CN109135809A - A kind of naphtha deaerating type of cycles and deoxidation method - Google Patents
A kind of naphtha deaerating type of cycles and deoxidation method Download PDFInfo
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- CN109135809A CN109135809A CN201810885086.9A CN201810885086A CN109135809A CN 109135809 A CN109135809 A CN 109135809A CN 201810885086 A CN201810885086 A CN 201810885086A CN 109135809 A CN109135809 A CN 109135809A
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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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of naphtha deaerating type of cycles, including deoxygenation return tank, condenser, oxygen-removing tower reflux pump, tower bottom heat exchanger plus hydrogen feed pump, bottom reboiler, oxygen-removing tower, corrosion inhibiter storage device and inert gas storage device, oxygen-removing tower includes oxygen-removing tower gas-phase space；Condenser is connect with deoxygenation column overhead and deoxygenation return tank respectively by pipeline, deoxygenation return tank, oxygen-removing tower reflux pump and tower bottom heat exchanger pass through pipeline successively line, tower bottom heat exchanger respectively with deoxygenation column overhead, oxygen-removing tower tower bottom, bottom reboiler and hydrogen feed pump is added to connect by pipeline, bottom reboiler is connect with oxygen-removing tower gas-phase space, hydrogen feed pump is added to connect with oxygen-removing tower tower bottom by pipeline, inert gas storage device is connect with oxygen-removing tower gas-phase space.The present invention effectively optimizes cell process process, reduces unit investment and land occupation, the introducing of corrosion inhibiter and inert gas effectively reduce the corrosion risk of oxygen-removing tower, extend the service life of oxygen-removing tower.
Description
Technical field
The invention belongs to technical field of petrochemical industry, and in particular to a kind of naphtha deaerating type of cycles and deoxidation method.
Background technique
Raw material naphtha can bring oxygen, after naphtha is contacted with dissolved oxygen, light oil into during transport, handling and storage
Unsaturated hydrocarbons in raw material generates free radical as the active hydrogen in alkene, naphthalenes and tetrahydronaphthalene is reacted with oxygen, causes chain reaction
Generate peroxide；Peroxide is decomposed into various oxidation products again, and oxidation product again can be miscellaneous with the activity of sulfur-bearing, oxygen, nitrogen
Atomic compound occurs polymerization reaction and generates oxidated gum and high polymer；The thiosulfonic acid that aromatic alcohol oxidation generates can be sent out with pyrroles
Raw condensation reaction generates polymer.It is industrial often to be taken off with hydrogenation technique for the purification naphtha or kerosene raffinate of production high-quality
Except impurity such as sulphur, nitrogen in raw material, the easy downstream equipment such as colloid and polymer at high temperature, as heating furnace tube, raw material/
Further condensation coking, causes heating furnace tube, pre-hydrogenator and system at the top of effluent exchanger, pre-hydrogenator
Pressure drop increases, and hydrogenation plant frequent shutdowns is forced to handle.Therefore, when can not achieve material direct-furnish between device, light oil raw material
When transport facility being needed to transport and store, then need to add light oil raw material deoxygenation measure.
Yang Kaiyan, application [J] of the deoxyprocess on continuous reformer, petrochemical technology and application, 2012,30(4):
340-342.A kind of thermal de-aeration technique is disclosed, naphtha is changed through stripping oxygen-removing tower feed exchanger tube side with deoxidation naphtha
Enter stripping oxygen-removing tower after heat.Enter stripping oxygen-removing tower after light component, a small amount of moisture and the water cooled device condensation cooling of tops to return
It flows in tank, light component and oxygen-containing gas in return tank are sent to fuel gas system.Liquid portion is big after stripping oxygen-removing tower stripping
Part returns to stripper after bottom reboiler heats, and rest part enters after stripping oxygen-removing tower feed exchanger shell side heat exchange
Raw material surge tank.
105969421 B of CN disclose a kind of purification low pressure deoxidation of petroleum naphtha hydrogenation and charging heat exchange optimization method and
System.This method is filtered naphtha, and deoxidation tower is sent into after heat exchange and carries out deoxidation treatment, deoxidation tower top gaseous phase warp
After cooling, deoxidation return tank of top of the tower is sent into turn by liquid phase infinite reflux to deoxidation column overhead, deoxidation return tank of top of the tower top is not coagulated
Gas is discharged into torch pipe network；Naphtha returns after entering the heating of deoxidation tower bottom reboiler after a part of deoxidation for distillating deoxidation tower tower bottom
It returns in deoxidation tower tower reactor；Wherein, with the heat exchange of filtered naphtha be another part deoxidation that deoxidation tower tower bottom distillates after
Naphtha, naphtha enters raw material surge tank as petroleum naphtha hydrogenation raw material after the deoxidation after heat exchange.
