CN115477958A - Quenching oil viscosity reducing system and method - Google Patents
Quenching oil viscosity reducing system and method Download PDFInfo
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- CN115477958A CN115477958A CN202110667474.1A CN202110667474A CN115477958A CN 115477958 A CN115477958 A CN 115477958A CN 202110667474 A CN202110667474 A CN 202110667474A CN 115477958 A CN115477958 A CN 115477958A
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- 238000010791 quenching Methods 0.000 title claims abstract description 77
- 230000000171 quenching effect Effects 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 33
- 230000001603 reducing effect Effects 0.000 title claims abstract description 26
- 239000002904 solvent Substances 0.000 claims abstract description 272
- 238000000605 extraction Methods 0.000 claims abstract description 128
- 238000000926 separation method Methods 0.000 claims abstract description 38
- 238000011084 recovery Methods 0.000 claims abstract description 25
- 238000002347 injection Methods 0.000 claims abstract description 16
- 239000007924 injection Substances 0.000 claims abstract description 16
- 239000003921 oil Substances 0.000 claims description 142
- 239000012071 phase Substances 0.000 claims description 76
- 239000007789 gas Substances 0.000 claims description 57
- 239000000295 fuel oil Substances 0.000 claims description 40
- 230000009467 reduction Effects 0.000 claims description 13
- 239000007792 gaseous phase Substances 0.000 claims description 11
- 238000005192 partition Methods 0.000 claims description 8
- 230000000694 effects Effects 0.000 abstract description 18
- 230000008569 process Effects 0.000 abstract description 3
- 239000000306 component Substances 0.000 description 102
- 239000000203 mixture Substances 0.000 description 7
- 239000012808 vapor phase Substances 0.000 description 7
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012533 medium component Substances 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
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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
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/302—Viscosity
Abstract
The invention discloses a quenching oil viscosity reducing system and a quenching oil viscosity reducing method, which comprise the following steps: a stripping column; an extraction tower; the solvent output end of the solvent supply device is connected with the first extraction solvent inlet and the second extraction solvent inlet; the solvent recovery device is connected with a first light component outlet and a heavy solute outlet of the extraction tower, the solvent recovery device can separate out gas phase solvent and output the gas phase solvent through a gas phase solvent output end, the gas phase solvent output end is connected with a gas phase inlet and a first solvent input end of the solvent supply device, the solvent recovery device can separate out light oil and output the light oil through a light oil output end, and the light oil output end is connected with a light oil output pipeline and a light solute injection port; this system realizes twice light, the heavy component separation of quench oil through setting up strip tower and extraction column, has not only guaranteed the separation effect of heavy component, can also alleviate the load in the twice process.
Description
Technical Field
The invention belongs to the technical field of quenching oil viscosity reduction, and particularly relates to a quenching oil viscosity reduction system and method.
Background
The steam cracking method has a leading position in the production of ethylene, an ethylene device originally enters a quenching zone after being preheated, quenching oil and quenching water provide heat and generate steam for downstream users, along with the operation at high temperature, the viscosity of the quenching oil can be gradually increased, the fluidity is worsened and blocks equipment and pipelines in severe cases, the temperature of a quenching oil tower kettle is low, the temperature of the tower top is high, the generation amount of dilution steam is reduced, a large amount of medium-pressure steam needs to be supplemented, the comprehensive energy consumption of the ethylene device is increased, more sewage is discharged, the production load of the device can be influenced in severe cases, and therefore the viscosity control of the quenching oil is always an urgent problem to solve.
In the prior art, in the traditional viscosity reducing method, steam stripping quenching oil and ethane furnace pyrolysis gas stripping quenching oil are most widely applied, and during steam stripping, lighter components are easy to separate, but medium and heavy components are hardly extracted, so that the efficiency is low; compared with a steam stripping method, the method for stripping the cracked gas of the ethane furnace can better separate light and medium components in the quenching oil, but the heat of the cracked gas is greatly wasted.
Patent documents CN104449826a and CN104449827a both disclose a method for reducing ethylene unit quenching oil viscosity reduction, the former mainly describes the method, and the latter mainly describes its system and method, although they are different, the common features are: (1) extracting by adopting a common extraction tower; and (2) the operating pressure is the supercritical pressure, namely above 4 MpaG. The problems caused by this are that the solvent and the quench oil are not sufficiently mixed in the extraction column, and the column pressure is too high, which imposes higher requirements on the column material, operation, and the like.
