Method and device for co-producing low-carbon olefins and high-octane gasoline from Fischer-Tropsch synthesis products

Abstract

The present invention provides a method for co-producing low-carbon olefins and high-octane gasoline from Fischer-Tropsch synthesis products and a device for implementing the method. The method of the present invention feeds different Fischer-Tropsch synthesis products into three series-connected reactors respectively, wherein the first reactor is mainly used to process Fischer-Tropsch low-carbon saturated hydrocarbons for catalytic thermal cracking reaction; the second reactor is mainly used to process Fischer-Tropsch light oil for catalytic cracking reaction; the third reactor is mainly used to process Fischer-Tropsch heavy oil for catalytic cracking and aromatization reaction, thereby achieving the purpose of co-producing low-carbon olefins and high-octane gasoline with a higher yield. In particular, the method of the present invention can achieve the goal of obtaining low-carbon olefins with a yield of more than 39% and at the same time obtaining more than 34% of gasoline products with an octane number of more than 95.

Description

Technical Field

[0001] The present invention belongs to the field of Fischer-Tropsch synthesis product processing, and relates to a conversion method for Fischer-Tropsch synthesis products and a device for implementing the method, and specifically relates to a method for co-producing low-carbon olefins and high-octane gasoline from Fischer-Tropsch synthesis products and a device for implementing the method. Background Art

[0002] Fischer-Tropsch synthesis is a process that uses synthesis gas as raw material to synthesize liquid fuels mainly composed of saturated straight-chain hydrocarbons under catalysts and appropriate reaction conditions. Since sulfur and nitrogen pollutants are removed in the synthesis gas purification unit, Fischer-Tropsch synthesis technology can obtain extremely clean Fischer-Tropsch synthetic oil, and the source of synthesis gas is wide, which can be converted from coal, natural gas, coalbed methane and biomass, and is not restricted by natural oil reserves. Low-carbon olefins and high-octane gasoline both have high added value and can bring considerable economic benefits. Therefore, using Fischer-Tropsch synthesis products as raw materials to produce chemical raw materials, such as low-carbon olefins and high-octane gasoline, can better adapt to market changes.

[0003] It can be seen from the literature reports in recent years that the processing of Fischer-Tropsch synthesis products mainly adopts catalytic cracking technology, and the target product is mainly clean gasoline. Patent application CN106609154A discloses a method for producing gasoline from Fischer-Tropsch synthesis oil, which uses two parallel reactors to process Fischer-Tropsch oil products, wherein the first reactor is a riser reactor, the active components of the catalyst are zeolite molecular sieves and five-membered ring high silicon zeolite, and the processing distillation range is 200-750°C for Fischer-Tropsch synthesis products; the second reactor is a riser reactor, a fluidized bed reactor, a moving bed reactor, and a downward reactor, using a mixed catalyst of a catalyst to be regenerated and a regenerated catalyst as an aromatization catalyst to process liquefied gas and / or gasoline fractions. The conversion of Fischer-Tropsch synthesis products into aromatics requires a lower oil agent contact temperature and a longer oil agent contact time, while the oil agent contact temperature of this method is high and the contact time is short, and the aromatics yield is not ideal; in addition, this method cannot obtain more low-carbon olefins.

[0004] Patents CN105567299B, CN105567307B and CN106609151B disclose methods for producing light olefins from Fischer-Tropsch synthesis products. However, these methods do not focus on how to obtain gasoline.

[0005] From the existing technologies disclosed in this field, the processing of Fischer-Tropsch synthesis products mainly focuses on the process of producing gasoline from Fischer-Tropsch synthesis products or producing low-carbon olefins from Fischer-Tropsch synthesis products, while there are few reports on the process of co-producing high-octane gasoline in the process of producing low-carbon olefins from Fischer-Tropsch synthesis products. Summary of the invention

[0006] In order to solve the above problems, the inventors provide a method for co-producing low-carbon olefins and high-octane gasoline from Fischer-Tropsch synthesis products, and also provide a device for implementing the method. The method of the present invention feeds different Fischer-Tropsch synthesis products into three reactors in series, wherein the first reactor is mainly used to process Fischer-Tropsch low-carbon saturated hydrocarbons for catalytic thermal cracking reaction; the second reactor is mainly used to process Fischer-Tropsch light oil for catalytic cracking reaction; the third reactor is mainly used to process Fischer-Tropsch heavy oil for catalytic cracking and aromatization reaction, thereby achieving the purpose of co-producing low-carbon olefins and high-octane gasoline with a higher yield. In particular, the method of the present invention can achieve the purpose of obtaining a gasoline product with an octane number of more than 95 at a yield of more than 34% while obtaining low-carbon olefins at a yield of more than 39%.

[0007] In one aspect, the present invention provides a method for co-producing light olefins and high-octane gasoline from a Fischer-Tropsch synthesis product, the method comprising:

[0008] (1) feeding a Fischer-Tropsch low-carbon saturated hydrocarbon and an optional atomizing medium into a first reactor in an atomized form, contacting with a first catalyst and performing a catalytic thermal cracking reaction to obtain a first reactant stream and feeding the first reactant stream to a second reactor;

[0009] (2) feeding the Fischer-Tropsch light oil and an optional atomizing medium into a second reactor in an atomized form, mixing with the first reactant stream, contacting with a second catalyst and performing a catalytic cracking reaction to obtain a second reactant stream and feeding the second reactant stream to a third reactor;

[0010] (3) feeding the Fischer-Tropsch heavy oil and an optional atomizing medium into a third reactor in an atomized form, mixing with the second reactant stream, contacting with a third catalyst and performing catalytic cracking and aromatization reactions to obtain a third reactant stream;

[0011] (4) subjecting the third reaction stream obtained in step (3) to sedimentation separation to remove the spent catalyst from the third reaction stream; subjecting the obtained reaction products to fractionation to obtain gas phase products, gasoline products, and heavy oil, wherein the gas phase products are subjected to olefin separation to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins; subjecting the spent catalyst to stripping, optionally charring, and regenerating to obtain a regenerated catalyst, wherein the regenerated catalyst is returned to the first reactor, the second reactor, and the third reactor for recycling.

[0012] In some embodiments, the method further comprises returning the low-carbon saturated hydrocarbons obtained in step (4) to the first reactor for recycling.

[0013] On the other hand, the present invention provides a co-production device for implementing the above method, that is, a device for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products, the device comprising a reaction system, a regeneration system and a product separation system.

[0014] Wherein, the reaction system comprises:

[0015] The first reactor;

[0016] a second reactor, the second reactor being arranged in series with the first reactor;

[0017] a third reactor, wherein the third reactor is arranged in series with the second reactor;

[0018] a settling unit connected in fluid communication with the third reactor and the product separation system;

[0019] Wherein, the regeneration system is used for catalyst regeneration, and the regeneration system comprises:

[0020] a stripping section fluidly connected to the settling unit; and

[0021] A regenerator is fluidly connected to the stripping section and the first, second and third reactors.

[0022] In some embodiments, the product separation system comprises:

[0023] (a) a fractionation unit,

[0024] (b) an olefin separation unit,

[0025] The fractionation unit is connected to the sedimentation unit in a fluid communication manner, and the olefin separation unit is connected to the fractionation unit in a fluid communication manner.

[0026] In a preferred embodiment, the regeneration system further comprises:

[0027] A char drum is fluidly connected to the stripping section and the regenerator.

[0028] In some embodiments, a combustion furnace is further provided in the regeneration system, and the combustion furnace is fluidically connected to the coke drum to provide high-temperature flue gas containing oxygen to the coke drum.

[0029] The method described in the present invention can achieve the following beneficial effects:

[0030] (1) The method of the present invention can obtain light olefins at a yield of more than 39% (e.g., 39%-55%) and a gasoline product with an octane number of more than 95 (e.g., 95-99) at a yield of more than 34% (e.g., 34%-49%).

