CN207193211U - A kind of gasoline system of processing - Google Patents
A kind of gasoline system of processing Download PDFInfo
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- CN207193211U CN207193211U CN201721208784.2U CN201721208784U CN207193211U CN 207193211 U CN207193211 U CN 207193211U CN 201721208784 U CN201721208784 U CN 201721208784U CN 207193211 U CN207193211 U CN 207193211U
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Abstract
Gasoline manufacture field is the utility model is related to, discloses a kind of gasoline system of processing, the system includes：Gasoline Cutting Tap (1), gasoline Cutting Tap (1) are used to gasoline being cut into light gasoline fraction, middle gasoline fraction and heavy naphtha；Selective hydrodesulfurization reactor (2), selective hydrodesulfurization reactor (2) are used to carry out selective hydrodesulfurization processing to heavy naphtha, obtain sulfur-free gasoline；Extraction distillation tower (3), extraction distillation tower (3) are stripped distillation for centering gasoline fraction, and extraction distillation tower (3) tower top obtains that raffinate is non-aromatic, and bottom of towe obtains the rich solvent containing aromatic hydrocarbons and sulfide；Methyltertiarvbutyl ether reactor (4), methyltertiarvbutyl ether reactor (4) are used to carry out etherification reaction to light gasoline fraction；The non-aromatic Cutting Tap of raffinate (15), the non-aromatic Cutting Tap of raffinate (15) are used for cut non-aromatic to raffinate.Gasoline system of processing energy consumption provided by the utility model is low, desulfuration efficiency is high, and loss of octane number is relatively low.
Description
Technical field
Gasoline manufacture field is the utility model is related to, in particular it relates to a kind of gasoline system of processing.
Background technology
As people are to the pay attention to day by day of environmental protection, environmental regulation is also increasingly strict, and reduces the sulfur content quilt of gasoline
It is considered to improve one of most important measure of air quality.Most of sulphur in China's gasoline products come from hot-working petroleum tune
Charge-coupled point, such as catalytically cracked gasoline.Therefore, it is necessary to catalytically cracked gasoline is subjected to deep desulfuration, simple catalytic gasoline desulfurization
Technology can all bring a problem：The octane number of catalytic gasoline declines.
In order on the premise of certain desulfurization depth is ensured, make as far as possible few alkene saturation, at present, the work of researcher's exploitation
Skill technology mainly has：The S-zorb technologies of sinopec exploitation, the RSDS technique of sinopec Research Institute of Petro-Chemical Engineering exploitation, with
And French Prime-G+ technologies.
The S-zorb technologies of sinopec exploitation are used for full cut catalytic gasoline desulfurization, and sulfur content can control after desulfurization
Below 10ppm, the loss of octane number of full cut catalytic gasoline is in 1-2 unit.Sinopec Research Institute of Petro-Chemical Engineering develops
RSDS technique catalytic gasoline is first cut into light and heavy fractions, extraction desulfurization alcohol is passed through in light fraction, and selective hydrogenation is gone in heavy distillat
Desulfurization, when the product sulfur content of the technology is less than 10ppm, light fraction yield about 20%, largely need to be hydrogenated with, full cut vapour
About 3-4 unit of oily loss of octane number.Gasoline is hydrogenated with by French Prime-G+ technologies in advance before gasoline cutting is carried out,
Lighter sulfide and alkadienes are acted on forming high boiling sulfide by pre- hydrogenation process, and alkene is not saturated, the technology
Loss of octane number be also about 3-4 unit.
In addition, departments of government currently actively ferments state's VI standards, state's V gasoline standards to state's VI gasoline standards
The colleague that quality upgrading essentially consists in reduction content of sulfur in gasoline strictly controls mercaptan sulfur content, state's V gasoline standards to state's VI gasoline
The quality upgrading of standard also includes adjustment Benzene In Gasoline (being not more than 0.8% (v)), aromatic hydrocarbons (being not more than 38% (v)), alkene (no
More than 18% (v)) content, while strict control gasoline reconciles and combined (for example, control saturated vapor pressure and T50 indexs).