Deoxygenation tower process is stripped in above-mentioned naphtha, in practice, serious corrosion occurs at the top of stripping oxygen-removing tower
Heat exchanger tube perforation or the blocking of serious dirt just occur for problem, tower top water cooler or air cooler per March to half a year or so, feed inlet with
Upper tower tray blocking is serious, is up to 9200 mg/L, pH value through iron ion content in certain device assay return tank point water-water phase
Up to 5.5.
Summary of the invention
In order to solve the above technical problems, the present invention provides a kind of naphtha deaerating type of cycles and deoxidation method.
Specific technical solution is as follows:
A kind of naphtha deaerating type of cycles, the difference is that, the system comprises deoxygenation return tank, condenser, oxygen-removing towers to return
Flow pump, tower bottom heat exchanger plus hydrogen feed pump, bottom reboiler, oxygen-removing tower, corrosion inhibiter storage device and inert gas storage dress
It sets, the oxygen-removing tower includes oxygen-removing tower gas-phase space；The condenser by pipeline respectively with the deoxygenation column overhead and described
The connection of deoxygenation return tank, the deoxygenation return tank, the oxygen-removing tower reflux pump and the tower bottom heat exchanger pass through pipeline successively
Line, the tower bottom heat exchanger respectively with the deoxygenation column overhead, the oxygen-removing tower tower bottom, the bottom reboiler and it is described plus
Hydrogen feed pump is connected by pipeline, and the bottom reboiler connect with the oxygen-removing tower gas-phase space, it is described add hydrogen feed pump and
The oxygen-removing tower tower bottom is connected by pipeline, and the inert gas storage device is connect with the oxygen-removing tower gas-phase space.
In above-mentioned technical proposal, the deoxygenation return tank include feed naphtha entrance, gas-liquid entrance, fuel discharge pipe,
Deoxygenation return tank gas-phase space and deoxygenation return tank raw material space；The condenser is connect with the gas-liquid entrance, the deoxygenation
Return tank gas-phase space is connected to the gas-liquid entrance and fuel discharge pipe, the deoxygenation return tank raw material space and the stone brain
Oily feed(raw material)inlet connection.
In above-mentioned technical proposal, valve, the valve are installed between the tower bottom heat exchanger and the oxygen-removing tower tower bottom
For triple valve or bypass valve, pipeline and described plus hydrogen feed pump between the oxygen-removing tower tower bottom and the tower bottom heat exchanger
Pipeline between the oxygen-removing tower tower bottom is connected on the valve.
A kind of naphtha deoxidation method, the difference is that, by tank field Lai through filtering out the feed naphtha of impurity,
It is handled into above-mentioned naphtha deaerating type of cycles, feed naphtha filtered first is carried out into the deoxygenation return tank tank bottom
Place exchanges heat after oxygen-removing tower reflux pump pressurization into the tower bottom heat exchanger tube pass, carries out subsequently into the oxygen-removing tower
Deoxygenation is stripped, the deoxygenation overhead gas is mixed with corrosion inhibiter, enters the oxygen-removing tower return tank after condenser condensation
Gas-phase space, fixed gas are discharged into fuel gas system by the fuel discharge pipe, and oil mutually flows back, and the oil of reflux is mutually secondary stripping
Oily phase returns to oxygen-removing tower after the pressurization of oxygen-removing tower reflux pump and carries out stripping deoxygenation again；Tower bottom using the bottom reboiler into
Row heating, inert gas enter the oxygen-removing tower spirit phase space and strip deoxygenation together with the heat that bottom reboiler provides, most
Downstream units are pumped by tower bottom heat exchanger and the secondary stripped oil phase and the hydrogenated charging of raw material heat exchange.
In above-mentioned technical proposal, the inert gas is nitrogen or fuel gas, the volume flow and fixed gas of inert gas
The ratio between volume flow be 1:(3 ~ 5), the position of Inlet Position 0~200mm on the bottom reboiler return port.
In above-mentioned technical proposal, the deoxygenation column overhead operating pressure is gauge pressure 0.5MPa~0.7MPa；The deoxygenation
Column overhead operation temperature is 85 DEG C~148 DEG C, and the oxygen-removing tower gas-phase space operation temperature is 155 DEG C~200 DEG C；It is described secondary
Stripped oil phase and the mass ratio of charging are (0.04~0.1): 1.
