CN113736517A - Cracking stripping tower - Google Patents
Cracking stripping tower Download PDFInfo
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- CN113736517A CN113736517A CN202111251967.3A CN202111251967A CN113736517A CN 113736517 A CN113736517 A CN 113736517A CN 202111251967 A CN202111251967 A CN 202111251967A CN 113736517 A CN113736517 A CN 113736517A
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- tower
- stripping tower
- stripping
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- oil
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- 238000005336 cracking Methods 0.000 title claims abstract description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 57
- 239000001257 hydrogen Substances 0.000 claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 55
- 238000006243 chemical reaction Methods 0.000 claims abstract description 51
- 238000010438 heat treatment Methods 0.000 claims abstract description 26
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 24
- 230000023556 desulfurization Effects 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 238000010992 reflux Methods 0.000 claims description 23
- 239000012071 phase Substances 0.000 claims description 14
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 12
- 239000007791 liquid phase Substances 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 230000003009 desulfurizing effect Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 125000003118 aryl group Chemical group 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 claims description 4
- 239000011261 inert gas Substances 0.000 claims description 4
- 230000002378 acidificating effect Effects 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 abstract description 7
- 239000000446 fuel Substances 0.000 abstract description 6
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000009834 vaporization Methods 0.000 abstract description 3
- 230000008016 vaporization Effects 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 88
- 239000002283 diesel fuel Substances 0.000 description 29
- 239000002994 raw material Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- 238000005191 phase separation Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 238000004508 fractional distillation Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000010724 circulating oil Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Images
Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
-
- 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
- C10G7/12—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Landscapes
- 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 provides a cracking stripping tower, which relates to the technical field of stripping towers and comprises a reaction unit, wherein a recycle hydrogen desulfurization unit and a front stripping tower unit are arranged at the rear section of the reaction unit, and a main fractionation unit and a side stripping tower unit are sequentially arranged at the rear section of the front stripping tower unit. The invention adds the second stripping tower to strip hot low-fraction oil directly, while the first stripping tower is only used for stripping cold low-fraction oil, because the bottom oil of the cold low-fraction oil stripping tower contains a large amount of diesel components, the bottom oil can directly enter the light diesel stripping tower along with the feeding of the light diesel stripping tower, then the diesel components are extracted from the tower bottom to be used as a diesel product, the secondary vaporization of the diesel components is avoided, the feeding heating furnace of the fractionating tower can only gasify a small amount of diesel components, the load of the heating furnace is greatly reduced, the fuel consumption is correspondingly reduced, the load of the hydrogenation feeding heating furnace is synchronously reduced, the fuel consumption is also reduced, and thus the energy consumption of the device is reduced.
Description
Technical Field
The invention relates to the technical field of stripping towers, in particular to a cracking stripping tower capable of obviously reducing energy consumption.
Background
Stripping is a unit operation for recovering absorbed solute and separating the absorbent from the solute to obtain regeneration, and in some cases, stripping is also used for removing light components in liquid, for example, in the oil refining industry, steam is often used as a stripping agent to remove light components of oil varieties, so that stripping can be used in combination with absorption or independently, the stripping tower can be in a plate tower or a packed tower, and the raw materials are fed into the tower from the top and separated from the tower from the bottom; the desorbent enters the tower from the bottom of the tower, is in countercurrent contact with the liquid raw material in the tower, and is separated from the tower together with the component to be distilled at the top of the tower, the concentrated end is at the top of the tower, the dilute end is at the bottom of the tower, and the equilibrium partial pressure of solute in a liquid phase in the stripping tower is greater than that in a gas phase.
In the steam stripping process, solute molecules need to be changed into gas, so the process is a heat absorption process, in the traditional device, raw oil is heated by a heating furnace and then enters a main fractionating tower to separate naphtha, diesel oil and hydrogenation tail oil, the diesel oil component needs to be vaporized firstly and then can be extracted from a lateral line, the heating furnace needs to provide the heat of vaporization of the diesel oil, the feeding heating furnace of the fractionating tower has larger heat load, and the fuel consumption is larger.
Disclosure of Invention
Technical problem to be solved
Aiming at the defects of the prior art, the invention provides a cracking stripping tower, which solves the problem of higher fuel consumption in the prior device.
