CN111484868A - Naphtha fraction device - Google Patents

Naphtha fraction device Download PDF

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Publication number
CN111484868A
CN111484868A CN201910779739.XA CN201910779739A CN111484868A CN 111484868 A CN111484868 A CN 111484868A CN 201910779739 A CN201910779739 A CN 201910779739A CN 111484868 A CN111484868 A CN 111484868A
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China
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outlet pipe
oil
oil outlet
component
pipe
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邵文
刘一鸣
宋业阳
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China National Petroleum Corp
CNPC EastChina Design Institute Co Ltd
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China National Petroleum Corp
CNPC EastChina Design Institute Co Ltd
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Priority to CN201910779739.XA priority Critical patent/CN111484868A/en
Publication of CN111484868A publication Critical patent/CN111484868A/en
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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
    • C10G7/00—Distillation of hydrocarbon oils

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  • Chemical & Material Sciences (AREA)
  • 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 a naphtha fractionating device, and belongs to the field of petroleum fractionation. The device comprises: fractionating tower, air condenser, reflux tank and reboiling furnace. The fractionation column comprises a first portion, a second portion, and a third portion; the first part is connected with an air condenser, and the air condenser is connected with a reflux tank; the third part is connected with a reboiling furnace. Thus, when naphtha enters the naphtha fractionating apparatus, C which is fractionated4The following components are drawn off at the bottom of the reflux drum C5‑C6Component can be extracted from the second fraction C7The above components may be drawn from the bottom of the third section. Therefore, the naphtha can be efficiently and quickly separated from the fractionating tower, and the fractionating process is simplified. In addition, because the equipment required by the fractionating device is reduced, the energy consumption and the occupied area of the equipment are reduced, and the investment cost is reduced.

Description

Naphtha fraction device
Technical Field
The invention relates to the field of petroleum fractionation, in particular to a naphtha fractionation device.
Background
The products of naphtha fractionation can be used as feed for isomerization and catalytic reforming. For example, C in naphtha7The components can be used as raw materials for catalytic reforming;c in naphtha5-C6Component C can be used as the raw material for isomerization4The following components can be used as raw materials of alkyl gasoline or laminated gasoline, etc. Therefore, it is necessary to provide a naphtha fractionation apparatus for performing a naphtha fractionation operation.
The related art provides a fractionation apparatus including: fractionating tower and rectifying tower connected in series, and fractionating tower top4The following components, C to be remained5-C6Component (A) and (C)7Introducing the above components into a rectifying tower, and separating C from the top of the rectifying tower5-C6Component C is separated from the bottom of the rectifying tower7The components are as follows.
In the process of implementing the invention, the inventor finds that the related art has at least the following problems:
when naphtha is fractionated by the series connection of the fractionating tower and the rectifying tower, the fractionation process is long, the used equipment is more, the occupied area and the energy consumption are large, and the investment cost is higher.
Disclosure of Invention
The invention provides a naphtha fractionating device, which can solve the problems of long fractionating process, more used equipment, large occupied area and energy consumption and higher operation cost in the related technology. The technical scheme is as follows:
the embodiment of the invention provides a naphtha fractionating device, which comprises: a fractionating tower, an air condenser, a reflux tank and a reboiling furnace;
the fractionating tower comprises a first part, a second part and a third part which are sequentially communicated from top to bottom;
the top of the first part is connected with the air condenser through a first oil outlet pipe, the air condenser is connected with the reflux tank, the bottom of the reflux tank is connected with a second oil outlet pipe, the second oil outlet pipe is used for extracting one part of the first component, and the other part of the first component returns to the fractionating tower for further fractionation; the first side of the second part is connected with a first oil inlet pipe, the first oil inlet pipe is used for allowing naphtha to enter the fractionating tower, the first side of the second part is connected with a third oil outlet pipe, and the third oil outlet pipe is used for extracting a second component; a second oil inlet pipe is connected to the side edge of the third part, the second oil inlet pipe is connected with the first side of the reboiling furnace, a fourth oil outlet pipe is connected to the bottom of the third part, the fourth oil outlet pipe is connected with the first side of the reboiling furnace, the fourth oil outlet pipe is used for extracting one part of third components, the reboiling furnace is used for heating the other part of third components, and the heated other part of third components enter the fractionating tower through the second oil inlet pipe for further fractionation;
the second part also comprises an oil collecting tray, a downcomer, a liquid collecting tank and a riser; one end of the downcomer is connected with the first side of the oil collecting tray, and the other end of the downcomer extends into the oil collecting tray; the liquid collecting groove is arranged on a first side of the oil collecting tray, the first side is opposite to the first side, and the bottom end of the liquid collecting groove is communicated with the third oil outlet pipe; the downcomer is used to separate the second component from the first component; the liquid collecting tank is used for collecting the second component; and a gas phase channel is arranged in the middle of the oil collecting tray, one end of the gas riser is communicated with the gas phase channel, and the other end of the gas riser extends into the first part.
