A moving bed solid acid alkylation continuous reaction system and method

Abstract

The present application relates to a kind of mobile bed solid acid alkylation continuous reaction system and method, the system includes solid acid alkylation reactor (a), multiple catalysts to be regenerated pouring tank (e) and catalyst regenerator (g);The catalyst outlet of the catalyst to be regenerated pouring tank (e) is communicated with the catalyst regenerator (g) of spent agent inlet, the regenerated agent outlet of the catalyst regenerator (g) is communicated with the catalyst inlet of the solid acid alkylation reactor (a) by regenerated agent conveying pipeline;First catalyst conveying medium inlet is provided on the spent agent conveying pipeline, and second catalyst conveying medium inlet is provided on the regenerated agent conveying pipeline.This system can connect mobile bed solid acid alkylation reaction system and catalyst regeneration system, and then make solid acid alkylation reaction process and catalyst regeneration process continuous.

Description

Technical Field

[0001] This application relates to the field of solid acid alkylation, specifically to a continuous reaction system and method for solid acid alkylation. Background Technology

[0002] Alkylated oil is a mixture primarily composed of C8 branched alkanes, free of olefins, aromatics, sulfur, nitrogen, and other substances. It exhibits low sensitivity and vapor pressure, making it a clean and ideal component for high-octane gasoline. Solid acid alkylation processes use solid acids as catalysts, eliminating environmental pollution and posing no issues with equipment corrosion or catalyst transportation safety. With increasingly stringent safety and environmental regulations, alkylation technology is considered a safe and green option with promising development prospects. Fixed-bed solid acid alkylation processes typically involve at least two fixed-bed reactors. Each reactor undergoes periodic regeneration to restore catalyst activity, and continuous production is maintained through frequent switching between regeneration and reaction processes across multiple reactors. Although fixed-bed solid acid alkylation is relatively simple, it suffers from low catalyst utilization and challenges in continuous and smooth operation. Summary of the Invention

[0003] The purpose of this disclosure is to solve the problem of difficulty in connecting the moving bed solid acid alkylation reaction system and the regeneration system, so as to enable the solid acid alkylation reaction process and the catalyst regeneration process to proceed continuously.

[0004] To achieve the above objectives, the first aspect of this disclosure provides a moving bed solid acid alkylation continuous reaction system, comprising a solid acid alkylation reactor, multiple catalyst regeneration tanks, and a catalyst regenerator; the solid acid alkylation reactor includes a vertical first shell, a first catalyst channel, a feed inlet, and a reaction product outlet; the first catalyst channel is axially disposed within the first shell, its top extending upwards to the outside of the first shell to form a catalyst inlet, and its bottom forming a catalyst outlet; the interior of the first catalyst channel is in fluid communication with the outside; multiple catalyst regeneration tanks are arranged in parallel and positioned above the catalyst regenerator; each catalyst regeneration tank includes a tank body, a catalyst inlet, and a catalyst outlet; the catalyst regeneration tanks are arranged in parallel within the moving bed solid acid alkylation reactor, comprising a solid acid alkylation reactor, multiple catalyst regeneration tanks, and a catalyst regenerator ... The catalyst inlet of the biocatalyst dumping tank is switchably connected to the catalyst outlet of the solid acid alkylation reactor via a regenerator delivery pipeline; the catalyst regenerator includes a vertical second shell and a second catalyst channel; the second catalyst channel is axially disposed inside the second shell, the top of the second catalyst channel extends upward to the outside of the second shell to form a regenerator inlet, and the bottom of the second catalyst channel forms a regenerator outlet; the catalyst outlet of the biocatalyst dumping tank is connected to the regenerator inlet of the catalyst regenerator, and the regenerator outlet of the catalyst regenerator is connected to the catalyst inlet of the solid acid alkylation reactor via a regenerator delivery pipeline; the regenerator delivery pipeline is provided with a first catalyst delivery medium inlet, and the regenerator delivery pipeline is provided with a second catalyst delivery medium inlet.

[0005] Optionally, the first catalyst channel is formed as a cylindrical body with an annular cross-section for accommodating a solid acid catalyst; the inner and outer walls of the cylindrical body are coaxially arranged with the first shell, a feed distribution area is formed between the outer wall of the first catalyst channel and the inner wall of the shell, and a discharge area is formed between the inner walls, the feed distribution area and the discharge area are fluidly connected only through the first catalyst channel; the raw material inlet of the solid acid alkylation reactor is connected to the feed distribution area, and the reaction product outlet of the solid acid alkylation reactor is connected to the discharge area; the inner and outer walls of the first catalyst channel are respectively provided with openings to allow fluid communication between the inside and outside of the cylindrical body, the size of the openings being smaller than the size of the solid acid catalyst; the reaction product outlet of the solid acid alkylation reactor is also connected to the raw material inlet of the solid acid alkylation reactor through a circulating material pipeline.