(II) technical scheme
In order to achieve the purpose, the invention is realized by the following technical scheme: add and split strip tower, including the reaction unit, the reaction unit back end is provided with circulating hydrogen desulfurization unit and leading strip tower unit, leading strip tower unit back end has set gradually main fractional distillation unit and side stripper unit, all be provided with the multiunit between reaction unit, circulating hydrogen desulfurization unit, leading strip tower unit, main fractional distillation unit and the side stripper unit and be used for the pipeline that gaseous phase, liquid phase pass through and be used for the pump that the pressurization was carried, still be provided with liquid level controller, flow controller and the multiunit heat exchanger that is used for controlling liquid level and flow between reaction unit, circulating hydrogen desulfurization unit, leading strip tower unit, main fractional distillation unit and the side stripper unit.
Preferably, the reaction unit includes that raw oil filter, raw oil buffer tank, reaction feeding heating furnace, reactor device and the hot high pressure separator that set gradually from the front to the back, hot high pressure separator multiunit output difference fixedly connected with cold high pressure separator, hydraulic turbine and cold low pressure separator, the hot low pressure separator of one end fixedly connected with of hot high pressure separator is kept away from to hydraulic turbine, the reactor device comprises first hydrofining reactor, second hydrofining reactor and hydrocracking reactor.
Preferably, the recycle hydrogen desulfurization unit comprises a recycle hydrogen desulfurization tower, a recycle hydrogen compressor and a fresh hydrogen compressor which are sequentially arranged from left to right, a liquid separation tank is further arranged between the recycle hydrogen desulfurization tower and the recycle hydrogen compressor, and the recycle hydrogen desulfurization tower is fixedly connected with the reaction unit.
Preferably, leading stripper unit includes second stripping tower, first stripping tower second stripping tower entrance point and reaction unit fixed connection, first stripping tower output fixedly connected with stripping tower top reflux drum, lean oil absorption tower and deethanizer in proper order, still be provided with the sour water flash tank between stripping tower top reflux drum and cold high pressure separator, the cold low pressure separator, second stripping tower, first stripping tower top all are provided with stripping tower overhead air cooler and stripping tower top water cooler.
Preferably, the main fractionating unit comprises a fractionating tower feeding flash tank and a main fractionating tower which are sequentially arranged from left to right, a fractionating tower feeding heating furnace is further arranged between the fractionating tower feeding flash tank and the main fractionating tower, a fractionating tower top air cooler, a fractionating tower top water cooler and a fractionating tower top reflux tank are arranged at the top of the main fractionating tower, the fractionating tower feeding flash tank is fixedly connected with a first stripping tower in the front stripping tower unit, and one of the multiple groups of interfaces of the main fractionating tower is fixedly connected with a second stripping tower in the front stripping tower unit.
Preferably, the side stripper unit comprises a third stripper, a fourth stripper, a debutanizer, a condensed ring aromatic stripper and a fifth stripper which are respectively and fixedly connected to a plurality of groups of interfaces of the main fractionating tower, one end of the debutanizer, which is far away from the main fractionating tower, is sequentially provided with a naphtha desulfurizing tank and a naphtha separating tower, the third stripper is a light diesel stripper, the fourth stripper is a heavy diesel stripper, the fifth stripper is a heavy naphtha stripper, and the bottom of the condensed ring aromatic stripper is provided with an unconverted oil steam generator and an unconverted oil air cooler.
Preferably, the stock oil surge tank is provided with an inert gas for protecting the stock oil from air.
Preferably, the mixed feeding temperature of the first hydrofining reactor, the second hydrofining reactor and the hydrocracking reactor is controlled by adjusting the fuel gas quantity of the reaction feeding heating furnace.
The working principle is as follows: the method comprises the following steps of carrying out heat exchange on condensed water from a device containing external coker gas oil and an acid water device through a heat exchanger, combining the condensed water with the device containing external coker gas oil, sending the combined mixture into a device body under the control of a flow and liquid level controller, carrying out heat exchange on the mixed raw material, removing particles larger than twenty-five micrometers in the raw material through a raw material oil filter, fully mixing the particles with circulating oil from a fractionation part, and then sending the mixture into a raw material oil buffer tank, wherein the raw material oil buffer tank is protected by inert gas, so that the raw material oil is not in contact with air.
Further, the raw oil from the raw oil buffer tank is boosted by a pump, mixed with the mixed hydrogen from the heat exchanger under the control of the flow controller, heated to the reaction temperature by the heat exchanger and the reaction feeding heating furnace, and enters the first hydrofining reactor and the second hydrofining reactor for hydrofining reaction, and the temperature of the mixed feeding of the hydrofining reactors is controlled by adjusting the fuel gas of the reaction feeding heating furnace.
