of the three-level preheater 6
Material outlet is connected with the material inlet of two-stage flash tank 7, and there is the two-stage flash tank 7 two-stage flash gaseous phase outlet and two level to dodge
Steam liquid-phase outlet, the material inlet of the two-stage flash liquid-phase outlet and product fractionating column charging heating furnace 8 of the two-stage flash tank 7
It is connected, the product fractionating column 9 has flash distillation gas phase entrance and heating furnace product inlet, and the one-level of the primary flash tank 5 is dodged
Vapor phase exports and the two-stage flash gaseous phase outlet of two-stage flash tank 7 is connected with the flash distillation gas phase entrance of product fractionating column 7, described
The material outlet of product fractionating column charging heating furnace 8 is connected with the heating furnace product inlet of product fractionating column 7.It will be let out with traditional
The hydrocracked product fractionating system that pressure valve is arranged on after preheater is compared, and the system that first aspect present invention provides is by pressure release
Valve is connected to after hydrogen sulfide stripping tower, and the pressure release of feed stream elder generation can reduce temperature, then preheated through one-level, two level preheating when
Higher flash temperature is can reach without higher heat exchange heat source temperature, then by three-level preheating and two-stage flash, can be made
The increase of flashed vapour Phase Proportion, flash liquid Phase Proportion reduce, and effectively reduce the load of product fractionating column charging heating furnace, realize whole
Body it is energy-saving.In order to adapt to this transformation, the heat exchange area of one-level preheater can be increased, to cause logistics fully to change
Heat, reach required temperature.Further, since system energy consumption reduces, heating furnace can be fed to product fractionating column and carry out underload
Adaptability reform, the method for transformation is well known to those skilled in the art, and the present invention repeats no more.
According to the first aspect of the invention, the one-level preheater 3 also has one-level preheater heat transferring medium entrance and one
The outlet of level preheater heat transferring medium, the one-level preheater heat transferring medium entrance in two on product fractionating column 9 with circulating logistics
Outlet is connected；Also there is the two level preheater 4 two level preheater heat transferring medium entrance and two level preheater heat transferring medium to export,
The two level preheater heat transferring medium entrance is connected with the bottom product outlet on product fractionating column 9；The three-level preheater 6 is also
Exported with three-level preheater heat transferring medium entrance and three-level preheater heat transferring medium, the three-level preheater heat transferring medium entrance
It is connected with the outlet of two level preheater heat transferring medium.
Second aspect of the present invention, there is provided a kind of fractional method of hydrocracked product, this method include：A, make to split from hydrogenation
Change the hydrocracked product in reactor out to be stripped in hydrogen sulfide stripping tower 1, obtained stripper bottom product thing
Stream 10 first passes through charging relief valve 2 and carries out pressure release, and the logistics after pressure release is preheated into one-level preheater 3, and it is pre- to obtain one-level
Hot 12, the pre- hot 12 of one-level is entered two level preheater 4 and continue to preheat, obtain the pre- hot 13 of two level；
B, the pre- hot 13 of two level for obtaining step a enters primary flash tank 5 and carries out primary flash, obtains the He of primary flash gas phase 14
Primary flash liquid phase 15；C, the primary flash liquid phase 15 for obtaining step b enters three-level preheater 6 and preheated, and obtains three-level
Pre- hot 16；D, the pre- hot 16 of three-level for obtaining step c enters two-stage flash tank 7 and carries out two-stage flash, obtains two level
Flash gas phase 17 and two-stage flash liquid phase 19；E, the two-stage flash liquid phase 19 for obtaining step d enters the charging of product fractionating column and added
Hot stove 8 is heated, and obtains heating furnace product 20, the heating furnace product 20 is entered from the bottom of product fractionating column 9 and is divided
Evaporate processing；Make the primary flash gas phase 14 that step b is obtained and the two-stage flash gas phase 17 that step d is obtained from the product fractionating column
7 middle part carries out fractionation processing.After feeding relief valve pressure release, stream temperature reduces the logistics of stripper bottom product,
Preheated again through one-level, two level preheating when can reach higher flash temperature without higher heat exchange heat source temperature, then by three
Level preheating and two-stage flash, the increase of flashed vapour Phase Proportion can be made, flash liquid Phase Proportion reduces, and effectively reduces product fractionating column
The load of heating furnace is fed, is realized overall energy-saving.