Patent No. CN104449808A discloses a system and a method for reducing ethylene unit quenching oil viscosity reduction, wherein quenching oil is subjected to gasification flash evaporation before entering an extraction tower, and is extracted by supercritical solvent after light components are separated. The method firstly heats the quenching oil to the maximum 500 ℃, wastes a large amount of heat energy, cannot achieve the purpose of saving energy, an extraction tower cannot well mix the solvent and the quenching oil, and the system also has the problems of manufacture, operation, stability and the like caused by overhigh pressure.
Therefore, the common quenching oil viscosity reducing method cannot achieve the purposes of saving energy consumption and efficiently separating effective components in the quenching oil, and how to reduce the viscosity of the quenching oil under mild pressure and temperature and reduce the cost is always a difficult problem in the quenching oil viscosity reducing process.
Disclosure of Invention
The invention aims to provide a quenching oil viscosity reducing system and a quenching oil viscosity reducing method aiming at the defects in the prior art, the system realizes twice light and heavy component separation of quenching oil by arranging a stripping tower and an extraction tower, not only ensures the separation effect of heavy components, but also reduces the load in two procedures, the system is also provided with a solvent recovery device, can effectively recover the solvent to realize the recycling of the solvent and reduce the cost, and the extraction tower can introduce a gas-phase solvent with the same component as the solvent into a lower end socket through a gas-phase inlet to improve the extraction effect.
To achieve the above object, the present invention provides a quenching oil viscosity reducing system, comprising:
a stripping column to which a quench oil feed line and a steam line are connected;
an extraction column, the extraction column comprising:
the tower comprises a tower barrel, a partition wall is arranged in the tower barrel, the partition wall divides the tower barrel into a first space and a second space which are mutually independent, a columnar space is arranged in the center of the interior of the tower barrel, a first solute inlet, a first extraction solvent inlet, a second solute inlet and a second extraction solvent inlet which are respectively communicated with the first space and the second space are formed in the outer wall of the tower barrel, and the first solute inlet and the second solute inlet are connected with a first heavy component outlet of the stripping tower;
the upper end socket is arranged at the upper end of the tower cylinder and is isolated from the tower cylinder, and the upper part of the upper end socket is provided with a gas phase inlet and two gas phase outlets which are respectively communicated with the first space and the second space;
the lower end socket is arranged at the lower end of the tower cylinder and is communicated with the tower cylinder, a light solute injection opening is formed in the outer wall of the lower end socket, and a heavy solute discharge opening is formed in the lower end of the lower end socket;
the rotary table device is arranged inside the lower end socket;
a solvent supply device, a solvent output end of the solvent supply device is connected with the first extraction solvent inlet and the second extraction solvent inlet;
solvent recovery unit, solvent recovery unit with the first light component export of extraction tower with heavy solute discharge port is connected, solvent recovery unit can separate out gaseous phase solvent and will gaseous phase solvent exports through gaseous phase solvent output, gaseous phase solvent output with gaseous phase entry with solvent supply device's first solvent input is connected, solvent recovery unit can separate light oil and will light oil exports through the light oil output, the light oil output with light oil export outward pipeline with the light solute injection mouth is connected.
Optionally, the first heavy component outlet is connected to the extraction tower through a first pipeline, a heavy oil pump and a heavy oil heat exchanger are disposed on the first pipeline, and an output end of the heavy oil heat exchanger is connected to the first solute inlet and the second solute inlet.
Optionally, the solvent supply device comprises:
the mixer is provided with the first solvent input end, the second solvent input end and a solvent output end, and the second solvent input end is connected with a second solvent conveying pipeline;
and one end of the second pipeline is connected with the input end of the first solvent, the other end of the second pipeline is connected with a solvent compressor, and a solvent heat exchanger is arranged on the second pipeline.
Optionally, the solvent recovery apparatus comprises:
the first solvent separation tank is provided with a first light oil input port, a first gas-phase solvent output port and a first light oil output port, and the first light oil input port is connected with the gas-phase outlet;
the second solvent separation tank is provided with a second light oil input port, a second gas-phase solvent output port and a second light oil output port, and the second light oil input port is connected with the first light oil output port;
and the third solvent separation tank is provided with a heavy oil input port, a third gas-phase solvent output port and a heavy oil output port, and the heavy oil input port is connected with the heavy solute discharge port.
Optionally, the gaseous phase export pass through the third pipeline with first light oil input connection, be provided with first valve and light oil heat exchanger on the third pipeline, first light oil delivery outlet pass through the fourth pipeline with second light oil input connection, be provided with the second valve on the fourth pipeline, heavy solute discharge port pass through the fifth pipeline with heavy oil input connection, be provided with the third valve on the fifth pipeline.
Optionally, the first vapor phase solvent output port, the second vapor phase solvent output port, and the third vapor phase solvent output port are connected to the solvent compressor through a sixth pipeline.