[0031] (2) The present invention feeds Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil, and Fischer-Tropsch heavy oil into the first reactor, the second reactor, and the third reactor, respectively. Fischer-Tropsch low-carbon saturated hydrocarbons undergo catalytic thermal cracking reactions by contacting with the catalyst at a relatively high temperature, Fischer-Tropsch light oil undergoes catalytic cracking reactions by contacting with the catalyst at a relatively high temperature, and Fischer-Tropsch heavy oil undergoes catalytic cracking and aromatization reactions by contacting with the catalyst at a relatively low temperature. The purpose of co-producing low-carbon olefins and high-octane gasoline can be better achieved by flexibly adjusting the feed raw material ratios of the three reactors.

[0032] (3) The present invention can increase the secondary reaction of the olefins of the catalytic cracking intermediate products of the Fischer-Tropsch synthesis product (such as the superposition cyclodehydrogenation reaction, etc.), which is beneficial to obtain more aromatic components in gasoline, thereby improving the octane number of gasoline. Therefore, the present invention uses three reactors to process the Fischer-Tropsch synthesis products respectively according to the different properties of the Fischer-Tropsch synthesis products, thereby achieving the co-production of low-carbon olefins and high-octane gasoline.

[0033] (4) The prior art has disclosed methods for producing gasoline and light olefins separately from Fischer-Tropsch synthesis products. The present invention adopts different processing methods for raw materials with different carbon numbers. The shorter the carbon number of the raw material, the higher the contact temperature with the catalyst; the longer the carbon number of the raw material, the lower the contact temperature with the catalyst. By processing multiple raw materials, it is possible to produce light olefins and high-octane gasoline at the same time, thereby achieving good economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 The diagram is a schematic diagram of an exemplary apparatus for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products according to the present invention.

[0035] Description of the reference numerals is as follows:

[0036] 1, first reactor; 2, second reactor; 3, third reactor; 4, combustion furnace; 5, charring tank; 6, regenerator; 7, reactor settler; 8, regenerator settler; 9, waiting pipe; 10, stripping section; 11, regeneration pipe I; 12, regeneration pipe II; 13, regeneration pipe III; 14, fractionation unit; 15, olefin separation unit.

[0037] I, Fischer-Tropsch low-carbon saturated hydrocarbons; II, Fischer-Tropsch light oil; III, Fischer-Tropsch heavy oil; IV, atomizing medium; V, stripping steam; VI, flue gas; VII, gas phase products; VIII, gasoline; IX, heavy oil; X, dry gas; XI, low-carbon saturated hydrocarbons; XII, low-carbon olefins. DETAILED DESCRIPTION

[0038] In order to better understand the present invention, it is further described below in conjunction with specific embodiments, but these embodiments should not be construed as any limitation to the present invention.

[0039] In the present invention, unless otherwise specified, the term "lower olefin" refers to C2-C4 olefin, for example, including ethylene, propylene, 1-butene, isobutylene, cis-2-butene, trans-2-butene or a mixture thereof.

[0040] In the present invention, unless otherwise specified, the term "lower carbon saturated hydrocarbon" refers to C2-C4 alkane, for example, including ethane, propane, butane, isobutane or a mixture thereof.

[0041] In the present invention, unless otherwise specified, the term "gas phase product" refers to the fraction with a distillation range below 15°C in the product.

[0042] In the present invention, unless otherwise specified, the term "gasoline product" refers to the fraction with a distillation range of 15°C to 220°C in the product.

[0043] In the present invention, unless otherwise specified, the term "aromatic hydrocarbons" refers to C6-C10 aromatic hydrocarbons, including benzene, toluene, ethylbenzene, o-xylene, m-xylene, p-xylene, and C9, C10 aromatic hydrocarbons or mixtures thereof.

[0044] In the present invention, unless otherwise specified, the term "heavy oil" refers to the fraction with a distillation range above 220°C in the product.

[0045] In the present invention, unless otherwise specified, the term "dry gas" refers to the remaining portion after separating the "olefins (i.e., light olefins)" and light saturated hydrocarbons in the "gas phase product". For example, the dry gas may include hydrogen, methane or a mixture thereof.

[0046] In the present invention, unless otherwise specified, the term "octane number" refers to the research octane number obtained by analyzing the "gasoline" product.

[0047] In the present invention, unless otherwise specified, the term "spent catalyst" refers to a carbon-containing catalyst after the catalyst has been reacted. For example, the term "spent catalyst" may refer to a carbon-containing catalyst before the catalyst has been reacted and steam stripped. In some cases, the term "spent catalyst" includes a carbon-containing catalyst obtained by reacting and stripping the catalyst, which is generally referred to as a stripped spent catalyst.

[0048] In the present invention, unless otherwise specified, the term "carbon deposition" refers to the carbon content of the spent catalyst characterized by a sulfur-carbon analyzer or a thermogravimetric analyzer, and then the total carbon content of the spent catalyst is calculated in combination with the loading amount.

[0049] In one aspect, the present invention provides a method for co-producing light olefins and high-octane gasoline from a Fischer-Tropsch synthesis product, the method comprising:

[0050] (1) feeding a Fischer-Tropsch low-carbon saturated hydrocarbon and an optional atomizing medium into a first reactor in an atomized form, contacting with a first catalyst and performing a catalytic thermal cracking reaction to obtain a first reactant stream and feeding the first reactant stream to a second reactor;

[0051] (2) feeding the Fischer-Tropsch light oil and an optional atomizing medium into a second reactor in an atomized form, mixing with the first reactant stream, contacting with a second catalyst and performing a catalytic cracking reaction to obtain a second reactant stream and feeding the second reactant stream to a third reactor;

[0052] (3) feeding the Fischer-Tropsch heavy oil and an optional atomizing medium into a third reactor in an atomized form, mixing with the second reactant stream, contacting with a third catalyst and performing catalytic cracking and aromatization reactions to obtain a third reactant stream;

[0053] (4) subjecting the third reaction stream obtained in step (3) to sedimentation separation to remove the spent catalyst from the third reaction stream; subjecting the obtained reaction products to fractionation to obtain gas phase products, gasoline products, and heavy oil, wherein the gas phase products are subjected to olefin separation to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins; subjecting the spent catalyst to stripping, optionally charring, and regenerating to obtain a regenerated catalyst, wherein the regenerated catalyst is returned to the first reactor, the second reactor, and the third reactor for recycling.

[0054] In some embodiments, the method further comprises returning the low-carbon saturated hydrocarbons obtained in step (4) to the first reactor for recycling.

[0055] In step (1), the Fischer-Tropsch low-carbon saturated hydrocarbons are C2-C4 alkanes obtained by separating olefins from Fischer-Tropsch liquefied gas, and specifically may include ethane, propane, butane, isobutane or a mixture thereof. Wherein, the Fischer-Tropsch liquefied gas may be C2-C4 hydrocarbons in the Fischer-Tropsch synthesis product. For example, the Fischer-Tropsch liquefied gas may include ethane, ethylene, propane, propylene, n-butane, isobutane, cis-2-butene, trans-2-butene or a mixture thereof.

[0056] In step (2), the Fischer-Tropsch light oil is selected from Fischer-Tropsch synthesis light components with an initial boiling point of 36° C. to 220° C., but is not limited thereto. In some embodiments, the Fischer-Tropsch light oil mainly comprises C5-C12 hydrocarbons in the Fischer-Tropsch synthesis product.

[0057] In step (3), the Fischer-Tropsch heavy oil is a Fischer-Tropsch synthesis heavy component having an initial boiling point greater than 220° C., preferably greater than 280° C. In some embodiments, the Fischer-Tropsch heavy oil mainly comprises hydrocarbons above C12 in the Fischer-Tropsch synthesis product.

[0058] In the present invention, the mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil may be (5-30):(5-40):(30-90).

[0059] In a preferred embodiment, in step (1), step (2) or step (3), the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil is mixed with the optional atomizing medium for atomization. Wherein, the atomizing medium can be selected from one or more of methanol, ethanol, propanol, dry gas, nitrogen or water vapor, such as a mixture thereof. The dry gas includes one or more of hydrogen, methane and ethane. In some embodiments, the dry gas may be hydrogen, methane or ethane in the Fischer-Tropsch product. In the present invention, atomization can be carried out according to the operating process available in the art.