[0006] Optionally, the system further includes a reactor catalyst feed hopper and a reactor catalyst discharge hopper; the reactor catalyst feed hopper is located above the solid acid alkylation reactor and its outlet is connected to the catalyst inlet of the solid acid alkylation reactor via a catalyst discharge pipe; the reactor catalyst discharge hopper is located below the solid acid alkylation reactor and its inlet is connected to the catalyst outlet of the solid acid alkylation reactor, and its outlet is connected to the catalyst inlet of a plurality of catalyst regeneration tanks via a regenerator delivery pipeline; the regenerator outlet of the catalyst regenerator is connected to the inlet of the reactor catalyst feed hopper via the regenerator delivery pipeline.

[0007] Optionally, the system further includes a regenerator feed hopper and a regenerator discharge hopper; the regenerator feed hopper is disposed between the catalyst to be regenerated discharge tank and the catalyst regenerator, and the inlet of the regenerator feed hopper is connected to the catalyst outlet of the catalyst to be regenerated discharge tank through an outlet pipe; each outlet pipe is equipped with a shut-off valve; the outlet of the regenerator feed hopper is connected to the regenerator inlet of the catalyst regenerator through a regenerator discharge pipe; the regenerator discharge hopper is disposed below the catalyst regenerator, the inlet of the regenerator discharge hopper is connected to the regenerator outlet of the catalyst regenerator, and the outlet of the regenerator discharge hopper is connected to the catalyst inlet of the solid acid alkylation reactor through the regenerator conveying pipeline.

[0008] Optionally, the inner sleeve is provided inside the tank of the catalyst to be regenerated, and the inner sleeve is coaxially disposed at the lower part of the tank body of the catalyst to be regenerated, so as to form a filtrate zone between the inner sleeve and the inner wall of the tank body; the inner sleeve has filter holes, and the pore size of the filter holes is smaller than the particle size of the solid acid alkylation catalyst; optionally, the tank body of the filtrate zone is provided with a filtrate outlet, and the filtrate outlet is connected to the raw material inlet of the solid acid alkylation reactor through a filtrate pipeline; the catalyst inlet of each catalyst to be regenerated tank is connected to the catalyst delivery pipeline through an inlet pipeline, and each inlet pipeline is provided with a shut-off valve; the system includes two catalyst to be regenerated tanks.

[0009] Optionally, the catalyst regenerator further includes a first regeneration medium inlet, a first regeneration medium outlet, a second regeneration medium inlet, and a second regeneration medium outlet; the second catalyst channel is formed as a cylindrical body with an annular cross-section, and the second catalyst channel is coaxially arranged with the second shell of the catalyst regenerator so that the catalyst to be generated can move downward along the second catalyst channel; the interior and exterior of the second catalyst channel are in fluid communication through the channel sidewall, and the shell-side space formed between the channel sidewall and the inner wall of the second shell includes, from top to bottom, an upper shell-side section, a middle shell-side section, and a lower shell-side section, and the middle shell-side section and the lower shell-side section are not in fluid communication; the first regeneration medium inlet and the first regeneration medium outlet are located in the lower shell-side section. The second regeneration medium inlet is located in the middle section of the shell side, and the second regeneration medium outlet is located in the upper section of the shell side; the first regeneration medium outlet and the second regeneration medium inlet are connected by a regeneration medium pipeline, and a booster fan and a heater are provided on the regeneration medium pipeline; the catalyst regenerator also includes an immersion tank and a regenerator leg, the immersion tank is located below the catalyst regenerator and its top is fixedly connected to the bottom wall of the second shell, the regenerator leg is connected to the bottom of the second catalyst channel and extends downward through the bottom wall of the second shell into the immersion tank, the bottom of the immersion tank is provided with an opening to form the regenerator outlet of the catalyst regenerator; the upper part of the immersion tank is provided with an immersion medium inlet.

[0010] The second aspect of this disclosure employs a method for a continuous solid acid alkylation reaction using the system described in any one of the first aspects of this disclosure. The method includes: introducing a C4 feedstock into a solid acid alkylation reactor via the feedstock inlet; introducing a solid acid alkylation catalyst into the solid acid alkylation reactor via a catalyst inlet, moving downwards along a first catalyst channel, and reacting with the C4 feedstock; introducing a portion of the catalyst transport medium into a spent catalyst transport pipeline via a first catalyst transport medium inlet, transporting the spent catalyst from the first catalyst channel to a spent catalyst regeneration tank; when the regenerated catalyst in the spent catalyst regeneration tank reaches a capacity threshold, switching the spent catalyst to another spent catalyst regeneration tank; introducing a regeneration medium into a catalyst regenerator to regenerate the spent catalyst; and introducing another portion of the catalyst transport medium into a regenerated catalyst transport pipeline via a second catalyst transport medium inlet, transporting the regenerated catalyst from the catalyst regenerator to the catalyst inlet of the solid acid alkylation reactor.

