Method and apparatus for desulfurizing and separating light products of catalytic cracking

Abstract

A method and apparatus for desulfurizing and separating catalytic cracking light products. The method includes the following steps: 1) contacting the catalytic cracking light products with a desulfurizing adsorbent in an adsorptive desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally subjecting the desulfurized products to gas-liquid separation to obtain a desulfurized rich gas and a desulfurized crude gasoline. The catalytic cracking light products are overhead oil gas from a catalytic cracking fractionation tower or a rich gas and a crude gasoline from a catalytic cracking fractionation tower; and 2) separately sending the desulfurized rich gas and the desulfurized crude gasoline obtained in step 1) to a catalytic cracking absorption stabilization system for separation to obtain a desulfurized dry gas, a desulfurized liquefied gas, and a desulfurized stabilized gasoline. The method and apparatus are suitable for use in treating the catalytic cracking light products obtained from the catalytic cracking fractionation tower, and can produce a high yield of refined gasoline and a low octane loss.

Description

Detailed Description of the Invention

[0001] [Cross - References to Related Applications] This application claims priority from Chinese Patent Application No. 201911049476.3, filed on October 31, 2019, "Method and Apparatus for Desulfurization and Separation of Catalytic Cracking Light Products", Chinese Patent Application No. 201911049636.4, filed on October 31, 2019, "Desulfurization and Separation Method of Catalytic Cracking Light Products", Chinese Patent Application No. 201911049459.X, filed on October 31, 2019, "Method and Apparatus for Desulfurization and Separation of Catalytic Cracking Light Products", Chinese Patent Application No. 201911049466.X, filed on October 31, 2019, "Desulfurization and Separation Method and Apparatus of Catalytic Cracking Light Products", Chinese Patent Application No. 201911049630.7, filed on October 31, 2019, "Desulfurization Method and Desulfurization Apparatus of Catalytic Cracking Light Products", and Chinese Patent Application No. 201911049610.X, filed on October 31, 2019, "Desulfurization Method of Catalytic Cracking Light Oil Products, Method and Apparatus for Producing Low - Sulfur Light Oil Products by Catalytic Cracking". The entire contents of these are incorporated herein by reference.

[0002] [Technical Field] This application relates to the field of petrochemical industry, and particularly to a method for desulfurizing hydrocarbon oils, and more specifically to a method and apparatus for desulfurizing and separating catalytic cracking light products.

[0003] [Background Art] The catalytic cracking unit of an oil refinery is a major source of light olefins, liquefied gas, and gasoline. In the existing catalytic cracking process, the reaction products from the catalytic cracking unit are fractionated to obtain components such as rich gas, crude gasoline, light cycle oil, heavy gas oil, slurry oil, etc. The rich gas is passed through an absorption-desorption tower and a reabsorption tower to obtain a dry gas product, which can be used as a purified fuel gas after desulfurization. The crude gasoline can be separated in an absorption stabilization tower to obtain liquefied gas and stabilized catalytic cracking gasoline. The catalytic cracking gasoline is produced as a product after desulfurization, and the liquefied gas can be produced as a product after desulfurization, or can be used as a starting material for providing high-value components such as propylene and butylene for other devices.

[0004] All of the dry gas, liquefied gas, and catalytic cracking gasoline must be desulfurized under increasingly strict environmental regulations and downstream process requirements. Currently, the desulfurization processes for dry gas, liquefied gas, and catalytic cracking gasoline are carried out separately due to the limitations of desulfurization technologies. In processes such as alkali washing desulfurization commonly used for dry gas and liquefied gas, a large amount of waste liquid, waste residues, etc. are generated. Also, in the existing liquefied gas desulfurization process, there is a problem that the sulfur content becomes excessively high due to insufficient desulfurization degree, resulting in limited applications.

[0005] The adsorption desulfurization method of hydrocarbon oil is a method for desulfurizing light hydrocarbon oil by adsorption in the presence of hydrogen, which has characteristics such as high desulfurization degree and low hydrogen consumption, and can be used to produce fuel oil with a sulfur content of less than 30 μg / g. However, when used to process catalytic cracking light products, this method has problems such as low liquid yield of catalytic cracking products and large octane number loss of gasoline.

[0006] [Summary of the Invention] In view of the problems of the prior art, the object of the present application is to provide a method and apparatus for desulfurization and separation of catalytic cracking light products that can be used to produce desulfurized dry gas, liquefied gas, and stabilized catalytic cracking gasoline in high yields and qualities.

[0007] To achieve the above object, in this aspect, the present application provides a method for desulfurization and separation of catalytic cracking light products, comprising: 1) contacting the catalytic cracking light products with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally performing gas-liquid separation on the obtained desulfurized products to obtain a desulfurized rich gas and desulfurized crude gasoline, wherein the catalytic cracking light products are a top oil-gas fraction from a catalytic cracking fractionation tower, or a rich gas and crude gasoline from a catalytic cracking fractionation tower; 2) separately sending the desulfurized rich gas and desulfurized crude gasoline obtained in step 1) to a catalytic cracking absorption stabilization system for separation to obtain a desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline. A method including the above steps is provided.

[0008] Preferably, the catalytic cracking absorption stabilization system includes an absorption tower, a reabsorption tower, a stripping tower, and a stabilization tower, and step 2) includes: 2a) introducing the desulfurized rich gas into the absorption tower from the bottom, and contacting it with the desulfurized crude gasoline introduced into the absorption tower from the top in a countercurrent manner for mass transfer to obtain a top stream and a bottom product; 2b) introducing the top stream of the absorption tower into the reabsorption tower from the bottom, and contacting it with the light cycle oil from the catalytic cracking fractionation tower introduced into the reabsorption tower from the top in a countercurrent manner for mass transfer to obtain the desulfurized dry gas at the top of the reabsorption tower and concentrated light cycle oil at the bottom of the reabsorption tower, and optionally recycling the concentrated light cycle oil to the catalytic cracking fractionation tower; 2c) stripping the bottom product of the absorption tower in the stripping tower to obtain a top gas and a bottom product, and optionally recycling the top gas to the absorption tower; 2d) sending the bottom product of the stripping tower to the stabilization tower, and fractionating it in the stabilization tower to obtain the desulfurized liquefied gas and the desulfurized stabilized gasoline. The method further includes the above steps.

[0009] In another aspect, the present application is a method for producing a low-sulfur light oil product by catalytic cracking, comprising: i) contacting a catalytic cracking feedstock with a catalytic cracking catalyst for a reaction under catalytic cracking conditions; ii) performing gas-solid separation on the reaction product obtained in step i) to obtain a reaction oil gas and a spent catalyst; iii) fractionating the reaction oil gas obtained in step ii) in a catalytic cracking fractionation column to obtain a catalytic cracking light product, a light cycle oil, a diesel oil, and an oil slurry; iv) desulfurizing and separating the catalytic cracking light product from the catalytic cracking fractionation column using the desulfurization and separation method for the catalytic cracking light product according to the present application to obtain a desulfurized dry gas, a desulfurized liquefied gas, and a desulfurized stabilized gasoline; v) optionally, regenerating the spent catalyst obtained in step ii) and recycling the regenerated catalyst to a riser reactor for reuse. A method is provided that includes the above steps.

[0010] In another aspect, the present application is an apparatus for desulfurizing and separating a catalytic cracking light product, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series. The absorption stabilization unit includes an absorption column, a stripping column, a reabsorption column, and a stabilization column connected in series. The adsorption desulfurization unit includes a fluidized bed desulfurization reaction unit, an adsorbent regenerator, and a lock hopper connected between the fluidized bed desulfurization reaction unit and the adsorbent regenerator for performing pressure change and atmosphere conversion. The fluidized bed desulfurization reaction unit communicates with the catalytic cracking fractionation column to receive the catalytic cracking light product from the catalytic cracking fractionation column. An apparatus is provided, wherein an oil-gas discharge port of the fluidized bed desulfurization reaction unit communicates with the absorption column of the absorption stabilization unit, or communicates with the absorption column of the absorption stabilization unit via a gas-liquid separation tank.

[0011] Compared with the prior art, the method and apparatus for desulfurization and separation of the catalytic cracking light products according to the present application have one or more of the following advantages.

[0012] 1) The top-oil gas fraction from the catalytic cracking fractionation column or the catalytic cracking light products such as rich gas and crude gasoline from the catalytic cracking fractionation column are first subjected to adsorption desulfurization and then to absorption stabilization, as a result of which the loss of gasoline yield encountered in the conventional method can be minimized.

[0013] 2) The rich gas and crude gasoline from the catalytic cracking fractionation column are subjected to adsorption desulfurization, and the loss of light olefins in the rich gas is low. In the adsorption desulfurization reactor, hydrogen in the rich gas serves as a source of hydrogen involved in the reaction, and hydrogen consumption can be saved. After adsorption desulfurization, the rich gas and crude gasoline are passed through an absorption stabilization system to obtain desulfurized dry gas, liquefied gas and stabilized gasoline, and their sulfur content can be 10 ppm or less, and even 1 ppm or less.

[0014] 3) The equipment for desulfurizing dry gas, liquefied gas, etc. required in a conventional refinery is eliminated, and problems such as waste liquid and waste residues that the conventional desulfurization process may encounter are avoided.

[0015] 4) When two desulfurization reactors are respectively used to process crude gasoline and rich gas, the two desulfurization reactors can be operated relatively independently, and the olefin saturation rate during the desulfurization of rich gas is reduced.

[0016] 5) In a preferred embodiment, the crude gasoline and the desulfurization adsorbent flow upward simultaneously in the first fluidized bed desulfurization reactor, as a result of which a long reaction time can be obtained to ensure complete removal of sulfides such as thiophene that are difficult to remove. The rich gas is brought into contact with the desulfurization adsorbent in a countercurrent manner in the second fluidized bed desulfurization reactor for adsorption desulfurization, as a result of which the contact time between the olefins in the rich gas and the adsorbent can be reduced, and the saturation rate of light olefins is reduced.

[0017] [Brief Description of the Drawings] The drawings forming a part of this specification are provided to assist in the understanding of the present application and should not be considered limiting. The present application can be interpreted with reference to the drawings in combination with the following detailed description.

[0018] FIG. 1A is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit which is a first type of embodiment of the present application.

[0019] FIG. 1B is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a second type of embodiment of the present application.

[0020] FIG. 1C is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a third type of embodiment of the present application.

[0021] FIG. 1D is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a fourth type of embodiment of the present application.

[0022] FIG. 1Ea is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a fifth type of embodiment of the present application.

[0023] FIG. 1Eb is a schematic diagram of another preferred embodiment of an adsorption desulfurization unit according to a fifth type of embodiment of the present application.

[0024] FIG. 1F is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a sixth type of embodiment of the present application.

[0025] FIG. 2 is a schematic diagram of a preferred embodiment of an absorption stabilization unit according to the present application.

[0026] [Detailed Description of the Invention] Hereinafter, the present application will be described in more detail with reference to specific embodiments and the accompanying drawings. It should be noted that the specific embodiments of the present application are provided for illustrative purposes only and are not intended to limit in any way.

[0027] In the context of this application, any specific numerical value including the endpoints of a numerical range described herein should not be limited to its exact value, but should be further construed to include all values close to the exact value, for example, all values within ±5% of the exact value. Further, with respect to any numerical range described herein, any combination can be made between the endpoints of the range, between each endpoint and any specific value within the range, or between any two specific values within the range to provide one or more new numerical ranges, in which case the new numerical ranges should also be regarded as specifically described in this application.

[0028] Unless otherwise specified, the terms used herein have the same meaning as commonly understood by those skilled in the art. When the terms are defined herein and their definitions are different from the ordinary understanding in the technical field, the definitions provided herein shall prevail.

[0029] In this application, the term "rich gas" refers to the gas distillate obtained from the catalytic cracking fractionation column, mainly containing C1-C4 hydrocarbon components, as well as a small amount of C5 hydrocarbon components and a very small amount of C6 components, and may also contain other components such as nitrogen, carbon dioxide, carbon monoxide, hydrogen, and hydrogen sulfide. Its sulfur content is 30-50000 μg / g, for example, 50 μg / g or more.

[0030] In this application, "crude gasoline" refers to the distillate from the catalytic cracking fractionation column having a distillation range of 30-210°C, mainly containing C4-C12 hydrocarbon components. Its sulfur content is 30-50000 μg / g, for example, 50 μg / g or more.

[0031] In the present application, the "top oil-gas distillate" refers to the distillate obtained from the top of a catalytic cracking fractionation column having a distillation range covering both rich gas and crude gasoline, mainly containing C1 to C12 hydrocarbon components, and may also contain other components such as nitrogen, carbon dioxide, carbon monoxide, hydrogen, and hydrogen sulfide. Its sulfur content is 30 to 50000 μg / g, for example, 50 μg / g or more.

[0032] According to the present application, the "bottom" of a reactor or vessel refers to the portion of the reactor or vessel from 0% to 10% of the height from the bottom to the top. The "lower part" of a reactor or vessel refers to the portion of the reactor or vessel from 0% to 50% of the height from the bottom to the top. The "upper part" of a reactor or vessel refers to the portion of the reactor or vessel from 50% to 100% of the height from the bottom to the top of the reactor or vessel. The "top" of a reactor or vessel refers to the portion of the reactor or vessel from 90% to 100% of the height from the bottom to the top of the reactor or vessel.

[0033] In the context of the present application, in addition to the explicitly described subject matter, the subject matter not described is considered to be the same as that known in the art without any modification. Furthermore, any of the embodiments described in this specification can be freely combined with one or more of the other embodiments described in this specification, and the technical solutions or concepts obtained in this way are considered to be part of the original disclosure or original description of the present application, and should not be considered as new matters not disclosed or anticipated in this specification unless it is obvious to those skilled in the art that such a combination is clearly unreasonable.

[0034] All patent documents and non-patent documents (including but not limited to textbooks and journal articles) cited in this specification are incorporated herein by reference in their entirety.

[0035] As described above, in a first aspect, the present application is a method for desulfurization and separation of catalytic cracking light products, 1) Contact the catalytic cracking light products with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally perform gas-liquid separation on the obtained desulfurized products to obtain desulfurized rich gas and desulfurized crude gasoline, wherein the catalytic cracking light products are the top oil-gas fraction from the catalytic cracking fractionation tower, or the rich gas and crude gasoline from the catalytic cracking fractionation tower. 2) Send the desulfurized rich gas and desulfurized crude gasoline obtained in step 1) separately to a catalytic cracking absorption stabilization system for separation to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline. Provide a method comprising the above steps.

[0036] Preferably, the catalytic cracking absorption stabilization system comprises an absorption tower, a reabsorption tower, a stripping tower, and a stabilization tower, and step 2) comprises: 2a) Introduce the desulfurized rich gas into the absorption tower from the bottom and contact it with the desulfurized crude gasoline introduced into the absorption tower from the top in a countercurrent manner for mass transfer to obtain a top stream and a bottom product. 2b) Introduce the top stream of the absorption tower into the reabsorption tower from the bottom and contact it with the light cycle oil from the catalytic cracking fractionation tower introduced into the reabsorption tower from the top in a countercurrent manner for mass transfer to obtain the desulfurized dry gas at the top of the reabsorption tower and concentrated light cycle oil at the bottom of the reabsorption tower. Optionally, recycle the concentrated light cycle oil to the catalytic cracking fractionation tower. 2c) Strip the bottom product of the absorption tower in the stripping tower to obtain a top gas and a bottom product. Optionally, recycle the top gas to the absorption tower. 2d) Send the bottom product of the stripping tower to the stabilization tower, fractionate it in the stabilization tower to obtain the desulfurized liquefied gas and the desulfurized stabilized gasoline. Further include the above steps.

[0037] More preferably, the operating conditions of the absorption column include a pressure of 0.2 to 3.0 MPa (preferably 0.5 to 1.6 MPa) and a temperature of 20 to 100 °C (preferably 30 to 70 °C); the operating conditions of the desorption column include a pressure of 0.1 to 3.0 MPa (preferably 0.5 to 2.5 MPa) and a temperature of 20 to 250 °C (preferably 50 to 200 °C); the operating conditions of the re-absorption column preferably include a pressure of 0.1 to 3.0 MPa (preferably 0.5 to 2.5 MPa) and a temperature of 20 to 100 °C (preferably 30 to 70 °C); the operating conditions of the stabilization column preferably include a pressure of 0.1 to 3.0 MPa (preferably 0.5 to 2.5 MPa) and a temperature of 20 to 250 °C (preferably 50 to 200 °C).

[0038] 〔First type of embodiment〕 According to the first type of embodiment of the method according to the present application, the catalytic cracking light product is the top oil-gas fraction from the catalytic cracking fractionation column, and step 1) further includes the following steps: 1a) Introducing the top oil-gas fraction from the catalytic cracking fractionation column into a fluidized bed desulfurization reactor from the bottom, and bringing it into contact with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) Performing gas-solid separation on the reaction stream obtained at the upper part of the fluidized bed desulfurization reactor to obtain a reaction oil gas and a sulfur-filled adsorbent; 1c) Performing gas-liquid separation on the reaction oil gas obtained in step 1b) to obtain the desulfurized rich gas and desulfurized crude gasoline; and, 1d) Sending the sulfur-filled adsorbent obtained in step 1b) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the fluidized bed desulfurization reactor after reduction.

[0039] In some preferred embodiments, the overhead oil-gas fraction from the catalytic cracking fractionation column is introduced into an adsorption desulfurization reaction unit, contacted with a desulfurization adsorbent in the presence of hydrogen for desulfurization, and a reaction oil gas is obtained. The reaction oil gas is passed through a gas-liquid separation tank for separation, and a desulfurized rich gas and a desulfurized crude gasoline are obtained. The desulfurized rich gas is introduced from the bottom into an absorption column and contacted with the crude gasoline introduced from the top into the absorption column for mass transfer. The overhead stream of the absorption column is introduced from the bottom into a reabsorption column and contacted with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer, and a desulfurized dry gas is obtained from the top of the reabsorption column. The concentrated light cycle oil obtained at the bottom of the reabsorption column is recycled to the catalytic cracking fractionation column. The bottom product of the absorption column is sent to a stabilization column after passing through a desorption column, fractionated in the stabilization column, and a desulfurized liquefied gas and a desulfurized stabilized gasoline are obtained. The overhead gas of the desorption column is recycled to the absorption column.

[0040] In a further preferred embodiment, after preheating the overhead oil-gas fraction of the catalytic cracking fractionation column to the required temperature, the overhead oil-gas fraction is introduced from the bottom into a fluidized bed desulfurization reactor and contacted with a desulfurization adsorbent in the reactor for desulfurization while flowing from the bottom to the top. The reacted spent adsorbent, which is a high sulfur charge, is separated from the oil gas and then introduced into a fluidized bed regenerator for regeneration by contacting with oxygen. The regenerated adsorbent is recycled to the desulfurization reactor for reuse after reduction. The mixture, which is the desulfurization product, is passed through a gas-liquid separator to obtain a desulfurized rich gas and a desulfurized crude gasoline. A part of the desulfurized rich gas and the desulfurized crude gasoline and / or the stabilized gasoline is passed through an absorption column, and the overhead gas product of the absorption column is absorbed using the light cycle oil from the catalytic cracking fractionation column and separated in a reabsorption column. A desulfurized dry gas is obtained at the top of the reabsorption column. Concentrated light cycle oil is obtained at the bottom of the reabsorption column, and the concentrated light cycle oil is recycled to the catalytic cracking fractionation column. The bottom product of the absorption column is sent to a stabilization column after passing through a desorption column, fractionated in the stabilization column, and a desulfurized liquefied gas and a desulfurized stabilized catalytic cracking gasoline are obtained. The overhead gas of the desorption column is mixed with the desulfurized rich gas and then sent to the absorption column.

[0041] In a further preferred embodiment, the overhead oil-gas fraction of the catalytic cracking fractionation column is heated to 100 to 500 °C. The heated overhead oil-gas fraction of the catalytic cracking fractionation column is used as the hydrocarbon oil feedstock of the fluidized bed desulfurization reactor. The hydrocarbon oil feedstock, or a mixture of the hydrocarbon oil feedstock and a hydrogen donor, is introduced into the fluidized bed reactor from the bottom. The sulfur-containing hydrocarbon oil feedstock is subjected to a reaction with a desulfurization adsorbent for adsorptive desulfurization under reaction conditions including a temperature of 200 to 550 °C (preferably 300 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), a weight hourly space velocity of 0.1 to 100 h -1 (preferably 1 to 10 h -1 ), and a volume ratio of the hydrogen donor to the gasoline feedstock of 0.01 to 1000 (preferably 0.05 to 500).

[0042] Preferably, the mixture of the hydrocarbon oil feedstock and the hydrogen donor is uniformly distributed into the reactor through a feed distribution plate and sufficiently contacts the desulfurization adsorbent in the reactor. The desulfurization adsorbent is introduced from the bottom of the fluidized bed desulfurization reactor.

[0043] Preferably, a gas-solid separator is provided in the sedimentation separation section at the top of the fluidized bed desulfurization reactor. The reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation. The separated sulfur-loaded used adsorbent (also referred to as "sulfur-loaded catalyst") is stripped to remove the adsorbed hydrocarbons and then sent to an adsorbent regenerator. The regenerated desulfurization adsorbent is sent to an adsorbent reducer for reduction, and the reduced desulfurization adsorbent is introduced from the bottom of the fluidized bed desulfurization reactor to realize a continuous cycle of adsorptive desulfurization reaction, adsorbent regeneration, adsorbent reduction, and adsorptive desulfurization reaction.

[0044] The hydrocarbon oil product obtained after the reaction is sent to a gas-liquid separation tank after heat exchange to obtain desulfurized rich gas and desulfurized crude gasoline. The operating pressure of the gas-liquid separation tank is 0.2 to 4.0 MPa (preferably 0.5 to 3.0 MPa), and the operating temperature is 20 to 300 °C (preferably 50 to 200 °C).

[0045] FIG. 1A is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a first type of embodiment of the present application. As shown in FIG. 1A, the adsorption desulfurization unit includes a fluidized bed desulfurization reactor 102, a receiver 106 of the reactor, a lock hopper 108 for isolating the reaction-regeneration system, a regenerator feed tank 111, an adsorbent regenerator 114, and a receiver 117 of the regenerator, which are in communication in sequence. The receiver 117 of the regenerator communicates with an adsorbent reducer 120 via a lock hopper 108 and a pipeline 119, and the adsorbent reducer 120 communicates with the bottom of the fluidized bed desulfurization reactor 102.

[0046] The preheated top oil-gas fraction and hydrogen gas from the catalytic cracking fractionation tower are introduced into the bottom of the fluidized bed desulfurization reactor 102 via a pipeline 101 and brought into contact with the desulfurization adsorbent in the fluidized bed desulfurization reactor 102 for the adsorption desulfurization reaction. The adsorbent partially filled with sulfur moves upward together with the reaction materials. After the reaction, the reaction oil gas and the adsorbent are passed through a sedimentation separation section at the top of the reactor 102 for oil-adsorbent separation. The obtained reaction oil gas is a mixture of desulfurized rich gas, desulfurized crude gasoline, and hydrogen, which is sent to a gas-liquid separation tank (not shown) via a pipeline 104. The desulfurized rich gas and the desulfurized crude gasoline are obtained by condensation gas-liquid separation and sent to the next product separation and stabilization system for processing.