Optionally, the second light component outlet and the second light oil outlet of the stripping tower are respectively connected to the light oil export pipeline through a seventh pipeline and an eighth pipeline, and the heavy oil outlet is connected to the heavy oil export pipeline.
The invention also provides a quenching oil viscosity reducing method, which utilizes the quenching oil viscosity reducing system and comprises the following steps:
steam stripping is carried out on the quenching oil, and a first heavy component and a first light component are separated;
extracting the first heavy component by an extraction tower and a solvent supply device to obtain a second heavy component and a second light component;
recovering the solvent in the second heavy fraction and the second light fraction and delivering the recovered solvent to the solvent supply.
Optionally, the extracting the first heavy component by the extraction tower and the solvent supply device to obtain a second heavy component and a second light component comprises:
delivering the first heavy component to the extraction column through a first solute inlet and a second solute inlet;
delivering an extraction solvent to the extraction column through a first extraction solvent inlet and a second extraction solvent inlet with the solvent supply;
and separating the second heavy component and the second light component by contacting the first heavy component with the extraction solvent in the extraction tower, wherein the second heavy component is discharged through a heavy solute discharge port, and the second light component is discharged through a gas phase outlet.
Optionally, the extracting the first heavy component by the extraction tower and the solvent supply device to obtain a second heavy component and a second light component further comprises:
injecting a recovered solvent into the upper end socket through a gas phase inlet, wherein the recovered solvent is a gas phase solvent;
the gas-phase solvent enters the lower end socket downwards through the columnar space and contacts with the first heavy component;
and injecting the second light component into the lower end socket through the light solute injection port.
The invention provides a quenching oil viscosity reducing system and a quenching oil viscosity reducing method, which have the beneficial effects that:
1. the system realizes the twice light and heavy component separation of the quenching oil by arranging the stripping tower and the extraction tower, thereby not only ensuring the separation effect of the heavy component, but also lightening the load in the two procedures;
2. the system is also provided with a solvent recovery device, so that the solvent can be effectively recovered, the recycling of the solvent is realized, and the cost is reduced;
3. the extraction tower of the system can introduce a gas phase solvent with the same component as the solvent into the lower end socket through the gas phase inlet, so that the extraction effect is improved;
4. the extraction tower of the system is provided with a rotary disc device, so that the flowability of heavy component solute can be increased, and blockage can be prevented;
5. the tower drum of the extraction tower of the system is provided with two mutually independent spaces, when the tower drum on one side breaks down, the tower drum on the other side can be used for working, and the continuous operation of the process is ensured;
6. due to the improvement of the extraction effect of the extraction tower and the increase of the fluidity of heavy component solute, the operation pressure of the extraction tower is obviously reduced, and the operation stability of the system is improved.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings, wherein like reference numerals generally represent like parts in the exemplary embodiments of the present invention.
FIG. 1 shows a schematic diagram of a quench oil detackification system according to a first embodiment of the present invention.
FIG. 2 shows a schematic diagram of the configuration of an extraction column of a quench oil viscosity reduction system according to a first embodiment of the present invention.
FIG. 3 is a schematic top sectional view of an upper head of an extraction column of a quench oil viscosity reduction system according to an embodiment of the invention.
FIG. 4 is a schematic top sectional view of the tower of an extraction column of a quenching oil viscosity reduction system according to an embodiment of the invention.
FIG. 5 is a schematic top sectional view of the lower head of an extraction column of a quench oil viscosity reduction system according to an embodiment of the invention.
FIG. 6 is a flow chart illustrating a method of viscosity reduction of quench oil according to a second embodiment of the present invention.