Optionally, the apparatus further comprises a pressure pump disposed at the bottom of the return tank, the pressure pump being configured to pressurize the component in the return tank.
Optionally, the apparatus further comprises a reflux line, one end of the reflux line is connected with the bottom of the reflux tank, the other end of the reflux line is connected with the first part, and the reflux line is used for returning the other part of the first component to the fractionating tower for further fractionation.
Optionally, the reflux pressure of the reflux line is 0.3MPa to 0.5 MPa.
Optionally, the device still includes pressure controller, first play oil pipe the second play oil pipe first advance oil pipe the third play oil pipe the fourth play oil pipe with all be provided with on the second advances oil pipe pressure controller.
Optionally, the device further comprises a flow controller, wherein the first oil outlet pipe, the second oil outlet pipe, the first oil inlet pipe, the third oil outlet pipe, the fourth oil outlet pipe and the second oil inlet pipe are both provided with the flow controller.
Optionally, the device still includes temperature sensor, first play oil pipe the second play oil pipe first advance oil pipe the third play oil pipe the fourth play oil pipe with all be provided with on the second advances oil pipe temperature sensor.
Optionally, the number of trays in the oil collection tray is 75-85.
Optionally, the fractionation column has a feed pressure in the range of from 0.3MPa to 0.5 MPa.
Optionally, the fractionation column has a fractionation pressure of from 0.2MPa to 0.5 MPa.
The technical scheme of the invention has the following beneficial effects:
the device provided by the embodiment of the invention adopts an air condenser pair C at the top of the fractionating tower4Condensing the following components by a reflux drum connected with an air condenser4Refluxing the following components to fractionate a part C of naphtha4The following components are withdrawn at the bottom of the reflux drum and C can be withdrawn through the third outlet of the second section of the fractionation column5-C6Withdrawing the fraction C through a fourth outlet line at the bottom of the fractionating tower7The above components are extracted, and the other part C7The components are heated by a reboiling furnace and then enter a fractionating tower for further splitting. Therefore, the light component, the intermediate component and the heavy component of naphtha can be efficiently and quickly separated from the fractionating tower by one fractionating tower, and the fractionating process is simplified. In addition, because the equipment required by the fractionating device is reduced, the energy consumption and the occupied area of the equipment are reduced, and the investment cost is reduced.
Drawings
FIG. 1 is a schematic view of the structure of a naphtha fractionation unit according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of the structure of a naphtha fractionation unit according to an embodiment of the present invention;
fig. 3 is a schematic structural view of a naphtha fractionating apparatus according to an embodiment of the present invention.
Reference numerals:
1: a fractionating column; 11: a first section of a fractionation column; 12: a second portion; 13: a third portion; 2: an air condenser; 3: a reflux tank; 31: a return line; 4: a reboiling furnace; 5: a first oil outlet pipe; 6: a second oil outlet pipe; 7: a first oil inlet pipe; 8: a third oil outlet pipe; 9: a fourth oil outlet pipe; 10: a second oil inlet pipe; 14: an oil collecting tray; 15: a downcomer; 16: a liquid collecting tank; 17: a gas lift pipe; 18: a pressure pump; 19: a pressure controller; 20: a flow controller.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, embodiments of the present invention will be described in detail with reference to the accompanying drawings.
C produced by fractionating naphtha5-C6The components can be used as isomerization raw oil to enter an isomerization device. The isomerization device is an important device of a refinery, which can produce isomerized gasoline with high octane number and no olefin, aromatic hydrocarbon and sulfur, provides excellent blending components for blending gasoline, and the obtained isomerized hydrocarbon can be further dehydrogenated to produce isomerized olefin, and provides raw materials for producing MTBE (methyl tert-butyl ether, MTBE for short).