[0047] The used adsorbent is transferred from the upper part of the fluidized bed desulfurization reactor 102 to the receiver 106 of the reactor through the adsorbent transfer horizontal pipe 105. After stripping in the receiver 106 of the reactor, it is sent to the lock hopper 108 through the pipeline 107. After being purged with nitrogen, the high-pressure hydrogen environment in the lock hopper is changed to a low-pressure inert atmosphere. The purge gas is sent to the combustion furnace through the pipeline 109 for combustion. The used adsorbent is sent to the regenerator supply tank 111 through the pipeline 110, lifted by the lift gas, and sent to the adsorbent regenerator 114 through the pipeline 112. An oxygen-containing gas is introduced into the adsorbent regenerator from the bottom through the pipeline 113. The used adsorbent is brought into contact with the oxygen-containing gas in the adsorbent regenerator 114 for sulfur combustion and carbon combustion to obtain the regenerated adsorbent. The sulfur-containing exhaust gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and sent to the sulfur production system, or is subjected to alkali washing through the pipeline 115 to remove SOx. The regenerated adsorbent is sent from the adsorbent regenerator to the receiver 117 of the regenerator through the pipeline 116, lifted by nitrogen, sent to the lock hopper 108 through the pipeline 118, stripped and purged with hydrogen. Then, the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 108 and introduced into the reducer 120 for reduction through the pipeline 119. The reduced and regenerated adsorbent is introduced into the fluidized bed desulfurization reactor 102 through the pipeline 121, and as a result, a continuous adsorptive desulfurization reaction is realized.

[0048] 〔Second Type of Embodiment〕 According to the second type of embodiment of the method according to the present application, the catalytic cracking light products are the rich gas and the crude gasoline from the catalytic cracking fractionation tower, and step 1) further includes the following steps: 1a) A step of introducing the crude gasoline from the catalytic cracking fractionation tower into the fluidized bed desulfurization reactor from the bottom and bringing it into contact with the desulfurization adsorbent introduced into the reactor from the bottom in the presence of hydrogen for a desulfurization reaction; 1b) Introducing the rich gas from the catalytic cracking fractionation column into the fluidized bed desulfurization reactor at a position of 30% to 80%, preferably 40% to 70% of the height from the bottom to the top, and mixing it with the flow in the reactor for the desulfurization reaction; 1c) Performing gas-solid separation on the reaction stream obtained at the upper part of the fluidized bed desulfurization reactor to obtain the reaction oil gas and the sulfur-loaded adsorbent; 1d) A process of performing gas-liquid separation on the reaction oil gas obtained in step 1c) to obtain the desulfurized rich gas and the desulfurized crude gasoline, preferably, the operating conditions of the gas-liquid separation include a pressure of 0.2 to 4.0 MPa, preferably 0.5 to 3.0 MPa, and a temperature of 20 to 300 °C, preferably 50 to 200 °C; and 1e) Feeding the sulfur-loaded adsorbent obtained in step 1c) to the adsorbent regenerator for regeneration by calcining in the presence of an oxygen-containing gas, and recycling the regenerated desulfurized adsorbent to the fluidized bed desulfurization reactor after reduction, Preferably, the sulfur contents in the rich gas and the crude gasoline from the catalytic cracking fractionation column are each independently greater than 30 μg / g, particularly greater than 50 μg / g.

[0049] In some preferred embodiments, the crude gasoline from the catalytic cracking fractionation column is introduced from the bottom into a fluidized bed desulfurization reactor and brought into contact with a desulfurization adsorbent in the presence of hydrogen while flowing upward. The rich gas from the catalytic cracking fractionation column is introduced into the fluidized bed desulfurization reactor at a position 30 - 80% of the height from the bottom to the top, mixed with the reaction stream, then brought into contact with the desulfurization adsorbent for the reaction, and the reaction oil gas obtained by gas-solid separation at the top of the reactor is introduced into a gas-liquid separation tank for separation to obtain desulfurized rich gas and desulfurized crude gasoline. The sulfur-loaded adsorbent is calcined and regenerated in an adsorbent regenerator. The regenerated desulfurization adsorbent is recycled to the fluidized bed desulfurization reactor for reuse after reduction. The desulfurized rich gas is introduced from the bottom into an absorption column and brought into contact with the desulfurized crude gasoline introduced into the absorption column from the top for mass transfer. The top stream of the absorption column is introduced from the bottom into a reabsorption column and brought into contact with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer. The desulfurized dry gas is obtained at the top of the reabsorption column, the concentrated light cycle oil obtained at the bottom of the reabsorption column is recycled to the catalytic cracking fractionation column, the bottom product of the absorption column is sent to a stabilization column after passing through a stripping column, fractionated in the stabilization column to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and the top gas of the stripping column is recycled to the absorption column.

[0050] In a further preferred embodiment, the crude gasoline from the catalytic cracking fractionation column is preheated to the required temperature and introduced into the fluidized bed desulfurization reactor from the bottom. During the flow from the bottom to the top, it is brought into contact with the desulfurization adsorbent in the reactor for desulfurization. The rich gas is introduced into the fluidized bed desulfurization reactor from the upper central part, mixed with the reaction flow, brought into contact with the desulfurization adsorbent for the reaction, and subjected to gas-solid separation at the top of the fluidized bed desulfurization reactor. The separated used adsorbent with high sulfur filling is introduced into the adsorbent regenerator to be regenerated by contacting with oxygen, and the regenerated adsorbent is recycled to the desulfurization reactor for reuse after reduction. The reaction oil gas obtained by gas-solid separation is passed through a gas-liquid separator to obtain desulfurized rich gas and desulfurized crude gasoline. The desulfurized rich gas is introduced into the absorption column from the bottom and brought into contact with the desulfurized crude gasoline introduced into the absorption column from the top for mass transfer. The top gas product of the absorption column is absorbed using the light cycle oil from the catalytic cracking fractionation column, separated in the reabsorption column, and desulfurized dry gas is obtained at the top of the reabsorption column. Concentrated light cycle oil is obtained at the bottom of the reabsorption column. The concentrated light cycle oil is recycled to the catalytic cracking fractionation column. The bottom product of the absorption column is sent to the stabilization column after passing through the stripping column, fractionated in the stabilization column, and desulfurized liquefied gas and desulfurized stabilized catalytic cracking gasoline are obtained. The top gas of the stripping column is mixed with the desulfurized rich gas and then sent to the absorption column.

[0051] In a further preferred embodiment, the crude gasoline from the catalytic cracking fractionation column is heated to 100 - 500 °C and introduced into the fluidized bed adsorption desulfurization reactor from the bottom together with a hydrogen donor. The rich gas from the catalytic cracking fractionation column is preheated to a temperature of 150 - 450 °C and introduced at a position 30 - 80% of the height from the bottom to the top of the fluidized bed desulfurization reactor.

[0052] The fluidized bed desulfurization reactor is preferably a dense phase bed reactor. The height of the adsorbent bed layer through which the rich gas passes is controlled to be 10 - 60% of the total height of the adsorbent bed layer in the fluidized bed desulfurization reactor.

[0053] The operating conditions of the fluidized bed desulfurization reactor are preferably a temperature of 200 to 550 °C (preferably 300 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), a weight hourly space velocity of 0.1 to 100 h -1 (preferably 1 to 10 h -1 ), and a volume ratio of the hydrogen donor to the gasoline feedstock of 0.01 to 1000 (preferably 0.05 to 500). In the presence of hydrogen, the reaction oil gas containing crude gasoline and rich gas is brought into contact with the desulfurization adsorbent to carry out the adsorption desulfurization reaction. After separating the desulfurization adsorbent from the reaction oil gas, the sulfur-filled used adsorbent is stripped to remove the adsorbed hydrocarbons and sent to the adsorbent regenerator. The regenerated desulfurization adsorbent is sent to the adsorbent reducer for reduction, and the reduced desulfurization adsorbent is introduced from the bottom of the fluidized bed desulfurization reactor to realize a continuous cycle of adsorption desulfurization reaction, adsorbent regeneration, adsorbent reduction, and adsorption desulfurization reaction.

[0054] Preferably, at the bottom of the fluidized bed adsorption desulfurization reactor, a mixture of crude gasoline and a hydrogen donor is uniformly distributed into the reactor through a feed distribution plate and brought into sufficient contact with the desulfurization adsorbent in the reactor. The desulfurization adsorbent is introduced from the bottom of the fluidized bed reactor.

[0055] The reaction oil gas obtained after gas-solid separation is sent to a gas-liquid separation tank after heat exchange to obtain desulfurized rich gas and desulfurized crude gasoline. The operating pressure of the gas-liquid separation tank is 0.2 to 4.0 MPa (preferably 0.5 to 3.0 MPa), and the operating temperature is 20 to 300 °C (preferably 50 to 200 °C).

[0056] Figure 1B is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit which is a second type of embodiment of the present application. As shown in Figure 1B, the adsorption desulfurization unit includes a fluidized bed desulfurization reactor 202, a reactor receiver 206, a lock hopper 208 for isolating the reaction-regeneration system, a regenerator feed tank 211, an adsorbent regenerator 214, and a regenerator receiver 217, which are communicated in sequence. The lock hopper 208 communicates with an adsorbent reducer 220 via a pipeline 219, and the adsorbent reducer 220 communicates with the bottom of the fluidized bed desulfurization reactor 202.

[0057] The preheated crude gasoline and hydrogen are introduced into the bottom of the fluidized bed desulfurization reactor 202 via a pipeline 201, contact with the desulfurization adsorbent in the fluidized bed desulfurization reactor 202 for the desulfurization reaction, and the adsorbent partially filled with sulfur moves upward together with the reaction materials. The preheated rich gas is introduced into the fluidized bed desulfurization reactor via a pipeline 203 at a position 30 - 80% of the height from the bottom to the top of the fluidized bed desulfurization reactor 202 and mixed with the reaction oil gas and the desulfurization adsorbent for the desulfurization reaction. The reacted reaction oil gas and adsorbent are passed through a sedimentation separation section at the top of the fluidized bed desulfurization reactor 202 for oil-adsorbent separation. The obtained reaction oil gas is a mixture of desulfurized rich gas, desulfurized crude gasoline and hydrogen, and is sent to a gas-liquid separation tank (not shown) via a pipeline 204. The desulfurized rich gas and desulfurized crude gasoline obtained by condensation gas-liquid separation are sent to the next product separation and stabilization system for treatment.

[0058] The used adsorbent is transferred from the upper part of the fluidized bed desulfurization reactor 202 to the receiver 206 of the reactor through the adsorbent transfer horizontal pipe 205, stripped in the receiver 206 of the reactor, then sent to the lock hopper 208 through the pipeline 207, purged with nitrogen, and then changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure inert atmosphere. The purge gas is sent to the combustion furnace through the pipeline 209 for combustion. The used adsorbent is sent to the regenerator supply tank 211 through the pipeline 210, lifted by the lift gas, and sent to the adsorbent regenerator 214 through the pipeline 212. An oxygen-containing gas is introduced into the adsorbent regenerator from the bottom through the pipeline 213. The used adsorbent is brought into contact with the oxygen-containing gas in the adsorbent regenerator 214 for sulfur combustion and carbon combustion to obtain the regenerated adsorbent. The sulfur-containing exhaust gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and sent to the sulfur production system, or subjected to alkali washing through the pipeline 215 to remove SOx. The regenerated adsorbent is sent from the adsorbent regenerator to the receiver 217 of the regenerator through the pipeline 216, lifted by nitrogen, sent to the lock hopper 208 through the pipeline 218, stripped and purged with hydrogen, and then the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 208 and introduced into the reducer 220 for reduction through the pipeline 219. The reduced and regenerated adsorbent is introduced into the fluidized bed desulfurization reactor 202 through the pipeline 221, as a result, realizing a continuous adsorption desulfurization reaction.

[0059] 〔Embodiment of the Third Type〕 According to the embodiment of the third type of the method according to the present application, the catalytic cracking light product is the rich gas and the crude gasoline from the catalytic cracking fractionation tower, and step 1) further includes the following steps: 1a) Introducing the crude gasoline from the catalytic cracking fractionation tower into the first fluidized bed desulfurization reactor from the bottom, and bringing it into contact with the desulfurization adsorbent introduced into the reactor from the bottom in the presence of hydrogen for the desulfurization reaction; 1b) Separating the gas-solid of the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain crude desulfurized gasoline and a desulfurization adsorbent partially filled with sulfur, and sending the desulfurization adsorbent partially filled with sulfur to the second fluidized bed desulfurization reactor; 1c) Introducing the rich gas from the catalytic cracking fractionation tower into the second fluidized bed desulfurization reactor from the bottom, and contacting it with the desulfurization adsorbent partially filled with sulfur introduced into the reactor from the bottom for the desulfurization reaction; 1d) Separating the gas-solid of the reaction stream obtained at the upper part of the second fluidized bed desulfurization reactor to obtain desulfurized rich gas and a sulfur-filled adsorbent; and 1e) Sending the sulfur-filled adsorbent obtained in step 1d) to the adsorbent regenerator for regeneration by calcining in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction.

[0060] In some preferred embodiments, the crude gasoline from the catalytic cracking fractionation tower is introduced into the first fluidized bed desulfurization reactor from the bottom, flowed upward, and contacted with the desulfurization adsorbent in the presence of hydrogen for desulfurization, and subjected to gas-solid separation in the upper sedimentation area. The separated desulfurization adsorbent partially filled with sulfur is introduced into the second fluidized bed desulfurization reactor. The separated reaction oil gas is crude desulfurized gasoline. The rich gas from the catalytic cracking fractionation tower is introduced into the second fluidized bed desulfurization reactor from the bottom, flowed upward, and contacted with the desulfurization adsorbent for desulfurization, and subjected to gas-solid separation in the upper sedimentation area. The separated reaction oil gas is desulfurized rich gas. The separated sulfur-filled adsorbent is passed through the adsorbent regenerator for regeneration by calcining using an oxygen-containing gas. The regenerated desulfurization adsorbent is recycled to the bottom of the first fluidized bed desulfurization reactor after reduction. The desulfurized rich gas and the crude desulfurized gasoline are separately sent to the absorption stabilization system for separation to obtain desulfurized dry gas, desulfurized liquefied gas and desulfurized stabilized gasoline.

[0061] Furthermore, in a further preferred embodiment, the crude gasoline from the catalytic cracking fractionation column or a mixture of crude gasoline and a hydrogen donor is preheated to a temperature of 100 to 500 °C (preferably 300 to 450 °C). The heated crude gasoline is used as a raw material for the first fluidized bed desulfurization reactor and introduced into the first fluidized bed desulfurization reactor from the bottom. The desulfurization adsorbent is introduced into the first fluidized bed desulfurization reactor from the bottom. The raw material is brought into contact with the desulfurization adsorbent for the adsorptive desulfurization reaction. The reaction stream flows from the bottom to the top, and the reaction oil gas and the desulfurization adsorbent are separated by gas-solid separation in a sedimentation area with an enlarged pipe diameter at the upper part of the first fluidized bed desulfurization reactor. The sedimentation area may further be provided with a gas-solid separation device such as a cyclone separator or a filter. The separated reaction oil gas is desulfurized crude gasoline. The separated desulfurization adsorbent partially filled with sulfur is passed through an adsorbent transfer tank. The desulfurization adsorbent is subjected to the system pressure in the adsorbent transfer tank and then introduced into the second fluidized bed desulfurization reactor.

[0062] The desulfurization adsorbent partially filled with sulfur is introduced into the second fluidized bed desulfurization reactor and brought into contact with rich gas or a mixture of rich gas and a hydrogen donor preheated to the temperature required for the desulfurization reaction. Sulfur in the rich gas is transferred to the desulfurization adsorbent, and in a sedimentation area with an enlarged pipe diameter at the upper part of the second fluidized bed desulfurization reactor, the reaction oil gas and the desulfurization adsorbent are gas-solid separated. The separated reaction oil gas is desulfurized rich gas. The separated desulfurization adsorbent with high sulfur filling is introduced into an adsorbent regenerator and brought into contact with an oxygen-containing gas for regeneration. The regenerated desulfurization adsorbent is recycled to the first fluidized bed desulfurization reactor for reuse after reduction.

[0063] The desulfurized rich gas is introduced into the absorption column from the bottom, and the desulfurized crude gasoline or crude gasoline and a part of the stabilized gasoline are introduced into the absorption column from the top and brought into contact with the rich gas in a countercurrent manner. The overhead gas product of the absorption column is absorbed using the light cycle oil from the catalytic cracking fractionation column and separated in the reabsorption column. The desulfurized dry gas is obtained at the top of the reabsorption column. The concentrated light cycle oil is obtained at the bottom of the reabsorption column. The concentrated light cycle oil is recycled to the catalytic cracking fractionation column. The bottom product of the absorption column is sent to the stabilization column after passing through the desorption column, fractionated in the stabilization column to obtain desulfurized liquefied gas and desulfurized stabilized catalytic cracking gasoline. The overhead gas of the desorption column is mixed with the desulfurized rich gas and then sent to the absorption column.

[0064] Preferably, the crude gasoline from the catalytic cracking fractionation column or a mixture of crude gasoline and a hydrogen donor is introduced into the first fluidized bed desulfurization reactor from the bottom. The mixture of crude gasoline and the hydrogen donor is uniformly distributed into the reactor through a feed distribution plate and brought into sufficient contact with the desulfurization adsorbent in the reactor.

[0065] In a further preferred embodiment, in the first fluidized bed desulfurization reactor, the sulfur-containing crude gasoline is under reaction conditions including a temperature of 200 to 550 °C (preferably 300 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), a weight hourly space velocity of 0.1 to 100 h -1 (preferably 1 to 10 h -1 ) and a volume ratio of the hydrogen donor to the gasoline feedstock of 0.01 to 1000 (preferably 0.05 to 500), and is brought into contact with the desulfurization adsorbent for the adsorptive desulfurization reaction to transfer sulfur to the desulfurization adsorbent.

[0066] After separating the desulfurization adsorbent from the reaction oil gas, the sulfur-filled used adsorbent is introduced into the adsorbent transfer tank and transferred to the second desulfurization regenerator after a pressure change.

[0067] The rich gas from the catalytic cracking fractionation column, or the rich gas and the hydrogen donor, are heated to a temperature of 100 to 500 °C (preferably 200 to 450 °C). The heated rich gas or the heated mixture of the rich gas and the hydrogen donor is introduced from the bottom into the second fluidized bed desulfurization reactor, and the sulfur-containing rich gas is at a temperature of 300 to 550 °C (preferably 350 to 500 °C), an absolute pressure of 0.1 to 3 MPa (preferably 0.2 to 2.5 MPa), 1 to 100 h -1 (preferably 2 to 20 h -1 ) of weight hourly space velocity, and a volume ratio of the hydrogen donor or hydrogen to the rich gas feedstock of 0.01 to 500 (preferably 0.05 to 300) under reaction conditions, and is brought into contact with the adsorbent partially filled with sulfur from the first reactor for the adsorptive desulfurization reaction. The operating pressure of the second fluidized bed desulfurization reactor is preferably 0.5 to 2.0 MPa lower than the operating pressure of the first fluidized bed desulfurization reactor.

[0068] The rich gas from the catalytic cracking fractionation column, or the mixture of the rich gas and the hydrogen donor, is uniformly distributed into the second fluidized bed desulfurization reactor through the feed distribution plate and brought into sufficient contact with the desulfurization adsorbent in the second fluidized bed desulfurization reactor.

[0069] After separating the sulfur-filled desulfurization adsorbent from the reaction oil gas in the sedimentation section with an enlarged pipe diameter at the upper part of the second fluidized bed desulfurization reactor, the sulfur-filled used adsorbent is stripped to remove the adsorbed hydrocarbons, lifted, and then sent to the fluidized bed regenerator. The regenerated desulfurization adsorbent is sent to the adsorbent reducer for reduction. The reduced desulfurization adsorbent is sent from the bottom to the first fluidized bed desulfurization reactor for reuse, and as a result, a continuous cycle of adsorptive desulfurization reaction, adsorbent regeneration, adsorbent reduction, and adsorptive desulfurization reaction is realized.

[0070] The reaction oil gas separated from the first fluidized bed desulfurization reactor is desulfurized crude gasoline. The reaction oil gas separated from the second fluidized bed desulfurization reactor is desulfurized rich gas.

[0071] Figure 1C is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to a third type of embodiment of the present application. As shown in Figure 1C, the adsorption desulfurization unit includes a first fluidized bed desulfurization reactor 302, an adsorbent transfer tank 305, a second fluidized bed desulfurization reactor 308, a reactor receiver 311, a lock hopper 313 for isolating the reaction-regeneration system, a regenerator feed tank 316, an adsorbent regenerator 319, and a regenerator receiver 322, which are connected in communication in sequence. The regenerator receiver 322 communicates with an adsorbent reducer 325 via the lock hopper 313. The adsorbent reducer 325 communicates with the bottom of the first fluidized bed desulfurization reactor 302 via a pipeline 326, providing a desulfurization adsorbent for the first fluidized bed desulfurization reactor.

[0072] Preheated crude gasoline and hydrogen from the catalytic cracking fractionation tower are introduced from the bottom into the first fluidized bed desulfurization reactor 302 via pipeline 301, and are brought into contact with a desulfurization adsorbent in the first fluidized bed desulfurization reactor 302 for the desulfurization reaction, and the adsorbent partially filled with sulfur moves upward together with the reaction materials. After the reaction, the reaction oil gas and the adsorbent are passed through the sedimentation separation section at the top of the first fluidized bed desulfurization reactor 302 for oil-adsorbent separation. The separated reaction oil gas is a mixture of desulfurized crude gasoline and hydrogen, and is sent via pipeline 303 to the next product separation and stabilization system for processing. The separated desulfurization adsorbent partially filled with sulfur is transferred from the first fluidized bed desulfurization reactor to the adsorbent transfer tank 305 via pipeline 304, and then from the adsorbent transfer tank 305 to the bottom of the second fluidized bed desulfurization reactor 308 via pipeline 306. A mixture of rich gas and hydrogen from the catalytic cracking fractionation tower is introduced from the bottom into the second fluidized bed desulfurization reactor 308 via pipeline 307, and is brought into contact with a desulfurization adsorbent for the adsorption desulfurization reaction to transfer the sulfur in the rich gas to the desulfurization adsorbent. The reaction mixture is subjected to gas-solid separation in the sedimentation area at the upper part of the second fluidized bed desulfurization reactor 308. The separated desulfurized rich gas is sent via pipeline 309 to the next product separation and stabilization system for processing. The separated sulfur-filled adsorbent is sent via the adsorbent transfer horizontal pipe 310 to the reactor receiver 311 at the upper part of the second fluidized bed desulfurization reactor 308, stripped in the reactor receiver 311, then sent via pipeline 312 to the lock hopper 313, purged with nitrogen, and then changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure inert atmosphere. The purge gas is sent via pipeline 314 to a combustion furnace for combustion. The sulfur-filled adsorbent is sent via pipeline 315 to the regenerator supply tank 316, where the sulfur-filled adsorbent is lifted by a lift gas and sent via pipeline 317 to the adsorbent regenerator 319. An oxygen-containing gas is introduced from the bottom into the adsorbent regenerator via pipeline 318. The used adsorbent is brought into contact with the oxygen-containing gas in the adsorbent regenerator 319 for sulfur combustion and carbon combustion to obtain a regenerated adsorbent.The sulfur-containing exhaust gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and sent to the sulfur production system, or is subjected to alkali washing via pipeline 320 to remove SOx. The regenerated adsorbent is sent from the adsorbent regenerator to the regenerator receiver 322 via pipeline 321, lifted by nitrogen, sent to the lock hopper 313 via pipeline 323, stripped and purged with hydrogen. Then, the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 313 and introduced into the adsorbent reducer 325 via pipeline 324 for reduction. The reduced and regenerated adsorbent is introduced into the first fluidized bed desulfurization reactor 302 via pipeline 326, resulting in a continuous adsorption desulfurization reaction.