Further, the reaction effluent from the hydrocracking reactor is subjected to heat exchange with the hot mixed raw oil, the bottom liquid of the stripping tower and the cold mixed raw material through a heat exchanger to recover heat as much as possible, the reaction effluent after heat exchange enters a hot high-pressure separator for gas-liquid separation, hot high-fraction gas enters a cold high-pressure separator after being subjected to heat exchange and cooled through the heat exchanger, hot high-fraction oil enters a hot low-pressure separator after being subjected to energy recovery through a hydraulic turbine under the control of a liquid level controller, hot low-fraction gas is mixed with the cold high-fraction oil after being cooled and enters a cold low-pressure separator, and hot low-fraction oil enters a second stripping tower under the control of the liquid level.
Specifically, the cooled hot high-pressure gas is subjected to oil-gas-water three-phase separation in a cold high-pressure separator, the circulating hydrogen cold high-pressure gas discharged from the top of the cold high-pressure separator is desulfurized through a circulating hydrogen desulfurization tower and a liquid separating tank in sequence, and desulfurized circulating hydrogen enters a circulating hydrogen compressor and is boosted and then divided into two paths: one path of the mixed hydrogen is used as a quench hydrogen reaction unit to control the temperature of each bed layer inlet of the first hydrofining reactor, the second hydrofining reactor and the hydrocracking reactor, the other path of the mixed hydrogen is mixed with new hydrogen from an outlet of a new hydrogen compressor to form mixed hydrogen, cold high-pressure oil enters a cold low-pressure separator under the control of liquid level, the cold low-pressure oil is sequentially subjected to heat exchange through a multi-stage heat exchanger and then is conveyed to a first stripping tower, and acid water discharged from the bottoms of the cold high-pressure separator and the cold low-pressure separator is conveyed to an acid water flash tank.
Specifically, fresh hydrogen from the outside of the device enters a fresh hydrogen compressor inlet liquid separating tank for liquid separation, is subjected to three-stage pressure boosting by the fresh hydrogen compressor and then is mixed with recycle hydrogen at a recycle hydrogen compressor outlet, and is subjected to heat exchange by a heat exchanger and then is mixed with raw oil.
Furthermore, after hot low-fraction oil from the reaction unit enters a second stripping tower, superheated steam is adopted for stripping at the bottom of the tower, gas phase at the top of the tower is used as feeding material of the first stripping tower, and tower bottom oil is subjected to heat exchange through a heat exchanger under the cascade control of a liquid level controller and a flow controller and then flows to the main fractionating tower.
Further, cold low oil from the reaction unit enters a first stripping tower, stripping steam enters from the bottom of the tower, tower top gas is cooled by an air cooler at the top of the stripping tower and a water cooler at the top of the stripping tower and then enters a reflux tank at the top of the stripping tower for oil, water and gas three-phase separation, a gas phase is used as the feeding material of a lean oil absorption tower under the control of pressure, after an oil phase at the top of the stripping tower is boosted by a pump, one part of the oil phase is used as the reflux of the first stripping tower under the control of a flow controller in a cascade mode, the other part of the oil phase is used as the feeding material of a deethanizer under the control of a liquid level controller and a flow controller, and discharged sulfur-containing sewage is conveyed to an acid water flash tank.
Further, the liquid at the bottom of the first stripping tower is subjected to heat exchange under the cascade control of a liquid level controller and a flow controller, then the liquid is separated from the gas phase by a fractionating tower feeding flash tank, and then the liquid is heated by a fractionating tower feeding heating furnace and then enters a main fractionating tower which is provided with two side line towers of a third stripping tower for stripping light diesel oil and a fourth stripping tower for stripping heavy diesel oil, the gas at the top of the main fractionating tower is cooled by a fractionating tower top air cooler and a fractionating tower top water cooler and enters a fractionating tower top reflux tank, after the liquid phase is boosted by a pump, one part of the liquid phase is taken as the top reflux of the main fractionating tower, the other part of the liquid phase is combined with the bottom oil of the deethanizer and is subjected to heat exchange by a heat exchanger and then enters a debutanizer, and the oily sewage at the bottom of the fractionating tower top reflux tank is boosted by the pump and then enters a reaction unit to be used as process water.
