CN113698955A - Aviation kerosene hydrogenation reaction product treatment system - Google Patents
Aviation kerosene hydrogenation reaction product treatment system Download PDFInfo
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- CN113698955A CN113698955A CN202010434333.0A CN202010434333A CN113698955A CN 113698955 A CN113698955 A CN 113698955A CN 202010434333 A CN202010434333 A CN 202010434333A CN 113698955 A CN113698955 A CN 113698955A
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- 239000003350 kerosene Substances 0.000 title claims abstract description 97
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 67
- 239000007795 chemical reaction product Substances 0.000 title claims abstract description 54
- 239000000047 product Substances 0.000 claims abstract description 244
- 238000005194 fractionation Methods 0.000 claims abstract description 134
- 238000001816 cooling Methods 0.000 claims abstract description 73
- 238000012545 processing Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 58
- 229910001868 water Inorganic materials 0.000 claims description 58
- 239000003963 antioxidant agent Substances 0.000 claims description 20
- 230000003078 antioxidant effect Effects 0.000 claims description 20
- 238000002347 injection Methods 0.000 claims description 20
- 239000007924 injection Substances 0.000 claims description 20
- 238000001179 sorption measurement Methods 0.000 claims description 18
- 230000001105 regulatory effect Effects 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 2
- 238000004508 fractional distillation Methods 0.000 claims 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 58
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 38
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 38
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 29
- 229910021529 ammonia Inorganic materials 0.000 abstract description 29
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 29
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 29
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract description 20
- 239000000126 substance Substances 0.000 abstract description 20
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052802 copper Inorganic materials 0.000 abstract description 12
- 239000010949 copper Substances 0.000 abstract description 12
- 238000005260 corrosion Methods 0.000 abstract description 12
- 230000007797 corrosion Effects 0.000 abstract description 12
- 235000019270 ammonium chloride Nutrition 0.000 abstract description 10
- 238000007670 refining Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 44
- 235000006708 antioxidants Nutrition 0.000 description 18
- 238000010992 reflux Methods 0.000 description 15
- 239000003463 adsorbent Substances 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
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- 238000010521 absorption reaction Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000000087 stabilizing effect Effects 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910000952 Be alloy Inorganic materials 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
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- 238000011084 recovery Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
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- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- -1 iron ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
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Images
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
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
-
- 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
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/201—Impurities
- C10G2300/207—Acid gases, e.g. H2S, COS, SO2, HCN
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The application discloses aviation kerosene hydrogenation reaction product processing system belongs to oil refining technical field. The system comprises: the system comprises a fractionation device, a first pressurizing device, a first air cooling device and an oil phase product treatment device; the first inlet of the fractionating device is used for inputting aviation kerosene hydrogenation reaction products, the first outlet of the fractionating device is used for outputting gas-phase products, the second outlet of the fractionating device is used for outputting oil-phase products, the second outlet of the fractionating device is communicated with the inlet of the first pressurizing device, and the outlet of the first pressurizing device is communicated with the inlet of the first air cooling device; the outlet of the first air cooling device is respectively communicated with the second inlet of the fractionating device and the inlet of the oil phase product treatment device, and the outlet of the oil phase product treatment device is used for outputting the aviation kerosene product. Because the refluxed oil phase product hardly contains substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like, the refluxed oil phase product also does not contain ammonium chloride, so that indexes such as copper sheet corrosion of the finally obtained aviation kerosene product are stable and qualified.
Description
Technical Field
The application relates to the technical field of oil refining, in particular to a system for treating products of aviation kerosene hydrogenation reaction.
Background
With the rapid development of the civil aviation industry, the demand of aviation kerosene is increasing. The current relatively mature aviation kerosene refining process comprises a hydrogenation process. The hydrogenation process is to convert non-hydrocarbon compounds such as sulfur, nitrogen, oxygen, chlorine and the like in raw oil products into substances such as hydrogen sulfide, water, ammonia, hydrogen chloride and the like, and simultaneously, olefin and aromatic hydrocarbon are saturated. That is, the aviation kerosene hydrogenation reaction product comprises saturated products of hydrogen sulfide, water, ammonia, hydrogen chloride and the like, and olefins and aromatic hydrocarbons. And then, removing substances such as hydrogen sulfide, water, ammonia, hydrogen chloride and the like in the aviation kerosene hydrogenation reaction product to obtain the aviation kerosene product with better stability, combustibility and corrosivity.
In the related art, the aviation kerosene hydrogenation reaction product treatment device comprises a fractionating tower, an air cooler, a reflux tank and the like. And (3) feeding the aviation kerosene hydrogenation reaction product into a fractionating tower for fractionation, and outputting the fractionated gas-phase product from the tower top of the fractionating tower into an air cooler for cooling. The gas-phase product is cooled in an air cooler and then becomes a gas-water-oil three-phase mixed state, and then the gas-water-oil three-phase mixed state is sent into a reflux tank for gas-water-oil three-phase separation. In the reflux tank, the separated gas phase product enters a flare gas holder recovery system, the separated water phase product enters an acid water stripping system, one part of the separated oil phase product is output as crude naphtha, and the other part of the separated oil phase product reflows to the fractionating tower. And (4) outputting the oil phase product fractionated in the fractionating tower from the tower bottom of the fractionating tower, and treating to obtain the aviation kerosene product.
However, the gas phase product distilled from the aviation kerosene hydrogenation reaction product in the fractionating tower includes hydrogen sulfide, ammonia, hydrogen chloride and the like. When the oil phase product obtained after cooling the gas phase product is returned to the fractionating tower, these substances are re-fed into the fractionating tower along with the oil phase product. The ammonia and hydrogen chloride in these substances can react to form ammonium chloride, which is difficult to decompose in the fractionating tower due to the high decomposition temperature of ammonium chloride, and is mixed with the fractionated oil phase product and output from the bottom of the fractionating tower. The strong acidity of the ammonium chloride can cause unqualified indexes such as copper sheet corrosion of the finally obtained aviation kerosene product.
Disclosure of Invention
The application provides a aviation kerosene hydrogenation reaction product treatment system, which can ensure that indexes such as copper sheet corrosion of the finally obtained aviation kerosene product are qualified.
