CN107974289A - A kind of processing method and system of gasoline - Google Patents
A kind of processing method and system of gasoline Download PDFInfo
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- CN107974289A CN107974289A CN201610921940.3A CN201610921940A CN107974289A CN 107974289 A CN107974289 A CN 107974289A CN 201610921940 A CN201610921940 A CN 201610921940A CN 107974289 A CN107974289 A CN 107974289A
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Abstract
The present invention relates to a kind of processing method and system of gasoline, which includes：Gasoline stocks are cut, obtain light gasoline fraction, middle gasoline fraction and heavy naphtha；Gained light gasoline fraction is subjected to etherification process, obtains etherificate oil；Gasoline fraction in gained and heavy naphtha are sent into fluidizing reactor and is contacted with mixed catalyst and desulfurization and aromatization is carried out under hydro condition, obtains sulfur-free gasoline cut；Wherein, the mixed catalyst includes absorbing desulfurization catalyst and alkene aromatized catalyst；According to the flow direction of reaction mass in the fluidizing reactor, the middle gasoline fraction feed entrance point is located at the downstream of the heavy naphtha feed entrance point.Method and system provided by the invention can reduce sulphur and olefin(e) centent in gasoline, and can improve the octane number of gasoline at the same time and keep high yield of gasoline.
Description
Technical field
The present invention relates to a kind of processing method and system of gasoline.
Background technology
Atmosphere pollution getting worse caused by motor vehicle exhaust emission.As people are to the pay attention to day by day of environmental protection, China
The paces of vehicle fuel quality upgrading are accelerated, standard GB/T 17930-2013 requires sulfur content in gasoline to be not more than 10 μ g/
G, volume fraction of olefins are not more than 24%.
Catalytically cracked gasoline is the chief component of China's motor petrol, and 75% or so is accounted in gasoline pool, and it is special
Point is that have higher alkene and sulfur content.The deep desulfuration of gasoline is realized using hydrogen addition technology and is reduced in catalytically cracked gasoline
Olefin(e) centent it is not difficult, but since alkene is antiknock component, being greatly reduced for its content will cause octane number
Heavy losses, so as to influence the automobile-used performance of gasoline and the economic benefit of oil plant, therefore realizing the deep desulfuration of gasoline
Octane number is kept to become the hot spot of China's clean gasoline production at the same time.
At present, the deep desulfuration of gasoline is mainly using hydrodesulfurization or the method for adsorbing desulfurization.
Selective hydrodesulfurization is one of major way of current removing thiophene-type sulfide, but the reaction such as alkene saturation is same
Sample largely occurs, and causes loss of octane number larger.In addition, the deep hydrogenation method for recovering octane number is similarly approved by people,
It is while deep desulfuration and alkene saturation is carried out, sets second reactor to promote the cracking hydrocarbon of low octane rating, isomery
Change and alkylated reaction, so as to achieve the purpose that to recover octane number.Chinese patent CN101845322A discloses a kind of reduction vapour
The method of sulphur and olefin(e) centent in oil, raw material catalytic cracking gasoline first pass through pre-hydrogenator removing alkadienes, subsequently into
Fractionating column cutting is fractionated into light, heavy petrol, and light petrol carries out facing hydrogen absorption desulfurization, and heavy petrol adds into selective hydrogenation reactor
Hydrogen desulfurization, reaction effluent enter back into hydro-upgrading reactor and carry out hydro-upgrading, reduce olefin(e) centent, the heavy petrol after modification
The clean gasoline of standard requirement is met with light petrol absorption desulfurization product reconciliation.Absorbing desulfurization catalyst is in gasoline
Although sulfide has good removal effect, absorption desulfurization carries out under conditions of hydrogen is faced, can saturation catalytically cracked gasoline
In alkene, especially light petrol carries out absorption desulfurization, and the olefin component octane number in light petrol is higher, can cause the pungent of gasoline
Alkane value is largely lost.
Sulfur-containing compound in absorption method removing fuel oil, is that light oil is carried out using adsorbent to face hydrogen reaction absorption, raw
Into metal sulfide or using sulfide polarity removing sulphur, hydrogen consumption is relatively low, and desulfuration efficiency is high, can produce sulfur content in 10 μ g/g
Following gasoline.Although absorbing process realizes the deep desulfuration of gasoline under the conditions of low hydrogen consumption, gasoline product octane number still omits
There is loss.Especially when handling the gasoline stocks that olefin(e) centent is high and sulfur content is high, still cause octane number loss compared with
Greatly.
For most of catalytic cracking units, for propylene enhancing and butylene yield and the octane number for improving gasoline,
It is effective method using containing the catalyst with MFI structure molecular sieve or auxiliary agent.United States Patent (USP) USP3758403 is invented
The method of ZSM-5 molecular sieve is added in catalytic cracking catalyst can improve the octane number of gasoline and increase C3~C4 alkene
Yield.But as it is known by one skilled in the art, propylene enhancing and butylene yield are to sacrifice gasoline production as cost.
Aromatizing low-carbon paraffin is the effective ways for improving low-carbon alkanes utility value.People are to high silica alumina ratio molecular sieve
Substantial amounts of research is carried out for the aromatization process of catalyst, especially using ZSM-5, ZSM-11, ZSM-21 molecular sieve as catalyst
Process carried out substantial amounts of research, and using the zeolite with MFI structure be used to produce from coking or pyrolysis gasoline low
The aromatisation of carbon hydro carbons.
The content of the invention
The object of the present invention is to provide a kind of processing method and system of gasoline, method and system provided by the invention can
The sulphur and olefin(e) centent in gasoline are reduced, and the octane number of gasoline can be improved at the same time and keep high yield of gasoline.
To achieve these goals, the present invention provides a kind of vapour oil treatment process, which includes：Gasoline is former
Material is cut, and obtains light gasoline fraction, middle gasoline fraction and heavy naphtha；Gained light gasoline fraction is carried out at etherificate
Reason, obtains etherificate oil；Gasoline fraction in gained and heavy naphtha are sent into fluidizing reactor and contacted with mixed catalyst
And desulfurization and aromatization are carried out under hydro condition, obtain sulfur-free gasoline cut；Wherein, the mixed catalyst includes inhaling
Attached desulphurization catalyst and alkene aromatized catalyst；According to the flow direction of reaction mass in the fluidizing reactor, the middle vapour
Oil distillate feed entrance point is located at the downstream of the heavy naphtha feed entrance point.
Preferably, the method further includes：Gained etherificate oil and sulfur-free gasoline cut are mixed, obtain gasoline products.
