CN108659879A

CN108659879A - A kind of method of gasoline desulfurization

Info

Publication number: CN108659879A
Application number: CN201710194197.0A
Authority: CN
Inventors: 王新; 许友好; 白旭辉
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2017-03-28
Filing date: 2017-03-28
Publication date: 2018-10-16
Anticipated expiration: 2037-03-28
Also published as: CN108659879B

Abstract

The present invention relates to a kind of method of gasoline desulfurization, this method includes：Gasoline stocks are cut, light gasoline fraction and heavy naphtha are obtained；Gained heavy naphtha is sent into first set fluidizing reactor and is contacted with absorbing desulfurization catalyst and carries out the first desulphurization reaction in the case where facing hydrogen state, obtains the first desulfurization product；Gained light gasoline fraction is sent into second set of fluidizing reactor and carries out the second desulphurization reaction with absorbing desulfurization catalyst, obtains the second desulfurization product；Wherein, in first desulphurization reaction, the first reaction temperature is 380 470 DEG C, and the first reaction pressure is 2.0 3.5MPa；In second desulphurization reaction, the second reaction temperature is 360 450 DEG C, and the second reaction pressure is 1.5 3.0MPa.Method provided by the invention can reduce sulphur and olefin(e) centent in gasoline, and can reduce octane number loss simultaneously and keep high yield of gasoline.

Description

A kind of method of gasoline desulfurization

Technical field

The present invention relates to a kind of methods of gasoline desulfurization.

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 content will lead to octane number Heavy losses, to influence the automobile-used performance of gasoline and the economic benefit of oil plant, therefore in the deep desulfuration for realizing gasoline Octane number is kept to become the hot spot of China's clean gasoline production simultaneously.

Currently, the deep desulfuration of gasoline is mainly using hydrodesulfurization or the method for adsorbing desulfurization.Selective hydrodesulfurization It is one of the major way of current removing thiophene-type sulfide, but the reactions such as alkene saturation equally largely occur, and cause octane number It loses larger.In addition, the deep hydrogenation method for restoring octane number is similarly approved by people, it is to carry out deep desulfuration and alkene While saturation, setting second reactor is to promote cracking hydrocarbon, isomerization and the alkylated reaction of low octane rating, to reach Restore the purpose of octane number.Absorption method removes the sulfur-containing compound in fuel oil, be light oil is carried out facing hydrogen using adsorbent it is anti- It should adsorb, generate metal sulfide or remove sulphur using sulfide polarity, hydrogen consumption is relatively low, and desulfuration efficiency is high, can produce sulphur and contain Amount is in the 10 following gasoline of μ g/g.Although absorbing process realizes the deep desulfuration of gasoline under the conditions of low hydrogen consumes, gasoline product is pungent Alkane value is still slightly lost.Especially when handling olefin(e) centent height and the high gasoline stocks of sulfur content, still cause gasoline pungent The loss of alkane value is larger.

Chinese patent CN101845322A discloses a kind of method reducing sulfur in gasoline and olefin(e) centent, and catalytic material is split Change gasoline and first pass through pre-hydrogenator removing alkadienes, light, heavy petrol is fractionated into subsequently into fractionating column cutting, light petrol into Row faces hydrogen absorption desulfurization, and heavy petrol enters selective hydrogenation reactor hydrodesulfurization, and it is anti-that reaction effluent enters back into hydro-upgrading It answers device to carry out hydro-upgrading, reduces olefin(e) centent, the heavy petrol after modification reconciles with light petrol absorption desulfurization product to be met The clean gasoline that standard requires.

The method that Chinese patent CN1766057A discloses production low sulfur, low olefin gasoline, is by full boiling range cracked naphtha At least two fractions are separated into, polyunsaturated compounds are selectively hydrogenated, then by light gasoline fraction etherificate, heavy naphtha Hydrodesulfurization or chemisorption carry out removal of sulphur, finally merge two kinds of fractions and obtain low sulfur, low olefin gasoline.The present invention will be handled Low sulfur, low olefin gasoline is obtained, but gasoline product octane number is expected to reduce to a certain degree.

