CN108659879B

CN108659879B - Gasoline desulfurization method

Info

Publication number: CN108659879B
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: 2020-10-27
Anticipated expiration: 2037-03-28
Also published as: CN108659879A

Abstract

The invention relates to a method for desulfurizing gasoline, which comprises the following steps: cutting a gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction; feeding the obtained heavy gasoline fraction into a first set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a first desulfurization reaction in a hydrogen state to obtain a first desulfurization product; sending the obtained light gasoline fraction into a second set of fluidization reactor to carry out second desulfurization reaction with the adsorption desulfurization catalyst to obtain a second desulfurization product; wherein, in the first desulfurization reaction, the first reaction temperature is 380-; in the second desulfurization reaction, the second reaction temperature is 360-450 ℃, and the second reaction pressure is 1.5-3.0 MPa. The method provided by the invention can reduce the sulfur and olefin content in the gasoline, and can simultaneously reduce the octane number loss of the gasoline and keep the high gasoline yield.

Description

Gasoline desulfurization method

Technical Field

The invention relates to a method for desulfurizing gasoline.

Background

Air pollution caused by automobile exhaust emission is increasingly serious. With increasing attention of people on environmental protection, China speeds up the pace of upgrading the quality of automotive fuel, and the national standard GB17930-2013 requires that the sulfur content in gasoline is not more than 10 mu g/g and the volume fraction of olefin is not more than 24%.

The catalytic cracking gasoline is the main component of the motor gasoline in China, accounts for about 75% in a gasoline pool, and is characterized by having higher contents of olefin and sulfur. It is not difficult to realize deep desulfurization of gasoline and reduce the content of olefin in catalytically cracked gasoline by adopting a hydrogenation technology, but because olefin is a high-octane component, the great reduction of the content of olefin causes serious loss of the gasoline octane number, thereby affecting the automotive performance of gasoline and the economic benefit of a refinery, and therefore, the deep desulfurization of gasoline is realized while the gasoline octane number is kept to be a hotspot of clean gasoline production in China.

At present, the deep desulfurization of gasoline mainly adopts a hydrodesulfurization method or an adsorption desulfurization method. Selective hydrodesulfurization is one of the main modes for removing thiophene sulfides at present, but the reactions such as olefin saturation and the like also occur in large quantity, so that the octane number loss is large. In addition, a deep hydrogenation method for recovering octane number is also accepted, and a second reactor is arranged to promote cracking, isomerization and alkylation reactions of hydrocarbons with low octane number while deep desulfurization and olefin saturation are carried out, so that the aim of recovering octane number is fulfilled. The adsorption process for removing sulfur-containing compound from fuel oil is to use adsorbent to make hydrogen reaction adsorption on light oil to produce metal sulfide or to use sulfide polarity to remove sulfur, so that it has low hydrogen consumption and high desulfurizing efficiency, and can produce gasoline with sulfur content below 10 microgram/g. Although the adsorption process realizes deep desulfurization of gasoline under the condition of low hydrogen consumption, the octane number of the gasoline product is still slightly lost. Especially when processing gasoline feedstocks having high olefin content and high sulfur content, still results in a large loss in gasoline octane number.

Chinese patent CN101845322A discloses a method for reducing sulfur and olefin content in gasoline, the raw material catalytically cracked gasoline is first passed through a prehydrogenation reactor to remove diolefin, then is passed through a fractionating tower to be cut and fractionated into light gasoline and heavy gasoline, the light gasoline is undergone the process of hydrodesulphurization by hydrogen adsorption, the heavy gasoline is passed through a selective hydrogenation reactor to undergo hydrodesulfurization, the reaction effluent is passed through a hydro-upgrading reactor to undergo hydro-upgrading so as to reduce olefin content, and the heavy gasoline after being upgraded is blended with light gasoline adsorption desulfurization product to obtain the clean gasoline meeting the standard requirements.