Preferably, by weight and on the basis of the weight of the alkene aromatized catalyst, the alkene aromatisation is urged
Passivation content is 0.1-5.0 weight % in agent；The passivation is included selected from least one of carbon, sulphur and nitrogen element.
Preferably, the preparation process of the alkene aromatized catalyst includes：By fresh aromatized catalyst in pre-reaction
Contacted in device with carbon containing and/or sulphur and/or nitrogen compound and carry out green coke；Or aromatized catalyst will be regenerated in pre-reaction
Contacted in device with carbon containing and/or sulphur and/or nitrogen compound and carry out green coke；Or aromatized catalyst to be generated is carried out endless
Full coke burning regeneration.
Preferably, the pre-reactor is for the reactor outside the fluidizing reactor or for positioned at the fluidised form
Change the pre lift zone in reactor.
Preferably, the preparation process of the alkene aromatized catalyst includes：Fresh aromatized catalyst is subjected to aging
Processing；Wherein, the condition of the burin-in process includes：Temperature is 500-800 DEG C, and when the time is 1-360 small, aging atmosphere is water
Vapor atmosphere.
Preferably, the micro-activity of the alkene aromatized catalyst is 20-55, and the micro-activity uses RIPP 92-
The mat activity test method of 90 catalytic cracking industry equilibrium catalysts is measured.
Preferably, volume fraction of olefins is more than 20 body % in the gasoline stocks.
Preferably, in the gasoline stocks sulfur content more than 10 μ g/g.
Preferably, the gasoline stocks are selected from catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, thermal cracking vapour
At least one of oil and direct steaming gasoline.
Preferably, the cut point of the light gasoline fraction and middle gasoline fraction be 50-80 DEG C, the middle gasoline fraction with again
The cutting temperature of gasoline fraction is 80-130 DEG C.
Preferably, the step of etherification process includes：The light gasoline fraction is contacted with alcohols, makes the light petrol
Under the action of catalyst for etherification with alcohols etherification reaction occurs for the alkene in cut, obtains the etherificate oil；Wherein, the ether
The temperature for changing reaction is 20-200 DEG C, pressure 0.1-5MPa, when weight (hourly) space velocity (WHSV) is 0.1-20 small-1, the alcohols and light petrol
The molar ratio of cut is 1：(0.1-100), the catalyst for etherification include at least one in resin, molecular sieve and heteropoly acid
Kind.
Preferably, the fluidizing reactor is riser reactor and/or dense-phase fluidized bed reactor.
Preferably, the absorbing desulfurization catalyst contains silica, aluminium oxide, zinc oxide and desulphurizing activated metal, institute
It is selected from least one of cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium to state desulphurizing activated metal.
Preferably, on the basis of the butt weight of the absorbing desulfurization catalyst and in terms of oxide weight, the absorption
Zinc oxide described in desulphurization catalyst accounts for 10-90 weight %, and silica accounts for 5-85 weight %, and aluminium oxide accounts for 5-30 weight %；
On the basis of the butt weight of the absorbing desulfurization catalyst and in terms of element wt, taken off described in the absorbing desulfurization catalyst
The content of sulphur active metal is 5-30 weight %.
Preferably, counted and on the basis of the gross weight of the alkene aromatized catalyst by butt, the alkene aromatisation
Catalyst contains the molecular sieve of 10-30 weight %, the aromatization activity metal oxide of 0-20 weight % and 50-90 weight %'s
Carrier；Wherein, the molecular sieve includes Y molecular sieve and/or MFI structure molecular sieve, and the aromatization activity metal is selected from the
The metallic element of Group IVB, the metallic element of Group VB, the metallic element of group VIB, the metallic element of group VIII, group ib
Metallic element, the metallic element of group iib and at least one of the metallic element of group III A, the carrier includes oxidation
Silicon and/or aluminium oxide.
Preferably, the MFI structure molecular sieve is selected from least one of ZSM-5, ZSM-8 and ZSM-11, the virtue
Structure active metal is selected from least one of Fe, Zn and Ga.
Preferably, by weight, the ratio that the alkene aromatized catalyst accounts for the mixed catalyst is 1-30 weights
Measure %.
Preferably, the condition of the desulfurization and aromatization includes：Reaction temperature is 350-500 DEG C, and weight (hourly) space velocity (WHSV) is
When 2-50 is small-1The sum of, reaction pressure 0.5-3.0MPa, hydrogen volume and the middle gasoline fraction and heavy naphtha volume
Ratio is 1-500.
Preferably, the method further includes：The etherification process is carried out after the light gasoline fraction is pre-processed again,
Wherein, the pretreatment is selected from least one of caustic extraction processing, mercaptan conversion processing and selective hydrogenation processing.
The present invention also provides a kind of processing system of gasoline, the system include gasoline stocks fractionating column, fluidizing reactor,
High-pressure separator, pretreatment unit, ether-based device, etherification product fractionating column and mixer；The gasoline stocks fractionating column is set
There are gasoline stocks entrance, light gasoline fraction outlet, the outlet of middle gasoline fraction and heavy naphtha outlet, the fluidizing reactor
Lower part be provided with hydrogen inlet, enterprising material mouth and the lower feed inlet below the enterprising material mouth, the fluidization reaction
Desulfurization and aromatization products outlet are provided with the top of device, the etherification product fractionating column is provided with etherification product entrance, tail gas
Outlet and etherificate oil export；The middle gasoline fraction outlet of the gasoline stocks fractionating column and the upper feeding of the fluidizing reactor
Mouth is in fluid communication, the heavy naphtha outlet of the gasoline stocks fractionating column and the lower feed inlet fluid of the fluidizing reactor
Connection, the desulfurization of the fluidizing reactor and aromatization products outlet entering by the high-pressure separator and the mixer
Mouth is in fluid communication；The light gasoline fraction outlet of the gasoline stocks fractionating column passes sequentially through the pretreatment unit and ether-based device
It is in fluid communication with the etherification product entrance of the etherification product fractionating column, the etherificate oil export of the etherification product fractionating column and institute
The entrance for stating mixer is in fluid communication.
The present invention has following technique effect compared with prior art：
1st, method and system of the invention carries out the gasoline stocks of the high alkene of high-sulfur to be cut into light gasoline fraction, middle gasoline
Cut and heavy naphtha, by middle gasoline fraction and heavy naphtha and absorbing desulfurization catalyst and alkene aromatized catalyst into
Row desulfurization and aromatization, while content of sulfur in gasoline is reduced, can be cracked the alkene in gasoline and aromatisation,
Produce C5Following hydro carbons simultaneously cuts etherification reaction is carried out in light gasoline fraction, so as to both reduce the content of alkene in gasoline,
Also improve the octane number of gasoline and keep the high income of gasoline stocks, being capable of directly producing country V or even VI label gasoline of state.