In one aspect, a system for treating aviation kerosene hydrogenation reaction products is provided, the system comprising: the system comprises a fractionation device, a first pressurizing device, a first air cooling device and an oil phase product treatment device;
the first inlet of the fractionation device is used for inputting aviation kerosene hydrogenation reaction products, the first outlet of the fractionation device is used for outputting gas-phase products, the second outlet of the fractionation device is used for outputting oil-phase products, the second outlet of the fractionation device is communicated with the inlet of the first pressurizing device, and the outlet of the first pressurizing device is communicated with the inlet of the first air cooling device;
and the outlet of the first air cooling device is respectively communicated with the second inlet of the fractionating device and the inlet of the oil phase product treatment device, and the outlet of the oil phase product treatment device is used for outputting the aviation kerosene product.
Optionally, the system further comprises a heat exchange device comprising a first portion and a second portion;
the inlet of the first part is used for inputting the aviation kerosene hydrogenation reaction product, and the outlet of the first part is communicated with the first inlet of the fractionation device;
the inlet of the second part is communicated with the outlet of the first pressurizing device, and the outlet of the second part is communicated with the inlet of the first air cooling device.
Optionally, the oil phase product processing device comprises an adsorption tank, a coalescing filter and an antioxidant skid;
the inlet of adsorption tank with the outlet intercommunication of first air cooling device, the outlet of adsorption tank with the inlet intercommunication of coalescence filter, the outlet of coalescence filter with the outlet of anti-oxidant sled piece all communicates with first output pipeline, first output pipeline is used for exporting the aviation kerosene product.
Optionally, the fractionation unit comprises a fractionation column and a reboiler;
the first inlet of the fractionating tower is used for inputting the aviation kerosene hydrogenation reaction products, the first outlet of the fractionating tower is used for outputting gas-phase products, the second outlet of the fractionating tower is used for outputting oil-phase products, and the second outlet of the fractionating tower is communicated with the inlet of the first pressurizing device;
the second inlet of the fractionating tower is communicated with the outlet of the first air cooling device, the third outlet of the fractionating tower is used for outputting oil phase products, the third outlet of the fractionating tower is communicated with the inlet of the reboiler, and the outlet of the reboiler is communicated with the third inlet of the fractionating tower.
Optionally, the system further comprises a regulating valve;
the outlet of the first air cooling device is communicated with the second inlet of the fractionating device through a first pipeline and a return pipeline, the outlet of the first air cooling device is communicated with the inlet of the oil phase product treatment device through the first pipeline and a second output pipeline, the regulating valve is installed on the return pipeline, and the regulating valve is used for regulating the fluid flow in the return pipeline.
Optionally, the system further comprises a temperature sensor;
the temperature sensor is mounted on the first line, the temperature sensor being for detecting a temperature of fluid in the first line.
Optionally, the system further comprises a second air cooling device;
and the inlet of the second air cooling device is communicated with the first outlet of the fractionation device.
Optionally, the system further comprises a flow diversion device;
the export of second air cooling device with diverging device's entry intercommunication, diverging device's first export is used for exporting combustible gas, diverging device's second export is used for exporting sour water, diverging device's third export is used for exporting crude naphtha.
Optionally, the system further comprises a second pressurizing device;
the inlet of the second pressurizing device is communicated with the third outlet of the flow dividing device.
Optionally, the system further comprises a water injection device;
and a first outlet of the fractionating device is communicated with an inlet of the second air cooling device through a second pipeline, an outlet of the water injection device is communicated with the second pipeline, and an inlet of the water injection device is used for injecting water.
The technical scheme provided by the application can at least bring the following beneficial effects:
in the present embodiment, the entire gas phase product distilled out of the fractionation apparatus is sent out of the fractionation apparatus, and a part of the oil phase product distilled out of the fractionation apparatus is refluxed into the fractionation apparatus to be fractionated again. Since the hydrogen sulfide, ammonia, hydrogen chloride and the like are generally distributed in the gas-phase product, the hydrogen sulfide, ammonia, hydrogen chloride and the like in the fractionation device continuously move to the top of the fractionation device and are continuously sent out of the fractionation device through the first outlet of the fractionation device. Because substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like are not generally distributed in the oil-phase product, after the oil-phase product flows back into the fractionation device, the mass of the substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like contained in the fractionation device is not increased, but the partial pressure of the substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like in the fractionation device is reduced, so that the substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like can be better output out of the fractionation device along with the gas-phase product, and the energy consumption of the fractionation device can be reduced. And because the refluxed oil phase product hardly contains substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like, the refluxed oil phase product does not contain ammonium chloride, so that the finally obtained aviation kerosene product does not contain ammonium chloride, and further, indexes such as copper sheet corrosion of the aviation kerosene product are stable and qualified.
Drawings
FIG. 1 is a schematic diagram of a first system for processing products of a aviation kerosene hydrogenation reaction provided in an embodiment of the present application;
FIG. 2 is a schematic diagram of a second system for processing products of a aviation kerosene hydrogenation reaction provided in an embodiment of the present application;
FIG. 3 is a schematic diagram of a third system for processing products of a aviation kerosene hydrogenation reaction provided in an embodiment of the present application;
FIG. 4 is a schematic illustration of a fourth system for processing aviation kerosene hydrogenation reaction products as provided in an embodiment of the present application;
FIG. 5 is a schematic diagram of a fifth system for processing products of a aviation kerosene hydrogenation reaction according to an embodiment of the present application;
FIG. 6 is a schematic diagram of a sixth system for processing products of a aviation kerosene hydrogenation reaction according to embodiments of the present application;
FIG. 7 is a schematic diagram of a seventh system for processing products of a aviation kerosene hydrogenation reaction according to an embodiment of the present application;
FIG. 8 is a schematic structural diagram of an eighth system for processing products of a aviation kerosene hydrogenation reaction provided in an embodiment of the present application.
