阅读说明：本技术 双颗粒催化剂耦合催化方法及反应系统 (Double-particle catalyst coupling catalysis method and reaction system ) 是由 王龙延 杨鑫 雷世远 孟凡东 王松江 孙世源 于 2021-10-14 设计创作，主要内容包括：本发明涉及气-固相化学反应领域,公开了双颗粒催化剂耦合催化方法及反应系统。方法包括：使由再生器导出的轻颗粒催化剂进入含有重颗粒催化剂的第一流化床反应器中,重颗粒催化剂在第一流化床反应器中参与进行第一化学反应,轻颗粒催化剂为第一化学反应供热或取热；轻颗粒催化剂进入第二流化床反应器中参与进行第二化学反应；然后催化剂颗粒进入再生器中再生；经再生器再生后的催化剂颗粒被再次输送至第一流化床反应器。反应系统,其包括：第一流化床反应器、第二流化床反应器以及再生器。本发明可实现在同一系统不同反应区中实现催化剂和化学反应的高度匹配；可实现两种颗粒快速的传热,可实现热量的高效利用避免热量浪费,减少设备投资。(The invention relates to the field of gas-solid phase chemical reaction, and discloses a coupling catalysis method and a coupling catalysis system for a double-particle catalyst. The method comprises the following steps: the light particle catalyst led out from the regenerator enters a first fluidized bed reactor containing a heavy particle catalyst, the heavy particle catalyst participates in a first chemical reaction in the first fluidized bed reactor, and the light particle catalyst supplies heat or takes heat for the first chemical reaction; the light particle catalyst enters a second fluidized bed reactor to participate in a second chemical reaction; then the catalyst particles enter a regenerator for regeneration; the catalyst particles regenerated by the regenerator are again transferred to the first fluidized bed reactor. A reaction system, comprising: a first fluidized bed reactor, a second fluidized bed reactor, and a regenerator. The invention can realize the high matching of the catalyst and the chemical reaction in different reaction zones of the same system; the quick heat transfer of two kinds of granules can be realized, thermal high efficiency utilization can be realized and heat waste is avoided, and equipment investment is reduced.)

1. The double-particle catalyst coupling catalysis method is characterized by comprising the following steps:

the method comprises the steps of enabling light particle catalysts discharged from a regenerator or light particle catalysts carrying partial heavy particle catalysts to enter a first fluidized bed reactor containing the heavy particle catalysts, enabling the heavy particle catalysts to participate in a first chemical reaction in the first fluidized bed reactor, and enabling first reaction raw materials to be converted into first reaction products, wherein the light particle catalysts supply heat or heat for the first chemical reaction;

the light particle catalyst or the light particle catalyst carrying part of the heavy particle catalyst enters a second fluidized bed reactor by controlling the flow rate of carrier gas of the fluidized bed, and the light particle catalyst participates in a second chemical reaction, so that a second reaction raw material is converted into a second reaction product;

the light particle catalyst passing through the second fluidized bed reactor or the light particle catalyst carrying part of the heavy particle catalyst is conveyed to the regenerator by carrier gas for regeneration;

the light particle catalyst regenerated by the regenerator or the light particle catalyst carrying a part of the heavy particle catalyst is conveyed to the first fluidized bed reactor again by the carrier gas.

2. The dual-particle catalyst coupled catalysis method of claim 1, wherein the first chemical reaction is an endothermic reaction, the second chemical reaction is an exothermic reaction, the temperature of the light-particle catalyst after regeneration is higher than the temperature in the first fluidized bed reactor, and the light-particle catalyst after regeneration provides heat for the first chemical reaction as a heat donor.

3. The dual particle catalyst coupled catalytic process of claim 1, wherein the first chemical reaction is an exothermic reaction, the second chemical reaction is an endothermic reaction, the temperature of the regenerated light particle catalyst is lower than the temperature in the first fluidized bed reactor, and the regenerated light particle catalyst acts as a heat sink to carry away heat in the first fluidized bed reactor.

4. The dual particle catalyst coupled catalytic process of claim 1, wherein the particle size of the heavy particle catalyst is larger than the particle size of the light particle catalyst.

5. The dual particle catalyst coupled catalysis method according to any of claims 1 to 4, wherein the particle density of the heavy particle catalyst is greater than the particle density of the light particle catalyst.