2nd, desulfurization and aromatization of the invention are carried out using two kinds of catalyst in a fluidizing reactor, are both carried
High reaction efficiency, also reduces cost of investment, without increasing or changing reactor.
3rd, method of the invention can also reduce the light component in gasoline, reduce gasoline vapour pressure.
4th, light gasoline fraction is carried out etherification process by the present invention, can either reduce wherein alkene, additionally it is possible to produce higher octane
The etherificate oil of value, improves the octane number of gasoline products.
5th, the present invention by gasoline stocks be cut into it is light, in, heavy naphtha, gasoline fraction is handled from molecular level, no
Only operation is flexible, also helps the hydrogenation saturation for reducing alkene.
6th, of the invention desulfurization and aromatization are carried out using two kinds of catalyst in a fluidizing reactor, can be with
Gasoline step-by-step processing method (desulfurization after aromatisation, or gasoline elder generation aromatisation after the desulfurization of gasoline elder generation) is avoided to need individually increase aromatization
Change reactor and subsystem, can also avoid gasoline desulfurization and aromatisation coupled catalyst is needed to change existing absorption desulfurization and urged
The preparation process flow and catalyst abrasion intensity of agent and aromatized catalyst, both improve reaction efficiency, also reduce
Cost of investment.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Attached drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of flow diagram of embodiment of the method for the present invention, also a kind of specific including present system
The structure diagram of embodiment.
Description of reference numerals
Gasoline fraction in 1 gasoline stocks, 2 gasoline stocks fractionating column 3
4 heavy naphtha, 5 hydrogen, 6 fluidizing reactor
7 enterprising 8 times feed inlets of material mouth, 9 desulfurization and aromatization products
10 high-pressure separator, 11 tail gas, 12 sulfur-free gasoline cut
13 light gasoline fraction, 14 pretreatment unit 15 is etherified preceding light petrol
16 ether-based device, 17 methanol, 18 etherification product
19 etherification product fractionating column, 20 tail gas 21 is etherified oil
22 mixer, 23 gasoline products
Embodiment
The embodiment of the present invention is described in detail below in conjunction with attached drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
RIPP test methods for details, reference can be made in the present invention《Petrochemical Engineering Analysis method》, Yang Cui surely compile by grade, nineteen ninety version.
The present invention provides a kind of vapour oil treatment process, which includes：Gasoline stocks are cut, are obtained light
Gasoline fraction, middle gasoline fraction and heavy naphtha；Gained light gasoline fraction is subjected to etherification process, obtains etherificate oil；By institute
Gasoline fraction and heavy naphtha, which are sent into, in obtaining contacts with mixed catalyst in fluidizing reactor and is carried out under hydro condition
Desulfurization and aromatization, obtain sulfur-free gasoline cut；Wherein, the mixed catalyst includes absorbing desulfurization catalyst and alkene
Aromatized catalyst；According to the flow direction of reaction mass in the fluidizing reactor, the middle gasoline fraction feed entrance point is located at
The downstream of the heavy naphtha feed entrance point.The feed entrance point refers to what fluidizing reactor was set from bottom to top
Material inlet.
According to the present invention, for direct producing country V even VI label gasoline of state.The method can also include：By gained
Etherificate oil and the mixing of sulfur-free gasoline cut, obtain gasoline products.
According to the present invention, desulfurization and aromatization refer to gasoline stocks under hydro condition in absorbing desulfurization catalyst and
Desulfurization is carried out under the collective effect of alkene aromatized catalyst and alkene is converted into the process of aromatic hydrocarbons, it is during which anti-with cracking
Should, its condition can include：Reaction temperature is 350-500 DEG C, is preferably 380-420 DEG C, when weight (hourly) space velocity (WHSV) is 2-50 small-1, it is excellent
Elect as 5-20 it is small when-1, reaction pressure 0.5-3.0MPa, is preferably 1.5-2.5MPa, hydrogen volume and the middle gasoline fraction
Ratio with the sum of heavy naphtha volume is (in the status of criterion (STP) 0 DEG C of (273K), 1.01 × 105Under Pa) it is 1-500, it is excellent
Elect 50-200 as.
According to the present invention, absorbing desulfurization catalyst is well-known to those skilled in the art that can contain silica, oxygen
Change aluminium, zinc oxide and desulphurizing activated metal, the desulphurizing activated metal can be selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver,
At least one of tin and vanadium.
A kind of embodiment, on the basis of the butt weight of the absorbing desulfurization catalyst and with oxide weight
Meter, zinc oxide described in the absorbing desulfurization catalyst account for 10-90 weight %, and silica accounts for 5-85 weight %, and aluminium oxide accounts for
5-30 weight %；On the basis of the butt weight of the absorbing desulfurization catalyst and in terms of element wt, the absorption desulfurization is urged
The content of desulphurizing activated metal described in agent is 5-30 weight %.
According to the present invention, the absorbing desulfurization catalyst can also contain 1-10 weight % class coke mass.Industrial practice
Show, desulfuration efficiency and octane number loss of the carbon content on absorbing desulfurization catalyst to absorbing desulfurization catalyst has shadow
Ring, with increasing for absorbing desulfurization catalyst carbon content, absorbing desulfurization catalyst desulfuration efficiency progressively declines, octane number damage
Mistake reduces therewith.Similarly, the sulfur content that absorbing desulfurization catalyst keeps certain is very important.Practice have shown that suction to be generated
It is 9 weight %-10 weight % that attached desulphurization catalyst, which carries sulfur content, and regenerative adsorption desulphurization catalyst carries 5 weight %-6 weight % of sulfur content,
The sulphur difference of absorbing desulfurization catalyst to be generated and regenerative adsorption desulphurization catalyst is the most suitable for 4 weight % or so.To reduce gasoline
Loss of octane number, the behaviour that will have been generally acknowledged that rational " small sulphur is poor, big cycle volume " operation adjustment is " partial circulating amount, big sulphur are poor "
Make, reduce regenerative adsorption desulphurization catalyst sulfur content, improve absorbing desulfurization catalyst sulfur content to be generated, reduce octane number damage
Lose, two kinds of operation essence have been to maintain the higher load sulfur content for the absorbing desulfurization catalyst that reaction is participated in reactor, reduce and inhale
The activity of attached desulphurization catalyst, reduces loss of octane number.