Description of the reference numerals:
1. a tower drum; 2. a partition wall; 3. a first space; 4. a second space; 5. a columnar space; 6. a first solute inlet; 7. a first extraction solvent inlet; 8. a second solute inlet; 9. a second extraction solvent inlet; 10. an upper end enclosure; 11. a gas phase inlet; 12. a gas phase outlet; 13. light oil export lines; 14. a lower end enclosure; 15. a light solute injection port; 16. a heavy solute vent; 17. a turntable device; 18. a drive motor; 19. a rotating shaft; 20. an impeller; 21. a blade; 22. a column plate; 23. a stripping column; 24. a quench oil feed line; 25. a steam line; 26. a first pipeline; 27. a heavy oil pump; 28. a heavy oil heat exchanger; 29. a mixer; 30. a second pipeline; 31. a solvent heat exchanger; 32. a first solvent separation tank; 33. a second solvent separation tank; 34. a third solvent separation tank; 35. a heavy oil export pipeline; 36. a third pipeline; 37. a light oil heat exchanger; 38. a fourth pipeline; 39. a fifth pipeline; 40. a sixth pipeline; 41. a second solvent transfer line; 42. a seventh line; 43. an eighth line; 44. a solvent compressor.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
Example one
As shown in FIGS. 1-5, the present invention provides a quenching oil viscosity reducing system, comprising:
stripping tower 23, wherein quenching oil feeding line 24 and steam line 25 are connected to stripping tower 23;
an extraction column, the extraction column comprising:
the device comprises a tower barrel 1, a partition wall 2 is arranged in the tower barrel 1, the partition wall 2 divides the tower barrel 1 into a first space 3 and a second space 4 which are mutually independent, a columnar space 5 is arranged in the center of the interior of the tower barrel 1, a first solute inlet 6, a first extraction solvent inlet 7, a second solute inlet 8 and a second extraction solvent inlet 9 which are respectively communicated with the first space 3 and the second space 4 are formed in the outer wall of the tower barrel 1, and the first solute inlet 6 and the second solute inlet 8 are connected with a first heavy component outlet of a stripping tower 23;
the upper end socket 10 is arranged at the upper end of the tower barrel 1 and is isolated from the tower barrel 1, and the upper part of the upper end socket 10 is provided with a gas phase inlet 11 and two gas phase outlets 12 which are respectively communicated with the first space 3 and the second space 4;
the lower end socket 14 is arranged at the lower end of the tower barrel 1 and communicated with the tower barrel 1, a light solute injection opening 15 is formed in the outer wall of the lower end socket 14, and a heavy solute discharge opening 16 is formed in the lower end of the lower end socket 14;
the rotary table device 17 is arranged inside the lower end socket 14;
the solvent output end of the solvent supply device is connected with the first extraction solvent inlet 7 and the second extraction solvent inlet 9;
the solvent recovery device is connected with a first light component outlet and a heavy solute outlet 16 of the extraction tower, the solvent recovery device can separate gas phase solvent and output the gas phase solvent through a gas phase solvent output end, the gas phase solvent output end is connected with a gas phase inlet 11 and a first solvent input end of the solvent supply device, the solvent recovery device can separate light oil and output the light oil through a light oil output end, and the light oil output end is connected with a light oil output pipeline 13 and a light solute injection port 15.
Specifically, medium-pressure or high-pressure steam is adopted in the stripping tower 23, the steam temperature is higher than 200 ℃, the weight ratio of the steam to the quenching oil is 0.1-99, the quenching oil is subjected to steam stripping, and a first heavy component and a first light component are separated; after pressurization and temperature reduction/heating, the first heavy component is respectively input into an extraction tower as a high-viscosity solute through a first solute inlet 6 and a second solute inlet 8, the operating pressure in the extraction tower can be lower than 1Mpa, and the operating temperature is 30-120 ℃; the solvent supply device inputs an extraction solvent into the extraction tower, a second heavy component and a second light component are obtained through separation of the extraction tower, the second light component and the second heavy component are recovered from the gas-phase solvent through the solvent recovery device, and the recovered gas-phase solvent can be returned to the solvent supply device for recycling, so that the cost is saved; meanwhile, the recovered gas-phase solvent can be input into the extraction tower through the gas-phase inlet 11, so that the extraction effect is improved; light oil separated from the second light component by the solvent recovery device can converge with the first light component, and the converged light component can be output through the light oil output pipeline 13 or can be partially output to the light solute injection port 15, so that the fluidity of high-viscosity solute in the extraction tower is improved.
Optionally, the steam is 1.2MPaG, medium pressure steam at 280 ℃; the weight ratio of steam to quench oil is 0.1 to 99.
Alternatively, the extraction solvent is a C4 alkane and the weight ratio of extraction solvent to stripped quench oil is 5.
Optionally, the carousel means 17 comprises:
the driving motor 18 is arranged at the top end of the upper end socket 10;
the rotating shaft 19 is connected with the output end of the driving motor 18, the rotating shaft 19 penetrates through the upper end socket 10 and the columnar space 5, and the lower end of the rotating shaft extends into the lower end socket 14;
and an impeller 20 disposed at a lower end of the rotating shaft 19, wherein at least two blades 21 are disposed around the impeller 20.
Specifically, the driving motor 18 can drive the impeller 20 and the blades 21 to rotate through the rotating shaft 19, the impeller 20 and the blades 21 are arranged close to the heavy solute discharge port 16, and then the heavy solute in the lower seal head 14 is driven to be discharged through the heavy solute discharge port 16.
Optionally, a plurality of trays 22 are provided in the tower 1 in both the first space 3 and the second space 4, each tray 22 having a size smaller than the cross-sectional size of the first space 3 and the second space 4.