6. A dual particle fluidized bed reaction system for carrying out the method of any one of claims 1 to 5, comprising:

the first fluidized bed reactor, the second fluidized bed reactor and the regenerator which are sequentially connected in series to form a closed loop are arranged, and the second fluidized bed reactor is positioned above the first fluidized bed reactor.

7. The dual particle fluidized bed reaction system of claim 6, wherein a cooler is connected to the first fluidized bed reactor.

8. The dual particle fluidized bed reaction system of claim 6, wherein the first fluidized bed reactor is coupled with a heavy particle catalyst dedicated regenerator.

9. The dual particle fluidized bed reaction system of claim 6, wherein the bottom of the first fluidized bed reactor is provided with a catalyst particle inlet and the top of the first fluidized bed reactor is provided with a light particle catalyst outlet.

10. The dual particle fluidized bed reaction system of claim 6, wherein the sidewall of the first fluidized bed reactor is provided with a heavy particle catalyst inlet.

Technical Field

The invention relates to the field of gas-solid phase chemical reaction, in particular to a coupling catalysis method and a coupling catalysis system for a double-particle catalyst.

Background

Gas-solid fluidized bed reactors and liquid-solid fluidized bed reactors (also known as slurry bed or suspension bed reactors) are widely used in the fields of petroleum refining, petrochemical industry, coal chemical industry and the like. The solid particles (catalyst or heat carrier) are in a fluidized state under the action of the flow force of a continuous phase (gas or liquid or gas-liquid emulsified phase), the solid particles are in good contact with the continuous phase in a suspension state, and the solid particles also have the property similar to fluid, so that the solid particles are easy to introduce, discharge and convey in a chemical reactor. The solid particles are mixed intensely in the fluidized bed reactor, so that the material concentration and the temperature of the fluidized bed reactor tend to be uniform, and the heat transfer and mass transfer rates between the continuous phase fluid and the solid particles are higher than those of other contact modes.

Most of the novel chemical reactions in fluidized bed reactors are accompanied by thermal effects, resulting in significant changes in the bed temperature, deviation of the chemical reaction temperature from the optimum conditions, and deterioration of the conversion or product selectivity. The technical method for solving the problem is mainly to lead the heat required by the reaction or the surplus heat generated by the reaction into or out of the reactor by a heat carrier of gas-phase or liquid-phase fluid (such as steam, heat conduction oil and the like) in a partition wall heat transfer mode. The heat-carrying fluid of the introduced reaction heat supply and the introduced reaction heat extraction is sent to a heating or cooling device to be heated or cooled and then is recycled to the fluidized bed reactor. This not only increases the investment costs of the plant, but also results in energy waste and a reduction in the energy efficiency of the process due to heat losses during the heating/cooling and heat transfer fluid transport processes.

In view of this, the invention is particularly proposed.

Disclosure of Invention

The invention aims to provide a double-particle catalyst coupling catalysis method and a reaction system.

The invention is realized by the following steps:

in a first aspect, the present invention provides a dual particulate catalyst coupled catalysis process comprising:

the light particle catalyst discharged from the regenerator or the light particle catalyst carrying part of the heavy particle catalyst enters a first fluidized bed reactor containing the heavy particle catalyst, the heavy particle catalyst participates in a first chemical reaction in the first fluidized bed reactor, so that a first reaction raw material is converted into a first reaction product, and the light particle catalyst supplies heat or takes heat for the first chemical reaction;

the light particle catalyst or the light particle catalyst carrying part of the heavy particle catalyst enters a second fluidized bed reactor by controlling the flow rate of carrier gas of the fluidized bed, and the light particle catalyst participates in a second chemical reaction, so that a second reaction raw material is converted into a second reaction product;

the light particle catalyst passing through the second fluidized bed reactor or the light particle catalyst carrying part of the heavy particle catalyst is conveyed to a regenerator by carrier gas for regeneration;

the light particle catalyst regenerated by the regenerator or the light particle catalyst carrying a part of the heavy particle catalyst is transported to the first fluidized bed reactor again by the carrier gas.

In an alternative embodiment, the first chemical reaction is an endothermic reaction, the temperature of the regenerated light-particle catalyst is higher than the temperature in the first fluidized bed reactor, and the regenerated light-particle catalyst is regenerated to supply heat to the first chemical reaction as a heat supply body.