According to the present invention, alkene aromatized catalyst is to refer to hydrocarbon conversions such as the alkene in gasoline stocks be aromatic hydrocarbons
Catalyst, generally comprise molecular sieve, preferably include molecular sieve, carrier and metal, for example, in terms of butt and with the alkene virtue
On the basis of the gross weight of structure catalyst, the alkene aromatized catalyst can the molecular sieve containing 10-30 weight %, 0-20
The aromatization activity metal oxide of weight % and the carrier of 50-90 weight %；Wherein, the molecular sieve can include Y molecules
Sieve and/or MFI structure molecular sieve, be preferably five-membered ring high-silica zeolite, the high-silica zeolite can be Hydrogen or
By rare earth and/or P Modification, its silica alumina ratio is preferably greater than 100, and more preferably greater than 150.The MFI structure molecular sieve is can
With selected from least one of ZSM-5, ZSM-8 and ZSM-11.The aromatization activity metal can play partial desulfurization or hydrocarbon
Class transformation function, such as can be the metallic element selected from group ivb, the metallic element of Group VB, the metal member of group VIB
The metallic element of element, the metallic element of group VIII, the metallic element of group ib, the metallic element of group iib and group III A
At least one of, the metallic element preferred Zr or/and Ti of wherein group ivb；The preferred V of metallic element of Group VB；Group VIB
Metallic element preferred Mo or/and W；One or both of metallic element preferred Fe, Co, Ni of group VIII above element；
The preferred Cu of metallic element of group ib；The preferred Zn of metallic element of group iib；The preferred Ga of metallic element of group III A.It is described
Aromatization activity metal is preferably selected from least one of Fe, Zn and Ga, and content is preferably 0.5-5 weight %.The carrier
Preferably include silica and/or aluminium oxide.The particle diameter of the alkene aromatized catalyst is generally 20-120 microns, with absorption
Desulphurization catalyst particle diameter is suitable.Absorbing desulfurization catalyst and alkene aromatized catalyst are separately formed by the present invention (such as sprays
It is dry) after be used in mixed way.
A kind of embodiment, the MFI structure molecular sieve, its preparation process can include ammonia exchange, P Modification,
Metal component modification and calcination process step, are in particular by the conventional crystallization obtained sodium form with MFI structure point
Son sieve is according to molecular sieve：Ammonia salt：H2O=1：(0.1-1)：The weight ratio of (5-10) is in room temperature to when exchange 0.3-1 is small at 100 DEG C
After filter, be introduced into phosphorus-containing compound and containing one or more compounds pair in Fe, Co, Ni, Zn, Mn, Ga and Sn
Molecular sieve is modified, when roasting 0.5-8 is small at 400-800 DEG C afterwards, wherein the processing procedure of described roasting can also be
Carried out under steam atmosphere.Further, MFI structure molecular sieve provided by the present invention, to molecular sieve in preparation process
Being modified can be carried out by the way of dipping or ion exchange.Further, the phosphorus-containing compound can be choosing
From one of phosphoric acid, ammonium hydrogen phosphate, ammonium dihydrogen phosphate or ammonium phosphate or its mixture.Further, the Fe, Co, Ni, Zn,
Mn, Ga and Sn compound can be selected from their water soluble salt, the water soluble salt can be selected from sulfate, nitrate,
One kind in chlorate.Further, MFI structure molecular sieve provided by the present invention, contains phosphorus and metal component, its acid site
Combined with the dehydrogenation close centre of metal, and the presence of phosphorus at the same time can not only improve the structural stability of molecular sieve but also make gold
The ability of dehydrogenation sulfurization of category.
The method that the present invention introduces metal active constituent on molecular sieve or carrier, can use existing various gold-supporteds
Belong to the method for the method of oxide, such as dipping, i.e., using one or more of metal salt solution impregnated zeolites or carrier；It is or heavy
The method in shallow lake, i.e., using on one or more of metal salt solutions or its oxide, hydroxide deposition to molecular sieve or carrier；Or
Person's soild oxide and/or its precursor-metal salt or its hydroxide and molecular sieve or carrier mechanical mixture, grinding or not
The method of grinding；Or colloidal sol facture, gelling process and hydro-thermal method etc..The metal salt is mainly the sulfate of metal, nitre
Hydrochlorate, acetate, halide and metal ammonium salt, metal sodium salt etc..Method for optimizing present invention introduces metal active constituent is heavy
The method in shallow lake or the method for dipping.
Present inventors discovered unexpectedly that the micro-activity of alkene aromatized catalyst effect in 20-55 is more excellent,
The micro-activity is measured using the mat activity test method of RIPP 92-90 catalytic cracking industry equilibrium catalysts.But
From manufacturer's production or homemade qualified not yet used fresh aromatized catalyst, activity is generally more than 60, activity
Higher, cracking performance is stronger, and therefore, fresh aromatized catalyst needs to be handled, and to reduce acid amount, increases acid strength, has
Beneficial to the generation for reducing hydrogen transfer reaction.
A kind of embodiment, the alkene aromatized catalyst pass through Passivation Treatment, and the alkene aromatisation through transpassivation is urged
Passivation content can be 0.1-5.0 weight % in agent, be preferably 0.3-2.0 weight %, more preferably 0.3-1 weights
Measure %；The passivation can be included selected from least one of carbon, sulphur and nitrogen element.The step of Passivation Treatment, can wrap
Include：Fresh aromatized catalyst is contacted in pre-reactor with carbon containing and/or sulphur and/or nitrogen compound and carries out green coke；
Or regeneration aromatized catalyst is contacted in pre-reactor with carbon containing and/or sulphur and/or nitrogen compound and carries out green coke；
Or aromatized catalyst to be generated is subjected to incomplete singeing regeneration.The aromatized catalyst to be generated refers to react in fluidization
Passing through in device is reduced using the catalyst for having loaded certain coke, activity, is not enough to continue to react.Aromatisation to be generated is urged
Agent, which carries out incomplete singeing regeneration, reduces loaded coke content, can obtain more suitable activity.The regeneration
Aromatized catalyst is generally 450-690 DEG C by aromatized catalyst to be generated through regeneration gained, regeneration temperature completely, regeneration gas
Generally oxygen-containing gas, returns in fluidizing reactor by regenerated catalyst circulation and recycles.Regenerate aromatized catalyst
Coke content is generally below 0.1 weight %, hyperactivity, therefore is needed as fresh aromatized catalyst in pre-reactor
Middle carry out green coke.