Since technique is when reducing sulfur content of catalytic cracking gasoline for gasoline absorbing desulfurization (abbreviation S Zorb), octane number Lose less, while plant energy consumption is relatively low.Therefore, domestic many oil plants select S Zorb technologies to handle catalytic cracking vapour Oil builds more set S Zorb devices, the in this way space there is optimization catalytically cracked gasoline processing technological flow.

Invention content

The object of the present invention is to provide a kind of method of gasoline desulfurization, method provided by the invention can reduce in gasoline Sulphur and olefin(e) centent, and octane number loss can be reduced simultaneously and keep high yield of gasoline.

To achieve the goals above, the present invention provides a kind of method of gasoline desulfurization, and this method includes：By gasoline stocks into Row cutting, obtains light gasoline fraction and heavy naphtha；By gained heavy naphtha be sent into first set fluidizing reactor in Absorbing desulfurization catalyst contacts and carries out the first desulphurization reaction in the case where facing hydrogen state, obtains the first desulfurization product；By the light vapour of gained Oil distillate is sent into second set of fluidizing reactor and the second desulphurization reaction is contacted and carried out with absorbing desulfurization catalyst, obtains second Desulfurization product；Wherein, the condition of first desulphurization reaction includes：First reaction temperature is 380-470 DEG C, the first reaction pressure For 2.0-3.5MPa；The condition of second desulphurization reaction includes：Second reaction temperature is 360-450 DEG C, the second reaction pressure For 1.5-3.0MPa.

Optionally, second reaction temperature is 5 DEG C -30 DEG C lower than the first reaction temperature；And/or second reaction pressure Power is lower 0.1MPa-1.0MPa than the first reaction pressure.

Optionally, this method further includes：The first desulfurization product of gained is mixed with the second desulfurization product, obtains gasoline production Product.

Optionally, volume fraction of olefins is more than 10 body % in the gasoline stocks.

Optionally, in the gasoline stocks sulfur content more than 10 μ g/g.

Optionally, 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.

Optionally, the cut point of the light gasoline fraction and heavy naphtha is 60-100 DEG C.

Optionally, the first set fluidizing reactor and second set of fluidizing reactor are each independently selected from fluidisation Bed, riser, downstriker pipeline reactor, the compound reactor being made of riser and fluid bed, by riser and downlink Formula pipeline constitute compound reactor, be made of two or more risers compound reactor, by two or two A above fluid bed compound reactor constituted and the recombination reaction being made of two or more downstriker pipelines One or more of at least one of device, preferably equal diameter riser, reducing riser, dense-phase fluidized bed reactor, the A set of fluidizing reactor and second set of fluidizing reactor belong to gasoline absorbing desulfurization device.

Optionally, 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.

Optionally, on the basis of the dry 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 dry 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 %.

Compared with prior art, the invention has the advantages that：

1, gasoline stocks are divided into light gasoline fraction and heavy naphtha by method of the invention, then evaporate two kinds of gasoline It is handled in two sets of fluidizing reactors respectively, reaction condition that is harsh or mitigating can be respectively adopted, reducing gasoline group While dividing sulfur content, additionally it is possible to keep the octane number and high yield of gasoline.

2, method of the invention has optimized and combined catalytic gasoline processing technological flow, and gasoline can be managed from molecular level Component.

Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.

Description of the drawings

Attached drawing is to be used to provide further understanding of the present invention, an and 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 specific implementation mode of the method for the present invention.

Reference sign

1 gasoline stocks Cutting Tap, 2 first set fluidizing reactor, 3 first set high-pressure separator

4 second sets of fluidizing reactors, 5 second sets of 6 mixers of high-pressure separator

7 pipeline, 8 pipeline, 9 pipeline

10 pipeline, 11 pipeline, 12 pipeline

13 pipeline, 14 pipeline, 15 pipeline

16 pipeline, 17 pipeline, 18 pipeline

Specific implementation mode

The specific implementation mode of the present invention is described in detail below in conjunction with attached drawing.It should be understood that this place is retouched The specific implementation mode stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.

