CN116410770B - Aviation kerosene hydrogenation system adopting nitrogen stripping - Google Patents
Aviation kerosene hydrogenation system adopting nitrogen stripping Download PDFInfo
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- CN116410770B CN116410770B CN202111648204.2A CN202111648204A CN116410770B CN 116410770 B CN116410770 B CN 116410770B CN 202111648204 A CN202111648204 A CN 202111648204A CN 116410770 B CN116410770 B CN 116410770B
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 56
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 239000003350 kerosene Substances 0.000 title claims abstract description 47
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 106
- 238000000926 separation method Methods 0.000 claims abstract description 66
- 239000007789 gas Substances 0.000 claims abstract description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000002737 fuel gas Substances 0.000 claims abstract description 14
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 9
- 239000007791 liquid phase Substances 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 238000007599 discharging Methods 0.000 claims description 20
- 239000002253 acid Substances 0.000 claims description 16
- 238000010992 reflux Methods 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 10
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052802 copper Inorganic materials 0.000 abstract description 5
- 239000010949 copper Substances 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 5
- 230000007797 corrosion Effects 0.000 abstract description 5
- 230000008014 freezing Effects 0.000 abstract description 4
- 238000007710 freezing Methods 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000005504 petroleum refining Methods 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 58
- 239000000047 product Substances 0.000 description 21
- 239000007795 chemical reaction product Substances 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- KWIUHFFTVRNATP-UHFFFAOYSA-N Betaine Natural products C[N+](C)(C)CC([O-])=O KWIUHFFTVRNATP-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- KWIUHFFTVRNATP-UHFFFAOYSA-O N,N,N-trimethylglycinium Chemical compound C[N+](C)(C)CC(O)=O KWIUHFFTVRNATP-UHFFFAOYSA-O 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 229960003237 betaine Drugs 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- -1 meanwhile Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/04—Dewatering
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
-
- 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
Abstract
The invention relates to the field of petroleum refining, in particular to a aviation kerosene hydrogenation system adopting nitrogen stripping, which at least comprises the following components: hydrogen gas source, raw oil from tank farm, deoxygenated water from boundary farm, superheated low pressure steam to boundary farm, low pressure nitrogen gas source, fuel gas source, sour water stripping system, low split gas to boundary farm and refined aviation kerosene to boundary farm, the system further comprising: the device comprises a first separation part, a hydrogenation reaction part, a second separation part, a stripping part, a heat exchange part and a charging part. The beneficial effects of the invention are as follows: because the nitrogen is adopted as the air source of the stripping tower, the problems of the freezing point of the aviation kerosene and the corrosion of the copper sheet of the aviation kerosene caused by the water carried by the aviation kerosene are effectively solved, and the water content of the aviation kerosene is reduced by adopting the nitrogen as the stripping medium, so that the aviation kerosene is qualified.
Description
Technical Field
The invention relates to the field of petroleum refining, in particular to a aviation kerosene hydrogenation system adopting nitrogen stripping.
Background
Steam stripping is used for hydrogenation of the prior aviation kerosene, the water content of the aviation kerosene is too high by steam stripping, the water carried by the aviation kerosene product and the corrosion of the copper sheet of the aviation kerosene are unqualified, the freezing point of the aviation kerosene is unqualified, a hydrogenation device stripping tower is used for steam stripping, a reboiler heating system is not arranged at the bottom of the tower, a heat source at the bottom of the tower is mainly provided by heat of reaction products, the gasification rate of light components is insufficient to carry all hydrogen sulfide out stripping, and part of hydrogen sulfide is carried to the back of the product in a dissolved form to influence the corrosion of the copper sheet of the aviation kerosene product, so that a new aviation kerosene hydrogenation system is needed, and the aviation kerosene achieves low water content and meets the use standard of the aviation kerosene.
Disclosure of Invention
The application provides a aviation kerosene hydrogenation system adopting nitrogen stripping, which solves the problems of unqualified corrosion of aviation kerosene copper sheets and unqualified aviation kerosene freezing point caused by excessive water content of aviation kerosene, realizes qualified aviation kerosene and meets the use standard of aviation kerosene.