[0011] Optionally, the method further includes: cooling the regenerant from the catalyst regenerator through an immersion medium before returning it to the catalyst inlet of the solid acid alkylation reactor; wherein the immersion medium is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons; and the catalyst delivery medium is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons.

[0012] Optionally, the method further includes: before the regeneration treatment, preheating the regeneration medium by contacting it with the regenerator at the bottom of the second catalyst channel, and pressurizing and heating the preheated regeneration medium; wherein the preheated regeneration medium is pressurized to 0.8–3.5 MPa and then heated to 150–300°C; the regeneration medium and the regenerator are in cross-flow contact; the regeneration medium is hydrogen and / or a mixture of hydrogen and hydrocarbons.

[0013] Optionally, the reactants are a mixture of C4 alkanes and C4 olefins; the reaction temperature of the solid acid alkylation reactor is 10–90°C; and the average particle size of the solid acid alkylation catalyst is 1–5 mm.

[0014] Through the above technical solution, the first catalyst channel and the second catalyst channel are arranged axially within the corresponding shells, enabling the solid acid alkylation catalyst to move downwards by gravity. The first catalyst channel and the second catalyst channel are connected by a regenerator delivery pipeline containing a delivery medium, allowing the catalyst to circulate between the first and second catalyst channels, thus enabling the solid acid alkylation reaction process and the catalyst regeneration process to proceed continuously, achieving the effect of continuous reaction of the reactants. By adding multiple parallel catalyst discharge tanks to the delivery pipelines of the solid acid alkylation reactor and the catalyst regenerator, the moving bed solid acid alkylation reaction system and the regeneration system can be connected.

[0015] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0016] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings:

[0017] Figure 1 This is a process flow diagram of a specific embodiment of a moving bed solid acid alkylation continuous reaction system disclosed herein.

[0018] Explanation of reference numerals in the attached figures

[0019] a. Solid acid alkylation reactor; b. Reactor catalyst feed hopper; c. Reactor catalyst discharge hopper; d. Reactant material circulation pump; e. Catalyst to be regenerated discharge tank; f. Regenerator feed hopper; g. Catalyst regenerator; h. Immersion tank; i. Regenerator discharge hopper; j. Heater; n. Booster fan; s. Inner sleeve; t. Catalyst discharge pipe; v. Shut-off valve;

[0020] 1. C4 feedstock; 2. Reaction cycle stream; 3. Catalyst transport medium; 4. Alkylation products; 5. Solid acid alkylation catalyst; 6. Regeneration medium; 7. Immersion medium. Detailed Implementation

[0021] The following provides a detailed description of specific embodiments of this disclosure. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit this disclosure.

[0022] like Figure 1 As shown, the first aspect of this disclosure provides a moving bed solid acid alkylation continuous reaction system, which includes a solid acid alkylation reactor a, multiple catalyst regeneration tanks e, and a catalyst regenerator g. The solid acid alkylation reactor a includes a vertical first shell, a first catalyst channel, a feed inlet, and a reaction product outlet. The first catalyst channel is axially disposed within the first shell, with its top extending upwards to the outside of the first shell to form a catalyst inlet, and its bottom forming a catalyst outlet. The interior of the first catalyst channel is in fluid communication with the outside. Multiple catalyst regeneration tanks e are arranged in parallel and positioned above the catalyst regenerator g. Each catalyst regeneration tank e includes a tank body, a catalyst inlet, and a catalyst outlet. The catalyst inlet of the catalyst discharge tank e is switchably connected to the catalyst outlet of the solid acid alkylation reactor a via a regenerator delivery pipeline; the catalyst regenerator g includes a vertical second shell and a second catalyst channel; the second catalyst channel is axially disposed inside the second shell, the top of the second catalyst channel extends upward to the outside of the second shell to form a regenerator inlet, and the bottom of the second catalyst channel forms a regenerator outlet; the catalyst outlet of the catalyst discharge tank e is connected to the regenerator inlet of the catalyst regenerator g, and the regenerator outlet of the catalyst regenerator g is connected to the catalyst inlet of the solid acid alkylation reactor a via a regenerator delivery pipeline; the regenerator delivery pipeline is provided with a first catalyst delivery medium inlet, and the regenerator delivery pipeline is provided with a second catalyst delivery medium inlet.

[0023] Through the above technical solution, this disclosure connects the catalyst outlet of the catalyst regeneration tank e to the catalyst regenerator g's catalyst inlet, and the catalyst regenerator g's regenerator outlet is connected to the catalyst inlet of the solid acid alkylation reactor a via a regenerator delivery pipeline. This connection method allows the moving bed solid acid alkylation reaction system and the catalyst regeneration system to be linked, enabling the solid acid alkylation reaction process and the catalyst regeneration process to proceed continuously. The solid acid alkylation reactor a is a liquid-solid radial moving bed reactor; within the reactor, the solid acid alkylation catalyst 5 moves downwards by gravity within the catalyst channel, and the reactant stream cross-flows through the catalyst channel, contacting the catalyst and undergoing an alkylation reaction.