In above-mentioned technical proposal, the corrosion inhibiter is passivation membranous type corrosion inhibiter, and the implantation quality of corrosion inhibiter is liquid of top of the tower
The 0.05%~0.1% of body reflux mass.
In above-mentioned technical proposal, the feed naphtha is after the heat exchange of tower bottom heat exchanger tube pass, into the deoxygenation tower temperature
Degree is not more than 90 DEG C, is not less than 1.0m/s in pipeline flow velocity.
In above-mentioned technical proposal, the feed naphtha entrance is extended to away from oxygen-removing tower return tank bottom 150mm.
In above-mentioned technical proposal, feed naphtha mutually enters the reflux pump with the secondary stripped oil together and pressurizes.
Compared with prior art, the beneficial effects of the present invention are naphtha deaerating type of cycles of the present invention and method, the present invention
Oxygen-removing tower return tank merges return tank in traditional treatment method with unit raw material surge tank deoxygenation column bottoms pump with hydrogen feed pump is added,
Cell process process is effectively optimized, reduces unit investment and land occupation, the introducing of corrosion inhibiter and inert gas, which effectively reduces, to remove
The corrosion risk of oxygen column extends the service life of oxygen-removing tower.
Detailed description of the invention
Fig. 1 is naphtha deaerating type of cycles figure；
Fig. 2 is oxygen-removing tower return tank structure chart；
Wherein, 1- deoxygenation return tank, the feed(raw material)inlet 101-, 102- gas-liquid entrance, 103- fuel discharge pipe, the reflux of 104- oxygen-removing tower
Tank gas-phase space, 105- oxygen-removing tower return tank raw material space, 2- condenser, 3- oxygen-removing tower reflux pump, 4- tower bottom heat exchanger, 5- add
Hydrogen feed pump, 6- bottom reboiler, 7- oxygen-removing tower, 701- oxygen-removing tower gas-phase space, 8- corrosion inhibiter storage device, 9- inert gas
Storage device, 901- control valve, 10- valve.
Specific embodiment
This year invention is described in detail with specific embodiment with reference to the accompanying drawing.
Embodiment one
Naphtha deaerating type of cycles, the system comprises deoxygenation return tank 1, condenser 2, oxygen-removing tower reflux pump 3, tower bottom heat exchanger 4,
Add hydrogen feed pump 5, bottom reboiler 6, oxygen-removing tower 7, corrosion inhibiter storage device 8 and inert gas storage device 9, the oxygen-removing tower
7 include oxygen-removing tower gas-phase space 701；The condenser 2 is flowed back with 7 tower top of oxygen-removing tower and the deoxygenation respectively by pipeline
Tank 1 connects, and the deoxygenation return tank 1, the oxygen-removing tower reflux pump 3 and the tower bottom heat exchanger 4 pass through pipeline successively line,
The tower bottom heat exchanger 4 respectively with 7 tower top of oxygen-removing tower, 7 tower bottom of the oxygen-removing tower, the bottom reboiler 6 and it is described plus
Hydrogen feed pump 5 is connected by pipeline, and the bottom reboiler 6 is connect with the oxygen-removing tower gas-phase space 701, the charging of described plus hydrogen
Pump 5 is connect with 7 tower bottom of oxygen-removing tower by pipeline, the inert gas storage device 9 and the oxygen-removing tower gas-phase space 701
It is connected by pipeline.
The deoxygenation return tank includes feed naphtha entrance 101, gas-liquid entrance 102, fuel discharge pipe 103, deoxygenation time
Flow tank gas-phase space 104 and deoxygenation return tank raw material space 105；The condenser 2 is connect with the gas-liquid entrance 102, described
Deoxygenation return tank gas-phase space 104 is connected to the gas-liquid entrance 102 and fuel discharge pipe 105, the deoxygenation return tank raw material
Space 105 is connect with the feed(raw material)inlet 101.The gas-liquid entrance 102 of oxygen-removing tower return tank 1 and feed(raw material)inlet 101 are located at
1 different parts of oxygen-removing tower return tank avoid oxygen-containing higher fixed gas from mixing with feed naphtha, oxygen-removing tower deoxygenation are effectively ensured
Effect.