Chinese patent CN1766057A discloses a process for producing low sulfur low olefin gasoline by separating full boiling range cracked naphtha into at least two fractions, selectively hydrogenating polyunsaturated compounds, then etherifying light gasoline fractions, hydrodesulfurizing heavy gasoline fractions or chemisorbing to remove sulfur, and finally combining the two fractions to obtain low sulfur low olefin gasoline. The invention will treat low sulfur low olefin gasoline, but the octane number of the gasoline product is expected to be reduced to some extent.

The gasoline adsorption desulfurization (S Zorb for short) process has less octane number loss of gasoline and lower energy consumption of the device when reducing the sulfur content of the catalytically cracked gasoline. Therefore, in many domestic oil refineries, the S Zorb technology is selected to treat the catalytic cracking gasoline, and a plurality of sets of S Zorb devices are built, so that a space for optimizing the catalytic cracking gasoline treatment process flow exists.

Disclosure of Invention

The invention aims to provide a method for desulfurizing gasoline, which can reduce the contents of sulfur and olefin in the gasoline, and can simultaneously reduce the octane number loss of the gasoline and keep the high gasoline yield.

In order to achieve the above object, the present invention provides a method for desulfurizing gasoline, the method comprising: cutting a gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction; feeding the obtained heavy gasoline fraction into a first set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a first desulfurization reaction in a hydrogen state to obtain a first desulfurization product; feeding the obtained light gasoline fraction into a second set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a second desulfurization reaction to obtain a second desulfurization product; wherein the conditions of the first desulfurization reaction include: the first reaction temperature is 380-470 ℃, and the first reaction pressure is 2.0-3.5 MPa; the conditions of the second desulfurization reaction include: the second reaction temperature is 360-450 ℃, and the second reaction pressure is 1.5-3.0 MPa.

Optionally, the second reaction temperature is 5-30 ℃ lower than the first reaction temperature; and/or the second reaction pressure is 0.1MPa to 1.0MPa lower than the first reaction pressure.

Optionally, the method further includes: and mixing the obtained first desulfurization product with the second desulfurization product to obtain a gasoline product.

Optionally, the volume fraction of olefins in the gasoline feedstock is greater than 10% by volume.

Optionally, the sulfur content in the gasoline raw material is above 10 μ g/g.

Optionally, the gasoline raw material is at least one selected from catalytically cracked gasoline, coker gasoline, thermally cracked gasoline and straight run gasoline.

Optionally, the cut points of the light gasoline fraction and the heavy gasoline fraction are 60-100 ℃.

Optionally, the first set of fluidization reactor and the second set of fluidization reactor are independently selected from at least one of a fluidized bed, a riser, a descending conveyor line reactor, a composite reactor composed of a riser and a fluidized bed, a composite reactor composed of a riser and a descending conveyor line, a composite reactor composed of two or more risers, a composite reactor composed of two or more fluidized beds, and a composite reactor composed of two or more descending conveyor lines, and preferably one or more of a riser with an equal fluidization diameter, a variable diameter riser, and a dense-phase fluidized bed reactor, and both the first set of fluidization reactor and the second set of fluidization reactor belong to a gasoline adsorption desulfurization device.

Optionally, the adsorption desulfurization catalyst contains silica, alumina, zinc oxide and a desulfurization active metal, wherein the desulfurization active metal is at least one selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium.

Optionally, on the basis of the dry weight of the adsorption desulfurization catalyst and by weight of oxides, the adsorption desulfurization catalyst contains 10-90 wt% of zinc oxide, 5-85 wt% of silica, and 5-30 wt% of alumina; the content of the desulfurization active metal in the adsorption desulfurization catalyst is 5-30 wt% based on the dry weight of the adsorption desulfurization catalyst and calculated by the weight of elements.

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

1. the method of the invention divides the gasoline raw material into light gasoline fraction and heavy gasoline fraction, then the two gasoline fractions are respectively treated in two sets of fluidization reactors, which can respectively adopt harsh or mild reaction conditions, and can maintain the octane number and high yield of the gasoline while reducing the sulfur content of the gasoline component.

2. The method optimizes and integrates the catalytic gasoline treatment process flow, and can manage gasoline components on a molecular level.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic flow diagram of one embodiment of the process of the present invention.