In an alternative embodiment, the first chemical reaction is an exothermic reaction, the second chemical reaction is an endothermic reaction, the temperature of the regenerated light particle catalyst is lower than that in the first fluidized bed reactor, and the regenerated light particle catalyst is used as a heat sink to take away heat in the first fluidized bed reactor.

In an alternative embodiment, the particle size of the heavy particulate catalyst is greater than the particle size of the light particulate catalyst.

In an alternative embodiment, the particle density of the heavy particulate catalyst is greater than the particle density of the light particulate catalyst.

In a second aspect, the present invention provides a dual particle fluidized bed reaction system for carrying out the method according to any one of the preceding embodiments, comprising:

the first fluidized bed reactor, the second fluidized bed reactor and the regenerator which are closed loops are sequentially connected in series, and the second fluidized bed reactor is positioned above the first fluidized bed reactor.

In an alternative embodiment, a cooler is connected to the first fluidized bed reactor.

In an alternative embodiment, the first fluidized bed reactor is connected to a regenerator dedicated to the heavy particulate catalyst.

In an alternative embodiment, the bottom of the first fluidized bed reactor is provided with a catalyst particle inlet and the top of the first fluidized bed reactor is provided with a light particle catalyst outlet.

In an alternative embodiment, the side wall of the first fluidized bed reactor is provided with a heavy particulate catalyst inlet.

The invention has the following beneficial effects:

through circulation of the two kinds of particles in the system, two kinds of reactions can be realized in the same system; the continuous circulation of the light particle catalyst is separated from the contact of the heavy particle catalyst, so that the rapid heat transfer of the two particles can be realized, and when the two chemical reactions are specific reactions, the high-efficiency utilization of heat can be realized, the waste of heat is avoided, and the equipment investment is reduced. The method can be widely applied to the chemical engineering fields of petroleum refining, petrochemical industry, natural gas chemical industry, coal chemical industry, biochemical industry and the like.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.

FIG. 1 is a schematic representation of one of the three types of heavy and light particle catalysts of the present invention;

FIG. 2 is a schematic representation of one of the three types of heavy and light particle catalysts in the present invention;

FIG. 3 is a schematic representation of one of the three types of heavy and light particle catalysts in the present invention;

FIG. 4 is a schematic structural view of a double-particle fluidized bed reaction system provided in example 1 of the present invention;

FIG. 5 is a schematic structural view of a double-particle fluidized bed reaction system provided in example 2 of the present invention;

FIG. 6 is a schematic structural view of a two-particle fluidized bed reaction system provided in example 3 of the present invention.

Icon: 1-a first fluidized bed reactor; 2-regenerated catalyst line; 3-a catalyst particle inlet; 4-a heavy-particle catalyst inlet; 5-outlet of light particle catalyst; 6-a second fluidized bed reactor; 7-spent catalyst line; 8-a regenerator; 9-regenerator tonic port; 10-a regenerator dedicated for heavy particulate catalyst; 11-a cooler; 12-discharge hole.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.

The following describes the coupling catalysis method of the double-particle catalyst and the double-particle fluidized bed reaction system.

Referring to fig. 4-6, an embodiment of the present invention provides a dual-particle fluidized bed reaction system, which includes:

the first fluidized bed reactor 1, the second fluidized bed reactor 6 and the regenerator 8 which are sequentially connected in series to form a closed loop, wherein the second fluidized bed reactor 6 is positioned above the first fluidized bed reactor 1. The height of the regenerator 8 is located between the height of the first fluidized bed reactor 1 and the second fluidized bed reactor 6.

The embodiment of the invention provides a double-particle catalyst coupling catalysis method, which comprises the following steps:

the light particle catalyst discharged from the regenerator 8 or the light particle catalyst carrying a part of the heavy particle catalyst is introduced into the first fluidized bed reactor 1 containing the heavy particle catalyst, the heavy particle catalyst participates in a first chemical reaction in the first fluidized bed reactor 1, so that the first reaction raw material is converted into a first reaction product, and the light particle catalyst supplies heat or takes heat for the first chemical reaction.

The light particle catalyst or the light particle catalyst carrying part of the heavy particle catalyst enters the second fluidized bed reactor 6 by controlling the flow rate of the carrier gas of the fluidized bed, and the light particle catalyst participates in the second chemical reaction, so that the second reaction raw material is converted into a second reaction product.

