CN113897213A - Grading separation device and process method for independently processing condensate oil - Google Patents

Grading separation device and process method for independently processing condensate oil Download PDF

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Publication number
CN113897213A
CN113897213A CN202111346467.8A CN202111346467A CN113897213A CN 113897213 A CN113897213 A CN 113897213A CN 202111346467 A CN202111346467 A CN 202111346467A CN 113897213 A CN113897213 A CN 113897213A
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China
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separation tower
carbon
component
outlet
naphtha
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张森
李克昌
蔡勇昆
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Fujian Fuhaichuang Petrochemical Co ltd
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Fujian Fuhaichuang Petrochemical Co ltd
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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

Abstract

The invention relates to the technical field of petrochemical industry, in particular to a grading separation device for independently processing condensate oil, which comprises a carbon five-component separation tower, wherein a gas phase outlet at the top of the carbon five-component separation tower is connected with a feed inlet of a debutanizer, an oil phase outlet at the bottom of the carbon five-component separation tower is connected with a feed inlet of a heavy naphtha separation tower, a gas phase outlet at the top of the heavy naphtha separation tower is connected with a feed inlet of a light naphtha separation tower, and the carbon five-component separation tower, the debutanizer, the heavy naphtha separation tower and the light naphtha separation tower are all connected with a light hydrocarbon recovery system. The technical scheme of the invention adopts the fractionating tower to cut the five carbon components, and the condensate oil is treated by respectively fractionating the light components and the heavy components, so that the condensate oil is separately processed, and the invention has the advantages of short treatment flow, high operation precision, low energy consumption and less investment.

Description

Grading separation device and process method for independently processing condensate oil
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a fractionation device and a process method for independently processing condensate oil.
Background
The condensate oil is a liquid phase component condensed from natural gas of a condensate gas field, the main component of the condensate oil is a mixture of C5-C8 hydrocarbons, the fraction of the condensate oil is mostly at 20-200 ℃, the specific gravity is less than 0.78, the condensate oil has the characteristics of light specific gravity and high light component content compared with crude oil, at present, more than 12200 condensate gas fields are found all over the world, the condensate oil production places in China are mainly distributed in Xinjiang oil fields, China Central plains oil fields, east China sea oil fields and the like, particularly Tarim oil fields in Xinjiang, the condensate oil storage accounts for 80% of the total storage capacity of the whole country, and the yield of the condensate oil is continuously increased along with the rapid development of the natural gas industry.
However, at present, no device for specially processing condensate oil exists in China, the existing device for separating condensate oil is obtained by modifying an atmospheric and vacuum distillation tower, most functions of the atmospheric and vacuum distillation tower are in treatment of heavy oil, the condensate oil cannot be separately treated by the atmospheric and vacuum distillation tower, the condensate oil can only be mixed with crude oil, but a large amount of light components enable the condensate oil to be volatile in the mixing process, so that the loss is too large, and the separation capability and the pump performance of a tray can be influenced after the light components are volatilized, and the environment can be polluted.
Disclosure of Invention
The first purpose of the invention is to provide a fractional separation device for independently processing condensate oil, which solves the problems of difficult processing and recovery, environmental protection and the like caused by the volatile light components of the condensate oil, realizes the independent processing of the condensate oil, and has the advantages of short processing flow, high operation precision, low energy consumption and less investment; a second object of the present invention is to provide a process for the separate processing of condensate.
The invention provides a fractionation device for independently processing condensate oil, which comprises a fractionation system and a light hydrocarbon recovery system, wherein the fractionation system comprises a carbon five-component separation tower, a gas phase outlet at the top of the carbon five-component separation tower is sequentially connected with a carbon five-component separation tower cooling device and a carbon five-component separation tower reflux tank, and a liquid phase outlet at the bottom of the carbon five-component separation tower reflux tank is connected with a feed inlet of a debutanizer;
a gas phase outlet at the top of the debutanizer is sequentially connected with a debutanizer cooling device and a debutanizer reflux tank, a liquefied gas outlet is arranged at the bottom of the debutanizer reflux tank, and a first carbon five component outlet is arranged at the bottom of the debutanizer;
an oil phase outlet at the bottom of the carbon five-component separation tower is connected with a feed inlet of a heavy naphtha separation tower, a gas phase outlet at the top of the heavy naphtha separation tower is sequentially connected with a cooling device of the heavy naphtha separation tower and a reflux tank of the heavy naphtha separation tower, a liquid phase outlet at the bottom of the reflux tank of the heavy naphtha separation tower is connected with a feed inlet of a light naphtha separation tower, and a diesel component outlet is arranged at the bottom of the heavy naphtha separation tower;
a gas phase outlet at the top of the light naphtha separation tower is sequentially connected with a light naphtha separation tower cooling device and a light naphtha separation tower reflux tank, a second carbon five-component outlet is arranged at the bottom of the light naphtha separation tower reflux tank, a light naphtha outlet is arranged on the side wall of the light naphtha separation tower, and a heavy naphtha outlet is arranged at the bottom of the light naphtha separation tower;
and the gas phase outlet at the top of the reflux tank of the carbon five-component separation tower, the gas phase outlet at the top of the reflux tank of the debutanizer, the gas phase outlet at the top of the reflux tank of the heavy naphtha separation tower and the heavy naphtha outlet are all connected with the light hydrocarbon recovery system.
The distillation principle of a fractionating tower in a fractionation system is the same, a tower bottom heating device is adopted to provide heat for the fractionating tower to vaporize materials at the tower bottom, oil gas rises along the tower, liquid at the upper part of the fractionating tower falls along the tower, the gas-liquid two phases are in countercurrent contact, during the two-phase contact, volatile (low boiling point) components in descending liquid are continuously transferred into steam, difficultly volatile (high boiling point) components in the steam are continuously transferred into the descending liquid, a tower section above a feed inlet of the fractionating tower is further concentrated for the volatile components in the ascending steam, the tower section is called a rectification section, the concentration of the volatile components at the tower top is higher the closer the steam is, the volatile components below the feed inlet of the fractionating tower are extracted from the descending liquid, the tower section is called a stripping section, the concentration of the difficultly volatile components at the tower bottom of the descending liquid is higher the closer the descending liquid is, the rectification section is combined with the stripping section, so that two components in a liquid mixture are completely separated, the purpose of component separation is achieved.
The fractionating system further comprises a deethanizer, a liquid phase outlet at the bottom of the reflux tank of the carbon five-component separation tower is connected with a feed inlet of the deethanizer, a corrosion inhibitor injection port of the deethanizer is arranged at the top of the deethanizer, a gas phase outlet at the top of the deethanizer is sequentially connected with a deethanizer cooling device and a deethanizer reflux tank, a first fuel gas outlet is arranged at the bottom of the deethanizer reflux tank, and the first fuel gas outlet is connected with a reflux port of the deethanizer;
the tower bottom of the deethanizer is provided with a deethanizer reboiler, an oil phase outlet at the bottom of the deethanizer is respectively connected with an inlet of the deethanizer reboiler and a feed inlet of the debutanizer, and an outlet of the deethanizer reboiler is connected with a reboiling liquid inlet of the deethanizer.
If the content of the fuel gas in the liquid phase material separated by the reflux tank of the carbon five-component separation tower is high, feeding the separated liquid phase material into a deethanizer for rectification, distilling the fuel gas by the deethanizer, and then feeding the fuel gas into a debutanizer for rectification; if the content of the fuel gas in the liquid phase material separated by the reflux tank of the carbon five-component separation tower is smaller, directly feeding the separated liquid phase material into a debutanizer for rectification.
Further, the light hydrocarbon recovery system comprises a light hydrocarbon absorption tower and an amine liquid absorption tower, a gas phase outlet at the top of the return tank of the five-carbon component separation tower, a gas phase outlet at the top of the return tank of the debutanizer, a gas phase outlet at the top of the return tank of the deethanizer, a gas phase outlet at the top of the return tank of the heavy naphtha separation tower and a heavy naphtha outlet are all connected with a feed inlet of the light hydrocarbon absorption tower, a gas phase outlet at the top of the light hydrocarbon absorption tower is connected with a feed inlet of the amine liquid absorption tower, and an absorption-rich oil outlet at the bottom of the light hydrocarbon absorption tower is connected with a feed inlet of the five-carbon component separation tower;
and a liquid phase outlet at the bottom of the amine liquid absorption tower is connected with an inlet of a sulfur recovery system, an outlet of the sulfur recovery system is connected with an alkali liquor inlet of the amine liquid absorption tower, and a second fuel gas outlet is arranged at the top of the amine liquid absorption tower.
The noncondensable gases separated from the reflux tanks of the carbon five-component separation tower, the debutanizer reflux tank, the deethanizer reflux tank and the heavy naphtha separation tower respectively enter a light hydrocarbon absorption tower, and heavy naphtha generated at the bottom of the light naphtha separation tower is sent to the light hydrocarbon absorption tower to be absorbedThe tower is used as an absorbent, heavy naphtha is contacted with the non-condensable gas in the light hydrocarbon absorption tower to absorb macromolecular hydrocarbons carried in the non-condensable gas, after the absorption process is finished, the non-condensable gas is sent to the amine liquid absorption tower, after the non-condensable gas enters the amine liquid absorption tower, the non-condensable gas is subjected to amine washing by lean amine liquid to remove hydrogen sulfide in the non-condensable gas, the non-condensable gas after the amine washing is subjected to alkali washing by NaOH to convert mercaptan in the non-condensable gas into sodium mercaptan and water, so that the content of the mercaptan in the non-condensable gas is lower than 343mg/Nm3And the non-condensable gas after desulfurization treatment is taken as a fuel gas product to be output, the generated sodium mercaptan and water enter a sulfur recovery system together with NaOH, air is introduced into the sulfur recovery system to reduce the sodium mercaptan into NaOH and disulfide under the action of a methyldiethanolamine catalyst in a sulfur recovery unit, and the generated NaOH returns to an amine liquid absorption tower to continue the alkali washing reaction.