[0024] In one embodiment, the first catalyst channel is formed as a cylindrical body with an annular cross-section to accommodate the solid acid alkylation catalyst 5. The inner and outer walls of the cylindrical body are coaxially arranged with the first shell, so that the solid acid alkylation catalyst 5 can be evenly distributed in the solid acid alkylation reactor a, thereby improving the reaction efficiency. A feed distribution zone is formed between the outer wall of the first catalyst channel and the inner wall of the first shell, and a discharge zone is formed between the inner walls. The feed distribution zone and the discharge zone are only fluidly connected through the first catalyst channel, so that the C4 feedstock 1 can pass through the first catalyst channel before entering the discharge zone, thereby accelerating the reaction efficiency. The original solid acid alkylation reactor a... The feed inlet is connected to the feed distribution area, and the reaction product outlet of the solid acid alkylation reactor a is connected to the discharge area. The inner and outer walls of the first catalyst channel have openings to allow fluid communication between the inside and outside of the cylinder. The size of the openings is smaller than the size of the solid acid alkylation catalyst 5, so that the solid acid alkylation catalyst 5 continuously flows within the first catalyst channel. Optionally, the reaction product outlet of the solid acid alkylation reactor a is also connected to the feed inlet of the solid acid alkylation reactor a via a circulating material pipeline, so that the C4 feedstock 1 and the reaction circulating stream enter the solid acid alkylation reactor a together for reaction, which can make the reaction more complete and improve the purity of the product.

[0025] In one embodiment, the system further includes a reactor catalyst feed hopper b and a reactor catalyst discharge hopper c, so that the material in the reactor catalyst feed hopper b and the reactor catalyst discharge hopper c can be buffered, and the material flow rate can be stabilized, thereby achieving the function of flow control; the reactor catalyst feed hopper b is arranged above the solid acid alkylation reactor a, and the outlet of the reactor catalyst feed hopper b is connected to the catalyst inlet of the solid acid alkylation reactor a through the catalyst discharge pipe t, for storing solid acid alkylation catalyst 5, and for timely replenishment of catalyst into the solid acid alkylation reactor a; the reactor catalyst discharge hopper c is arranged... The catalyst regenerator g is positioned below the solid acid alkylation reactor a, with the inlet of the reactor catalyst discharge hopper c connected to the catalyst outlet of the solid acid alkylation reactor a. The outlet of the reactor catalyst discharge hopper c is connected to the catalyst inlets of multiple catalyst regeneration tanks e through the regenerator conveying pipeline, so that the regenerator can be conveyed to the catalyst regeneration tanks e through the conveying medium in the pipeline. The regenerator outlet of the catalyst regenerator g is connected to the inlet of the reactor catalyst feed hopper b through the regenerator conveying pipeline, and is used to convey the regenerated solid acid alkylation catalyst 5 to the catalyst feed hopper b, thereby enabling the material to react continuously.

[0026] In one embodiment, the system further includes a regenerator feed hopper f and a regenerator discharge hopper i; the regenerator feed hopper f is disposed between the catalyst receiving tank e and the catalyst regenerator g, and the inlet of the regenerator feed hopper f is connected to the catalyst outlet of the catalyst receiving tank e through an outlet pipe, for storing the regenerating agent flowing out of the catalyst receiving tank e in the regenerator feed hopper f; each outlet pipe is provided with a shut-off valve v; the outlet of the regenerator feed hopper f is connected to the regenerating agent in the catalyst regenerator g through a regenerating agent discharge pipe. The inlet is connected; the regenerator discharge hopper i is located below the catalyst regenerator g, and the inlet of the regenerator discharge hopper i is connected to the regenerator outlet of the catalyst regenerator g, so that the regenerator stored in the regenerator feed hopper f can be replenished to the catalyst regenerator g at any time; the outlet of the regenerator discharge hopper i is connected to the inlet of the reactor catalyst feed hopper b above the solid acid alkylation reactor a through the regenerator conveying pipeline, and the outlet of the reactor catalyst feed hopper b is connected to the catalyst inlet of the solid acid alkylation reactor a.

[0027] In one embodiment, an inner sleeve s is provided inside the tank body of the catalyst regeneration tank e. The inner sleeve s is coaxially disposed at the lower part of the tank body of the catalyst regeneration tank e to form a filtrate zone between the inner sleeve s and the inner wall of the tank body. The inner sleeve s has filter holes, the pore size of which is smaller than the particle size of the solid acid alkylation catalyst 5. Optionally, the tank body of the filtrate zone is provided with a filtrate outlet, which is connected to the raw material inlet of the solid acid alkylation reactor a through a filtrate pipeline, so that the reaction product in the filtrate can be reused as a reaction raw material. Optionally, the catalyst inlet of each catalyst regeneration tank e is connected to the catalyst delivery pipeline through an inlet pipeline for delivering the catalyst to the catalyst delivery pipeline. Each inlet pipeline is provided with a shut-off valve v. Optionally, the system includes two catalyst regeneration tanks e.