Description of the reference numerals

1 gasoline raw material cutting tower 2 first set of fluidization reactor 3 first set of high-pressure separator

4 second set of fluidization reactor 5 second set of high pressure separator 6 mixer

7 line 8 line 9 line

Line 10 line 11 line 12 line

13 line 14 line 15 line

16 line 17 line 18 line

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

The RIPP test method can be found in petrochemical analysis, Yangcui and other editions, 1990 edition.

The invention provides a method for desulfurizing gasoline, which comprises the following steps: cutting a gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction; feeding the obtained heavy gasoline fraction into a first set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a first desulfurization reaction in a hydrogen state to obtain a first desulfurization product; feeding the obtained light gasoline fraction into a second set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a second desulfurization reaction to obtain a second desulfurization product; wherein the conditions of the first desulfurization reaction include: the first reaction temperature is 380-470 ℃, and the first reaction pressure is 2.0-3.5 MPa; the conditions of the second desulfurization reaction include: the second reaction temperature is 360-450 ℃, and the second reaction pressure is 1.5-3.0 MPa.

According to the present invention, the desulfurization reaction refers to a process of desulfurization of a gasoline raw material in a hydrogen state under the action of an adsorption desulfurization catalyst, and the conditions generally include: the reaction temperature is 350-500 ℃, the reaction pressure is 0.5-3.5MPa, and the weight hourly space velocity is 2-50 h^-1Hydrogen to gasoline feedstock volume ratio (at standard conditions (STP)0 deg.C (273K), 1.01X 10⁵Pa) is 1-500.

The inventors of the present invention have surprisingly found that the yield and octane number of gasoline products can be improved by performing a desulfurization reaction on the heavy gasoline fraction and the light gasoline fraction obtained by cutting a gasoline raw material, respectively. For example, the first reaction temperature of the first desulfurization reaction may be 380-; the second reaction temperature of the second desulfurization reaction may be 360-450 deg.C, preferably 380-430 deg.C, and the second reaction pressure may be 1.5-3.0MPa, preferably 2.0-2.7 MPa.

Further, the present inventors have found that controlling the desulfurization reaction conditions of the heavy gasoline fraction and the light gasoline fraction can further improve the yield and octane number of the gasoline product, for example, the second reaction temperature is at least 5 ℃ lower than the first reaction temperature, preferably at least 10 ℃ lower, more preferably at least 20 ℃ lower, further preferably at least 30 ℃ lower, and further, the second reaction temperature is 5 to 30 ℃ lower than the first reaction temperature; and/or the second reaction pressure is at least 0.1MPa lower than the first reaction pressure, preferably at least 0.2MPa lower, more preferably at least 0.5MPa lower, even more preferably at least 1.0MPa lower, and still more preferably the second reaction pressure is 0.1MPa to 1.0MPa lower than the first reaction pressure.

According to the invention, in order to directly produce the gasoline of the national V or VI label, the method can also comprise the following steps: and mixing the obtained first desulfurization product with the second desulfurization product to obtain a gasoline product.

According to the present invention, the gasoline raw material is well known to those skilled in the art and may be at least one selected from the group consisting of catalytically cracked gasoline, coker gasoline, thermally cracked gasoline, and straight run gasoline. The gasoline treated in accordance with the present invention is preferably a high olefin and high sulfur gasoline having an olefin volume fraction of generally greater than 10 volume percent, preferably greater than 20 volume percent, more preferably greater than 30 volume percent, even more preferably greater than 40 volume percent, and even more preferably greater than 50 volume percent; the sulfur content is generally 10. mu.g/g or more, preferably 50. mu.g/g or more, more preferably 100. mu.g/g or more, still more preferably 500. mu.g/g or more, and still more preferably 1000. mu.g/g or more, and the organic sulfides in gasoline are generally mercaptans, sulfides, thiophenes, alkylthiophenes, benzothiophenes, methylbenzothiophenes and the like.