C produced by fractionating naphtha7The components can be used as catalytic reforming raw oil to enter a catalytic reforming device. The catalytic reforming device is an important device of an oil refinery, the reformed oil produced by the catalytic reforming device is rich in aromatic hydrocarbon, has the characteristics of high octane number, low olefin content, basically no sulfur and the like, can be directly used as a high octane number blending component of the vehicle gasoline, and can also be used for producing aromatic hydrocarbon products such as benzene, toluene, xylene and the like.
However, since the impurity content in the typical catalytic reforming stock oil exceeds a predetermined limit amount, the catalytic reforming stock oil needs to be pretreated before catalytic reforming. The reforming pretreatment device has three functions, namely cutting of catalytic reforming raw oil, hydrofining and removal of heteroatom compounds in the catalytic reforming raw oil, and dehydration and hydrogen sulfide removal of hydrogenation products.
With the stricter environmental regulations on the exhaust gas emission of gasoline, countries have strict limits on the benzene content in gasoline, and the benzene in the reformate is one of the main sources of benzene in gasoline. One of the main proposals for reducing the benzene content in reformate is to remove the benzene-producing reactant from the raw oil by catalytic reforming in a reforming pretreatment apparatus. In view of the above, it is necessary to provide a fractionating apparatus for fractionating C in naphtha5-C6Component (A) and (C)7The components are separated out and used as raw materials of catalytic reforming.
Fig. 1 is a schematic structural view of a naphtha fractionating apparatus according to an embodiment of the present invention. Referring to fig. 1, the apparatus includes: a fractionating tower 1, an air condenser 2, a reflux tank 3 and a reboiling furnace 4.
The fractionating column 1 comprises a first section 11, a second section 12 and a third section 13 which are sequentially communicated from top to bottom;
the top of the first part 11 is connected with an air condenser 2 through a first oil outlet pipe 5, the air condenser 2 is connected with a reflux tank 3, the bottom of the reflux tank 3 is connected with a second oil outlet pipe 6, the second oil outlet pipe 6 is used for extracting a part of first components, and the other part of the first components are returned to the fractionating tower 1 for further fractionation; a first oil inlet pipe 7 is connected to a first side of the second part 12, naphtha enters the fractionating tower 1 through the first oil inlet pipe 7, a third oil outlet pipe 8 is connected to a second side of the second part 12, and the third oil outlet pipe 8 is used for extracting a second component; a second oil inlet pipe 10 is connected to the side edge of the third part 13, the second oil inlet pipe 10 is connected with the first side of the reboiling furnace 4, a fourth oil outlet pipe 9 is connected to the bottom of the third part 13, the fourth oil outlet pipe 9 is connected with the second side of the reboiling furnace 4, the fourth oil outlet pipe 9 is used for extracting one part of the third components, the reboiling furnace 4 is used for heating the other part of the third components, and the heated other part of the third components enter the fractionating tower 1 through the second oil inlet pipe 10 for further fractionation;
the second section 12 also includes a collector tray 14, a downcomer 15, a sump 16 and a riser 17; one end of the downcomer 15 is connected with the first side of the oil collecting tray 14, and the other end of the downcomer 15 extends into the oil collecting tray 14; the liquid collecting groove 16 is arranged on a first side of the oil collecting tray 14, the first side is opposite to the first side, and the bottom end of the liquid collecting groove 16 is communicated with the third oil outlet pipe 8; a downcomer 15 for separating the second component from the first component; a sump 16 for collecting the second component; the middle of the oil collecting tray 14 is provided with a gas phase channel, one end of the gas riser 17 is communicated with the gas phase channel, and the other end of the gas riser 17 extends into the first part 11.
The device provided by the embodiment of the invention at least has the following technical effects.