The bottom oil of the main fractionating tower is pumped up, under the control of a liquid level controller, one part of the bottom oil is used as hydrogenated circulating oil after heat exchange and is sent to a raw oil buffer tank in a reaction unit, the other part of the bottom oil enters a condensed ring aromatic hydrocarbon stripping tower for steam stripping, the top gas of the tower returns to the main fractionating tower, and a small amount of unconverted oil at the bottom of the tower is cooled out of the device through an unconverted oil steam generator and an unconverted oil air cooler.
Heavy naphtha is pumped out from the upper side line of the main fractionating tower and enters a fifth stripping tower for stripping the heavy naphtha under the control of a liquid level controller, the gas at the top of the fifth stripping tower returns to the main fractionating tower, the bottom product of the fifth stripping tower is boosted by a pump and then mixed with the bottom oil of the debutanizer under the control of a flow controller, and the mixture is desulfurized by a naphtha desulfurizing tank and then used as the feed of a naphtha separating tower.
Light diesel oil is extracted from the upper middle section side line of the main fractionating tower and enters a third stripping tower for stripping light diesel oil under the control of liquid level, the top gas of the third stripping tower returns to the main fractionating tower, the heat source at the bottom of the third stripping tower is the lower middle section reflux liquid extracted from the main fractionating tower, and the bottom product of the third stripping tower is boosted by a pump and mixed with heavy diesel oil under the control of a flow controller.
Heavy diesel oil is extracted from the lower middle section side line of the main fractionating tower, one part of the heavy diesel oil is pressurized by a pump and returns to the main fractionating tower after heat exchange, the other part of the heavy diesel oil enters a fourth stripping tower for stripping the heavy diesel oil under the control of a liquid level controller, the top gas of the fourth stripping tower returns to the main fractionating tower, the bottom heat source of the fourth stripping tower is bottom oil of the main fractionating tower, and a bottom product of the fourth stripping tower is pressurized by the pump and is mixed with the pressurized bottom oil of the third stripping tower after heat exchange.
And (3) mixing the light diesel oil and the heavy diesel oil, then exchanging heat with the raw oil through a heat exchanger, and then cooling the mixed diesel oil after heat exchange to fifty ℃ to be used as a diesel oil product outlet device.
(III) advantageous effects
The invention provides a crack stripper. The method has the following beneficial effects:
1. the invention adds a second stripping tower to strip hot low-fraction oil directly, while the first stripping tower is only used for stripping cold low-fraction oil, because the bottom oil of the cold low-fraction oil stripping tower contains a large amount of diesel components, the bottom oil can directly enter the light diesel stripping tower along with the feeding of the light diesel stripping tower, then the diesel components are extracted from the tower bottom to be used as diesel products, thus secondary vaporization of the diesel components is avoided, the second stripping tower is used for directly stripping the hot low-fraction oil, the bottom oil of the second stripping tower is subjected to gas-liquid phase separation through a newly-added fractionating tower feeding flash tank after heat exchange, and then enters the fractionating tower after being heated by a fractionating tower feeding heating furnace, so that the fractionating tower feeding heating furnace can only gasify a small amount of diesel components, the load of the heating furnace is greatly reduced, the fuel consumption is correspondingly reduced, and the energy consumption of the device is reduced.
2. The invention adds a second stripping tower and a fractionating tower feeding flash tank, the load of the hydrogenation feeding heating furnace is synchronously reduced, and the fuel consumption is also reduced.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention;
FIG. 2 is a schematic view of a partial structure of a reaction unit according to the present invention;
FIG. 3 is a schematic view of a partial structure of a recycle hydrogen desulfurization unit according to the present invention;
FIG. 4 is a schematic view of a partial structure of a pre-stripper unit according to the present invention;
FIG. 5 is a schematic view of a partial configuration of a main fractionation unit and a side stripper unit according to the present invention.