The technical problems solved by the invention can be realized by adopting the following technical scheme:
An aviation kerosene hydrogenation system employing nitrogen stripping, comprising at least: hydrogen gas source, raw oil from tank farm, deoxygenated water from boundary farm, superheated low pressure steam to boundary farm, low pressure nitrogen gas source, fuel gas source, sour water stripping system, low split gas to boundary farm and refined aviation kerosene to boundary farm, the system further comprising: ;
The first separation part is communicated with a raw oil self-tank area at the feeding end of the oil-water separation part and is also respectively communicated with a fuel gas source and an acid water stripping system;
The hydrogenation reaction part is respectively communicated with a hydrogen gas source and an oil outlet end of the oil-water separator, and an air outlet end of the hydrogenation reaction part is communicated with the second separation part;
the second separation part is communicated with the discharge end of the hydrogenation reaction part, the feed end of the first separation part, the sour water stripping system and the low-pressure gas separation to the boundary region respectively;
the stripping part is communicated with the discharge end of the second separation part, is communicated with a low-pressure nitrogen source and is used as a stripping gas source through nitrogen;
The heat exchange part is respectively communicated with the deoxygenated water from the boundary region, the superheated low-pressure steam to the boundary region, the second separation part and the discharge end of the stripping part;
And the feeding part is communicated with the discharge end of the heat exchange part, and the discharge end of the feeding part is communicated with the refined aviation kerosene to the boundary region.
Further, the first separation part comprises a first oil-water separator, a first feeding pump and a first heat exchanger, raw oil is communicated with the first feeding end of the first oil-water separator from the tank area through the first heat exchanger, an oil outlet of the first oil-water separator is communicated with the hydrogenation reaction part through the first feeding pump, a water outlet end of the first oil-water separator is communicated with the acid water stripping system, and an air inlet end of the first oil-water separator is communicated with a fuel gas source.
Further, the hydrogenation portion includes heat exchanger two, reaction feeding stove, liquid phase hydrogenation reactor and circulating pump, reaction feeding stove feed end is through heat exchanger two and separation portion intercommunication, the intercommunication has the circulation pipeline between liquid phase hydrogenation reactor's the discharge end and the feed end, and the circulating pump concatenates on the circulation pipeline, and reaction feeding stove's the discharge end and circulation pipeline intercommunication, switch on the hydrogen gas source between heat exchanger two and the separation portion one, the hydrogen gas source still communicates with liquid phase hydrogenation reactor, liquid phase hydrogenation reactor's the discharge end still communicates with separation portion two, concatenate heat exchanger two between liquid phase hydrogenation reactor's the discharge end and the separation portion two, liquid phase hydrogenation reactor's the end of giving vent to anger and separation portion two intercommunication.
Further, the second separation part comprises a hot low-pressure separator, a cold low-pressure separator and a first air cooler, wherein the feeding end of the hot low-pressure separator is communicated with the discharging end of the hydrogenation reaction part, the discharging end of the hot low-pressure separator is communicated with the feeding end of the cold low-pressure separator through the first air cooler, the first air cooler is communicated with the heat exchange part, the discharging end of the cold low-pressure separator is communicated with the feeding end of the first separation part, the discharging end and the discharging end of the cold low-pressure separator are respectively communicated with a low-pressure gas separation to boundary area and an acid water stripping system, and the discharging end of the hot low-pressure separator is communicated with the stripping part.
Further, the stripping part comprises a stripping tower, a product pump, a reflux pump, an air cooler II and an oil-water separator II, wherein the discharging end of the hot low-pressure separator is communicated with the feeding end of the stripping tower, the discharging end of the stripping tower is communicated with the heat exchange part through the product pump, the air inlet end of the stripping tower is communicated with a low-pressure nitrogen gas source, the air outlet pipe of the stripping tower is communicated with the feeding end of the oil-water separator II through the air cooler II, the discharging end of the oil-water separator II is communicated with the reflux end of the stripping tower through the reflux pump, the water outlet end of the oil-water separator II is communicated with the acid water stripping system, and the air cooler II is communicated with the heat exchange part.
Further, the heat exchange part comprises a heat exchanger III, a heat exchanger IV, a desuperheater, a heating furnace convection chamber and an air cooler III, the deoxygenated water is communicated with the air cooler I, the air cooler II and the desuperheater respectively from the boundary region, the deoxygenated water is communicated with the desuperheater through the heat exchanger III, the heat exchanger IV and the heating furnace convection chamber, the desuperheater is communicated with the overheated low-pressure steam to the boundary region, the discharge end of the stripping tower is communicated with the three feed ends of the air cooler through the heat exchanger IV, the heat exchanger III, the heat exchanger I, and the three discharge end of the air cooler is communicated with the feeding part.