Further, the cooling device of the carbon five-component separation tower comprises a heat exchanger of the carbon five-component separation tower and an air cooler of the carbon five-component separation tower, the cooling device of the deethanizer comprises a heat exchanger of the deethanizer and an air cooler of the deethanizer, an outlet of the heat exchanger of the carbon five-component separation tower is connected with an inlet of the heat exchanger of the deethanizer, an outlet of the heat exchanger of the deethanizer is connected with a feed inlet of the carbon five-component separation tower, and an inlet of the heat exchanger of the carbon five-component separation tower is connected with the pretreatment system;
the pretreatment system comprises an electric desalting system, a demercuration system and a hydrogenation reaction system which are sequentially connected, and an outlet of the hydrogenation reaction system is connected with an inlet of the heat exchanger of the carbon five-component separation tower.
The condensate oil is subjected to primary heat exchange by a heat source in an electric desalting system, mixed with water and a demulsifier, and then enters a primary electric desalting tank to remove most of salt contained in the condensate oil, an electric field is applied to the condensate oil subjected to primary desalting for secondary electric desalting, so that the salt content in the condensate oil is less than 3mgNaCl/L, the electric desalting system is adopted to remove impurities such as salt, water, oil sludge and the like in the condensate oil, the optimal desalting effect is achieved by controlling parameters such as the feeding temperature, the water injection amount, the demulsifying injection amount, the electric field intensity, the mixing intensity and the like of the electric desalting system, and qualified feeding is provided for a fractionation system.
The method comprises the steps of further optimizing desalted condensate oil by using a demercuration system, enabling the desalted condensate oil to enter the demercuration system after heat exchange and cooling, enabling the condensate oil to have hydrogenolysis reaction by adding a hydrogenolysis catalyst under the condition of hydrogen so as to reduce organic mercury carried in the condensate oil, converting the organic mercury into adsorbable inorganic mercury, and then adsorbing the inorganic mercury in a physical adsorption and filtration mode so as to achieve the purpose of demercuration, so that the mercury content in the condensate oil is less than 5ppb, and enabling the condensate oil to reach the condition of entering a downstream device by controlling parameters such as the operating temperature, the operating pressure, the operating flow, the hydrogen-hydrocarbon ratio and the like of the demercuration system.
The hydrogenation reaction system is adopted to carry out desulfurization and sweetening treatment on the condensate oil after demercuration, the condensate oil is prevented from corroding equipment, the pretreated condensate oil enters the carbon five-component separation tower after being subjected to heat exchange through the carbon five-component separation tower heat exchanger and the deethanizer heat exchanger to 155-180 ℃, and the operation energy consumption of the fractionation system can be effectively reduced.
Further, a corrosion inhibitor injection port of the carbon five-component separation tower is arranged at the top of the carbon five-component separation tower, and a liquid phase outlet at the bottom of a reflux tank of the carbon five-component separation tower is connected with a reflux port of the carbon five-component separation tower;
a carbon five-component separation tower reboiler heating furnace is arranged at the tower bottom of the carbon five-component separation tower, an oil phase outlet at the bottom of the carbon five-component separation tower is connected with an inlet of the carbon five-component separation tower reboiler heating furnace, and an outlet of the carbon five-component separation tower reboiler heating furnace is connected with a reboiler liquid inlet of the carbon five-component separation tower;
the tower top of the debutanizer is provided with a debutanizer corrosion inhibitor injection port, the debutanizer cooling device comprises a debutanizer condenser, and the liquefied gas outlet is connected with the reflux port of the debutanizer;
the tower bottom of the debutanizer is provided with a debutanizer reboiler, the first carbon five-component outlet is connected with the inlet of the debutanizer reboiler, and the outlet of the debutanizer reboiler is connected with the reboiled liquid inlet of the debutanizer.
The device adopts the reboiler heating furnace of the carbon five-component separation tower to provide heat for the carbon five-component separation tower, the carbon five-component separation tower is the first tower for condensate oil feeding, the heat load requirement is high, therefore, the reboiler heating furnace of the carbon five-component separation tower is adopted for heating, an air preheating system is arranged to reduce the exhaust gas temperature, the heating efficiency is improved, the operation energy consumption of the carbon five-component separation tower is reduced, the heat load required by the debutanizer is small, therefore, the reboiler of the debutanizer is adopted for heating, and the operation energy consumption of the grading separation device can be effectively reduced.
Further, a corrosion inhibitor injection port of the heavy naphtha separation tower is arranged at the top of the heavy naphtha separation tower, the cooling device of the heavy naphtha separation tower comprises a condenser of the heavy naphtha separation tower, and a liquid phase outlet at the bottom of the reflux tank of the heavy naphtha separation tower is connected with a reflux port of the heavy naphtha separation tower;
a heavy naphtha separation tower reboiler heating furnace is arranged at the bottom of the heavy naphtha separation tower, the diesel component outlet is connected with an inlet of the heavy naphtha separation tower reboiler heating furnace, and an outlet of the heavy naphtha separation tower reboiler heating furnace is connected with a heavy boiling liquid inlet of the heavy naphtha separation tower;
the top of the light naphtha separation tower is provided with a light naphtha separation tower corrosion inhibitor injection port, the light naphtha separation tower cooling device comprises a light naphtha separation tower condenser, and the second carbon five component outlet is connected with a reflux port of the light naphtha separation tower;
the bottom of the light naphtha separation tower is provided with a light naphtha separation tower reboiler, the heavy naphtha outlet is connected with the inlet of the light naphtha separation tower reboiler, and the outlet of the light naphtha separation tower reboiler is connected with the heavy boiling liquid inlet of the light naphtha separation tower.
Adopt heavy naphtha knockout tower reboiler heating furnace to provide the heat for heavy naphtha knockout tower, heavy component content is higher in the feeding of heavy naphtha knockout tower, required heat load is great, consequently, adopt heavy naphtha knockout tower reboiler heating furnace to heat, and set up air preheating system and reduce exhaust gas temperature, improve the heating efficiency of heavy naphtha knockout tower reboiler heating furnace, and the required heat load of light naphtha knockout tower is less, consequently, adopt light naphtha knockout tower reboiler to heat, different heating device is selected to the heat load demand of difference to this application, and is more economical and convenient.
The tower top of the fractionating tower is provided with a corrosion inhibitor filling opening, the liquefied gas component and the fuel gas component both contain hydrogen sulfide medium, wet hydrogen sulfide in oil gas at the tower top can corrode equipment and pipelines at the tower top of the fractionating tower, and corrosion is prevented by injecting a corrosion inhibitor at the tower top.
Further, the liquefied gas outlet is connected with a liquefied gas desulfurization system, and a liquefied gas air cooler and a liquefied gas water circulating cooler are arranged between the liquefied gas outlet and the liquefied gas desulfurization system;
the first carbon five component outlet and the second carbon five component outlet are connected with a carbon five component tank area through a debutanizer discharge pump, and a carbon five component air cooler and a carbon five component water distribution circulating cooler are arranged between the debutanizer discharge pump and the carbon five component tank area;
the light naphtha outlet is connected with a light naphtha tank zone, and a light naphtha air cooler and a light naphtha water circulating cooler are arranged between the light naphtha outlet and the light naphtha tank zone;
the heavy naphtha outlet is connected with a heavy naphtha tank area, and a heavy naphtha air cooler and a heavy naphtha water circulating cooler are arranged between the heavy naphtha outlet and the heavy naphtha tank area;
the diesel component outlet is connected with a diesel component tank area, and a diesel component air cooler and a diesel component water circulating cooler are arranged between the diesel component outlet and the diesel component tank area;
the first fuel gas outlet is connected with a first fuel gas pipe network, and the second fuel gas outlet is connected with a second fuel gas pipe network.
The liquefied gas desulfurization system is divided into a desulfurization unit and an alkali liquor regeneration unit, the desulfurization unit is used for carrying out desulfurization treatment on the rectified liquefied gas, the working principle of the desulfurization unit is the same as that of an amine liquid absorption tower, firstly, lean amine liquid is used for carrying out amine elution on the liquefied gas to remove hydrogen sulfide in the liquefied gas, the liquefied gas after the amine washing is subjected to alkali washing by NaOH, mercaptan in the liquefied gas is converted into sodium mercaptan and water, the content of the mercaptan in the liquefied gas is lower than 343mg/Nm3, the desulfurized liquefied gas is output as a liquefied gas product, the working principle of the alkali liquor regeneration unit is the same as that of a sulfur recovery system, the sodium mercaptan, the water and the NaOH generated by the desulfurization unit enter the alkali liquor regeneration unit together, air is introduced under the action of a methyl diethanolamine catalyst to reduce the sodium mercaptan into NaOH and a disulfide, and the generated NaOH returns to the desulfurization unit to continue alkali washing reaction.
The liquefied gas, the five components in carbon, light naphtha, heavy naphtha and diesel oil components etc. product need cool off to below 45 ℃ and just can advance the jar, and this application combines together air cooler and circulating water cooler, both can cool off the product to below 45 ℃, and the energy consumption is lower simultaneously, can effectively reduce fractionation system's running cost.