[0060] In a specific embodiment, the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon to the atomizing medium may be 1:(0-1), preferably 1:(0.1-1), for example, 1:0, 1:0.1, 1:0.15, 1:0.18, 1:0.2, 1:0.25, 1:0.3, 1:0.35, 1:0.4, 1:0.45, 1:0.5, 1:0.55, 1:0. 6, 1:0.65, 1:0.7, 1:0.75, 1:0.8, 1:0.85, 1:0.9, 1:0.95 or 1:1; or, the mass ratio of the Fischer-Tropsch light oil to the atomizing medium may be 1:(0-1), preferably 1:(0.1-1), for example, 1:0, 1:0.1, 1:0.15, 1:0.18, 1:0.2, 1:0.25, 1:0. :0.3, 1:0.35, 1:0.4, 1:0.45, 1:0.5, 1:0.55, 1:0.6, 1:0.65, 1:0.7, 1:0.75, 1:0.8, 1:0.85, 1:0.9, 1:0.95 or 1:1; or, the mass ratio of the Fischer-Tropsch heavy oil to the atomizing medium may be 1:(0-1), preferably 1:(0.1-1) , for example, 1:0, 1:0.1, 1:0.15, 1:0.18, 1:0.2, 1:0.25, 1:0.3, 1:0.35, 1:0.4, 1:0.45, 1:0.5, 1:0.55, 1:0.6, 1:0.65, 1:0.7, 1:0.75, 1:0.8, 1:0.85, 1:0.9, 1:0.95 or 1:1.

[0061] Preferably, in step (1), the weight ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon to the atomizing medium is 1:(0-0.6), preferably 1:(0.15-0.6). Preferably, in step (2), the weight ratio of the Fischer-Tropsch light oil to the atomizing medium is 1:(0-0.8), preferably 1:(0.15-0.5). Preferably, in step (3), the weight ratio of the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0-0.8), preferably 1:(0.15-0.5).

[0062] In some preferred embodiments, in step (1), step (2) or step (3), the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil are preheated before atomization. Preferably, the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil are preheated to 100°C-400°C. More preferably, in step (1), the Fischer-Tropsch low-carbon saturated hydrocarbons are preheated to 100°C-350°C. Preferably, in step (2), the Fischer-Tropsch light oil is preheated to 100°C-350°C. In step (3), the Fischer-Tropsch heavy oil is preheated to 100°C-350°C.

[0063] In some preferred embodiments, the active components of the first catalyst, the second catalyst and the third catalyst of the present invention are selected from at least one of the following: unmodified or modified eight-membered ring molecular sieve, ten-membered ring molecular sieve or twelve-membered ring molecular sieve, or metal oxide. Preferably, the eight-membered ring molecular sieve, ten-membered ring molecular sieve or twelve-membered ring molecular sieve can be selected from SAPO-34, SAPO-18, ITQ-13, IM-5, ZSM-5, ZSM-11, MCM-22, EU-1, beta, mordenite molecular sieve, etc. Preferably, the metal oxide can be selected from one or more of zinc oxide, lanthanum oxide, magnesium oxide, manganese oxide, cerium oxide, gallium oxide, chromium oxide, nickel oxide and tungsten oxide.

[0064] In some preferred embodiments, the active components of the first catalyst, the second catalyst and the third catalyst account for 20wt%-60wt% of the catalyst weight on a dry basis. In addition, preferably, in addition to the active components, the first catalyst, the second catalyst and the third catalyst also contain a remaining amount of aluminum oxide and / or silicon oxide as a carrier.

[0065] In some preferred embodiments, the first catalyst may be a mixed catalyst of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the first catalyst may be 0wt%-2.00wt%. In another further preferred embodiment, the second catalyst may be a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the second catalyst may be 0wt%-2.0wt%. In another further preferred embodiment, the third catalyst may be a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the third catalyst may be 0wt%-2.0wt%.

[0066] In some preferred embodiments, in step (1), the reaction conditions of the first reactor are: temperature 500°C-750°C, preferably 580°C-680°C; pressure 0.01-0.7 MPa, preferably 0.1-0.5 MPa; weight hourly space velocity 10-300 h -1 , preferably 40-200h -1 ; Agent-oil ratio 0.5-50, preferably 5-30.

[0067] In some preferred embodiments, in step (2), the reaction conditions of the second reactor are: temperature 450°C-700°C, preferably 530°C-630°C; pressure 0.01-0.7MPa, preferably 0.1-0.5MPa; weight hourly space velocity 1-150h -1 , preferably 40-120h -1 ; Agent-oil ratio 1-40, preferably 5-25.

[0068] In some preferred embodiments, in step (3), the reaction conditions of the third reactor are: temperature 400°C-650°C, preferably 480°C-580°C; pressure 0.01-0.7MPa, preferably 0.1-0.5MPa; weight hourly space velocity 0.5-30h -1 , preferably 2-20h -1 ; Agent-oil ratio 1-20, preferably 2-15.

[0069] In some preferred embodiments, the first reactor is a transport bed reactor, a fast bed reactor or a turbulent bed reactor, preferably a transport bed reactor and a fast bed reactor. The raw materials with shorter carbon chains can contact with the catalyst at a higher temperature to undergo catalytic thermal cracking reaction, thereby obtaining more olefins.

[0070] In some preferred embodiments, the second reactor is a fast bed reactor, a turbulent bed reactor or a bubbling bed reactor, preferably a turbulent bed reactor or a fast bed reactor, wherein the raw material with a moderate carbon chain length can contact with the catalyst at a higher temperature to undergo a catalytic cracking reaction, thereby obtaining more olefins.

[0071] In some preferred embodiments, the third reactor is a turbulent bed reactor, a bubbling bed reactor or a bulk fluidized bed reactor, preferably a turbulent bed reactor or a bubbling bed reactor. The raw materials with longer carbon chains can contact with the catalyst at a lower temperature and undergo more catalytic cracking reactions, superposition reactions, cyclization reactions, hydrogen transfer reactions and aromatization reactions under the condition of lower space velocity, thereby obtaining more high-octane components in gasoline, such as aromatics.

[0072] In some preferred embodiments, in step (4), the operating pressure of the sedimentation separation is 0.01-0.7 MPa, preferably 0.1-0.5 MPa.

[0073] Herein, fractionation, olefin separation and stripping are all performed by conventional operations in the art without any particular limitation.

[0074] In some preferred embodiments, 10-90% of the low-carbon saturated hydrocarbons obtained in step (4) can be returned to the first reactor for recycling.

[0075] In some preferred embodiments, in step (4), the spent catalyst is contacted with an oxygen-containing gas to carry out the optional charring and regeneration under the following conditions: a pressure of 0.01-0.7 MPa, preferably 0.1-0.5 MPa; a temperature of 550° C.-750° C., preferably 580° C.-700° C. Preferably, the oxygen-containing gas may be air or oxygen-containing high-temperature flue gas.

[0076] In another aspect, the present invention provides a co-production device for implementing the above method, that is, a device for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products, the device comprising a reaction system, a regeneration system and a product separation system.

[0077] Wherein, the reaction system comprises:

[0078] The first reactor;

[0079] a second reactor, the second reactor being arranged in series with the first reactor;

[0080] a third reactor, wherein the third reactor is arranged in series with the second reactor;

[0081] a settling unit connected in fluid communication with the third reactor and the product separation system;

[0082] Wherein, the regeneration system comprises:

[0083] a stripping section fluidly connected to the settling unit;

[0084] A regenerator is fluidly connected to the stripping section and the first, second and third reactors.

[0085] In a preferred embodiment, the regeneration system further comprises:

[0086] A char drum is fluidly connected to the stripping section and the regenerator.

[0087] In some embodiments, a combustion furnace is further provided in the regeneration system, and the combustion furnace is fluidically connected to the charring drum to provide oxygen-containing high-temperature flue gas (for example, the flue gas temperature is 550° C.-750° C.) to the charring drum.