Reference numerals:
1: a fractionation unit; 11: a fractionating column; 111: a first inlet of a fractionation unit or fractionation column; 112: a first outlet of a fractionation unit or fractionation column; 113: a second outlet of the fractionation unit or fractionation column; 114: a second inlet of the fractionation unit or fractionation column; 115: a third outlet of the fractionation column; 116: a third inlet of the fractionation column; 12: a reboiler; 121: an inlet of a reboiler; 122: an outlet of the reboiler; 2: a first pressurizing device; 21: an inlet of a first pressurizing device; 22: an outlet of the first pressurizing device; 3: a first air cooling device; 31: the inlet of the first air cooling device; 32: an outlet of the first air cooling device; 4: an oil phase product treatment device; 41: an adsorption tank; 411: an inlet of an oil phase product treatment device or an adsorption tank; 412: an outlet of the adsorption tank; 42: a coalescing filter; 421: an inlet of a coalescing filter; 422: an outlet of the coalescing filter; 43: an antioxidant prying block; 5: a heat exchange device; 51: a first portion of a heat exchange device; 52: a second portion of the heat exchange means; 6: adjusting a valve; 7: a first pipeline; 8: a return line; 91: a first output line; 92: a second output line; 10: a temperature sensor; 13: a second air cooling device; 131: the inlet of the second air cooling device; 132: an outlet of the second air cooling device; 14: a flow divider; 141: an inlet of the flow diversion device; 142: a first outlet of the flow diversion device; 143: a second outlet of the flow diversion device; 144: a third outlet of the flow diversion device; 15: a second pressurizing device; 151: an inlet of a second pressurizing device; 16: a water injection device; 161: an outlet of the water injection device; 162: an inlet of a water injection device; 17: a second pipeline.
Detailed Description
To make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below with reference to the accompanying drawings.
FIG. 1 is a schematic diagram of a system for processing products of a aviation kerosene hydrogenation reaction according to an embodiment of the present application. Referring to fig. 1, the system includes: a fractionation device 1, a first pressurizing device 2, a first air cooling device 3 and an oil phase product treatment device 4; the first inlet 111 of the fractionation device 1 is used for inputting the aviation kerosene hydrogenation reaction product, the first outlet 112 of the fractionation device 1 is used for outputting a gas-phase product, the second outlet 113 of the fractionation device 1 is used for outputting an oil-phase product, the second outlet 113 of the fractionation device 1 is communicated with the inlet 21 of the first pressurizing device 2, and the outlet 22 of the first pressurizing device 2 is communicated with the inlet 31 of the first air cooling device 3; the outlet 32 of the first air cooling device 3 is respectively communicated with the second inlet 114 of the fractionating device 1 and the inlet 411 of the oil phase product treatment device 4, and the outlet of the oil phase product treatment device 4 is used for outputting the aviation kerosene product.
The fractionation apparatus 1 is an apparatus for fractionating a product of a aviation kerosene hydrogenation reaction. The size of the fractionation unit 1 may be set as long as it is ensured that the aviation kerosene hydrogenation reaction product can be fractionated in the fractionation unit 1.
In addition, the first inlet 111 of the fractionation unit 1 is an inlet for inputting the aviation kerosene hydrogenation reaction product. The position of the first inlet 111 can be set according to the use requirement, for example, the first inlet 111 can be arranged at the side of the fractionation device 1.
Further, the first outlet 112 of the fractionation apparatus 1 is an outlet for outputting a fractionated gas-phase product. The first outlet 112 is generally disposed at the top of the fractionation device 1 because the density of the gas phase product is small, so that the gas phase product can be easily outputted out of the fractionation device 1.
Note that the second outlet 113 of the fractionation apparatus 1 is an outlet for outputting the fractionated oil-phase product. The second outlet 113 is generally disposed at the bottom of the fractionation device 1 because the oil phase product has a greater density, so that the oil phase product can be more easily output to the fractionation device 1.
In addition, the second inlet 114 of the fractionation apparatus 1 is an inlet for inputting the oil-phase product subjected to pressure cooling. The position of the second inlet 114 can be set according to the use requirement, for example, the second inlet 114 can be set at the side of the fractionating apparatus 1.
It is noted that, since the fractionated oil phase product may still contain a small amount of gas phase product, after the oil phase product treated by the first air cooling device 3 enters the fractionating device 1 again through the second inlet 114 of the fractionating device 1, the part of the refluxed oil phase product can be further fractionated, so that the yield of the finally obtained aviation kerosene product can be high.
In addition, the oil-phase product refluxed into the fractionation device 1 through the second inlet 114 of the fractionation device 1 passes through the first air cooling device 3, so that the temperature of the oil-phase product refluxed into the fractionation device 1 is low. Therefore, after the oil phase product is mixed with the aviation kerosene hydrogenation reaction product entering the fractionating device 1, the temperature can be reduced, and the aviation kerosene hydrogenation reaction product is at the optimal fractionating temperature, so that the fractionation can be carried out more fully.
The first pressurizing means 2 is a means for increasing the pressure of the fractionated oil-phase product to impart flow power to the oil-phase product. The size and type of the first pressurizing means 2 can be selected according to the use requirement, for example, the first pressurizing means 2 can be a pressurizing pump.
The first air cooling device 3 is a device for changing the temperature of the fractionated oil phase product. The size and type of the first air cooling device 3 can be selected according to the use requirement, for example, the first air cooling device 3 can be a natural ventilation type air cooler, a blast type air cooler, an induced draft type air cooler, and the like.
Further, the oil-phase product treatment apparatus 4 is an apparatus for treating the cooled oil-phase product to obtain a aviation kerosene product.
Specifically, when the aviation kerosene hydrogenation reaction product treatment system is used for treating aviation kerosene hydrogenation reaction products, the aviation kerosene hydrogenation reaction products enter the fractionation device 1 through the first inlet 111 of the fractionation device 1, and then the aviation kerosene hydrogenation reaction products are fractionated into oil phase products and gas phase products in the fractionation device 1. The gas phase product will be output through a first outlet 112 of the fractionation device 1 and the oil phase product will be output through a second outlet 113 of the fractionation device 1 to the first pressurizing device 2. The pressurized oil phase product is cooled in the first air cooling device 3. A part of the cooled oil phase product enters an oil phase product treatment device 4 for treatment to obtain a aviation kerosene product; another portion of the cooled oil phase product is returned to the fractionation unit 1 through the second inlet 114 of the fractionation unit 1 for further fractionation.