The cutting mode of the gasoline fraction is not particularly limited in the present invention. For example, for the catalytic cracking gasoline, the gasoline cut can be cut by a gasoline cutting tower, and a two-stage condensation cooling process such as a catalytic cracking main fractionating tower arrangement can also be adopted. The cut point of the light gasoline fraction and the heavy gasoline fraction may be 60 to 100 ℃, preferably 60 to 80 ℃, and more preferably 65 to 80 ℃, and the dry point of the Engler distillation of the light gasoline fraction is preferably 60 to 100 ℃, and more preferably 60 to 80 ℃. The cutting of gasoline feedstocks is generally carried out in a fractionation column with a distillation range from low to high, for example, the operating conditions of a gasoline cutting fractionation column are: the temperature at the top of the tower is 60-80 ℃, the temperature at the bottom of the tower is 120-160 ℃, and the operating pressure is 0.05-0.3 MPa.

Fluidized reactors according to the invention are well known to the person skilled in the art and may be, for example, at least one reactor selected from the group consisting of fluidized beds, risers, downgoing line reactors, composite reactors comprising risers and fluidized beds, composite reactors comprising risers and downgoing lines, composite reactors comprising two or more risers, composite reactors comprising two or more fluidized beds and composite reactors comprising two or more downgoing lines, preferably riser reactors and/or fluidized bed reactors, each of which may be divided into two or more reaction zones. The fluidized bed reactor can be one or more selected from a fixed fluidized bed, a bulk fluidized bed, a bubbling bed, a turbulent bed, a fast bed, a conveying bed and a dense-phase fluidized bed; the riser reactor can be one or more selected from the group consisting of an equal-diameter riser, an equal-linear-speed riser and various variable-diameter risers. Preferably, the fluidization reactor is selected from dense phase fluidization reactors, more preferably a variable diameter riser reactor.

According to the present invention, the adsorption desulfurization catalyst is well known to those skilled in the art, and for example, the adsorption desulfurization catalyst may contain silica, alumina, zinc oxide, and a desulfurization active metal, which may be at least one selected from the group consisting of cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin, and vanadium.

In one embodiment, the adsorbed desulfurization catalyst comprises 10-90 wt.% zinc oxide, 5-85 wt.% silica, and 5-30 wt.% alumina, based on the dry weight of the adsorbed desulfurization catalyst and based on the weight of the oxides; the content of the desulfurization active metal in the adsorption desulfurization catalyst is 5-30 wt% based on the dry weight of the adsorption desulfurization catalyst and calculated by the weight of elements.

A specific embodiment of the present invention will be provided with reference to the accompanying drawings, but the present invention is not limited thereto.

As shown in fig. 1, a gasoline fraction enters a gasoline raw material cutting tower 1 through a pipeline 7, a light gasoline fraction obtained at the top of the tower is introduced into a first set of fluidized reactor 2 through a pipeline 8, is mixed with hydrogen introduced through a pipeline 9, carries out a first desulfurization reaction under the action of an adsorption desulfurization catalyst, and a generated reaction oil gas is introduced into a first set of high-pressure separator 3 through a pipeline 10, and is separated to obtain a light gasoline product which is led out through a pipeline 11; the heavy gasoline fraction obtained from the bottom of the gasoline raw material cutting tower 1 is introduced into the second set of fluidization reactor 4 through the pipeline 13, is mixed with the hydrogen introduced through the pipeline 14, is subjected to a second desulfurization reaction under the action of the adsorption desulfurization catalyst, and the generated reaction oil gas is introduced into the second set of high-pressure separator 5 through the pipeline 15, and is separated to obtain a heavy gasoline product which is led out through the pipeline 16. The heavy gasoline product and the light gasoline product are converged to a mixer 6 through a pipeline to obtain a gasoline product.

The following examples further illustrate the invention but are not intended to limit the invention thereto.

The adsorptive desulfurization catalysts used in the following examples and comparative examples were produced by catalyst division of petrochemical Co., Ltd., China, under the product number FCAS, and the properties of the adsorptive desulfurization catalysts are shown in Table 3.