[0088] In some embodiments, the fuel gas and air are sent into the combustion furnace and ignited to generate oxygen-containing high-temperature flue gas, and then the oxygen-containing high-temperature flue gas is allowed to enter the coke tank. In some embodiments, the fuel gas can be selected from liquefied petroleum gas, and the composition is C3, C4 alkane.

[0089] In some embodiments, the product separation system comprises:

[0090] a fractionation unit connected in fluid communication with the sedimentation unit;

[0091] An olefin separation unit is fluidly connected to the fractionation unit.

[0092] In some preferred embodiments, the first reactor is a transport bed reactor, a fast bed reactor or a turbulent bed reactor, preferably a transport bed reactor or a fast bed reactor.

[0093] In some preferred embodiments, the second reactor is a fast bed reactor, a turbulent bed reactor or a bubbling bed reactor, preferably a fast bed reactor or a turbulent bed reactor.

[0094] In some preferred embodiments, the third reactor is a turbulent bed reactor, a bubbling bed reactor or a bulk fluidized bed reactor, preferably a turbulent bed reactor or a bubbling bed reactor.

[0095] Herein, the first reactor, the second reactor and the third reactor may share one settler.

[0096] The method provided by the present invention is further described below in conjunction with the accompanying drawings.

[0097] The Fischer-Tropsch low-carbon saturated hydrocarbons preheated to 100°C-400°C and the optional atomizing medium are mixed and atomized in a mass ratio of 1:(0-1) and then fed into the first reactor; the reaction temperature is 500°C-750°C, the reaction pressure is 0.01-0.7MPa, the catalyst-oil ratio is 0.5-50, and the weight hourly space velocity is 10-300h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0098] The Fischer-Tropsch light oil preheated to 100-400°C and the optional atomizing medium are mixed and atomized in a mass ratio of 1:(0-1) and then fed into the second reactor; the Fischer-Tropsch light oil is mixed with the first reactant stream after entering the second reactor, and the reaction temperature is 450-700°C, the reaction pressure is 0.01-0.7MPa, the agent-oil ratio is 1-40, and the weight hourly space velocity is 1-150h -1 The second reactant stream carrying the second catalyst after the reaction is sent to the third reactor.

[0099] The Fischer-Tropsch heavy oil preheated to 100°C-400°C and the optional atomizing medium are mixed and atomized in a mass ratio of 1:(0-1) and then fed into the third reactor; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor, and the reaction temperature is 400°C-650°C, the reaction pressure is 0.01-0.7MPa, the agent-oil ratio is 1-20, and the weight hourly space velocity is 0.5-30h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0100] The third reactant stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.01-0.7 MPa to obtain a reaction product and a catalyst to be produced. The reaction product enters a fractionation unit for fractionation to obtain a gas phase product, a gasoline product and a heavy oil, wherein the gas phase product enters an olefin separation unit for olefin separation to obtain dry gas, low carbon saturated hydrocarbons and low carbon olefins. In some preferred embodiments, 10-90% of the obtained low carbon saturated hydrocarbons can be returned to the first reactor for recycling.

[0101] The catalyst to be regenerated is steam stripped in the stripping section and then sent to an optional coking tank and regenerator through a regeneration pipe for optional coking and regeneration. It is contacted with an oxygen-containing gas (such as air) at a temperature of 550°C-750°C and a pressure of 0.1-0.7MPa to burn off the carbon deposits to obtain a regenerated catalyst. The regenerated catalyst is circulated back to the first reactor, the second reactor and the third reactor through regeneration pipe I, regeneration pipe II and regeneration pipe III for recycling.

[0102] The exemplary technical solutions of the present invention can be described by the contents in the following numbered paragraphs, but the protection scope of the present invention is not limited thereto:

[0103] 1. A method for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products, the method comprising:

[0104] (1) feeding a Fischer-Tropsch low-carbon saturated hydrocarbon and an optional atomizing medium into a first reactor in an atomized form, contacting with a first catalyst and performing a catalytic thermal cracking reaction to obtain a first reactant stream and feeding the first reactant stream to a second reactor;

[0105] (2) feeding the Fischer-Tropsch light oil and an optional atomizing medium into a second reactor in an atomized form, mixing with the first reactant stream, contacting with a second catalyst and performing a catalytic cracking reaction to obtain a second reactant stream and feeding the second reactant stream to a third reactor;

[0106] (3) feeding the Fischer-Tropsch heavy oil and an optional atomizing medium into a third reactor in an atomized form, mixing with the second reactant stream, contacting with a third catalyst and performing catalytic cracking and aromatization reactions to obtain a third reactant stream;

[0107] (4) subjecting the third reaction stream obtained in step (3) to sedimentation separation to remove the spent catalyst from the third reaction stream; subjecting the obtained reaction products to fractionation to obtain gas phase products, gasoline products, and heavy oil, wherein the gas phase products are subjected to olefin separation to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins; subjecting the spent catalyst to stripping, optionally charring, and regenerating to obtain a regenerated catalyst, wherein the regenerated catalyst is returned to the first reactor, the second reactor, and the third reactor for recycling.

[0108] 2. The method as described in paragraph 1, wherein the method further comprises returning the low-carbon saturated hydrocarbons obtained in step (4) to the first reactor for recycling.

[0109] 3. The method as described in paragraph 1, wherein the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil and the Fischer-Tropsch heavy oil is (5-30): (5-40): (30-90).

[0110] 4. The method according to any one of paragraphs 1 to 3, wherein in step (1), step (2) or step (3), the atomizing medium is selected from methanol, ethanol, propanol, dry gas, nitrogen or water vapor, or a mixture thereof.

[0111] 5. The method as described in paragraph 4, wherein the dry gas comprises one or more of hydrogen, methane and ethane.

[0112] 6. The method described in paragraph 4, wherein the dry gas is hydrogen, methane, and ethane in Fischer-Tropsch products.

[0113] 7. A method as described in any one of paragraphs 1-3, wherein, in step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0-1).

[0114] 8. The method described in paragraph 7, wherein, in step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0.1-1).

[0115] 9. The method of paragraph 7, wherein, in step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:0, 1:0.1, 1:0.15, 1:0.18, 1:0.2, 1:0.25, 1:0.3, 1:0.35, 1:0.4, 1:0.45, 1:0.5, 1:0.55, 1:0.6, 1:0.65, 1:0.7, 1:0.75, 1:0.8, 1:0.85, 1:0.9, 1:0.95 or 1:1.

[0116] 10. A method as described in any one of paragraphs 1-3, wherein, in step (1), the weight ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the atomizing medium is 1:(0-0.6); or wherein, in step (2), the weight ratio of the Fischer-Tropsch light oil to the atomizing medium is 1:(0-0.8); or wherein, in step (3), the weight ratio of the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0-0.8).

[0117] 11. A method as described in paragraph 10, wherein, in step (1), the weight ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the atomizing medium is 1:(0.15-0.6); or wherein, in step (2), the weight ratio of the Fischer-Tropsch light oil to the atomizing medium is 1:(0.15-0.5); or wherein, in step (3), the weight ratio of the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0.15-0.5).

[0118] 12. The method of any one of paragraphs 1 to 3, wherein in step (1), step (2) or step (3), the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil is preheated before atomization.

[0119] 13. The method of paragraph 12, wherein the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil is preheated to 100°C-400°C.

[0120] 14. The method of paragraph 13, wherein the Fischer-Tropsch low carbon saturated hydrocarbons are preheated to 100°C-350°C; or, wherein the Fischer-Tropsch light oil is preheated to 100°C-350°C; or, wherein the Fischer-Tropsch heavy oil is preheated to 100°C-350°C.

[0121] 15. The method of any one of paragraphs 1 to 3, wherein the active components of the first catalyst, the second catalyst and the third catalyst are at least one selected from the following: unmodified or modified eight-membered ring molecular sieve, ten-membered ring molecular sieve or twelve-membered ring molecular sieve, or metal oxide.