Wherein, 1, raw oil filter; 2. a raw oil buffer tank; 3. a reaction feed heating furnace; 4. a first hydrofinishing reactor; 5. a second hydrofinishing reactor; 6. a hydrocracking reactor; 7. a hot high pressure separator; 8. a cold high pressure separator; 9. a hydraulic turbine; 10. a hot low pressure separator; 11. a cold low pressure separator; 12. a second stripping column; 13. a recycle hydrogen desulfurization tower; 14. liquid separating tank; 15. a recycle hydrogen compressor; 16. a fresh hydrogen compressor; 17. a first stripping column; 18. an acidic water flash tank; 19. a reflux tank at the top of the stripping tower; 20. a lean oil absorption tower; 21. a deethanizer; 22. a fractionating tower feeding flash tank; 23. a fractionating tower feeding heating furnace; 24. a main fractionation column; 25. a third stripping column; 26. a fourth stripping column; 27. a reflux drum at the top of the fractionating tower; 28. a debutanizer column; 29. a condensed ring aromatic hydrocarbon stripping tower; 30. a fifth stripping column; 31. a naphtha devulcanizer; 32. a naphtha splitter column.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example (b):
as shown in fig. 1 to 5, a cracking stripper is provided in an embodiment of the present invention, and includes a reaction unit, a recycle hydrogen desulfurization unit and a front stripper unit are disposed at a rear section of the reaction unit, a main fractionation unit and a side stripper unit are sequentially disposed at a rear section of the front stripper unit, a plurality of groups of pipelines for passing a gas phase and a liquid phase and pumps for pressure delivery are disposed between the reaction unit, the recycle hydrogen desulfurization unit, the front stripper unit, the main fractionation unit, and the side stripper unit, and a liquid level controller, a flow controller, and a plurality of groups of heat exchangers are further disposed between the reaction unit, the recycle hydrogen desulfurization unit, the front stripper unit, the main fractionation unit, and the side stripper unit for controlling a liquid level and a flow rate.
The reaction unit comprises a raw oil filter 1, a raw oil buffer tank 2, a reaction feeding heating furnace 3, a reactor device and a hot high-pressure separator 7 which are sequentially arranged from front to back, wherein a plurality of groups of output ends of the hot high-pressure separator 7 are respectively and fixedly connected with a cold high-pressure separator 8, a hydraulic turbine 9 and a cold low-pressure separator 11, one end of the hydraulic turbine 9 far away from the hot high-pressure separator 7 is fixedly connected with a hot low-pressure separator 10, the reactor device consists of a first hydrofining reactor 4, a second hydrofining reactor 5 and a hydrocracking reactor 6, after heat exchange, particles larger than twenty-five microns in the raw materials are removed through the raw oil filter 1, the raw oil from the raw oil buffer tank 2 is pressurized through a pump, is mixed with mixed hydrogen from a heat exchanger under the control of a flow controller and then is heated to the reaction temperature through the heat exchanger and the reaction feeding heating furnace 3, entering a first hydrofining reactor 4 and a second hydrofining reactor 5 for hydrofining reaction, and further entering a hydrocracking reactor 6 for hydrocracking reaction of the hydrofining reaction effluent.
The recycle hydrogen desulfurization unit comprises a recycle hydrogen desulfurization tower 13, a recycle hydrogen compressor 15 and a new hydrogen compressor 16 which are sequentially arranged from left to right, a liquid separation tank 14 is further arranged between the recycle hydrogen desulfurization tower 13 and the recycle hydrogen compressor 15, the recycle hydrogen desulfurization tower 13 is fixedly connected with the reaction unit, and the desulfurized recycle hydrogen enters the recycle hydrogen compressor 15 and is divided into two paths after being boosted: one path is used as a quenching hydrogen reaction unit to control the inlet temperature of each bed layer of the first hydrofining reactor 4, the second hydrofining reactor 5 and the hydrocracking reactor 6, the other path is mixed with new hydrogen from an outlet of a new hydrogen compressor 16 to form mixed hydrogen, and cold high-pressure oil enters a cold low-pressure separator 11 under the control of liquid level.
The preposed stripping tower unit comprises a second stripping tower 12, a first stripping tower 17, the inlet end of the second stripping tower 12 is fixedly connected with the reaction unit, the output end of the first stripping tower 17 is fixedly connected with a stripping tower top reflux tank 19, a lean oil absorption tower 20 and a deethanizer 21 in sequence, an acid water flash tank 18 is also arranged between the stripping tower top reflux tank 19 and the cold high-pressure separator 8 as well as between the cold low-pressure separator 11, a stripping tower top air cooler and a stripping tower top water cooler are arranged at the tops of the second stripping tower 12 and the first stripping tower 17, hot low fraction oil from the reaction unit enters the second stripping tower 12, superheated steam is adopted at the bottom of the tower for stripping, the tower top gas phase is used as the feeding material of the first stripping tower 17, the tower bottom oil enters a main distillation tower 24 after heat exchange through a heat exchanger under the cascade control of a liquid level controller and a flow controller, the cold low fraction oil from the reaction unit enters the first stripping tower 17, steam stripping steam enters from the bottom of the tower, gas at the top of the tower enters a reflux tank 19 at the top of the stripping tower after being cooled by an air cooler at the top of the stripping tower and a water cooler at the top of the stripping tower to carry out oil-water-gas three-phase separation, the gas phase is used as the feeding material of a lean oil absorption tower 20 under the pressure control, the oil phase at the top of the tower is boosted by a pump, one part of the oil phase is used as the reflux of a first stripping tower 17 under the cascade control of a flow controller, the other part of the oil phase is used as the feeding material of a deethanizer 21 under the control of a liquid level controller and a flow controller, and the discharged sulfur-containing sewage is conveyed to an acidic water flash tank 18.