[0073] 〔Fourth type of embodiment〕 According to the fourth type of embodiment of the present application, the catalytic cracking light products are rich gas and crude gasoline from the catalytic cracking fractionation tower, and step 1) further includes the following steps: 1a) Introducing the crude gasoline from the catalytic cracking fractionation tower into the first fluidized bed desulfurization reactor from the bottom and bringing it into contact with the desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for the desulfurization reaction; 1b) Performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain the first reaction oil gas and the desulfurization adsorbent partially filled with sulfur, and sending the desulfurization adsorbent partially filled with sulfur to the second fluidized bed desulfurization reactor; 1c) Introducing the rich gas from the catalytic cracking fractionation tower into the second fluidized bed desulfurization reactor from the bottom and bringing it into contact with the desulfurization adsorbent partially filled with sulfur introduced from the bottom of the reactor for the desulfurization reaction; 1d) Performing gas-solid separation on the reaction stream obtained from the upper part of the second fluidized bed desulfurization reactor to obtain the second reaction oil gas and the sulfur-filled adsorbent, and recycling the second reaction oil gas to the first fluidized bed desulfurization reactor (preferably, the upper part of the first fluidized bed desulfurization reactor); 1e) A step of subjecting the first reaction oil gas obtained in step 1b) to gas-liquid separation to obtain a desulfurized rich gas and desulfurized crude gasoline; and, 1f) A step of sending the sulfur-loaded adsorbent obtained in step 1d) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurized adsorbent to a fluidized bed desulfurization reactor after reduction.

[0074] In a preferred embodiment, the crude gasoline and hydrogen donor from the catalytic cracking fractionation column are introduced into the bottom of the first fluidized bed desulfurization reactor, and while flowing upward, they are brought into contact with a desulfurization adsorbent for desulfurization. The sulfur-partially filled desulfurization adsorbent obtained by gas-solid separation at the top of the reactor is introduced into the second fluidized bed desulfurization reactor. The rich gas and hydrogen donor from the catalytic cracking fractionation column are introduced into the bottom of the second fluidized bed desulfurization reactor and brought into contact with the desulfurization adsorbent for desulfurization. After the reaction, the reaction oil gas separated from the desulfurization adsorbent is recycled to the upper part of the first fluidized bed desulfurization reactor. The reaction oil gas obtained by gas-solid separation in the first fluidized bed desulfurization reactor is subjected to gas-liquid separation to obtain a desulfurized rich gas and desulfurized crude gasoline. The desulfurized rich gas is introduced into the absorption tower from the bottom and brought into contact with the desulfurized crude gasoline introduced into the absorption tower from the top for mass transfer. The top stream of the absorption tower is introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer. The desulfurized dry gas is obtained from the top of the reabsorption tower, and the concentrated light cycle oil obtained at the bottom of the reabsorption tower is recycled to the catalytic cracking fractionation column. The bottom product of the absorption tower is sent to a stabilization tower after passing through a stripping tower, and fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the stripping tower is recycled to the absorption tower.

[0075] In a further preferred embodiment, a mixture of the crude gasoline from the catalytic cracking fractionation column and the hydrogen donor is preheated to the required temperature and introduced into the first fluidized bed desulfurization reactor from the bottom, and while flowing from the bottom to the top, it is brought into contact with a desulfurization adsorbent in the first fluidized bed desulfurization reactor for desulfurization. The reaction mixture is subjected to gas-solid separation at the top of the first fluidized bed desulfurization reactor. The obtained sulfur-partially filled desulfurization adsorbent is introduced into the top of the second fluidized bed desulfurization reactor and brought into contact with the rich gas preheated to the required temperature and / or a mixture of the rich gas and the hydrogen donor introduced into the reactor from the bottom for the desulfurization reaction. The desulfurized rich gas is recycled from the second fluidized bed desulfurization reactor to the upper part of the first fluidized bed desulfurization reactor. The used adsorbent obtained after the reaction in the second fluidized bed desulfurization reactor is separated from the reaction oil gas, changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure oxygen atmosphere, and then introduced into an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas. The regenerated desulfurization adsorbent is recycled to the bottom of the first fluidized bed desulfurization reactor for reuse after reduction.

[0076] The reaction oil gas obtained by separation at the top of the first fluidized bed desulfurization reactor is introduced into a gas-liquid separation tank, separated by condensation and cooling to obtain desulfurized rich gas and desulfurized crude gasoline. The desulfurized rich gas is introduced into an absorption tower from the bottom and brought into contact with a part of the crude gasoline and / or stabilized gasoline introduced into the absorption tower in a countercurrent manner from the top. The top gas product of the absorption tower is introduced into a reabsorption tower, absorbed using the light cycle oil from the catalytic cracking fractionation column, separated there, and desulfurized dry gas is obtained at the top of the reabsorption tower, and concentrated light cycle oil is obtained at the bottom of the reabsorption tower. The concentrated light cycle oil is recycled to the catalytic cracking fractionation column. The bottom product of the absorption tower is sent to a stabilization tower after passing through a stripping tower, fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the stripping tower is mixed with the desulfurized rich gas and then passed through the absorption tower.

[0077] Furthermore, in a further preferred embodiment, the crude gasoline obtained from the catalytic cracking fractionation column is heated to 100 to 500 °C. The heated crude gasoline is used as a raw material for the first fluidized bed desulfurization reactor. The crude gasoline (preferably a mixture of crude gasoline and a hydrogen donor) is introduced into the first fluidized bed desulfurization reactor from the bottom. The mixture of crude gasoline and hydrogen donor is uniformly distributed into the reactor through a feed distribution plate and brought into sufficient contact with the desulfurization adsorbent in the reactor.

[0078] The desulfurization adsorbent is introduced into the first fluidized bed desulfurization reactor (preferably a dense phase bed reactor) from the bottom.

[0079] Preferably, the sulfur-containing crude gasoline is, in the presence of hydrogen, at a temperature of 200 to 550 °C (preferably 300 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), 0.1 to 100 h -1 (preferably 1 to 10 h -1 ) weight hourly space velocity, and a volume ratio of the hydrogen donor to the gasoline raw material of 0.01 to 1000 (preferably 0.05 to 500), and brought into contact with the desulfurization adsorbent for the adsorption desulfurization reaction under the reaction conditions.

[0080] In the first fluidized bed desulfurization reactor, after separating the desulfurization adsorbent from the reaction oil gas, the sulfur-filled used adsorbent is passed through the second fluidized bed desulfurization reactor.

[0081] The rich gas and / or hydrogen donor from the catalytic cracking fractionation column is heated to 100 to 500 °C. The sulfur content of the rich gas is 30 μg / g or more (especially 50 μg / g or more). The heated rich gas and / or its mixture with the hydrogen donor is introduced from the bottom of the second fluidized bed reactor. The sulfur-containing rich gas is at a temperature of 300 to 550 °C (preferably 350 to 500 °C), an absolute pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), 0.1 to 100 h -1 (preferably 2 to 20 h -1Under reaction conditions including the weight hourly space velocity of ), and the volume ratio of the hydrogen donor or hydrogen to the rich gas raw material of 0.01 to 500 (preferably 0.05 to 300), for the adsorptive desulfurization reaction, the sulfur from the first reactor is contacted with the adsorbent partially filled with sulfur.

[0082] The mixture of rich gas and / or hydrogen donor is uniformly distributed into the second fluidized bed desulfurization reactor through the feed distribution plate and sufficiently contacts the desulfurization adsorbent in the second fluidized bed desulfurization reactor.

[0083] After separating the sulfur-filled desulfurization adsorbent in the second fluidized bed desulfurization reactor from the reaction oil gas, the used adsorbent is stripped to remove the adsorbed hydrocarbons, and then lifted and sent to the adsorbent regenerator. The regenerated desulfurization adsorbent is sent to the adsorbent reducer for reduction. The reduced desulfurization adsorbent is sent to the first fluidized bed desulfurization reactor from the bottom for reuse, and as a result, a continuous cycle of adsorptive desulfurization reaction, adsorbent regeneration, adsorbent reduction, and adsorptive desulfurization reaction is realized.

[0084] The reaction oil gas separated in the first fluidized bed desulfurization reactor is sent to a gas-liquid separation tank after heat exchange, and desulfurized rich gas and desulfurized crude gasoline are obtained. The operating pressure of the gas-liquid separation tank is 0.2 to 4.0 MPa (preferably 0.5 to 3.0 MPa), and the operating temperature is 20 to 300 °C (preferably 50 to 200 °C).

[0085] Figure 1D is a schematic diagram of a preferred embodiment of the adsorptive desulfurization unit which is the fourth type of embodiment of the present application. As shown in Figure 1D, the adsorptive desulfurization unit includes a first fluidized bed desulfurization reactor 402, a second fluidized bed desulfurization reactor 406, a reactor receiver 409, a lock hopper 411 for isolating the reaction-regeneration system, a regenerator supply tank 414, an adsorbent regenerator 417, and a regenerator receiver 420, which are connected in series in turn. The regenerator receiver 420 communicates with the adsorbent reducer 423 via the lock hopper 411. The adsorbent reducer 423 communicates with the bottom of the first fluidized bed desulfurization reactor 402 and supplies the desulfurization adsorbent to the first fluidized bed desulfurization reactor 402.

[0086] The preheated crude gasoline and hydrogen from the catalytic cracking fractionation column are introduced through pipeline 401 to the bottom of the first fluidized bed desulfurization reactor 402, and are brought into contact with the desulfurization adsorbent in the first fluidized bed desulfurization reactor 402 for the desulfurization reaction. The adsorbent partially filled with sulfur moves upward together with the reaction materials. After the reaction, the reaction oil gas and the adsorbent are passed through the sedimentation separation section at the top of the first fluidized bed desulfurization reactor 402 for oil-adsorbent separation. The obtained reaction oil gas is a mixture of desulfurized rich gas, desulfurized crude gasoline and hydrogen. The mixture is sent through pipeline 403 to a gas-liquid separation tank (not shown), and the desulfurized rich gas and desulfurized crude gasoline obtained by condensation gas-liquid separation are sent to the next product separation and stabilization system for treatment. The desulfurization adsorbent partially filled with sulfur is transferred from the first fluidized bed desulfurization reactor through pipeline 404 to the bottom of the second fluidized bed desulfurization reactor 406. A mixture of rich gas and hydrogen from the catalytic cracking fractionation column is introduced from the bottom of the second fluidized bed desulfurization reactor 406 and brought into contact with the desulfurization adsorbent for the adsorption desulfurization reaction. The reaction mixture is subjected to gas-solid separation in the sedimentation area at the upper part of the second fluidized bed desulfurization reactor. The separated sulfur-filled adsorbent is sent through the adsorbent transfer horizontal pipe 408 at the upper part of the second fluidized bed desulfurization reactor to the reactor receiver 409, stripped in the reactor receiver 409, and then sent through pipeline 410 to the lock hopper 411, purged with nitrogen, and changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure inert atmosphere. The purge gas is sent through pipeline 412 to a combustion furnace for combustion. The sulfur-filled adsorbent is sent through pipeline 413 to the regenerator supply tank 414, the sulfur-filled adsorbent is lifted by the lift gas, and sent through pipeline 415 to the adsorbent regenerator 417. An oxygen-containing gas is introduced from the bottom through pipeline 416 into the adsorbent regenerator. The used adsorbent is brought into contact with the oxygen-containing gas in the adsorbent regenerator 417 for sulfur combustion and carbon combustion to obtain a regenerated adsorbent. The sulfur-containing exhaust gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and sent to a sulfur production system, or is subjected to alkali washing through pipeline 418 to remove SOx.The regenerated adsorbent is sent from the adsorbent regenerator to the receiver 420 of the regenerator via pipeline 419, lifted by nitrogen, sent to the lock hopper 411 via pipeline 421, stripped and purged with hydrogen. Then, the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 411 and introduced into the adsorbent reducer 423 for reduction via pipeline 422. The reduced and regenerated adsorbent is introduced into the first fluidized bed desulfurization reactor 402 via pipeline 424, thereby realizing a continuous adsorptive desulfurization reaction.

[0087] 〔Fifth type of embodiment〕 According to the fifth type of embodiment of the method according to the present application, the catalytic cracking light product is the rich gas and the crude gasoline from the catalytic cracking fractionation column, and step 1) further includes the following steps: 1a) Introducing the crude gasoline from the catalytic cracking fractionation column into the first fluidized bed desulfurization reactor from the bottom, and bringing it into contact with the desulfurization adsorbent introduced into the reactor from the bottom in the presence of hydrogen for the desulfurization reaction; 1b) Taking out a part of the desulfurization adsorbent from the lower central part of the first fluidized bed desulfurization reactor, passing it through the bottom of the second fluidized bed desulfurization reactor, bringing it into contact with the rich gas from the catalytic cracking fractionation column introduced into the reactor from the bottom for the desulfurization reaction, and recycling the reaction stream obtained from the upper part of the second fluidized bed desulfurization reactor to the first fluidized bed desulfurization reactor (preferably, the upper part of the first fluidized bed desulfurization reactor); 1c) Performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain the reaction oil gas and the sulfur-filled adsorbent; 1d) Performing gas-liquid separation on the reaction oil gas obtained in step 1c) to obtain the desulfurized rich gas and the desulfurized crude gasoline; and, 1e) Sending the sulfur-filled adsorbent obtained in step 1c) to the adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction.

[0088] In a preferred embodiment, the crude gasoline from the catalytic cracking fractionation column is introduced from the bottom into the first fluidized bed desulfurization reactor and brought into contact with a desulfurization adsorbent for desulfurization while flowing upward. A part of the desulfurization adsorbent is introduced into the second fluidized bed desulfurization reactor under the control of a slide valve and brought into contact with rich gas preheated to the temperature required for the desulfurization reaction. The reacted rich gas and desulfurization adsorbent are returned to the upper part of the first fluidized bed desulfurization reactor and subjected to gas-solid separation in the sedimentation area at the upper part of the first fluidized bed desulfurization reactor. The separated used adsorbent is regenerated in an adsorbent regenerator by calcination in the presence of an oxygen-containing gas. The regenerated desulfurization adsorbent is recycled to the bottom of the first fluidized bed desulfurization reactor for reuse after reduction. The separated reaction oil gas is separated into desulfurized rich gas and desulfurized crude gasoline in a gas-liquid separation tank, and these are separately sent to an absorption stabilization system for further separation to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0089] In another preferred embodiment, a sedimentation area and a gas-solid separator are provided at the upper part of the second fluidized bed desulfurization reactor. The reaction oil gas and desulfurization adsorbent in the second fluidized bed desulfurization reactor are subjected to gas-solid separation, the separated desulfurization adsorbent is recycled to the upper part of the first fluidized bed desulfurization reactor, and the separated reaction oil gas is directly sent to an absorption stabilization system for further separation. The reaction oil gas obtained by gas-solid separation at the top of the first fluidized bed desulfurization reactor is desulfurized crude gasoline.

[0090] Furthermore, in a further preferred embodiment, the crude gasoline from the catalytic cracking fractionation column, or a mixture of the crude gasoline and a hydrogen donor, is preheated to 100 to 500 °C (preferably 200 to 450 °C). The heated crude gasoline is used as a raw material for the first fluidized bed desulfurization reactor and is introduced into the first fluidized bed desulfurization reactor from the bottom, and the desulfurization adsorbent is introduced into the first fluidized bed desulfurization reactor from the bottom. The reaction oil gas is brought into contact with the desulfurization adsorbent for the adsorptive desulfurization reaction. The reaction flow flows from the bottom to the top, and at a position 20 to 60% of the height from the bottom to the top of the first fluidized bed desulfurization reactor, a part of the desulfurization adsorbent partially filled with sulfur is taken out, and then this part is introduced into the second fluidized bed desulfurization reactor under the control of a slide valve and brought into contact with the rich gas from the catalytic cracking fractionation column or a mixture of the rich gas and a hydrogen donor that is introduced into the reactor from the bottom and preheated to the required temperature for the desulfurization reaction. The reacted rich gas and the desulfurization adsorbent are returned to the upper part of the first fluidized bed desulfurization reactor. The reaction oil gas and the desulfurization adsorbent are separated in a sedimentation area where the pipe diameter is enlarged at the upper part of the first fluidized bed desulfurization reactor. The sedimentation area may further be provided with a gas-solid separation device such as a cyclone separator or a filter. The separated reaction oil gas is sent to a gas-liquid separation tank to be separated into desulfurized crude gasoline and desulfurized rich gas. The separated used adsorbent with high sulfur filling is introduced into an adsorbent regenerator and brought into contact with oxygen for regeneration. The regenerated adsorbent is recycled to the first fluidized bed desulfurization reactor for reuse after reduction.

[0091] In another further preferred embodiment, the reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation in a sedimentation area where the pipe diameter is enlarged at the upper part of the second fluidized bed desulfurization reactor. The sedimentation area may further be provided with a gas-solid separation device such as a cyclone separator or a filter. The separated desulfurization adsorbent is recycled to the upper part of the first fluidized bed desulfurization reactor. The separated reaction oil gas is desulfurized rich gas, which is directly sent to an absorption stabilization system for further separation. The reaction oil gas obtained by gas-solid separation at the top of the first fluidized bed desulfurization reactor is desulfurized crude gasoline.

[0092] In a particularly preferred embodiment, the crude gasoline or a mixture of crude gasoline and a hydrogen donor is introduced into the first fluidized bed desulfurization reactor from the bottom. The mixture of crude gasoline and a hydrogen donor is uniformly distributed into the reactor through a feed distribution plate and sufficiently contacts the desulfurization adsorbent in the reactor. The sulfur-containing crude gasoline is at a temperature of 200 to 550 °C (preferably 300 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), and a weight hourly space velocity of 0.1 to 100 h -1 (preferably 1 to 10 h -1 ), and a volume ratio of the hydrogen donor to the gasoline feedstock of 0.01 to 1000 (preferably 0.05 to 500), and is contacted with the desulfurization adsorbent for an adsorption desulfurization reaction under the reaction conditions.

[0093] In the first fluidized bed desulfurization reactor, the desulfurization adsorbent partially filled with sulfur is passed through a slide valve to the second fluidized bed desulfurization reactor and contacted with the rich gas introduced into the reactor from the bottom or a mixture of rich gas and a hydrogen donor for the desulfurization reaction.

[0094] The sulfur content of the rich gas is 30 μg / g or more, particularly 50 μg / g or more. The preheating temperature of the rich gas or the rich gas and the hydrogen donor is 100 to 500 °C, preferably 250 to 450 °C. The rich gas or the mixture of rich gas and a hydrogen donor is uniformly distributed into the second fluidized bed desulfurization reactor through a feed distribution plate and sufficiently contacts the desulfurization adsorbent in the second fluidized bed desulfurization reactor.

[0095] The heated mixture of rich gas and / or hydrogen donor is introduced from the bottom of the second fluidized bed desulfurization reactor. The sulfur-containing rich gas is at a temperature of 250 to 550 °C (preferably 350 to 500 °C), a pressure of 0.5 to 5 MPa (preferably 1.0 to 3.5 MPa), and a weight hourly space velocity of 0.1 to 100 h -1 (preferably 1 to 20 h -1Under reaction conditions including the weight hourly space velocity of [[ID=]], and a hydrogen-to-oil molar ratio of 0.01 to 1000 (preferably 0.05 to 300), for the adsorptive desulfurization reaction, sulfur from the first reactor is contacted with an adsorbent partially filled with sulfur.

[0096] After separating the used desulfurization adsorbent in the first fluidized bed desulfurization reactor from the reaction oil gas, the sulfur-filled used adsorbent is stripped to remove the adsorbed hydrocarbons, then lifted and sent to a fluidized bed regenerator. The regenerated desulfurization adsorbent is sent to an adsorbent reducer for reduction, and the reduced desulfurization adsorbent is sent from the bottom to the first fluidized bed desulfurization reactor for reuse, as a result, a continuous cycle of adsorptive desulfurization reaction, adsorbent regeneration, adsorbent reduction and adsorptive desulfurization reaction is realized.

[0097] When the oil gas and desulfurization adsorbent in the second fluidized bed desulfurization reactor return to the upper part of the first fluidized bed desulfurization reactor, the reaction oil gas separated from the first fluidized bed desulfurization reactor is sent to a gas-liquid separation tank after heat exchange, and desulfurized rich gas and desulfurized crude gasoline are obtained. The operating pressure of the gas-liquid separation tank is 0.2 to 4.0 MPa (preferably 0.5 to 3.0 MPa), and the operating temperature is 20 to 300 °C (preferably 50 to 200 °C).

[0098] When a sedimentation section with an enlarged pipe diameter and a gas-solid separation device are provided at the upper part of the second fluidized bed desulfurization reactor, the reaction oil gas and desulfurization adsorbent in the second fluidized bed desulfurization reactor are subjected to gas-solid separation at the top of the reactor. The separated reaction oil gas is desulfurized rich gas. The separated desulfurization adsorbent is recycled to the upper part of the first fluidized bed desulfurization reactor.

[0099] Figure 1Ea is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to the fifth type of embodiment of the present application. As shown in Figure 1Ea, the adsorption desulfurization unit includes a first fluidized bed desulfurization reactor 502, a reactor receiver 509, a lock hopper 511 for isolating the reaction-regeneration system, a regenerator supply tank 514, and an adsorbent regenerator 517, which are communicated in sequence. The adsorbent regenerator 517 is communicated with a regenerator receiver 520, a lock hopper 511, and an adsorbent reducer 523 in sequence. The adsorbent reducer 523 communicates with the bottom of the first fluidized bed desulfurization reactor 502 to provide a desulfurization adsorbent thereto. The lower center of the first fluidized bed desulfurization reactor 502 communicates with the bottom of the second fluidized bed desulfurization reactor 506, and the top of the second fluidized bed desulfurization reactor communicates with the upper part of the first fluidized bed desulfurization reactor 502.