The device provided by the embodiment of the invention passes through an air condenser 2 pair C at the top of a fractionating tower 14Condensing the following components by a reflux drum 3 connected to an air condenser 24Refluxing the following components to fractionate a part C of naphtha4The following components are withdrawn at the bottom of the reflux drum 3 and C can be taken off via the third outlet line 8 of the second section 12 of the fractionation column 15-C6Withdrawing the fraction C through a fourth outlet line 9 at the bottom of the fractionating tower 17The above components are extracted, and the other part C7The above components are heated by a reboiling furnace 4 and then enter a fractionating tower 1 for further splitting. Therefore, the light component, the intermediate component and the heavy component of naphtha can be efficiently and quickly separated from the fractionating tower 1 through one fractionating tower 1, and the fractionating process is simplified. In addition, because the equipment required by the fractionating device is reduced, the fuel gas, the steam, the deoxygenated water, the electric quantity and the like required by the equipment are changed, and the energy consumption of the equipment is reduced. And because a tower and accessory supporting facilities thereof are reduced, the occupied area is saved, and the investment cost is reduced, wherein the occupied area can be reduced by more than 40 percent, and the investment cost can be saved by more than 30 percent.
It should be noted that the first component mentioned in the examples of the present invention may be C4The second component may be C5-C6Component C as the third component7The components are as follows. Naphtha is fractionated in a fractionating column 1 to obtain C4The following components, C5-C6Component (A) and (C)7The above component wherein C4The following components are gas phase light components, C5-C6The component is a liquid phase component, C7The components are liquid phase heavy components. The first section 11 of the fractionation column 1 is a light fraction separation zone, i.e., a zone where C can be separated4The following components and C5-C6Component (A) and (C)7The above components are separated, and the second part 12 is a rectification zone, i.e. a zone where C can be separated5-C6Component (A) and (C)7The above components are separated off and the third section 13 is a stripping zone, i.e.where C is obtained7The components are as follows.
The side of the third portion 13 may be the same side as the first side of the second portion 12, or may be the same side as the second side of the second portion 12.
The air condenser 2 is used for condensing C4The following components are condensed into gas-liquid phase mixed components from a single gas phase component, and the reflux tank 3 is used for condensing C4The following components are subjected to gas-liquid phase separation, and the reboiling furnace 4 is used for providing a heat source for the fractionating tower 1 so as to ensure the temperature in the fractionating tower 1.
Finally, the size of the oil collecting tray 14 may be set according to the diameter of the fractionating tower 1, for example, when the diameter of the fractionating tower 1 is 4m (meter), the diameter of the oil collecting tray 14 may be 3.7m, and the diameter of the oil collecting tray 14 is not limited thereto in the embodiment of the present invention, as long as the oil collecting tray can conveniently collect C5-C6The components are mixed. And when the bottom end of the collecting tank 16 and the third oil outlet pipe 8 are positioned at the same horizontal plane, no pressure difference exists between the collecting tank 16 and the third oil outlet pipe 8.
The gas phase channel is arranged in the middle of the oil collecting tray 14 in order to ensure that C is arranged below the oil collecting tray 144The following components may be normally raised to the first section 11 of the fractionation column 1, and also the gas-liquid phase in the fractionation column 1 may be maintained in equilibrium.
Illustratively, fractionation using the naphthaWhen the device fractionates naphtha, the naphtha enters the fractionating tower 1 through the first oil inlet pipe 7 connected with the first side of the second part 12 for fractionation to obtain C4The following components, C5-C6Component (A) and (C)7The components are as follows. Wherein C is separated from naphtha by a fractionating tower 14When the following components pass through the oil collecting tray 14, C is because the gas phase channel is arranged in the middle of the oil collecting tray 14 and is connected with one end of the gas-lift pipe 17, and the other end of the gas-lift pipe 17 extends into the first part 114The following components may rise through a riser 17 into the first section 11 at the top of the fractionation column 1. C4The following components enter the air condenser 2 through a first oil outlet pipe 5 at the top of the first part 11 for condensation, and the condensed component C4The following components were fed to the reflux drum 3. In reflux drum 3 for condensed C4Subjecting the following components to gas-liquid phase separation to obtain gas phase C4The following components are taken as liquefied gas products and are pumped out through a second oil outlet pipe 6 at the bottom of the reflux tank 3 to obtain liquid-phase C4The following components are returned to the fractionation column 1 as reflux.