The invention provides a process method for independently processing condensate oil, which comprises the following steps:
s1, sending condensate oil to a carbon five-component separation tower for rectification, condensing oil gas at the top of the carbon five-component separation tower through a cooling device of the carbon five-component separation tower, then, sending the condensed oil gas into a reflux tank of the carbon five-component separation tower for separation, sending separated uncondensed gas to a light hydrocarbon recovery system for recovery, taking separated liquid-phase materials as feeding materials of a debutanizer, and taking heavy components at the bottom of the carbon five-component separation tower as feeding materials of a heavy naphtha separation tower;
s2, sending the liquid phase material separated in the step S1 to a debutanizer for rectification, condensing oil gas at the top of the debutanizer from a debutanizer cooling device, then sending the condensed oil gas into a debutanizer reflux tank for separation, sending the separated uncondensed gas to a light hydrocarbon recovery system for recovery, discharging the separated liquefied gas from a liquefied gas outlet, and discharging the carbon five component at the bottom of the debutanizer from a first carbon five component outlet;
s3, the heavy naphtha separation tower is used for rectifying the recombination at the bottom of the five-carbon component separation tower in the step S1, oil gas at the top of the heavy naphtha separation tower is condensed by a heavy naphtha separation tower cooling device and then enters a heavy naphtha separation tower reflux tank for separation, the separated uncondensed gas is sent to the light hydrocarbon recovery system for recovery, the separated mixed naphtha is used as a feeding hole of the light naphtha separation tower, and the diesel component at the bottom of the heavy naphtha separation tower is discharged from a diesel component outlet;
s4, sending the mixed naphtha separated in the step S3 to the light naphtha separation tower for rectification, condensing the carbon five components at the top of the light naphtha separation tower through a cooling device of the light naphtha separation tower, then entering a reflux tank of the light naphtha separation tower, and discharging from a second carbon five component outlet, discharging light naphtha in the light naphtha separation tower from a light naphtha outlet, sending one part of heavy naphtha at the bottom of the light naphtha separation tower to the light naphtha recovery system as an absorbent, and discharging the other part of heavy naphtha from the heavy naphtha outlet;
s5, noncondensable gas separated by the carbon five-component separation tower reflux tank, the debutanizer reflux tank and the heavy naphtha separation tower reflux tank is respectively sent to the light hydrocarbon recovery system for mixing, and heavy naphtha at the bottom of the light naphtha separation tower is sent to the light hydrocarbon recovery system and then is contacted with the noncondensable gas to absorb macromolecular hydrocarbons carried in the noncondensable gas.
Further, the process method for treating the condensate oil comprises the following steps:
s1, sending condensate oil to a carbon five-component separation tower for rectification, condensing oil gas at the top of the carbon five-component separation tower through a cooling device of the carbon five-component separation tower, then, sending the condensed oil gas into a reflux tank of the carbon five-component separation tower for separation, sending separated uncondensed gas to a light hydrocarbon recovery system for recovery, taking separated liquid-phase materials as feeding materials of a deethanizer, and taking heavy components at the bottom of the carbon five-component separation tower as feeding materials of a heavy naphtha separation tower;
s2, sending the liquid-phase material separated in the step S1 to the deethanizer for rectification, condensing oil gas at the top of the deethanizer through the deethanizer, then sending the condensed oil gas into a reflux tank of the deethanizer for separation, sending the separated uncondensed gas to the light hydrocarbon recovery system for recovery, discharging the separated fuel gas from the first fuel gas outlet, and taking the carbon five component and the liquefied gas component at the bottom of the deethanizer as the feeding materials of the debutanizer;
s3, sending the carbon five component and the liquefied gas component at the bottom of the deethanizer in the step S2 to the debutanizer for rectification, condensing oil gas at the top of the debutanizer from a debutanizer cooling device, then sending the condensed oil gas into a debutanizer reflux tank for separation, sending the separated uncondensed gas to a light hydrocarbon recovery system for recovery, discharging the separated liquefied gas from a liquefied gas outlet, and discharging the carbon five component at the bottom of the debutanizer from a first carbon five component outlet;
s4, the heavy naphtha separation tower is used for rectifying the recombination at the bottom of the carbon five-component separation tower in the step S1, oil gas at the top of the heavy naphtha separation tower is condensed by the heavy naphtha separation tower cooling device and then enters the heavy naphtha separation tower reflux tank for separation, the separated non-condensable gas is sent to the light hydrocarbon recovery system for recovery, the separated mixed naphtha is used as the feeding port of the light naphtha separation tower, and the diesel component at the bottom of the heavy naphtha separation tower is discharged from the diesel component outlet;
s5, sending the mixed naphtha separated in the step S4 to the light naphtha separation tower for rectification, wherein the carbon five components at the top of the light naphtha separation tower are condensed by the condenser of the light naphtha separation tower and then enter the reflux tank of the light naphtha separation tower to be discharged from the second carbon five component outlet, the light naphtha in the light naphtha separation tower is discharged from the light naphtha outlet, the heavy naphtha at the bottom of the light naphtha separation tower is sent from one part to the light naphtha recovery system to be used as an absorbent, and the other part is discharged from the heavy naphtha outlet;
s6, noncondensable gas that five component separation tower reflux drum of carbon, deethanizer reflux drum, debutanizer reflux drum and heavy naphtha knockout drum reflux drum separated sends respectively to the light dydrocarbon recovery system mixes, heavy naphtha in light naphtha knockout drum bottom send to contact with noncondensable gas behind the light dydrocarbon recovery system in order to absorb the macromolecular hydrocarbons that carry in the noncondensable gas.
Further, in step S6, the non-condensable gas in the light hydrocarbon recovery system is desulfurized after absorbing the macromolecular hydrocarbons with heavy naphtha, and the desulfurized non-condensable gas is produced as a fuel gas product.
The invention has the beneficial effects that:
(1) the technical scheme of the invention adopts the fractionating tower to cut the five carbon components, and the light and heavy components are respectively rectified in a grading manner to treat the condensate oil, so that the condensate oil is independently processed, the problems of difficult processing and recovery, environmental protection and the like caused by the volatile light components of the condensate oil are solved, and the invention has the advantages of short processing flow, high operation precision, low energy consumption and less investment.
(2) The technical scheme of the invention is provided with a light hydrocarbon recovery system, noncondensable gas generated at the top of the fractionating tower is sent to the light hydrocarbon recovery system for recovery, heavy naphtha is adopted to absorb macromolecular hydrocarbons carried in the noncondensable gas and then carry out desulfurization treatment, and the noncondensable gas after desulfurization treatment is output as a fuel gas product, thereby solving the problems of difficult processing and recovery, environmental protection and the like caused by volatile light components of condensate oil.
(3) The technical scheme of the invention adopts the operation of the fractionating towers, controls the components of the five carbon components in the liquefied gas, the components of C3 and C4 in the five carbon components product, and the initial boiling point, the dry point, the flash point, the Reid vapor pressure and other quality indexes of the light naphtha, the heavy naphtha and the diesel component by controlling the operation parameters of each fractionating tower, has simple operation and high fractionation precision, and is suitable for processing most condensate oil with the dry point less than 450 ℃.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural view of a condensate fractionation apparatus according to an embodiment of the present invention;
FIG. 2 is a process flow diagram of a condensate fractionation process in an embodiment of the present invention.