Further, the charging part comprises a filtering separator, a coalescer, a cooler and a dosing system, wherein the three discharging ends of the air cooler are communicated with the refined aviation kerosene to the boundary region through the filtering separator, the coalescer and the cooler which are connected in series, and the discharging end of the dosing system is communicated with the feeding end of the filtering separator.
The beneficial effects of the invention are as follows: because the nitrogen is adopted as the air source of the stripping tower, the problems of the freezing point of the aviation kerosene and the corrosion of the copper sheet of the aviation kerosene caused by the water carried by the aviation kerosene are effectively solved, and the water content of the aviation kerosene is reduced by adopting the nitrogen as the stripping medium, so that the aviation kerosene is qualified.
Because the secondary line regulating valve of the raw oil heated by the heat exchanger II is fully opened, the high-conversion shell side hand valve for feeding reaction materials is closed, the heat exchange of the raw material for taking reaction products is reduced, the temperature of the reaction products fed into the low-pressure separator is increased, and the feeding temperature of the stripping tower is further increased.
Drawings
The invention will be further described with reference to the drawings and examples.
Fig. 1 is a schematic structural view of the present invention.
In the figure: 1-a hydrogen gas source; 2-raw oil is discharged from a tank area; 3-deoxidizing water self-limiting area; 4-superheating low pressure steam to the interface; 5-a low-pressure nitrogen source; 6-a fuel gas source; 7-an acid water stripping system; 8-low gas separation to the boundary region; 9-refining aviation kerosene to a boundary region; 10-an oil-water separator I; 11-a first feed pump; 12-a first heat exchanger; 13-a second heat exchanger; 14-a reaction feed furnace; 15-a liquid phase hydrogenation reactor; 16-a circulation pump; 17-a circulation line; 18-a thermal low pressure separator; 19-a cold low pressure separator; 20-an air cooler I; 21-a stripper; 22-product pump; 23-reflux pump; 24-an air cooler II; 25-a second oil-water separator; 26-a third heat exchanger; 27-a fourth heat exchanger; 28-desuperheater; 29-a convection chamber of a heating furnace; 30-an air cooler III; 31-a filtration separator; 32-a coalescer; 33-a cooler; 34-dosing system.
Detailed Description
Example 1:
Referring to fig. 1, a schematic structural diagram of embodiment 1 of the present invention is provided, which is a aviation kerosene hydrogenation system adopting nitrogen stripping, at least comprising: a hydrogen gas source 1, raw oil from a tank area 2, deoxygenated water from a boundary area 3, superheated low-pressure steam to a boundary area 4, a low-pressure nitrogen gas source 5, a fuel gas source 6, an acid water stripping system 7, low-pressure gas separation to a boundary area 8 and refined aviation kerosene to a boundary area 9, which belong to the existing facilities, and the system also comprises;
the first separation part is communicated with the raw oil from the tank area 2 at the feeding end of the oil-water separation part and is also respectively communicated with the fuel gas source 6 and the acid water stripping system 7;
The hydrogenation reaction part is respectively communicated with the hydrogen gas source 1 and the oil outlet end of the oil-water separator, and the air outlet end of the hydrogenation reaction part is communicated with the second separation part;
the second separation part is respectively communicated with the discharge end of the hydrogenation reaction part, the feed end of the first separation part, the sour water stripping system 7 and the low-pressure gas separation to boundary area 8;
The stripping part is communicated with the discharge end of the second separation part, is communicated with a low-pressure nitrogen source 5 and is used as a gas source of stripping through nitrogen;
The heat exchange part is respectively communicated with deoxygenated water from the boundary area 3, the superheated low-pressure steam to the boundary area 4, the second separation part and the discharge end of the stripping part;
And the feeding part is communicated with the discharge end of the heat exchange part, and the discharge end of the feeding part is communicated with the refined aviation kerosene to the boundary region 9.