According to the second aspect of the invention, the bottom product logistics of the hydrogen sulfide stripping tower 1 is through feeding the pressure release of relief valve 2
Pressure before can be 0.8-1.2MPa and temperature can be 190-210 DEG C, and the pressure after feeding the pressure release of relief valve 2 can be with
It can be 180-205 DEG C to control as 0.5-0.7MPa and temperature.
According to the second aspect of the invention, the logistics of stripper bottom product is after feeding relief valve pressure release, stream temperature
Less than 205 DEG C are reduced to, thus temperature can be used as heat exchange of 210-250 DEG C of the process-stream 21 as one-level preheater 3
Thermal source.The process-stream 21 circulates logistics in may come from two in product fractionating column 9, can be from other works
Process system, as long as meeting said temperature scope.Logistics is circulated in described two and refers to that the stage casing of product fractionating column second is flowed back, and
When circulating logistics during the process-stream 21 is two, the logistics 22 after heat exchange is recycled back to the middle part of the product fractionating column 9.When
The process-stream 21 is when coming from the logistics of other process systems, and the logistics 22 after heat exchange cycles back to source streams dress
Put.
According to the second aspect of the invention, the temperature of logistics is 195-210 DEG C after one-level preheats, can be by the production
The bottom of towe fractionated products 23 that temperature in product fractionating column 9 is 250-330 DEG C continue as the heat exchange thermal source of the two level preheater 4
Two level preheating is carried out, further improves the gas phase ratio in logistics.
According to the second aspect of the invention, the temperature of the primary flash may be controlled to 190-220 DEG C, and pressure can be controlled
0.4-0.6MPa is made as, gas phase ratio may be controlled to 15-30 mass % after the primary flash, and liquid phase ratio may be controlled to
70-85 mass %.
According to the second aspect of the invention, after primary flash, in order to further improve logistics gas phase ratio, primary flash is made
Liquid phase 15 enters three-level preheater 6 and preheated, can be by tower that the temperature after two level preheater 4 exchanges heat is 210-250 DEG C
Heat exchange thermal source of the bottom fractionated products logistics 24 as the three-level preheater 6.
According to the second aspect of the invention, in order to further increase flashed vapour Phase Proportion, enter the pre- hot 16 of three-level
Two-stage flash tank 7 carries out two-stage flash, and the temperature of the two-stage flash may be controlled to 200-220 DEG C, and pressure may be controlled to
0.4-0.6MPa, gas phase ratio may be controlled to 5-10 mass % after the two-stage flash, and liquid phase ratio may be controlled to 90-95
Quality %.
According to the second aspect of the invention, the two level that control enters in product fractionating column charging heating furnace 8 is dodged
The temperature of steaming liquid phase 19 is 200-220 DEG C.
According to the second aspect of the invention, one that the step b at the middle part for entering the product fractionating column 7 is obtained is controlled
The temperature for the two-stage flash gas phase 17 that level flash distillation gas phase 14 and step d are obtained is 200-220 DEG C.
Pass through above-mentioned technical proposal, the fractional method of hydrocracked product provided by the invention can reduce product fractionating column and enter
Expect heating furnace load 20-30%, the energy consumption of whole device reduces 5-20%, has the advantages of energy-efficient.
The present invention is further illustrated by embodiment below in conjunction with accompanying drawing, but therefore the present invention is not taken office
What is limited.