In the present invention RIPP test methods for details, reference can be made to《Petrochemical analysis method》, Yang Cui is surely equal to be compiled, nineteen ninety version.

The present invention provides a kind of method of gasoline desulfurization, and this method includes：Gasoline stocks are cut, light petrol is obtained Fraction and heavy naphtha；Gained heavy naphtha is sent into first set fluidizing reactor and is contacted with absorbing desulfurization catalyst And the first desulphurization reaction is carried out in the case where facing hydrogen state, obtain the first desulfurization product；Gained light gasoline fraction is sent into second set of stream The second desulphurization reaction is contacted and carried out in state reactor with absorbing desulfurization catalyst, obtains the second desulfurization product；Wherein, described The condition of first desulphurization reaction includes：First reaction temperature is 380-470 DEG C, and the first reaction pressure is 2.0-3.5MPa；It is described The condition of second desulphurization reaction includes：Second reaction temperature is 360-450 DEG C, and the second reaction pressure is 1.5-3.0MPa.

According to the present invention, desulphurization reaction refer to gasoline stocks under the action of under facing hydrogen state in absorbing desulfurization catalyst into The process of row desulfurization, condition generally may include：Reaction temperature is 350-500 DEG C, reaction pressure 0.5-3.5MPa, when heavy Air speed is 2-50 hours^-1, hydrogen is with gasoline stocks volume ratio (in the status of criterion (STP) 0 DEG C of (273K), 1.01 × 10⁵Under Pa) For 1-500.

Inventor is it was unexpectedly observed that the heavy naphtha of gasoline stocks cutting gained and light gasoline fraction are distinguished Desulphurization reaction is carried out, the yield and octane number of gasoline products can be improved.For example, the first reaction temperature of the first desulphurization reaction can Think that 380-470 DEG C, preferably 410-450 DEG C, the first reaction pressure can be 2.0-3.5MPa, preferably 2.2-3.0MPa； Second reaction temperature of the second desulphurization reaction can be 360-450 DEG C, and preferably 380-430 DEG C, the second reaction pressure can be 1.5-3.0MPa preferably 2.0-2.7MPa.

Further, inventor also found the desulphurization reaction condition of control heavy naphtha and light gasoline fraction, The yield and octane number of gasoline products can be further increased, for example, second reaction temperature is at least than the first reaction temperature It is low 5 DEG C, 10 DEG C preferably at least low, it is 20 DEG C more preferably at least low, it is further preferably 30 DEG C at least low, further, described Two reaction temperatures are 5-30 DEG C lower than the first reaction temperature；And/or second reaction pressure is at least lower than the first reaction pressure 0.1MPa, preferably at least low 0.2MPa, more preferably at least low 0.5MPa, further preferably at least low 1.0MPa, further, Second reaction pressure is lower 0.1MPa-1.0MPa than the first reaction pressure.

According to the present invention, in order to which direct producing country V even VI label gasoline of state, this method can also include：By gained One desulfurization product is mixed with the second desulfurization product, obtains gasoline products.

According to the present invention, gasoline stocks are well-known to those skilled in the art, can be selected from catalytically cracked gasoline, 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, volume fraction of olefins are generally higher than 10 body %, preferably greater than 20 body %, more preferably greater than 30 body %, Further preferably greater than 40 body % are further more 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 are still more preferably more than 1000 μ g/g, having in gasoline Machine sulfide is generally mercaptan, thioether, thiophene, alkylthrophene, benzothiophene and methyl benzothiophene etc..