Specifically, a plurality of trays 22 are arranged along a horizontal cross-section in the first space 3 and the second space 4, each tray 22 blocking a portion of the cross-section in the first space 3 or the second space 4.
Alternatively, a plurality of trays 22 are staggered within the first space 3 and the second space 4 such that the flow trajectories of the liquid and the gas within the first space 3 and the second space 4 are S-shaped.
Specifically, the plurality of tower plates 22 arranged in a staggered manner can increase the residence time of the solute and the extraction solvent in the first space 3 and the second space 4, and can fully mix the solute and the extraction solvent, thereby improving the extraction effect.
Optionally, the cylindrical space 5 extends through the tower 1 and is in communication with the upper head 10 and the lower head 14.
Specifically, the columnar space 5 is communicated with the upper end socket 10 and the lower end socket 14, so that gas with the same components as the solvent can be conveniently injected into the lower end socket 14 through the columnar space 5, and further the gas is contacted with the high-viscosity solute, and the extraction effect is improved.
Optionally, the cylindrical space 5 is isolated from the first space 3 and the second space 4 by an outer wall.
Specifically, the outer wall of the cylindrical space 5 may prevent the gas with the same composition as the solvent injected into the lower head 14 from contacting the gas and the liquid in the tower 1.
Alternatively, the cross-sectional shape of the columnar space 5 is circular.
In other examples, the cross-sectional shape of the columnar space 5 may also be square or polygonal.
Alternatively, the cross-sectional dimension of the rotating shaft 19 is smaller than the cross-sectional dimension of the cylindrical space 5.
Specifically, the sectional dimension of the rotating shaft 19 is smaller than the sectional dimension of the columnar space 5, so that a gap can be ensured between the rotating shaft 19 and the columnar space 5, the injection of gas with the same components as the solvent is facilitated, and the rotating shaft 19 can be prevented from contacting the outer wall of the columnar space 5 when rotating.
Alternatively, the cross-sectional shape of the rotating shaft 19 is circular.
In other examples, the cross-sectional shape of the rotating shaft 19 may also be a square or a regular polygon.
Optionally, the upper head 10 is filled with a gas phase, which is a gas or an inert gas having the same composition as the solvent.
Specifically, the gas phase in the upper end enclosure 10 is not in contact with the liquid phase or the gas phase in the tower barrel 1, a partition plate can be arranged between the upper end enclosure 10 and the tower barrel 1 for isolation, and the gas phase is arranged to ensure that only the gas phase exists in the upper end enclosure 10.
In this embodiment, the first heavy component outlet is connected to the extraction tower through a first pipeline 26, a heavy oil pump 27 and a heavy oil heat exchanger 28 are disposed on the first pipeline 26, and the output end of the heavy oil heat exchanger 28 is connected to the first solute inlet 6 and the second solute inlet 8.
Specifically, the first heavy component separated after steam stripping enters the extraction tower after pressurization and temperature reduction/heating.
In the present embodiment, the solvent supply device includes:
a mixer 29, wherein the mixer 29 is provided with a first solvent input end, a second solvent input end and a solvent output end, and the second solvent input end is connected with a second solvent conveying pipeline 41;
one end of the second pipeline 30 is connected with the first solvent input end, the other end is connected with a solvent compressor 44, and the second pipeline 30 is provided with a solvent heat exchanger 31.
Specifically, the extraction solvent adopts one or a mixture of C3-C5 alkane or alkene, and the weight ratio of the extraction solvent to the stripped quenching oil is 0.5-10; the extraction solvent is in a subcritical state, namely the pressure and the temperature are both less than the critical pressure and the critical temperature of the solvent or the mixed solvent; the mixer 29 can mix the recovered vapor phase solvent with a newly introduced second solvent, and supply the mixture to the extraction column.
In this embodiment, the solvent recovery apparatus includes:
the first solvent separation tank 32 is provided with a first light oil input port, a first gas phase solvent output port and a first light oil output port, and the first light oil input port is connected with the gas phase outlet 12;
a second solvent separation tank 33, wherein a second light oil input port, a second gas phase solvent output port and a second light oil output port are arranged on the second solvent separation tank 33, and the second light oil input port is connected with the first light oil output port;
and a third solvent separation tank 34, wherein the third solvent separation tank 34 is provided with a heavy oil input port, a third gas phase solvent output port and a heavy oil output port, and the heavy oil input port is connected with the heavy solute discharge port 16.
Specifically, the first solvent separation tank 32 and the second solvent separation tank 33 are light oil solvent separation tanks, and the third solvent separation tank 34 is a heavy oil solvent separation tank.