[0122] 16. The method of paragraph 15, wherein the eight-membered ring molecular sieve, the ten-membered ring molecular sieve or the twelve-membered ring molecular sieve is selected from SAPO-34, SAPO-18, ITQ-13, IM-5, ZSM-5, ZSM-11, MCM-22, EU-1, beta, and mordenite molecular sieves; preferably, the metal oxide is selected from one or more of zinc oxide, lanthanum oxide, magnesium oxide, manganese oxide, cerium oxide, gallium oxide, chromium oxide, nickel oxide, and tungsten oxide.

[0123] 17. The method of paragraph 15, wherein the active components of the first catalyst, the second catalyst, and the third catalyst account for 20 wt% to 60 wt% of the weight of the catalyst on a dry basis.

[0124] 18. The method according to paragraph 17, wherein the first catalyst, the second catalyst and the third catalyst further contain a residual amount of aluminum oxide and / or silicon oxide as a carrier in addition to the active component.

[0125] 19. A method as described in any one of paragraphs 1-3, wherein the first catalyst is a mixed catalyst of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the first catalyst is 0wt%-2.00wt%; or, wherein the second catalyst is a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the second catalyst is 0wt%-2.0wt%; or, wherein the third catalyst is a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the third catalyst is 0wt%-2.0wt%.

[0126] 20. The method according to any one of paragraphs 1 to 3, wherein in step (1), the reaction conditions of the first reactor are: temperature 500°C-750°C; pressure 0.01-0.7 MPa; weight hourly space velocity 10-300 h -1 ; Agent-oil ratio 0.5-50.

[0127] 21. The method of paragraph 20, wherein the temperature is 580°C-680°C; or the pressure is 0.1-0.5 MPa; or the weight hourly space velocity is 40-200 h -1 ; Alternatively, the agent-oil ratio is 5-30.

[0128] 22. The method according to any one of paragraphs 1 to 3, wherein in step (2), the reaction conditions of the second reactor are: temperature 450°C-700°C; pressure 0.01-0.7 MPa; weight hourly space velocity 1-150 h -1 ; Agent-oil ratio 1-40.

[0129] 23. The method of paragraph 22, wherein the temperature is 530°C-630°C; or, the pressure is 0.1-0.5 MPa; or, the weight hourly space velocity is 40-120 h -1 ; Alternatively, the agent-oil ratio is 5-25.

[0130] 24. The method according to any one of paragraphs 1 to 3, wherein in step (3), the reaction conditions of the third reactor are: temperature 400°C-650°C; pressure 0.01-0.7 MPa; weight hourly space velocity 0.5-30 h -1 ; Agent-oil ratio 1-20.

[0131] 25. The method of paragraph 24, wherein the temperature is 480°C-580°C; or, the pressure is 0.1-0.5 MPa; or, the weight hourly space velocity is 2-20 h -1 ; Alternatively, the agent-oil ratio is 2-15.

[0132] 26. The method of any one of paragraphs 1 to 3, wherein the first reactor is a transport bed reactor, a fast bed reactor or a turbulent bed reactor; or, the second reactor is a fast bed reactor, a turbulent bed reactor or a bubbling bed reactor; or, the third reactor is a turbulent bed reactor, a bubbling bed reactor or a dispersed fluidized bed reactor.

[0133] 27. The method of paragraph 26, wherein the first reactor is a transport bed reactor or a fast bed reactor; or, the second reactor is a fast bed reactor or a turbulent bed reactor; or, the third reactor is a bubbling bed reactor or a turbulent bed reactor.

[0134] 28. The method according to any one of paragraphs 1 to 3, wherein in step (4), the operating pressure of the sedimentation separation is 0.01-0.7 MPa.

[0135] 29. The method of paragraph 2, wherein 10%-90% of the low-carbon saturated hydrocarbons obtained in step (4) are returned to the first reactor for recycling.

[0136] 30. The method of any one of paragraphs 1 to 3, wherein in step (4), the spent catalyst is contacted with an oxygen-containing gas and optionally charred and regenerated under the following conditions: a pressure of 0.01-0.7 MPa; and a temperature of 550° C.-750° C.

[0137] 31. The method of paragraph 29, wherein the oxygen-containing gas is air or oxygen-containing high-temperature flue gas.

[0138] 32. A device for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products, the device comprising a reaction system, a regeneration system and a product separation system,

[0139] Wherein, the reaction system comprises:

[0140] The first reactor;

[0141] a second reactor, the second reactor being arranged in series with the first reactor;

[0142] a third reactor, wherein the third reactor is arranged in series with the second reactor;

[0143] a settling unit connected in fluid communication with the third reactor and the product separation system;

[0144] Wherein, the regeneration system comprises:

[0145] a stripping section fluidly connected to the settling unit;

[0146] a regenerator connected in fluid communication to the stripping section and the first, second and third reactors,

[0147] Wherein, the product separation system comprises:

[0148] a fractionation unit connected in fluid communication with the sedimentation unit;

[0149] An olefin separation unit is fluidly connected to the fractionation unit.

[0150] 33. The apparatus of paragraph 32, wherein the regeneration system further comprises:

[0151] A char drum is fluidly connected to the stripping section and the regenerator.

[0152] 34. The apparatus as described in paragraph 33, wherein a combustion furnace is further provided in the regeneration system, and the combustion furnace is fluidically connected to the coke drum to provide oxygen-containing high-temperature flue gas to the coke drum.

[0153] 35. The apparatus of any of paragraphs 32-34, wherein the first reactor, the second reactor, and the third reactor share a common settler.

[0154] Example

[0155] Unless otherwise specified, the reagents, materials and devices involved in the following examples are all commercially available in the art; the conventional operations involved in the following examples can be found in patents, patent applications and publications disclosed in the art (for example, He Yongde, ed., "Modern Coal Chemical Technology Handbook", Chemical Industry Press, 2003, the entire contents of which are incorporated herein).

[0156] The relevant properties of the Fischer-Tropsch heavy oil, Fischer-Tropsch light oil, Fischer-Tropsch low-carbon saturated hydrocarbons and dry gas used in the following examples are shown in Tables 1, 2 and 3.

[0157] Table 1 Relevant properties of Fischer-Tropsch synthesis products

[0158]

[0159]

[0160] Note: * means the upper limit of chromatographic detection is 720℃, eluting at 79%; / ** means exceeding the upper limit of detection

[0161] Table 2 Fischer-Tropsch low carbon saturated hydrocarbon composition

[0162] Content, wt% Ethane 5％ Propane 40％ Butane 21％ Isobutane 34％

[0163] Table 3 Composition of dry gas

[0164] Content, wt% hydrogen 36％ Methane 64％

[0165] Table 4 Molecular sieve, type and content of modifying elements, composition, specific surface area and pore volume of catalysts

[0166]

[0167]

[0168] Example 1

[0169] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 10:10:80, and the catalyst is the above-mentioned cat-1 catalyst.

[0170] The Fischer-Tropsch low-carbon saturated hydrocarbons and methanol preheated to 250°C are mixed and fed into the first transport bed reactor by methanol atomization, and the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to methanol is 1:0.25; at a reaction temperature of 660°C, a catalyst-to-oil ratio of the first catalyst and the Fischer-Tropsch low-carbon saturated hydrocarbons in the first reactor of 10, and a weight hourly space velocity of 60h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0171] The Fischer-Tropsch light oil preheated to 200°C and methanol were mixed and fed into the second fast bed reactor by methanol atomization, and the mass ratio of Fischer-Tropsch light oil to methanol was 1:0.25; the Fischer-Tropsch light oil was mixed with the first reactant stream after entering the second reactor; at a reaction temperature of 560°C, a catalyst-to-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil of 8, and a weight hourly space velocity of 50h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reactant stream. The second reactant stream carries the reacted second catalyst to the third reactor.