[0100] The preheated crude gasoline from the catalytic cracking fractionation tower and hydrogen are introduced into the bottom of the first fluidized bed desulfurization reactor 502 through the pipeline 501, and are brought into contact with the desulfurization adsorbent in the first fluidized bed desulfurization reactor 502 for the desulfurization reaction. The adsorbent partially filled with sulfur moves upward together with the reaction materials. At a position 20 - 60% of the height from the bottom to the top of the first fluidized bed desulfurization reactor 502, a part of the desulfurization adsorbent is taken out, and then this part is passed through the second fluidized bed desulfurization reactor 506 under the control of a slide valve and brought into contact with the rich gas preheated to the required temperature and / or a mixture of a hydrogen donor and the rich gas introduced into the reactor from the bottom for the desulfurization reaction.

[0101] The reacted rich gas and the desulfurization adsorbent are returned to the upper part of the first fluidized bed desulfurization reactor 502. The reaction oil gas and the adsorbent in the first fluidized bed desulfurization reactor 502 are passed through the sedimentation separation section at the top of the reactor for oil-adsorbent separation. The obtained reaction oil gas is a mixture of desulfurized rich gas, desulfurized crude oil gas, and hydrogen. The mixture is sent through pipeline 503 to a gas-liquid separation tank (not shown). The desulfurized rich gas and desulfurized crude gasoline obtained by condensation gas-liquid separation are sent to the next product separation and stabilization system for treatment. The sulfur-loaded desulfurization adsorbent is sent from the first fluidized bed desulfurization reactor through the adsorbent transfer horizontal pipe 508 to the receiver 509 of the reactor, and then, after being stripped in the receiver 509 of the reactor, it is sent through pipeline 510 to the lock hopper 511, purged with nitrogen, and then changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure inert atmosphere. The purge gas is sent through pipeline 512 to a combustion furnace and burned. The sulfur-loaded adsorbent is sent through pipeline 513 to the regenerator supply tank 514, where it is lifted by the lift gas and sent through pipeline 515 to the adsorbent regenerator 517. An oxygen-containing gas is introduced into the adsorbent regenerator from the bottom through pipeline 516. The used adsorbent is contacted with the oxygen-containing gas in the adsorbent regenerator 517 for sulfur combustion and carbon combustion to obtain a regenerated adsorbent. The sulfur-containing exhaust gas is separated from the regenerated adsorbent at the top of the adsorbent regenerator and sent to a sulfur production system or subjected to alkali washing through pipeline 518 to remove SOx. The regenerated adsorbent is sent from the adsorbent regenerator through pipeline 519 to the receiver 520 of the regenerator, lifted by nitrogen, sent through pipeline 521 to the lock hopper 511, stripped and purged with hydrogen, and then the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 511 and introduced through pipeline 522 into the reducer 523 for reduction. The reduced and regenerated adsorbent is introduced through pipeline 524 into the first fluidized bed desulfurization reactor 502, resulting in a continuous adsorption desulfurization reaction.

[0102] Figure 1Eb is a schematic diagram of another preferred embodiment of the adsorption desulfurization unit according to the fifth type of embodiment of the present application. As shown in Figure 1Eb, a sedimentation section with an enlarged pipe diameter is provided at the upper part of the second fluidized bed desulfurization reactor 506. A gas-solid separator is provided in the sedimentation section. The reaction oil gas and desulfurization adsorbent in the second fluidized bed desulfurization reactor 506 are subjected to gas-solid separation at its upper part, and the obtained desulfurized rich gas is sent through the pipeline 526 to the next product separation and stabilization system for treatment. The separated desulfurization adsorbent is returned to the upper part of the first fluidized bed desulfurization reactor 502. The reaction oil gas separated from the top of the first fluidized bed desulfurization reactor 502 is a mixture of desulfurized crude gasoline and hydrogen, and is sent through the pipeline 503 to the next product separation and stabilization system for treatment.

[0103] 〔Sixth type of embodiment〕 According to the sixth type of embodiment of the method according to the present application, the catalytic cracking light products are the rich gas and crude gasoline from the catalytic cracking fractionation tower, and step 1) further includes the following steps: 1a) Introducing the crude gasoline from the catalytic cracking fractionation tower into the first fluidized bed desulfurization reactor from the bottom, and contacting it with the desulfurization adsorbent introduced into the reactor from the bottom in the presence of hydrogen for the desulfurization reaction; 1b) Performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain desulfurized crude gasoline and sulfur-filled adsorbent, and sending a part of the sulfur-filled adsorbent to the upper part of the second fluidized bed desulfurization reactor; 1c) Introducing the rich gas from the catalytic cracking fractionation tower into the second fluidized bed desulfurization reactor from the bottom, and contacting it in a countercurrent manner with the sulfur-filled adsorbent introduced from the upper end of the reactor for the desulfurization reaction, obtaining desulfurized rich gas at the upper end of the second fluidized bed desulfurization reactor, taking out the reacted sulfur-filled adsorbent from the bottom of the second fluidized bed desulfurization reactor, and recycling it to the first fluidized bed desulfurization reactor; and, 1e) Sending the remainder of the sulfur-filled adsorbent obtained in step 1b) to the adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction.

[0104] In a preferred embodiment, the crude gasoline from the catalytic cracking fractionation column is introduced from the bottom into the first fluidized bed desulfurization reactor, and while flowing upward, it is brought into contact with a desulfurization adsorbent in the presence of hydrogen in a co-current manner for desulfurization. The reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation in the sedimentation zone at the upper part of the first fluidized bed desulfurization reactor. A part of the sulfur-loaded adsorbent is introduced from the top of the adsorbent bed layer into the upper part of the second fluidized bed desulfurization reactor through a slide valve. Another part of the sulfur-loaded adsorbent is regenerated in an adsorbent regenerator by calcination. The regenerated desulfurization adsorbent is recycled to the bottom of the first fluidized bed desulfurization reactor for reuse after reduction. The rich gas from the catalytic cracking fractionation column is introduced from the bottom into the second fluidized bed desulfurization reactor and brought into contact with the desulfurization adsorbent in a counter-current manner for the adsorptive desulfurization reaction. The desulfurization adsorbent is recycled from the bottom of the second fluidized bed desulfurization reactor to the first fluidized bed desulfurization reactor after the reaction. The desulfurized crude gasoline obtained from the top of the first fluidized bed desulfurization reactor and the desulfurized rich gas obtained from the top of the second fluidized bed desulfurization reactor are separately sent to an absorption stabilization unit for further separation to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0105] In a more preferred embodiment, a mixture of the crude gasoline from the catalytic cracking fractionation column and a hydrogen donor is preheated to 100 to 500 °C (preferably 200 to 450 °C). The heated crude gasoline is used as a raw material for the first fluidized bed desulfurization reactor and introduced from the bottom of the reactor. The desulfurization adsorbent is introduced into the first fluidized bed desulfurization reactor from the bottom, and the reaction oil gas is brought into contact with the desulfurization adsorbent for the adsorption desulfurization reaction. While the reaction stream simultaneously flows upward, the reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation in the sedimentation area at the upper part of the first fluidized bed desulfurization reactor. A part of the separated sulfur-loaded adsorbent is passed through a slide valve to the second fluidized bed desulfurization reactor, and another part of the sulfur-loaded adsorbent is regenerated in an adsorbent regenerator by calcination in the presence of an oxygen-containing gas. The regenerated desulfurization adsorbent is recycled to the bottom of the first fluidized bed desulfurization reactor for reuse after reduction. The reaction oil gas obtained by separation in the first fluidized bed desulfurization reactor is a mixture of desulfurized crude gasoline and hydrogen, and is sent to the next absorption stabilization unit for further separation.

[0106] Furthermore, in a further preferred embodiment, the crude gasoline, or a mixture of the crude gasoline and a hydrogen donor, is introduced into the first fluidized bed desulfurization reactor from the bottom. The mixture of the crude gasoline and the hydrogen donor is uniformly distributed into the reactor through a supply distribution plate and sufficiently contacts the desulfurization adsorbent in the reactor. The reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation in the sedimentation area with an enlarged pipe diameter at the upper part of the first fluidized bed desulfurization reactor. The sedimentation area may further be provided with a gas-solid separation device such as a cyclone separator or a filter. The desulfurization adsorbent is introduced into the second fluidized bed reactor from the upper part and brought into contact with a rich gas or a mixture of a rich gas and a hydrogen donor preheated to a required temperature, which is introduced into the reactor in a countercurrent manner from the bottom for the desulfurization reaction. The reaction oil gas and the desulfurization adsorbent are subjected to gas-solid separation in the sedimentation area at the upper part of the second fluidized bed desulfurization reactor (it is preferable that a gas-solid separation device such as a filter is provided in the sedimentation area). The separated reaction oil gas is a desulfurized rich gas and is introduced into an absorption stabilization system for further separation.

[0107] Particularly preferably, the first fluidized bed desulfurization reactor communicates with the position at 80-90% of the height from the bottom to the top of the second fluidized bed desulfurization reactor at a position of 50-90% of the height from the bottom to the top of the first fluidized bed desulfurization reactor.

[0108] Particularly preferably, the supply gas velocity of the first fluidized bed desulfurization reactor is 0.25-10 m / s, and the supply gas velocity of the second fluidized bed desulfurization reactor is 0.05-1.5 m / s.

[0109] In a particularly preferred embodiment, the first fluidized bed desulfurization reactor is operated under conditions including a temperature of 200-550 °C (preferably 300-500 °C), a pressure of 0.5-5 MPa (preferably 1.0-3.5 MPa), and a weight hourly space velocity of 0.1-100 h -1 (preferably 1-10 h -1 ). Preferably, in the presence of hydrogen, sulfur-containing crude gasoline is contacted with a desulfurization adsorbent for an adsorption desulfurization reaction at a volume ratio of 0.01-1000 (preferably 0.05-500) of the hydrogen donor to the gasoline raw material.

[0110] In a particularly preferred embodiment, the rich gas from the catalytic cracking fractionation column or a mixture of the rich gas and a hydrogen donor is heated to 100-500 °C (preferably 250-450 °C). The heated rich gas or the heated mixture of the rich gas and the hydrogen donor is introduced into the second fluidized bed desulfurization reactor from the bottom. The rich gas is contacted with a sulfur-filled adsorbent flowing from the top to the bottom in a countercurrent manner for an adsorption desulfurization reaction under reaction conditions including a temperature of 200-550 °C (preferably 300-500 °C), a pressure of 0.5-5 MPa (preferably 1.0-3.5 MPa), a weight hourly space velocity of 0.1-100 h -1 (preferably 1-10 h -1 ) and a volume ratio of the hydrogen donor or hydrogen to the rich gas raw material of 0.01-1000 (preferably 0.05-500).

[0111] A mixture of rich gas and / or hydrogen donor is uniformly distributed into the second fluidized bed desulfurization reactor through a supply distribution plate and sufficiently contacts with the desulfurization adsorbent in the second fluidized bed desulfurization reactor.

[0112] The sulfur-loaded adsorbent in the second fluidized bed desulfurization reactor is recycled from the bottom to the first fluidized bed desulfurization reactor after the reaction. After the sulfur-loaded adsorbent is separated from the reaction oil gas at the upper part of the first fluidized bed desulfurization reactor, the used adsorbent is stripped to remove the adsorbed hydrocarbons, then lifted and sent to the adsorbent regenerator. The regenerated desulfurization adsorbent is sent to the adsorbent reducer for reduction, and the reduced desulfurization adsorbent is sent from the bottom to the first fluidized bed desulfurization reactor for reuse, as a result, a continuous cycle of adsorption desulfurization reaction, adsorbent regeneration, adsorbent reduction and adsorption desulfurization reaction is realized.

[0113] The reaction oil gas obtained from the top of the first fluidized bed desulfurization reactor is a mixture of desulfurized crude gasoline and hydrogen, and the desulfurized rich gas is obtained from the top of the second fluidized bed desulfurization reactor.

[0114] Figure 1F is a schematic diagram of a preferred embodiment of an adsorption desulfurization unit according to the sixth type of embodiment of the present application. As shown in Figure 1F, the adsorption desulfurization unit includes a first fluidized bed desulfurization reactor 602, a reactor receiver 605, a lock hopper 613 for isolating the reaction regeneration system, a regenerator supply tank 616, and an adsorbent regenerator 619, which are communicated in sequence. The adsorbent regenerator 619 is communicated with a regenerator receiver 622, a lock hopper 613, and an adsorbent reducer 625 in sequence. The adsorbent reducer 625 communicates with the bottom of the first fluidized bed desulfurization reactor 602 to provide the desulfurization adsorbent to the reactor. The upper part of the first fluidized bed desulfurization reactor 602 communicates with the upper part of the second fluidized bed desulfurization reactor 608, and the bottom of the second fluidized bed desulfurization reactor 608 communicates with the bottom of the first fluidized bed desulfurization reactor 602.

[0115] Preheated crude gasoline and hydrogen from the catalytic cracking fractionation tower are introduced through pipeline 601 to the bottom of the first fluidized bed desulfurization reactor 602. For the desulfurization reaction, they are brought into contact with a desulfurization adsorbent in the first fluidized bed desulfurization reactor 602. The adsorbent partially filled with sulfur moves upward together with the reaction materials. At a position 50 - 90% of the height from the bottom to the top of the first fluidized bed desulfurization reactor, a part of the desulfurization adsorbent is taken out and then passed through the control of a slide valve to the upper part of the second fluidized bed desulfurization reactor, and is brought into contact with rich gas from the catalytic cracking fractionation tower or a mixture of rich gas and a hydrogen donor preheated to the required temperature introduced from the bottom to the second fluidized bed desulfurization reactor in a countercurrent manner for the adsorption desulfurization reaction.

[0116] The reacted rich gas and desulfurization adsorbent are subjected to oil-adsorbent separation in the sedimentation separation section at the top of the second fluidized bed desulfurization reactor. The separated desulfurized rich gas is sent through pipeline 609 to the next absorption stabilization unit for treatment. The separated desulfurization adsorbent flows downward and is introduced from the bottom of the second fluidized bed desulfurization reactor 608 to the lower part of the first fluidized bed desulfurization reactor 602, and is mixed with the desulfurization adsorbent entering the lower part of the first fluidized bed desulfurization reactor 602 from the adsorbent reducer 625 and the crude gasoline and hydrogen from pipeline 601 and then flows upward. The reaction oil gas and desulfurization adsorbent are subjected to gas-solid separation at the top of the first fluidized bed desulfurization reactor 602. The separated reaction oil gas, which is a mixture of desulfurized crude gasoline and hydrogen, is sent through pipeline 603 to the next product separation and stabilization system.

[0117] The separated sulfur-loaded adsorbent is sent from the first fluidized bed desulfurization reactor 602 to the reactor receiver 605 via the adsorbent transfer horizontal pipe 604. After being stripped in the reactor receiver 605, it is sent to the lock hopper 613 via the pipeline 612, purged with nitrogen, and changed from the high-pressure hydrogen environment in the lock hopper to a low-pressure inert atmosphere. The purge gas is sent to the combustion furnace via the pipeline 614 for combustion. The sulfur-loaded adsorbent is sent to the regenerator supply tank 616 via the pipeline 615, where the sulfur-loaded adsorbent is lifted by the lift gas and sent to the adsorbent regenerator 619 via the pipeline 617. The oxygen-containing gas is introduced into the adsorbent regenerator from the bottom via the pipeline 618. The used adsorbent is brought into contact with the oxygen-containing gas in the adsorbent regenerator 619 for sulfur combustion and carbon combustion. The sulfur-containing exhaust gas is separated from the adsorbent at the top of the adsorbent regenerator and sent to the sulfur production system or subjected to alkali washing via the pipeline 620 to remove SOx. The regenerated adsorbent is sent from the adsorbent regenerator to the regenerator receiver 622 via the pipeline 621, lifted by nitrogen, sent to the lock hopper 613 via the pipeline 623, stripped and purged with hydrogen, and then the regenerated adsorbent is changed to a high-pressure hydrogen environment in the lock hopper 613 and sent to the adsorbent reducer 625 via the pipeline 624 for reduction. The reduced and regenerated adsorbent is introduced into the first fluidized bed desulfurization reactor 602 via the pipeline 626, resulting in a continuous adsorption desulfurization reaction.

[0118] In the preferred embodiments of the first to sixth embodiments, the hydrogen donor is one selected from hydrogen gas, hydrogen-containing gas, and hydrogen donor reagent, or a mixture of two or more of them. Hydrogen gas represents hydrogen gas having various purities. The hydrogen-containing gas is preferably one of the dry gas produced by the method of the present application, catalytic cracking (FCC) dry gas, coking dry gas, and pyrolysis dry gas, or a mixture of two or more of them, and the hydrogen content per volume is preferably more than 20%. The hydrogen donor reagent is one selected from tetrahydronaphthalene, decahydronaphthalene, and indane, or a mixture of two or more of them.

[0119] In a preferred embodiment of the first to sixth embodiments, the adsorbent regenerator is a fluidized bed reactor. The oxygen-containing gas is introduced into the adsorbent regenerator from the bottom, and the used adsorbent filled with sulfur is contacted with the oxygen-containing gas introduced from the lower end of the regenerator for regeneration by firing under reaction conditions including a regeneration temperature of 300 to 800 ° C (preferably 350 to 600 ° C) and a regeneration pressure of 0.1 to 3.0 MPa (preferably 0.1 to 1.0 MPa). The oxygen-containing gas may be air, or may be a mixture of air or oxygen and an inert gas (such as nitrogen).

[0120] The regenerated desulfurization adsorbent taken out from the adsorbent regenerator is stripped to remove adsorbed impurities (such as adsorbed oxygen), and then lifted and sent to the adsorbent reducer.

[0121] The regenerated desulfurization adsorbent sent to the adsorbent reducer is contacted with a reducing gas and reduced under conditions including a reduction temperature of 250 to 550 ° C (preferably 300 to 450 ° C), a reduction pressure of 0.2 to 5.0 MPa (preferably 0.5 to 3.5 MPa), and a reducing gas that is hydrogen or a gas rich in hydrogen.

[0122] In a preferred embodiment of the first to sixth types of embodiments, the desulfurized rich gas is introduced into the absorption tower from the bottom after cooling. A part of the desulfurized crude gasoline or crude gasoline and stabilized gasoline is introduced into the absorption tower from the top after heat exchange and contacted with the rich gas in a countercurrent manner for mass transfer to obtain a desulfurized rich gas with a reduced component exceeding C2 (excluding C2) and a desulfurized rich gas with a reduced component below C2 (an increased component exceeding C2). The operating pressure of the absorption tower is 0.2 to 3.0 MPa (preferably 0.5 to 1.6 MPa), and the operating temperature is 20 to 100 ° C (preferably 30 to 70 ° C). The stabilized gasoline is preferably the desulfurized stabilized gasoline produced by the apparatus of the present application.

[0123] The desulfurized rich gas with components reduced beyond C2 is sent to a reabsorption column and contacted with the light cycle oil fraction from the catalytic cracking fractionation column to obtain a desulfurized dry gas product with further reduced components beyond C2. The concentrated light cycle oil fraction that has absorbed components beyond C2 is returned to the catalytic cracking fractionation column. The operating pressure of the reabsorption column is 0.1 - 3.0 MPa (preferably 0.5 - 2.5 MPa), and the operating temperature is 20 - 100 °C (preferably 30 - 70 °C). The diesel oil fraction from the catalytic cracking fractionation column is preferably light cycle oil.

[0124] The desulfurized crude gasoline with components reduced below C2 is sent to a stripping column to obtain desulfurized crude gasoline with further reduced components below C2. The overhead gas product of the stripping column is mixed with the desulfurized rich gas and then recycled to the absorption column. The operating pressure of the stripping column is 0.1 - 3.0 MPa (preferably 0.5 - 2.5 MPa), and the operating temperature is 20 - 250 °C (preferably 50 - 200 °C).

[0125] The desulfurized crude gasoline with further reduced components below C2 is sent to a stabilizer column for fractionation to obtain a desulfurized liquefied gas and a stabilized catalytic cracking gasoline product. The operating pressure of the stabilizer column is 0.1 - 3.0 MPa (preferably 0.5 - 2.5 MPa), and the operating temperature is 20 - 250 °C, (preferably 50 - 200 °C).

[0126] In the preferred embodiments of the first to sixth types of embodiments, the desulfurization adsorbent includes one or a mixture of two or more of various supported metal oxide adsorbents, supported metal oxides carrying metal promoters, and various sulfur conversion agents and sulfur adsorbents. Preferably, the desulfurization adsorbent includes an adsorbent carrier and a metal component supported on the adsorbent carrier, and the desulfurization adsorbent includes 70 to 95% by weight of the carrier and 5 to 30% by weight of the metal component based on the total weight of the desulfurization adsorbent. The adsorbent carrier may also be a mixture of zinc oxide, silica and / or alumina, and the metal component may also be one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium. The desulfurization adsorbent preferably has a form of fine spheres having an average particle diameter of 20 to 200 μm (preferably 40 to 100 μm) in order to facilitate fluidization.

[0127] FIG. 2 is a schematic diagram of a preferred embodiment of the absorption stabilization unit according to the present application. As shown in FIG. 2, the desulfurized rich gas passes through pipeline 709, and a part of the desulfurized crude gasoline or the crude gasoline and the stabilized gasoline passes through pipeline 703 and enters the absorption tower 734, where they come into contact in a countercurrent manner for mass transfer, obtaining a desulfurized rich gas with a reduced content of components exceeding C2 (excluding C2) and a desulfurized crude gasoline with a reduced content of components below C2 (an increased content of components exceeding C2). The desulfurized rich gas with a reduced content of components exceeding C2 is introduced into the reabsorption tower 736 via pipeline 731 and brought into contact with the light cycle oil from the catalytic cracking fractionation tower introduced via pipeline 729 for mass transfer, obtaining a desulfurized dry gas with a further reduced content of components exceeding C2 (discharged from the reabsorption tower via pipeline 738). The concentrated light cycle oil that has absorbed a part of the components exceeding C2 is recycled from the bottom of the reabsorption tower to the catalytic cracking fractionation tower via pipeline 742. The desulfurized crude gasoline with a reduced content of components below C2 is introduced into the desorption tower 735 via pipeline 732, and the components below C2 are further removed, and then introduced into the stabilization tower 737 via pipeline 733, where it is fractionated in the stabilization tower 737 to obtain desulfurized liquefied gas 740 and desulfurized stabilized catalytic cracking gasoline 741. The top gas product of the desorption tower 735 is taken out via pipeline 730 and sent to the absorption tower 734 together with the desulfurized rich gas from pipeline 709.

[0128] In a second aspect, the present application provides a method for producing low-sulfur light oil by catalytic cracking, comprising the following steps: i) A step of bringing a catalytic cracking raw material into contact with a catalytic cracking catalyst for a reaction under catalytic cracking conditions, preferably a step in a riser reactor; ii) A step of performing gas-solid separation on the reaction product obtained in step i) to obtain a reaction oil gas and a used catalyst; iii) A step of fractionating the reaction oil gas obtained in step ii) in a catalytic cracking fractionation tower to obtain a catalytic cracking light product, a light cycle oil, diesel oil, and an oil slurry; iv) A step of desulfurizing and separating the catalytic cracking light products according to the present application from the catalytic cracking fractionation column to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline using the desulfurization and separation method of the catalytic cracking light products; v) Optionally, a step of regenerating the used catalyst obtained in step ii) and recycling the regenerated catalyst to the riser reactor for reuse.