Then when naphtha is fractionated by a fractionating tower 1, C is fractionated5-C6When component (C) is5-C6The components flow into the downcomer 15 through the other end of the downcomer 15 that extends into the second section 12. Since one end of the downcomer 15 is connected to the oil collecting tray 14, C5-C6The components flow into the oil collection tray 14, and C, which will flow into the oil collection tray 145-C6The components are collected in a sump 16. Since the bottom end of the sump 16 is connected to the third outlet line 8, C5-C6When the components are collected in the sump 16, C5-C6The components are pumped out through a third flow line 8 connected to the second side of the second portion 12. Finally, a part C of the tower bottom is treated7The above components are pumped out through a fourth oil outlet pipe 9 connected with the bottom of the third part 13, and the rest C7The components enter a reboiling furnace 4 through the second side of the reboiling furnace 4, and the rest C heated by the reboiling furnace 47The components enter the fractionating tower 1 through the second oil inlet pipe 10 to be fractionated again. Thus, naphtha can be efficiently and quickly separated from the fractionating tower 1, and the process is simplifiedAnd (4) a fractionation process. In addition, because the equipment required by the fractionating device is reduced, the equipment energy consumption is low, the occupied area is small, and the investment cost is also low.
Optionally, referring to fig. 2, the apparatus further comprises a pressurizing pump 18, the pressurizing pump 18 being provided at the bottom of the reflux drum 3, the pressurizing pump 18 being used for pressurizing the components in the reflux drum 3.
Note that the pressurizing pump 18 can supply C in the reflux tank 34The following components are at a pressure such that they can be returned to the fractionation column 1 from the top of the reflux drum 3.
For example, when C4The following components are condensed by an air condenser 2 and then changed into gas-liquid mixed components from single gas-phase components, and then the gas-liquid components are subjected to gas-liquid phase separation by a reflux tank 3, and a pressure pump 18 at the bottom of the reflux tank 3 supplies certain pressure to the liquid-phase components, so that the liquid-phase components flow back into the fractionating tower 1 from the top of the reflux tank 3.
Optionally, the apparatus further comprises a reflux line 31, one end of the reflux line 31 is connected to the bottom of the reflux drum 3, the other end is connected to the first section 11, and the reflux line 31 is used for returning another part of the first component to the fractionating tower 1 for further fractionation.
It should be noted that the pipe diameter of the return line 31 can be applied to C in the return tank 3 by the pressurizing pump 184The pressure of the component is set, for example, when the pressurizing pump 18 applies the pressure to C in the reflux drum 34The pipe diameter of the return line 31 may be set to 65mm (millimeters) at a pressure of 0.1MPa of the following components. Embodiments of the present invention are not limited to this for the diameter of the return line 31. The reflux pressure of the reflux pipeline 31 is 0.3MPa-0.5MPa, and the specific value of the reflux pressure can be determined according to C in the reflux tank 34The amounts of the following components are set, for example, when C4The following components are 150g/m2In this case, the reflux pressure may be 0.3 MPa.
Illustratively, when the pressurizing pump 18 feeds C in the reflux drum 34C of liquid phase at a certain pressure of the following components4The following components flow into the return line 31, and C is given through the return line 314Reflux pressure of the following composition was adjusted so that C4The following components are returned to the fractionation column 1.
Optionally, referring to fig. 3, the apparatus further comprises a pressure controller 19, and the pressure controller 19 is disposed on each of the first oil outlet pipe 5, the second oil outlet pipe 6, the first oil inlet pipe 7, the third oil outlet pipe 8, the fourth oil outlet pipe 9 and the fifth oil outlet pipe 10.
In addition, the pressure controller 19 is capable of controlling the pressure of the naphtha-separated component passing through the respective components during the fractionation operation.
Illustratively, a pressure controller 19 is provided on the first oil outlet pipe 5 to control the tower top C4The pressure at which the following components enter the air condenser 2 through the first oil outlet pipe 5 is set to ensure the C entering the air condenser 24The following components can be sufficiently condensed. A pressure controller 19 is provided on the second outlet pipe 6 for controlling the C extracted as liquefied gas product4The following components were added to ensure that the reflux operation was adequately performed. The pressure controller 19 is arranged on the first oil inlet pipe 7, so that the pressure of naphtha entering the fractionating tower 1 can be controlled, and the energy consumption of a fractionating device is reduced. A pressure controller 19 is provided on the third flow line 8 to determine C drawn through the third flow line 85-C6The pressure of the components, reduces the energy consumption of the second part 12. A pressure controller 19 is provided on the fourth oil line 9 to determine C drawn through the fourth oil line 97The above component pressures reduce the energy consumption of the third section 13. A pressure controller 19 is provided on the second feed line 10 to determine the flow rate C of the heavy boiler 4 back to the fractionating tower 17Pressure of the above components, ensure C7The above components can be further sufficiently subjected to a fractionation operation.