Therefore, while deep desulfurization of gasoline can be realized by needing one kind badly, the gasoline system of processing of loss of octane number is reduced,
And it is the quality upgrading spare interface of state VI gasoline standards from now on.
Utility model content
During existing gasoline hydrodesulfurizationmethod, the defects of loss of octane number is serious, the utility model provides a kind of vapour
Oily system of processing.The gasoline system of processing energy consumption is low, desulfuration efficiency is high, and loss of octane number is relatively low, and is state VI vapour from now on
The quality upgrading spare interface of oil standard.
Inventor of the present utility model has found that it is in horse that the RON (research octane number (RON)) of catalytic gasoline, which is, in research process
Saddle distribution, low between Liang Duan senior middle schools, leading portion octane number is contributed mainly by alkene, and rear end is contributed mainly by aromatic hydrocarbons, and with urging
Change the increase of gasoline endpoint, olefin(e) centent gradually reduces, and alkene is mainly distributed on -135 DEG C of initial boiling point with tails.For
Both ensure gasoline Research octane number, control olefin(e) centent to meet state's VI gasoline standards again, inventor of the present utility model exists
Further research process are found, in gasoline process, gasoline first is cut into light gasoline fraction, middle gasoline fraction and again
Gasoline fraction, light gasoline fraction is then subjected to etherification process, middle gasoline fraction is stripped distillation processing, and heavy naphtha enters
Row selective hydrodesulfurization is handled, and effectively can be separated alkene and sulfide, and middle gasoline fraction is stripped distillation processing
The non-aromatic and sulfur-rich aromatic hydrocarbons of raffinate is obtained, by being cut to obtain light fraction and again into the non-aromatic Cutting Tap of raffinate by raffinate is non-aromatic
Cut, light fraction (octane contribution is high) is used for blended gasoline, and heavy distillat (octane contribution is low) can be used as reformer feed,
Avoided by the technical scheme in sweetening process, loss of octane number caused by the saturation of alkene, and be state VI gasoline from now on
The quality upgrading spare interface of standard.
Based on this, the utility model provides a kind of gasoline system of processing, and the system includes：
Gasoline Cutting Tap, the gasoline Cutting Tap are used to gasoline being cut into light gasoline fraction, middle gasoline fraction and weight vapour
Oil distillate；
Selective hydrodesulfurization reactor, the selective hydrodesulfurization reactor are used to carry out the heavy naphtha
Selective hydrodesulfurization is handled, and obtains sulfur-free gasoline；
Extraction distillation tower, the extraction distillation tower are used to be stripped distillation, extraction distillation tower to the middle gasoline fraction
Tower top obtains that raffinate is non-aromatic, and bottom of towe obtains the rich solvent containing aromatic hydrocarbons and sulfide；
Methyltertiarvbutyl ether reactor, the methyltertiarvbutyl ether reactor are used to carry out etherification reaction to the light gasoline fraction, obtain being etherified vapour
Oil；And
The non-aromatic Cutting Tap of raffinate, the non-aromatic Cutting Tap of raffinate are used for cut non-aromatic to the raffinate.
Preferably, the extractive distillation column overhead is provided with reflux pipeline, and return tank is connected with reflux pipeline, described
Raffinate is non-aromatic to be partly recycled in extraction distillation tower tower by return tank, and remainder is cut into the non-aromatic Cutting Tap of raffinate
Cut, obtain product and go out device.
Preferably, cooler is provided with the reflux pipeline that the extractive distillation column overhead is set.
Preferably, the system also includes：First stripper, first stripper are used to contain aromatic hydrocarbons and vulcanization by described in
The rich solvent of thing is stripped to obtain solvent and sulfur-rich aromatic hydrocarbons；Bottom of towe outlet and first stripper of the extraction distillation tower
Entrance connection.
Preferably, the bottom of towe outlet of first stripper connects with the entrance of extraction distillation tower.
Preferably, the system also includes：The reformer and aromatic extraction unit connected by pipeline, the reformer
Entrance connected with the tower top outlet of first stripper.