The light particle catalyst passed through the second fluidized bed reactor 6 or the light particle catalyst entrained with a part of the heavy particle catalyst is transported by the carrier gas to the regenerator 8 for regeneration.

The light particle catalyst regenerated by the regenerator 8 or the light particle catalyst with a part of the heavy particle catalyst entrained therein is again transported to the first fluidized bed reactor 1 by the carrier gas.

In the following description, the first chemical reaction is expressed as an X reaction, and the second chemical reaction is expressed as a Y reaction.

According to the system and the method provided by the application, a first reaction raw material is used as a carrier gas of a heavy particle catalyst and a light particle catalyst in a first fluidized bed reactor 1, a raw material for reacting an X reaction product and a Y reaction product after passing through the first fluidized bed reactor 1 is used as a carrier gas of a light particle catalyst or a light particle catalyst carrying part of the heavy particle catalyst and entering a second fluidized bed reactor 6, and after reacting in the second fluidized bed reactor 6, the X reaction product and the Y reaction product are discharged from a discharge hole 12 at the top of the second fluidized bed reactor 6 together. After separation, the light particle catalyst or the mixed particle catalyst enters a regenerator 8 to be regenerated, and the regenerated particle catalyst returns to the first fluidized bed reactor 1 under the action of gravity. Therefore, two reactions can be carried out in the same system to produce corresponding reaction products, the light particle catalyst is separated after being continuously circulated and contacted with the heavy particle catalyst, and the quick heat transfer of the two particles can be realized.

The heavy particle catalyst is used as a catalyst for the first chemical reaction and is kept in a fluidized bed layer form in the first fluidized bed reactor 1, has the characteristics of long retention time, high concentration and the like, and fully promotes the X reaction. The existing regeneration mode is generally scorch regeneration, the regenerated particle catalyst carries higher heat, and if the reaction X is an endothermic reaction, the temperature of the regenerated light particle catalyst is higher than that in the first fluidized bed reactor 1. The regenerated light particle catalyst is regenerated and used as a heat supply body to supply heat for the first chemical reaction. If X is exothermic reaction, Y is endothermic reaction, and the temperature of the regenerated light particle catalyst is lower than the temperature in the first fluidized bed reactor 1, the regenerated light particle catalyst is used as a cold source to take away the heat in the first fluidized bed reactor 1.

Therefore, the system and the method provided by the application can realize that two reactions occur in the same system to produce two reaction products through the circulation of the two particles in the system; the continuous circulation of the light particle catalyst is separated from the contact of the heavy particle catalyst, so that the rapid heat transfer of the two particles can be realized, and when the two chemical reactions are specific reactions, the high-efficiency utilization of heat can be realized, the waste of heat is avoided, and the equipment investment is reduced.

Specifically, the heavy particle catalyst and the light particle catalyst may be in the following three forms, respectively: 1. as shown in fig. 1, the densities of the heavy and light particulate catalysts are similar, with the particle size of the heavy particulate catalyst being significantly larger than the particle size of the light particulate catalyst; 2. as shown in fig. 2, the particle sizes of the heavy and light particle catalysts are similar, with the particle density of the heavy particle catalyst being significantly greater than the density of the light particle catalyst; 3. as shown in fig. 3, the particle size and density of the heavy particulate catalyst are both greater than the particle size and density of the light particulate catalyst, respectively.

Further, the bottom of the first fluidized bed reactor 1 is provided with a catalyst particle inlet 3, and the top of the first fluidized bed reactor 1 is provided with a light particle catalyst outlet 5.

Preferably, the sidewall of the first fluidized bed reactor 1 is provided with a heavy particulate catalyst replenishment port 4.

The features and properties of the present invention are described in further detail below with reference to examples.

Example 1

As shown in fig. 4, in this example, the particle sizes of the selected heavy particle catalyst and the light particle catalyst are similar, and the particle density of the heavy particle catalyst is significantly greater than that of the light particle catalyst.