In this embodiment, the gas phase outlet 12 is connected to the first light oil inlet via a third line 36, the third line 36 is provided with a first valve and a light oil heat exchanger 37, the first light oil outlet is connected to the second light oil inlet via a fourth line 38, the fourth line 38 is provided with a second valve, the heavy solute outlet 16 is connected to the heavy oil inlet via a fifth line 39, and the fifth line 39 is provided with a third valve.
In this embodiment, the first vapor phase solvent output, the second vapor phase solvent output, and the third vapor phase solvent output are connected to a solvent compressor 44 through a sixth line 40.
Specifically, the recovered solvents in the first gas-phase solvent output port, the second gas-phase solvent output port, and the third gas-phase solvent output port are gas-phase solvents, and are mixed in the sixth pipeline 40 and then fed back to the solvent compressor 44, and then enter the solvent supply device in a circulating manner, so that the solvent is recycled.
In this embodiment, the second light component outlet and the second light oil outlet of the stripping tower 23 are connected to the light oil export line 13 through a seventh line 42 and an eighth line 43, respectively, and the heavy oil export is connected to the heavy oil export line 35.
Specifically, the first light components and the light oil in the second light component outlet and the second light oil outlet are merged and delivered to the outside in the light oil delivery line 13.
In summary, when the quenching oil viscosity reducing system provided by the invention is used, quenching oil and medium-pressure steam are conveyed into the stripping tower 23 through the quenching oil feeding pipeline 24 and the steam pipeline 25, the quenching oil is separated into a first heavy component and a first light component by steam stripping, the first heavy component is conveyed to the heavy oil output pipeline 35, and the first light component is divided into two parts which are respectively conveyed into the first space 3 and the second space 4 of the extraction tower; the first solvent enters the mixer 29 through the solvent heat exchanger 31 by the solvent compressor 44, meanwhile, the second solvent is conveyed to the mixer 29 by conveying to form an extraction solvent, the extraction solvent is respectively conveyed to the first space 3 and the second space 4 of the extraction tower by two branches, the first solute inlet 6 and the second solute inlet 8 are arranged above the first extraction solvent inlet 7 and the second extraction solvent inlet 9, the solute of the first heavy component is in countercurrent contact with the extraction solvent to form a second light component and a second heavy component, the second light component is upward, the second heavy component is downward, the second light component is discharged through the gas phase outlet 12, and the second heavy component enters the lower end socket 14 and is discharged through the heavy solute discharge port 16.
The discharged second heavy component and the second light component enter a solvent recovery device, and the second light component passes through a first solvent separation tank 32 and a second solvent separation tank 33 and is separated twice, so that light oil and a gas phase solvent are effectively separated, and the separation effect is improved; the second heavy component passes through a third solvent separation tank 34 to separate heavy oil and gas phase solvent, the heavy oil can be output through a heavy oil output pipeline 35, and the gas phase solvent flows back to a solvent compressor 44 of the solvent supply device, so that the recycling of the solvent is realized.
In addition, in order to improve the extraction effect and ensure the fluidity of the second heavy component, a gas-phase solvent with the same component as the extraction solvent can be injected into the upper end enclosure 10 from the gas-phase inlet 11, so that only a gas phase is ensured in the upper end enclosure 10, and the gas phase enters the lower end enclosure 14 from the columnar space 5 downwards and is further contacted with the solute of the first heavy component with high viscosity, so that the solute is further extracted, the extraction effect is improved, and the viscosity reduction effect is improved; and the rotary table device 17 in the lower end enclosure 14 can rotate, drive the heavy solute to discharge from the heavy solute discharge port 16 outside the column, when the first heavy component solute has too high viscosity, resulting in poor flowability of the solute in the lower end enclosure 14, light oil recovered by the solute recovery device can be injected through the light solute injection port 15 as light solute, so as to increase the flowability of the first heavy component solute; because the above means has effectively improved the extraction effect, has increased the mobility of first heavy ends solute, has improved the visbreaking effect to the quench oil, the operating pressure of this extraction tower can reduce by a wide margin, and the operating pressure of extraction tower can drop to below 1Mpa, improves operating stability.
Example two
As shown in FIG. 6, the present invention also provides a method for reducing the viscosity of quenching oil, which uses the above-mentioned quenching oil viscosity reducing system, the method includes:
carrying out steam stripping on the quenching oil to separate out a first heavy component and a first light component;
extracting the first heavy component through an extraction tower and a solvent supply device to obtain a second heavy component and a second light component;
recovering the solvent in the second heavy component and the second light component and transferring the recovered solvent to a solvent supply device.