It should be noted that the setting position of the pressure controller 19 may be preset according to the use requirement, and the setting position of the pressure controller 19 is not limited to this in the embodiment of the present invention.
Optionally, referring to fig. 3, the apparatus further includes a flow controller 20, and the flow controller 20 is disposed on each of the first oil outlet pipe 5, the second oil outlet pipe 6, the first oil inlet pipe 7, the third oil outlet pipe 8, the fourth oil outlet pipe 9 and the second oil inlet pipe 10.
Additionally, the flow controller 20 may control the flow of the naphtha separated components through the various components during the fractionation operation.
Illustratively, the flow controller 20 is provided on the first flowline 5 to control the top C of the tower4The flow rate of the following components when entering the air condenser 2 through the first oil outlet pipe 5 is ensured to C entering the air condenser 24The following components can be sufficiently condensed. A flow controller 20 is provided on the second outlet pipe 6 for controlling the C extracted as liquefied gas product4The flow rates of the following components. The flow controller 20 is arranged on the first oil inlet pipe 7, so that the flow of naphtha entering the fractionating tower 1 can be controlled, and the energy consumption of a fractionating device is reduced. A flow controller 20 is provided on the third flowline 8 to determine the C drawn through the third flowline 85-C6The flow of the components, reduces the energy consumption of the second portion 12. A flow controller 20 is provided on the fourth flowline 9 to determine the C drawn through the fourth flowline 97The flow rate of the above components reduces the energy consumption of the third section 13. A flow controller 20 is provided on the second feed pipe 10 to determine the flow rate C of the heavy boiling furnace 4 back to the fractionating tower 17Flow rate of the above components, ensure C7The above components can be further sufficiently subjected to a fractionation operation.
It should be noted that the setting position of the flow controller 20 may be preset according to the use requirement, and the specific setting position of the flow controller 20 in the embodiment of the present invention is not limited thereto.
Optionally, referring to fig. 3, the device further includes a temperature sensor 21, and the temperature sensors 21 are disposed on the first oil outlet pipe 5, the second oil outlet pipe 6, the first oil inlet pipe 7, the third oil outlet pipe 8, the fourth oil outlet pipe 9 and the second oil inlet pipe 10.
In addition, the temperature sensor 21 may control the temperature of the naphtha separated component passing through the various components during the fractionation operation.
Illustratively, a temperature sensor 21 is provided on the first outlet pipe 5 to control the tower top C4The following components are introduced into the air condenser 2 through the first oil outlet pipe 5 at a temperature to ensure C introduced into the air condenser 24The following components can be fully mixedCondensation is carried out. The second oil outlet pipe 6 is provided with a temperature sensor 21 which can control the C extracted as liquefied gas product4The temperatures of the following components. The temperature sensor 21 is arranged on the first oil inlet pipe 7, so that the flow of naphtha entering the fractionating tower 1 can be controlled, and the energy consumption of a fractionating device is reduced. A temperature sensor 21 is provided on the third outlet pipe 8 to determine C drawn through the third outlet pipe 85-C6The temperature of the components, reduces the energy consumption of the second part 12. A temperature sensor 21 is provided on the fourth oil outlet pipe 9, and C extracted through the fourth oil outlet pipe 9 can be determined7The above temperatures of the components reduce the energy consumption of the third section 13. The temperature sensor 21 is arranged on the second oil inlet pipe 10, and the C flowing back to the fractionating tower 1 through the reboiling furnace 4 can be determined7Temperature of the above components, ensure C7The above components can be further sufficiently subjected to a fractionation operation.
It should be noted that the installation position of the temperature sensor 21 can be preset according to the use requirement, and the specific installation position of the temperature sensor 21 in the embodiment of the present invention is not limited thereto.
Optionally, the number of the trays in the oil collecting tray 14 is multiple, and for example, the number of the trays can be 75-85. Exemplary, there may be 75, 76, 77, 78, 79, 80, 81, 82, 83, 84, 85, etc.
It should be noted that the trays in the oil collecting trays 14 are used for collecting the respective components fractionated from naphtha. When the number of trays is larger, more components can be collected, thereby saving the separation flow.