The present invention has no specifically limited the cutting mode of gasoline fraction.For example, for catalytically cracked gasoline, gasoline Gasoline Cutting Tap may be used in the cutting of fraction, can also use the condensed in two stages cooling of such as catalytic cracking main fractionating tower setting Flow.The cut point of the light gasoline fraction and heavy naphtha can be 60-100 DEG C, preferably 60-80 DEG C, further excellent It is selected as 65-80 DEG C, the Engler distillation of the light gasoline fraction does preferably 60-100 DEG C, further preferably 60-80 DEG C.Vapour The cutting of oily raw material carries out generally in fractionating column according to boiling range from low to high, for example, the operation item of the fractionating column of gasoline cutting Part is：Tower top temperature is 60-80 DEG C, and column bottom temperature is 120-160 DEG C, operating pressure 0.05-0.3MPa.

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 with fluid bed riser, defeated by riser and downstriker Compound reactor that line sending is constituted, the compound reactor being made of two or more risers, by two or two with On the fluid bed compound reactor constituted and the compound reactor being made of two or more downstriker pipelines in At least one, preferably riser reactor and/or fluidized-bed reactor, each above-mentioned reactor be segmented into two or two A above reaction zone.The fluidized-bed reactor can be selected from fixed fluidized bed, dispersion fluidized bed, bubbling bed, turbulent bed, Fast bed, conveying one or more of bed and dense-phase fluidized bed；The riser reactor can be to be promoted selected from equal diameter Pipe, etc. one or more of linear speeds riser and various variable diameters risers.Preferably, the fluidizing reactor is selected from close Phase fluidizing reactor, more preferably variable diameters riser reactor.

According to the present invention, absorbing desulfurization catalyst is well-known to those skilled in the art, for example, the absorption desulfurization is urged Agent can contain silica, aluminium oxide, zinc oxide and desulphurizing activated metal, the desulphurizing activated metal can be selected from At least one of cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium.

A kind of specific implementation mode, on the basis of the dry 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 dry 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 %.

A kind of specific implementation mode of the present invention is provided below in conjunction with attached drawing, but it is not thereby limiting the invention.

As shown in Figure 1, gasoline fraction enters gasoline stocks Cutting Tap 1 through pipeline 7, the light gasoline fraction that tower top obtains is through pipe Line 8 introduces first set fluidizing reactor 2, is mixed with the hydrogen introduced through pipeline 9, under the action of absorbing desulfurization catalyst into The reaction oil gas of the first desulphurization reaction of row, generation introduces first set high-pressure separator 3, isolated light petrol product through pipeline 10 It is drawn through pipeline 11；The heavy naphtha that 1 bottom of tower of gasoline stocks Cutting Tap obtains introduces second set of fluidization reaction through pipeline 13 Device 4 mixes with the hydrogen introduced through pipeline 14, the second desulphurization reaction is carried out under the action of absorbing desulfurization catalyst, generation Reaction oil gas introduces second set of high-pressure separator 5 through pipeline 15, and isolated heavy petrol product is drawn through pipeline 16.Heavy petrol produces Object and light petrol product converge to mixer 6 through pipeline, obtain gasoline products.

The following examples will be further described the present invention, but not thereby limiting the invention.

Absorbing desulfurization catalyst used in following example and comparative example is by Sinopec Group Catalyst branch produces, and goods number FCAS, absorbing desulfurization catalyst property is listed in table 3.

In following embodiment and comparative example, NiO, ZnO, Al in catalyst₂O₃、SiO₂Content x-ray fluorescence method It measures, wherein Al₂O₃、SiO₂Content measured referring specifically to RIPP 134-90, remaining composition measuring method is similar.

The octane number of gasoline is measured using RIPP 85-90 methods in the embodiment of the present invention and comparative example, gasoline PONA (being tested using RIPP81-90 test methods) is analyzed using simulation distillation and gasoline detailed hydrocarbon, during content of sulfur in gasoline uses Magnificent people's republic's standard GB/T/T380-1977 oil product sulphur content determination methods (Ignition Lamp Method) are measured.

Fluidizing reactor used in embodiment and comparative example is small fixed fluidized bed unit.