Preferably, the reformer includes the reformed pre-hydrogenated processor and reforming reactor connected by pipeline, institute
Stating reformed pre-hydrogenated processor also includes reformer feed entrance, the reformed pre-hydrogenated processor be used to removing reformer feed and
Poison the material of reforming catalyst in sulfur-rich aromatic hydrocarbons, the reforming reactor is used to carry out catalytic reforming reaction.
Preferably, reforming reaction product Cutting Tap is connected between the reforming reactor and aromatic extraction unit, it is described
The tower top outlet of reforming reaction product Cutting Tap connects with the entrance of aromatic extraction unit.
Preferably, the system also includes：For carrying out the gasoline pre-hydrotreating device of weighted BMO spaces, the vapour to gasoline
The outlet of oily pre-hydrotreating device connects with the entrance of gasoline Cutting Tap.
Preferably, the system also includes the second stripper for being connected with selective hydrodesulfurization reactor outlet, and described the
Two strippers are used for the hydrogen sulfide being stripped off in the sulfur-free gasoline.
The defects of the utility model is directed to during existing gasoline hydrodesulfurizationmethod, and loss of octane number is serious, and combine state
The new demand that VI gasoline standards propose to gasoline, it is creative using gasoline Cutting Tap by gasoline be cut into light gasoline fraction, in
Gasoline fraction and heavy naphtha, light gasoline fraction is then subjected to etherification process, middle gasoline fraction in extraction distillation tower and
Solvent is stripped distillation so that sulfide and aromatic hydrocarbons are dissolved in solvent in middle gasoline fraction, effectively by sulfide and alkene group
Point separate, and raffinate that middle gasoline fraction extractive distillation is obtained is non-aromatic is cut, and obtained heavier fraction can conduct
Reformer feed.Sulfur-rich aromatic hydrocarbons and reformer feed are further preferably subjected to reforming reaction jointly, then carry out Aromatics Extractive Project, the mistake
Heavy olefins in the less middle gasoline fraction of octane contribution can be used to produce aromatic hydrocarbons by journey, effectively adjust in gasoline products
Each component content.
Using gasoline system of processing provided by the utility model, alkene can be avoided while effectively removing sulfur in gasoline
Loss of octane number caused by the saturation of hydrocarbon, and be the quality upgrading spare interface of state VI gasoline standards from now on.The utility model carries
Compared with prior art, following advantage be present in the gasoline system of processing of confession：
(1) extractive distillation technical finesse gasoline fraction is used, the solvent carrying problem of treated gasoline is solved, eliminates essence
The washing of gasoline processed, so as to the discharge for reducing plant running energy consumption, avoiding sour water, while also just it is not present to washing
The refined problem of water；
(2) extractive distillation technology is used, alkene polarity and the race problem of sulfide polarity and solvent is solved, is not present
The problem of high-octane olefin component is lost in sulfur-rich aromatic component, therefore washing oil circulation need not be returned, so energy consumption is low；
(3) the problem of the utility model is lost in sulfur-rich aromatic component in the absence of high-octane olefin component, therefore
The pentane component of anti-top light olefin need not be added for this, so device material consumption is low；
(4) because no light component returns washing lotion circulation, eliminate and return washing lotion tower, so device, which is not present, rushes tower, foaming etc.
Problem, improve plant running stability；
(5) alkene, aromatic hydrocarbons and benzene content in gasoline pool can be adjusted flexibly according to their needs in enterprise.
Other features and advantages of the utility model will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is to be further understood for providing to of the present utility model, and a part for constitution instruction, and following
Embodiment be used to explain the utility model together, but do not form to limitation of the present utility model.In the accompanying drawings：
Fig. 1 is a kind of gasoline system of processing of embodiment provided by the utility model.