Description of reference numerals:
1-electric desalting system, 2-demercuration system, 3-hydrogenation reaction system, 4-carbon five-component separation tower, 5-carbon five-component separation tower corrosion inhibitor injection opening, 6-carbon five-component separation tower heat exchanger, 7-carbon five-component separation tower air cooler, 8-carbon five-component separation tower reflux tank, 9-carbon five-component separation tower reflux pump, 10-carbon five-component separation tower reboiler heating furnace feed pump, 11-carbon five-component separation tower reboiler heating furnace, 12-carbon five-component separation tower discharge pump, 13-deethanizer, 14-deethanizer corrosion inhibitor injection opening, 15-deethanizer heat exchanger, 16-deethanizer air cooler, 17-deethanizer reflux tank, 18-first fuel gas outlet, 19-deethanizer reflux pump, 20-deethanizer discharge pump, 21-deethanizer reboiler, 22-debutanizer, 23-debutanizer corrosion inhibitor injection port, 24-debutanizer condenser, 25-debutanizer reflux tank, 26-liquefied gas outlet, 27-debutanizer reflux pump, 28-liquefied gas air cooler, 29-liquefied gas water circulating cooler, 30-liquefied gas desulfurization system, 31-first carbon five-component outlet, 32-debutanizer discharge pump, 33-debutanizer reboiler, 34-carbon five-component air cooler, 35-carbon five-component water circulating cooler, 36-carbon five-component tank zone, 37-heavy naphtha separation tower, 38-heavy naphtha separation tower corrosion inhibitor injection port, 39-heavy naphtha separation tower condenser, 40-heavy naphtha separation tower reflux tank, 41-heavy naphtha separation tower reflux pump, 42-diesel component outlet, 43-heavy naphtha separation tower reboiler heating furnace feed pump, 44-heavy naphtha reboiler heating furnace, 45-heavy naphtha separation tower discharge pump, 46-diesel component air cooler, 47-diesel component water circulation cooler, 48-diesel component tank zone, 49-light naphtha separation tower, 50-light naphtha separation tower corrosion inhibitor injection port, 51-light naphtha separation tower condenser, 52-light naphtha separation tower reflux tank, 53-second five-carbon component outlet, 54-light naphtha separation tower reflux pump, 55-light naphtha outlet, 56-light naphtha air cooler, 57-light naphtha water circulation cooler, 58-light naphtha tank zone, 59-heavy naphtha outlet, 60-light naphtha separation tower discharge pump, 61-light naphtha separation tower reboiler, 62-heavy naphtha air cooler, 63-heavy naphtha water circulation cooler, 64-heavy naphtha tank field, 65-light hydrocarbon absorption tower, 66-light hydrocarbon absorption tower discharge pump, 67-amine liquid absorption tower, 68-second fuel gas outlet, 69-first fuel gas pipe network, 70-second fuel gas pipe network, 71-sulfur recovery unit.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments, and it should be understood that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "top," "bottom," "inner," "outer," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the present invention and simplicity in description, but do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed in a particular orientation, and be operated, and thus should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, features defined as "first", "second", may explicitly or implicitly include one or more of the described features. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise. Furthermore, the terms "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Examples
A classification separation device for independently processing condensate oil is shown in figure 1 and comprises a pretreatment system, a fractionation system and a light hydrocarbon recovery system, wherein the pretreatment system comprises an electric desalting system 1, a demercuration system 2 and a hydrogenation reaction system 3 which are sequentially connected, the condensate oil is treated by the pretreatment system before entering the fractionation system, the condensate oil is subjected to primary heat exchange by an internal heat source of the electric desalting system 1, the condensate oil subjected to heat exchange is mixed with water and a demulsifier and then enters a primary electric desalting tank to remove most of salt contained in the condensate oil, an electric field is applied to the condensate oil subjected to primary desalting to perform secondary electric desalting to ensure that the salt content in the condensate oil is less than 3mgNaCl/L, impurities such as salt, water, grease and the like in the condensate oil are removed by the electric desalting system 1, and qualified feeding is provided for the fractionation system; the condensed oil after desalination is further optimized by adopting a demercuration system 2, after the condensed oil enters the demercuration system 2, the condensed oil is subjected to hydrogenolysis reaction by adopting a hydrogenolysis catalyst under the condition of hydrogen so as to reduce organic mercury carried in the condensed oil, the organic mercury is converted into adsorbable inorganic mercury, and then the inorganic mercury is adsorbed by a physical adsorption filtration mode so as to achieve the purpose of demercuration, so that the mercury content in the condensed oil is less than 5 ppb; and the condensate oil after demercuration is subjected to desulfurization and demercaptanization treatment by adopting a hydrogenation reaction system 3, so that the condensate oil is prevented from corroding equipment, the condensate oil after pretreatment enters a fractionation system to be separated from five carbon components, and light components and heavy components are fractionated and rectified respectively.
The fractionation system comprises a carbon five-component separation tower 4, a gas phase outlet at the top of the carbon five-component separation tower 4 is sequentially connected with a carbon five-component separation tower heat exchanger 6, a carbon five-component separation tower air cooler 7 and a carbon five-component separation tower reflux tank 8, an inlet of the carbon five-component separation tower heat exchanger 6 is connected with an outlet of the hydrogenation reaction system 3, an outlet of the carbon five-component separation tower heat exchanger 6 is connected with an inlet of a deethanizer heat exchanger 15, an outlet of the deethanizer heat exchanger 15 is connected with a feed inlet of the carbon five-component separation tower 4, and pretreated condensate oil enters the carbon five-component separation tower 4 from the feed inlet of the carbon five-component separation tower 4 for rectification after being subjected to heat exchange to 155-180 ℃ by the carbon five-component separation tower heat exchanger 6 and the deethanizer heat exchanger 15.
A carbon five-component separation tower reboiler heating furnace 11 is arranged at the bottom of the carbon five-component separation tower 4, the carbon five-component separation tower reboiler heating furnace 11 is adopted to provide heat for the carbon five-component separation tower 4 to vaporize condensate at the bottom of the tower, oil gas at the top of the carbon five-component separation tower 4 enters a carbon five-component separation tower reflux tank 8 for separation after heat exchange and condensation through a carbon five-component separation tower heat exchanger 6 and a carbon five-component separation tower air cooler 7, a gas phase outlet at the top of the carbon five-component separation tower reflux tank 8 is connected with a light hydrocarbon recovery system, a liquid phase outlet at the bottom of the carbon five-component separation tower reflux tank 8 is connected with a carbon five-component separation tower reflux pump 9, the carbon five-component separation tower reflux pump 9 is connected with a reflux port of the carbon five-component separation tower 4, non-condensed gas separated from the carbon five-component separation tower reflux tank 8 is sent to the light hydrocarbon recovery system for recovery, and a separated liquid phase material part enters the carbon five-component separation tower 4 from the reflux port of the carbon five-component separation tower 4, descending the column as overhead reflux.
The carbon five component separation tower reflux pump 9 is also respectively connected with a feed inlet of a deethanizer 13 and a feed inlet of a debutanizer 22, if the content of fuel gas in the separated liquid phase material is high, the carbon five component separation tower reflux pump 9 feeds the residual liquid phase material into the deethanizer 13 from the feed inlet of the deethanizer 13 for rectification, a deethanizer reboiler 21 is arranged at the tower bottom of the deethanizer 13, a deethanizer heat exchanger 15, a deethanizer air cooler 16 and a deethanizer reflux tank 17 are sequentially connected with a gas phase outlet at the top of the deethanizer reflux tank 13, the gas phase outlet at the top of the deethanizer reflux tank 17 is connected with a light hydrocarbon recovery system, a first fuel gas outlet 18 is arranged at the bottom of the deethanizer reflux tank 17, the first fuel gas outlet 18 is connected with a deethanizer reflux pump 19, and the deethanizer reflux pump 19 is respectively connected with a reflux port of the deethanizer 13 and a first fuel gas pipe network 69. A deethanizer reboiler 21 is adopted to provide heat for a deethanizer 13 to vaporize liquid phase materials at the bottom of the deethanizer, oil gas at the top of the deethanizer 13 enters a deethanizer reflux tank 17 for separation after being subjected to heat exchange and condensation through a deethanizer heat exchanger 15 and a deethanizer air cooler 16, separated uncondensed gas is sent to a light hydrocarbon recovery system for recovery, separated fuel gas is discharged from a first fuel gas outlet 18 and is divided into two parts by a deethanizer reflux pump 19, one part enters the deethanizer 4 from a reflux port of the deethanizer 4 to descend along the tower as top reflux, and the other part is sent to a first fuel gas pipe network 69 as a fuel gas product.
An oil phase outlet at the bottom of the deethanizer 13 is connected with a deethanizer discharge pump 20, the deethanizer discharge pump 20 is respectively connected with feed inlets of a deethanizer reboiler 21 and a debutanizer 22, the deethanizer reboiler 21 is connected with a reboiling liquid inlet of the deethanizer 13, liquefied gas and carbon five components at the bottom of the deethanizer 13 are divided into two parts by the deethanizer discharge pump 20, one part is heated by the deethanizer reboiler 21 and then returns to the deethanizer 13, and the other part is used as feed of the debutanizer 22 and enters the debutanizer 22 from the feed inlet of the debutanizer 22 for rectification.
If the content of the fuel gas in the liquid phase material separated by the reflux tank 8 of the carbon five-component separation tower is less, the liquid phase material can be directly sent to the debutanizer 22 for rectification.
The tower bottom of debutanizer tower 22 is equipped with debutanizer tower reboiler 33, the gaseous phase export at debutanizer tower 22 top has connected gradually debutanizer tower condenser 24 and debutanizer tower reflux drum 25, the gaseous phase export and the light hydrocarbon recovery system at debutanizer tower reflux drum 25 top are connected, the bottom of debutanizer tower reflux drum 25 is equipped with liquefied gas export 26, liquefied gas export 26 is connected with liquefied gas desulfurization system 30, be equipped with liquefied gas air cooler 28 and liquefied gas water circulative cooling ware 29 between liquefied gas export 26 and liquefied gas desulfurization system 30. A debutanizer reboiler 33 is adopted to provide heat for the debutanizer 22 to enable liquefied gas and carbon five components at the bottom of the debutanizer to be vaporized, oil gas at the top of the debutanizer 22 is condensed by a debutanizer condenser 24 and then enters a debutanizer reflux tank 25 for separation, separated noncondensable gas enters a light hydrocarbon recovery system for recovery, and separated liquefied gas is cooled to below 45 ℃ by a liquefied gas air cooler 28 and a liquefied gas water circulating cooler 29 and then enters a liquefied gas desulfurization system 30.
The liquefied gas desulfurization system 30 is divided into a desulfurization unit and an alkali liquor regeneration unit, the desulfurization unit is used for desulfurization treatment of the rectified liquefied gas, firstly lean amine liquid is used for amine elution of the liquefied gas to remove hydrogen sulfide in the liquefied gas, and the liquefied gas is subjected to amine washingThe liquefied gas is subjected to alkali washing by NaOH to convert mercaptan in the liquefied gas into sodium mercaptan and water, so that the content of the mercaptan in the liquefied gas is lower than 343mg/Nm3The desulfurized liquefied gas is produced as a liquefied gas product, the generated sodium mercaptide and water enter an alkali liquor regeneration unit together with NaOH, air is introduced under the action of a methyldiethanolamine catalyst to reduce the sodium mercaptide into NaOH and disulfide, and the generated NaOH returns to the desulfurization unit to continue to carry out an alkali washing reaction.