The main fractionating unit comprises a fractionating tower feeding flash tank 22 and a main fractionating tower 24 which are sequentially arranged from left to right, a fractionating tower feeding heating furnace 23 is further arranged between the fractionating tower feeding flash tank 22 and the main fractionating tower 24, a fractionating tower top air cooler, a fractionating tower top water cooler and a fractionating tower top reflux tank 27 are arranged at the tower top of the main fractionating tower 24, the fractionating tower feeding flash tank 22 is fixedly connected with a first stripping tower 17 in a front stripping tower unit, one group of a plurality of groups of interfaces of the main fractionating tower 24 is fixedly connected with a second stripping tower 12 in the front stripping tower unit, liquid at the bottom of the first stripping tower 17 is subjected to heat exchange under the cascade control of a liquid level controller and a flow controller, then is subjected to gas-liquid phase separation through the fractionating tower feeding flash tank 22, and then enters the main fractionating tower 24 after being heated by the fractionating tower feeding heating furnace 23, the main fractionating tower 24 is provided with a third stripping tower 25 for stripping light diesel oil and a fourth side-line tower 26 for stripping heavy diesel oil, the gas at the top of the main fractionating tower 24 enters a fractionating tower top reflux tank 27 after being cooled by a fractionating tower top air cooler and a fractionating tower top water cooler, after the liquid phase is boosted by a pump, one part of the liquid phase is used as the top reflux of the main fractionating tower 24, the other part of the liquid phase and the oil at the bottom of the deethanizer 21 are combined and are subjected to heat exchange by a heat exchanger and then enter a debutanizer 28, and the oil-containing sewage at the bottom of the fractionating tower top reflux tank 27 is boosted by a pump and then enters a reaction unit to be used as process water.
The side stripper unit comprises a third stripper 25, a fourth stripper 26, a debutanizer 28, a fused ring aromatic hydrocarbon stripper 29 and a fifth stripper 30 which are respectively and fixedly connected to a plurality of groups of interfaces of a main fractionating tower 24, one end of the debutanizer 28, which is far away from the main fractionating tower 24, is sequentially provided with a naphtha desulfurizing tank 31 and a naphtha separating tower 32, the third stripper 25 is a light diesel oil stripper, the fourth stripper 26 is a heavy diesel oil stripper, the fifth stripper 30 is a heavy naphtha stripper, an unconverted oil steam generator and an unconverted oil air cooler are arranged at the bottom of the fused ring aromatic hydrocarbon stripper 29, the bottom oil of the main fractionating tower 24 is boosted by a pump, one part of the bottom oil is used as hydrogenation cycle oil to be fed into a raw oil buffer tank 2 in the reaction unit after heat exchange under the control of a liquid level controller, the other part of the bottom oil is fed into the fused ring aromatic hydrocarbon stripper 29 for steam stripping, the top gas is returned to the main fractionating tower 24, and a small amount of unconverted oil at the bottom passes through the unconverted oil steam generator, The unconverted oil air cooler is cooled and discharged, heavy naphtha is extracted from the upper side line of a main fractionating tower 24 and enters a fifth stripping tower 30 for stripping the heavy naphtha under the control of a liquid level controller, the top gas of the fifth stripping tower 30 returns to the main fractionating tower 24, the bottom product of the fifth stripping tower 30 is boosted by a pump and then is mixed with the bottom oil of a debutanizer 28 under the control of a flow controller, the mixture is desulfurized by a naphtha desulfurizing tank 31 and then is used as the feed of a naphtha separating tower 32, light diesel oil is extracted from the upper middle section side line of the main fractionating tower and enters a third stripping tower 25 for stripping light diesel oil under the control of the liquid level, the top gas of the third stripping tower 25 returns to the main fractionating tower 24, the heat source at the bottom of the third stripping tower 25 is the lower middle section reflux liquid extracted from the main fractionating tower 24, the bottom product of the third stripping tower 25 is boosted by the pump and is mixed with the heavy diesel oil under the control of the flow controller, the heavy diesel oil is extracted from the lower middle section side line of the main fractionating tower 24, one part is pressurized by a pump and returns to the main fractionating tower 24 after heat exchange, the other part enters a fourth stripping tower 26 for stripping heavy diesel oil under the control of a liquid level controller, the gas at the top of the fourth stripping tower 26 returns to the main fractionating tower 24, the heat source at the bottom of the fourth stripping tower 26 is main fractionating tower bottom oil, the pressure of the tower bottom product of the fourth stripping tower 26 is boosted by the pump, the tower bottom product is mixed with the tower bottom oil of the third stripping tower 25 after boosting after heat exchange, the light diesel oil and the heavy diesel oil are mixed and then exchange heat with raw oil through a heat exchanger, and the mixed diesel oil after heat exchange is cooled to fifty ℃ as a diesel oil product outlet device.