[0028] In this embodiment, the inner sleeve s is provided inside the tank of the catalyst to be regenerated discharge tank e, and the inner sleeve s has filter holes. The pore size of the filter holes is smaller than the particle size of the solid acid alkylation catalyst 5, which can initially separate the catalyst to be regenerated and the conveying medium 3 entering the tank of the catalyst to be regenerated discharge tank e. By setting a shut-off valve v, the transmission of the catalyst to be regenerated and the conveying medium 3 can be better controlled. By setting two or more catalyst to be regenerated discharge tanks e, the transmission of the catalyst to be regenerated can be further controlled.

[0029] In one embodiment, the catalyst regenerator g further includes a first regeneration medium inlet, a first regeneration medium outlet, a second regeneration medium inlet, and a second regeneration medium outlet; the second catalyst channel is formed as a cylindrical body with an annular cross-section, so that the substrate is evenly distributed within the catalyst regenerator g, thereby enhancing the efficiency of the regeneration reaction; the second catalyst channel is coaxially arranged with the second shell of the catalyst regenerator g, so that the substrate can move downward along the second catalyst channel; the interior and exterior of the second catalyst channel are fluidly connected through the channel sidewall; the shell-side space formed between the channel sidewall and the inner wall of the second shell includes, from top to bottom, an upper shell-side section, a middle shell-side section, and a lower shell-side section; the middle shell-side section and the lower shell-side section are not fluidly connected; the first regeneration medium inlet and the first regeneration medium outlet are provided with... The catalyst regenerator g is located in the lower shell side, the second regeneration medium inlet is located in the middle shell side, and the second regeneration medium outlet is located in the upper shell side. The first regeneration medium outlet and the second regeneration medium inlet are connected by a regeneration medium pipeline, and the regeneration medium pipeline is equipped with a booster fan n and a heater j. Optionally, the catalyst regenerator g further includes an immersion tank h and a regenerator feed hopper f. The immersion tank h is located below the catalyst regenerator g and its top is fixedly connected to the bottom wall of the second shell. The regenerator feed hopper f is connected to the bottom of the second catalyst channel and extends downward through the bottom wall of the second shell into the immersion tank h. The bottom of the immersion tank h has an opening to form the regenerator outlet of the catalyst regenerator g. The upper part of the immersion tank h has an immersion medium inlet.

[0030] In this embodiment, the catalyst regenerator g is a gas-solid radial moving bed reactor. In addition, the catalyst regenerator g also includes a booster fan n and a heater j. The first regeneration medium outlet in the lower section is connected to the inlet of the booster fan n; the outlet of the booster fan n is connected to the inlet of the heater j; and the outlet of the heater j is connected to the regeneration medium inlet in the middle section of the catalyst regenerator g. Through the combined action of the booster fan n and the heater j, the spent catalyst can be regenerated in a suitable temperature and regeneration medium 6.

[0031] The second aspect of this disclosure employs a method for a continuous solid acid alkylation reaction using the system described in any one of the first aspects of this disclosure. The method includes: introducing C4 feedstock 1 into a solid acid alkylation reactor a via the feedstock inlet; introducing a solid acid alkylation catalyst 5 into the solid acid alkylation reactor a via a catalyst inlet, moving downwards along a first catalyst channel, and reacting with the C4 feedstock 1; introducing a portion of the catalyst transport medium 3 into a regenerator transport pipeline via a first catalyst transport medium inlet, transporting the regenerator from the first catalyst channel to a catalyst regeneration tank e; when the regenerator in the catalyst regeneration tank e reaches a preset capacity threshold indicated by a level gauge, the regenerator can be manually or automatically switched to another catalyst regeneration tank e; introducing a regeneration medium 6 into a catalyst regenerator g to regenerate the regenerator; and introducing another portion of the catalyst transport medium 3 into a regenerator transport pipeline via a second catalyst transport medium inlet, transporting the regenerator from the catalyst regenerator g to the catalyst inlet of the solid acid alkylation reactor a.

[0032] The above technical solution involves adding C4 feedstock 1 and solid acid alkylation catalyst 5 to solid acid alkylation reactor a for reaction. The reaction product is divided into two streams: one stream returns to the system for further recycling, and the other stream is the obtained product. This method improves the quality of the obtained product. Simultaneously, the spent catalyst is fed into the catalyst regeneration tank e via catalyst transport medium 3 for subsequent regeneration. This method combines the moving bed solid acid alkylation reaction and the regeneration reaction, thus achieving continuous operation of both the solid acid alkylation process and the catalyst regeneration process.