The bottom of the debutanizer 22 is provided with a first carbon five-component outlet 31, the first carbon five-component outlet 31 is connected with a debutanizer discharge pump 32, the debutanizer discharge pump 32 is respectively connected with a debutanizer reboiler 33 and a carbon five-component tank area 36, the debutanizer reboiler 33 is connected with a reboiling liquid inlet of the debutanizer 22, and a carbon five-component air cooler 34 and a carbon five-component water-division circulating cooler 35 are arranged between the debutanizer discharge pump 32 and the carbon five-component tank area 36. The carbon five-component at the bottom of the debutanizer 22 is divided into two parts by a debutanizer discharge pump 32, one part is heated by a debutanizer reboiler 33 and then returned to the debutanizer 22, and the other part is cooled to below 45 ℃ by a carbon five-component air cooler 34 and a carbon five-component water division circulating cooler 35 and then sent to a carbon five-component tank area 36 to be output as a carbon five-component product.
An oil phase outlet at the bottom of the carbon five-component separation tower 4 is respectively connected with a feeding pump 10 of a reboiler heating furnace of the carbon five-component separation tower and a discharging pump 12 of the carbon five-component separation tower, the feeding pump 10 of the reboiler heating furnace of the carbon five-component separation tower is connected with a reboiler heating furnace 11 of the carbon five-component separation tower, the reboiler heating furnace 11 of the carbon five-component separation tower is connected with a reboiler inlet of the carbon five-component separation tower 4, and the discharging pump 12 of the carbon five-component separation tower is connected with a feeding port of a heavy naphtha separation tower 37. Heavy components at the bottom of the carbon five-component separation tower 4 are divided into two parts, one part is heated by a reboiler heating furnace 11 of the carbon five-component separation tower and then returns to the carbon five-component separation tower 4, and the other part is used as feed of a heavy naphtha separation tower 37 and enters the heavy naphtha separation tower 37 from a feed inlet of the heavy naphtha separation tower 37 for rectification.
The bottom of the heavy naphtha separation tower 37 is provided with a heavy naphtha separation tower reboiler heating furnace 44, the gas phase outlet at the top of the heavy naphtha separation tower 37 is sequentially connected with a heavy naphtha separation tower condenser 39 and a heavy naphtha separation tower reflux tank 40, the gas phase outlet at the top of the heavy naphtha separation tower reflux tank 40 is connected with a light hydrocarbon recovery system, the liquid phase outlet at the bottom of the heavy naphtha separation tower reflux tank 40 is connected with a heavy naphtha separation tower reflux pump 41, and the heavy naphtha separation tower reflux pump 41 is respectively connected with the reflux port of the heavy naphtha separation tower 37 and the feed inlet of a light naphtha separation tower 49. A heavy naphtha separation tower reboiler heating furnace 44 is adopted to provide heat for the heavy naphtha separation tower 37 to vaporize mixed naphtha at the bottom of the tower, oil gas at the top of the heavy naphtha separation tower 37 is condensed by a heavy naphtha separation tower condenser 39 and then enters a heavy naphtha separation tower reflux tank 40 to be separated, separated uncondensed gas is sent to a light hydrocarbon recovery system to be recovered, the separated mixed naphtha is divided into two parts by a heavy naphtha separation tower reflux pump 41, one part enters the heavy naphtha separation tower 37 from a reflux port of the heavy naphtha separation tower 37 to be used as top reflux to descend along the tower, the other part is used as feeding of a light naphtha separation tower 49, and the feeding of the light naphtha separation tower 49 is rectified by a feeding port of the light naphtha separation tower 49.
A light naphtha separation tower reboiler 61 is arranged at the bottom of the light naphtha separation tower 49, a light naphtha separation tower condenser 51 and a light naphtha separation tower reflux tank 52 are sequentially connected to a liquid phase outlet at the top of the light naphtha separation tower 49, a second carbon five-component outlet 53 is arranged at the bottom of the light naphtha separation tower reflux tank 52, the second carbon five-component outlet 53 is connected with a light naphtha separation tower reflux pump 54, and the light naphtha separation tower reflux pump 54 is respectively connected with a reflux port of the light naphtha separation tower 49 and a debutanizer reflux pump 27. A light naphtha separation tower reboiler 61 is adopted to provide heat for a light naphtha separation tower 49, the carbon five-component at the top of the light naphtha separation tower 49 is condensed by a light naphtha separation tower condenser 51 and then enters a light naphtha separation tower reflux tank 52, the carbon five-component is discharged from a second carbon five-component outlet 53, a light naphtha separation tower reflux pump 54 divides the carbon five-component discharged from the second carbon five-component outlet 53 into two parts, one part enters the light naphtha separation tower 49 from a reflux port of the light naphtha separation tower 49 and descends along the tower as tower top reflux, the other part and the carbon five-component discharged from a first carbon five-component outlet 31 are combined and then cooled to below 45 ℃ by a carbon five-component air cooler 34 and a carbon five-component water separation circulating cooler and then are sent to a carbon five-component tank area 36 to be used as a carbon five-component product.
A light naphtha outlet 55 is formed in the side wall of the light naphtha separation tower 49, the light naphtha outlet 55 is connected with a light naphtha tank area 58, and a light naphtha air cooler 56 and a light naphtha water circulation cooler 57 are arranged between the light naphtha outlet 55 and the light naphtha tank area 58. The light naphtha separated in the light naphtha separation tower 49 is cooled to 45 ℃ or lower by a light naphtha air cooler 56 and a light naphtha water circulation cooler 57, and then sent to a light naphtha tank 58 to be produced as a light naphtha product.
The bottom of light naphtha knockout tower 49 is equipped with heavy naphtha export 59, heavy naphtha export 59 is connected with light naphtha knockout tower discharge pump 60, light naphtha knockout tower discharge pump 60 is connected with light naphtha knockout tower reboiler 61, heavy naphtha tank field 64 and light hydrocarbon recovery system respectively, light naphtha knockout tower reboiler 61 is connected with the reboiling liquid inlet of light naphtha knockout tower 49, be equipped with heavy naphtha air cooler 62 and heavy naphtha water circulation cooler 63 between light naphtha knockout tower discharge pump 60 and heavy naphtha tank field 64. Heavy naphtha at the bottom of the light naphtha separation tower 49 is divided into three parts by a discharge pump 60 of the light naphtha separation tower, one part is heated by a reboiler 61 of the light naphtha separation tower and then returns to the light naphtha separation tower 49, one part is sent to a light hydrocarbon recovery system to be used as an absorbent to absorb macromolecular hydrocarbons carried by non-condensable gas in the light hydrocarbon recovery system, and the other part is cooled to below 45 ℃ by a heavy naphtha air cooler 62 and a heavy naphtha oil-water circulation cooler 63 and then sent to a heavy naphtha tank area 58 to be used as a heavy naphtha product to be output.
The bottom of the heavy naphtha separation tower 37 is provided with a diesel component outlet 42, the diesel component outlet 42 is respectively connected with a heavy naphtha separation tower reboiler heating furnace feed pump 43 and a heavy naphtha separation tower discharge pump 45, the heavy naphtha separation tower reboiler heating furnace feed pump 43 is connected with a heavy naphtha separation tower reboiler heating furnace 44, the heavy naphtha separation tower reboiler heating furnace 44 is connected with a heavy naphtha separation tower 37 reboiled liquid inlet, the heavy naphtha separation tower discharge pump 45 is connected with a diesel component tank area 48, and a diesel component air cooler 46 and a diesel component water circulation cooler 47 are arranged between the heavy naphtha separation tower discharge pump 45 and the diesel component tank area 48. The diesel component at the bottom of the heavy naphtha separation tower 37 is divided into two parts, one part is heated by a heavy naphtha separation tower reboiler heating furnace 43 and then returned to the heavy naphtha separation tower 37, and the other part is cooled to below 45 ℃ by a diesel component air cooler 46 and a diesel component water circulation cooler 47 and then sent to a diesel component tank area 48 to be output as a diesel component product.
The light hydrocarbon recovery system comprises a light hydrocarbon absorption tower 65 and an amine liquid absorption tower 67, a gas phase outlet at the top of a carbon five-component separation tower reflux tank 8, a gas phase outlet at the top of a deethanizer reflux tank 17, a gas phase outlet at the top of a debutanizer reflux tank 25, a gas phase outlet at the top of a heavy naphtha separation tower reflux tank 40 and a heavy naphtha outlet 59 at the bottom of a light naphtha separation tower 49 are connected with a feed inlet of the light hydrocarbon absorption tower 65, uncondensed gas separated from the carbon five-component separation tower reflux tank 8, the deethanizer reflux tank 17, the debutanizer reflux tank 25 and the heavy naphtha separation tower reflux tank 40 is sent to the light hydrocarbon absorption tower 65 to be mixed, and heavy naphtha in the light naphtha separation tower 49 enters the light hydrocarbon absorption tower 65 to be in gas-liquid contact with the uncondensed gas so as to absorb macromolecular hydrocarbons carried in the uncondensed gas.
The gas phase export at light hydrocarbon absorption tower 65 top is connected with amine liquid absorption tower 67's feed inlet, the back that the absorption process finishes, the gas phase export of noncondensable gas at light hydrocarbon absorption tower 65 top is discharged, carry out desulfurization treatment in getting into amine liquid absorption tower 67 from amine liquid absorption tower 67's feed inlet, the rich absorption oil export light hydrocarbon absorption tower discharge pump 66 of light hydrocarbon absorption tower 65 bottom is connected, light hydrocarbon absorption tower discharge pump 66 is connected with the feed inlet of five component separation towers of carbon 4. The rich absorption oil at the bottom of the light hydrocarbon absorption tower 65 enters the carbon five-component separation tower 4 from the feed inlet of the carbon five-component separation tower 4 by adopting a discharge pump 66 of the light hydrocarbon absorption tower, and descends along the tower together with the condensate oil at the feed inlet of the carbon five-component separation tower 4.