[0129] According to the present application, steps i), ii), and iii) can be carried out under conventional conditions using conventional raw materials, catalysts, and apparatuses, which are not strictly limited in the present application, and thus will not be described in detail herein.

[0130] In a third aspect, the present application provides a desulfurization and separation apparatus for catalytic cracking light products. The apparatus comprises an adsorption desulfurization unit and an absorption stabilization unit connected in series. The absorption stabilization unit comprises an absorption tower, a desorption tower, a reabsorption tower, and a stabilization tower connected in series. The adsorption desulfurization unit comprises a fluidized bed desulfurization reaction unit, an adsorbent regenerator, and a lock hopper connected between the fluidized bed desulfurization reaction unit and the adsorbent regenerator for performing pressure change and atmosphere conversion. The fluidized bed desulfurization reaction unit communicates with the catalytic cracking fractionation column for receiving the catalytic cracking light products from the catalytic cracking fractionation column. The oil-gas discharge port of the fluidized bed desulfurization reaction unit communicates with the absorption tower of the absorption stabilization unit, or communicates with the absorption tower of the absorption stabilization unit via a gas-liquid separation tank.

[0131] In a preferred embodiment, the adsorption desulfurization unit has the fluidized bed desulfurization reaction unit, the receiver of the reactor, the lock hopper, the regenerator feed tank, the adsorbent regenerator, and the receiver of the regenerator connected in series. The receiver of the regenerator communicates with the adsorbent reducer via the lock hopper, and the adsorbent reducer communicates with the fluidized bed desulfurization reaction unit.

[0132] In some further preferred embodiments, the fluidized bed type desulfurization reaction unit has a first fluidized bed type desulfurization reactor, an optional adsorbent transfer tank, and a second fluidized bed type desulfurization reactor communicating in sequence, and the adsorbent reducer communicates with the bottom of the first fluidized bed type desulfurization reactor and / or the second fluidized bed type desulfurization reactor.

[0133] In some further preferred embodiments, the fluidized bed type desulfurization reaction unit includes a first fluidized bed type desulfurization reactor and a second fluidized bed type desulfurization reactor. The first fluidized bed type desulfurization reactor communicates with the receiver of the reactor. The adsorbent reducer communicates with the bottom of the first fluidized bed type desulfurization reactor and / or the second fluidized bed type desulfurization reactor. The lower central part of the first fluidized bed type desulfurization reactor communicates with the bottom of the second fluidized bed type desulfurization reactor, and the upper part of the second fluidized bed type desulfurization reactor communicates with the upper part of the first fluidized bed type desulfurization reactor; More preferably, the first fluidized bed type desulfurization reactor communicates with the bottom of the second fluidized bed type desulfurization reactor at a position 20% to 60% of the height from the bottom to the top. The first fluidized bed type desulfurization reactor communicates with the top of the second fluidized bed type desulfurization reactor at a position 60% to 90% of the height from the bottom to the top. A solid-gas separation device is provided in the sedimentation part at the upper part of the first fluidized bed type desulfurization reactor. A solid-gas separation device may or may not be provided at the upper part of the second fluidized bed type desulfurization reactor.

[0134] In some further preferred embodiments, the fluidized bed type desulfurization reaction unit includes a first fluidized bed type desulfurization reactor and a second fluidized bed type desulfurization reactor. The first fluidized bed type desulfurization reactor communicates with the receiver of the reactor. The adsorbent reducer communicates with the bottom of the first fluidized bed type desulfurization reactor and / or the second fluidized bed type desulfurization reactor. The upper part of the first fluidized bed type desulfurization reactor communicates with the upper part of the second fluidized bed type desulfurization reactor, and the bottom of the second fluidized bed type desulfurization reactor communicates with the bottom of the first fluidized bed type desulfurization reactor; More preferably, the first fluidized bed type desulfurization reactor communicates with a position 50% to 90% of the height from the bottom to the top of the second fluidized bed type desulfurization reactor at a position 80% to 90% of the height from the bottom to the top.

[0135] In some preferred embodiments, the present application provides the following technical solutions.

[0136] (A1) A method for desulfurization and separation of catalytic cracking light products, the method having the following features: The overhead oil-gas fraction from the top of the catalytic cracking fractionation tower is introduced into an adsorption desulfurization reaction unit, contacted with a desulfurization adsorbent in the presence of hydrogen for desulfurization, and the resulting reaction oil gas is introduced into a gas-liquid separation tank for separation to obtain desulfurized rich gas and desulfurized crude gasoline; The desulfurized rich gas is introduced into an absorption tower from the bottom and contacted with the desulfurized crude gasoline introduced into the absorption tower from the top for absorption; The overhead stream of the absorption tower is introduced into a reabsorption tower from the bottom and contacted with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for absorption. Desulfurized dry gas is obtained from the top of the reabsorption tower, and the concentrated light cycle oil obtained at the bottom of the reabsorption tower is recycled to the catalytic cracking fractionation tower; The bottom product of the absorption tower is sent to a stabilization tower after passing through a desorption tower, fractionated in the stabilization tower, and desulfurized liquefied gas and desulfurized stabilized gasoline are obtained; The overhead gas of the desorption tower is recycled to the absorption tower.

[0137] (A2) A method for desulfurization and separation of catalytic cracking light products according to item A1, wherein the overhead oil-gas fraction of the catalytic cracking fractionation tower is introduced from the bottom of a fluidized bed desulfurization reactor, and while flowing upward, it is contacted with a desulfurization adsorbent introduced into the reactor from the bottom for desulfurization reaction, subjected to gas-solid separation at the upper part of the fluidized bed desulfurization reactor, the separated reaction oil gas is introduced into an absorption and stabilization unit, and the separated sulfur-loaded adsorbent is introduced into an adsorbent regenerator to be regenerated by calcination in the presence of an oxygen-containing gas, and the regenerated desulfurized adsorbent is recycled to the fluidized bed desulfurization reactor after reduction.

[0138] (A3) The conditions of the fluidized bed desulfurization reactor include an operating temperature of 200 - 550 °C, an absolute pressure of 0.5 - 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 - 100 h -1 and a molar ratio of hydrogen to oil of 0.01 - 5. The method for desulfurization and separation of catalytic cracking light products according to item A2.

[0139] (A4) The conditions of the fluidized bed desulfurization reactor include an operating temperature of 300 - 500 °C, an absolute pressure of 1.0 - 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 - 10 h -1 and a molar ratio of hydrogen to oil of 0.1 - 1, for the method of desulfurization and separation of the light catalytic cracking products in item A3.

[0140] (A5) The operating conditions of the adsorbent regenerator include a regeneration temperature of 300 - 800 °C and a regeneration pressure of 0.1 - 3.0 MPa, for the method of desulfurization and separation of the light catalytic cracking products in item A2.

[0141] (A6) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 - 600 °C and a regeneration pressure of 0.1 - 1.0 MPa, for the method of desulfurization and separation of the light catalytic cracking products in item A5.

[0142] (A7) The desulfurization adsorbent includes a desulfurization adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 - 95 wt%, and the content of the metal component is 5 - 30 wt%, for the method of desulfurization and separation of the catalytic cracking light products in item A1 or A2.

[0143] (A8) The operating conditions of the gas-liquid separation tank include a pressure of 0.2 - 4.0 MPa and a temperature of 20 - 300 °C; the operating conditions of the absorption tower include a pressure of 0.2 - 3.0 MPa and a temperature of 20 - 100 °C; the operating conditions of the desorption tower include a pressure of 0.1 - 3.0 MPa and a temperature of 20 - 250 °C; the operating conditions of the reabsorption tower include a pressure of 0.1 - 3.0 MPa and a temperature of 20 - 100 °C; the operating conditions of the stabilization tower include a pressure of 0.1 - 3.0 MPa and a temperature of 20 - 250 °C, for the method of desulfurization and separation of the light catalytic cracking products in item A2.

[0144] (A9) The operating conditions of the gas-liquid separation tank include a pressure of 0.5 to 3.0 MPa and a temperature of 50 to 200 °C; the operating conditions of the absorption tower include a pressure of 0.5 to 1.6 MPa and a temperature of 30 to 70 °C, the operating conditions of the desorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C; the operating conditions of the reabsorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 30 to 70 °C; the operating conditions of the stabilization tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C, a method for desulfurization and separation of the light catalytic cracking products of item A8.

[0145] (A10) The top oil-gas fraction of the catalytic cracking fractionation tower contains hydrocarbon components of C1 to C12, and its sulfur content is 30 to 50000 μg / g, a method for desulfurization and separation of the light catalytic cracking products of item A1 or A2.

[0146] (A11) A method for producing a low-sulfur light oil product by catalytic cracking, a method having the following characteristics: introducing the catalytic cracking feedstock into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation tower for fractionation to obtain a top oil-gas fraction, a light cycle oil, a diesel oil, and an oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; Introducing the top oil-gas fraction from the catalytic cracking fractionation tower into an adsorption desulfurization reaction unit and an absorption stabilization unit, and treating it using the method for desulfurization and separation of the catalytic cracking light products specified in items A1 to A10 to obtain a desulfurized dry gas, a desulfurized liquefied gas, and a desulfurized stabilized gasoline.

[0147] (A12) A separation and desulfurization device for catalytic cracking light products, comprising a catalytic cracking fractionation tower, an adsorption desulfurization unit, and an absorption stabilization unit that are connected in series in sequence; the adsorption desulfurization unit includes a fluidized bed desulfurization reactor, a lock hopper for isolating the reaction-regeneration system, and an adsorbent regenerator; the oil-gas discharge port of the fluidized bed desulfurization reactor communicates with a gas-liquid separation tank, and the absorption stabilization unit consists of an absorption tower, a desorption tower, a reabsorption tower, and a stabilization tower that are connected in series in sequence, a device.

[0148] (A13) The adsorption desulfurization unit includes a fluidized bed desulfurization reactor, a receiver of the reactor, a lock hopper for isolating the reaction-regeneration system, a regenerator supply tank, an adsorbent regenerator, and a receiver of the regenerator, which are connected in series. The receiver of the regenerator communicates with the adsorbent reducer through the lock hopper, and the adsorbent reducer communicates with the bottom of the fluidized bed desulfurization regenerator. The desulfurization device for the catalytic cracking light product of item A12.

[0149] (B1) A method for desulfurization and separation of catalytic cracking light products, including the following steps: (1) Introduce crude gasoline from the bottom into the fluidized bed desulfurization reactor from the catalytic cracking fractionation tower, and while flowing upward, contact it with the desulfurization adsorbent in the presence of hydrogen for desulfurization. At a position 30-80% of the height of the fluidized bed desulfurization reactor, introduce rich gas from the bottom to the top, mix it with the reaction stream, then contact it with the desulfurization adsorbent for reaction, introduce the reaction oil gas obtained by gas-liquid separation into the gas-liquid separation tank for separation to obtain desulfurized rich gas and desulfurized crude gasoline. Burn the sulfur-loaded adsorbent in the adsorbent regenerator for regeneration, and recycle the regenerated desulfurization adsorbent to the fluidized bed desulfurization reactor for reuse after reduction. (2) Introduce the desulfurized rich gas from the bottom into the absorption tower, contact it with the desulfurized crude gasoline introduced from the top of the absorption tower for absorption, introduce the top stream of the absorption tower from the bottom into the reabsorption tower, contact it with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for absorption, and obtain desulfurized dry gas from the top of the reabsorption tower. Recycle the concentrated light cycle oil obtained at the bottom of the reabsorption tower to the catalytic cracking fractionation tower, send the bottom product of the absorption tower to the stabilization tower after passing through the desorption tower, fractionate it in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and recycle the top gas of the desorption tower to the absorption tower.

[0150] (B2) The method for desulfurization and separation of light catalytic cracking products of item B1, where rich gas is introduced into the fluidized bed desulfurization reactor at a position 40-70% of the height from the bottom.

[0151] (B3) The conditions of the fluidized bed desulfurization reactor include an operating temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 -1, and a molar ratio of hydrogen to oil of 0.01 to 5. A method for desulfurization and separation of the light catalytic cracking products of item B1 or B2.

[0152] (B4) The conditions of the fluidized bed desulfurization reactor include an operating temperature of 300 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 10 h -1 -1, and a molar ratio of hydrogen to oil of 0.1 to 1. A method for desulfurization and separation of the light catalytic cracking products of item B3.

[0153] (B5) The sulfur-filled adsorbent is regenerated by reacting with an oxygen-containing gas in an adsorbent regenerator under conditions including a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa. A method for desulfurization and separation of the light catalytic cracking products of item B1 or B2.

[0154] (B6) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 to 600 °C and a regeneration pressure of 0.1 to 1.0 MPa. A method for desulfurization and separation of the light catalytic cracking products of item B5.

[0155] (B7) The desulfurization adsorbent includes a desulfurization adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 to 95 wt%, and the content of the metal component is 5 to 30 wt%. A method for desulfurization and separation of the catalytic cracking light products of item B1.

[0156] (B8) The operating conditions of the gas-liquid separation tank include an operating pressure of 0.2 to 4.0 MPa and an operating temperature of 20 to 300 °C; the operating conditions of the absorption tower include an operating pressure of 0.2 to 3.0 MPa and an operating temperature of 20 to 100 °C; the operating conditions of the desorption tower include an operating pressure of 0.1 to 3.0 MPa and an operating temperature of 20 to 250 °C; the operating conditions of the reabsorption tower include an operating pressure of 0.1 to 3.0 MPa and an operating temperature of 20 to 100 °C; the operating conditions of the stabilization tower include an operating pressure of 0.1 to 3.0 MPa and an operating temperature of 20 to 250 °C, a method for desulfurization and separation of the light catalytic cracking products of item B1.

[0157] (B9) The operating conditions of the gas-liquid separation tank include an operating pressure of 0.5 to 3.0 MPa and an operating temperature of 50 to 200 °C; the operating conditions of the absorption tower include an operating pressure of 0.5 to 1.6 MPa and an operating temperature of 30 to 70 °C; the operating conditions of the desorption tower include an operating pressure of 0.5 to 2.5 MPa and an operating temperature of 50 to 200 °C; the operating conditions of the reabsorption tower include an operating pressure of 0.5 to 2.5 MPa and an operating temperature of 30 to 70 °C; the operating conditions of the stabilization tower include an operating pressure of 0.5 to 2.5 MPa and an operating temperature of 50 to 200 °C, a method for desulfurization and separation of the light catalytic cracking products of item B8.

[0158] (B10) The sulfur content in the rich gas and crude gasoline from the catalytic cracking unit is more than 30 μg / g, preferably more than 50 μg / g, a method for desulfurization and separation of the light products derived from catalytic cracking of item B1.

[0159] (B11) A method for producing a low-sulfur light oil product by catalytic cracking, a method having the following characteristics: introducing a catalytic cracking raw material into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation tower for fractionation to obtain rich gas, crude gasoline, light cycle oil, diesel oil, and oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; By the desulfurization and separation method of the catalytic cracking light product specified in Items B1 to B10, the rich gas and the crude gasoline in the catalytic cracking fractionation tower are desulfurized and separated to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0160] (C1) A desulfurization method for a catalytic cracking light product, comprising the following steps: (1) Introduce the crude gasoline from the catalytic cracking fractionation tower from the bottom into the first desulfurization reactor, contact it with a desulfurization adsorbent in the presence of hydrogen for desulfurization, subject the resulting product to gas-solid separation in the upper sedimentation area, introduce the separated desulfurization adsorbent partially filled with sulfur into the second desulfurization reactor, and use the separated reaction oil gas as desulfurized crude gasoline. (2) Introduce the rich gas from the catalytic cracking fractionation tower from the bottom of the second desulfurization reactor, contact it with the desulfurization adsorbent for desulfurization while flowing upward, subject the resulting product to gas-solid separation in the upper sedimentation area, use the reaction oil gas obtained by separation as desulfurized rich gas, pass the separated sulfur-filled adsorbent through an adsorbent regenerator to regenerate it by calcination in the presence of an oxygen-containing gas, and recycle the regenerated desulfurized adsorbent to the bottom of the first desulfurization reactor after reduction. (3) Send the desulfurized rich gas and the desulfurized crude gasoline separately to an absorption and stabilization unit for separation to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0161] (C2) In step (3), introduce the desulfurized rich gas from the bottom into the absorption tower, contact it with the desulfurized crude gasoline introduced from the top of the absorption tower for absorption, introduce the top stream of the absorption tower from the bottom of the reabsorption tower, contact it with the light cycle oil from the catalytic cracking fractionator in a countercurrent manner for absorption, obtain desulfurized dry gas from the top of the reabsorption tower, recycle the concentrated light cycle oil obtained at the bottom of the reabsorption tower to the catalytic cracking fractionator, pass the bottom product of the absorption tower through a desorption tower and then send it to a stabilization tower, fractionate it in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and recycle the top gas of the desorption tower to the absorption tower. The desulfurization method of the catalytic cracking light product of item C1.

[0162] (C3) The conditions of the first desulfurization reactor include an operating temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 , and a molar ratio of hydrogen to oil of 0.01 to 1000, for the desulfurization method of the light catalytic cracking products of item C1 or C2.

[0163] (C4) The conditions of the first desulfurization reactor include an operating temperature of 300 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 10 h -1 , and a molar ratio of hydrogen to oil of 0.05 to 500, for the desulfurization method of the light catalytic cracking products of item C3.

[0164] (C5) The conditions of the second desulfurization reactor include an operating temperature of 300 to 550 °C, an absolute pressure of 0.1 to 3 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 100 h -1 , and a molar ratio of hydrogen to oil of 0.01 to 500, for the desulfurization method of the catalytic cracking light products of item C1 or C2.

[0165] (C6) The conditions of the second desulfurization reactor include an operating temperature of 350 to 500 °C, an absolute pressure of 0.2 to 2.5 MPa, a weight hourly space velocity of the oil gas raw material of 2 to 20 h -1 , and a molar ratio of hydrogen to oil of 0.05 to 300, and the operating pressure of the second desulfurization reactor is 0.5 to 2.0 MPa lower than that of the first desulfurization reactor, for the desulfurization method of the light catalytic cracking products of item C5.

[0166] (C7) The operating conditions of the adsorbent regenerator include a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa, for the desulfurization method of the catalytic cracking light products of item C1 or C2.

[0167] (C8) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 to 600 °C and a regeneration pressure of 0.1 to 1.0 MPa, for the desulfurization method of the catalytic cracking light products of item C7.

[0168] (C9) The desulfurization adsorbent contains an adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 to 95% by weight, and the content of the metal component is 5 to 30% by weight. The adsorbent carrier is a mixture of zinc oxide, silica and / or alumina, and the metal component is one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium. A desulfurization method for catalytic cracking light products of any of items C1 to C8.

[0169] (C10) The operating conditions of the absorption tower include a pressure of 0.2 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the desorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C; the operating conditions of the reabsorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stabilization tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C. A desulfurization method for catalytic cracking light products of item C2.

[0170] (C11) The operating conditions of the absorption tower include a pressure of 0.5 to 1.6 MPa and a temperature of 30 to 70 °C; the operating conditions of the desorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C; the operating conditions of the reabsorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 30 to 70 °C; the operating conditions of the stabilization tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C. A desulfurization method for catalytic cracking light products of item C10.

[0171] (C12) A method for producing a low-sulfur light oil product by catalytic cracking, the method having the following characteristics: introducing a catalytic cracking feedstock into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation tower for fractionation to obtain rich gas, crude gasoline, light cycle oil, diesel oil and oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; The crude gasoline and rich gas from the catalytic cracking fractionation column are respectively introduced into the first desulfurization reactor and the second desulfurization reactor of the adsorption desulfurization reaction unit, and are subjected to adsorption desulfurization and absorption stabilization separation using the desulfurization method for catalytic cracking light products specified in Items C1 to C11 to obtain desulfurized dry gas, desulfurized liquefied gas, and stabilized gasoline.

[0172] (C13) A separation and desulfurization device for catalytic cracking light products, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series; the adsorption desulfurization unit comprising a first desulfurization reactor, an adsorption transfer tank, a second desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feed tank, an adsorbent regenerator, and a regenerator receiver connected in series; the regenerator receiver communicating with a reducer via a lock hopper, the reducer communicating with the bottom of the first desulfurization reactor, and the absorption stabilization unit comprising an absorption tower, a desorption tower, a reabsorption tower, and a stabilization tower connected in series.

[0173] (D1) A desulfurization and separation method for catalytic cracking light products, having the following characteristics: introducing the crude gasoline and hydrogen donor from the catalytic cracking fractionation column into the bottom of the first desulfurization reactor and contacting with a desulfurization adsorbent for desulfurization while flowing upward; introducing the desulfurization adsorbent partially filled with sulfur, obtained by gas-solid separation at the top of the reactor, into the second desulfurization reactor; introducing the rich gas and hydrogen donor from the catalytic cracking fractionation column into the bottom of the second desulfurization reactor, contacting with the desulfurization adsorbent for desulfurization, and recycling the reaction oil gas separated from the desulfurization adsorbent after the reaction to the first desulfurization reactor. In the first desulfurization reactor, the reaction oil gas obtained by gas-solid separation is separated into desulfurized rich gas and desulfurized crude gasoline. The desulfurized rich gas is introduced from the bottom into the absorption tower and brought into contact with the desulfurized crude gasoline introduced from the top of the absorption tower for absorption. The top stream of the absorption tower is introduced from the bottom into the reabsorption tower and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for absorption. The desulfurized dry gas is obtained at the top of the reabsorption tower, and the concentrated light cycle oil obtained at the bottom of the reabsorption tower is recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower is sent to the stabilization tower after passing through the desorption tower, fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and the top gas of the desorption tower is recycled to the absorption tower.

[0174] (D2) A method for desulfurization and separation of light catalytic cracking products according to item D1, wherein a mixture of reaction oil gas and desulfurization adsorbent is subjected to gas-solid separation at the top of a second desulfurization reactor, and the sulfur-filled adsorbent obtained by separation is regenerated by calcination in the presence of an oxygen-containing gas, and the regenerated desulfurization adsorbent is recycled to the fluidized bed desulfurization reactor after reduction.

[0175] (D3) The conditions of the first desulfurization reactor include an operating temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 and a molar ratio of hydrogen to oil of 0.01 to 1000. A method for desulfurization and separation of light catalytic cracking products according to item D1 or D2.

[0176] (D4) The conditions of the first desulfurization reactor include an operating temperature of 300 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 10 h -1 and a hydrogen-oil molar ratio of 0.05 to 500. A method for desulfurization and separation of light catalytic cracking products according to item D3.

[0177] (D5) The conditions of the second desulfurization reactor include an operating temperature of 300 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of 1 to 100 h -1A method for desulfurization and separation of light catalytic cracking products of item D1 or D2, including the weight hourly space velocity of the oil gas raw material and the molar ratio of hydrogen to oil of 0.01 to 500.

[0178] (D6) The conditions of the second desulfurization reactor include an operating temperature of 350 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, and a weight hourly space velocity of the oil gas raw material of 2 to 20 h -1 A method for desulfurization and separation of light catalytic cracking products of item D5, including the weight hourly space velocity of the oil gas raw material and the hydrogen-oil molar ratio of 0.05 to 300.