Triple valve 10 is installed between 7 tower bottom of the tower bottom heat exchanger 4 and the oxygen-removing tower, 7 tower bottom of oxygen-removing tower with
The pipeline between pipeline and described plus 7 tower bottom of hydrogen feed pump 5 and the oxygen-removing tower between the tower bottom heat exchanger 4 is connected to institute
It states on triple valve 10.
Pipeline between the inert gas storage device 9 and the oxygen-removing tower gas-phase space 701 is connected and installed with adjusting
Valve 901, the control valve 901 are connect with the fuel discharge pipe 103.
Embodiment two
Process flow: by tank field Lai through filtering out the feed naphtha of mechanical admixture, into above-mentioned naphtha deaerating type of cycles into
Row processing, feed naphtha filtered first carry out the deoxygenation return tank raw material space into 1 tank bottom of deoxygenation return tank
105, after the oxygen-removing tower reflux pump 3 pressurization, exchange heat into 4 tube side of tower bottom heat exchanger, subsequently into the oxygen-removing tower 7
Stripping deoxygenation is carried out, the 7 top gas body of oxygen-removing tower is mixed with corrosion inhibiter, enters the oxygen-removing tower after the condenser 2 condensation
Return tank gas-phase space 104, fixed gas are discharged into fuel gas system by the fuel discharge pipe 103, and oil mutually flows back, the oil of reflux
Mutually it is secondary stripped oil phase, returns to oxygen-removing tower 7 after the pressurization of oxygen-removing tower reflux pump 3 and carry out stripping deoxygenation again；Tower bottom uses institute
It states bottom reboiler 6 to be heated, inert gas enters the heat that the oxygen-removing tower gas-phase space 104 is provided with bottom reboiler 6
Amount strips deoxygenation together, is most sent into downstream through tower bottom heat exchanger 4 and secondary stripped oil phase and the hydrogenated feed pump 5 of raw material heat exchange afterwards
Unit.The flow control of inert gas is by between the inert gas storage device 9 and the oxygen-removing tower gas-phase space 701
Control valve 901 controlled, feed naphtha mutually enter together with the secondary stripped oil deoxygenation reflux pump 3 plus
Pressure.
Wherein 7 tower top pressure of oxygen-removing tower is 0.5 MPa of gauge pressure, and tower top operation temperature is 90 DEG C, oxygen-removing tower gas-phase space 701
Operation temperature is 155 DEG C, and the mass ratio of the secondary stripped oil phase and charging is 0.08:1.
Wherein the feed naphtha is 80 DEG C into 7 temperature of oxygen-removing tower after the heat exchange of 4 tube side of tower bottom heat exchanger,
It is 1.7m/s in pipeline flow velocity.Using threeway or bypass valve, control is except the temperature for entering the oxygen-removing tower.
Wherein the ratio between the volume flow of inert gas and the volume flow of tower top fixed gas are 1:4, and inert gas, which enters, to be removed
Oxygen column gas-phase space 701, the position of the oxygen-removing tower gas-phase space 701 100mm on 6 return port of bottom reboiler.
Wherein the injection rate of corrosion inhibiter is 0.07% that the implantation quality of corrosion inhibiter is overhead liquid reflux mass.
Embodiment three
Process flow is with embodiment two, and wherein 7 pressure on top surface of oxygen-removing tower is 0.6 MPa of gauge pressure, and tower top operation temperature is 95 DEG C, deoxygenation
Tower meteorological spatial operation temperature is 166 DEG C, the mass ratio 0.08:1 of the secondary stripped oil phase and charging.
Wherein the feed naphtha is 80 DEG C into 7 temperature of oxygen-removing tower after the heat exchange of 4 tube side of tower bottom heat exchanger,
It is 1.5m/s in pipeline flow velocity.Using threeway or bypass valve, control is except the temperature for entering the oxygen-removing tower.
Wherein the ratio between the volume flow of inert gas and the volume flow of tower top fixed gas are 1:4.5, and inert gas enters
Oxygen-removing tower gas-phase space 701, the position of the oxygen-removing tower gas-phase space 701 100mm on 6 return port of bottom reboiler.
Wherein the injection rate of corrosion inhibiter is 0.05% that the implantation quality of corrosion inhibiter is overhead liquid reflux mass.
Example IV
Process flow is with embodiment two, and wherein 7 tower top pressure of oxygen-removing tower is 0.7 MPa of gauge pressure, and tower top operation temperature is 140 DEG C,
Oxygen-removing tower meteorological spatial operation temperature is 178 DEG C, the mass ratio 0.08:1 of the secondary stripped oil phase and charging.