Illustratively, C when naphtha is fractionated5-C6Component (A) and (C)7The oil collection trays 14 may be aligned with C as the above components flow through the oil collection trays 145-C6Component (A) and (C)7The above components are separated. When the number of the tower trays is between 75 and 85, C can be ensured5-C6Component (A) and (C)7The above components are sufficiently separated so that the components in the sump 16 are all C5-C6And (4) components.
Alternatively, the feed pressure to the fractionation column 1 is from 0.3MPa to 0.5 MPa.
As an example, it may be 0.3MPa, 0.35MPa, 0.4MPa, 0.41MPa, 0.45MPa, 0.5MPa or the like.
It should be noted that the feeding pressure is the pressure when the naphtha enters the fractionating tower 1 through the first oil inlet pipe 7.
Illustratively, the amount of feed pressure value affects the energy consumed by the fractionation column 1. When the feeding pressure is 0.3MPa-0.5MPa, the energy consumed by the fractionating tower 1 can be reduced while the naphtha is fully fractionated by the fractionating tower 1.
Optionally, the fractionation column 1 has a fractionation pressure of 0.2MPa to 0.5 MPa.
As an example, it may be 0.2MPa, 0.3MPa, 0.35MPa, 0.4MPa, 0.41MPa, 0.45MPa, 0.5MPa or the like.
The fractionation pressure is a pressure at which naphtha is fractionated in the fractionation tower 1.
Illustratively, the amount of fractionation operation pressure value affects the energy consumed by the fractionation column 1. When the fractionation operation pressure is 0.2MPa to 0.5MPa, the energy consumed by the fractionating tower 1 can be reduced while the naphtha is sufficiently fractionated by the fractionating tower 1.
For the sake of easy understanding, the naphtha fractionating apparatus provided in the examples of the present invention will be illustrated in comparison with the naphtha fractionating apparatus provided in the related art.
Naphtha is fractionated using a naphtha fractionator according to an embodiment of the present invention, wherein the composition of naphtha entering the naphtha fractionator is shown in table 1 and the process parameters are shown in table 2. Wherein the process conditions are as follows: the throughput was 47 ten thousand tons/year, the feed pressure was 0.41MPa (g, gauge), the operating pressure of the fractionating column was 0.35MPa (g), and the number of trays required was 80. Fraction of C in the product5Purity of component (mol ) 99%, C5-C6Purity of component (C) 98.4% (mol)7The purity of the above components is 99.3% (mol). It can be seen from table 2 that the energy saving of the naphtha fractionating apparatus provided in the example of the present invention is 18.7%.
TABLE 1
Components mol％
C2(C2Component (A) TRACE
C3(C3Component (A) TRACE
IC4(Isobutane) TRACE
NC4(n-butane) TRACE
IC5(isopentane) 0.0990
NC5(n-pentane) 0.1113
C5OLENIN(C5Olefins) TRACE
CP (cyclopentane) 0.0270
IC6(isohexane) 0.0974
NC6(n-hexane)) 0.0590
C6OLENIN(C6Olefins) TRACE
MCP (methylcyclopentane) 0.0153
CH (cyclohexane) 0.0126
Benzene (BENZENE) 0.0244
C7 +(C7The above components) 0.5540
Total of 1.0000
TABLE 2
Figure BDA0002176197430000111
Naphtha was fractionated using a two-column series fractionator provided in the related art, wherein the composition of naphtha entering the naphtha fractionator is shown in table 1 and the process parameters are shown in table 2. The process conditions are as follows: the treatment capacity is 47 ten thousand tons per year, the feeding pressure is 0.41MPa (g), the operation pressure of a fractionating tower is 0.35MPa (g), and C removal is carried out6The column operating pressure was 0.12MPa (g) and the number of trays required was 61. Fraction of C in the product5The purity of the following components is 99% (mol), C5-C6Purity of component (C) is 98% (mol)7The purity of the components is 99 percent (mol).
It should be noted that the content of a part of the components in table 1 is trace, which means that the content of the component is small and is close to 0.