[0033] In one embodiment, the method further includes: cooling the regenerant from the catalyst regenerator g through an immersion medium 7 before returning it to the catalyst inlet of the solid acid alkylation reactor a; wherein the immersion medium 7 is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons; and the catalyst delivery medium 3 is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons.

[0034] In this embodiment, the soaking medium 7 can accelerate the heat dissipation of the regenerator from the catalyst regenerator g, and at the same time wash out the impurities in the regenerator, increasing the catalytic activity of the regenerated solid acid alkylation catalyst 5, thereby enhancing the performance of the solid acid alkylation reaction.

[0035] In one embodiment, the method further includes: before the regeneration treatment, preheating the regeneration medium 6 by contacting it with the regenerator at the lower part of the second catalyst channel, and pressurizing and heating the preheated regeneration medium 6; wherein the preheated regeneration medium 6 is pressurized to 0.8-3.5 MPa and then heated to 150-300°C; the regeneration medium 6 is in cross-flow contact with the regenerator; the regeneration medium 6 is hydrogen and / or a mixture of hydrogen and hydrocarbons.

[0036] In one embodiment, the C4 feedstock 1 is a mixture of C4 alkanes and C4 olefins; the reaction temperature of the solid acid alkylation reactor a is 10–90°C; and the solid acid alkylation catalyst 5 is a particulate solid acid alkylation catalyst with an average particle size of 1–5 mm.

[0037] The present disclosure is further described in detail below through examples. All raw materials used in the examples are commercially available.

[0038] In a preferred embodiment of this disclosure, such as Figure 1 As shown, the method for continuous reaction of solid acid alkylation includes the following steps:

[0039] Liquid C4 feedstock 1 and reaction recycle stream 2 are fed together as reaction streams from the feed inlet of solid acid alkylation reactor a into the feed distribution zone of the reactor; solid acid alkylation catalyst 5 in the reactor catalyst feed hopper b enters the first catalyst channel of the reactor from the top of the reactor by gravity and moves downward along the first catalyst channel by gravity; the liquid C4 feedstock 1 and solid acid alkylation catalyst 5 undergo cross-flow contact reaction; the reaction temperature of the solid acid alkylation reactor a is 10-90℃; the average particle size of the solid acid alkylation catalyst 5 is 1-5mm.

[0040] The liquid reaction products flow out of the reactor's reaction product outlet and are divided into two streams. One stream is used as alkylation product 4, and the other stream is used as reaction circulation stream 2. It is pressurized by the reaction material circulation pump d and then mixed with C4 feedstock 1.

[0041] Solid acid alkylation catalyst 5, flowing from the bottom of the reactor, falls into the reactor catalyst discharge hopper c, and is then pumped by liquid isobutane, which serves as the catalyst transport medium 3, to a catalyst regeneration tank e. When the regenerated catalyst tank e receives enough regenerant to reach its capacity threshold, the feed is switched to another catalyst regeneration tank e. After dehydration, the regenerant in the catalyst regeneration tank e falls into the regenerator feed hopper f by gravity. The liquid isobutane discharged from the catalyst regeneration tank e flows by gravity to the inlet of the reactant circulation pump d.

[0042] The regenerator feed hopper f is fed into the second catalyst channel from the top of the catalyst regenerator g by gravity. It then passes through the second catalyst channel by gravity and falls into the soaking medium 7 liquid isobutane in the soaking tank h via the catalyst feed pipe t.

[0043] The regeneration medium 6 enters from the regeneration medium inlet of the lower section of the catalyst regenerator g, flows through the catalyst channel of the lower section, and then flows out from the regeneration medium outlet of the lower section. After being pressurized to 0.8-3.5 MPa by the booster fan n, it is heated to 150-300℃ by the heater j and then enters from the regeneration medium inlet of the middle section of the catalyst regenerator. It flows through the middle and upper catalyst channels in turn and then flows out from the regeneration medium outlet at the top of the catalyst regenerator g.

[0044] The solid acid alkylation catalyst to be regenerated is first heated to the regeneration temperature by the regeneration medium 6 in the catalyst channel of the catalyst regenerator g. After regeneration is completed, it is cooled by the regeneration medium 6. After flowing out of the catalyst regenerator g, it falls into the liquid isobutane in the soaking tank h and continues to cool.

[0045] The solid acid alkylation catalyst 5 in the soaking tank h falls into the regenerator discharge hopper i; then is pumped and carried by isobutane to the reactor catalyst feed hopper b.

[0046] The above method achieves the connection between low-temperature solid acid alkylation liquid, solid moving bed reaction and high-temperature solid acid alkylation catalyst gas, solid moving bed regeneration, that is, the moving bed solid acid alkylation reaction system and the catalyst regeneration system are connected, so that the solid acid alkylation reaction and the catalyst regeneration reaction can proceed continuously and stably.