[0172] The Fischer-Tropsch heavy oil preheated to 150°C and methanol are mixed and sent to the third turbulent bed reactor by methanol atomization, and the mass ratio of the Fischer-Tropsch heavy oil to methanol is 1:0.25; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; at a reaction temperature of 470°C, a catalyst-to-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil of 2.2, and a weight hourly space velocity of 4h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0173] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in the settler at an operating pressure of 0.3 MPa to obtain reaction products and catalyst to be produced; the reaction products enter the fractionation unit to obtain gas phase products, gasoline products, and heavy oil, wherein the gas phase products pass through the olefin separation unit to obtain dry gas, low carbon saturated hydrocarbons, and low carbon olefins. Among them, 10% of the low carbon saturated hydrocarbons are returned to the first reactor for refining.

[0174] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0175] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 630℃ and the pressure is 0.3MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0176] Comparative Example 1

[0177] The reaction conditions of this comparative example are the same as those in the first reactor of Example 1, except that the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil are mixed and then all enter the first reactor, and the second reactor is only used to upgrade the catalyst, and the third reactor is only used to circulate the catalyst. As can be seen from Comparative Example 1, the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil all enter the first reactor for reaction, and more olefins are obtained, but the yield and octane number of the gasoline product are low.

[0178] Comparative Example 2

[0179] Except that the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil are mixed and then all enter the third reactor, the reaction conditions of this comparative example are the same as the reaction conditions in the third reactor of Example 1, and the first reactor and the second reactor are only used to improve the catalyst. It can be seen from Comparative Example 2 that the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil all enter the third reactor for reaction, producing more liquid products, while the yield and octane number of low-carbon olefins and gasoline products are relatively low.

[0180] Example 2

[0181] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 5:15:80, and the catalyst is the above-mentioned cat-2 catalyst.

[0182] The Fischer-Tropsch low-carbon saturated hydrocarbons and methanol preheated to 280°C are mixed and fed into the first fast bed reactor by methanol atomization, and the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to methanol is 1:0.25; at a reaction temperature of 610°C, a catalyst-to-oil ratio of the first catalyst and the Fischer-Tropsch low-carbon saturated hydrocarbons in the first reactor of 15, and a weight hourly space velocity of 45h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0183] The Fischer-Tropsch light oil preheated to 250°C and methanol were mixed and sent to the second turbulent bed reactor by methanol atomization, and the mass ratio of Fischer-Tropsch light oil to methanol was 1:0.25; the Fischer-Tropsch light oil was mixed with the first reaction stream after entering the second reactor; at a reaction temperature of 560°C, a catalyst-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil of 10, and a weight hourly space velocity of 60h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reaction stream. The second reaction stream carries the reacted second catalyst and is lifted to the third reactor through the lifting pipe.

[0184] The Fischer-Tropsch heavy oil preheated to 180°C and methanol are mixed and sent into the third bubbling bed reactor by methanol atomization, and the mass ratio of the Fischer-Tropsch heavy oil to methanol is 1:0.25; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; at a reaction temperature of 490°C, a catalyst-to-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil of 3.5, and a weight hourly space velocity of 4h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0185] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.5 MPa to obtain a reaction product and a catalyst to be produced; the reaction product is fractionated to obtain a gas phase product, a gasoline product, and a heavy oil, wherein the gas phase product is passed through an olefin separation unit to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins. Among them, 20% of the low-carbon saturated hydrocarbons are returned to the first reactor for refining.

[0186] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0187] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 580℃ and the pressure is 0.5MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0188] Example 3

[0189] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 5:5:90, and the catalyst is the above-mentioned cat-3 catalyst.

[0190] The Fischer-Tropsch low-carbon saturated hydrocarbons preheated to 250°C were mixed with water vapor and fed into the first turbulent bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the water vapor was 1:0.35; at a reaction temperature of 580°C, a catalyst-to-oil ratio of the first catalyst in the first reactor to the Fischer-Tropsch low-carbon saturated hydrocarbons was 20, and a weight hourly space velocity of 45h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0191] The Fischer-Tropsch light oil preheated to 200°C and water vapor are mixed and sent into the second bubbling bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch light oil to the water vapor is 1:0.25; the Fischer-Tropsch light oil is mixed with the first reactant stream after entering the second reactor; at a reaction temperature of 530°C, a catalyst-to-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil of 20, and a weight hourly space velocity of 45h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reactant stream. The second reactant stream carries the reacted second catalyst to the third reactor.

[0192] The Fischer-Tropsch heavy oil preheated to 180°C is mixed with water vapor and sent into the third dispersed fluidized bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch heavy oil to the water vapor is 1:0.35; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; at a reaction temperature of 490°C, a catalyst-to-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil of 2.4, and a weight hourly space velocity of 4.5h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0193] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.3 MPa to obtain a reaction product and a catalyst to be produced; the reaction product is fractionated to obtain a gas phase product, a gasoline product, and a heavy oil, wherein the gas phase product is passed through an olefin separation unit to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins. Among them, 30% of the low-carbon saturated hydrocarbons are returned to the first reactor for refining.

[0194] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0195] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 630℃ and the pressure is 0.3MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0196] Example 4

[0197] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 20:20:60, and the catalyst is the above-mentioned cat-4 catalyst.

[0198] The Fischer-Tropsch low-carbon saturated hydrocarbons preheated to 280°C were mixed with dry gas and fed into the first transport bed reactor by dry gas atomization. The mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the dry gas was 1:0.25. The reaction temperature was 530°C, the catalyst-to-oil ratio of the first catalyst in the first reactor to the Fischer-Tropsch low-carbon saturated hydrocarbons was 6, and the weight hourly space velocity was 100h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0199] The Fischer-Tropsch light oil preheated to 250°C and dry gas are mixed and fed into the second fast bed reactor by dry gas atomization, and the mass ratio of the Fischer-Tropsch light oil to the dry gas is 1:0.18; the Fischer-Tropsch light oil is mixed with the first reactant stream after entering the second reactor; at a reaction temperature of 530°C, a catalyst-to-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil of 25, and a weight hourly space velocity of 75h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reactant stream. The second reactant stream carries the reacted second catalyst to the third reactor.

[0200] The Fischer-Tropsch heavy oil preheated to 180°C and dry gas are mixed and sent into the third turbulent bed reactor by dry gas atomization, and the mass ratio of the Fischer-Tropsch heavy oil to the dry gas is 1:0.3; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; at a reaction temperature of 430°C, a catalyst-to-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil of 5.5, and a weight hourly space velocity of 10h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0201] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.3 MPa to obtain a reaction product and a catalyst to be produced; the reaction product is fractionated to obtain a gas phase product, a gasoline product, and a heavy oil, wherein the gas phase product is passed through an olefin separation unit to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins. Among them, 40% of the low-carbon saturated hydrocarbons are returned to the first reactor for refining.

[0202] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0203] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 680℃ and the pressure is 0.3MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0204] Example 5

[0205] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 25:30:45, and the catalyst is the above-mentioned cat-5 catalyst.

[0206] The Fischer-Tropsch low-carbon saturated hydrocarbons preheated to 250°C were mixed with dry gas and fed into the first fast bed reactor by dry gas atomization, and the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the dry gas was 1:0.6; at a reaction temperature of 670°C, a catalyst-to-oil ratio of the first catalyst in the first reactor to the Fischer-Tropsch low-carbon saturated hydrocarbons was 15, and a weight hourly space velocity of 120h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0207] The Fischer-Tropsch light oil preheated to 200°C and dry gas were mixed and fed into the second turbulent bed reactor by dry gas atomization, and the mass ratio of the Fischer-Tropsch light oil to the dry gas was 1:0.3; the Fischer-Tropsch light oil was mixed with the first reactant stream after entering the second reactor; at a reaction temperature of 610°C, a catalyst-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil of 8, and a weight hourly space velocity of 100h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reactant stream. The second reactant stream carries the reacted second catalyst to the third reactor.