The stock oil surge tank 2 is provided with an inert gas for protecting the stock oil from air.
The mixed feeding temperature of the first hydrofining reactor 4, the second hydrofining reactor 5 and the hydrocracking reactor 6 is controlled by adjusting the fuel gas amount of the reaction feeding heating furnace 3.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (5)
1. The cracking stripping tower comprises a reaction unit and is characterized in that: the device comprises a reaction unit, a circulating hydrogen desulfurization unit, a front stripping tower unit, a plurality of groups of pipelines for gas phase and liquid phase to pass through and pumps for pressurizing and conveying, wherein the rear section of the reaction unit is provided with the circulating hydrogen desulfurization unit and the front stripping tower unit;
the reaction unit comprises a raw oil filter (1), a raw oil buffer tank (2), a reaction feeding heating furnace (3), a reactor device and a hot high-pressure separator (7) which are sequentially arranged from front to back, wherein multiple groups of output ends of the hot high-pressure separator (7) are respectively and fixedly connected with a cold high-pressure separator (8), a hydraulic turbine (9) and a cold low-pressure separator (11), one end, far away from the hot high-pressure separator (7), of the hydraulic turbine (9) is fixedly connected with a hot low-pressure separator (10), and the reactor device consists of a first hydrofining reactor (4), a second hydrofining reactor (5) and a hydrocracking reactor (6);
the recycle hydrogen desulfurization unit comprises a recycle hydrogen desulfurization tower (13), a recycle hydrogen compressor (15) and a fresh hydrogen compressor (16) which are sequentially arranged from left to right, a liquid separation tank (14) is also arranged between the recycle hydrogen desulfurization tower (13) and the recycle hydrogen compressor (15), and the recycle hydrogen desulfurization tower (13) is fixedly connected with the reaction unit;
the pre-stripping tower unit comprises a second stripping tower (12), a first stripping tower (17), the inlet end of the second stripping tower (12) is fixedly connected with the reaction unit, the output end of the first stripping tower (17) is fixedly connected with a stripping tower top reflux tank (19), a lean oil absorption tower (20) and a deethanizer (21) in sequence, an acidic water flash tank (18) is further arranged between the stripping tower top reflux tank (19) and the cold high-pressure separator (8) and the cold low-pressure separator (11), and stripping tower top air coolers and stripping tower top water coolers are arranged at the tops of the second stripping tower (12) and the first stripping tower (17).
2. The topping stripper of claim 1, wherein: the main fractionating unit comprises a fractionating tower feeding flash tank (22) and a main fractionating tower (24) which are sequentially arranged from left to right, a fractionating tower feeding heating furnace (23) is further arranged between the fractionating tower feeding flash tank (22) and the main fractionating tower (24), a fractionating tower top air cooler, a fractionating tower top water cooler and a fractionating tower top reflux tank (27) are arranged at the tower top of the main fractionating tower (24), the fractionating tower feeding flash tank (22) is fixedly connected with a first stripping tower (17) in a front stripping tower unit, and one of a plurality of groups of interfaces of the main fractionating tower (24) is fixedly connected with a second stripping tower (12) in the front stripping tower unit.
3. The topping stripper of claim 2, wherein: the side stripper unit comprises a third stripping tower (25), a fourth stripping tower (26), a debutanizer (28), a fused ring aromatic stripping tower (29) and a fifth stripping tower (30) which are respectively and fixedly connected to a plurality of groups of interfaces of a main fractionating tower (24), wherein a naphtha desulfurizing tank (31) and a naphtha separating tower (32) are sequentially arranged at one end, far away from the main fractionating tower (24), of the debutanizer (28), the third stripping tower (25) is a light diesel stripping tower, the fourth stripping tower (26) is a heavy diesel stripping tower, the fifth stripping tower (30) is a heavy naphtha stripping tower, and a non-converted oil steam generator and a non-converted oil air cooler are arranged at the bottom of the fused ring aromatic stripping tower (29).