After the non-condensable gas enters the amine liquid absorption tower 67, firstly, the lean amine liquid is adopted to carry out amine elution on the non-condensable gas to remove hydrogen sulfide in the non-condensable gas, the amine-washed non-condensable gas is subjected to alkali washing by NaOH, mercaptan in the non-condensable gas is converted into sodium mercaptide and water, and the non-condensable gas is enabled to be free from sodium mercaptide and waterThe mercaptan content in the condensed gas is less than 343mg/Nm3The top of the amine liquid absorption tower 67 is provided with a second fuel gas outlet 68, the second fuel gas outlet 68 is connected with a second fuel gas pipe network 70, the desulfurized noncondensable gas is sent to the second fuel gas pipe network 70 to be output as a fuel gas product, the amine liquid absorption tower 67 and the sulfur recovery unit 71 form a circulation loop, sodium mercaptan and water generated in the amine liquid absorption tower 67 enter the sulfur recovery unit 71 together with NaOH, air is introduced into the sulfur recovery unit 71 under the action of a methyldiethanolamine catalyst in the sulfur recovery unit 71 to reduce the sodium mercaptan into NaOH and disulfide, and the generated NaOH returns to the amine liquid absorption tower 67 to continue the alkaline washing reaction.
The top of the carbon five-component separation tower 4 is provided with a corrosion inhibitor injection port 5 of the carbon five-component separation tower, the top of the deethanizer 13 is provided with a corrosion inhibitor injection port 14 of the deethanizer, the top of the debutanizer 22 is provided with a corrosion inhibitor injection port 23 of the debutanizer, the top of the heavy naphtha separation tower 37 is provided with a corrosion inhibitor injection port 38 of the heavy naphtha separation tower, the top of the light naphtha separation tower 49 is provided with a corrosion inhibitor injection port 50 of the light naphtha separation tower, liquefied gas components and fuel gas components all contain hydrogen sulfide medium, wet hydrogen sulfide in oil gas at the top of the fractionating tower can corrode tower top equipment and pipelines, the corrosion inhibitor injection port is arranged at the top of the fractionating tower, injecting corrosion inhibitor into the tower top to play the role of corrosion prevention, controlling the grading separation device by a Distributed Control System (DCS), and an emergency stop and safety chain protection system (ESD & SIS) is arranged, so that the operation is safer and more reliable.
The process method for processing the condensate oil by using the fractionation device comprises the following steps as shown in figure 2:
s1, conveying condensate oil to an electric desalting system 1, primarily exchanging heat through a heat source in the electric desalting system, mixing the condensate oil with water and a demulsifier, then feeding the mixture into a primary electric desalting tank, removing most of salt contained in the condensate oil, and applying an electric field to the condensate oil subjected to primary desalting for secondary electric desalting to ensure that the salt content in the condensate oil is less than 3 mgNaCl/L;
s2, sending the desalted condensate oil to a demercuration system 2, adding a hydrogenolysis catalyst to enable the condensate oil to carry out hydrogenolysis reaction under the condition of hydrogen so as to reduce organic mercury carried in the condensate oil, converting the organic mercury into adsorbable inorganic mercury, and then adsorbing the inorganic mercury in a physical adsorption and filtration mode to achieve the purpose of demercuration, so that the mercury content in the condensate oil is less than 5 ppb;
s3, sending the condensate oil after demercuration treatment to a hydrogenation reaction system 3, carrying out desulfurization and demercaptanization treatment on the condensate oil through the hydrogenation reaction system 3, exchanging heat of the condensate oil after desalination, demercuration and desulfurization treatment to 155-180 ℃ through a carbon five-component separation tower heat exchanger 6 and a deethanizer heat exchanger 15, and then entering a carbon five-component separation tower 4 for rectification;
s4, a reboiler heating furnace 11 of the carbon five-component separation tower vaporizes condensate oil at the bottom of the carbon five-component separation tower 4, the oil gas rises along the tower, enters a reflux tank 8 of the carbon five-component separation tower after being subjected to heat exchange and condensation by a heat exchanger 6 of the carbon five-component separation tower and an air cooler 7 of the carbon five-component separation tower, is separated, noncondensable gas is separated and sent to a light hydrocarbon absorption tower 65 for recovery, separated liquid-phase materials are divided into two parts, one part is used as the top reflux of the carbon five-component separation tower 4 and falls along the tower, and the other part is used as the feeding of a deethanizer 13 or a debutanizer 22;
s5, if the content of fuel gas in the liquid phase material separated by the reflux tank 8 of the carbon five-component separation tower is high, the separated liquid phase material is sent to a deethanizer 13 for rectification, a deethanizer reboiler 21 enables the liquid phase material at the bottom of the deethanizer 13 to be vaporized, oil gas rises along the tower, enters a deethanizer reflux tank 17 for separation after being subjected to heat exchange and condensation through a deethanizer heat exchanger 15 and a deethanizer air cooler 16, separated non-condensable gas is sent to a light hydrocarbon absorption tower 65 for recovery, and the separated fuel gas is sent to a first fuel gas pipe network 69 to be output as a fuel gas product;
s6, dividing a carbon five component and a liquefied gas component at the bottom of the deethanizer 13 into two parts, wherein one part is heated by a deethanizer reboiler 21 and then returns to the deethanizer 13, and the other part enters the debutanizer 22 for rectification as a feed material of the debutanizer 22;
if the content of the fuel gas in the liquid phase material separated by the reflux tank 8 of the carbon five-component separation tower is less, directly sending the separated liquid phase material to a debutanizer 22 for rectification;
s7, a reboiler 33 of the debutanizer enables five carbon components and liquefied gas components at the bottom of the debutanizer 22 to be vaporized, oil gas rises along the debutanizer, the oil gas is condensed by a debutanizer condenser 24 and then enters a debutanizer reflux tank 25 for separation, the separated uncondensed gas is sent to a light hydrocarbon absorption tower 65 for recovery, and the separated liquefied gas is sent to a liquefied gas desulfurization system 30 after being cooled to below 45 ℃ by a liquefied gas air cooler 28 and a liquefied gas water circulating cooler 29;
s8, after the liquefied gas rectified by the debutanizer 22 enters a liquefied gas desulfurization system 30, a desulfurization unit is used for carrying out desulfurization treatment on the liquefied gas, firstly, lean amine liquid is used for carrying out amine elution on the liquefied gas to remove hydrogen sulfide in the liquefied gas, the liquefied gas after the amine washing is subjected to alkali washing by NaOH, mercaptan in the liquefied gas is converted into sodium mercaptan and water, and the content of the mercaptan in the liquefied gas is lower than 343mg/Nm3The desulfurized liquefied gas is produced as a liquefied gas product, sodium mercaptide and water generated by the desulfurization unit enter an alkali liquor regeneration unit together with NaOH, air is introduced under the action of a methyldiethanolamine catalyst to reduce the sodium mercaptide into NaOH and disulfide, and the generated NaOH returns to the desulfurization unit to continue to carry out an alkali washing reaction;
s9, dividing the carbon five-component at the bottom of the debutanizer 22 into two parts, heating one part by a debutanizer reboiler 33 and then returning the heated part to the debutanizer 22, cooling the other part by a carbon five-component air cooler 34 and a carbon five-component water-division circulating cooler 35 to below 45 ℃, and then sending the cooled part to a carbon five-component tank area 36 to be output as a carbon five-component product;
s10, the heavy component at the bottom of the carbon five-component separation tower 4 is divided into two parts, one part is heated by a reboiler heating furnace 11 of the carbon five-component separation tower and then returns to the carbon five-component separation tower 4, and the other part enters a heavy naphtha separation tower 37 for rectification as the feed of the heavy naphtha separation tower 37;
s11, vaporizing heavy components at the bottom of the tower by a heavy naphtha separation tower reboiler 44, ascending oil gas along the tower, condensing the oil gas by a heavy naphtha separation tower condenser 39, then separating the oil gas in a heavy naphtha separation tower reflux tank 40, sending separated uncondensed gas to a light hydrocarbon absorption tower 65 for recovery, and feeding the separated mixed naphtha serving as the feed of a light naphtha separation tower 49 into a light naphtha separation tower 49 for rectification;
s12, a light naphtha separation tower reboiler 61 provides heat for a light naphtha separation tower 49, the quintuple carbon at the top of the light naphtha separation tower 49 is condensed by a light naphtha separation tower condenser 51 and then enters a light naphtha separation tower reflux tank 52, the quintuple carbon in the light naphtha separation tower reflux tank 52 is divided into two parts, one part of the quintuple carbon is used as the top reflux of the light naphtha separation tower 49 to descend along the tower, the other part of the quintuple carbon is combined with the quintuple carbon discharged from a first quintuple carbon outlet 31, and the combined quintuple carbon is cooled to below 45 ℃ by a quintuple air cooler 34 and a quintuple carbon diversion circulating cooler 35 and then is sent to a quintuple carbon tank area 36 to be used as a quintuple carbon product for output;
s13, taking out light naphtha in the light naphtha separation tower 49 as a side product, cooling the light naphtha to be below 45 ℃ through a light naphtha air cooler 56 and a light naphtha water circulating cooler 57, and sending the light naphtha to a light naphtha tank area 58 to be output as a light naphtha product;
s14, dividing heavy naphtha at the bottom of a light naphtha separation tower 49 into three parts, heating one part of the heavy naphtha by a light naphtha separation tower reboiler 61 and returning the part of the heavy naphtha to the light naphtha separation tower 49, sending one part of the heavy naphtha to a light hydrocarbon absorption tower 65 as an absorbent, cooling the other part of the light naphtha to a temperature below 45 ℃ by a heavy naphtha air cooler 62 and a heavy naphtha oil-water circulation cooler 63, sending the cooled part of the heavy naphtha to a heavy naphtha tank area 64, and outputting the product of the heavy naphtha;
s15, dividing the diesel component at the bottom of the heavy naphtha separation tower 37 into two parts, heating one part by a heavy naphtha separation tower reboiler heating furnace 44 and returning the heated part to the heavy naphtha separation tower 37, cooling the other part by a diesel component air cooler 46 and a diesel component water circulation cooler 47 to below 45 ℃, and sending the cooled part to a diesel component tank area 48 to be output as a diesel component product;
s16, feeding noncondensable gas separated by the carbon five-component separation tower reflux tank 8, the deethanizer reflux tank 17, the debutanizer reflux tank 25 and the heavy naphtha separation tower reflux tank 40 to a light hydrocarbon absorption tower 65 for mixing, allowing heavy naphtha at the bottom of the light naphtha separation tower 49 to enter the light hydrocarbon absorption tower 65 and then to be in gas-liquid contact with the noncondensable gas to absorb macromolecular hydrocarbons carried in the noncondensable gas, allowing the noncondensable gas to enter an amine liquid absorption tower 67 for desulfurization treatment after the absorption process is finished, and allowing rich absorption oil at the bottom of the light hydrocarbon absorption tower 65 to enter the carbon five-component separation tower 4 as the feed of the carbon five-component separation tower 4 for rectification;
s17, after the non-condensable gas enters an amine liquid absorption tower 67, firstly, amine elution is carried out on the non-condensable gas by adopting lean amine liquid to remove hydrogen sulfide in the non-condensable gas, the amine-washed non-condensable gas is subjected to alkali washing by NaOH, mercaptan in the non-condensable gas is converted into sodium mercaptan and water, and the content of the mercaptan in the non-condensable gas is lower than 343mg/Nm3The desulfurized non-condensable gas is sent to a second fuel gas pipe network 70 to be output as a fuel gas product;
s18, sodium mercaptan and water generated in the amine liquid absorption tower 67 enter the sulfur recovery unit 71 together with NaOH, air is introduced into the sulfur recovery unit 71 under the action of a methyldiethanolamine catalyst in the sulfur recovery unit 71 to reduce the sodium mercaptan into NaOH and disulfide, and the generated NaOH returns to the amine liquid absorption tower 67 to continue the alkaline washing reaction.