Embodiment
As shown in figure 1, the hydrocracked product from hydrocracking reactor out is set to be carried out in hydrogen sulfide stripping tower 1
Stripping, obtained stripper bottom product logistics 10 first pass through charging relief valve 2 and carry out pressure release, and the logistics 11 after pressure release enters one
Level preheater 3 is preheated, and obtains the pre- hot 12 of one-level, the pre- hot 12 of one-level is entered two level preheater 4 and is continued
Preheated, obtain the pre- hot 13 of two level；The pre- hot 13 of two level enters primary flash tank 5 and carries out primary flash, obtains one
Level flash distillation gas phase 14 and primary flash liquid phase 15；Primary flash liquid phase 15 enters three-level preheater 6 and preheated, and it is pre- to obtain three-level
Hot 16；The pre- hot 16 of three-level enters two-stage flash tank 7 and carries out two-stage flash, obtains two-stage flash gas phase 17 and two level is dodged
Steaming liquid phase 19；Two-stage flash liquid phase 19 enters product fractionating column charging heating furnace 8 and heated, and obtains heating furnace product 20, makes
The heating furnace product 20 carries out fractionation processing from the bottom of product fractionating column 9；What primary flash gas phase 14 and step d were obtained
Two-stage flash gas phase 17 carries out fractionation processing from the middle part of the product fractionating column 9.The heat exchange thermal source of one-level preheater 3 is
Temperature in product fractionating column 9 circulates logistics in being the two of 210-250 DEG C, the heat exchange thermal source of two level preheater 4 is fractionated for product
The bottom of towe fractionated products 23 that temperature in tower 9 is 250-330 DEG C, the heat exchange thermal source of three-level preheater 6 are to be changed through two level preheater 4
The bottom of towe fractionated products logistics 24 that temperature after heat is 210-250 DEG C.The pressure of stripper bottom product logistics 10 is 1.0MPa,
Temperature is 205 DEG C, flow 230t/h；Pressure is 0.7MPa after charging relief valve 2 carries out pressure release, and temperature is 195 DEG C；One-level
It is 2.5M kcal that preheating, which provides heat,；The pressure of the pre- hot of one-level is 0.68MPa, and temperature is 205 DEG C；Two level preheating provides
Heat is 1.3M kcal；The pressure of the pre- hot of two level is 0.65MPa, and temperature is 212 DEG C；The Stress control of primary flash is
0.45MPa, temperature control are 202 DEG C；The gas phase ratio of primary flash is 25.4 mass %, and liquid phase ratio is 74.6 mass %；
It is 1.4M kcal that three-level preheating, which provides heat,；The pressure of the pre- hot of three-level is 0.4MPa, and temperature is 210 DEG C；Two-stage flash
Stress control is 0.35MPa, and temperature control is 210 DEG C；The gas phase ratio of two-stage flash is 4.6 mass %, and liquid phase ratio is
95.4 quality %；The temperature for controlling the two-stage flash liquid phase 19 fed into product fractionating column in heating furnace 8 is 210 DEG C；Control
The temperature of primary flash gas phase 14 and two-stage flash gas phase 17 into the middle part of product fractionating column 9 is respectively 202 DEG C and 210
℃；The load of product fractionating column charging heating furnace 8 is 12.73M kcal；The energy consumption of whole device is that 29.5 kilograms of mark oil/tons are former
Material.
Comparative example
This comparative example uses 2,000,000 tons/year of hydrocracking unit product fractionating column feeding process flows of certain petroleum chemical enterprise, such as
Shown in Fig. 2, the hydrocracked product from hydrocracking reactor out is stripped in hydrogen sulfide stripping tower 1, obtain
Stripper bottom product logistics 10 enter one-level preheater 3 and preheated, obtain the pre- hot of one-level, then preheat one-level
Product enters primary flash tank 5 after the pressure release of relief valve 2 and carries out primary flash, obtains primary flash gas phase 14 and primary flash liquid
Phase 15；Primary flash gas phase 14 is directly entered product fractionating column 9, and primary flash liquid phase 15 enters product fractionating column charging heating furnace
8 are heated, and obtain heating furnace product 20, the heating furnace product 20 is carried out from the bottom of product fractionating column 9 at fractionation
Reason.The heat exchange thermal source of one-level preheater 3 is to circulate logistics during the temperature in product fractionating column 9 is the two of 210-250 DEG C.Stripper
The pressure of bottom product logistics 10 is 1.0MPa, and temperature is 205 DEG C, flow 230t/h；It is 1.8M that one-level preheating, which provides heat,
kcal；The pressure of the pre- hot of one-level is 0.9MPa, and temperature is 212 DEG C；The pre- hot of one-level carries out pressure release through feeding relief valve 2
Pressure is 0.65MPa afterwards, and temperature is 203 DEG C；The Stress control of primary flash is 0.45MPa, and temperature control is 193 DEG C；One-level
The gas phase ratio of flash distillation is 20.6 mass %, and liquid phase ratio is 79.4 mass %；Control enters product fractionating column charging heating furnace 8
In primary flash liquid phase 15 temperature be 193 DEG C；Temperature of the control into the primary flash gas phase 14 at the middle part of product fractionating column 9
Spend for 193 DEG C；The load of product fractionating column charging heating furnace 8 is 16.80M kcal；The energy consumption of whole device is 33.0 kilograms of marks
Oil/ton raw material.