The green coke of the fresh aromatized catalyst and regeneration aromatized catalyst can be reacted positioned at the fluidization
Carry out, can also be carried out in the pre lift zone in the fluidizing reactor, used in green coke in reactor outside device
Carbon containing and/or sulphur and/or nitrogen compound can be gasoline, hydrogen sulfide or carbon disulfide etc., and gasoline both can be the gasoline
Raw material, or the gasoline stocks outside fluidizing reactor, such as catalytically cracked gasoline, steam cracking gasoline or other
The gasoline of olefin-containing.
A kind of embodiment, the alkene aromatized catalyst pass through burin-in process.Burin-in process refers to deposit in vapor
Fresh aromatized catalyst is subjected to high-temperature process under the conditions, to reduce its activity.The condition of the burin-in process can be with
Including：Temperature is 500-800 DEG C, and when the time is 1-360 small, aging atmosphere is steam atmosphere, is preferably 100% vapor gas
Atmosphere.
A kind of embodiment of burin-in process, by fresh aromatized catalyst and vapor or steam-laden aging
Media contact, when (temperature be 500 DEG C -800 DEG C) aging 1 is small under certain thermal and hydric environment -360 it is small when after, obtained aging
Aromatized catalyst.Further, the burin-in process refers to fresh aromatized catalyst in 800 DEG C and 100% vapor
Under condition (with reference to RIPP 92-90) aging certain time to reduce activity, if ageing time is 4h or 17h.Further, newly
The ageing method of fresh aromatized catalyst is implemented：Fresh aromatized catalyst is loaded into the preferably close phase of reactor
Fluid bed, contacts with vapor or steam-laden aging medium, under certain thermal and hydric environment (temperature is 500 DEG C -800 DEG C)
When aging 1 is small -360 it is small when after, obtain aging aromatized catalyst.Further, the aging medium include air, dry gas,
Gas or air after regenerated flue gas, air and dry combustion gas and the gas or other gases such as nitrogen after burning oil firing.Institute
The weight ratio for stating the vapor in steam-laden aging medium and aging medium is 0.2-0.9, is preferably 0.40-0.60.Institute
The regenerating unit that regenerated flue gas can come from the present invention is stated, can be from other regenerating units.
According to alkene in gasoline and the difference of sulfur content, absorbing desulfurization catalyst and alkene aromatisation in fluidizing reactor
The ratio of catalyst can be different, for example, by weight, the alkene aromatized catalyst accounts for the ratio of the mixed catalyst
It is preferably 3-15 weight % for 1-30 weight %.
According to the present invention, it can be selected from catalytically cracked gasoline that gasoline stocks, which are well-known to those skilled in the art, urge
Change at least one of drippolene, coker gasoline, pressure gasoline and direct steaming gasoline.The gasoline that the present invention is handled is preferably height
Alkene and high sulfur oil, its volume fraction of olefins are generally higher than 20 body %, preferably greater than 30 body %, more preferably greater than 40 body %,
Further preferably greater than 50 body %, sulfur content is generally more than 10 μ g/g, preferably greater than 50 μ g/g, more preferably greater than 100 μ g/g,
Further preferably greater than 500 μ g/g, still more preferably more than 1000 μ g/g, the organic sulfur compound in gasoline be generally mercaptan,
Thioether, thiophene, alkylthrophene, benzothiophene and methyl benzothiophene etc..
According to the present invention, the cut point of the light gasoline fraction and middle gasoline fraction can be 50-80 DEG C, the middle gasoline
The cutting temperature of cut and heavy naphtha can be 80-130 DEG C.Desulfurization and the cutting of aromatization products are generally in fractionating column
Carried out from low to high according to boiling range, for example, the operating condition of the fractionating column of gasoline cutting is：Tower top temperature is 60-80 DEG C, bottom of towe
Temperature is 120-160 DEG C, operating pressure 0.05-0.3MPa.
According to the present invention, etherification process refers to C in light gasoline fraction5Following low-carbon hydro carbons (such as iso-amylene and ring
Amylene) and alcohols progress etherification reaction, to generate high-octane etherificate oil, for example, the step of etherification process can wrap
Include：The light gasoline fraction is contacted with alcohols, make the alkene in the light gasoline fraction under the action of catalyst for etherification with
Etherification reaction occurs for alcohols, obtains the etherificate oil；Wherein, the temperature of the etherification reaction can be 20-200 DEG C, and pressure can
0.1-5MPa is thought, when weight (hourly) space velocity (WHSV) can be 0.1-20 small-1, the molar ratio of the alcohols and light gasoline fraction can be 1：
(0.1-100), the catalyst for etherification can be included selected from least one of resin, molecular sieve and heteropoly acid, the hydro carbons
Can be selected from least one of methanol, ethanol and propyl alcohol.
A kind of embodiment of etherification process, one section of etherificate is loaded on by strong acid cation exchange resin catalyst
And/or in two sections of etherificate fixed bed reactors, etherificate will be passed through by the light gasoline fraction of the pretreatments such as desulfurization and dialkene removal
It is 50-90 DEG C in reaction temperature in reactor, liquid hourly space velocity (LHSV) 1.0-3.0h-1, methanol and light gasoline fraction active olefin (isomery
Alkene, such as iso-amylene) etherification reaction occurs under conditions of molar ratio 1-2, etherification product is sent into rectifying column separation, is obtained in bottom of towe
To etherificate oil, unreacted lighter hydrocarbons and methanol loop utilize.Etherification procedure reaction temperature preferably is inlet temperature 55-60
DEG C, outlet temperature is less than 90 DEG C, and air speed is preferably 1-2h-1, the molar ratio of methanol and light gasoline fraction is preferably 1.2-1.4.Its
In, one section of etherificate olefin(e) centent is higher, and suitably using mixed phase bed reactor, two sections of etherificate olefin(e) centents are relatively low, suitable using exhausted
Thermosetting fixed bed reactor.In addition, isomerization unit can also be applied to during Etherification of Light FCC Gasoline.Etherification of Light FCC Gasoline has reduction
Content of olefin in gasoline, improve octane number, reduce vapour pressure and improve added value and strengthen many advantages, such as reconciling benefit, etherificate
Oil can be used as octane number blend component, can also be mixed with heavy naphtha and be produced as full distillation gasoline
Product.