Description of reference numerals
1- gasoline Cutting Tap 2- selective hydrodesulfurization reactor 3- extraction distillation towers
4- methyltertiarvbutyl ether reactor 5- gasoline pre-hydrotreating device the first strippers of 6-
7- the first reboiler 8- the second stripper 9- coolers
The non-aromatic Cutting Taps of reboiler 15- raffinates of the second reboilers of 10- 11- the 3rd
The reformed pre-hydrogenated processor 162- reforming reactors 17- aromatic extraction units of 161-
18- return tank 19- reforming reaction product Cutting Taps
Embodiment
Specific embodiment of the present utility model is described in detail below.It is it should be appreciated that described herein
Embodiment is merely to illustrate and explained the utility model, is not limited to the utility model.
In the utility model, in the case where not making opposite explanation, the noun of locality such as " upper and lower " used typically refers to join
Examine shown in the drawings upper and lower, the noun of locality used typically refers to top, the bottom shown in refer to the attached drawing such as " top, bottom ", makes
The noun of locality such as " inside and outside " refers to the inside and outside of the profile relative to each part in itself.
The utility model provides a kind of gasoline system of processing, and the system includes：
Gasoline Cutting Tap 1, the gasoline Cutting Tap 1 are used to gasoline being cut into light gasoline fraction, middle gasoline fraction and again
Gasoline fraction；
Selective hydrodesulfurization reactor 2, the selective hydrodesulfurization reactor 2 are used to enter the heavy naphtha
Row selective hydrodesulfurization is handled, and obtains sulfur-free gasoline；
Extraction distillation tower 3, the extraction distillation tower 3 are used to be stripped distillation, extractive distillation to the middle gasoline fraction
The tower top of tower 3 obtains that raffinate is non-aromatic, and bottom of towe obtains the rich solvent containing aromatic hydrocarbons and sulfide；
Methyltertiarvbutyl ether reactor 4, the methyltertiarvbutyl ether reactor 4 are used to carry out etherification reaction to the light gasoline fraction, are etherified
Gasoline；And
The non-aromatic Cutting Tap 15 of raffinate, the non-aromatic Cutting Tap 15 of raffinate are used for cut non-aromatic to the raffinate.
In the utility model, to gasoline Cutting Tap, selective hydrodesulfurization reactor, extraction distillation tower, etherification reaction
There is no particular limitation for the concrete structure of device and the non-aromatic Cutting Tap of raffinate, can be various devices commonly used in the art.
In the utility model, as long as the gasoline Cutting Tap can realize the cutting function of gasoline, it is preferable that institute
Gasoline Cutting Tap is stated to be used to gasoline being cut into light gasoline fraction, middle gasoline fraction and heavy naphtha, and the preferably light vapour
The cut point of oil distillate and middle gasoline fraction is 60-80 DEG C, and the cut point of the middle gasoline fraction and heavy naphtha is 120-
150℃。
In the utility model, polar extraction and weight separated are carried out simultaneously in the extraction distillation tower, whole
Existing aromatic hydrocarbons, alkene, the polarity competition process of sulfide (mercaptan, thioether, thiophene) during individual, also there is light-heavy material distillation point
From process.Solvent polarity extracted character can be so played to greatest extent, can also embody component weight stalling characteristic so that molten
The sulfide that agent is carried in aromatic component and middle gasoline forms sulfur-rich aromatic hydrocarbons, alkene is hardly visible in sulfur-rich aromatic hydrocarbons, in essence
It is difficult to find sulfide in middle gasoline after system, and then loss of octane number can be reduced while deep desulfurization of gasoline is realized.
The utility model solves alkene polarity and the race problem of sulfide polarity and solvent, in the absence of high-octane
The problem of olefin component is lost in sulfur-rich aromatic component, therefore washing oil circulation need not be returned, enter without returning washing oil circulation
Relevant apparatus.
The problem of the utility model is lost in sulfur-rich aromatic component in the absence of high-octane olefin component, therefore be not required to
The pentane component of anti-top light olefin is added for this, therefore the relevant apparatus of the pentane component of anti-top light olefin need not be added.
The utility model due to no light component return washing lotion circulation, eliminate and return washing lotion tower, thus device be not present rush tower,
The problems such as foaming, improve plant running stability.