When in actual use, the method comprises the following steps: the raw oil is kerosene, the raw oil is sent into a first separation part from a tank area 2 for oil-water separation, water is discharged out of an acid water stripping system 7, the raw oil enters a hydrogenation reaction part, a hydrogen gas source 1 is connected into the hydrogenation reaction part at the same time, the raw oil reacts with hydrogen to remove sulfur, nitrogen and metal impurities to obtain reaction oil, the reaction oil enters a second separation part, the reaction oil is subjected to a gas-liquid separator through the second separation part to obtain thermal low-fraction oil for removing hydrogen, light hydrocarbon, ammonia and hydrogen sulfide for the second time, the raw oil is sent into a stripping part, the thermal low-fraction oil is further removed by nitrogen through the stripping part to remove hydrogen, light hydrocarbon, ammonia and hydrogen sulfide to obtain product oil, the product oil is subjected to heat exchange through a heat exchange part, meanwhile, the crude oil entering the first separation part is heated through the first separation part, the product oil enters a charging part after being cooled, and the product oil is dehydrated and mixed with additives through the charging part, and then enters a refined aviation kerosene to a boundary area 9.
In this embodiment, the hydrogen gas source 1, the raw oil from the tank farm 2, the deoxygenated water from the boundary farm 3, the superheated low-pressure steam to the boundary farm 4, the low-pressure nitrogen gas source 5, the fuel gas source 6, the sour water stripping system 7, the low-pressure gas to the boundary farm 8 and the refined aviation kerosene to the boundary farm 9 are all the prior art.
Example 2:
Referring to fig. 1, the present embodiment is different in that: the first separation part comprises a first oil-water separator 10, a first feeding pump 11 and a first heat exchanger 12, raw oil is communicated with the feeding end of the first oil-water separator 10 from the tank area 2 through the first heat exchanger 12, the oil outlet of the first oil-water separator 10 is communicated with the hydrogenation reaction part through the first feeding pump 11, the water outlet end of the first oil-water separator 10 is communicated with the acid water stripping system 7, and the air inlet end of the first oil-water separator 10 is communicated with the fuel gas source 6.
When in actual use, the method comprises the following steps: the raw oil is sent into an oil-water separator I10 from a tank area 2 through a heat exchanger I12, then the raw oil is subjected to oil-water separation through the oil-water separator I10 to obtain acidic water and dehydrated raw oil, meanwhile, fuel gas is injected into the oil-water separator I10 through a fuel gas source 6 during separation, the operation pressure of the oil-water separator I10 is stabilized, the outlet flow of a feed pump I11 is ensured to be stable, and meanwhile, when the raw oil passes through the heat exchanger I12, the temperature of the raw oil is increased through heat exchange with the product oil, the heat exchange final temperature of the raw oil is increased, and the heating load of a reaction feed furnace 14 is reduced.
Example 3:
Referring to fig. 1, the present embodiment is different in that: the hydrogenation portion includes heat exchanger two 13, reaction feeding stove 14, liquid phase hydrogenation reactor 15 and circulating pump 16, reaction feeding stove 14 feed end is through heat exchanger two 13 and separation portion intercommunication, the intercommunication has circulation pipeline 17 between the discharge end of liquid phase hydrogenation reactor 15 and the feed end, and circulating pump 16 concatenates on circulation pipeline 17, and reaction feeding stove 14's discharge end and circulation pipeline 17 intercommunication, switch on hydrogen gas source 1 between heat exchanger two 13 and the separation portion one, hydrogen gas source 1 still communicates with liquid phase hydrogenation reactor 15, liquid phase hydrogenation reactor 15's discharge end still communicates with the separation portion two, concatenate heat exchanger two 13 between liquid phase hydrogenation reactor 15's discharge end and the separation portion two, liquid phase hydrogenation reactor 15's gas outlet end and separation portion two intercommunication.
When in actual use, the method comprises the following steps: raw oil is mixed with hydrogen through a first feeding pump 11, enters a reaction feeding furnace 14 through a second heat exchanger 13, is heated and warmed to 240-260 ℃ through the reaction feeding furnace 14, then enters a liquid-phase hydrogenation reactor 15 through a circulating pipeline, raw oil is mixed with liquid-phase hydrogen, so that the raw oil contains oil and dissolves hydrogen, then a reaction product is discharged through a discharge end of the liquid-phase hydrogenation reactor 15, meanwhile, part of the discharged reaction product is mixed with the raw oil discharged from the reaction feeding furnace 14 through a circulating pump 16, hydrogen required by reaction is provided for fresh feeding, and meanwhile, the reaction product is subjected to heat exchange with the raw oil when entering a second separation part through the second heat exchanger 13, so that the temperature of the raw oil is increased.