The heavy particle catalyst and the light particle catalyst and the raw materials for the X reaction and the Y reaction enter the double-particle fluidized bed reaction system through a catalyst particle inlet 3 provided at the bottom of the first fluidized bed reactor 1. The chemical reaction in the first fluidized bed reactor 1 is strong endothermic reaction and is accompanied by slow inactivation of the heavy particle catalyst, and the heat required by the X reaction is loaded by a large amount of light particle catalyst which circulates, thereby ensuring that the temperature of the particle bed layer in the first fluidized bed reactor 1 is basically constant. The reaction product X, the light-particle catalyst and a small amount of heavy-particle catalyst are together separated from the first fluidized bed reactor 1 through a light-particle catalyst outlet 5 and enter a second fluidized bed reactor 6 to promote the reaction, then the light-particle catalyst and the heavy-particle catalyst brought out of the first fluidized bed reactor 1 together with the light-particle catalyst enter a regenerator 8 through a spent catalyst pipeline 7 to be regenerated, and the regenerated light-particle catalyst and the regenerated heavy-particle catalyst are circulated back to the first fluidized bed reactor 1 through a regenerated catalyst pipeline 2. The excess heat generated by the regenerator 8 is carried by the light-particle catalyst and is properly reduced in temperature after being consumed by the first fluidized bed reactor 1, thereby bringing benefits of product value increment and heat extraction reduction to the second fluidized bed reactor 6 and the regenerator 8 thereof. The heavy particle catalyst which is slowly deactivated can continuously enter the regenerator 8 shared by the two reactors to be continuously regenerated along with the light particle catalyst, and then the heavy particle catalyst is circulated back to the first fluidized bed reactor 1, and a separate regenerator 8 for the heavy particle catalyst is not needed. The heavy particle catalyst which needs to be supplemented due to the loss in the reaction process is directly supplemented from the heavy particle catalyst supplementing port 4.

Example 2

As shown in fig. 4, the density of the heavy-particle catalyst and the light-particle catalyst selected in this example is similar, and the particle size of the heavy-particle catalyst is larger than that of the light-particle catalyst.

The heavy particle catalyst and the light particle catalyst and the raw materials for the X reaction and the Y reaction enter the double-particle fluidized bed reaction system through a catalyst particle inlet 3 provided at the bottom of the first fluidized bed reactor 1. The chemical reaction in the first fluidized bed reactor 1 is strong endothermic reaction and is accompanied by slow inactivation of the heavy particle catalyst, and the heat required by the X reaction is loaded by a large amount of light particle catalyst which circulates, thereby ensuring that the temperature of the particle bed layer in the first fluidized bed reactor 1 is basically constant. The reaction product X, the light-particle catalyst and a small amount of heavy-particle catalyst are together separated from the first fluidized bed reactor 1 through a light-particle catalyst outlet 5 and enter a second fluidized bed reactor 6 to promote the reaction, then the light-particle catalyst and the heavy-particle catalyst brought out of the first fluidized bed reactor 1 together with the light-particle catalyst enter a regenerator 8 through a spent catalyst pipeline 7 to be regenerated, and the regenerated light-particle catalyst and the regenerated heavy-particle catalyst are circulated back to the first fluidized bed reactor 1 through a regenerated catalyst pipeline 2. The excess heat generated by the regenerator 8 is carried by the light-particle catalyst and is properly reduced in temperature after being consumed by the first fluidized bed reactor 1, thereby bringing benefits of product value increment and heat extraction reduction to the second fluidized bed reactor 6 and the regenerator 8 thereof. The heavy particle catalyst which is slowly deactivated can continuously enter the regenerator 8 shared by the two reactors to be continuously regenerated along with the light particle catalyst, and then the heavy particle catalyst is circulated back to the first fluidized bed reactor 1, and a separate regenerator 8 for the heavy particle catalyst is not needed. The heavy particle catalyst which needs to be supplemented due to the loss in the reaction process is directly supplemented from the heavy particle catalyst supplementing port 4.

Example 3

As shown in fig. 5, in the double-particle fluidized bed reaction system provided in this embodiment, the first fluidized bed reactor 1 is connected to a regenerator 10 dedicated to the heavy particle catalyst.

In this example, the particle sizes of the selected heavy particle catalyst and the light particle catalyst are similar, and the particle density of the heavy particle catalyst is significantly greater than that of the light particle catalyst.