According to a kind of preferred embodiment of the present utility model, the tower top of extraction distillation tower 3 is provided with reflux pipeline, and
Return tank 18 is connected with reflux pipeline, the raffinate is non-aromatic to be partly recycled in the tower of extraction distillation tower 3 by return tank 18, is remained
Remaining part point is cut into the non-aromatic Cutting Tap 15 of raffinate, is obtained product and is gone out device.
According to a kind of preferred embodiment of the present utility model, on the reflux pipeline that the tower top of extraction distillation tower 3 is set
It is provided with cooler 9.The cut that this kind of preferred embodiment is more beneficial for distilling the tower top of extraction distillation tower 3 carries molten
Agent replaces.
The cooler 9 is used to cool down the cut that the tower top of extraction distillation tower 3 distills.
In the utility model, after the non-aromatic partial reflux of raffinate, remainder can take part directly individually storage,
As gasoline blend component product, according to the difference of gasoline pool blend component, the harmonic proportion of middle gasoline is adjusted flexibly, can be with
The remainder is cut into the non-aromatic Cutting Tap 15 of raffinate, distinguished in the tower top and bottom of towe of the non-aromatic Cutting Tap 15 of raffinate
Light fraction (octane contribution is high) and heavy distillat (octane contribution is low) are obtained, the heavy distillat that can be obtained cutting is as reformation
Raw material, obtained light fraction will be cut as gasoline blend component product.Using this kind of embodiment, can cut off to octane number
Small heavier olefins are contributed, are more beneficial for meeting requirement of state's VI gasoline standards to olefin(e) centent.
There is no particular limitation to the cut point in the non-aromatic Cutting Tap of above-mentioned raffinate 15 for the utility model, and preferably cut point exists
Between 110-140 DEG C.
There is no particular limitation for concrete structure of the utility model to the non-aromatic Cutting Tap of the raffinate 15, as long as can be used in
The non-aromatic cutting of the raffinate, can be various Cutting Taps commonly used in the art.
According to a kind of preferred embodiment of the present utility model, the system also includes：For carrying out being hydrogenated with pre- place to gasoline
The gasoline pre-hydrotreating device 5 of reason, the outlet of the gasoline pre-hydrotreating device 5 connect with the entrance of gasoline Cutting Tap 1.
Before gasoline is cut, by the way that gasoline is carried out into pre-hydrotreating, the pre-hydrotreating causes in gasoline
Alkadienes saturation, small molecule sulfide is converted into macromolecular sulfide.This kind of preferred embodiment is advantageous to obtain sulfur content
Relatively low light gasoline fraction, so as to avoid loss of octane number to greatest extent.
According to a kind of preferred embodiment of the present utility model, the system also includes：First stripper 6, first vapour
Stripper 6 is used to be stripped the rich solvent containing aromatic hydrocarbons and sulfide to obtain solvent (bottom of towe) and sulfur-rich aromatic hydrocarbons (tower
Top)；The bottom of towe outlet of the extraction distillation tower 3 connects with the entrance of first stripper 6.Extraction distillation tower 3 by aromatic hydrocarbons and
Sulfide is dissolved in solvent, effectively separates sulfide and alkene, by the richness containing aromatic hydrocarbons and sulfide of the bottom of towe of extraction distillation tower 3
Solvent is sent into the first stripper 6 and stripped, and solvent and sulfur-rich aromatic hydrocarbons is efficiently separated, the solvent that bottom of towe obtains goes out device.
In the utility model, it is preferable that as shown in figure 1, the bottom of towe outlet of first stripper 6 and extraction distillation tower
3 entrance connection.The bottom of towe of first stripper 6 obtains recycling in solvent feeding extraction distillation tower 3.
According to the utility model, the bottom of towe of the first stripper 6 obtains being sent into extractive distillation after solvent may also pass through regeneration
Recycled in tower 3.There is no particular limitation to this for the utility model, and those skilled in the art can be carried out as the case may be
Appropriate selection.
According to the utility model, it is preferable that the system also includes：The reformer and Aromatics Extractive Project connected by pipeline fills
17 are put, the entrance of the reformer connects with the tower top outlet of first stripper 6.