The hydrogen gas functions to maintain the liquid level in the liquid phase hydrogenation reactor 15 and to extract the hydrogen gas required for the feedstock reaction.
And the reaction exhaust gas of the liquid phase hydrogenation reactor 15 enters the second separation part.
By closing the main valve through which the raw oil of the second heat exchanger 13 passes, the thermal displacement of the raw oil and the reaction product can be reduced, thereby further increasing the temperature of the reaction product.
Example 4:
referring to fig. 1, the present embodiment is different in that: the second separation part comprises a hot low-pressure separator 18, a cold low-pressure separator 19 and an air cooler I20, wherein the feed end of the hot low-pressure separator is communicated with the discharge end of the hydrogenation reaction part, the air outlet end of the hot low-pressure separator 18 is communicated with the feed end of the cold low-pressure separator 19 through the air cooler I20 respectively, the air cooler I20 is communicated with the heat exchange part, the discharge end of the cold low-pressure separator 19 is communicated with the feed end of the first separation part, the air outlet end and the water outlet end of the cold low-pressure separator 19 are communicated with the low-pressure gas separation to boundary 8 and the sour water stripping system 7 respectively, and the discharge end of the hot low-pressure separator 18 is communicated with the stripping part.
When in actual use, the method comprises the following steps: the reaction product is depressurized and then enters a thermal low-pressure separator 18 to separate a gas phase and a liquid phase, so as to obtain thermal low-pressure oil and reaction exhaust gas, and then the thermal low-pressure oil enters a stripping part.
Simultaneously, the reaction exhaust gas of the hot low-pressure separator 18 and the liquid-phase hydrogenation reactor 15 is cooled by the first air cooler 20 and enters the cold low-pressure separator 19 to obtain cold low-pressure oil, acid water and low-pressure gas, the low-pressure gas enters the low-pressure gas to the boundary region 8, the acid water enters the acid water stripping system 7, and the cold low-pressure oil flows back to the feeding end of the first oil-water separator 10 for retreatment.
Example 5:
Referring to fig. 1, the present embodiment is different in that: the stripping part comprises a stripping tower 21, a product pump 22, a reflux pump 23, an air cooler II 24 and an oil-water separator II 25, wherein the discharge end of the hot low-pressure separator 18 is communicated with the feed end of the stripping tower 21, the discharge end of the stripping tower 21 is communicated with the heat exchange part through the product pump 22, the air inlet end of the stripping tower 21 is communicated with the low-pressure nitrogen gas source 5, the air outlet pipe of the stripping tower 21 is communicated with the feed end of the oil-water separator II 25 through the air cooler II 24, the discharge end of the oil-water separator II 25 is communicated with the reflux end of the stripping tower 21 through the reflux pump 23, the water outlet end of the oil-water separator II 25 is communicated with the acid water stripping system 7, and the air cooler II 24 is communicated with the heat exchange part.
When in actual use, the method comprises the following steps: the hot low-pressure oil enters a stripping tower 21 through decompression, hydrogen sulfide and ammonia in the hot low-pressure oil are further removed by the stripping tower 21 through nitrogen, product oil and tower top exhaust gas are obtained, the tower top exhaust gas is cooled by an air cooler II 24 and enters an oil-water separator II 25, the oil-water separator II 25 is used for carrying out gas-oil-water separation on the tower top exhaust gas, acidic water, noncondensable gas and reflux oil are obtained, and the reflux oil is sent to a reflux end of the stripping tower 21 through a reflux pump 23 and is stripped again.
The product oil obtained from the stripper is fed to the heat exchange section by means of a product pump 22.
Example 6:
Referring to fig. 1, the present embodiment is different in that: the heat exchange part comprises a heat exchanger III 26, a heat exchanger IV 27, a desuperheater 28, a heating furnace convection chamber 29 and an air cooler III 30, deoxygenated water is communicated with the air cooler III 20, the air cooler II 24 and the desuperheater 28 from the boundary area 3 respectively, deoxygenated water is communicated with the desuperheater 28 from the boundary area 3 through the heat exchanger III 26, the heat exchanger IV 27 and the heating furnace convection chamber 29, the desuperheater 28 is communicated with the overheated low-pressure steam to the boundary area 4, the discharge end of the stripping tower 21 is communicated with the feed end of the air cooler III 30 through the heat exchanger IV 27, the heat exchanger III 26 and the heat exchanger I12, and the discharge end of the air cooler III 30 is communicated with the feed part. .