Embodiment 1

Gasoline fraction used in embodiment 1 is oil plant stable gasoline A, and property is listed in table 1.As shown in Figure 1, by steady Determine gasoline A to be distilled in gasoline stocks Cutting Tap 1, be cut into light gasoline fraction and heavy naphtha, controls the first light vapour The oil distillate end point of distillation is 65-70 DEG C (being carried out according to ASTM D86 standards).Wherein, the light petrol that stable gasoline A is cut evaporates Minute mark is LCN-A, and heavy naphtha is denoted as HCN-A, and property is listed in table 2；Heavy naphtha HCN-A is sent into first set fluidization Reactor 4 contacts with absorbing desulfurization catalyst FCAS and carries out the first desulphurization reaction in the case where facing hydrogen state, and reaction condition is listed in table 4.It is cooled and separated to obtain tail gas and the first desulfurization product (after being denoted as HCN-A desulfurization by the reaction product that reactor head obtains 4) gasoline, property are shown in Table；Gained light gasoline fraction LCN-A is sent into second set of fluidizing reactor 2 and absorbing desulfurization catalyst FCAS is contacted and is carried out the second desulphurization reaction in the case where facing hydrogen state, and reaction condition is equally listed in table 4, is obtained by reactor head Reaction product is cooled and separated to obtain tail gas and the second desulfurization product (is denoted as gasoline after LCN-A desulfurization, 4) property is shown in Table；By institute Heavy petrol product and the mixing of light petrol product are obtained, obtains the gasoline products as treated gasoline, property is shown in Table 5.

Embodiment 2

Embodiment 2 and the operation of embodiment 1 are essentially identical, the difference is that, the temperature of the second desulphurization reaction of control is 410 DEG C, gasoline products are obtained, property is shown in Table 5.

Embodiment 3

Embodiment 3 and the operation of embodiment 1 are essentially identical, the difference is that, the temperature of the second desulphurization reaction of control is 410 DEG C, pressure 1.9MPa, gasoline products are obtained, property is shown in Table 5.

Embodiment 4

Embodiment 4 and the operation of embodiment 1 are essentially identical, the difference is that, the temperature of the second desulphurization reaction of control is 415 DEG C, pressure 2.1MPa, gasoline products are obtained, property is shown in Table 5.

Comparative example 1

Stable gasoline A second set of fluidizing reactor 2 of feeding is contacted with absorbing desulfurization catalyst FCAS and is facing hydrogen shape Desulphurization reaction is carried out under state, reaction condition is listed in table 4, is cooled and separated to obtain tail by the desulfurization product that reactor head obtains Gasoline product (is denoted as gasoline after CN-A desulfurization, 4) property is shown in Table after gas and desulfurization.Gasoline is as gasoline products after CN-A desulfurization, Property is equally listed in table 5.

It can be seen from Table 5 that embodiment 1-4 is suitable with the desulfuration efficiency of comparative example 1, but the organon of embodiment 1 is pungent Alkane value 1.5 units of loss fewer than comparative example 1, research octane number (RON) 1.3 units of loss fewer than comparative example 1 of embodiment 2 are real Research octane number (RON) 1.5 units of loss fewer than comparative example 1 of example 3 are applied, the research octane number (RON) of embodiment 4 is fewer than comparative example 1 Lose 0.2 unit.Table 1

Gasoline stocks	Stable gasoline A
		20 DEG C of density, kg/m³	737.3
20 DEG C of refractive index	1.4212
		Carbon content, % (w)	86.36
Hydrogen content, % (w)	13.64
		Sulfur content, mg/L	421
Nitrogen content, mg/L	139
		Induction period, min	667
Race forms (FIA methods)
		Aromatic hydrocarbons, % (volume fraction)	15.4
Alkene, % (volume fraction)	54.9
		Saturated hydrocarbons, % (volume fraction)	29.7
Survey RON	90.9
		Survey MON	78.9
Normal pressure boiling range, DEG C
		IBP	44
5%	59
		10%	63
30%	80
		50%	106
70%	139
		90%	175
FBP	204