[0208] The Fischer-Tropsch heavy oil preheated to 150°C and dry gas are mixed and sent into the third bubbling bed reactor by dry gas atomization, and the mass ratio of the Fischer-Tropsch heavy oil to the dry gas is 1:0.18; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; at a reaction temperature of 530°C, a catalyst-to-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil of 6.2, and a weight hourly space velocity of 8h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0209] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.5 MPa to obtain a reaction product and a catalyst to be produced; the reaction product is fractionated to obtain a gas phase product, a gasoline product, and a heavy oil, wherein the gas phase product is passed through an olefin separation unit to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins. Among them, 50% of the low-carbon saturated hydrocarbons are returned to the first reactor for refining.

[0210] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0211] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 630℃ and the pressure is 0.5MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0212] Example 6

[0213] The mass ratio of Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil and Fischer-Tropsch heavy oil is 30:40:30, and the catalyst is the above-mentioned cat-6 catalyst.

[0214] The Fischer-Tropsch low-carbon saturated hydrocarbons preheated to 280°C were mixed with water vapor and fed into the first turbulent bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons to the water vapor was 1:0.3; the reaction temperature was 680°C, the reaction pressure was 0.2MPa, the catalyst-to-oil ratio of the first catalyst in the first reactor to the Fischer-Tropsch low-carbon saturated hydrocarbons was 10, and the weight hourly space velocity was 180h -1 The first catalyst is contacted with the first catalyst under the conditions of catalytic thermal cracking reaction to obtain a first reaction stream. The first reaction stream carries the first catalyst after the reaction upward and enters the second reactor.

[0215] The Fischer-Tropsch light oil preheated to 250°C and water vapor are mixed and sent into the second bubbling bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch light oil to the water vapor is 1:0.25; the Fischer-Tropsch light oil is mixed with the first reactant stream after entering the second reactor; the reaction temperature is 630°C, the reaction pressure is 0.2MPa, the catalyst-oil ratio of the second catalyst in the second reactor to the Fischer-Tropsch light oil is 5, and the weight hourly space velocity is 120h -1 The second catalyst is contacted with the second catalyst under the conditions of catalytic cracking reaction to obtain a second reactant stream. The second reactant stream carries the reacted second catalyst to the third reactor.

[0216] The Fischer-Tropsch heavy oil preheated to 180°C is mixed with water vapor and sent into the third dispersed fluidized bed reactor by water vapor atomization, and the mass ratio of the Fischer-Tropsch heavy oil to the water vapor is 1:0.2; the Fischer-Tropsch heavy oil is mixed with the second reactant stream after entering the third reactor; the reaction temperature is 460°C, the reaction pressure is 0.2MPa, the catalyst-oil ratio of the third catalyst in the third reactor to the Fischer-Tropsch heavy oil is 13, and the weight hourly space velocity is 16h -1 under the conditions of , and contacting with the third catalyst to undergo catalytic cracking and aromatization reactions to obtain a third reactant stream.

[0217] The third reaction stream carries the third catalyst after the reaction upward, and is separated by settling in a settler at an operating pressure of 0.2 MPa to obtain a reaction product and a catalyst to be produced; the reaction product is fractionated to obtain a gas phase product, a gasoline product, and a heavy oil, wherein the gas phase product is passed through an olefin separation unit to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins. Among them, 60% of the low-carbon saturated hydrocarbons are returned to the first reactor for refining.

[0218] The fuel gas and air enter the combustion furnace and are ignited to generate oxygen-containing high-temperature flue gas, which is then allowed to enter the coking tank.

[0219] The catalyst to be regenerated is steam stripped in the stripping section and then sent to the coke burning tank through the regeneration pipe to contact with the oxygen-containing high-temperature flue gas from the combustion furnace for coking; then it goes up to the regenerator to completely burn off the carbon deposits. The temperature of coking and regeneration is 700℃ and the pressure is 0.2MPa to obtain the regenerated catalyst, which is circulated back to the first reactor, the second reactor and the third reactor through the regeneration pipe I, the regeneration pipe II and the regeneration pipe III for recycling. The carbon deposit amount is calculated by measuring the carbon content in the catalyst to be regenerated.

[0220] The product distribution of this example is shown in Table 5.

[0221] Table 5 Product distribution of Examples and Comparative Examples

[0222]

[0223] The yields of gas products, gasoline, heavy oil, carbon deposits and olefins described in the above examples and comparative examples are calculated based on the total hydrocarbon content in the feed.

[0224] As can be seen from Table 5, the gas phase product of Comparative Example 1 is higher than that of Example 1, gasoline is lower than that of Example 1, heavy oil is higher than that of Example 1, and the yield and octane number of light olefins are lower than those of Example 1, wherein the octane number is only 85. This shows that it is not conducive to obtaining more target products when all raw materials enter the first reactor for reaction. The gas phase product of Comparative Example 2 is lower than that of Example 1, gasoline and heavy oil are basically equivalent to those of Example 1, and the yield of light olefins and the octane number of gasoline are lower than those of Example 1. This shows that it is not conducive to obtaining more target products when all raw materials enter the third reactor for reaction.

[0225] It can be seen from the remaining embodiments that if the reaction temperature is increased, more gas phase products can be obtained. If the reaction temperature is lowered, more liquid phase products can be obtained (the obtained gasoline and heavy oil are collectively referred to as "liquid phase products" relative to the gas phase products). For example, the reaction temperature of Example 1 is higher than that of Example 3, the gas phase product yield of Example 1 is higher than that of Example 3, and the liquid phase product of Example 1 is lower than that of Example 3, wherein the gasoline yield has increased by about 4%. If the proportion of Fischer-Tropsch heavy oil in the raw material is increased, the liquid phase product and the octane number of gasoline can be increased. If the proportion of low-carbon saturated hydrocarbons and Fischer-Tropsch light oil in the raw material is increased, more gas phase products and low-carbon olefin yields can be obtained. For example, the Fischer-Tropsch heavy oil in Example 3 accounts for 90% of the raw material, and the Fischer-Tropsch heavy oil in Example 6 only accounts for 30% of the raw material. The liquid phase product yield and gasoline octane number of Example 3 are both higher than those of Example 6, and the gas phase product yield and low-carbon olefin yield of Example 3 are lower than those of Example 6. Under different reaction conditions, the gasoline yield in each embodiment is above 34% (e.g., between 34.5-49.1%), the gasoline octane number is above 95 (e.g., between 95-99), and the olefin yield is above 39% (e.g., between 39.1-55.1%).

[0226] The embodiments of the present invention have been described in detail above. It is obvious to those skilled in the art that many modifications and changes can be made without departing from the basic spirit of the present invention. All these changes and improvements are included in the protection scope of the present invention.

Claims

1. A method for co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products, the method include: (1) feeding Fischer-Tropsch low-carbon saturated hydrocarbons and optional atomizing medium into a first reactor in an atomized form, contacting with a first catalyst and undergoing a catalytic thermal cracking reaction to obtain a first reactant stream, and feeding the first reactant stream to a second reactor; (2) feeding the Fischer-Tropsch light oil and an optional atomizing medium into a second reactor in an atomized form, mixing with the first reactant stream, contacting with a second catalyst and performing a catalytic cracking reaction to obtain a second reactant stream, and feeding the second reactant stream to a third reactor; (3) feeding the Fischer-Tropsch heavy oil and an optional atomizing medium into a third reactor in an atomized form, mixing with the second reactant stream, contacting with a third catalyst and performing catalytic cracking and aromatization reactions to obtain a third reactant stream; (4) subjecting the third reaction stream obtained in step (3) to sedimentation separation to remove the spent catalyst from the third reaction stream; subjecting the obtained reaction products to fractionation to obtain gas phase products, gasoline products, and heavy oil, wherein the gas phase products are subjected to olefin separation to obtain dry gas, low-carbon saturated hydrocarbons, and low-carbon olefins; subjecting the spent catalyst to stripping, optionally charring, and regenerating to obtain a regenerated catalyst, wherein the regenerated catalyst is returned to the first reactor, the second reactor, and the third reactor for recycling.

2. The method according to claim 1, in, The method further comprises returning the low-carbon saturated hydrocarbons obtained in step (4) to the first reactor for recycling.