When the condensate was processed alone at 550 ten thousand tons/year using the fractionation apparatus and process of the present example, the process parameters of the respective fractionation columns are shown in table 1.
TABLE 1
Figure BDA0003354175090000231
Figure BDA0003354175090000241
Figure BDA0003354175090000251
Test example
The condensate was treated by the fractionation device in the example, and the fractionated liquefied gas, the five carbon components, the light naphtha and the heavy naphtha were examined, and the examination results are shown in table 2.
TABLE 2
Figure BDA0003354175090000252
Figure BDA0003354175090000261
As can be seen from table 2, the detection results of the liquefied gas and the five-carbon component both satisfy specific indexes, which indicates that the fractionation device in the embodiment can fractionate the liquefied gas product and the five-carbon component product with qualified quality.
The fractionation effect among the light naphtha, the heavy naphtha and the diesel oil component is judged by adopting the Engler distillation gap, the higher the Engler distillation gap is, the better the fractionation precision is, the components can not be mutually overlapped, as can be seen from the table 2, the light naphtha-heavy naphtha degassing degree Engler distillation gap is more than 8 ℃, the fractionation precision of the fractionation device in the embodiment is high, the fractionation effect is good, the light naphtha and the heavy naphtha can be separated, and thus the light naphtha product with qualified quality is fractionated; the heavy naphtha-diesel void degree Engler distillation gap is more than 8 ℃, which shows that the heavy naphtha and the diesel components can be separated by adopting the grading separation device in the embodiment, so that the heavy naphtha diesel with qualified quality is fractionated; the final distillation point of condensate oil is below 400 ℃, the diesel oil components are fractionated at 190-400 ℃ according to the national standard, and when the diesel oil is fractionated by adopting the fractionation device in the embodiment, the diesel oil components can be guaranteed to be fractionated by controlling the process parameters to ensure that the diesel oil components have the initial distillation point (IBP) >190 ℃.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims (10)

1. The grading separation device for independently processing condensate oil is characterized by comprising a fractionating system and a light hydrocarbon recovery system, wherein the fractionating system comprises a carbon five-component separation tower, a gas-phase outlet at the top of the carbon five-component separation tower is sequentially connected with a cooling device of the carbon five-component separation tower and a reflux tank of the carbon five-component separation tower, and a liquid-phase outlet at the bottom of the reflux tank of the carbon five-component separation tower is connected with a feed inlet of a debutanizer;
a gas phase outlet at the top of the debutanizer is sequentially connected with a debutanizer cooling device and a debutanizer reflux tank, a liquefied gas outlet is arranged at the bottom of the debutanizer reflux tank, and a first carbon five component outlet is arranged at the bottom of the debutanizer;
an oil phase outlet at the bottom of the carbon five-component separation tower is connected with a feed inlet of a heavy naphtha separation tower, a gas phase outlet at the top of the heavy naphtha separation tower is sequentially connected with a cooling device of the heavy naphtha separation tower and a reflux tank of the heavy naphtha separation tower, a liquid phase outlet at the bottom of the reflux tank of the heavy naphtha separation tower is connected with a feed inlet of a light naphtha separation tower, and a diesel component outlet is arranged at the bottom of the heavy naphtha separation tower;
a gas phase outlet at the top of the light naphtha separation tower is sequentially connected with a light naphtha separation tower cooling device and a light naphtha separation tower reflux tank, a second carbon five-component outlet is arranged at the bottom of the light naphtha separation tower reflux tank, a light naphtha outlet is arranged on the side wall of the light naphtha separation tower, and a heavy naphtha outlet is arranged at the bottom of the light naphtha separation tower;
and the gas phase outlet at the top of the reflux tank of the carbon five-component separation tower, the gas phase outlet at the top of the reflux tank of the debutanizer, the gas phase outlet at the top of the reflux tank of the heavy naphtha separation tower and the heavy naphtha outlet are all connected with the light hydrocarbon recovery system.
2. The fractionation device for processing condensate oil individually according to claim 1, wherein the fractionation system further comprises a deethanizer, a liquid phase outlet at the bottom of the reflux tank of the carbon five component separation tower is connected with a feed inlet of the deethanizer, a corrosion inhibitor injection port of the deethanizer is arranged at the top of the deethanizer, a gas phase outlet at the top of the deethanizer is sequentially connected with a deethanizer cooling device and a deethanizer reflux tank, a first fuel gas outlet is arranged at the bottom of the deethanizer reflux tank, and the first fuel gas outlet is connected with a reflux port of the deethanizer;
the tower bottom of the deethanizer is provided with a deethanizer reboiler, an oil phase outlet at the bottom of the deethanizer is respectively connected with an inlet of the deethanizer reboiler and a feed inlet of the debutanizer, and an outlet of the deethanizer reboiler is connected with a reboiling liquid inlet of the deethanizer.
3. The fractionation plant for separately processing condensate oil according to claim 2, wherein the light hydrocarbon recovery system comprises a light hydrocarbon absorption tower and an amine liquid absorption tower, the gas phase outlet at the top of the carbon five component separation tower reflux drum, the gas phase outlet at the top of the debutanizer reflux drum, the gas phase outlet at the top of the deethanizer reflux drum, the gas phase outlet at the top of the heavy naphtha separation tower reflux drum and the heavy naphtha outlet are all connected to the feed inlet of the light hydrocarbon absorption tower, the gas phase outlet at the top of the light hydrocarbon absorption tower is connected to the feed inlet of the amine liquid absorption tower, and the rich absorption oil outlet at the bottom of the light hydrocarbon absorption tower is connected to the feed inlet of the carbon five component separation tower;
and a liquid phase outlet at the bottom of the amine liquid absorption tower is connected with an inlet of a sulfur recovery system, an outlet of the sulfur recovery system is connected with an alkali liquor inlet of the amine liquid absorption tower, and a second fuel gas outlet is arranged at the top of the amine liquid absorption tower.
4. The fractionation plant for processing condensate alone according to claim 2, wherein the carbon five component separation tower cooling device comprises a carbon five component separation tower heat exchanger and a carbon five component separation tower air cooler, the deethanizer cooling device comprises a deethanizer heat exchanger and a deethanizer air cooler, an outlet of the carbon five component separation tower heat exchanger is connected to an inlet of the deethanizer heat exchanger, an outlet of the deethanizer heat exchanger is connected to a feed inlet of the carbon five component separation tower, and an inlet of the carbon five component separation tower heat exchanger is connected to the pretreatment system;
the pretreatment system comprises an electric desalting system, a demercuration system and a hydrogenation reaction system which are sequentially connected, and an outlet of the hydrogenation reaction system is connected with an inlet of the heat exchanger of the carbon five-component separation tower.