Specifically, the method sequentially carries out steam stripping and extraction in an extraction tower on the cold oil to realize the separation of light and heavy components of the quenching oil twice, thereby not only ensuring the separation effect of the light and heavy components, but also improving the viscosity reducing effect of the quenching oil and lightening the load in two procedures; the method also adopts the solvent recovery device to effectively recover the solvent, thereby realizing the recycling of the solvent and reducing the cost.
In this embodiment, extracting the first heavy component by the extraction column and the solvent supply device to obtain the second heavy component and the second light component includes:
delivering the first heavy component to the extraction column through a first solute inlet and a second solute inlet;
conveying an extraction solvent to an extraction column through a first extraction solvent inlet and a second extraction solvent inlet by using a solvent supply device;
and separating the second heavy component and the second light component by contacting the first heavy component with the extraction solvent in the extraction tower, wherein the second heavy component is discharged through a heavy solute discharge port, and the second light component is discharged through a gas phase outlet.
In this embodiment, extracting the first heavy component by the extraction column and the solvent supply device to obtain the second heavy component and the second light component further includes:
injecting the recovered solvent into the upper end socket through a gas phase inlet, wherein the recovered solvent is a gas phase solvent;
the gas-phase solvent enters the lower end socket downwards through the columnar space and contacts with the first heavy component;
and injecting a second light component into the lower end socket through the light solute injection port.
Specifically, the recovered gas-phase solvent is introduced into the extraction tower from the gas-phase inlet to the lower end socket, so that the extraction effect is improved, and the viscosity reducing effect of the quenching oil is further improved; and part of the second light component is input back to the extraction tower through the light solute injection port, so that the viscosity of the solute in the extraction tower can be further reduced, the fluidity of the solute is improved, the blockage is avoided, and the viscosity reducing effect is further improved.
In conclusion, the viscosity of the quenching oil is 9845mPa.s (50 ℃) as an example when the quenching oil viscosity reducing method provided by the invention is implemented: introducing 10t/h of quenching oil into a stripping tower, stripping by 5t/h of 1.2MPaG and 280 ℃ medium-pressure steam to separate a first light component of 2439kg/h, separating a first heavy component from the lower part of the stripping tower, pressurizing to 0.9MPaG through a heavy oil pump and a heavy oil heat exchanger, 79 ℃, and dividing into two parts to enter an extraction tower; the first solvent circulated after the solvent compressor and solvent heat exchanger reached a subcritical state, 0.9MPaG,79.2 ℃, and the second solvent from outside the battery limits: mixing a subcritical n-butane solvent at a speed of 75.6t/h by a mixer to form an extraction solvent, dividing the extraction solvent into two parts, and feeding the two parts into an extraction tower, wherein the ratio of quenching oil to the extraction solvent is 1; separating the extracted second light component from the upper part of the extraction tower, decompressing to 0.8MPaG, heating to 80 ℃, and entering a first solvent separation tank; the 35.3t/h gas phase solvent can be recovered from the top of the first solvent separation tank, and the light oil at the bottom enters the second solvent separation tank after being decompressed to 0.3 MPaG; the gas phase solvent of 0.21t/h can be recovered from the top of the second solvent separation tank, and 1570kg/h of light oil at the bottom is mixed with the light oil of the first light component at the top of the stripping tower and then output through a light oil output pipeline; the extracted heavy oil is separated from the bottom of the extraction tower, directly decompressed to 0.1MPaG and then enters a third solvent separation tank, 1.73t/h of gas-phase solvent can be recovered from the top of the third solvent separation tank, and the heavy oil is output from a heavy oil output pipeline; the three gas-phase solvents are converged and then return to the solvent supply device for cyclic utilization; if necessary, partial gas phase solvent can be injected into the extraction tower through the gas phase inlet to improve the extraction effect, and if necessary, partial light oil can be injected into the extraction tower through the light solute injection port to improve the fluidity of the solute. In the embodiment, the total amount of the three gas-phase solvents is 37.24t/h, the solvent recovery rate is 98 percent, and the purity is 99.9 percent; the viscosity of the treated and converged viscosity-reducing oil 4009kg/h is less than 5mPa.s (50 ℃).