From embodiment and the result of comparative example, compared with conventional method, method of the invention produces stripper bottom of towe
Its temperature is reduced to 195 DEG C by 205 DEG C after the pressure release of product logistics elder generation；One-level, two level preheater increase heat 3.8Mkcal altogether；One-level
Flash temperature improves 9 DEG C；Primary flash gas phase ratio is improved to 25.4% by 20.6%；Primary flash liquid phase ratio is by 79.4%
It is reduced to 74.6%；Three-level preheater increase heat 1.4Mkcal；Two-stage flash gas phase ratio is 4.6%；Two-stage flash liquid phase
Ratio is 95.4%；One-level, two-stage flash gas phase totally 28.8%, adds 8.2%, liquid phase ratio is after two-stage flash
71.2%；Product fractionating column heating furnace load reduction about 24.2%；Plant energy consumption reduces about 10.6%.Energy-saving effect of the present invention shows
Write.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of hydrocracked product fractionating system, it is characterised in that the system includes：Hydrogen sulfide stripping tower (1), charging pressure release
Valve (2), one-level preheater (3), two level preheater (4), primary flash tank (5), three-level preheater (6), two-stage flash tank (7),
Product fractionating column charging heating furnace (8) and product fractionating column (9)；
Wherein, the tower base stream outlet of hydrogen sulfide stripping tower (1) is connected with the material inlet of charging relief valve (2), feeds pressure release
The material outlet of valve (2) is connected with the material inlet of one-level preheater (3), the material outlet and two of the one-level preheater (3)
The material inlet of level preheater (4) is connected, and the material of the material outlet and primary flash tank (5) of the two level preheater (4) enters
Mouth is connected, and the primary flash tank (5) has primary flash gaseous phase outlet and primary flash liquid-phase outlet, the primary flash tank
(5) primary flash liquid-phase outlet is connected with the material inlet of three-level preheater (6), and the material of the three-level preheater (6) goes out
Mouth is connected with the material inlet of two-stage flash tank (7), and there is the two-stage flash tank (7) two-stage flash gaseous phase outlet and two level to dodge
Steam liquid-phase outlet, the material of the two-stage flash liquid-phase outlet and product fractionating column charging heating furnace (8) of the two-stage flash tank (7)
Entrance is connected, and the product fractionating column (9) has flash distillation gas phase entrance and heating furnace product inlet, the primary flash tank (5)
Primary flash gaseous phase outlet and two-stage flash tank (7) two-stage flash gaseous phase outlet and product fractionating column (7) flash distillation gas phase
Entrance is connected, the heating furnace product inlet of the material outlet and product fractionating column (7) of the product fractionating column charging heating furnace (8)
It is connected.
2. system according to claim 1, wherein, the one-level preheater (3) also has one-level preheater heat transferring medium
Entrance and the outlet of one-level preheater heat transferring medium, the one-level preheater heat transferring medium entrance and two on product fractionating column (9)
Middle circulation stream outlet is connected；The two level preheater (4) also has two level preheater heat transferring medium entrance and two level preheater
Heat transferring medium exports, and the two level preheater heat transferring medium entrance is connected with the bottom product outlet on product fractionating column (9)；Institute
Stating three-level preheater (6), also there is three-level preheater heat transferring medium entrance and three-level preheater heat transferring medium to export, the three-level
Preheater heat transferring medium entrance is connected with the outlet of two level preheater heat transferring medium.