That is, in the present embodiment, the entire gas-phase product fractionated in the fractionation device 1 is sent out of the fractionation device 1, and a part of the oil-phase product fractionated in the fractionation device 1 is returned to the fractionation device 1 to be fractionated again. Since the hydrogen sulfide, ammonia, hydrogen chloride, and the like are generally distributed in the gas phase product, the hydrogen sulfide, ammonia, hydrogen chloride, and the like in the fractionation device 1 continuously move to the top of the fractionation device 1, and are continuously sent out of the fractionation device 1 through the first outlet 112 of the fractionation device 1. Since the substances such as hydrogen sulfide, ammonia, and hydrogen chloride are not generally distributed in the oil phase product, after the oil phase product flows back into the fractionation device 1, the mass of the substances such as hydrogen sulfide, ammonia, and hydrogen chloride contained in the fractionation device 1 is not increased, but the partial pressure of the substances such as hydrogen sulfide, ammonia, and hydrogen chloride in the fractionation device 1 is reduced, so that the substances such as hydrogen sulfide, ammonia, and hydrogen chloride can be better output out of the fractionation device 1 along with the gas phase product, and thus the energy consumption of the fractionation device 1 can be reduced. And because the refluxed oil phase product hardly contains substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like, the refluxed oil phase product does not contain ammonium chloride, so that the finally obtained aviation kerosene product does not contain ammonium chloride, and further, indexes such as copper sheet corrosion of the aviation kerosene product are stable and qualified.
Optionally, referring to fig. 2, the system further comprises a heat exchange device 5, the heat exchange device 5 comprising a first part 51 and a second part 52; the inlet of the first part 51 is used for inputting aviation kerosene hydrogenation reaction products (not shown in the figure), and the outlet of the first part 51 is communicated with the first inlet 111 (not shown in the figure) of the fractionation device 1; the inlet of the second section 52 communicates with the outlet 22 of the first pressurizing means 2 and the outlet of the second section 52 communicates with the inlet 31 of the first air-cooling means 3.
The heat exchanger 5 is a device for exchanging heat between the aviation kerosene hydrogenation reaction product and the fractionated oil phase product. The size and type of the heat exchange device 5 can be selected according to the use requirement, for example, the heat exchange device 5 can be a U-shaped tube heat exchanger, an immersed coil heat exchanger, a tube type heat exchanger and the like.
In addition, the heat exchange means 5 generally comprise a first portion 51 and a second portion 52, the first portion 51 and the second portion 52 being isolated from each other. First portion 51 may wrap around the periphery of second portion 52, or second portion 52 may wrap around the periphery of first portion 51. Illustratively, the first portion 51 may be shell-shaped, and the second portion 52 may be tubular, with the shell-shaped first portion 51 wrapping around the outer periphery of the tubular second portion 52.
Specifically, when the system for processing a aviation kerosene hydrogenation reaction product is used to process the aviation kerosene hydrogenation reaction product, the aviation kerosene hydrogenation reaction product may be first input into the first portion 51 through the inlet of the first portion 51, and the oil phase product pressurized by the first pressurizing device 2 may be input into the second portion 52 through the inlet of the second portion 52. And then the aviation kerosene hydrogenation reaction product and the oil phase product are subjected to heat exchange in the heat exchange device 5, so that the temperature of the aviation kerosene hydrogenation reaction product is increased, and the temperature of the oil phase product is reduced. Finally, the aviation kerosene hydrogenation reaction product with the increased temperature is output through the outlet of the first part 51 and then enters the fractionating device 1 through the first inlet 111 of the fractionating device 1 for fractionation. The oil phase product with reduced temperature is output through the outlet of the second section 52 and then enters the first air cooling device 3 through the inlet 31 of the first air cooling device 3 for cooling. Thus, the energy consumption of the fractionation unit 1 and the first air cooling unit 3 can be reduced.
Alternatively, referring to fig. 1, oil phase product treatment apparatus 4 includes an adsorption tank 41, a coalescing filter 42, and an antioxidant skid 43; the inlet 411 of the adsorption tank 41 is communicated with the outlet 32 of the first air cooling device 3, the outlet 412 of the adsorption tank 41 is communicated with the inlet 421 of the coalescing filter 42, the outlet 422 of the coalescing filter 42 and the outlet of the antioxidant pry block 43 are both communicated with the first output pipeline 91, and the first output pipeline 91 is used for outputting the aviation kerosene product.
The adsorption tank 41 is a member for absorbing a trace amount of hydrogen sulfide contained in the oil-phase product to remove the hydrogen sulfide from the oil-phase product. The size and material of the canister 41 may be selected according to the use requirement, and for example, the diameter of the canister 41 may be 3000 mm, 3600 mm, 4000 mm, or the like.
The values are described in the specification, the adsorption tank 41 usually contains an adsorbent. Because the solubility of hydrogen sulfide in the adsorbent is high, when the hydrogen sulfide is mixed with the adsorbent, the hydrogen sulfide can be dissolved in the adsorbent, so that the hydrogen sulfide is removed from the oil phase product. The type of adsorbent may be selected according to the use requirements, for example, the adsorbent may be zinc oxide.
In addition, the content of hydrogen sulfide in the refluxed oil-phase product is low, so that the content of hydrogen sulfide in the oil-phase product finally fractionated by the fractionation apparatus 1 is lower than that in the conventional case. In this case, the adsorbent replacement time in the canister 41 may be appropriately changed, and for example, the replacement time may be extended from half a year to one year. Thus, the replacement cost of the adsorbent and the cost of harmless treatment of the waste adsorbent can be reduced.
It should be noted that the coalescing filter 42 is a member for filtering solid particles and moisture included in the oil-phase product. The filtering precision of the coalescing filter 42 can be set according to the use requirement, for example, the filtering precision can be 1-5 μm (micrometer). For example, the filtration accuracy may be 1 μm, 2 μm, 3 μm, 4 μm, 5 μm, or the like.
In addition, coalescing filter 42 typically has multiple layers of filter media with small pores distributed through each layer of filter media. Since the fractionation apparatus 1 may have a problem of rusting or the like due to long-term operation, iron rust or iron dust may be doped in the fractionated oil phase product. When the oil-phase product enters the coalescing filter 42, rust or iron pieces are filtered out when passing through the multi-layer filter medium because the particles of rust or iron pieces are large. And because the oil and water have different surface tensions, when the oil phase product enters the coalescing filter 42, the oil will quickly pass through the pores of the filter media due to the difference in surface tension, while the water will pass through the pores at a much slower rate. When the slow flowing water converges into large droplets, it settles under the action of gravity and separates from the oil. In this way, solid particles and moisture in the oil phase product can be removed, so that the performance of the finally obtained aviation kerosene product is better.