3. The method according to claim 1, in, The mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil and the Fischer-Tropsch heavy oil is (5-30):(5-40):(30-90).

4. The method according to any one of claims 1 to 3, in, In step (1), step (2) or step (3), the atomizing medium is selected from methanol, ethanol, propanol, dry gas, nitrogen or water vapor, or a mixture thereof.

5. The method according to claim 4, in, The dry gas includes one or more of hydrogen, methane and ethane.

6. The method according to claim 4, in, The dry gas is hydrogen, methane and ethane in the Fischer-Tropsch product.

7. The method according to any one of claims 1 to 3, in, In step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0-1).

8. The method according to claim 7, in, In step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0.1-1).

9. The method according to claim 7, in, In step (1), step (2) or step (3), the mass ratio of the Fischer-Tropsch low-carbon saturated hydrocarbons, the Fischer-Tropsch light oil or the Fischer-Tropsch heavy oil to the atomizing medium is 1:0, 1:0.1, 1:0.15, 1:0.18, 1:0.2, 1:0.25, 1:0.3, 1:0.35, 1:0.4, 1:0.45, 1:0.5, 1:0.55, 1:0.6, 1:0.65, 1:0.7, 1:0.75, 1:0.8, 1:0.85, 1:0.9, 1:0.95 or 1:

1.

10. The method according to any one of claims 1 to 3, in, In step (1), the weight ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon to the atomizing medium is 1:(0-0.6); Or wherein, in step (2), the weight ratio of the Fischer-Tropsch light oil to the atomizing medium is 1:(0-0.8); or wherein, in step (3), the weight ratio of the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0-0.8).

11. The method according to claim 10, in, In step (1), the weight ratio of the Fischer-Tropsch low-carbon saturated hydrocarbon to the atomizing medium is 1:(0.15-0.6); Or wherein, in step (2), the weight ratio of the Fischer-Tropsch light oil to the atomizing medium is 1:(0.15-0.5); or wherein, in step (3), the weight ratio of the Fischer-Tropsch heavy oil to the atomizing medium is 1:(0.15-0.5).

12. The method according to any one of claims 1 to 3, in, In step (1), step (2) or step (3), the Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil is preheated before atomization.

13. The method according to claim 12, in, The Fischer-Tropsch low-carbon saturated hydrocarbons, Fischer-Tropsch light oil or Fischer-Tropsch heavy oil is preheated to 100°C-400°C.

14. The method according to claim 13, in, The Fischer-Tropsch low-carbon saturated hydrocarbons are preheated to 100°C-350°C; or, wherein, the Fischer-Tropsch light oil is preheated to 100°C-350°C; or, wherein, the Fischer-Tropsch heavy oil is preheated to 100°C-350°C.

15. The method according to any one of claims 1 to 3, in, The active component of the first catalyst, the second catalyst and the third catalyst is at least one of the following: unmodified or modified eight-membered ring molecular sieve, ten-membered ring molecular sieve or twelve-membered ring molecular sieve, or metal oxide.

16. The method of claim 15, in, The eight-membered ring molecular sieve, the ten-membered ring molecular sieve or the twelve-membered ring molecular sieve is selected from SAPO-34, SAPO-18, ITQ-13, IM-5, ZSM-5, ZSM-11, MCM-22, EU-1, beta, and mordenite molecular sieves; or, the metal oxide is one or more of zinc oxide, lanthanum oxide, magnesium oxide, manganese oxide, cerium oxide, gallium oxide, chromium oxide, nickel oxide, and tungsten oxide.

17. The method of claim 15, in, The active components of the first catalyst, the second catalyst and the third catalyst account for 20 wt% to 60 wt% of the weight of the catalyst on a dry basis.

18. The method of claim 17, in, In addition to the active components, the first catalyst, the second catalyst and the third catalyst also contain a residual amount of aluminum oxide and / or silicon oxide as a carrier.

19. The method according to any one of claims 1 to 3, in, The first catalyst is a mixed catalyst of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the first catalyst is 0wt%-2.00wt%; or, the second catalyst is a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the second catalyst is 0wt%-2.0wt%; or, the third catalyst is a mixture of a regenerated catalyst and a catalyst to be regenerated, wherein the carbon content of the third catalyst is 0wt%-2.0wt%.

20. The method according to any one of claims 1 to 3, in, In step (1), the reaction conditions of the first reactor are: temperature 500°C-750°C; pressure 0.01-0.7 MPa; weight hourly space velocity 10-300 h -1 ; Agent-oil ratio 0.5-50.

21. The method of claim 20, in, The temperature is 580°C-680°C; or the pressure is 0.1-0.5MPa; or the weight hourly space velocity is 40-200h -1 ; Alternatively, the agent-oil ratio is 5-30.

22. The method according to any one of claims 1 to 3, in, In step (2), the reaction conditions of the second reactor are: temperature 450°C-700°C; pressure 0.01-0.7 MPa; weight hourly space velocity 1-150h -1 ; Agent-oil ratio 1-40.

23. The method of claim 22, in, The temperature is 530°C-630°C; or, the pressure is 0.1-0.5MPa; or, the weight hourly space velocity is 40-120h -1 ; Alternatively, the agent-oil ratio is 5-25.

24. The method according to any one of claims 1 to 3, in, In step (3), the reaction conditions of the third reactor are: temperature 400°C-650°C; pressure 0.01-0.7 MPa; weight hourly space velocity 0.5-30h -1 ; Agent-oil ratio 1-20.

25. The method of claim 24, in, The temperature is 480°C-580°C; or, the pressure is 0.1-0.5MPa; or, the weight hourly space velocity is 2-20h -1 ; Alternatively, the agent-oil ratio is 2-15.

26. The method according to any one of claims 1 to 3, in, The first reactor is a transport bed reactor, a fast bed reactor or a turbulent bed reactor; or, the second reactor is a fast bed reactor, a turbulent bed reactor or a bubbling bed reactor; Alternatively, the third reactor is a turbulent bed reactor, a bubbling bed reactor or a dispersed fluidized bed reactor.

27. The method of claim 26, in, The first reactor is a transport bed reactor or a fast bed reactor; or, the second reactor is a fast bed reactor or a turbulent bed reactor; or, the third reactor is a bubbling bed reactor or a turbulent bed reactor.

28. The method according to any one of claims 1 to 3, in, In step (4), the operating pressure of the sedimentation separation is 0.01-0.7 MPa.

29. The method of claim 2, in, 10%-90% of the low-carbon saturated hydrocarbons obtained in step (4) are returned to the first reactor for recycling.

30. The method according to any one of claims 1 to 3, in, In step (4), the spent catalyst is contacted with an oxygen-containing gas to be optionally burned and regenerated under the following conditions: a pressure of 0.01-0.7 MPa; a temperature of 550°C-750°C.

31. The method of claim 30, in, The oxygen-containing gas is air or oxygen-containing high-temperature flue gas.

32. A device suitable for the method of co-producing light olefins and high-octane gasoline from Fischer-Tropsch synthesis products according to any one of claims 1 to 31, the device comprising a reaction system, a regeneration system and a product separation system, in, The reaction system comprises: The first reactor; a second reactor, the second reactor being arranged in series with the first reactor; a third reactor, wherein the third reactor is arranged in series with the second reactor; a settling unit connected in fluid communication with the third reactor and the product separation system; Wherein, the regeneration system comprises: a stripping section fluidly connected to the settling unit; a regenerator connected in fluid communication to the stripping section and the first, second and third reactors, Wherein, the product separation system comprises: a fractionation unit connected in fluid communication with the sedimentation unit; An olefin separation unit is fluidly connected to the fractionation unit.

33. The device of claim 32, in, The regeneration system further comprises: A char drum is fluidly connected to the stripping section and the regenerator.

34. The device of claim 33, in, The regeneration system is further provided with a combustion furnace, which is connected to the coke burning drum in a fluid communication manner to provide high-temperature flue gas containing oxygen to the coke burning drum.

35. The device according to any one of claims 32 to 34, in, The first reactor, the second reactor and the third reactor share a settler.

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