In the following examples and comparative examples, NiO, ZnO and Al were contained in the catalyst₂O₃、SiO₂The content of (B) is determined by X-ray fluorescence, wherein Al is₂O₃、SiO₂The content of (A) is determined by referring to RIPP 134-90, and the determination method of the rest components is similar.

The octane number of the gasoline in the examples and the comparative examples of the invention is measured by an RIPP 85-90 method, the gasoline PONA is measured by simulated distillation and gasoline monomer hydrocarbon analysis (by an RIPP81-90 test method), and the sulfur content of the gasoline is measured by a sulfur content measurement method (a light combustion method) of a petroleum product according to the national standard GB/T380-1977 of the people's republic of China.

The fluidized reactors used in the examples and comparative examples were small fixed fluidized bed devices.

Example 1

The gasoline fraction used in example 1 was refinery stabilized gasoline a, the properties of which are given in table 1. As shown in fig. 1, stabilized gasoline a is distilled in a gasoline feedstock cutting column 1, cut into a light gasoline fraction and a heavy gasoline fraction, the first light gasoline fraction having an end point of 65-70 ℃ (according to ASTM D86). Wherein, the light gasoline fraction obtained by cutting the stable gasoline A is marked as LCN-A, the heavy gasoline fraction is marked as HCN-A, and the properties are listed in Table 2; the heavy gasoline fraction HCN-A is sent into A first set of fluidization reactor 4 to contact with an adsorption desulfurization catalyst FCAS and is subjected to A first desulfurization reaction in A hydrogen state, and the reaction conditions are listed in Table 4. Cooling and separating the reaction product obtained from the top of the reactor to obtain tail gas and A first desulfurization product (marked as desulfurized gasoline of HCN-A, the properties of which are shown in Table 4); sending the obtained light gasoline fraction LCN-A into A second set of fluidization reactor 2 to contact with an adsorption desulfurization catalyst FCAS and carrying out A second desulfurization reaction in A hydrogen state, wherein the reaction conditions are also listed in Table 4, and cooling and separating A reaction product obtained from the top of the reactor to obtain A tail gas and A second desulfurization product (marked as LCN-A desulfurized gasoline, the properties of which are shown in Table 4); the heavy gasoline product and the light gasoline product obtained were mixed to obtain a gasoline product as refined gasoline, the properties of which are shown in table 5.

Example 2

Example 2 was operated substantially the same as example 1 except that the temperature of the second desulfurization reaction was controlled to 410 c to obtain a gasoline product having the properties shown in table 5.

Example 3

Example 3 the same operation as in example 1 was followed except that the temperature of the second desulfurization reaction was controlled at 410 deg.C and the pressure at 1.9MPa to obtain a gasoline product having the properties shown in Table 5.

Example 4

Example 4 was conducted in substantially the same manner as in example 1 except that the temperature of the second desulfurization reaction was controlled to 415 deg.c and the pressure was controlled to 2.1MPa, to obtain a gasoline product having the properties shown in table 5.

Comparative example 1

The stable gasoline A is sent into A second set of fluidization reactor 2 to contact with an adsorption desulfurization catalyst FCAS and carry out desulfurization reaction in A hydrogen state, the reaction conditions are listed in Table 4, and the desulfurization product obtained from the top of the reactor is cooled and separated to obtain tail gas and A desulfurized gasoline product (marked as CN-A desulfurized gasoline, the properties of which are shown in Table 4). The properties of the CN-A desulfurized gasoline as A gasoline product are also set forth in Table 5.

As can be seen from table 5, examples 1-4 have comparable desulfurization efficiencies to comparative example 1, but example 1 lost 1.5 units less research octane number than comparative example 1, example 2 lost 1.3 units less research octane number than comparative example 1, example 3 lost 1.5 units less research octane number than comparative example 1, and example 4 lost 0.2 units less research octane number than comparative example 1. TABLE 1