The antioxidant skid 43 is a member for adding an antioxidant to the oil phase product. The size and the material of the antioxidant pry block 43 can be set according to the use requirement, for example, the material of the antioxidant pry block 43 can be alloy, stainless steel and the like.
In addition, the content of the antioxidant added to the oil phase product by the antioxidant skid 43 can be selected according to the use requirement, for example, the added amount of the antioxidant can be 17mg/L (milligrams per liter) to 24 mg/L. Illustratively, the antioxidant may be added in an amount of 17mg/L, 19mg/L, 21mg/L, or 24 mg/L.
Specifically, when the cooled oil-phase product is treated by the oil-phase product treatment apparatus 4, the oil-phase product enters the adsorption tank 41 through the inlet 411 of the adsorption tank 41, and at this time, the oil-phase product removes hydrogen sulfide contained therein in the adsorption tank 41. Thereafter, the oil phase product enters coalescing filter 42 through inlet 421 of coalescing filter 42, and at this time, the oil phase product removes solid particles and moisture contained therein in coalescing filter 42. Then, the oil phase product enters the first output pipeline 91, the antioxidant skid 43 injects the antioxidant into the first output pipeline 91, and the oil phase product in the first output pipeline 91 is mixed with the antioxidant. Finally, the hydrogen sulfide, solid particles and moisture are removed, and the oil phase product mixed with the antioxidant is output from the first output line 91 as a aviation kerosene product. Therefore, the final output aviation kerosene product is ensured to have less impurities and better properties.
Alternatively, referring to fig. 1, the fractionation apparatus 1 includes a fractionation column 11 and a reboiler 12; a first inlet 111 of the fractionating tower 11 is used for inputting the aviation kerosene hydrogenation reaction product, a first outlet 112 of the fractionating tower 11 is used for outputting a gas-phase product, a second outlet 113 of the fractionating tower 11 is used for outputting an oil-phase product, and the second outlet 113 of the fractionating tower 11 is communicated with the inlet 21 of the first pressurizing device 2; the second inlet 114 of the fractionating tower 11 is communicated with the outlet 32 of the first air cooling device 3, the third outlet 115 of the fractionating tower 11 is used for outputting oil-phase products, the third outlet 115 of the fractionating tower 11 is communicated with the inlet 121 of the reboiler 12, and the outlet 122 of the reboiler 12 is communicated with the third inlet 116 of the fractionating tower 11.
It should be noted that the fractionating tower 11 is a member for fractionating the aviation kerosene hydrogenation reaction product to produce an oil phase product and a gas phase product. The material and size of the fractionating tower 11 may be set according to the use requirement, and for example, the inner diameter of the fractionating tower 11 may be 3 meters.
In addition, the first inlet 111 of the fractionation tower 11 is an inlet for inputting the aviation kerosene hydrogenation reaction product. The position of the first inlet 111 may be set according to the use requirement, for example, the first inlet 111 may be arranged at the side of the fractionating tower 11.
Further, the first outlet 112 of the fractionation column 11 is an outlet for outputting a fractionated gas-phase product. The first outlet 112 is generally disposed at the top of the fractionation column 11 because the density of the gas-phase product is small, so that the gas-phase product can be more easily output to the fractionation column 11.
Note that the second outlet 113 and the third outlet 115 of the fractionation column 11 are outlets for outputting the fractionated oil-phase product. The second outlet 113 is generally disposed at the bottom of the fractionation tower 11 because the oil phase product has a greater density, so that the oil phase product can be more easily output to the fractionation tower 11.
In addition, the second inlet 114 of the fractionation column 11 is an inlet for inputting the oil-phase product subjected to pressure cooling. The position of the second inlet 114 can be set according to the use requirement, for example, the second inlet 114 can be set at the side of the fractionating tower 11.
Furthermore, the specific operation conditions of the fractionating tower 11 can be set according to the use requirement, for example, when the pressure drop loss caused by material flow is not counted, the operation pressure of the fractionating tower 11 can be 0.15-0.50 MPag. Illustratively, the operating pressure may be 0.15Mpag, 0.20Mpag, 0.25Mpag, 0.33Mpag, 0.42Mpag, 0.50Mpag, or the like. The feed operating temperature of the fractionating column 11 may be 180 to 250 ℃. Illustratively, the feed operating temperature may be 180, 210 ℃, or 250 ℃, among others. The operation temperature of the bottom of the fractionating tower 11 may be 240 to 280 ℃. Illustratively, the operating temperature of the bottom of the column may be 240 ℃, 253 ℃, 270 ℃, or 280 ℃, etc.
It should be noted that the reboiler 12 is a member for supplying a heat source to the fractionating tower 11 to ensure sufficient fractionation of the aviation kerosene hydrogenation reaction product into a gas phase product and an oil phase product. The type and size of the reboiler 12 may be set according to the use requirement, for example, the reboiler 12 may be a kettle reboiler, a thermosiphon reboiler, or the like.
Specifically, the aviation kerosene hydrogenation reaction product enters the fractionating tower 11 through the first inlet 111 of the fractionating tower 11, and the aviation kerosene hydrogenation reaction product is fractionated into a gas phase product and an oil phase product in the fractionating tower 11. Then, the fractionated gas phase product is output through a first outlet 112 of the fractionating tower 11, a part of the fractionated oil phase product enters the first pressurizing device 2 through a second outlet 113 of the fractionating tower 11 to be pressurized, and enters the first air cooling device 3 to be cooled after being pressurized, a part of the cooled oil phase product returns to the fractionating tower 11 through a second inlet 114 of the fractionating tower 11 to be fractionated again, and the other part of the cooled oil phase product enters the oil phase product processing device 4 to be processed, so as to obtain the aviation kerosene product. The separated oil phase product is fed into the reboiler 12 through the third outlet 115 of the fractionation tower 11, and is returned to the fractionation tower 11 through the third inlet 116 of the fractionation tower 11 after the temperature of the reboiler 12 is raised. Thus, the aviation kerosene hydrogenation reaction product can be fully fractionated. And as the oil phase product which does not contain hydrogen sulfide, ammonia, hydrogen chloride and the like basically flows back into the fractionating tower 11, the total content of the hydrogen sulfide, the ammonia, the hydrogen chloride and the like in the fractionating tower 11 is lower, so that the fractionating tower 11 can fractionate the aviation kerosene hydrogenation reaction product and the refluxed oil phase product under lower operating pressure and operating temperature, and the energy consumption of the fractionating tower 11 can be further reduced.