3. a kind of fractional method of hydrocracked product, it is characterised in that this method includes：
A, the hydrocracked product from hydrocracking reactor out is stripped in hydrogen sulfide stripping tower (1), obtain
Stripper bottom product logistics (10) first pass through charging relief valve (2) and carry out pressure release, logistics after pressure release enters one-level preheating
Device (3) is preheated, and obtains the pre- hot of one-level (12), then make the pre- hot of one-level (12) enter two level preheater (4) after
It is continuous to be preheated, obtain the pre- hot of two level (13)；
B, the pre- hot of two level (13) for obtaining step a enters primary flash tank (5) and carries out primary flash, obtains primary flash
Gas phase (14) and primary flash liquid phase (15)；
C, the primary flash liquid phase (15) for obtaining step b is preheated into three-level preheater (6), obtains the pre- hot of three-level
(16)；
D, the pre- hot of three-level (16) for obtaining step c enters two-stage flash tank (7) and carries out two-stage flash, obtains two-stage flash
Gas phase (17) and two-stage flash liquid phase (19)；
E, the two-stage flash liquid phase (19) for obtaining step d enters product fractionating column charging heating furnace (8) and heated, and is added
Hot stove product (20), the heating furnace product (20) is set to carry out fractionation processing from the bottom of product fractionating column (9)；Make step b
The two-stage flash gas phase (17) that obtained primary flash gas phase (14) and step d obtains is from the middle part of the product fractionating column (9)
Into carrying out fractionation processing.
4. the method according to claim 11, wherein, using the process-stream (21) that temperature is 210-250 DEG C as described one
The heat exchange thermal source of level preheater (3).
5. the method according to claim 11, wherein, by the tower that the temperature in the product fractionating column (9) is 250-330 DEG C
Heat exchange thermal source of the bottom fractionated products (23) as the two level preheater (4).
6. wherein, it will be according to the method for claim 5,210-250 DEG C through the temperature after two level preheater (4) heat exchange
Heat exchange thermal source of the bottom of towe fractionated products logistics (24) as the three-level preheater (6).
7. according to the method for claim 3, wherein, the bottom product logistics of the hydrogen sulfide stripping tower (1) is let out through charging
Pressure before pressure valve (2) pressure release is 0.8-1.2MPa and temperature is 190-210 DEG C, the pressure after feeding relief valve (2) pressure release
Power control is 0.5-0.7MPa and temperature is 180-205 DEG C.
8. according to the method for claim 3, wherein, the temperature control of the primary flash is 190-220 DEG C, Stress control
For 0.4-0.6MPa, the control of gas phase ratio be 15-30 mass % after the primary flash, and it is 70-85 matter that liquid phase ratio, which controls,
Measure %.
9. according to the method for claim 3, wherein, the temperature control of the two-stage flash is 200-220 DEG C, Stress control
For 0.4-0.6MPa, the control of gas phase ratio be 5-10 mass % after the two-stage flash, and it is 90-95 matter that liquid phase ratio, which controls,
Measure %.
10. according to the method for claim 3, wherein, control feeds the institute in heating furnace (8) into the product fractionating column
The temperature for stating two-stage flash liquid phase (19) is 200-220 DEG C.
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| CN110511784A (en) * | 2019-09-02 | 2019-11-29 | 上海优华系统集成技术股份有限公司 | It is hydrocracked fractionating column tail oil heat utilization system and method |
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| US7087153B1 (en) * | 2003-02-04 | 2006-08-08 | Uop Llc | Combination hydrocracking process for the production of ultra low sulfur diesel |
| CN202730081U (en) * | 2012-06-13 | 2013-02-13 | 中国石油天然气股份有限公司 | Hydrocracking device for inhibiting temperature runaway by utilizing reaction pressure |
| CN103059918A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Vacuum distillation method for gradual gasification segmented feed |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US7087153B1 (en) * | 2003-02-04 | 2006-08-08 | Uop Llc | Combination hydrocracking process for the production of ultra low sulfur diesel |
| CN103059918A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Vacuum distillation method for gradual gasification segmented feed |
| CN202730081U (en) * | 2012-06-13 | 2013-02-13 | 中国石油天然气股份有限公司 | Hydrocracking device for inhibiting temperature runaway by utilizing reaction pressure |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110511784A (en) * | 2019-09-02 | 2019-11-29 | 上海优华系统集成技术股份有限公司 | It is hydrocracked fractionating column tail oil heat utilization system and method |
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