Table 2

Table 3

Catalyst	FCAS
		Chemical composition, weight %
Aluminium oxide	11
		Nickel oxide	20
Zinc oxide	49
		Silica	20
Apparent density, kg/m³	1130
		Screening composition, weight %
0~40 micron	14.5
		40~80 microns	51.9
>80 microns	33.6

Table 4

Table 5

Experimental program	Embodiment 1	Embodiment 2	Embodiment 3	Embodiment 4	Comparative example 1
						Gasoline types	Gasoline products	Gasoline products	Gasoline products	Gasoline products	Gasoline products
20 DEG C of density, kg/m³	738.6	738.7	738.5	740.1	740.1
						Vapour pressure (RVPE), kPa	51	51	51	50	50
Sulfur content, mg/L	9.4	9.4	9.4	9.4	10
						Race forms (FIA methods)
Aromatic hydrocarbons, % (volume fraction)	15.6	15.6	15.7	15.8	15.5
						Alkene, % (volume fraction)	36.6	35.4	36.2	32.0	31.8
Saturated hydrocarbons, % (volume fraction)	47.8	49.0	48.1	52.2	52.7
						Survey RON	88.5	88.3	88.5	87.2	87.0
Survey MON	78.2	78.0	78.2	77.2	77.2
						Normal pressure boiling range, DEG C
IBP	44	44	44	44	45
						5%	58	58	58	58	60
10%	65	65	65	65	67
						30%	83	83	83	83	84
50%	100	100	100	100	102
						70%	136	136	136	136	137
90%	172	172	172	172	175
						FBP	201	201	201	201	203

Claims

1. a kind of method of gasoline desulfurization, this method include：

Gasoline stocks are cut, light gasoline fraction and heavy naphtha are obtained；

Gained heavy naphtha is sent into first set fluidizing reactor and is contacted with absorbing desulfurization catalyst and is facing hydrogen state The first desulphurization reaction of lower progress, obtains the first desulfurization product；

Gained light gasoline fraction is sent into second set of fluidizing reactor to contact with absorbing desulfurization catalyst and carry out second and is taken off Reaction of Salmon-Saxl obtains the second desulfurization product；

Wherein, the condition of first desulphurization reaction includes：First reaction temperature is 380-470 DEG C, and the first reaction pressure is 2.0-3.5MPa；The condition of second desulphurization reaction includes：Second reaction temperature is 360-450 DEG C, and the second reaction pressure is 1.5-3.0MPa。

2. according to the method described in claim 1, wherein, second reaction temperature is 5 DEG C -30 DEG C lower than the first reaction temperature； And/or second reaction pressure is lower 0.1MPa-1.0MPa than the first reaction pressure.

3. according to the method described in claim 1, this method further includes：The first desulfurization product of gained is mixed with the second desulfurization product It closes, obtains gasoline products.

4. according to the method described in claim 1, wherein, volume fraction of olefins is more than 10 body % in the gasoline stocks.

5. according to the method described in claim 1, wherein, sulfur content is more than 10 μ g/g in the gasoline stocks.

6. 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.

7. according to the method described in claim 1, wherein, the cut point of the light gasoline fraction and heavy naphtha is 60-100 ℃。

8. according to the method described in claim 1, wherein, the first set fluidizing reactor and second set of fluidizing reactor It is each independently selected from fluid bed, riser, downstriker pipeline reactor, the recombination reaction being made of riser and fluid bed Device, the compound reactor being made of with downstriker pipeline riser, be made of two or more risers it is compound It reactor, the compound reactor being made of two or more fluid beds and is conveyed by two or more downstrikers At least one of the compound reactor that line is constituted.

9. the method according to claim 1 or 8, wherein the first set fluidizing reactor and second set of fluidization are anti- Device is answered to be each independently selected from one or more of equal diameter riser, variable diameters riser, dense-phase fluidized bed reactor, the A set of fluidizing reactor and second set of fluidizing reactor belong to gasoline absorbing desulfurization device.

10. 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.

11. according to the method described in claim 10, wherein, on the basis of the dry 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 dry 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 %.