Optionally, referring to fig. 3, the system further comprises a regulating valve 6; the outlet 32 of the first air cooling device 3 is communicated with the second inlet 114 of the fractionation device 1 through a first pipeline 7 and a return pipeline 8, the outlet 32 of the first air cooling device 3 is communicated with the inlet 411 of the oil-phase product treatment device 4 through a first pipeline 7 and a second output pipeline 92, a regulating valve 6 is installed on the return pipeline 8, and the regulating valve 6 is used for regulating the flow rate of the fluid in the return pipeline 8.
It should be noted that the type and size of the regulating valve 6 can be selected according to the use requirement, for example, the regulating valve 6 can be an electric regulating valve, a pneumatic regulating valve, a hydraulic regulating valve, etc.
In addition, the fluid flow in the return line 8 can be set according to the requirements of use. In the embodiment of the present application, the ratio between the amount of the oil-phase product in the return line 8 and the amount of the oil-phase product output from the outlet 32 of the first air cooling device 3 may be referred to as a reflux ratio. For example, the reflux ratio may be 0.5 to 5.0. Illustratively, the reflux ratio may be 0.5, 1, 1.5, 2, 3, 4, or 5, and so forth. Among them, the reflux ratio may preferably be 1 to 3 for better reflux.
Further, the first line 7 is a line for outputting an oil-phase product, the reflux line 8 is a line for refluxing a part of the oil-phase product to the fractionation device 1, and the second output line 92 is a line for transferring another part of the oil-phase product to the oil-phase product treatment device 4. The pipe diameters of the first pipeline 7, the return pipeline 8 and the second output pipeline 92 can be set according to the use requirement, for example, the pipe diameters of the first pipeline 7, the return pipeline 8 and the second output pipeline 92 can be set to 65 mm.
Specifically, when the oil-phase product is output from the first air cooling device 3 into the first pipeline 7, a part of the oil-phase product enters the return pipeline 8, the regulating valve 6 installed on the return pipeline 8 regulates the flow rate of the oil-phase product in the return pipeline 8, and the oil-phase product subjected to flow rate regulation flows back into the fractionation device 1. Another portion of the oil phase product will enter the second output line 92 and enter the oil phase product treatment device 4 through the second output line 92 for treatment. Since the flow rate of the oil-phase product flowing back into the fractionation device 1 can be adjusted by the adjusting valve 6, the flow rate of the oil-phase product flowing back into the fractionation device 1 can be ensured to be controllable, and thus the oil-phase product flowing back into the fractionation device 1 can be ensured to be sufficiently fractionated.
Optionally, referring to fig. 4, the system further comprises a temperature sensor 10; a temperature sensor 10 is mounted on the first line 7, the temperature sensor 10 being used to detect the temperature of the fluid in the first line 7.
It should be noted that the temperature sensor 10 can detect the temperature of the oil phase product flowing through the first line 7. The material and type of the temperature sensor 10 can be selected according to the use requirement, for example, the temperature sensor 10 can be a thermocouple type temperature sensor, a thermistor type temperature sensor, or the like.
In addition, the temperature of the oil phase product in the first pipeline 7 can be set according to the use requirement, for example, the temperature of the oil phase product in the first pipeline 7 can be 40-55 ℃. Illustratively, the temperature of the oil phase product in the first line 7 may be 40 ℃, 45 ℃, 50 ℃, or 55 ℃, etc.
Specifically, when the oil-phase product enters the first line 7, the temperature of the oil-phase product can be detected by the temperature sensor 10 installed on the first line 7, thereby ensuring that the temperature of the oil-phase product entering the return line 8 and the second output line 92 is satisfactory. In this manner, when the temperature of the oil-phase product in the reflux line 8 is satisfied as required, the temperature in the fractionation device 1 can be lowered after the refluxed oil-phase product is refluxed into the fractionation device 1, so that fractionation in the fractionation device 1 can be performed more easily. When the temperature of the oil phase product in the second output line 92 is satisfactory, safe output of the aviation kerosene product can be facilitated.
Optionally, referring to fig. 5, the system further comprises a second air cooling device 13; the inlet 131 of the second air cooling device 13 is in communication with the first outlet 112 of the fractionation unit 1.
The second air cooling device 13 is a device for changing the temperature of the gas-phase product that is separated. The size and type of the second air cooling device 13 can be selected according to the use requirement, for example, the second air cooling device 13 can be a natural ventilation type air cooler, a blast type air cooler, an induced draft type air cooler, etc.
Specifically, after the fractionated gas phase product is output from the first outlet 112 of the fractionation unit 1, the gas phase product is cooled by entering the second air cooling unit 13 through the inlet 131 of the second air cooling unit 13. Upon cooling, the gas phase product will change from a single gas phase to a mixture of gas, liquid and oil three phases. Thus, the fractionated gas-phase product can be conveniently collected and reused at the later stage.
Optionally, referring to fig. 5, the system further comprises a flow diversion device 14; the outlet 132 of the second air cooling device 13 is communicated with the inlet 141 of the flow dividing device 14, the first outlet 142 of the flow dividing device 14 is used for outputting combustible gas, the second outlet 143 of the flow dividing device 14 is used for outputting sour water, and the third outlet 144 of the flow dividing device 14 is used for outputting raw naphtha.
The flow dividing device 14 is a device for separating the gas-phase product cooled by the second air cooling device 13.
In addition, the densities of the gas phase, the water phase and the oil phase are different, wherein the density of the gas phase is the smallest and the density of the water phase is the largest. Therefore, when the gas phase, the water phase and the oil phase enter the separation device 14 for separation, the gas phase with the lowest density will rise to the top of the flow dividing device 14, the water phase with the highest density will settle to the bottom of the flow dividing device 14, and the oil phase will be located between the gas phase and the water phase.
Specifically, after the cooled gas-phase product is output through the outlet 132 of the second air cooling device 13, the cooled gas-phase product enters the flow dividing device 14 through the inlet 141 of the flow dividing device 14 to be separated into a gas phase, a water phase and an oil phase, the separated gas phase can be output as a combustible gas from the first outlet 142 and enter the flare gas cabinet recovery system to be recovered, the separated water phase can be output as sour water from the second outlet 143 and enter the sour water stripping system to be stripped, and the separated oil phase can be output as crude naphtha from the third outlet 144 and enter the absorption stabilization system to be treated. Therefore, the fractionated gas-phase product can be recycled, and the utilization rate of resources is improved.