According to the utility model, it is preferable that the reformer includes the reformed pre-hydrogenated processor connected by pipeline
161 and reforming reactor 162, the reformed pre-hydrogenated processor 161 also include reformer feed entrance, the reformed pre-hydrogenated place
Reason device 161 is used to remove the material for poisoning reforming catalyst in reformer feed and sulfur-rich aromatic hydrocarbons, and the reforming reactor 162 is used
In progress catalytic reforming reaction (obtaining reforming reaction product).
According to a kind of preferred embodiment of the present utility model, the reforming reactor 162 and aromatic extraction unit 17 it
Between be connected with reforming reaction product Cutting Tap 19, the tower top outlet and aromatic extraction unit of the reforming reaction product Cutting Tap 19
17 entrance connection.
Using above-mentioned preferred embodiment of the present utility model, the sulfur-rich aromatic hydrocarbons that the tower top of the first stripper 6 can be obtained
Enter reformed pre-hydrogenated processor 161 and reforming reactor 162 after being mixed with naphtha jointly, in reformed pre-hydrogenated processor
Reformed pre-hydrogenated reaction is carried out in 161, the sulphur in reformer feed and sulfur-rich aromatic hydrocarbons, nitrogen, oxygen etc. can be poisoned into reforming catalyst
Devolatilization, the reaction product of reformed pre-hydrogenated processor 161 enters reforming reactor 162, enters in reforming reactor 162
Row catalytic reforming reaction, obtained reforming reaction product is sent into reforming reaction product Cutting Tap 19, the cutting of reforming reaction product
The bottom of towe of tower 19 obtains Reformed Gasoline, and the material that tower top obtains is sent into aromatic extraction unit 17, Aromatics Extractive Project as extracting raw material
The top of device 17 obtains aromatic hydrocarbons (mainly including C6-C8), and the product (low value-added C9 and C10) that bottom obtains can be used as vapour
Oily blend component recalls to gasoline pool.
It should be noted that the utility model is to reforming cut point and Aromatics Extractive Project in reaction product Cutting Tap 19
There is no particular limitation for actual conditions, and those skilled in the art can suitably be selected according to the actual conditions that gasoline reconciles.
There is no particular limitation to the aromatic extraction unit 17 for the utility model, can be commonly used in the art each
Kind aromatic extraction unit, as long as the extracting of aromatic hydrocarbons can be realized.
According to a kind of preferred embodiment of the present utility model, the bottom of first stripper 6 is provided with first and boiled again
Device 7.
According to a kind of preferred embodiment of the present utility model, the system also includes and selective hydrodesulfurization reactor 2
Second stripper 8 of outlet, second stripper 8 are used for the hydrogen sulfide being stripped off in the sulfur-free gasoline.In this reality
In new, hydrogenation saturated reaction is both carried out in selective hydrodesulfurization reactor 2, carries out hydrodesulfurization reaction again, can be with
Selective hydrodesulfurization reaction condition is selected according to actual conditions.Alkene in heavy naphtha is to the lighter vapour of octane contribution
Oil distillate and middle gasoline fraction are small, in order to meet requirement of state's VI gasoline standards to olefin(e) centent, can react bar by controlling
Part controls the saturation capacity of alkene.The utility model preferred embodiment being capable of flexible modulation alkene, aromatic hydrocarbons and benzene content.
According to a kind of preferred embodiment of the present utility model, the bottom of second stripper 8 is provided with second and boiled again
Device 10.
According to a kind of preferred embodiment of the present utility model, the bottom of the extraction distillation tower 3 is provided with the 3rd and boiled again
Device 11.
Specific set location of the utility model to first reboiler 7, the second reboiler 10 and the 3rd reboiler 11
And there is no particular limitation for concrete structure, can be selected according to this area conventional technical means.
Reboiler is set to be used to heat steam in the first stripper 6, the second stripper 8 and extraction distillation tower 3, after heating
Steam be used for strip or extract.