[0179] (D7) The operating conditions of the adsorbent regenerator include a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa, for a method for desulfurization and separation of light catalytic cracking products of item D1 or D2.

[0180] (D8) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 to 600 °C and a regeneration pressure of 0.1 to 1.0 MPa, for a method for desulfurization and separation of light catalytic cracking products of item D7.

[0181] (D9) The desulfurization adsorbent includes an adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 to 95 wt%, and the content of the metal component is 5 to 30 wt%. The adsorbent carrier is a mixture of zinc oxide, silica and / or alumina, and the metal component is one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium, for a method for desulfurization and separation of any catalytic cracking light products of items D1 to D8.

[0182] (D10) The operating conditions of the absorption tower include a pressure of 0.2 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the desorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C; the operating conditions of the reabsorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stabilization tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C, for a method for desulfurization of catalytic cracking light products of item D1 or D2.

[0183] (D11) The operating conditions of the absorption tower include a pressure of 0.5 to 1.6 MPa and a temperature of 30 to 70 °C; the operating conditions of the desorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C; the operating conditions of the re-absorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 30 to 70 °C; the operating conditions of the stabilization tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C, which is a method for desulfurizing the catalytic cracking light product of item D10.

[0184] (D12) A method for producing a low-sulfur light oil product by catalytic cracking, the method having the following characteristics: introducing the catalytic cracking feedstock into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation tower for fractionation to obtain rich gas, crude gasoline, light cycle oil, diesel oil, and oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; Introducing the crude gasoline and rich gas from the catalytic cracking fractionation tower into the first desulfurization reactor and the second desulfurization reactor of the adsorption desulfurization reaction unit respectively, and subjecting them to adsorption desulfurization and absorption stabilization separation using the desulfurization and separation method of the catalytic cracking light product specified in items D1 to D11 to obtain desulfurized dry gas, desulfurized liquefied gas, and stabilized gasoline.

[0185] (D13) A separation and desulfurization device for catalytic cracking light products, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series in sequence; the adsorption desulfurization unit comprises a first desulfurization reactor, a second desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feed tank, an adsorbent regenerator, and a regenerator receiver connected in series in sequence; the regenerator receiver is continuously connected to the lock hopper and the adsorbent reducer, the adsorbent reducer is connected to the bottom of the first desulfurization reactor, and the absorption stabilization unit comprises an absorption tower, a desorption tower, a re-absorption tower, and a stabilization tower connected in series in sequence.

[0186] (E1) A method for desulfurizing catalytic cracking light products, the method comprising the following steps: (1) Introduce the crude gasoline from the catalytic cracking fractionation column into the first desulfurization reactor from the bottom, flow it upward, and contact it with the desulfurization adsorbent for desulfurization. Under the control of the slide valve, introduce a part of the desulfurization adsorbent into the second desulfurization reactor, contact it with the catalytic cracking rich gas preheated to the temperature required for the desulfurization reaction, recycle the reaction rich gas and the desulfurization adsorbent to the first desulfurization reactor, and perform gas-solid separation in the sedimentation area at the upper part of the first desulfurization reactor; (2) Regenerate the separated used desulfurization adsorbent by calcining it in the presence of an oxygen-containing gas in the adsorbent regenerator, and recycle the regenerated desulfurization adsorbent to the bottom of the first desulfurization reactor for reuse after reduction; (3) Separate the separated reaction oil gas in a gas-liquid separation tank to obtain desulfurized rich gas and desulfurized crude gasoline, send them separately to the absorption and stabilization system for further separation, and obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0187] (E2) Provide a sedimentation area and a gas-solid separator at the upper part of the second desulfurization reactor, subject the reaction oil gas and the desulfurization adsorbent in the second desulfurization reactor to gas-solid separation, directly send the separated reaction oil gas to the absorption and stabilization system for further separation, and return the desulfurization adsorbent to the first desulfurization reactor. The desulfurization method for catalytic cracking light products in item E1.

[0188] (E3) Introduce the desulfurized rich gas into the absorption tower from the bottom, contact it with the desulfurized crude gasoline introduced into the absorption tower from the top for absorption, introduce the top stream of the absorption tower into the reabsorption tower from the bottom, contact it with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for absorption, obtain the desulfurized dry gas from the top of the reabsorption tower, recycle the concentrated light cycle oil from the bottom of the reabsorption tower to the catalytic cracking fractionation column, send the bottom product of the absorption tower to the stabilization tower after passing through the desorption tower, fractionate it in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and recycle the top gas of the desorption tower to the absorption tower. The desulfurization method for catalytic cracking light products in item E1 or E2.

[0189] (E4) The conditions of the first desulfurization reactor include an operating temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, and is a desulfurization method for the catalytic cracking light product of item E1 or E2.

[0190] (E5) The conditions of the first desulfurization reactor include an operating temperature of 300 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 10 h -1 -1, and a hydrogen-oil molar ratio of 0.05 to 500, and is a desulfurization method for the light catalytic cracking product of item E4.

[0191] (E6) The conditions of the second desulfurization reactor include an operating temperature of 250 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, and is a desulfurization method for the catalytic cracking light product of item E1 or E2.

[0192] (E7) The conditions of the second desulfurization reactor include an operating temperature of 350 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 20 h -1 -1, and a hydrogen-oil molar ratio of 0.05 to 300, and is a desulfurization method for the light catalytic cracking product of item E6.

[0193] (E8) The operating conditions of the adsorbent regenerator include a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa, and is a desulfurization method for the catalytic cracking light product of item E1 or E2.

[0194] (E9) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 to 600 °C and a regeneration pressure of 0.1 to 1.0 MPa, and is a desulfurization method for the catalytic cracking light product of item E8.

[0195] (E10) The desulfurization adsorbent contains an adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 to 95% by weight, and the content of the metal component is 5 to 30% by weight. The adsorbent carrier is a mixture of zinc oxide, silica and / or alumina, and the metal component is one or more selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin and vanadium. A desulfurization method for catalytic cracking light products of any of items E1 to E9.

[0196] (E11) The operating conditions of the absorption tower include a pressure of 0.2 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the desorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C; the operating conditions of the reabsorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stabilization tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C. A desulfurization method for catalytic cracking light products of item E3.

[0197] (E12) The operating conditions of the absorption tower include a pressure of 0.5 to 1.6 MPa and a temperature of 30 to 70 °C; the operating conditions of the desorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C; the operating conditions of the reabsorption tower include a pressure of 0.5 to 2.5 MPa and a temperature of 30 to 70 °C; the operating conditions of the stabilization tower include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C. A desulfurization method for catalytic cracking light products of item E11.

[0198] (E13) A method for producing a low-sulfur light oil product by catalytic cracking, the method having the following features: introducing a catalytic cracking feedstock into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation tower for fractionation to obtain rich gas, crude gasoline, light cycle oil, diesel oil and oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; The crude gasoline and rich gas from the catalytic cracking fractionation tower are respectively introduced into the first desulfurization reactor and the second desulfurization reactor, and are subjected to adsorption desulfurization and absorption stabilization separation using the methods specified in Items E1 to E12 to obtain desulfurized dry gas, desulfurized liquefied gas, and stabilized gasoline.

[0199] (E14) A catalytic cracking light product separation and desulfurization device, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series; the adsorption desulfurization unit comprises a first desulfurization reactor, a reactor receiver, a lock hopper, a regenerator feed tank, an adsorbent regenerator, and a regenerator receiver connected in series; the regenerator receiver communicates with an adsorbent reducer through a lock hopper, the adsorbent reducer communicates with the bottom of the first desulfurization reactor, the central lower part of the first desulfurization reactor communicates with the second desulfurization reactor, and the top of the second desulfurization reactor communicates with the upper part of the first desulfurization reactor. The absorption stabilization unit consists of an absorption tower, a stripping tower, a reabsorption tower, and a stabilization tower connected in series.

[0200] (E15) The first desulfurization reactor communicates with the bottom of the second desulfurization reactor at a position 20 - 60% of the height from the bottom to the top, the first desulfurization reactor communicates with the top of the second desulfurization reactor at a position 60 - 90% of the height from the bottom to the top. A gas-solid separation device is provided in the sedimentation area at the upper part of the first desulfurization reactor, and a gas-solid separation device is provided or not provided at the upper part of the second desulfurization reactor. The catalytic cracking light product separation and desulfurization device of Item E14.

[0201] (F1) A method for desulfurizing catalytic cracking light products, comprising the following steps: (1) Introduce the crude gasoline from the catalytic cracking fractionation tower into the first desulfurization reactor from the bottom, and while flowing upward, contact it with a desulfurization adsorbent in the presence of hydrogen. Subject the reaction oil gas and the desulfurization adsorbent to gas-solid separation in the sedimentation area at the upper part of the first desulfurization reactor. Introduce a part of the sulfur-loaded adsorbent from the top of the adsorbent bed layer into the upper part of the second desulfurization reactor through a slide valve, regenerate another part of the sulfur-loaded adsorbent by calcination in an adsorbent regenerator, and recycle the regenerated desulfurized adsorbent to the bottom of the first desulfurization reactor for reuse after reduction. (2) Introduce the rich gas from the catalytic cracking fractionation column into the second desulfurization reactor from the bottom, contact it with the desulfurization adsorbent in a countercurrent manner for the adsorption desulfurization reaction, and recycle the desulfurization adsorbent from the bottom of the second desulfurization reactor to the first desulfurization reactor after the reaction; (3) Send the crude desulfurized gasoline obtained from the top of the first desulfurization reactor and the desulfurized rich gas obtained from the top of the second desulfurization reactor separately to the absorption and stabilization unit, and further separate them to obtain desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline.

[0202] (F2) Introduce the desulfurized rich gas into the absorption column from the bottom, contact it with the crude desulfurized gasoline introduced into the absorption column from the top for absorption, introduce the top stream of the absorption column into the reabsorption column from the bottom, contact it with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for absorption, obtain the desulfurized dry gas from the top of the reabsorption column, recycle the concentrated light cycle oil obtained at the bottom of the reabsorption column to the catalytic cracking fractionation column, send the bottom product of the absorption column to the stabilization column after passing through the desorption column, fractionate in the stabilization column to obtain desulfurized liquefied gas and desulfurized stabilized gasoline, and recycle the top gas of the desorption column to the absorption column. The desulfurization method for catalytic cracking light products of item F1.

[0203] (F3) The supply gas velocity of the first desulfurization reactor is 0.25 - 10 m / s, the supply gas velocity of the second desulfurization reactor is 0.05 - 1.5 m / s, and the first desulfurization reactor and the second desulfurization reactor are fluidized bed reactors. The desulfurization and separation method for catalytic cracking light products of item F1 or F2.

[0204] (F4) The conditions of the first desulfurization reactor include an operating temperature of 200 - 550 °C, an absolute pressure of 0.5 - 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 - 100 h -1 and a molar ratio of hydrogen to oil of 0.01 - 1000. The desulfurization method for catalytic cracking light products of item F1 or F2.

[0205] (F5) The conditions of the first desulfurization reactor include an operating temperature of 300 - 500 °C, an absolute pressure of 1.0 - 3.5 MPa, 1 - 10 h -1A method for desulfurizing light catalytic cracking products of item F4, including the weight hourly space velocity of the oil gas raw material and the molar ratio of hydrogen to oil of 0.05 to 500.

[0206] (F6) The conditions of the second desulfurization reactor include an operating temperature of 300 to 550 °C, an absolute pressure of 0.5 to 5 MPa, and a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h -1 A method for desulfurizing catalytic cracking light products of item F1 or F2, including the weight hourly space velocity of the oil gas raw material and the molar ratio of hydrogen to oil of 0.01 to 500.

[0207] (F7) The conditions of the second desulfurization reactor include an operating temperature of 350 to 500 °C, an absolute pressure of 1.0 to 3.5 MPa, and a weight hourly space velocity of the oil gas raw material of 1 to 20 h -1 A method for desulfurizing light catalytic cracking products of item F6, including the weight hourly space velocity of the oil gas raw material and the molar ratio of hydrogen to oil of 0.05 to 300.

[0208] (F8) The operating conditions of the adsorbent regenerator include a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa, for a method for desulfurizing catalytic cracking light products of item F1 or F2.

[0209] (F9) The operating conditions of the adsorbent regenerator include a regeneration temperature of 350 to 600 °C and a regeneration pressure of 0.1 to 1.0 MPa, for a method for desulfurizing catalytic cracking light products of item F8.

[0210] (F10) The desulfurization adsorbent includes a desulfurization adsorbent carrier and a metal component supported on the adsorbent carrier. With respect to the total weight of the desulfurization adsorbent, the content of the desulfurization adsorbent carrier is 70 to 95 wt%, and the content of the metal component is 5 to 30 wt%. A method for desulfurizing catalytic cracking light products of any one of items F1 to F9.

[0211] (F11) The operating conditions of the absorption column include a pressure of 0.2 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the desorption column include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C; the operating conditions of the re-absorption column include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stabilization column include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C, a method for desulfurizing the catalytic cracking light products of item F2.

[0212] (F12) The operating conditions of the absorption column include a pressure of 0.5 to 1.6 MPa and a temperature of 30 to 70 °C; the operating conditions of the desorption column include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C; the operating conditions of the re-absorption column include a pressure of 0.5 to 2.5 MPa and a temperature of 30 to 70 °C; the operating conditions of the stabilization column include a pressure of 0.5 to 2.5 MPa and a temperature of 50 to 200 °C, a method for desulfurizing the catalytic cracking light products of item F11.

[0213] (F13) A method for producing a low-sulfur light oil product by catalytic cracking, a method having the following characteristics: introducing the catalytic cracking raw material into a riser reactor, contacting it with a catalytic cracking catalyst for reaction under catalytic cracking conditions, and subjecting it to gas-solid separation at the top of the riser reactor; introducing the obtained reaction oil gas into a catalytic cracking fractionation column for fractionation to obtain rich gas, crude gasoline, light cycle oil, diesel oil, and oil slurry; regenerating the separated catalytic cracking catalyst and then recycling it to the riser reactor for reuse; Introduce the crude gasoline and rich gas into the first desulfurization reactor and the second desulfurization reactor respectively, and use the desulfurization method of the catalytic cracking light products specified in items F1 to F12 for adsorption desulfurization and absorption stabilization separation to obtain desulfurized dry gas, desulfurized liquefied gas, and stabilized gasoline.

[0214] (F14)A desulfurization device for catalytic cracking light products, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series; the adsorption desulfurization unit comprises a first desulfurization reactor, a receiver of the reactor, a lock hopper, a regenerator feed tank, and an adsorbent regenerator connected in series; the adsorbent regenerator is continuously connected to the receiver of the regenerator, the lock hopper, the adsorbent reducer, and the bottom of the first desulfurization reactor, the upper part of the first desulfurization reactor is connected to the upper part of the second desulfurization reactor, and the bottom of the second desulfurization reactor is connected to the bottom of the first desulfurization reactor; the absorption stabilization unit comprises an absorption tower, a desorption tower, a reabsorption tower, and a stabilization tower connected in series.

[0215] (F15)The desulfurization device for catalytic cracking light products according to item F14, wherein the first desulfurization reactor communicates with a position from 80% to 90% of the height from the bottom to the top of the second fluidized bed desulfurization reactor at a position from 50% to 90% of the height from the bottom to the top.

[0216] 〔Example〕 The following examples are provided to further illustrate the present application and are not intended to be limited to any aspect. The raw material rich gas and crude gasoline used in the examples were obtained from the catalytic cracking unit of the Yanshan Division of China Petroleum & Chemical Corporation. The desulfurization adsorbent is available under the trade name FCAS from the Nanjing Catalyst Branch of China Petroleum & Chemical Corporation. The desulfurization adsorbent contains zinc oxide, silica, and alumina as carriers and Ni as a promoter, and its properties are listed in Table 1.

[0217]

Table 1

[0218] In each of the examples and comparative examples, the sulfur content in the dry gas and the liquefied gas was analyzed by GC-SCD using an Agilent GC-7890A gas chromatograph. The sulfur content in gasoline was analyzed using a ZSX100X fluorescence spectrometer manufactured by Rigaku Corporation. The hydrocarbon compositions of the dry gas, the liquefied gas, and gasoline were analyzed and measured by gas chromatography.

[0219] The calculation methods for the ethylene saturation rate, the propylene saturation rate, and the olefin saturation rate in gasoline are as follows. In Comparative Example 2 and some of the examples, the mass fraction of ethylene in the dry gas, the mass fraction of propylene in the liquefied gas, and the mass fraction of olefins in gasoline obtained after adsorption desulfurization and absorption stabilization separation are determined based on the mass content of ethylene in the dry gas, the mass content of propylene in the liquefied gas, and the mass content of olefins in gasoline that have not been desulfurized in Comparative Example 1. Then, the mass percentage of the difference between the reference value and the value measured after desulfurization is taken as the saturation rate of the corresponding olefin.

[0220] Ethylene saturation rate = ((mass fraction of ethylene in Comparative Example 1 - mass fraction of ethylene after desulfurization) / mass fraction of ethylene in Comparative Example 1) × 100% Propylene saturation rate = ((mass fraction of propylene in Comparative Example 1 - mass fraction of propylene after desulfurization) / mass fraction of propylene in Comparative Example 1) × 100% Gasoline olefin saturation rate = ((mass fraction of olefins in gasoline in Comparative Example 1 - mass fraction of olefins in gasoline after desulfurization) / mass fraction of olefins in gasoline in Comparative Example 1) × 100%.

[0221] (Comparative Example 1) Taking the cracking unit of the Yangshan Business Department as an example, the rich gas and crude gasoline produced by the cracking fractionation tower were separately introduced into the absorption and stabilization unit of the cracking unit. The rich gas was introduced into the absorption tower from the bottom and brought into contact with the crude gasoline introduced into the absorption tower from the top for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the cracking fractionation tower in a countercurrent manner for mass transfer. Dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the cracking fractionation tower. The bottom product of the absorption tower was sent to the stabilization tower after passing through the desorption tower and fractionated in the stabilization tower to obtain liquefied gas and stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower.

[0222] The properties of the obtained non-desulfurized dry gas, liquefied gas and stabilized gasoline are shown in Table 2.

[0223] (Comparative Example 2) Using the stabilized gasoline obtained in Comparative Example 1 as a raw material, it was introduced into a gasoline fluidized bed desulfurization reactor and brought into contact with a desulfurization adsorbent for the adsorption desulfurization reaction. The reaction oil gas and sulfur-loaded adsorbent at the top of the adsorption desulfurization reactor were subjected to gas-solid separation. The separated reaction oil gas was cooled to obtain desulfurized stabilized gasoline. The separated sulfur-loaded adsorbent was introduced into an adsorbent regenerator and regenerated by reaction and calcination under regeneration conditions in the presence of an oxygen-containing gas. The regenerated desulfurization adsorbent was introduced into an adsorbent reducer and reacted with a reducing gas under reducing conditions to obtain a reduced desulfurization adsorbent, which was recycled to the adsorption desulfurization reactor for reuse.

[0224] The desulfurization adsorbent used was FCAS, and its properties are shown in Table 1. The adsorption desulfurization reaction was carried out under reaction conditions including a reaction temperature of 400 °C, a reaction pressure of 2.0 MPa, a weight hourly space velocity of 5 h -1 and a volume ratio of hydrogen to oil of 45, and the results are shown in Table 2. The sulfur content of the desulfurized stabilized gasoline was 2.6 ppm, the octane number loss was 0.8 units, and the yield of the refined gasoline decreased by 0.6%.

[0225]

Table 2

[0226] (Example I-1) The effect of adsorption desulfurization on the total overhead light fraction of the catalytic cracking fractionation column was evaluated in a small fixed fluidized bed reactor.

[0227] A mixture of rich gas and crude gasoline from the catalytic cracking fractionation column was used as the raw material, first introduced into the adsorption desulfurization reaction unit for desulfurization, and then introduced into the absorption stabilization unit for separation. The process flow of the adsorption desulfurization unit shown in Figure 1A was adopted, and a mixture of rich gas and crude gasoline was introduced from the bottom into the fluidized bed desulfurization reactor. In the presence of FCAS as the desulfurization adsorbent, the reaction temperature was 400 °C, the reaction pressure was 2.0 MPa, and the reaction time was 5 h -1It was reacted under reaction conditions including the weight hourly space velocity and the volume ratio of hydrogen to oil of 45. After separating the oil gas obtained after the reaction from the desulfurization adsorbent, it was passed through a gas-liquid separation tank for cooling and separation to obtain desulfurized rich gas and desulfurized crude gasoline. The process flow of the absorption stabilization unit shown in Figure 2 was adopted, and the desulfurized rich gas separated from the gas-liquid separation tank was introduced from the bottom into the absorption tower. The pressure at the top of the absorption tower was 1.405 MPa, the temperature at the top of the absorption tower was 34.5 °C, and the temperature at the bottom of the absorption tower was 43.3 °C. The desulfurized crude gasoline separated from the gas-liquid separation tank was introduced from the top into the absorption tower and brought into contact with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced from the bottom into the reabsorption tower and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.370 MPa, the temperature at the top of the reabsorption tower was 34.3 °C, and the temperature at the bottom of the reabsorption tower was 41.8 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in a desorption tower. The pressure at the top of the desorption tower was 1.477 MPa, the temperature at the top of the desorption tower was 76.5 °C, and the temperature at the bottom of the desorption tower was 131.9 °C. The bottom product of the desorption tower was sent to a stabilization tower. The pressure at the top of the stabilization tower was 0.889 MPa, the temperature at the top of the stabilization tower was 57.8 °C, and the temperature at the bottom of the stabilization tower was 167.6 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table 1-3.

[0228] (Example I-2) The experiment was carried out with the reaction oil gas and the desulfurization adsorbent in a fluidized bed desulfurization reactor at a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, and 8 h -1Under reaction conditions including the weight hourly space velocity and the volume ratio of hydrogen to oil of 100, it was contacted and reacted. The oil gas was separated from the desulfurization adsorbent after the reaction, cooled and separated in a gas-liquid separation tank to obtain desulfurized rich gas and desulfurized crude gasoline. Except for this, a mixture of rich gas and crude gasoline obtained from the catalytic cracking fractionation column was used as a raw material, and the same reaction procedure and desulfurization adsorbent as in Example I-1 were used. The rich gas separated from the gas-liquid separation tank was introduced into the absorption column from the bottom. The pressure at the top of the absorption column was 1.432 MPa, the temperature at the top of the absorption column was 33.8 °C, and the temperature at the bottom of the absorption column was 45.6 °C. The crude gasoline separated from the gas-liquid separation tank was introduced into the absorption column from the top and contacted with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption column was introduced into the reabsorption column from the bottom and contacted with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption column was 1.395 MPa, the temperature at the top of the reabsorption column was 35.9 °C, and the temperature at the bottom of the reabsorption column was 45.1 °C. The desulfurized dry gas was obtained at the top of the reabsorption column. The concentrated light cycle oil obtained at the bottom of the reabsorption column was recycled to the catalytic cracking fractionation column. The bottom product of the absorption column was desorbed in a desorption column. The pressure at the top of the desorption column was 1.562 MPa, the temperature at the top of the desorption column was 80.9 °C, and the temperature at the bottom of the desorption column was 143.5 °C. The bottom product of the desorption column was sent to a stabilization column. The pressure at the top of the stabilization column was 0.912 MPa, the temperature at the top of the stabilization column was 59.8 °C, and the temperature at the bottom of the stabilization column was 172.3 °C. The bottom product was fractionated in the stabilization column to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorption column was recycled to the absorption column. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas and desulfurized stabilized gasoline are shown in Table I-3.