Optionally, referring to fig. 6, the system further comprises a second pressurizing means 15; the inlet 151 of the second pressurizing means 15 communicates with the third outlet 144 of the flow dividing means 14.
It should be noted that the second pressurizing means 15 is a means for increasing the pressure of the oil phase so that the oil phase can be better introduced into the absorption stabilizing system. The size and type of the second pressurizing means 15 can be selected according to the use requirement, for example, the second pressurizing means 15 can be a pressurizing pump.
Specifically, after the separated oil phase is outputted as raw naphtha from the third outlet 144, the oil phase enters the second pressurizing device 15 through the inlet 151 of the second pressurizing device 15, and the pressure of the oil phase itself is increased by the second pressurizing device 15. Therefore, the oil phase has better power, so that the oil phase can enter the absorption stabilizing system more smoothly. That is, the oil phase output from the third outlet 144 of the flow dividing device 14 can be pressurized by the second pressurizing device 15 before entering the absorption stabilizing system.
Optionally, referring to fig. 7, the system further comprises a water injection means 16; the first outlet 112 of the fractionation unit 1 communicates with the inlet 131 of the second air cooling unit 13 through the second line 17, the outlet 161 of the water injection unit 16 communicates with the second line 17, and the inlet 162 of the water injection unit 16 is used for injecting water.
Note that the water injection device 16 is a device for injecting water into the second line 17. The size and material of the water injection device 16 may be selected according to the use requirement, and for example, the material of the water injection device 16 may be alloy, stainless steel, or the like.
In addition, the water injected by the water injection device 16 may be selected according to the use requirement, for example, the injected water may be deoxygenated water. Because the deoxygenated water is clean and free of impurities, and does not contain magnesium ions, calcium ions, iron ions and the like, other impurities cannot be introduced into the fractionated gas-phase product.
It should be noted that the time for injecting water by the water injector 16 can be selected according to the use requirement, for example, water can be injected into the second pipeline 17 once per month through the water injector 16, and the time for each water injection does not exceed 24 hours.
The amount of water injected by the water injection device 16 may be selected according to the use requirement, and for example, the mass of the injected water may be 1% to 10%, for example, 1%, 3%, 5%, 7%, 10%, or the like, of the gas-phase product fractionated by the fractionation device 1. Wherein, for better washing the gas phase product, the water injection amount is preferably 2.5 to 6.0 percent of the gas phase product.
Specifically, after the gas-phase product is introduced into the second line 17 through the first outlet 112 of the fractionation unit 1, water may be injected into the second line 17 through the water injection device 16. Since the gas phase product generally contains ammonium salts, after water is injected into the second pipeline 17, the ammonium salts contained in the gas phase product can be washed away after the water is mixed with the gas phase product, so that the gas phase product can be reused later.
In the present embodiment, the entire gas phase product fractionated in the fractionation apparatus 1 is sent out of the fractionation apparatus 1, and a part of the oil phase product fractionated in the fractionation apparatus 1 is returned to the fractionation apparatus 1 to be fractionated again. Since the hydrogen sulfide, ammonia, hydrogen chloride, and the like are generally distributed in the gas phase product, the hydrogen sulfide, ammonia, hydrogen chloride, and the like in the fractionation device 1 continuously move to the top of the fractionation device 1, and are continuously sent out of the fractionation device 1 through the first outlet 112 of the fractionation device 1. Since the substances such as hydrogen sulfide, ammonia, and hydrogen chloride are not generally distributed in the oil phase product, after the oil phase product flows back into the fractionation device 1, the mass of the substances such as hydrogen sulfide, ammonia, and hydrogen chloride contained in the fractionation device 1 is not increased, but the partial pressure of the substances such as hydrogen sulfide, ammonia, and hydrogen chloride in the fractionation device 1 is reduced, so that the substances such as hydrogen sulfide, ammonia, and hydrogen chloride can be better output out of the fractionation device 1 along with the gas phase product, and thus the energy consumption of the fractionation device 1 can be reduced. And because the refluxed oil phase product hardly contains substances such as hydrogen sulfide, ammonia, hydrogen chloride and the like, the refluxed oil phase product does not contain ammonium chloride, so that the finally obtained aviation kerosene product does not contain ammonium chloride, and further, indexes such as copper sheet corrosion of the aviation kerosene product are stable and qualified.
In order to make the technical solutions and advantages of the present application more clear, the following detailed description will be given by means of alternative embodiments.
Example 1
Referring to fig. 8, the aviation kerosene hydrogenation reaction product is introduced into the fractionating tower 11 through the first inlet 111 to be fractionated. The fractionated gas phase product is output from the first outlet 112 to the second air cooling device 13 to be cooled. The cooled gas phase product is then fed to the splitting device 14 for separation, the separated gas phase is output through the first outlet 142, the separated water phase is output through the second outlet 143, and the separated oil phase is output through the third outlet 144. The fractionated oil phase product is output from the second outlet 113 and enters the first pressurizing device 2 for pressurizing, and the pressurized oil phase product enters the heat exchange device 5 for heat exchange with the aviation kerosene hydrogenation reaction product. Then the oil phase product enters the first air cooling device 3 for cooling, then a part of the oil phase product returns to the fractionating tower 11 from the second inlet 114, and the other part of the oil phase product is treated by the adsorption tank 41, the coalescing filter 42 and the antioxidant skid block 43 and then sent to a aviation kerosene product tank area as aviation kerosene products for storage.
Example 2
The raw oil with the sulfur content of 623 mug/g, the nitrogen content of 8 mug/g and the chlorine content of 1.3 mug/g is hydrotreated to obtain a aviation kerosene hydrogenation reaction product, and then the aviation kerosene hydrogenation reaction product is conveyed into a aviation kerosene hydrogenation reaction product treatment system shown in figure 8 to be treated. At this time, the operating pressure of the fractionating tower 11 in the aviation kerosene hydrogenation reaction product treatment system was 0.33MPag, the feed operating temperature of the fractionating tower 11 was 210 ℃, the bottom operating temperature of the fractionating tower 11 was 253 ℃, the temperature of the oil phase product in the reflux line 8 was 40 ℃, and the reflux ratio was 1.