According to the present invention, fluidizing reactor is well-known to those skilled in the art, for example, can be selected from fluid bed,
It is riser, downstriker pipeline reactor, the compound reactor being made of riser with fluid bed, defeated by riser and downstriker
Line sending form compound reactor, be made of two or more risers compound reactor, by two or two with
On the fluid bed compound reactor, the compound reactor that is made of two or more downstriker pipelines that form, it is excellent
Elect riser reactor and/or fluidized-bed reactor as, above-mentioned every kind of reactor is segmented into two or more reactions
Area.The fluidized-bed reactor can be selected from fixed fluidized bed, dispersion fluidized bed, bubbling bed, turbulent bed, fast bed, conveying
One or more in bed and dense-phase fluidized bed；The riser reactor can be selected from equal diameter riser, etc. linear speed carry
One or more in riser and various variable diameters risers.Preferably, it is anti-to be selected from dense-phase fluidized for the fluidizing reactor
Answer device.It should be noted that the fluidizing reactor is at least provided with two feed inlets, including at least one heavy naphtha
Feed inlet and at least one middle gasoline fraction feed inlet, and the feed inlet of each heavy naphtha is respectively positioned on each middle gasoline
The upstream of cut feed inlet.Being arranged such can be by the preferentially absorption with desulphurizing activated higher of the heavy naphtha of sulfur content higher
Hydrodesulfurization catalyst, to realize from molecular level processes gasoline fraction, improves absorption desulfuration efficiency.
According to the present invention, light gasoline fraction need to generally be pre-processed before etherification reaction is carried out, to remove sulfide
With the impurity such as alkadienes, to extend the service life of catalyst for etherification.Therefore, the method for the invention can also include：Will be described light
Gasoline fraction carries out the etherification process again after being pre-processed, wherein, the pretreatment can be selected from caustic extraction processing,
At least one of mercaptan conversion processing and selective hydrogenation processing.Caustic extraction processing uses lye by the sulphur of light gasoline fraction
Alcohol extracting is removed into lye；Small molecule mercaptan is converted into other sulfide and removed by mercaptan conversion processing, can be used
The mode such as conventional alkali-free sweetening technique and pre- hydrogenation carries out, and used catalyst and co-catalyst all can be commonly used in the art
Catalyst.Selective hydrogenation processing is well-known to those skilled in the art, for removing alkadienes in gasoline, and can be by 3-
Methyl isophthalic acid-isomerization of butene is 2-methyl-1-butene alkene.
The present invention also provides a kind of processing system of gasoline, which includes gasoline stocks fractionating column 2, fluidizing reactor
6th, high-pressure separator 10, pretreatment unit 14, ether-based device 16, etherification product fractionating column 19 and mixer 22；The gasoline is former
Material fractionating column 2 is provided with gasoline stocks entrance, light gasoline fraction outlet, the outlet of middle gasoline fraction and heavy naphtha outlet, institute
The lower part for stating fluidizing reactor 6 is provided with hydrogen inlet, enterprising material mouth and the lower feed inlet below the enterprising material mouth,
The top of the fluidizing reactor 6 is provided with desulfurization and aromatization products outlet, and the etherification product fractionating column 19 is provided with
Etherification product entrance, offgas outlet and etherificate oil export；The outlet of middle gasoline fraction and the stream of the gasoline stocks fractionating column 2
The enterprising material mouth of state reactor 6 is in fluid communication, heavy naphtha outlet and the fluidization of the gasoline stocks fractionating column 2
The lower feed inlet of reactor 6 is in fluid communication, and the desulfurization of the fluidizing reactor 6 and aromatization products outlet pass through the high pressure
Separator 10 and the entrance of the mixer 22 are in fluid communication；The light gasoline fraction outlet of the gasoline stocks fractionating column 2 is successively
It is in fluid communication by the pretreatment unit 14 and ether-based device 16 and the etherification product entrance of the etherification product fractionating column 19,
The etherificate oil export of the etherification product fractionating column 19 is in fluid communication with the entrance of the mixer 22.The fluidizing reactor
6 hydrogen inlet can be same entrance with enterprising material mouth, can also be same entrance with lower feed inlet, be preferably enterprising material mouth
It is hydrogen inlet with lower feed inlet.
The present invention is further illustrated below in conjunction with attached drawing, but the present invention is not therefore subject to any restriction.
As shown in Figure 1, high alkene and high-sulfur gasoline stocks 1 are first passed through gasoline stocks fractionating column 2 carries out cutting fractionation, point
Evaporate for light gasoline fraction 13, middle gasoline fraction 3 and heavy naphtha 4, wherein, the cut point of light, middle gasoline fraction is 50~80
DEG C, in, the cut point of heavy naphtha be 80~130 DEG C；After middle gasoline fraction 3 and heavy naphtha 4 are each mixed with hydrogen 5
The enterprising material mouth 7 of fluidizing reactor 6 and lower feed inlet 8 are respectively enterd, with absorbing desulfurization catalyst and alkene Aromatizatian catalytic
Agent contact carries out absorption desulfurization and aromatization, and desulfurization and aromatization products 9 enter high-pressure separator 10, obtain sulfur-free gasoline
Cut 12 and tail gas 11.Light gasoline fraction 13 enters light vapour before pretreatment unit 14 is etherified after the pretreatment such as removal of mercaptans
Oil 15, is then mixed into Etherification of Light FCC Gasoline device 16 with methanol 17 and is reacted, etherification product 18 is fractionated into tower 19 and is fractionated
To etherificate oil 21 and the tail gas 20 containing methanol.Sulfur-free gasoline cut 12 after adsorbing desulfurization and the etherificate oil 21 after etherification process
Clean gasoline with high octane product 23 is mixed to get in mixer 22.
The following examples will be further described the present invention, but not thereby limiting the invention.
The full cut of gasoline stocks used in embodiment and comparative example is stable gasoline A, its property is listed in table 1.
Absorbing desulfurization catalyst used in embodiment and comparative example is catalyzed by Sinopec Group
Agent branch company produces, goods number FCAS, and used aromatized catalyst makes catalyst by oneself for laboratory, and the trade mark is
OTAZ-C-3, absorbing desulfurization catalyst and aromatized catalyst property are listed in table 2.
Wherein, the preparation method of aromatized catalyst OTAZ-C-3 is：By 50g (NH4)2SO4It is dissolved in 1000g water, to institute
Obtain and 100g (butt) crystallization product ZSM-5 molecular sieve (Chang Ling catalyst plant produces, non-amine method synthesis) is added in solution, at 95 DEG C
After exchanging 1h, filter cake is filtered to obtain；By 8.6g (NH4)2HPO4It is dissolved in 60g water, is mixed with dipping and dries with filter cake；Add
6.0gGa(NO3)3·9H2O is dissolved in 120g water, is mixed with dipping and is dried with above-mentioned sample；Gained sample is in 580 DEG C of calcination process 3
Hour, obtain molecular sieve product；Gained molecular sieve product is added in 500 grams of (butt) sial colloids, it is spray-dried to be made
Microspherical catalyst.