When in actual use, the method comprises the following steps: the product oil heats deoxidized water through a third heat exchanger 26 and a fourth heat exchanger 27, then heats the hot flue gas of a convection chamber 29 of the heating furnace again, then enters a desuperheater 28, and then enters the overheated low-pressure steam to a boundary zone 4 through the desuperheater 28 for supplying other low-pressure steam users, the deoxidized water is directly connected with the desuperheater 28 to further increase the steam, and meanwhile, the deoxidized water is communicated with a first air cooler 20 and a second air cooler 24 to prevent the crystallization of reaction exhaust gas and tower top exhaust gas betaine, so that the normal operation of the first air cooler 20 and the second air cooler 24 is ensured.
The product oil enters the feeding part through the third heat exchanger 26 and the fourth heat exchanger 27 and then enters the feeding part through the third air cooler 30, and the product oil is further cooled through the third air cooler 30.
Example 7:
Referring to fig. 1, the present embodiment is different in that: the charging part comprises a filtering separator 31, a coalescer 32, a cooler 33 and a dosing system 34, wherein the discharging end of the air cooler three 30 is communicated with the refined aviation kerosene to the boundary zone 9 through the filtering separator 31, the coalescer 32 and the cooler 33 which are connected in series, and the discharging end of the dosing system 34 is communicated with the feeding end of the filtering separator 31.
When in actual use, the method comprises the following steps: the product oil cooled by the air cooler III 30 is mixed with an antioxidant by a dosing system 34, filtered by a filtering separator 31 to remove impurities from the product oil, dehydrated by a coalescer 32, cooled to 30 ℃ by a cooler 33, and discharged into the refined aviation kerosene to the boundary region 9.
The embodiments of the present invention have been described in detail with reference to the drawings, but the present invention is not limited to the above embodiments, and various changes can be made within the scope of the knowledge of those skilled in the art without departing from the spirit of the present invention, which is within the scope of the present invention.
Claims (1)
1. An aviation kerosene hydrogenation system employing nitrogen stripping, comprising at least: hydrogen gas source (1), raw oil from tank field (2), deoxygenated water from boundary field (3), overheated low pressure steam to boundary field (4), low pressure nitrogen gas source (5), fuel gas source (6), sour water stripping system (7), low gas separation to boundary field (8) and refined aviation kerosene to boundary field (9), its characterized in that still includes:
The first separation part is communicated with the raw oil from the tank area (2) at the feeding end of the oil-water separation part and is also respectively communicated with a fuel gas source (6) and an acid water stripping system (7);
the hydrogenation reaction part is respectively communicated with a hydrogen gas source (1) and an oil outlet end of the oil-water separator, and an air outlet end of the hydrogenation reaction part is communicated with the second separation part;
The second separation part is respectively communicated with the discharge end of the hydrogenation reaction part, the feed end of the first separation part, the sour water stripping system (7) and the low-pressure gas separation to the boundary zone (8);
the stripping part is communicated with the discharge end of the second separation part, is communicated with a low-pressure nitrogen gas source (5) and is used as a gas source of stripping through nitrogen;
The heat exchange part is respectively communicated with the deoxygenated water self-limiting area (3), the superheated low-pressure steam self-limiting area (4), the separation part II and the discharge end of the stripping part;
The feeding part is communicated with the discharge end of the heat exchange part, and the discharge end of the feeding part is communicated with the refined aviation kerosene to the boundary region (9);
The first separation part comprises a first oil-water separator (10), a first feeding pump (11) and a first heat exchanger (12), raw oil is communicated with the feeding end of the first oil-water separator (10) from the tank area (2) through the first heat exchanger (12), an oil outlet of the first oil-water separator (10) is communicated with the hydrogenation reaction part through the first feeding pump (11), the water outlet end of the first oil-water separator (10) is communicated with the acid water stripping system (7), and the air inlet end of the first oil-water separator (10) is communicated with the fuel gas source (6);