Under the conditions, the aviation kerosene hydrogenation reaction product treatment system is operated for 1500 hours, the indexes of copper sheet corrosion and the like of the aviation kerosene product obtained finally are copper sheet corrosion stability level 1a, and the copper sheet corrosion indexes are stable and qualified.
Comparative example 1
The method comprises the steps of carrying out hydrotreatment on raw oil with the sulfur content of 623 mug/g, the nitrogen content of 8 mug/g and the chlorine content of 1.3 mug/g to obtain a aviation kerosene hydrogenation reaction product, and then conveying the aviation kerosene hydrogenation reaction product into a aviation kerosene hydrogenation reaction product treatment device provided by the related technology for treatment. At this time, the operating pressure level of the fractionating tower in this apparatus was 0.33MPag, the feed operating temperature of the fractionating tower was 210 ℃, the bottom operating temperature of the fractionating tower was 253 ℃, the reflux operating temperature of the gas-phase product was 40 ℃, and the reflux ratio was 1.
Under the conditions, the aviation kerosene hydrogenation reaction product treatment device is operated for 1500 hours, the indexes of copper sheet corrosion and the like of the aviation kerosene product obtained finally are copper sheet corrosion grade 2, and the copper sheet corrosion index is unqualified.
The above description is only exemplary of the present application and should not be taken as limiting the present application, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. A system for treating products of a aviation kerosene hydrogenation reaction, the system comprising: a fractionation device (1), a first pressurizing device (2), a first air cooling device (3) and an oil phase product treatment device (4);
the first inlet (111) of the fractionation device (1) is used for inputting aviation kerosene hydrogenation reaction products, the first outlet (112) of the fractionation device (1) is used for outputting gas-phase products, the second outlet (113) of the fractionation device (1) is used for outputting oil-phase products, the second outlet (113) of the fractionation device (1) is communicated with the inlet (21) of the first pressurizing device (2), and the outlet (22) of the first pressurizing device (2) is communicated with the inlet (31) of the first air cooling device (3);
an outlet (32) of the first air cooling device (3) is respectively communicated with a second inlet (114) of the fractionating device (1) and an inlet (411) of the oil phase product processing device (4), and an outlet of the oil phase product processing device (4) is used for outputting the aviation kerosene product.
2. The system according to claim 1, characterized in that it further comprises heat exchange means (5), said heat exchange means (5) comprising a first portion (51) and a second portion (52);
the inlet of the first part (51) is used for inputting the aviation kerosene hydrogenation reaction products, and the outlet of the first part (51) is communicated with the first inlet (111) of the fractionation device (1);
the inlet of the second section (52) communicates with the outlet (22) of the first pressurizing means (2), and the outlet of the second section (52) communicates with the inlet (31) of the first air-cooling means (3).
3. The system according to claim 1, wherein the oil phase product treatment device (4) comprises an adsorption tank (41), a coalescing filter (42), and an antioxidant skid (43);
the inlet (411) of the adsorption tank (41) is communicated with the outlet (32) of the first air cooling device (3), the outlet (412) of the adsorption tank (4) is communicated with the inlet (421) of the coalescing filter (42), the outlet (422) of the coalescing filter (42) is communicated with the outlet of the antioxidant pry block (43) and is communicated with a first output pipeline (91), and the first output pipeline (91) is used for outputting the aviation kerosene product.
4. The system according to claim 1, wherein the fractionation unit (1) comprises a fractionation column (11) and a reboiler (12);
a first inlet (111) of the fractionating tower (11) is used for inputting the aviation kerosene hydrogenation reaction products, a first outlet (112) of the fractionating tower (11) is used for outputting gas-phase products, a second outlet (113) of the fractionating tower (11) is used for outputting oil-phase products, and the second outlet (113) of the fractionating tower (11) is communicated with an inlet (21) of the first pressurizing device (2);
the second inlet (114) of the fractionating tower (11) is communicated with the outlet (32) of the first air cooling device (3), the third outlet (115) of the fractionating tower (11) is used for outputting oil phase products, the third outlet (115) of the fractionating tower (11) is communicated with the inlet (121) of the reboiler (12), and the outlet (122) of the reboiler (12) is communicated with the third inlet (116) of the fractionating tower (11).
5. A system according to any of claims 1-4, characterized in that the system further comprises a regulating valve (6);
export (32) of first air cooling device (3) with second entry (114) of fractional distillation unit (1) are through first pipeline (7) and return line (8) intercommunication, export (32) of first air cooling device (3) with entry (411) of oil phase product processing apparatus (4) are passed through first pipeline (7) and second output pipeline (92) intercommunication, install governing valve (6) on return line (8), governing valve (6) are used for adjusting fluid flow in return line (8).
6. The system of claim 5, wherein the system further comprises a temperature sensor (10);
the temperature sensor (10) is mounted on the first line (7), the temperature sensor (10) being for detecting a temperature of a fluid in the first line (7).
7. A system according to any of claims 1-4, characterized in that the system further comprises a second air cooling means (13);
the inlet (131) of the second air cooling device (13) is communicated with the first outlet (112) of the fractionation device (1).
8. The system of claim 7, further comprising a flow diversion device (14);
the outlet (132) of the second air cooling device (13) is communicated with the inlet (141) of the flow dividing device (14), the first outlet (142) of the flow dividing device (14) is used for outputting combustible gas, the second outlet (143) of the flow dividing device (14) is used for outputting acid water, and the third outlet (144) of the flow dividing device (14) is used for outputting crude naphtha.
9. The system according to claim 8, characterized in that it further comprises second pressurizing means (15);
the inlet (151) of the second pressurizing means (15) communicates with the third outlet (144) of the flow dividing means (14).
10. The system according to claim 7, characterized in that it further comprises a water injection device (16);
the first outlet (112) of the fractionation device (1) is communicated with the inlet (131) of the second air cooling device (13) through a second pipeline (17), the outlet (161) of the water injection device (16) is communicated with the second pipeline (17), and the inlet (162) of the water injection device (16) is used for injecting water.
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| CN202010434333.0A CN113698955A (en) | 2020-05-21 | 2020-05-21 | Aviation kerosene hydrogenation reaction product treatment system |
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