In following embodiment and comparative example, Na in catalyst2O、NiO、ZnO、Ga2O3、Al2O3、SiO2Content X
Ray fluorescence measures, wherein Al2O3、SiO2Content referring specifically to RIPP134-90 measure, remaining composition measuring method phase
Seemingly.
GB/T5487-1995 and GB/T is respectively adopted in the octane number RON and MON of gasoline in the embodiment of the present invention and comparative example
503-1995 standard methods are measured, anti-knock index=(MON+RON)/2, gasoline PONA using simulation distillation and it is gasoline detailed
Hydrocarbon analyzes (ASTM D2887 and ASTM D6733-01 (2011) test method is respectively adopted to be tested), and content of sulfur in gasoline is adopted
It is measured with SH/T0689-2000.
Embodiment 1
Stable gasoline A is distilled in fractionating column, be cut into it is light, in, heavy naphtha, control light gasoline fraction is whole
Evaporate is a little 80~130 DEG C for 60~70 DEG C (being carried out according to ASTM D86 standards), the middle gasoline fraction end point of distillation.Wherein, vapour is stablized
The light gasoline fraction that oily A distills is denoted as LCN-A, and middle gasoline fraction is denoted as MCN-A, and heavy naphtha is denoted as HCN-A, property
It is shown in Table 3.Light gasoline fraction carries out desulfurization, dialkene removal pretreatment through finishing reactor under hydro condition, makes light gasoline fraction
Middle sulfur content and diene content are down to below 10ppm, and methyltertiarvbutyl ether reactor is then mixed into methanol and carries out etherification reaction,
Etherification reaction condition is：55-80 DEG C of reaction temperature, air speed 1.2h-1, methanol rubs with light gasoline fraction active olefin (isomeric olefine)
Your ratio 1.2, oil gas enters etherificate fractionating column and separates after the etherificate reacted, and top gaseous phase is to include residual carbon five and methanol
Containing methanol-fueled exhaust, bottom of towe obtains etherificate oil, and the tower top temperature for being etherified fractionating column is 60-80 DEG C, and column bottom temperature is 110-140 DEG C.
Etherificate oil is denoted as LCN-A-M, and property is shown in Table 3.
The fresh aromatized catalyst that the trade mark is OTAZ-C-3 is loaded into dense-phase fluidized bed reactor, in aging temperature 780
DEG C, when continuous ageing 8 is small under 100% water vapor conditions, obtain the OTAZ-C-3 catalyst of aging, micro-activity 45.
The heavy naphtha that the middle gasoline fraction and numbering that numbering is MCN-A are HCN-A respectively enters fluidizing reactor
Enterprising material mouth and lower feed inlet, in small-sized continuous fluidized bed reactor with including sulfur absorbent catalyst FCAS and aging
The mixed catalyst contact of aromatized catalyst OTAZ-C-3 (OTAZ-C-3 accounts for the 7% of total catalyst weight), wherein MCN-A exists
Residence time in reactor is shorter than the residence time of HCN-A, carries out absorption desulfurization and aromatization.Operating condition is：Instead
It is 400 DEG C, reactor pressure 2.1MPa to answer temperature, when total weight (hourly) space velocity (WHSV) of middle gasoline fraction and heavy naphtha is 6 small-1,
The ratio of the sum of hydrogen volume and the middle gasoline fraction and heavy naphtha volume is 75.The desulfurization obtained by reactor head
It is cooled and separated to obtain tail gas and sulfur-free gasoline cut with aromatization products.The regeneration temperature of mixed catalyst is 550 DEG C, then
Recycled in mixed catalyst Returning reactor after life.Sulfur-free gasoline cut property is shown in Table 3, and sulfur-free gasoline cut is with being etherified
After oily LCN-A-M mixing, gasoline products are obtained, main character is listed in table 4.
Comparative example 1
Essentially identical with the operation of comparative example 1, difference is all to be inhaled using absorbing desulfurization catalyst FCAS
Attached desulphurization reaction, after sulfur-free gasoline cut is mixed with etherificate oil LCN-A-M, obtains gasoline products, main character is listed in table 4.
It can be seen from Table 4 that embodiment 1 is suitable with the desulfuration efficiency of comparative example 1, and the organon octane of embodiment 1
Value increases about 4.5 units than comparative example 1.
Table 1
Table 2
| Catalyst | FCAS | OTAZ-C-3 |
| Chemical composition, weight % | ||
| Aluminium oxide | 13 | 50.3 |
| Sodium oxide molybdena | / | 0.06 |
| Nickel oxide | 21 | / |
| Zinc oxide | 52 | / |
| Gallium oxide | / | 1.5 |
| Silica | 14 | 48.14 |
| Apparent density, kg/m3 | 1010 | 800 |
| Pore volume, mL/g | / | 0.27 |
| Specific surface area, m2/g | / | 218 |
| Abrasion index, again during %-1 | / | 1.5 |
| Screening composition, weight % | ||
| 0~40 micron | 14.5 | 13.9 |
| 40~80 microns | 51.9 | 49.5 |
| >80 microns | 33.6 | 36.6 |
| Micro-activity | / | 80 |
Table 3
Table 4
Claims (21)
1. a kind of vapour oil treatment process, the processing method include：
Gasoline stocks are cut, obtain light gasoline fraction, middle gasoline fraction and heavy naphtha；
Gained light gasoline fraction is subjected to etherification process, obtains etherificate oil；
Gasoline fraction in gained and heavy naphtha are sent into fluidizing reactor and is contacted with mixed catalyst and is facing hydrogen bar
Desulfurization and aromatization are carried out under part, obtains sulfur-free gasoline cut；Wherein, the mixed catalyst includes absorption desulfurization catalyst
Agent and alkene aromatized catalyst；
According to the flow direction of reaction mass in the fluidizing reactor, the middle gasoline fraction feed entrance point is located at the heavy petrol
The downstream of cut feed entrance point.
2. according to the method described in claim 1, the method further includes：Gained etherificate oil and sulfur-free gasoline cut are mixed,
Obtain gasoline products.
3. according to the method described in claim 1, wherein, by weight and using the weight of the alkene aromatized catalyst as base
Standard, passivation content is 0.1-5.0 weight % in the alkene aromatized catalyst；The passivation include selected from carbon, sulphur and
At least one of nitrogen element.