The hydrogenation reaction part comprises a second heat exchanger (13), a reaction feeding furnace (14), a liquid-phase hydrogenation reactor (15) and a circulating pump (16), wherein the feeding end of the reaction feeding furnace (14) is communicated with the separation part through the second heat exchanger (13), a circulating pipeline (17) is communicated between the discharging end and the feeding end of the liquid-phase hydrogenation reactor (15), the circulating pump (16) is connected on the circulating pipeline (17) in series, the discharging end of the reaction feeding furnace (14) is communicated with the circulating pipeline (17), a hydrogen gas source (1) is communicated between the second heat exchanger (13) and the first separation part, the hydrogen gas source (1) is also communicated with the liquid-phase hydrogenation reactor (15), the discharging end of the liquid-phase hydrogenation reactor (15) is also communicated with the second separation part, the discharging end of the liquid-phase hydrogenation reactor (15) is connected with the second separation part in series, and the discharging end of the liquid-phase hydrogenation reactor (15) is communicated with the second separation part;
The second separation part comprises a hot low-pressure separator (18), a cold low-pressure separator (19) and a first air cooler (20), wherein the feed end of the hot low-pressure separator is communicated with the discharge end of the hydrogenation reaction part, the discharge end of the hot low-pressure separator (18) is communicated with the feed end of the cold low-pressure separator (19) through the first air cooler (20) respectively, the first air cooler (20) is communicated with the heat exchange part, the discharge end of the cold low-pressure separator (19) is communicated with the feed end of the first separation part, the discharge end and the discharge end of the cold low-pressure separator (19) are communicated with the low-pressure gas-separating boundary region (8) and the sour water stripping system (7) respectively, and the discharge end of the hot low-pressure separator (18) is communicated with the stripping part;
The stripping part comprises a stripping tower (21), a product pump (22), a reflux pump (23), an air cooler II (24) and an oil-water separator II (25), wherein the discharge end of the hot low-pressure separator (18) is communicated with the feed end of the stripping tower (21), the discharge end of the stripping tower (21) is communicated with the heat exchange part through the product pump (22), the air inlet end of the stripping tower (21) is communicated with a low-pressure nitrogen gas source (5), the air outlet pipe of the stripping tower (21) is communicated with the feed end of the oil-water separator II (25) through the air cooler II (24), the discharge end of the oil-water separator II (25) is communicated with the reflux end of the stripping tower (21) through the reflux pump (23), and the water outlet end of the oil-water separator II (25) is communicated with the acid water stripping system (7), and the air cooler II (24) is communicated with the heat exchange part;
The heat exchange part comprises a third heat exchanger (26), a fourth heat exchanger (27), a desuperheater (28), a heating furnace convection chamber (29) and a third air cooler (30), the deoxygenated water self-limiting area (3) is respectively communicated with the first air cooler (20), the second air cooler (24) and the desuperheater (28), the deoxygenated water self-limiting area (3) is also communicated with the desuperheater (28) through the third heat exchanger (26), the fourth heat exchanger (27) and the heating furnace convection chamber (29), the desuperheater (28) is communicated with the superheated low-pressure steam to the limiting area (4), the discharge end of the stripping tower (21) is communicated with the feed end of the third air cooler (30) through the fourth heat exchanger (27), the third heat exchanger (26), the first heat exchanger (12), and the discharge end of the third air cooler (30) is communicated with the feed part;
The charging part comprises a filtering separator (31), a coalescer (32), a cooler (33) and a dosing system (34), wherein the discharging end of the air cooler III (30) is communicated with the refined aviation kerosene to the boundary zone (9) through the filtering separator (31), the coalescer (32) and the cooler (33) which are connected in series, and the discharging end of the dosing system (34) is communicated with the feeding end of the filtering separator (31).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202111648204.2A CN116410770B (en) | 2021-12-31 | 2021-12-31 | Aviation kerosene hydrogenation system adopting nitrogen stripping |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105670689A (en) * | 2016-02-01 | 2016-06-15 | 北京燕山玉龙石化工程有限公司 | Kerosene-hydrogenation production process and system |
| CN108018078A (en) * | 2016-10-31 | 2018-05-11 | 中国石化工程建设有限公司 | One kind boat coal liquid-phase hydrogenatin system and boat coal liquid phase hydrogenating method |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105670689A (en) * | 2016-02-01 | 2016-06-15 | 北京燕山玉龙石化工程有限公司 | Kerosene-hydrogenation production process and system |
| CN108018078A (en) * | 2016-10-31 | 2018-05-11 | 中国石化工程建设有限公司 | One kind boat coal liquid-phase hydrogenatin system and boat coal liquid phase hydrogenating method |
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