The heavy particle catalyst and the light particle catalyst and the raw materials for the X reaction and the Y reaction enter the double-particle fluidized bed reaction system through a catalyst particle inlet 3 provided at the bottom of the first fluidized bed reactor 1. The chemical reaction in the first fluidized bed reactor 1 is strong endothermic reaction and is accompanied by slow inactivation of the heavy particle catalyst, and the heat required by the X reaction is loaded by a large amount of light particle catalyst which circulates, thereby ensuring that the temperature of the particle bed layer in the first fluidized bed reactor 1 is basically constant. The reaction product X and the light-particle catalyst are separated from the first fluidized bed reactor 1 through a light-particle catalyst outlet 5 and enter a second fluidized bed reactor 6 to promote the reaction, then the light-particle catalyst enters a regenerator 8 through a spent catalyst pipeline 7, and the regenerated light-particle catalyst is circulated back to the first fluidized bed reactor 1 through a regenerated catalyst pipeline 2. The excess heat generated by the regenerator 8 is carried by the light-particle catalyst and is properly reduced in temperature after being consumed by the first fluidized bed reactor 1, thereby bringing benefits of product value increment and heat extraction reduction to the second fluidized bed reactor 6 and the regenerator 8 thereof. The slowly deactivated heavy particulate catalyst is periodically or continuously regenerated in a heavy particulate catalyst dedicated regenerator 10 and then recycled back to the first fluidized bed reactor 1. The heavy particulate catalyst to be replenished in the course of the reaction due to the loss is directly supplied from the heavy particulate catalyst replenishing port 4 or supplied through the regenerator replenishing port 9 thereof.

Example 4

As shown in fig. 6, in the double-particle fluidized-bed reaction system of the present embodiment, the first fluidized-bed reactor 1 is connected to a cooler 11.

The particle size and density of the heavy particle catalyst selected in this example were both greater than the particle size and density of the light particle catalyst, respectively.

The heavy particle catalyst and the light particle catalyst and the raw materials for the X reaction and the Y reaction enter the double-particle fluidized bed reaction system through a catalyst particle inlet 3 provided at the bottom of the first fluidized bed reactor 1. The chemical reaction taking place in the first fluidized bed reactor 1 is a strongly exothermic reaction, but the regeneration of the heavy particle catalyst is substantially not required. One part of heat generated by the X reaction is taken out by the light particle catalyst, and the other part of heat is taken out by a cooler 11 which is specially and independently arranged for the heavy particle catalyst, so that the temperature of a particle bed layer in the first fluidized bed reactor 1 is ensured to be basically constant. The reaction product X and the light-particle catalyst are separated from the first fluidized bed reactor 1 through a light-particle catalyst outlet 5 and enter a second fluidized bed reactor 6 to promote the reaction, the regenerated light-particle catalyst is circulated back to the first fluidized bed reactor 1 through a regenerated catalyst pipeline 2, and the regenerated light-particle catalyst is circulated back to the first fluidized bed reactor 1 through the regenerated catalyst pipeline 2. The heat generated in the process of the regenerator 8 is not enough to ensure that the light-particle catalyst can stably supply heat to the second fluidized bed reactor 6, and the temperature of the light-particle catalyst can be moderately increased after passing through the first fluidized bed reactor 1, so that the second fluidized bed reactor 6 and the regenerator 8 thereof are increased in value and the benefit of heat supplement is reduced. The heavy particle catalyst which needs to be supplemented due to the loss in the reaction process is directly supplemented from the heavy particle catalyst supplementing port 4.

Examples of the experiments

The reaction methods provided in examples 1 to 3 were put into practical use.

The X reaction is low-carbon alkane dehydrogenation reaction, the reaction raw material is propane with the purity of 99.9 percent, and the heavy particle catalyst is CrOx/Al₂O₃(ii) a The Y reaction is aromatization reaction, the reaction raw material is catalytic gasoline, and the light particle catalyst is HZSM-5 molecular sieve.

Tables 1-3 show the specific parameters for practical operation of the process provided in examples 1-3. The composition of the product obtained from the reaction is reported in table 4.

TABLE 1 catalytic gasoline Properties

TABLE 2 catalyst Components

TABLE 3 Main Process conditions

TABLE 4 product distribution and Properties

In summary, the system and method provided by the present application can realize two different types of reactions in the same system by circulating two types of particles in the system; the continuous circulation of the light particle catalyst is separated from the contact of the heavy particle catalyst, so that the rapid heat transfer of the two particles can be realized, and when the two chemical reactions are specific reactions, the high-efficiency utilization of heat can be realized, the waste of heat is avoided, and the equipment investment is reduced. The method can be widely applied to the chemical engineering fields of petroleum refining, petrochemical industry, natural gas chemical industry, coal chemical industry, biochemical industry and the like.

The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.