4. the method according to claim 1 or 3, wherein, the preparation process of the alkene aromatized catalyst includes：
Fresh aromatized catalyst is contacted in pre-reactor with carbon containing and/or sulphur and/or nitrogen compound and carries out green coke；
Or
Regeneration aromatized catalyst is contacted in pre-reactor with carbon containing and/or sulphur and/or nitrogen compound and carries out green coke；
Or
Aromatized catalyst to be generated is subjected to incomplete singeing regeneration.
5. according to the method described in claim 4, wherein, the pre-reactor is the reaction outside the fluidizing reactor
Device is the pre lift zone in the fluidizing reactor.
6. according to the method described in claim 1, wherein, the preparation process of the alkene aromatized catalyst includes：Will be fresh
Aromatized catalyst carries out burin-in process；Wherein, the condition of the burin-in process includes：Temperature is 500-800 DEG C, time 1-
360 it is small when, aging atmosphere is steam atmosphere.
7. according to the method described in claim 1, wherein, the micro-activity of the alkene aromatized catalyst is 20-55, described
Micro-activity is measured using the mat activity test method of RIPP 92-90 catalytic cracking industry equilibrium catalysts.
8. according to the method described in claim 1, wherein, volume fraction of olefins is more than 20 body % in the gasoline stocks.
9. according to the method described in claim 1, wherein, sulfur content is more than 10 μ g/g in the gasoline stocks.
10. according to the method described in claim 1, wherein, the gasoline stocks are selected from catalytically cracked gasoline, catalytic pyrolysis vapour
At least one of oil, coker gasoline, pressure gasoline and direct steaming gasoline.
11. according to the method described in claim 1, wherein, the cut point of the light gasoline fraction and middle gasoline fraction is 50-80
DEG C, the cutting temperature of the middle gasoline fraction and heavy naphtha is 80-130 DEG C.
12. according to the method described in claim 1, wherein, the step of etherification process, includes：By the light gasoline fraction with
Alcohols contacts, and makes the alkene in the light gasoline fraction that etherification reaction occur with alcohols under the action of catalyst for etherification, obtains
The etherificate oil；Wherein, the temperature of the etherification reaction is 20-200 DEG C, pressure 0.1-5MPa, weight (hourly) space velocity (WHSV) 0.1-20
Hour-1, the molar ratio of the alcohols and light gasoline fraction is 1：(0.1-100), the catalyst for etherification include selected from resin, divide
At least one of son sieve and heteropoly acid.
13. according to the method described in claim 1, wherein, the fluidizing reactor is riser reactor and/or dense-phase flow
Fluidized bed reactor.
14. according to the method described in claim 1, wherein, the absorbing desulfurization catalyst contains silica, aluminium oxide, oxygen
Change zinc and desulphurizing activated metal, the desulphurizing activated metal be in cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium extremely
Few one kind.
15. according to the method for claim 14, wherein, on the basis of the butt weight of the absorbing desulfurization catalyst and with
Oxide weight meter, zinc oxide described in the absorbing desulfurization catalyst account for 10-90 weight %, and silica accounts for 5-85 weights
% is measured, aluminium oxide accounts for 5-30 weight %；On the basis of the butt weight of the absorbing desulfurization catalyst and in terms of element wt, institute
The content for stating desulphurizing activated metal described in absorbing desulfurization catalyst is 5-30 weight %.
16. according to the method described in claim 1, wherein, in terms of butt and with the gross weight of the alkene aromatized catalyst
On the basis of, the alkene aromatized catalyst contains the molecular sieve of 10-30 weight %, the aromatization activity metal of 0-20 weight %
The carrier of oxide and 50-90 weight %；Wherein, the molecular sieve includes Y molecular sieve and/or MFI structure molecular sieve, the virtue
Structure active metal is the metallic element selected from group ivb, the metallic element of Group VB, the metallic element of group VIB, Section VIII
The metallic element of race, the metallic element of group ib, the metallic element of group iib and group III A metallic element at least one
Kind, the carrier includes silica and/or aluminium oxide.
17. according to the method for claim 16, wherein, the MFI structure molecular sieve is selected from ZSM-5, ZSM-8 and ZSM-
At least one of 11, the aromatization activity metal is selected from least one of Fe, Zn and Ga.
18. according to the method described in claim 1, wherein, by weight, the alkene aromatized catalyst accounts for the mixing and urges
The ratio of agent is 1-30 weight %.
19. according to the method described in claim 1, wherein, the condition of the desulfurization and aromatization includes：Reaction temperature is
350-500 DEG C, when weight (hourly) space velocity (WHSV) is 2-50 small-1, reaction pressure 0.5-3.0MPa, hydrogen volume and the middle gasoline fraction and
The ratio of the sum of heavy naphtha volume is 1-500.
20. according to the method described in claim 1, the method further includes：After the light gasoline fraction is pre-processed again
The etherification process is carried out, wherein, the pretreatment is at caustic extraction processing, mercaptan conversion processing and selective hydrogenation
At least one of reason.
21. a kind of processing system of gasoline, which includes gasoline stocks fractionating column (2), fluidizing reactor (6), high pressure point
From device (10), pretreatment unit (14), ether-based device (16), etherification product fractionating column (19) and mixer (22)；
The gasoline stocks fractionating column (2) be provided with gasoline stocks entrance, light gasoline fraction outlet, middle gasoline fraction outlet and again
Gasoline fraction exports, and the lower part of the fluidizing reactor (6) is provided with hydrogen inlet, enterprising material mouth and positioned at the upper feeding
The lower feed inlet of mouthful lower section, desulfurization and aromatization products outlet, the etherificate are provided with the top of the fluidizing reactor (6)
Product fractionation tower (19) is provided with etherification product entrance, offgas outlet and etherificate oil export；
The middle gasoline fraction outlet of the gasoline stocks fractionating column (2) and the enterprising material mouth fluid of the fluidizing reactor (6)
Connection, the heavy naphtha outlet of the gasoline stocks fractionating column (2) and the lower feed inlet fluid of the fluidizing reactor (6)
Connection, the desulfurization of the fluidizing reactor (6) and aromatization products outlet are mixed by the high-pressure separator (10) with described
The entrance of clutch (22) is in fluid communication；
The light gasoline fraction outlet of the gasoline stocks fractionating column (2) passes sequentially through the pretreatment unit (14) and ether-based device
(16) the etherification product entrance with the etherification product fractionating column (19) is in fluid communication, the ether of the etherification product fractionating column (19)
Carburetion is exported to be in fluid communication with the entrance of the mixer (22).
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