Gasoline feedstock	Stable gasoline A
		Density at 20 ℃ in kg/m³	737.3
Refractive index at 20 DEG C	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
Group composition (FIA method)
		Aromatic hydrocarbons,% (volume fraction)	15.4
Olefin,% (volume fraction)	54.9
		Saturated hydrocarbons,% (volume fraction))	29.7
Measured RON	90.9
		Measured MON	78.9
Distillation range under normal pressure, deg.C
		IBP	44
5％	59
		10％	63
30％	80
		50％	106
70％	139
		90％	175
FBP	204

TABLE 2

TABLE 3

Catalyst and process for preparing same	FCAS
		Chemical composition, weight%
Alumina oxide
		11
Nickel oxide			20
	Zinc oxide	49
Silicon oxide			20
	Apparent density, kg/m³	1130
Sieving to obtain fine powder
	0 to 40 μm	14.5
40 to 80 μm			51.9
	>80 micron	33.6

TABLE 4

TABLE 5

Experimental protocol	Example 1	Example 2	Example 3	Example 4	Comparative example 1
						Gasoline type	Gasoline product	Gasoline product	Gasoline product	Gasoline product	Gasoline product
Density at 20 ℃ in kg/m³	738.6	738.7	738.5	740.1	740.1
						Vapor Pressure (RVPE), kPa	51	51	51	50	50
Sulfur content, mg/L	9.4	9.4	9.4	9.4	10
						Group composition (FIA method)
Aromatic hydrocarbons,% (volume fraction)	15.6	15.6	15.7	15.8	15.5
						Olefin,% (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
						Measured RON	88.5	88.3	88.5	87.2	87.0
Measured MON	78.2	78.0	78.2	77.2	77.2
						Distillation range under normal pressure, 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 method of desulfurizing gasoline, the method comprising:

cutting a gasoline raw material to obtain a light gasoline fraction and a heavy gasoline fraction;

feeding the obtained heavy gasoline fraction into a first set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a first desulfurization reaction in a hydrogen state to obtain a first desulfurization product;

feeding the obtained light gasoline fraction into a second set of fluidization reactor to contact with an adsorption desulfurization catalyst and perform a second desulfurization reaction to obtain a second desulfurization product;

wherein the conditions of the first desulfurization reaction include: the first reaction temperature is 380-470 ℃, and the first reaction pressure is 2.0-3.5 MPa; the conditions of the second desulfurization reaction include: the second reaction temperature is 360-450 ℃, and the second reaction pressure is 1.5-3.0 Mpa; the second reaction temperature is 5-30 ℃ lower than the first reaction temperature; and the second reaction pressure is 0.1MPa-1.0MPa lower than the first reaction pressure.

2. The method of claim 1, further comprising: and mixing the obtained first desulfurization product with the second desulfurization product to obtain a gasoline product.

3. The process of claim 1 wherein the volume fraction of olefins in the gasoline feedstock is greater than 10% by volume.

4. The process of claim 1 wherein the gasoline feedstock has a sulfur content of 10 μ g/g or greater.

5. The process of claim 1, wherein the gasoline feedstock is at least one selected from the group consisting of catalytically cracked gasoline, coker gasoline, thermally cracked gasoline, and straight run gasoline.

6. The process according to claim 1, wherein the cut points of the light and heavy gasoline fractions are between 60 and 100 ℃.

7. The method of claim 1, wherein the first set of fluidized reactors and the second set of fluidized reactors are each independently selected from at least one of a fluidized bed, a riser, a downline conveyor reactor, a composite reactor comprised of a riser and a fluidized bed, a composite reactor comprised of a riser and a downline conveyor, a composite reactor comprised of two or more risers, a composite reactor comprised of two or more fluidized beds, and a composite reactor comprised of two or more downlines.

8. The method as claimed in claim 1 or 7, wherein the first set of fluidization reactors and the second set of fluidization reactors are independently selected from one or more of a constant diameter riser, a variable diameter riser and a dense-phase fluidized bed reactor, and both the first set of fluidization reactors and the second set of fluidization reactors belong to a gasoline adsorption desulfurization device.

9. The method according to claim 1, wherein the adsorption desulfurization catalyst contains silica, alumina, zinc oxide, and a desulfurization active metal which is at least one selected from the group consisting of cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin, and vanadium.