[0047] The preferred embodiments of this disclosure have been described in detail above. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0048] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0049] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A moving bed solid acid alkylation continuous reaction system for C4 feedstock alkylation reaction, characterized in that, The system includes a solid acid alkylation reactor (a), multiple catalyst regeneration tanks (e), and a catalyst regenerator (g). The solid acid alkylation reactor (a) includes a vertical first shell, a first catalyst channel, a raw material inlet, and a reaction product outlet; the first catalyst channel is axially disposed inside the first shell, the top of the first catalyst channel extends upward to the outside of the first shell to form a catalyst inlet, and the bottom of the first catalyst channel forms a catalyst outlet; the interior of the first catalyst channel is in fluid communication with the outside. Multiple catalyst regeneration tanks (e) are arranged in parallel and positioned above the catalyst regenerator (g); each catalyst regeneration tank (e) includes a tank body, a catalyst inlet, and a catalyst outlet; the catalyst inlet of the catalyst regeneration tank (e) is switchably connected to the catalyst outlet of the solid acid alkylation reactor (a) via a catalyst delivery pipeline; The catalyst regenerator (g) includes a vertical second shell and a second catalyst channel; the second catalyst channel is axially disposed inside the second shell, the top of the second catalyst channel extends upward to the outside of the second shell to form a regenerator inlet, and the bottom of the second catalyst channel forms a regenerator outlet; the catalyst outlet of the catalyst discharge tank (e) is connected to the regenerator inlet of the catalyst regenerator (g), and the regenerator outlet of the catalyst regenerator (g) is connected to the catalyst inlet of the solid acid alkylation reactor (a) through a regenerator conveying pipeline; The pipeline for transporting the regenerator is provided with a first catalyst transport medium inlet, and the pipeline for transporting the regenerator is provided with a second catalyst transport medium inlet; the catalyst transport medium is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons. The inner sleeve (s) is provided inside the tank of the catalyst to be regenerated (e). The inner sleeve (s) is coaxially disposed at the lower part of the tank of the catalyst to be regenerated (e) to form a filtrate zone between the inner sleeve (s) and the inner wall of the tank. The inner sleeve (s) has filter holes, the pore size of which is smaller than the particle size of the solid acid alkylation catalyst (5). The tank of the filtrate zone is provided with a filtrate outlet, which is connected to the raw material inlet of the solid acid alkylation reactor (a) through a filtrate pipeline. The first catalyst channel is formed as a cylindrical body with an annular cross-section for containing a solid acid alkylation catalyst (5); the inner and outer walls of the first catalyst channel are respectively provided with openings to allow fluid communication between the inside and outside of the cylindrical body, and the size of the openings is smaller than the size of the solid acid alkylation catalyst (5); The catalyst regenerator (g) further includes a first regeneration medium inlet, a first regeneration medium outlet, a second regeneration medium inlet, and a second regeneration medium outlet; The second catalyst channel is formed as a cylindrical body with an annular cross-section. The second catalyst channel is coaxially arranged with the second shell of the catalyst regenerator (g) so that the recycled agent can move downward along the second catalyst channel. The interior and exterior of the second catalyst channel are fluidly connected through the channel sidewall. The shell-side space formed between the channel sidewall and the inner wall of the second shell includes an upper shell-side section, a middle shell-side section, and a lower shell-side section from top to bottom. The middle shell-side section and the lower shell-side section are not fluidly connected. The first regeneration medium inlet and the first regeneration medium outlet are located in the lower shell-side section, the second regeneration medium inlet is located in the middle shell-side section, and the second regeneration medium outlet is located in the upper shell-side section. The first regeneration medium outlet and the second regeneration medium inlet are connected through a regeneration medium pipeline. The regeneration medium pipeline is equipped with a booster fan (n) and a heater (j). The regeneration medium and the recycled agent are in cross-flow contact. The regeneration medium is hydrogen or a mixture of hydrogen and hydrocarbons.

2. The system according to claim 1, characterized in that, The inner and outer walls of the cylinder are coaxially arranged with the first shell. A feed distribution area is formed between the outer wall of the first catalyst channel and the inner wall of the first shell, and a discharge area is formed between the inner walls. The feed distribution area and the discharge area are only fluidly connected through the first catalyst channel. The raw material inlet of the solid acid alkylation reactor (a) is connected to the feed distribution area, and the reaction product outlet of the solid acid alkylation reactor (a) is connected to the discharge area.

3. The system according to claim 2, characterized in that, The reaction product outlet of the solid acid alkylation reactor (a) is also connected to the raw material inlet of the solid acid alkylation reactor (a) via a circulating material pipeline.