5. The fractionation device for processing condensate oil individually as claimed in claim 1, wherein the top of the carbon five-component separation tower is provided with a corrosion inhibitor injection port of the carbon five-component separation tower, and the liquid phase outlet at the bottom of the reflux tank of the carbon five-component separation tower is connected with the reflux port of the carbon five-component separation tower;
a carbon five-component separation tower reboiler heating furnace is arranged at the tower bottom of the carbon five-component separation tower, an oil phase outlet at the bottom of the carbon five-component separation tower is connected with an inlet of the carbon five-component separation tower reboiler heating furnace, and an outlet of the carbon five-component separation tower reboiler heating furnace is connected with a reboiler liquid inlet of the carbon five-component separation tower;
the tower top of the debutanizer is provided with a debutanizer corrosion inhibitor injection port, the debutanizer cooling device comprises a debutanizer condenser, and the liquefied gas outlet is connected with the reflux port of the debutanizer;
the tower bottom of the debutanizer is provided with a debutanizer reboiler, the first carbon five-component outlet is connected with the inlet of the debutanizer reboiler, and the outlet of the debutanizer reboiler is connected with the reboiled liquid inlet of the debutanizer.
6. The fractionation plant for separate processing of condensate according to claim 1, wherein the top of the heavy naphtha splitter is provided with a heavy naphtha splitter corrosion inhibitor injection port, the heavy naphtha splitter cooling unit comprises a heavy naphtha splitter condenser, and the liquid phase outlet at the bottom of the heavy naphtha splitter reflux drum is connected to the reflux port of the heavy naphtha splitter;
a heavy naphtha separation tower reboiler heating furnace is arranged at the bottom of the heavy naphtha separation tower, the diesel component outlet is connected with an inlet of the heavy naphtha separation tower reboiler heating furnace, and an outlet of the heavy naphtha separation tower reboiler heating furnace is connected with a heavy boiling liquid inlet of the heavy naphtha separation tower;
the top of the light naphtha separation tower is provided with a light naphtha separation tower corrosion inhibitor injection port, the light naphtha separation tower cooling device comprises a light naphtha separation tower condenser, and the second carbon five component outlet is connected with a reflux port of the light naphtha separation tower;
the bottom of the light naphtha separation tower is provided with a light naphtha separation tower reboiler, the heavy naphtha outlet is connected with the inlet of the light naphtha separation tower reboiler, and the outlet of the light naphtha separation tower reboiler is connected with the heavy boiling liquid inlet of the light naphtha separation tower.
7. The fractionation plant for processing condensate oil alone according to claim 3, wherein the liquefied gas outlet is connected to a liquefied gas desulfurization system, and a liquefied gas air cooler and a liquefied gas water circulating cooler are provided between the liquefied gas outlet and the liquefied gas desulfurization system;
the first carbon five component outlet and the second carbon five component outlet are connected with a carbon five component tank area through a debutanizer discharge pump, and a carbon five component air cooler and a carbon five component water distribution circulating cooler are arranged between the debutanizer discharge pump and the carbon five component tank area;
the light naphtha outlet is connected with a light naphtha tank zone, and a light naphtha air cooler and a light naphtha water circulating cooler are arranged between the light naphtha outlet and the light naphtha tank zone;
the heavy naphtha outlet is connected with a heavy naphtha tank area, and a heavy naphtha air cooler and a heavy naphtha water circulating cooler are arranged between the heavy naphtha outlet and the heavy naphtha tank area;
the diesel component outlet is connected with a diesel component tank area, and a diesel component air cooler and a diesel component water circulating cooler are arranged between the diesel component outlet and the diesel component tank area;
the first fuel gas outlet is connected with a first fuel gas pipe network, and the second fuel gas outlet is connected with a second fuel gas pipe network.
8. A process for the separate processing of condensate by means of a fractionation unit according to any one of claims 1 to 7, characterized by the steps of:
s1, sending condensate oil to a carbon five-component separation tower for rectification, condensing oil gas at the top of the carbon five-component separation tower through a cooling device of the carbon five-component separation tower, then, sending the condensed oil gas into a reflux tank of the carbon five-component separation tower for separation, sending separated uncondensed gas to a light hydrocarbon recovery system for recovery, taking separated liquid-phase materials as feeding materials of a debutanizer, and taking heavy components at the bottom of the carbon five-component separation tower as feeding materials of a heavy naphtha separation tower;
s2, sending the liquid phase material separated in the step S1 to a debutanizer for rectification, condensing oil gas at the top of the debutanizer from a debutanizer cooling device, then sending the condensed oil gas into a debutanizer reflux tank for separation, sending the separated uncondensed gas to a light hydrocarbon recovery system for recovery, discharging the separated liquefied gas from a liquefied gas outlet, and discharging the carbon five component at the bottom of the debutanizer from a first carbon five component outlet;
s3, the heavy naphtha separation tower is used for rectifying the recombination at the bottom of the five-carbon component separation tower in the step S1, oil gas at the top of the heavy naphtha separation tower is condensed by a heavy naphtha separation tower cooling device and then enters a heavy naphtha separation tower reflux tank for separation, the separated uncondensed gas is sent to the light hydrocarbon recovery system for recovery, the separated mixed naphtha is used as the feeding material of the light naphtha separation tower, and the diesel component at the bottom of the heavy naphtha separation tower is discharged from the diesel component outlet;
s4, sending the mixed naphtha separated in the step S3 to the light naphtha separation tower for rectification, condensing the carbon five components at the top of the light naphtha separation tower through a cooling device of the light naphtha separation tower, then entering a reflux tank of the light naphtha separation tower, and discharging from a second carbon five component outlet, discharging light naphtha in the light naphtha separation tower from a light naphtha outlet, sending one part of heavy naphtha at the bottom of the light naphtha separation tower to the light naphtha recovery system as an absorbent, and discharging the other part of heavy naphtha from the heavy naphtha outlet;
s5, noncondensable gas separated by the carbon five-component separation tower reflux tank, the debutanizer reflux tank and the heavy naphtha separation tower reflux tank is respectively sent to the light hydrocarbon recovery system for mixing, and heavy naphtha at the bottom of the light naphtha separation tower is sent to the light hydrocarbon recovery system and then is contacted with the noncondensable gas to absorb macromolecular hydrocarbons carried in the noncondensable gas.
9. A process for the separate processing of gas condensate according to claim 8, characterized in that it comprises the following steps:
s1, sending condensate oil to a carbon five-component separation tower for rectification, condensing oil gas at the top of the carbon five-component separation tower through a cooling device of the carbon five-component separation tower, then, sending the condensed oil gas into a reflux tank of the carbon five-component separation tower for separation, sending separated uncondensed gas to a light hydrocarbon recovery system for recovery, taking separated liquid-phase materials as feeding materials of a deethanizer, and taking heavy components at the bottom of the carbon five-component separation tower as feeding materials of a heavy naphtha separation tower;
s2, sending the liquid-phase material separated in the step S1 to the deethanizer for rectification, condensing oil gas at the top of the deethanizer through the deethanizer, then sending the condensed oil gas into a reflux tank of the deethanizer for separation, sending the separated uncondensed gas to the light hydrocarbon recovery system for recovery, discharging the separated fuel gas from the first fuel gas outlet, and taking the carbon five component and the liquefied gas component at the bottom of the deethanizer as the feeding materials of the debutanizer;
s3, sending the carbon five component and the liquefied gas component at the bottom of the deethanizer in the step S2 to the debutanizer for rectification, condensing oil gas at the top of the debutanizer from a debutanizer cooling device, then sending the condensed oil gas into a debutanizer reflux tank for separation, sending the separated uncondensed gas to the light hydrocarbon recovery system for recovery, discharging the separated liquefied gas from a liquefied gas outlet, and discharging the carbon five component at the bottom of the debutanizer from a first carbon five component outlet;
s4, the heavy naphtha separation tower is used for rectifying the recombination at the bottom of the carbon five-component separation tower in the step S1, oil gas at the top of the heavy naphtha separation tower is condensed by a cooling device of the heavy naphtha separation tower and then enters a reflux tank of the heavy naphtha separation tower for separation, the separated non-condensable gas is sent to the light hydrocarbon recovery system for recovery, the separated mixed naphtha is used as the feeding material of the light naphtha separation tower, and the diesel component at the bottom of the heavy naphtha separation tower is discharged from a diesel component outlet;
s5, sending the mixed naphtha separated in the step S4 to the light naphtha separation tower for rectification, wherein the carbon five components at the top of the light naphtha separation tower are condensed by the condenser of the light naphtha separation tower and then enter the reflux tank of the light naphtha separation tower to be discharged from the second carbon five component outlet, the light naphtha in the light naphtha separation tower is discharged from the light naphtha outlet, the heavy naphtha at the bottom of the light naphtha separation tower is sent from one part to the light naphtha recovery system to be used as an absorbent, and the other part is discharged from the heavy naphtha outlet;
s6, noncondensable gas that five component separation tower reflux drum of carbon, deethanizer reflux drum, debutanizer reflux drum and heavy naphtha knockout drum reflux drum separated sends respectively to the light dydrocarbon recovery system mixes, heavy naphtha in light naphtha knockout drum bottom send to contact with noncondensable gas behind the light dydrocarbon recovery system in order to absorb the macromolecular hydrocarbons that carry in the noncondensable gas.
10. The process of claim 9, wherein in step S6, the non-condensable gas in the light hydrocarbon recovery system is desulfurized after absorbing the macromolecular hydrocarbons with heavy naphtha, and the desulfurized non-condensable gas is produced as a fuel gas product.
CN202111346467.8A 2021-11-15 2021-11-15 Grading separation device and process method for independently processing condensate oil Pending CN113897213A (en)

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