Hereinafter, a kind of preferred embodiment of the present utility model is illustrated with reference to Fig. 1.
Pending gasoline is passed through in gasoline pre-hydrotreating device 5 and carries out pre-hydrotreating reaction, products therefrom introduces gasoline and cut
Cut in tower 1, gasoline is cut into three light gasoline fraction, middle gasoline fraction and heavy naphtha cuts, wherein, light gasoline fraction
Etherification reaction is carried out into methyltertiarvbutyl ether reactor 4, obtains etherified gasoline, heavy naphtha enters selective hydrodesulfurization reactor 2
Middle progress selective hydrodesulfurization reaction, obtains sulfur-free gasoline, and middle gasoline fraction enters extraction distillation tower 3, and (bottom is provided with the
Three reboilers 11 are used to heat steam), meanwhile, solvent is introduced into extraction distillation tower 3, is stripped in extraction distillation tower 3
Distillation, the tower top of extraction distillation tower 3 is provided with reflux pipeline, and cooler 9 and return tank 18 are provided with reflux pipeline, from extracting
The raffinate containing alkene and saturated hydrocarbons that the tower top of destilling tower 3 distills enters return tank 18, part after the cooling of cooler 9
Backflow, partly it is sent into the non-aromatic Cutting Tap 15 of raffinate as gasoline blend component, part and is cut, the heavy distillat that bottom of towe obtains can
So that as reformer feed, the light fraction that tower top obtains can be used as gasoline blend component.The bottom of towe of extraction distillation tower 3 obtains carrying aromatic hydrocarbons
The rich solvent of component and the sulfide in middle gasoline, extractive distillation effectively open sulfide and separation of olefins, carry aromatic hydrocarbons group
Point and sulfide in middle gasoline rich solvent be passed through the first stripper 6 (bottom be provided with the first reboiler 7 be used for heat steaming
Vapour), stripped, isolate lean solvent circuit time extraction distillation tower 3 and recycle, the tower top of the first stripper 6 obtains sulfur-rich
Aromatic hydrocarbons and naphtha (reformer feed) enter reformed pre-hydrogenated processor 161 jointly, remove sulfur-rich aromatic hydrocarbons with it is miscellaneous in naphtha
Matter (sulphur, oxygen, nitrogen), reforming reaction is carried out subsequently into reforming reactor 162, the product of reforming reaction is sent into reforming reaction production
Thing Cutting Tap 19, the bottom of towe of reforming reaction product Cutting Tap 19 obtain Reformed Gasoline, and overhead fraction is sent into aromatic extraction unit 17
Aromatics Extractive Project is carried out, tower top obtains aromatic hydrocarbons (mainly including C6-C8), and the product (low value-added C9 and C10) that bottom of towe obtains can
To recall to gasoline pool as gasoline blend component.The bottom of towe outlet of selective hydrodesulfurization reactor 2 is also associated with the second stripping
Tower 8 (bottom is provided with the second reboiler 10 and is used to heat steam), is used to the sulfur-free gasoline be stripped off by the second stripper 8
In hydrogen sulfide.
Using gasoline system of processing provided by the utility model, can be adjusted flexibly alkene in gasoline pool, aromatic hydrocarbons and
Benzene content, it is state VI gasoline standard spare interfaces, and while effectively removing sulfur in gasoline, avoids the saturation of alkene from causing
Loss of octane number.
Preferred embodiment of the present utility model, still, the utility model and unlimited is described in detail above in association with accompanying drawing
Detail in above-mentioned embodiment, can be to skill of the present utility model in range of the technology design of the present utility model
Art scheme carries out a variety of simple variants, and these simple variants belong to the scope of protection of the utility model.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, it can be combined by any suitable means.
In addition, it can also be combined between a variety of embodiments of the present utility model, as long as it is not disobeyed
Thought of the present utility model is carried on the back, it should equally be considered as content disclosed in the utility model.