Wherein the feed naphtha is 90 DEG C into 7 temperature of oxygen-removing tower after the heat exchange of 4 tube side of tower bottom heat exchanger,
It is 1.8m/s in pipeline flow velocity.Using threeway or bypass valve, control is except the temperature for entering the oxygen-removing tower.
Wherein the ratio between the volume flow of inert gas and the volume flow of tower top fixed gas are 1:5, and inert gas, which enters, to be removed
Oxygen column gas-phase space 701, the position of the oxygen-removing tower gas-phase space 701 100mm on 6 return port of bottom reboiler.
Wherein the injection rate of corrosion inhibiter is 0.08% that the implantation quality of corrosion inhibiter is overhead liquid reflux mass.
The inert gas is nitrogen or fuel gas, and the ratio between volume flow and the volume flow of fixed gas of inert gas are
1:(3 ~ 5), the position of Inlet Position 0~200mm on the bottom reboiler return port.The introducing of inert gas, on the one hand
Oxygen partial pressure in oxygen-removing tower is reduced, oxygen-removing tower reboiler heat is saved and is up to 25%, on the other hand reduce deoxygenation Tower System, especially
It is the concentration of tower top oxygen into return tank, reduces corrosion risk.
The deoxygenation column overhead operating pressure be gauge pressure 0.5MPa~0.7MPa, more preferably gauge pressure 0.55MPa~
0.65MPa；Deoxygenation tower top is forced into gauge pressure 0.5MPa~0.7MPa, operates relative to low pressure, C5 or more group in tower top fixed gas
Divide and significantly reduce, effectively reduce loss of material, avoids the fuel gas carrying liquid of discharge.
The deoxygenation column overhead operation temperature is 85 DEG C~148 DEG C, and the oxygen-removing tower gas-phase space operation temperature is 155 DEG C
~200 DEG C；The mass ratio (0.04~0.1) of the secondary stripped oil phase and charging: 1 more preferable (0.05~0.08): 1
The corrosion inhibiter is passivation membranous type corrosion inhibiter, the implantation quality of corrosion inhibiter be overhead liquid reflux mass 0.05%~
0.1%。
Enter corrosion inhibiter in oxygen-removing tower teeming, effectively slows down the corrosion of tower top to return tank.
The feed naphtha is not more than 90 DEG C after the heat exchange of tower bottom heat exchanger tube pass, into the oxygen-removing tower temperature,
Pipeline flow velocity is not less than 1.0m/s.Research shows that when feed naphtha oxygen content reaches 10mg/kg, insatiable hunger at 100 DEG C of temperature or more
It is likely to occur more apparent polymerization tendency with hydrocarbon, described remove is entered when feed naphtha oxygen content is less than or equal to 9 mg/kg
Oxygen column temperature is not more than 90 DEG C, when feed naphtha oxygen content is greater than 9 mg/kg, is not more than into the oxygen-removing tower temperature
85 DEG C, pipeline flow velocity is not less than 1.0m/s, effectively avoids oxygen-removing tower reflux-tower bottom heat exchanger tube pass fouling；The naphtha is former
Material entrance is extended to away from oxygen-removing tower return tank bottom 150mm.
The utilization of this example is merely to illustrate the protection scope that the present invention is not intended to limit the present invention.In addition, having read this
After the technology contents of invention, those skilled in the art can make various changes, modification or modification to the present invention, all these
Equivalent form also belongs within the required protection scope limited of the application.
Claims (10)
1. a kind of naphtha deaerating type of cycles, which is characterized in that the system comprises deoxygenation return tank, condenser, oxygen-removing tower reflux
Pump, tower bottom heat exchanger plus hydrogen feed pump, bottom reboiler, oxygen-removing tower, corrosion inhibiter storage device and inert gas storage device,
The oxygen-removing tower includes oxygen-removing tower gas-phase space；The condenser by pipeline respectively with the deoxygenation column overhead and the deoxygenation
Return tank connection, the deoxygenation return tank, the oxygen-removing tower reflux pump and the tower bottom heat exchanger pass through pipeline successively line,
The tower bottom heat exchanger respectively with the deoxygenation column overhead, the oxygen-removing tower tower bottom, the bottom reboiler and described plus hydrogen into
Material pump is connected by pipeline, and the bottom reboiler connect with the oxygen-removing tower gas-phase space, it is described add hydrogen feed pump with it is described
Oxygen-removing tower tower bottom is connected by pipeline, and the inert gas storage device is connect with the oxygen-removing tower gas-phase space.