From the above, it can be seen that the apparatus provided in the embodiment of the present invention fractionates naphtha, and then the fraction C4The following components, C5-C6Component (A) and (C)7The components are high in separation purity, and energy is effectively saved compared with a fractionation device provided by the related technology.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims (10)

1. A naphtha fractionation plant, characterized in that the plant comprises: a fractionating tower (1), an air condenser (2), a reflux tank (3) and a reboiling furnace (4);
the fractionating tower (1) comprises a first part (11), a second part (12) and a third part (13) which are communicated with each other from top to bottom in sequence;
the top of the first part (11) is connected with the air condenser (2) through a first oil outlet pipe (5), the air condenser (2) is connected with the reflux tank (3), the bottom of the reflux tank (3) is connected with a second oil outlet pipe (6), the second oil outlet pipe (6) is used for extracting one part of the first component, and the other part of the first component returns to the fractionating tower (1) for further fractionation;
a first oil inlet pipe (7) is connected to the first side of the second part (12), the first oil inlet pipe (7) is used for introducing naphtha into the fractionating tower (1), a third oil outlet pipe (8) is connected to the first side of the second part (12), and the third oil outlet pipe (8) is used for extracting a second component;
a second oil inlet pipe (10) is connected to the side edge of the third part (13), the second oil inlet pipe (10) is connected with the first side of the reboiling furnace (4), a fourth oil outlet pipe (9) is connected to the bottom of the third part (13), the fourth oil outlet pipe (9) is connected with the first side of the reboiling furnace (4), the fourth oil outlet pipe (9) is used for extracting one part of the third component, the reboiling furnace (4) is used for heating the other part of the third component, and the heated other part of the third component enters the fractionating tower (1) through the second oil inlet pipe (10) for further fractionation;
the second section (12) further comprises a collector tray (14), a downcomer (15), a sump (16) and a riser (17);
one end of the downcomer (15) is connected with the first side of the oil collecting tray (14), and the other end of the downcomer (15) extends into the oil collecting tray (14);
the liquid collecting groove (16) is arranged on a first side of the oil collecting tray (14), the first side is opposite to the first side, and the bottom end of the liquid collecting groove (16) is communicated with the third oil outlet pipe (8);
the downcomer (15) being for separating the second component from the first component;
the sump (16) is used for collecting the second component;
a gas phase channel is arranged in the middle of the oil collecting tray (14), one end of the gas lift pipe (17) is communicated with the gas phase channel, and the other end of the gas lift pipe (17) extends into the first part (11).
2. The device according to claim 1, characterized in that the device further comprises a pressure pump (18), the pressure pump (18) being arranged at the bottom of the return tank (3), the pressure pump (18) being adapted to pressurize the components in the return tank (3).
3. The apparatus according to claim 1, further comprising a reflux line (31), wherein one end of the reflux line (31) is connected to the bottom of the reflux drum (3) and the other end is connected to the first section (11), and wherein the reflux line (31) is used for returning the other part of the first component to the fractionating column (1) for further fractionation.
4. The apparatus according to claim 3, wherein the return pressure of the return line (31) is between 0.3MPa and 0.5 MPa.
5. The apparatus according to claim 1, further comprising a pressure controller (19), wherein the pressure controller (19) is disposed on each of the first oil outlet pipe (5), the second oil outlet pipe (6), the first oil inlet pipe (7), the third oil outlet pipe (8), the fourth oil outlet pipe (9) and the second oil inlet pipe (10).
6. The apparatus according to claim 1, further comprising a flow controller (20), wherein the flow controller (20) is disposed on each of the first oil outlet pipe (5), the second oil outlet pipe (6), the first oil inlet pipe (7), the third oil outlet pipe (8), the fourth oil outlet pipe (9) and the second oil inlet pipe (10).
7. The device according to claim 1, characterized in that it further comprises a temperature sensor (21), said temperature sensor (21) being arranged on each of said first outlet pipe (5), said second outlet pipe (6), said first inlet pipe (7), said third outlet pipe (8), said fourth outlet pipe (9) and said second inlet pipe (10).
8. The apparatus of claims 1-7, wherein the number of trays in said oil collection tray (14) is 75-85.
9. The apparatus according to any of claims 1 to 7, wherein the fractionation column (1) has a feed pressure of from 0.3MPa to 0.5 MPa.
10. The apparatus according to any of claims 1 to 7, wherein the fractionation column (1) has a fractionation pressure of 0.2MPa to 0.5 MPa.
CN201910779739.XA 2019-08-22 2019-08-22 Naphtha fraction device Pending CN111484868A (en)

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