Claims (10)
1. a kind of gasoline system of processing, it is characterised in that the system includes：
Gasoline Cutting Tap (1), the gasoline Cutting Tap (1) are used to gasoline being cut into light gasoline fraction, middle gasoline fraction and again
Gasoline fraction；
Selective hydrodesulfurization reactor (2), the selective hydrodesulfurization reactor (2) are used to enter the heavy naphtha
Row selective hydrodesulfurization is handled, and obtains sulfur-free gasoline；
Extraction distillation tower (3), the extraction distillation tower (3) are used to be stripped distillation, extractive distillation to the middle gasoline fraction
Tower (3) tower top obtains that raffinate is non-aromatic, and bottom of towe obtains the rich solvent containing aromatic hydrocarbons and sulfide；
Methyltertiarvbutyl ether reactor (4), the methyltertiarvbutyl ether reactor (4) are used to carry out etherification reaction to the light gasoline fraction, are etherified
Gasoline；And
The non-aromatic Cutting Tap of raffinate (15), the non-aromatic Cutting Tap of raffinate (15) are used for cut non-aromatic to the raffinate.
2. gasoline system of processing according to claim 1, it is characterised in that extraction distillation tower (3) tower top is provided with
Reflux pipeline, and return tank (18) is connected with reflux pipeline, non-aromatic be partly recycled to by return tank (18) of the raffinate is taken out
Carry in destilling tower (3) tower, remainder is cut into the non-aromatic Cutting Tap of raffinate (15), is obtained product and is gone out device.
3. gasoline system of processing according to claim 1, it is characterised in that what extraction distillation tower (3) tower top was set
Cooler (9) is provided with reflux pipeline.
4. gasoline system of processing according to claim 1, it is characterised in that the system also includes：First stripper (6),
First stripper (6) is used to be stripped to obtain solvent and sulfur-rich virtue by the rich solvent containing aromatic hydrocarbons and sulfide
Hydrocarbon；The bottom of towe outlet of the extraction distillation tower (3) connects with the entrance of first stripper (6).
5. gasoline system of processing according to claim 4, it is characterised in that the bottom of towe outlet of first stripper (6)
Connected with the entrance of extraction distillation tower (3).
6. gasoline system of processing according to claim 4, it is characterised in that the system also includes：Connected by pipeline
Reformer and aromatic extraction unit (17), the entrance of the reformer and the tower top outlet of first stripper (6) connect
It is logical.
7. gasoline system of processing according to claim 6, it is characterised in that the reformer includes connecting by pipeline
Reformed pre-hydrogenated processor (161) and reforming reactor (162), the reformed pre-hydrogenated processor (161) also include reform
Feed(raw material)inlet, the reformed pre-hydrogenated processor (161) are used to remove in reformer feed and sulfur-rich aromatic hydrocarbons to poison Reforming catalyst
The material of agent, the reforming reactor (162) are used to carry out catalytic reforming reaction.
8. gasoline system of processing according to claim 7, it is characterised in that the reforming reactor (162) and aromatic hydrocarbons are taken out
Carry and be connected with reforming reaction product Cutting Tap (19) between device (17), the tower top of the reforming reaction product Cutting Tap (19) goes out
Mouth connects with the entrance of aromatic extraction unit (17).
9. the gasoline system of processing according to any one in claim 1-8, it is characterised in that the system also includes：With
In the gasoline pre-hydrotreating device (5) that weighted BMO spaces are carried out to gasoline, the outlet of the gasoline pre-hydrotreating device (5) and vapour
The entrance connection of oily Cutting Tap (1).
10. the gasoline system of processing according to any one in claim 1-8, it is characterised in that
The system also includes the second stripper (8) with selective hydrodesulfurization reactor (2) outlet, second stripping
Tower (8) is used for the hydrogen sulfide being stripped off in the sulfur-free gasoline.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112933658A (en) * | 2021-01-25 | 2021-06-11 | 北方华锦化学工业股份有限公司 | Method and device for reducing solvent in raffinate oil of aromatic extraction device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112933658A (en) * | 2021-01-25 | 2021-06-11 | 北方华锦化学工业股份有限公司 | Method and device for reducing solvent in raffinate oil of aromatic extraction device |
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