2. a kind of naphtha deaerating type of cycles according to claim 1, which is characterized in that the deoxygenation return tank includes naphtha
Feed(raw material)inlet, gas-liquid entrance, fuel discharge pipe, deoxygenation return tank gas-phase space and deoxygenation return tank raw material space；The condensation
Device is connect with the gas-liquid entrance, and the deoxygenation return tank gas-phase space is connected to the gas-liquid entrance and fuel discharge pipe, institute
Deoxygenation return tank raw material space is stated to connect with the feed naphtha entrance.
3. a kind of naphtha deaerating type of cycles according to claim 1, which is characterized in that the tower bottom heat exchanger and the deoxygenation
Valve is installed, the valve is triple valve or bypass valve, and the oxygen-removing tower tower bottom is changed with the tower bottom between tower tower bottom
Pipeline and described plus between hydrogen feed pump and the oxygen-removing tower tower bottom pipeline between hot device are connected on the valve.
4. a kind of naphtha deoxidation method, which is characterized in that by tank field Lai through filtering out the feed naphtha of impurity, right of access
Benefit requires any one of 1 ~ 3 naphtha deaerating type of cycles to be handled, feed naphtha filtered first entered described in remove
At oxygen return tank tank bottom, after oxygen-removing tower reflux pump pressurization, exchange heat into the tower bottom heat exchanger tube pass, subsequently into institute
It states oxygen-removing tower and carries out stripping deoxygenation, mixed in the gas of the deoxygenation tower top with corrosion inhibiter, entered after condenser condensation
The oxygen-removing tower return tank gas-phase space, fixed gas are discharged into fuel gas system by the fuel discharge pipe, and oil mutually flows back, reflux
Oil mutually be secondary stripped oil phase, through oxygen-removing tower reflux pump pressurization after return oxygen-removing tower carry out stripping deoxygenation again；
Tower bottom is heated using the bottom reboiler, and inert gas enters the oxygen-removing tower gas-phase space and bottom reboiler
The heat of offer strips deoxygenation together, most afterwards through tower bottom heat exchanger and the secondary stripped oil phase and the hydrogenated charging of raw material heat exchange
It is pumped into downstream units.
5. a kind of naphtha deoxidation method according to claim 4, which is characterized in that the inert gas is nitrogen or fuel
Gas, the ratio between volume flow and the volume flow of fixed gas of inert gas are 1:(3 ~ 5), Inlet Position is in the bottom reboiler
The position of 0~200mm on return port.
6. a kind of naphtha deoxidation method according to claim 4, which is characterized in that the deoxygenation column overhead operating pressure
For gauge pressure 0.5MPa~0.7MPa；The deoxygenation column overhead operation temperature is 85 DEG C~148 DEG C, the oxygen-removing tower gas-phase space behaviour
Making temperature is 155 DEG C~200 DEG C, and the mass ratio of the secondary stripped oil phase and charging is (0.04~0.1): 1.
7. a kind of naphtha deoxidation method according to claim 4, which is characterized in that the corrosion inhibiter is that passivation membranous type is slow
Agent is lost, the implantation quality of corrosion inhibiter is the 0.05%~0.1% of overhead liquid reflux mass.
8. a kind of naphtha deoxidation method according to claim 4, which is characterized in that the feed naphtha exchanges heat through tower bottom
After the heat exchange of device tube side, it is not more than 90 DEG C into the oxygen-removing tower temperature, is not less than 1.0m/s in pipeline flow velocity.
9. a kind of naphtha deoxidation method according to claim 4, which is characterized in that the feed naphtha entrance extend to away from
At oxygen-removing tower return tank bottom 150mm.
10. a kind of naphtha deoxidation method according to claim 4, which is characterized in that feed naphtha and the secondary vapour
It mentions oily mutually together into deoxygenation reflux pump pressurization.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920834A (en) * | 2021-01-25 | 2021-06-08 | 琪优势化工(太仓)有限公司 | Alkane deoxidation tower system for slowing down corrosion of tower wall |
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| CN205974402U (en) * | 2016-07-05 | 2017-02-22 | 东营奥星石油化工有限公司 | Base oil is fractionating system in advance |
| CN205874318U (en) * | 2016-07-15 | 2017-01-11 | 茂名市银峰石化有限公司 | Naphtha anti -corrosion treatment system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112920834A (en) * | 2021-01-25 | 2021-06-08 | 琪优势化工(太仓)有限公司 | Alkane deoxidation tower system for slowing down corrosion of tower wall |
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