[0229]

Table 3

[0230] As can be seen from the results in Table I-3, the method for desulfurization and separation of the catalytic cracking light products according to the present application can simultaneously achieve desulfurization of dry gas and liquefied gas. The yields of dry gas and liquefied gas increase by 0.1% respectively, the yield of stabilized gasoline increases by 0.4 - 0.5%, the sulfur content of stabilized gasoline decreases, and the octane number loss decreases.

[0231] (Example II-1) Example II-1 shows the effect of simultaneously adsorbing and desulfurizing rich gas and crude gasoline. Using the rich gas and crude gasoline from the catalytic cracking fractionation column as raw materials, they were first introduced into the adsorption desulfurization reaction unit for desulfurization according to the process flow shown in Figure 1B, and then introduced into the absorption stabilization unit for separation according to the process flow shown in Figure 2. The crude gasoline from the catalytic cracking fractionation column was introduced from the bottom into the fluidized bed desulfurization reactor. In the presence of FCAS as the desulfurization adsorbent, at a reaction temperature of 400 °C, a reaction pressure of 2.0 MPa, and for 5 h -1It was reacted under reaction conditions including the weight hourly space velocity and a volume ratio of hydrogen to oil of 45. The rich gas from the catalytic cracking fractionation column was introduced into a fluidized bed desulfurization reactor at a position 60% of the height from the bottom to the top, and the height of the desulfurization adsorbent bed layer through which the rich gas passed was controlled to be 20% of the total height of the adsorbent bed layer in the reactor. The sulfur-containing rich gas was mixed with the reaction oil gas and the desulfurization adsorbent for the adsorptive desulfurization reaction. The reacted oil gas was introduced into a gas-liquid separation tank for cooling and separation, and desulfurized rich gas and desulfurized crude gasoline were obtained. The rich gas separated from the gas-liquid separation tank was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.758 MPa, the temperature at the top of the absorption tower was 43.6 °C, and the temperature at the bottom of the absorption tower was 52.7 °C. The crude gasoline separated from the gas-liquid separation tank was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.632 MPa, the temperature at the top of the reabsorption tower was 42.5 °C, and the temperature at the bottom of the reabsorption tower was 54.1 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation column, and the bottom product of the absorption tower was desorbed in a desorption tower. The pressure at the top of the desorption tower was 1.853 MPa, the temperature at the top of the desorption tower was 84.9 °C, and the temperature at the bottom of the desorption tower was 156.8 °C. The bottom product of the absorption tower was sent to a stabilization tower. The pressure at the top of the stabilization tower was 1.056 MPa, the temperature at the top of the stabilization tower was 63.8 °C, and the temperature at the bottom of the stabilization tower was 174.5 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower.

[0232] The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized gasoline are shown in Table II-3.

[0233] (Example II-2) The reaction temperature in the fluidized bed desulfurization reactor was 430 °C, the reaction pressure was 1.4 MPa, and the weight hourly space velocity was 8 h -1With the volume ratio of hydrogen to oil set at 100, the rich gas was preheated to 430 °C and introduced at the position 40% of the height from the bottom to the top in the fluidized bed desulfurization reactor. The adsorption bed through which the rich gas passed was controlled to be 30% of the total height of the adsorbent bed in the reactor. Except for this, an experiment was conducted using the rich gas and crude gasoline from the catalytic cracking fractionation tower as raw materials as described in Example II-1. The oil gas obtained after the reaction was cooled and separated in a gas-liquid separation tank to obtain desulfurized rich gas and desulfurized crude gasoline. The desulfurized rich gas was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.772 MPa, the temperature at the top of the absorption tower was 42.3 °C, and the temperature at the bottom of the absorption tower was 49.8 °C. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.598 MPa, the temperature at the top of the reabsorption tower was 43.5 °C, and the temperature at the bottom of the reabsorption tower was 47.6 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in a desorption tower. The pressure at the top of the desorption tower was 1.918 MPa, the temperature at the top of the desorption tower was 85.3 °C, and the temperature at the bottom of the desorption tower was 155.2 °C. The bottom product of the desorption tower was sent to a stabilization tower. The pressure at the top of the stabilization tower was 0.919 MPa, the temperature at the top of the stabilization tower was 59.5 °C, and the temperature at the bottom of the stabilization tower was 169.7 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower.

[0234] The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table II-3.

[0235]

Table 4

[0236] As can be seen from the results in Table II-3, the method for desulfurization and separation of the catalytic cracking light products according to the present application can simultaneously achieve desulfurization of dry gas and liquefied gas. The yields of dry gas and liquefied gas each increase by 0.1%, the yield of stabilized gasoline increases by 0.4 - 0.5%, the sulfur content of stabilized gasoline decreases, and the octane number loss decreases.

[0237] (Example III-1) The process flow of the adsorption desulfurization unit shown in Fig. 1C was adopted. The first fluidized bed desulfurization reactor was a fixed fluidized bed reactor. The desulfurization adsorbent was introduced into the first fluidized bed desulfurization reactor from the bottom. The crude gasoline and hydrogen from the catalytic cracking fractionation column were introduced into the bottom of the first fluidized bed desulfurization reactor tower and brought into contact with the desulfurization adsorbent for adsorption desulfurization. The reaction was carried out under reaction conditions including a reaction temperature of 400°C, a reaction pressure of 2.2 MPa, a weight hourly space velocity of 5h -1 and a volume ratio of hydrogen to oil of 45. After the reaction, a mixture of desulfurized crude gasoline and hydrogen was obtained. The second fluidized bed desulfurization reactor was a fixed fluidized bed reactor. The desulfurization adsorbent from the first fluidized bed desulfurization reactor was introduced into the bottom of the second fluidized bed desulfurization reactor through the adsorbent transfer tank. The rich gas from the catalytic cracking fractionation column was preheated to 400°C and introduced into the second fluidized bed reactor. The reaction temperature was 400°C, the reaction pressure was 1.0 MPa, and the weight hourly space velocity was 10h -1As a result, a desulfurized rich gas was obtained after the reaction. The desulfurized rich gas was introduced into the absorption column from the bottom, and the desulfurized crude gasoline was introduced into the absorption column from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The pressure at the top of the absorption column was 1.214 MPa, the temperature at the top of the absorption column was 30.1 °C, and the temperature at the bottom of the absorption column was 50.6 °C. The overhead stream of the absorption column was introduced into the reabsorption column from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation column in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption column was 1.158 MPa, the temperature at the top of the reabsorption column was 32.3 °C, and the temperature at the bottom of the reabsorption column was 48.9 °C. The desulfurized dry gas was obtained at the top of the reabsorption column. The concentrated light cycle oil obtained at the bottom of the reabsorption column was recycled to the catalytic cracking fractionation column. The bottom product of the absorption column was desorbed in the desorption column. The pressure at the top of the desorption column was 1.582 MPa, the temperature at the top of the desorption column was 68.4 °C, and the temperature at the bottom of the desorption column was 159.6 °C. The bottom product of the desorption column was sent to the stabilization column. The pressure at the top of the stabilization column was 1.025 MPa, the temperature at the top of the stabilization column was 68.9 °C, and the temperature at the bottom of the stabilization column was 178.3 °C. The bottom product was fractionated in the stabilization column to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The overhead gas of the desorption column was recycled to the absorption column. The results are shown in Table III-3.

[0238] (Example III-2) The first fluidized bed desulfurization reactor was operated under the same reaction scheme, raw materials, and desulfurization adsorbent as in Example III-1, except that the reaction conditions included a reaction temperature of 440 °C, a reaction pressure of 1.4 MPa, a weight hourly space velocity of 8 h -1 and a volume ratio of hydrogen to oil of 100, to obtain desulfurized crude gasoline. The reaction conditions of the second fluidized bed desulfurization reactor were a reaction temperature of 430 °C, a reaction pressure of 0.5 MPa, and a weight hourly space velocity of 12 h -1The weight hourly space velocity was included, and a desulfurized rich gas was obtained. The desulfurized rich gas was introduced into the absorption tower from the bottom. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The pressure at the top of the absorption tower was 1.255 MPa, the temperature at the top of the absorption tower was 40.5 °C, and the temperature at the bottom of the absorption tower was 50.2 °C. The overhead stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.189 MPa, the temperature at the top of the reabsorption tower was 41.8 °C, and the temperature at the bottom of the reabsorption tower was 48.6 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower, and the concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.251 MPa, the temperature at the top of the desorption tower was 56.2 °C, and the temperature at the bottom of the desorption tower was 118.9 °C. The bottom product was introduced into the stabilizer tower. The pressure at the top of the stabilizer tower was 0.812 MPa, the temperature at the top of the stabilizer tower was 53.1 °C, and the temperature at the bottom of the stabilizer was 159.8 °C. The bottom product was fractionated in the stabilizer tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The overhead gas of the desorption tower was recycled to the absorption tower. The results are shown in Table III-3.

[0239]

Table 5

[0240] As can be seen from Table III-3, the method for desulfurizing the catalytic cracking light products according to the present application can simultaneously achieve desulfurization of dry gas and liquefied gas. The yield of liquefied gas increases by 0.1%, the saturation rate of light olefins is low, and the yield of stabilized gasoline increases by 0.4 - 0.5%. The olefin saturation rate of stabilized gasoline decreases by 3 - 6%, and the research octane number (RON) loss value is smaller.

[0241] (Example IV-1) The sulfur-containing rich gas and the crude gasoline from the catalytic cracking fractionation column were processed using the process flow of the adsorption desulfurization unit shown in Fig. 1D. The desulfurization adsorbent from the adsorbent reducer was introduced into the bottom of the first fluidized bed desulfurization reactor. Using the sulfur-containing crude gasoline as a raw material, it was introduced into the bottom of the first fluidized bed desulfurization reactor, and the reaction was carried out under reaction conditions including a reaction temperature of 380 °C, a reaction pressure of 2.0 MPa, a weight hourly space velocity of 5 h -1 -1, and a volume ratio of hydrogen to oil of 60. The sulfur-containing rich gas was introduced into the bottom of the second fluidized bed desulfurization reactor and brought into contact with the desulfurization adsorbent from the first fluidized bed desulfurization reactor, which was reacted with the crude gasoline for the desulfurization reaction. The reaction temperature was 420 °C, the reaction pressure was 2.0 MPa, and the weight hourly space velocity was 5 h -1It was. The desulfurized rich gas was separated from the desulfurization adsorbent and returned to the first fluidized bed desulfurization reactor. The mixed desulfurized crude gasoline and rich gas product were further separated from the adsorbent in the first fluidized bed desulfurization reactor and passed through an absorption stabilization unit. The process flow of the absorption stabilization unit is shown in Figure 2, and the desulfurized rich gas was introduced from the bottom of the absorption tower. The pressure at the top of the absorption tower was 1.447 MPa, the temperature at the top of the absorption tower was 38.5 °C, and the temperature at the bottom of the absorption tower was 44.6 °C. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.394 MPa, the temperature at the top of the reabsorption tower was 36.8 °C, and the temperature at the bottom of the reabsorption tower was 45.4 °C. Desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in a desorption tower. The pressure at the top of the desorption tower was 1.536 MPa, the temperature at the top of the desorption tower was 78.9 °C, and the temperature at the bottom of the desorption tower was 137.5 °C. The bottom product of the desorption tower was sent to a stabilization tower. The pressure at the top of the stabilization tower was 0.872 MPa, the temperature at the top of the stabilization tower was 55.3 °C, and the temperature at the bottom of the stabilization tower was 160.7 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquid treatment gas and desulfurized stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table IV-3.

[0242] (Example IV-2) The process flows of the adsorption desulfurization unit and the absorption stabilization unit shown in Figures 1D and 2 were adopted. The desulfurization adsorbent from the adsorbent reducer was introduced into the first fluidized bed desulfurization reactor from the bottom. The sulfur-containing crude gasoline raw material was introduced into the first fluidized bed desulfurization reactor from the bottom, with a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, and 8 h -1It was reacted under reaction conditions including the weight hourly space velocity and the volume ratio of hydrogen to oil of 100. The sulfur-containing rich gas was introduced from the bottom into the second fluidized bed desulfurization reactor and contacted with the desulfurization adsorbent from the first fluidized bed desulfurization reactor and reacted with the crude gasoline for the desulfurization reaction. The reaction temperature was 445 °C, the reaction pressure was 1.4 MPa, and the weight hourly space velocity was 12 h -1 The desulfurized rich gas was separated from the desulfurization adsorbent and returned to the first fluidized bed desulfurization reactor. The mixed desulfurized crude gasoline and rich gas product were further separated from the adsorbent in the first fluidized bed desulfurization reactor and sent to the absorption stabilization unit. The desulfurized rich gas was introduced from the bottom into the absorption tower. The pressure at the top of the absorption tower was 1.658 MPa, the temperature at the top of the absorption tower was 45.1 °C, and the temperature at the bottom of the absorption tower was 52.6 °C. The desulfurized crude gasoline was introduced from the top into the absorption tower and contacted with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced from the bottom into the reabsorption tower and contacted with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.556 MPa, the temperature at the top of the reabsorption tower was 38.9 °C, and the temperature at the bottom of the reabsorption tower was 45.7 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower, the concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower, and the bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.728 MPa, the temperature at the top of the desorption tower was 80.9 °C, and the temperature at the bottom of the desorption tower was 142.5 °C. The bottom product of the desorption tower was sent to the stabilization tower. The pressure at the top of the stabilization tower was 0.806 MPa, the temperature at the top of the stabilization tower was 55.4 °C, and the temperature at the bottom of the stabilization tower was 159.7 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorber was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table IV-3.

[0243]

Table 6

[0244] The results in Table IV-3 show that the desulfurization and separation method of the catalytic cracking light products according to this application can simultaneously achieve the desulfurization of dry gas and liquefied gas, the yield of liquefied gas increases by 0.1%, the yield of stabilized gasoline increases by 0.4 - 0.6%, the sulfur content of stabilized gasoline decreases, the olefin saturation rate in gasoline decreases, and the octane number loss decreases.

[0245] (Example V-1) The process flow of the adsorption desulfurization unit shown in Figure 1Ea was adopted. The first fluidized bed desulfurization reactor and the second fluidized bed desulfurization reactor were used as fixed fluidized bed reactors. The desulfurization adsorbent was introduced into the first fluidized bed desulfurization reactor from the bottom. The crude gasoline and hydrogen from the catalytic cracking fractionation column were introduced into the first fluidized bed desulfurization reactor from the bottom, contacted with the desulfurization adsorbent for adsorption desulfurization, and reacted under conditions including a reaction temperature of 410 °C, a reaction pressure of 2.3 MPa, a weight hourly space velocity of 5 h -1 and a volume ratio of hydrogen to oil of 40. A part of the sulfur-loaded adsorbent was introduced into the second fluidized bed desulfurization reactor at a position 20% of the height from the bottom to the top of the first fluidized bed desulfurization reactor. The rich gas from the catalytic cracking fractionation column was introduced into the second fluidized bed desulfurization reactor from the bottom and contacted with the desulfurization adsorbent for adsorption desulfurization. The desulfurization reaction was carried out under conditions including a reaction temperature of 430 °C, a reaction pressure of 2.3 MPa, and a weight hourly space velocity of 8 h -1 . The reacted rich gas and desulfurization adsorbent were returned to the first fluidized bed desulfurization reactor at a position 70% of the height from the bottom to the top. The reaction oil gas and the desulfurization adsorbent were separated in the first reactor. The reaction oil gas was separated in a gas-liquid separation tank, and desulfurized rich gas and desulfurized crude gasoline components were obtained. The operating conditions of the gas-liquid separation tank included a pressure of 1.926 MPa and a temperature of 86 °C.

[0246] The process flow of the absorption stabilization unit is shown in Figure 2. The desulfurized rich gas was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.853 MPa, the temperature at the top of the absorption tower was 55.6 °C, and the temperature at the bottom of the absorption tower was 68.2 °C. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The overhead stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.730 MPa, the temperature at the top of the reabsorption tower was 51.2 °C, and the temperature at the bottom of the reabsorption tower was 62.8 °C. The desulfurized dry gas was obtained at the top of the reabsorber. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.890 MPa, the temperature at the top of the desorption tower was 88.5 °C, and the temperature at the bottom of the desorption tower was 162.7 °C. The bottom product of the absorption tower was sent to the stabilization tower. The pressure at the top of the stabilization tower was 1.251 MPa, the temperature at the top of the stabilization tower was 68.7 °C, and the temperature at the bottom of the stabilization tower was 189.6 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The overhead gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas and desulfurized stabilized gasoline are shown in Table V-3.

[0247] (Example V-2) The first fluidized bed desulfurization reactor was operated at a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, a weight hourly space velocity of 8 h -1 and a volume ratio of hydrogen to oil of 100, using the same desulfurization adsorbent and reaction scheme as in Example V-1. A part of the sulfur-loaded adsorbent was introduced into the second fluidized bed desulfurization reactor at a position 50% of the height from the bottom to the top of the first fluidized bed desulfurization reactor. In the second fluidized bed desulfurization reactor, the desulfurization reaction was carried out under conditions including a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, and a weight hourly space velocity of 12 h -1 . The reaction rich gas and the desulfurization adsorbent were returned to the first fluidized bed desulfurization reactor at a position 90% of the height from the bottom to the top.

[0248] The pressure at the top of the absorption tower was 1.806 MPa, the temperature at the top of the absorption tower was 55.2 °C, and the temperature at the bottom of the absorption tower was 67.5 °C. The pressure at the top of the re - absorption tower was 1.711 MPa, the temperature at the top of the re - absorption tower was 50.5 °C, and the temperature at the bottom of the re - absorption tower was 62.1 °C. The desulfurized dry gas was obtained at the top of the re - absorption tower. The pressure at the top of the desorption tower was 1.838 MPa, the temperature at the top of the desorption tower was 85.1 °C, and the temperature at the bottom of the desorption tower was 160.4 °C. The bottom product of the desorption tower was sent to the stabilization tower. The pressure at the top of the stabilization tower was 1.202 MPa, the temperature at the top of the stabilization tower was 65.3 °C, and the temperature at the bottom of the stabilization tower was 185.2 °C. After fractionation in the stabilization tower, desulfurized liquefied gas and desulfurized stabilized gasoline were obtained. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table V - 3.

[0249] (Example V - 3) The process flow of the adsorption desulfurization unit shown in Fig. 1Eb was adopted. Except for including a reaction temperature of 380 °C, a reaction pressure of 2.5 MPa, a weight hourly space velocity of 7 h -1 and a volume ratio of hydrogen to oil of 60 in the operating conditions of the first fluidized - bed desulfurization reactor, experiments were carried out using the same desulfurization adsorbent and reaction scheme as in Example V - 1. A part of the sulfur - loaded adsorbent was introduced into the second fluidized - bed desulfurization reactor at a position 60% of the height from the bottom to the top of the first fluidized - bed desulfurization reactor. The operating conditions of the second fluidized - bed desulfurization reactor included a reaction temperature of 445 °C, a reaction pressure of 1.0 MPa, and a weight hourly space velocity of 5 h -1 . The reaction rich gas and the desulfurization adsorbent were separated in the second fluidized - bed desulfurization reactor. The desulfurized rich gas was sent to the absorption and stabilization system. The desulfurization adsorbent was recycled to a position 90% of the height from the bottom to the top of the first fluidized - bed desulfurization reactor. The desulfurized crude gasoline was separated from the adsorbent in the first reactor.

[0250] The desulfurized rich gas was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.453 MPa, the temperature at the top of the absorption tower was 33.6 °C, and the temperature at the bottom of the absorption tower was 45.1 °C. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The overhead stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.389 MPa, the temperature at the top of the reabsorption tower was 35.6 °C, and the temperature at the bottom of the reabsorption tower was 45.7 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.623 MPa, the temperature at the top of the desorption tower was 63.9 °C, and the temperature at the bottom of the desorption tower was 145.4 °C. The bottom product of the desorption tower was sent to the stabilizer tower. The pressure at the top of the stabilizer tower was 0.935 MPa, the temperature at the top of the stabilizer tower was 52.4 °C, and the temperature at the bottom of the stabilizer tower was 173.1 °C. The bottom product was fractionated in the stabilizer tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The overhead gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table V-3.

[0251] (Example V-4) Except for including a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, a weight hourly space velocity of 8 h -1 per hour, and a volume ratio of hydrogen to oil of 200 in the operating conditions of the first fluidized bed desulfurization reactor, experiments were carried out using the same desulfurization adsorbent and reaction scheme as in Example V-3. A part of the sulfur-loaded adsorbent was introduced into the second fluidized bed desulfurization reactor at a position 30% of the height from the bottom to the top of the first fluidized bed desulfurization reactor. The operating conditions of the second fluidized bed desulfurization reactor included a reaction temperature of 380 °C, a reaction pressure of 0.5 MPa, and a weight hourly space velocity of 1 h -1 per hour. The reaction rich gas and the desulfurization adsorbent were separated in the second fluidized bed desulfurization reactor. The desulfurized rich gas was sent to the absorption and stabilization system. The desulfurization adsorbent was recycled to a position 80% of the height from the bottom to the top of the first fluidized bed desulfurization reactor.

[0252] The pressure at the top of the absorption tower was 1.286 MPa, the temperature at the top of the absorption tower was 30.5 °C, and the temperature at the bottom of the absorption tower was 40.2 °C. The pressure at the top of the re - absorption tower was 1.175 MPa, the temperature at the top of the re - absorption tower was 31.8 °C, and the temperature at the bottom of the re - absorption tower was 41.4 °C. Desulfurized dry gas was obtained at the top of the re - absorption tower. The pressure at the top of the desorption tower was 1.539 MPa, the temperature at the top of the desorption tower was 58.6 °C, and the temperature at the bottom of the desorption tower was 137.8 °C. The bottom product was sent to the stabilization tower. The pressure at the top of the stabilization tower was 0.783 MPa, the temperature at the top of the stabilization tower was 45.1 °C, and the temperature at the bottom of the stabilization tower was 153.3 °C. By fractionation in the stabilization tower, desulfurized liquefied gas and stabilized gasoline were obtained. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table V - 3.

[0253]

Table 7

[0254] As can be seen from Table V - 3, the method for desulfurizing the catalytic cracking light products according to the present application can simultaneously achieve desulfurization of dry gas and liquefied gas. The yield of liquefied gas increased by 0.1%, the saturation rate of light olefins was low, the yield of stabilized gasoline increased by 0.4 - 0.5%, the olefin saturation rate of stabilized gasoline decreased by 1.8 - 5%, and the research octane number (RON) loss value was smaller.