4. The system according to claim 1, characterized in that, The system also includes a reactor catalyst feed hopper (b) and a reactor catalyst discharge hopper (c); The reactor catalyst feed hopper (b) is located above the solid acid alkylation reactor (a), and the outlet of the reactor catalyst feed hopper (b) is connected to the catalyst inlet of the solid acid alkylation reactor (a) through the catalyst feed pipe (t). The reactor catalyst discharge hopper (c) is located below the solid acid alkylation reactor (a), and the inlet of the reactor catalyst discharge hopper (c) is connected to the catalyst outlet of the solid acid alkylation reactor (a). The outlet of the reactor catalyst discharge hopper (c) is connected to the catalyst inlet of a plurality of catalyst regeneration tanks (e) through the regenerated catalyst conveying pipeline. The regenerator outlet of the catalyst regenerator (g) is connected to the inlet of the reactor catalyst feed hopper (b) via the regenerator delivery pipeline.

5. The system according to claim 1, characterized in that, The system also includes a regenerator feed hopper (f) and a regenerator discharge hopper (i); The regenerator feed hopper (f) is located between the catalyst receiving tank (e) and the catalyst regenerator (g). The inlet of the regenerator feed hopper (f) is connected to the catalyst outlet of the catalyst receiving tank (e) through an outlet pipe. Each outlet pipe is equipped with a shut-off valve (v). The outlet of the regenerator feed hopper (f) is connected to the regenerator inlet of the catalyst regenerator (g) through a regenerator discharge pipe. The regenerator discharge hopper (i) is located below the catalyst regenerator (g). The inlet of the regenerator discharge hopper (i) is connected to the regenerator outlet of the catalyst regenerator (g). The outlet of the regenerator discharge hopper (i) is connected to the catalyst inlet of the solid acid alkylation reactor (a) through the regenerator conveying pipeline.

6. The system according to claim 1, characterized in that, The catalyst inlet of each of the catalyst regeneration tanks (e) is connected to the catalyst delivery pipeline via an inlet pipeline, and each of the inlet pipelines is equipped with a shut-off valve (v).

7. The system according to claim 1, characterized in that, The system includes two catalyst regeneration tanks (e).

8. The system according to claim 1, characterized in that, The catalyst regenerator (g) further includes an immersion tank (h) and a regenerator feed hopper (f). The immersion tank (h) is located below the catalyst regenerator (g) and its top is fixedly connected to the bottom wall of the second housing. The regenerator feed hopper (f) communicates with the bottom of the second catalyst channel and extends downward through the bottom wall of the second housing into the immersion tank (h). The bottom of the immersion tank (h) is provided with an opening to form the regenerator outlet of the catalyst regenerator (g). The upper part of the immersion tank (h) is provided with an immersion medium inlet.

9. A method for carrying out a continuous solid acid alkylation reaction using the system described in any one of claims 1 to 8, characterized in that, The method includes: The C4 feedstock (1) is introduced into the solid acid alkylation reactor (a) through the feedstock inlet; the solid acid alkylation catalyst (5) is introduced into the solid acid alkylation reactor (a) through the catalyst inlet, moves downward along the first catalyst channel, and reacts with the C4 feedstock (1); A portion of the catalyst transport medium (3) is introduced into the regenerated agent transport pipeline through the first catalyst transport medium inlet, and the regenerated agent from the first catalyst channel is transported to a catalyst regeneration tank (e). When the regenerated agent in the catalyst regeneration tank (e) reaches the capacity threshold, the regenerated agent is switched to another catalyst regeneration tank (e). The regeneration medium (6) is introduced into the catalyst regenerator (g) to regenerate the recycled agent. Another part of the catalyst transport medium (3) is introduced into the regenerator transport pipeline through the second catalyst transport medium inlet, and the regenerator from the catalyst regenerator (g) is transported to the catalyst inlet of the solid acid alkylation reactor (a).

10. The method according to claim 9, characterized in that, The method further includes: cooling the regenerant from the catalyst regenerator (g) through an immersion medium (7) before returning it to the catalyst inlet of the solid acid alkylation reactor (a); wherein the immersion medium (7) is selected from one or more of liquid isobutane, n-butane and mixed C4 hydrocarbons; The catalyst delivery medium (3) is selected from one or more of liquid isobutane, n-butane, and mixed C4 hydrocarbons.

11. The method according to claim 9, characterized in that, The method further includes: before the regeneration treatment, preheating the regeneration medium (6) by contacting the regenerator at the bottom of the second catalyst channel, and pressurizing and heating the preheated regeneration medium (6); wherein the preheated regeneration medium (6) is pressurized to 0.8~3.5 MPag and then heated to 150~300°C; the regeneration medium (6) is in cross-flow contact with the regenerator; The regeneration medium (6) is hydrogen or a mixture of hydrogen and hydrocarbons.

12. The method according to claim 9, characterized in that, The C4 feedstock (1) is a mixture of C4 alkanes and C4 olefins; the reaction temperature of the solid acid alkylation reactor (a) is 10-90°C; and the average particle size of the solid acid alkylation catalyst (5) is 1-5 mm.

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