4. The topping stripper of claim 3, wherein: and the raw oil buffer tank (2) is internally provided with inert gas for protecting the raw oil from contacting air.
5. The topping stripper of claim 4, wherein: the mixed feeding temperature of the first hydrofining reactor (4), the second hydrofining reactor (5) and the hydrocracking reactor (6) is controlled by adjusting the fuel gas amount of the reaction feeding heating furnace (3).
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| CN202111251967.3A CN113736517A (en) | 2021-10-27 | 2021-10-27 | Cracking stripping tower |
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| CN202111251967.3A CN113736517A (en) | 2021-10-27 | 2021-10-27 | Cracking stripping tower |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115386394A (en) * | 2022-07-22 | 2022-11-25 | 山东汇丰石化集团有限公司 | Energy-saving heat exchange system and heat exchange process of diesel hydrogenation device |
| CN115558518A (en) * | 2022-09-05 | 2023-01-03 | 中国石油化工股份有限公司 | Method for circularly dehydrating diesel oil during start-up of solvent deasphalting device |
| CN115948180A (en) * | 2023-03-14 | 2023-04-11 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine through hydrogenation |
| CN116286087A (en) * | 2023-03-30 | 2023-06-23 | 恒力石化（大连）炼化有限公司 | Method for producing high-quality industrial white oil by wax oil hydrocracking device |
| CN116875345A (en) * | 2023-09-07 | 2023-10-13 | 江苏龙腾城矿环境技术有限公司 | Tire oil deep processing method and system |
| CN118048173A (en) * | 2024-04-16 | 2024-05-17 | 东营联合石化有限责任公司 | Tail oil hydrocracking energy-saving device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102899081A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Wax oil hydrotreating method |
| US20130045138A1 (en) * | 2011-08-19 | 2013-02-21 | Uop Llc | Apparatus for recovering hydroprocessed hydrocarbons with two strippers in series |
| CN104312625A (en) * | 2014-09-30 | 2015-01-28 | 中国石油化工股份有限公司 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
| CN110643391A (en) * | 2019-09-02 | 2020-01-03 | 中科合成油技术有限公司 | Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil |
| CN214088414U (en) * | 2020-11-27 | 2021-08-31 | 浙江石油化工有限公司 | Wax oil hydrocracking unit |
-
2021
- 2021-10-27 CN CN202111251967.3A patent/CN113736517A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102899081A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Wax oil hydrotreating method |
| US20130045138A1 (en) * | 2011-08-19 | 2013-02-21 | Uop Llc | Apparatus for recovering hydroprocessed hydrocarbons with two strippers in series |
| CN104312625A (en) * | 2014-09-30 | 2015-01-28 | 中国石油化工股份有限公司 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
| CN110643391A (en) * | 2019-09-02 | 2020-01-03 | 中科合成油技术有限公司 | Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil |
| CN214088414U (en) * | 2020-11-27 | 2021-08-31 | 浙江石油化工有限公司 | Wax oil hydrocracking unit |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115386394A (en) * | 2022-07-22 | 2022-11-25 | 山东汇丰石化集团有限公司 | Energy-saving heat exchange system and heat exchange process of diesel hydrogenation device |
| CN115558518A (en) * | 2022-09-05 | 2023-01-03 | 中国石油化工股份有限公司 | Method for circularly dehydrating diesel oil during start-up of solvent deasphalting device |
| CN115558518B (en) * | 2022-09-05 | 2024-02-20 | 中国石油化工股份有限公司 | Method for circularly dehydrating starting diesel oil of solvent deasphalting device |
| CN115948180A (en) * | 2023-03-14 | 2023-04-11 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine through hydrogenation |
| CN116286087A (en) * | 2023-03-30 | 2023-06-23 | 恒力石化（大连）炼化有限公司 | Method for producing high-quality industrial white oil by wax oil hydrocracking device |
| CN116875345A (en) * | 2023-09-07 | 2023-10-13 | 江苏龙腾城矿环境技术有限公司 | Tire oil deep processing method and system |
| CN118048173A (en) * | 2024-04-16 | 2024-05-17 | 东营联合石化有限责任公司 | Tail oil hydrocracking energy-saving device |
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