[0255] (Example VI - 1) Rich gas and crude gasoline from the catalytic cracking fractionation column were used as raw materials, first introduced into the adsorption desulfurization reaction unit for desulfurization, and then introduced into the absorption stabilization unit for separation. The process flow of the adsorption desulfurization unit is shown in Figure 1F, and the process flow of the absorption stabilization unit is shown in Figure 2. The first fluidized bed desulfurization reactor was a small fixed fluidized bed reactor, the second fluidized bed desulfurization reactor was a countercurrent reactor, and the desulfurization adsorbent was FCAS. The desulfurization adsorbent from the reducer was introduced into the first fluidized bed desulfurization reactor from the bottom, and the crude gasoline and hydrogen from the catalytic cracking fractionation column were introduced into the first fluidized bed desulfurization reactor from the bottom and brought into contact with the desulfurization adsorbent for adsorption desulfurization. After the reaction, the reaction oil gas and the desulfurization adsorbent were separated to obtain a mixture of desulfurized crude gasoline and hydrogen. A part of the desulfurization adsorbent at the top of the adsorbent bed was introduced into the receiving tower of the reactor, and the other part was introduced into the upper part of the second fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicated with the position at 90% of the height from the bottom to the top of the second fluidized bed desulfurization reactor at the position at 80% of the height from the bottom to the top of the first fluidized bed desulfurization reactor. The rich gas from the catalytic cracking fractionation column was introduced into the second fluidized bed desulfurization reactor from the bottom, brought into contact with the desulfurization adsorbent in a countercurrent manner for mass transfer, and separated at the upper part of the second fluidized bed desulfurization reactor to obtain desulfurized rich gas. The operating conditions of the first fluidized bed desulfurization reactor included a reaction temperature of 400 °C, a reaction pressure of 1.8 MPa, a weight hourly space velocity of 7 h -1 and a volume ratio of hydrogen to oil of 75. The operating conditions of the second fluidized bed desulfurization reactor included a reaction temperature of 430 °C, a reaction pressure of 2.0 MPa, and 10 h -1It included the weight hourly space velocity. The desulfurized rich gas was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.428 MPa, the temperature at the top of the absorption tower was 30.6 °C, and the temperature at the bottom of the absorption tower was 45.1 °C. The desulfurized crude gasoline was introduced into the absorption tower from the top and brought into contact with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and brought into contact with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.220 MPa, the temperature at the top of the reabsorption tower was 31.2 °C, and the temperature at the bottom of the reabsorption tower was 56.3 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.621 MPa, the temperature at the top of the desorption tower was 85.1 °C, and the temperature at the bottom of the desorption tower was 153.6 °C. The bottom product of the desorption tower was sent to the stabilization tower. The pressure at the top of the stabilization tower was 0.901 MPa, the temperature at the top of the stabilization tower was 62.1 °C, and the temperature at the bottom of the stabilization tower was 143.2 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline are shown in Table VI-3.

[0256] (Example VI-2) The first fluidized bed desulfurization reactor was operated under reaction conditions including a reaction temperature of 430 °C, a reaction pressure of 1.4 MPa, a weight hourly space velocity of 8 h -1 except that the experiment was carried out using the same reaction scheme and desulfurization adsorbent as in Example VI-1. The rich gas from the catalytic cracking fractionation tower was preheated to 430 °C and then introduced into the second fluidized bed desulfurization reactor, with a reaction temperature of 445 °C, a reaction pressure of 0.5 MPa, and a weight hourly space velocity of 12 h -1Reaction was carried out under reaction conditions including , and crude desulfurized gasoline and hydrogen were obtained in the first fluidized bed desulfurization reactor, and rich desulfurized gas was obtained in the second fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicated with the position at 80% of the height from the bottom to the top of the second fluidized bed desulfurization reactor at the position of 60% of the height from its bottom to the top. The rich desulfurized gas was introduced into the absorption tower from the bottom. The pressure at the top of the absorption tower was 1.425 MPa, the temperature at the top of the absorption tower was 31.6 °C, and the temperature at the bottom of the absorption tower was 42.1 °C. The crude desulfurized gasoline was introduced into the absorption tower from the top and contacted with the rich gas in a countercurrent manner for mass transfer. The top stream of the absorption tower was introduced into the reabsorption tower from the bottom and contacted with the light cycle oil from the catalytic cracking fractionation tower in a countercurrent manner for mass transfer. The pressure at the top of the reabsorption tower was 1.119 MPa, the temperature at the top of the reabsorption tower was 33.6 °C, and the temperature at the bottom of the reabsorption tower was 46.5 °C. The desulfurized dry gas was obtained at the top of the reabsorption tower. The concentrated light cycle oil obtained at the bottom of the reabsorption tower was recycled to the catalytic cracking fractionation tower. The bottom product of the absorption tower was desorbed in the desorption tower. The pressure at the top of the desorption tower was 1.521 MPa, the temperature at the top of the desorption tower was 71.6 °C, and the temperature at the bottom of the desorption tower was 138.4 °C. The bottom product of the desorption tower was sent to the stabilization tower. The pressure at the top of the stabilization tower was 0.786 MPa, the temperature at the top of the stabilization tower was 61.3 °C, and the temperature at the bottom of the stabilization tower was 140.6 °C. The bottom product was fractionated in the stabilization tower to obtain desulfurized liquefied gas and desulfurized stabilized gasoline. The top gas of the desorption tower was recycled to the absorption tower. The properties of the obtained desulfurized dry gas, desulfurized liquefied gas and desulfurized stabilized gasoline are shown in Table VI-3.

[0257]

Table 8

[0258] As can be seen from the results in Table VI-3, the method of this application can simultaneously achieve desulfurization of gasoline, dry gas and liquefied gas. The yield of liquefied gas increases by 0.1%, and the saturation rates of ethylene and propylene are lower. The yield of stabilized gasoline increases by 0.4 - 0.5%, the olefin saturation rate in gasoline decreases, and the octane number loss decreases.

[0259] Although the present application has been described in detail above with reference to preferred embodiments, it is not intended to be limited to these embodiments. Various modifications are possible in accordance with the inventive concept of the present application, and these modifications are within the scope of the present application.

[0260] In addition, the various technical features described in the above embodiments may be appropriately combined without contradiction. To avoid unnecessary repetition, various possible combinations are not described in the present application, but such combinations are also included in the scope of the present application.

[0261] Also, various embodiments of the present application can be arbitrarily combined as long as they do not deviate from the gist of the present application, and such combined embodiments should be regarded as the disclosure of the present application.

Brief Description of the Drawings

[0262]

Figure 1A

Figure 1B

Figure 1C

Figure 1D

Figure 1Ea

Figure 1Eb

Figure 1F

Figure 2

Claims

1. A method for desulfurization and separation of catalytic cracking light products, comprising: 1) contacting the catalytic cracking light products with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, performing gas-liquid separation on the obtained desulfurized products to obtain a desulfurized rich gas and desulfurized crude gasoline, wherein the catalytic cracking light products are the overhead oil-gas fraction from the catalytic cracking fractionation tower, or contacting the catalytic cracking light products with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization to obtain a desulfurized rich gas and desulfurized crude gasoline, wherein the catalytic cracking light products are the rich gas and crude gasoline from the catalytic cracking fractionation tower, and 2) separately sending the desulfurized rich gas and desulfurized crude gasoline obtained in step 1) to a catalytic cracking absorption stabilization system for separation to obtain a desulfurized dry gas, desulfurized liquefied gas, and desulfurized stabilized gasoline, wherein the catalytic cracking absorption stabilization system comprises an absorption tower, a reabsorption tower, a stripping tower, and a stabilization tower, step 2) comprises: 2a) introducing the desulfurized rich gas into the absorption tower from the bottom and contacting it with the desulfurized crude gasoline introduced into the absorption tower from the top in a countercurrent manner for mass transfer to obtain an overhead stream and a bottom product; 2b) introducing the overhead stream of the absorption tower into the reabsorption tower from the bottom and contacting it with the light cycle oil from the catalytic cracking fractionation tower introduced into the reabsorption tower from the top in a countercurrent manner for mass transfer to obtain the desulfurized dry gas at the top of the reabsorption tower and concentrated light cycle oil at the bottom of the reabsorption tower, and recycling the concentrated light cycle oil to the catalytic cracking fractionation tower; 2c) stripping the bottom product of the absorption tower in the stripping tower to obtain a top gas and a bottom product, and recycling the top gas to the absorption tower; 2d) sending the bottom product of the stripping tower to the stabilization tower, fractionating in the stabilization tower to obtain the desulfurized liquefied gas and the desulfurized stabilized gasoline, further comprising: the operating conditions of the absorption tower include a pressure of 0.2 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stripping tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C; the operating conditions of the reabsorption tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 100 °C; the operating conditions of the stabilization tower include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C.

2. The catalytic cracking light product is the overhead oil-gas fraction from the catalytic cracking fractionation column, and the step 1) is 1a) introducing the overhead oil-gas fraction from the catalytic cracking fractionation column into a fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) performing gas-solid separation on the reaction stream obtained at the upper part of the fluidized bed desulfurization reactor to obtain a reaction oil gas and a sulfur-loaded adsorbent; 1c) performing gas-liquid separation on the reaction oil gas obtained in the step 1b) to obtain the desulfurized rich gas and the desulfurized crude gasoline, where the operating conditions of the gas-liquid separation are a pressure of 0.2 to 4.0 MPa and a temperature of 20 to 300 °C; 1d) sending the sulfur-loaded adsorbent obtained in the step 1b) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurized adsorbent to the fluidized bed desulfurization reactor after reduction; further comprising The overhead oil-gas fraction of the catalytic cracking fractionation column contains hydrocarbon components of C1 to C12 and has a sulfur content of 30 to 50,000 μg / g. The method according to claim 1.

3. The catalytic cracking light product is the rich gas and the crude gasoline from the catalytic cracking fractionation column, and the step 1) is 1a) introducing the crude gasoline from the catalytic cracking fractionation column into a fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) introducing the rich gas from the catalytic cracking fractionation column into the fluidized bed desulfurization reactor at a position 30 to 80% of the height from the bottom to the top, and mixing it with the flow in the reactor for a desulfurization reaction; 1c) performing gas-solid separation on the reaction stream obtained at the upper part of the fluidized bed desulfurization reactor to obtain a reaction oil gas and a sulfur-loaded adsorbent; 1d) performing gas-liquid separation on the reaction oil gas obtained in the step 1c) to obtain the desulfurized rich gas and the desulfurized crude gasoline, where the operating conditions of the gas-liquid separation include a pressure of 0.2 to 4.0 MPa and a temperature of 20 to 300 °C; 1e) sending the sulfur-loaded adsorbent obtained in the step 1c) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurized adsorbent to the fluidized bed desulfurization reactor after reduction; ​ further comprising The method according to claim 1, wherein the sulfur content in the rich gas and the crude gasoline from the catalytic cracking fractionation column is independently greater than 30 μg / g. **Claim 4** The operating conditions of the fluidized bed desulfurization reactor include a temperature of 200 to 550°C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 5, according to the method of claim 2 or 3. **Claim 5** The catalytic cracking light product is rich gas and crude gasoline from the catalytic cracking fractionation column, and step 1) is 1a) introducing the crude gasoline from the catalytic cracking fractionation column into a first fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain the desulfurized crude gasoline and a desulfurization adsorbent partially filled with sulfur, and sending the desulfurization adsorbent partially filled with sulfur to a second fluidized bed desulfurization reactor; 1c) introducing the rich gas from the catalytic cracking fractionation column into the second fluidized bed desulfurization reactor from the bottom, and contacting it with the desulfurization adsorbent partially filled with sulfur introduced from the bottom of the reactor for a desulfurization reaction; 1d) performing gas-solid separation on the reaction stream obtained at the upper part of the second fluidized bed desulfurization reactor to obtain the desulfurized rich gas and a sulfur-filled adsorbent; 1e) sending the sulfur-filled adsorbent obtained in step 1d) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction; The method according to claim 1, further comprising **Claim 6** The operating conditions of the first fluidized bed desulfurization reactor include a temperature of 200 to 550°C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas feedstock oil of 0.1 to 100 h －１ , and a molar ratio of hydrogen to oil of 0.01 to 1000, The operating conditions of the second fluidized bed type desulfurization reactor include a temperature of 300 to 550 °C, an absolute pressure of 0.1 to 3 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 500, The method according to claim 5, wherein the operating temperature of the second fluidized bed desulfurization reactor is 0.5 to 2.0 MPa lower than the operating temperature of the first fluidized bed desulfurization reactor. **Claim 7** The catalytic cracking light product is rich gas and crude gasoline from the catalytic cracking fractionation column, and step 1) is 1a) introducing the crude gasoline from the catalytic cracking fractionation column into a first fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain a first reaction oil gas and a desulfurization adsorbent partially filled with sulfur, and sending the desulfurization adsorbent partially filled with sulfur to a second fluidized bed desulfurization reactor; 1c) introducing the rich gas from the catalytic cracking fractionation column into the second fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent partially filled with sulfur introduced into the reactor from the bottom for the desulfurization reaction; 1d) performing gas-solid separation on the reaction stream obtained at the upper part of the second fluidized bed desulfurization reactor to obtain a second reaction oil gas and a sulfur-filled adsorbent, and recycling the second reaction oil gas to the first fluidized bed desulfurization reactor; 1e) performing gas-liquid separation on the first reaction oil gas obtained in step 1b) to obtain the desulfurized rich gas and the desulfurized crude gasoline; 1f) sending the sulfur-filled adsorbent obtained in step 1d) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the fluidized bed desulfurization reactor after reduction; The method according to claim 1, further comprising.

8. The operating conditions of the first fluidized bed desulfurization reactor include a temperature of 200 to 550°C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, The operating conditions of the second fluidized bed type desulfurization reactor include a temperature of 300 to 550°C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 500, The method according to claim 7.

9. The catalytic cracking light product is a rich gas and a crude gasoline from the catalytic cracking fractionation column, and step 1) is 1a) introducing the crude gasoline from the catalytic cracking fractionation column into the first fluidized bed desulfurization reactor from the bottom, and contacting it with a desulfurization adsorbent introduced into the reactor from the bottom in the presence of hydrogen for the desulfurization reaction; 1b) taking out a part of the desulfurization adsorbent from the lower central part of the first fluidized bed desulfurization reactor, passing it through the bottom of the second fluidized bed desulfurization reactor, contacting it with the rich gas from the catalytic cracking fractionation column introduced into the reactor from the bottom for the desulfurization reaction, and recycling the reaction stream obtained from the upper part of the second fluidized bed desulfurization reactor; 1c) performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain a reaction oil gas and a sulfur-filled adsorbent; 1d) performing gas-liquid separation on the reaction oil gas obtained in step 1c) to obtain the desulfurized rich gas and the desulfurized crude gasoline; 1e) sending the sulfur-filled adsorbent obtained in step 1c) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction; The method according to claim 1, further comprising.

10. The operating conditions of the first fluidized bed desulfurization reactor include a temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, The operating conditions of the second fluidized bed desulfurization reactor are a temperature of 250 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas feedstock of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, the method according to claim 9.

11. The catalytic cracking light product is a rich gas and a crude gasoline from the catalytic cracking fractionation column, and step 1) is 1a) Introducing the crude gasoline from the catalytic cracking fractionation column into the first fluidized bed desulfurization reactor from the bottom, and bringing it into contact with a desulfurization adsorbent introduced from the bottom of the reactor in the presence of hydrogen for a desulfurization reaction; 1b) Performing gas-solid separation on the reaction stream obtained at the upper part of the first fluidized bed desulfurization reactor to obtain the desulfurized crude gasoline and the sulfur-loaded adsorbent, and sending a part of the sulfur-loaded adsorbent to the upper part of the second fluidized bed desulfurization reactor; 1c) Introducing the rich gas from the catalytic cracking fractionation column into the second fluidized bed desulfurization reactor from the bottom, and bringing it into countercurrent contact with the sulfur-loaded adsorbent introduced into the reactor from the top of the reactor for a desulfurization reaction, obtaining the desulfurized rich gas at the upper end of the second fluidized bed desulfurization reactor, taking out the reacted sulfur-loaded adsorbent from the bottom of the second fluidized bed desulfurization reactor, and recycling it to the first fluidized bed desulfurization reactor; 1e) Sending the remainder of the sulfur-loaded adsorbent obtained in step 1b) to an adsorbent regenerator for regeneration by calcination in the presence of an oxygen-containing gas, and recycling the regenerated desulfurization adsorbent to the first fluidized bed desulfurization reactor after reduction; The method according to claim 1, further comprising.

12. The supply gas velocity of the first fluidized bed desulfurization reactor is 0.25 to 10 m / s, The supply gas velocity of the second fluidized bed desulfurization reactor is 0.05 to 1.5 m / s, the method according to claim 11.

13. The operating conditions of the first fluidized bed desulfurization reactor include a temperature of 200 to 550 °C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 1000, The operating conditions of the second fluidized bed desulfurization reactor are a temperature of 300 to 550°C, an absolute pressure of 0.5 to 5 MPa, a weight hourly space velocity of the oil gas raw material of 0.1 to 100 h －１ -1, and a molar ratio of hydrogen to oil of 0.01 to 500, the method according to claim 11 or 12.

14. The operating conditions of the adsorbent regenerator are including a regeneration temperature of 300 to 800 °C and a regeneration pressure of 0.1 to 3.0 MPa, The method according to any one of claims 2 to 13.

15. The desulfurization adsorbent includes a desulfurization adsorbent carrier and a metal component filled in the adsorbent carrier, The content of the desulfurization adsorbent carrier is 70 to 95% by weight, The content of the metal component is 5 to 30% by weight based on the total weight of the desulfurization adsorbent, The adsorbent carrier is selected from zinc oxide, silica, alumina or a mixture thereof, The metal component is selected from cobalt, nickel, copper, iron, manganese, molybdenum, tungsten, silver, tin, vanadium, or a combination thereof, the method according to any one of claims 1 to 14.

16. A method for producing a low-sulfur light oil product by catalytic cracking, i) A step of bringing a catalytic cracking feedstock into contact with a catalytic cracking catalyst in a riser reactor for the reaction under catalytic cracking conditions; ii) A step of performing gas-solid separation on the reaction product obtained in the step i) to obtain a reaction oil gas and a used catalyst; iii) A step of fractionating the reaction oil gas obtained in the step ii) in a catalytic cracking fractionation column to obtain a catalytic cracking light product, a light cycle oil, a diesel oil, and an oil slurry; iv) A step of desulfurizing and separating the catalytic cracking light product from the catalytic cracking fractionation column using the method according to any one of claims 1 to 15 to obtain a desulfurized dry gas, a desulfurized liquefied gas, and a desulfurized stabilized gasoline; v) A step of regenerating the used catalyst obtained in the step ii) and recycling the regenerated catalyst to the riser reactor for reuse; A method comprising the above steps.

17. An apparatus for desulfurization and separation of a catalytic cracking light product, comprising an adsorption desulfurization unit and an absorption stabilization unit connected in series in sequence; The absorption stabilization unit comprises an absorption column, a desorption column, a reabsorption column, and a stabilization column connected in series in sequence; In the absorption stabilization unit, the desulfurized rich gas passes through a pipeline, and the desulfurized crude gasoline or a part of the crude gasoline and the stabilized gasoline pass through a pipeline and enter the absorption column, contact in a countercurrent manner for mass transfer, to obtain a desulfurized rich gas with a reduced content of components exceeding C2 and a desulfurized crude gasoline with a reduced content of components below C2; The desulfurized rich gas with a reduced content of components exceeding C2 is introduced into the reabsorption column through a pipeline and contacted with the light cycle oil from the catalytic cracking fractionation column introduced through a pipeline for mass transfer, to obtain a desulfurized dry gas with a further reduced content of components exceeding C2, which is discharged from the reabsorption column through a pipeline; The concentrated light cycle oil that has absorbed a part of the components exceeding C2 is recycled from the bottom of the reabsorption column to the catalytic cracking fractionation column through a pipeline; The desulfurized crude gasoline with a reduced content of components below C2 is introduced into the desorption column through a pipeline, further removing the components below C2, and then introduced into the stabilization column through a pipeline, fractionated in the stabilization column to obtain a desulfurized liquefied gas and a desulfurized stabilized catalytic cracking gasoline; The top gas product of the desorption column is taken out through a pipeline and sent to the absorption column together with the desulfurized rich gas from the pipeline; The operating conditions of the stabilization column include a pressure of 0.1 to 3.0 MPa and a temperature of 20 to 250 °C. The adsorption desulfurization unit includes a fluidized bed desulfurization reactor, an adsorbent regenerator, and a lock hopper connected between the fluidized bed desulfurization reactor and the adsorbent regenerator and used for performing pressure change and atmosphere conversion. The fluidized bed desulfurization reactor communicates with the catalytic cracking fractionation column to receive the catalytic cracking light products from the catalytic cracking fractionation column. The oil-gas discharge port of the fluidized bed desulfurization reactor communicates with the absorption tower of the absorption and stabilization unit, or communicates with the absorption tower of the absorption and stabilization unit through a gas-liquid separation tank. In the adsorption desulfurization unit, the fluidized bed desulfurization reactor, the receiver of the reactor, the lock hopper, the supply tank of the regeneration tower, the adsorbent regenerator, and the receiver of the regenerator are sequentially communicated. The receiver of the regenerator communicates with the adsorbent reducer through the lock hopper. The adsorbent reducer communicates with the fluidized bed desulfurization reactor.

18. The fluidized bed desulfurization reactor includes a first fluidized bed desulfurization reactor, an adsorbent transfer tank, and a second fluidized bed desulfurization reactor that are sequentially communicated. The adsorbent reducer according to claim 17 communicates with the bottom of the first fluidized bed desulfurization reactor and / or the second fluidized bed desulfurization reactor.

19. The fluidized bed desulfurization reactor includes a first fluidized bed desulfurization reactor and a second fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicates with the receiver of the reactor. The adsorbent reducer communicates with the bottom of the first fluidized bed desulfurization reactor and / or the second fluidized bed desulfurization reactor. The central lower part of the first fluidized bed desulfurization reactor communicates with the bottom of the second fluidized bed desulfurization reactor. The upper part of the second fluidized bed desulfurization reactor communicates with the upper part of the first fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicates with the bottom of the second fluidized bed desulfurization reactor at a position 20 to 60% of the height from the bottom to the top, and the first fluidized bed desulfurization reactor communicates with the top of the second fluidized bed desulfurization reactor at a position 60 to 90% of the height from the bottom to the top. A solid-gas separation device is provided in the sedimentation area at the upper part of the first fluidized bed desulfurization reactor, and a solid-gas separation device is provided or not provided at the upper part of the second fluidized bed desulfurization reactor. The device according to claim 17.

20. The fluidized bed desulfurization reaction unit includes a first fluidized bed desulfurization reactor and a second fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicates with the receiver of the reactor. The adsorbent reducer communicates with the bottom of the first fluidized bed desulfurization reactor and / or the second fluidized bed desulfurization reactor. The upper part of the first fluidized bed desulfurization reactor communicates with the upper part of the second fluidized bed desulfurization reactor. The bottom of the second fluidized bed desulfurization reactor communicates with the bottom of the first fluidized bed desulfurization reactor. The first fluidized bed desulfurization reactor communicates with a position 80 to 90% of the height from the bottom to the top of the second fluidized bed desulfurization reactor at a position 50 to 90% of the height from the bottom to the top. The device according to claim 17.

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