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. A quench oil detackification system, comprising:
a stripping column to which a quench oil feed line and a steam line are connected;
an extraction column, the extraction column comprising:
the tower comprises a tower barrel, a partition wall is arranged in the tower barrel, the partition wall divides the tower barrel into a first space and a second space which are mutually independent, a columnar space is arranged in the center of the interior of the tower barrel, a first solute inlet, a first extraction solvent inlet, a second solute inlet and a second extraction solvent inlet which are respectively communicated with the first space and the second space are formed in the outer wall of the tower barrel, and the first solute inlet and the second solute inlet are connected with a first heavy component outlet of the stripping tower;
the upper end socket is arranged at the upper end of the tower cylinder and is isolated from the tower cylinder, and the upper part of the upper end socket is provided with a gas phase inlet and two gas phase outlets which are respectively communicated with the first space and the second space;
the lower end socket is arranged at the lower end of the tower cylinder and communicated with the tower cylinder, a light solute injection opening is formed in the outer wall of the lower end socket, and a heavy solute discharge opening is formed in the lower end of the lower end socket;
the rotary table device is arranged inside the lower end socket;
a solvent supply device, a solvent output end of the solvent supply device is connected with the first extraction solvent inlet and the second extraction solvent inlet;
solvent recovery unit, solvent recovery unit with the first light component export of extraction tower with heavy solute discharge port is connected, solvent recovery unit can separate out gaseous phase solvent and will gaseous phase solvent exports through gaseous phase solvent output, gaseous phase solvent output with gaseous phase entry with solvent supply device's first solvent input is connected, solvent recovery unit can separate light oil and will light oil exports through the light oil output, the light oil output with light oil export outward pipeline with the light solute injection mouth is connected.
2. The quench oil detackification system of claim 1, wherein the first heavy component outlet is connected to the extraction column by a first line, the first line having a heavy oil pump and a heavy oil heat exchanger disposed thereon, the output of the heavy oil heat exchanger being connected to the first solute inlet and the second solute inlet.
3. The quench oil detackification system of claim 1, wherein the solvent supply comprises:
the mixer is provided with the first solvent input end, a second solvent input end and a solvent output end, and the second solvent input end is connected with a second solvent conveying pipeline;
and one end of the second pipeline is connected with the input end of the first solvent, the other end of the second pipeline is connected with a solvent compressor, and a solvent heat exchanger is arranged on the second pipeline.
4. The quench oil detackification system of claim 3, wherein the solvent recovery device comprises:
the first solvent separation tank is provided with a first light oil input port, a first gas phase solvent output port and a first light oil output port, and the first light oil input port is connected with the gas phase outlet;
the second solvent separation tank is provided with a second light oil input port, a second gas-phase solvent output port and a second light oil output port, and the second light oil input port is connected with the first light oil output port;
and the third solvent separation tank is provided with a heavy oil input port, a third gas-phase solvent output port and a heavy oil output port, and the heavy oil input port is connected with the heavy solute discharge port.
5. The quenching oil viscosity breaking system of claim 4, wherein the gas phase outlet is connected to the first light oil inlet via a third line, the third line having a first valve and a light oil heat exchanger disposed thereon, the first light oil outlet being connected to the second light oil inlet via a fourth line, the fourth line having a second valve disposed thereon, the heavy solute outlet being connected to the heavy oil inlet via a fifth line, the fifth line having a third valve disposed thereon.
6. The quench oil detackification system of claim 4, wherein the first gas-phase solvent output, the second gas-phase solvent output, and the third gas-phase solvent output are connected to the solvent compressor by sixth lines.
7. The quench oil detackification system of claim 4, wherein the second light component outlet and the second light oil outlet of the stripping column are connected to the light oil export line through a seventh line and an eighth line, respectively, and the heavy oil outlet is connected to the heavy oil export line.
8. A method of reducing viscosity of quench oil using the quench oil viscosity reduction system of any one of claims 1-7, the method comprising:
steam stripping is carried out on the quenching oil, and a first heavy component and a first light component are separated;
extracting the first heavy component through an extraction tower and a solvent supply device to obtain a second heavy component and a second light component;
recovering the solvent in the second heavy fraction and the second light fraction and delivering the recovered solvent to the solvent supply.
9. The method of claim 8, wherein the extracting the first heavy component by the extraction tower and the solvent supply device to obtain a second heavy component and a second light component comprises:
delivering the first heavy component to the extraction column through a first solute inlet and a second solute inlet;
delivering an extraction solvent to the extraction column through a first extraction solvent inlet and a second extraction solvent inlet with the solvent supply;
and separating the second heavy component and the second light component by contacting the first heavy component with the extraction solvent in the extraction tower, wherein the second heavy component is discharged through a heavy solute discharge port, and the second light component is discharged through a gas phase outlet.
10. The method of claim 9, wherein the extracting the first heavy component by the extraction tower and the solvent supply device to obtain a second heavy component and a second light component further comprises:
injecting a recovered solvent into the upper end socket through a gas phase inlet, wherein the recovered solvent is a gas phase solvent;
the gas-phase solvent enters the lower end socket downwards through the columnar space and contacts with the first heavy component;
and injecting the second light component into the lower end socket through the light solute injection port.
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