A heating control method for a multi-stage fluidized circulation reaction system

Abstract

The present invention provides a multi-stage fluidized circulation reaction system and its heating control method, belonging to the technical field of fluidized bed reactors. The system includes: a regenerator for introducing a catalyst and a first reaction gas, where the catalyst forms a fluidized bed layer under the action of the first reaction gas and undergoes regeneration, and the regenerator is provided with a first light-transmitting area; a first heater for heating the regenerator; a riser reactor connected to the regenerator through a first pipeline, a first control valve is provided on the first pipeline, and the riser reactor is also used for introducing a second reaction gas to produce downstream products, and the riser reactor is provided with a second light-transmitting area; a second heater for heating the riser reactor; a settler connected to the riser reactor for settling the catalyst and discharging the downstream products, and the settler is also connected to the regenerator through a second pipeline, and a second control valve is provided on the second pipeline. The present invention can achieve the efficient progress of the chemical looping reaction and the recycling of the catalyst.

Description

Technical Field

[0001] The present application relates to the technical field of fluidized reactors, and in particular to a multi-stage fluidized circulation reaction system and a heating control method thereof. Background Art

[0002] In recent years, photothermal catalytic technology has shown broad application prospects in the fields of energy and environment. The process relies on the catalyst to absorb light energy and convert it into heat energy to drive the reaction, avoiding the overall heating of the reactor and making the reaction conditions milder. At the same time, the auxiliary effect of light also makes the catalyst show significantly higher performance than simple photocatalytic or thermal catalytic activity. However, most of the existing photothermal reactors are fixed bed type, which has problems such as small light receiving area and low heat transfer efficiency, making it difficult to achieve industrial application of photothermal catalysis. The fluidized bed reactor (FBR) is a reaction device that suspends solid particles (usually catalysts or reactants) in a fluid-like state by passing gas or liquid through them at high speed. In the fluidized bed, the gas-solid phase reaction mainly occurs at the interface between the particulate material and the reaction gas. Due to the continuous movement and mixing of the particles, the reaction interface is constantly updated, thereby reducing the shielding of light by the catalyst and improving the utilization efficiency of light.

[0003] The existing photothermal fluidized bed reactor is a single-stage structure and is not suitable for chemical chain reaction processes. Therefore, providing an efficient photothermal reaction system that can be applied to chemical chain reaction processes is a technical problem that needs to be solved urgently in this field. Summary of the invention

[0004] One object of the first aspect of the present invention is to provide a multi-stage fluidized circulation reaction system that can achieve efficient chemical chain reaction and recycling of catalysts.

[0005] Another object of the present invention is to give full play to the photothermal synergistic effect.

[0006] A further object of the present invention is to adapt to multi-scenario chemical chain catalysis processes and large-scale production.

[0007] An object of the second aspect of the present invention is to provide a heating control method for the above-mentioned multi-stage fluidized cycle reaction system, which can save energy while ensuring efficient reaction.

[0008] An embodiment of the present invention provides a multi-stage fluidized cycle reaction system, comprising:

[0009] A regenerator, used for introducing a catalyst and a first reaction gas, wherein the catalyst forms a fluidized bed layer and is regenerated under the action of the first reaction gas, and the regenerator is provided with a first light-transmitting area for transmitting light;

[0010] The first heater is used to heat the regenerator;

[0011] The riser reactor is connected to the regenerator through a first pipeline to introduce the catalyst. A first control valve is provided on the first pipeline. The riser reactor is also used to introduce a second reaction gas to produce downstream products. The riser reactor is provided with a second light-transmitting area for transmitting light;

[0012] The second heater is used to heat the riser reactor;

[0013] The settler is connected to the riser reactor and is used to settle the catalyst and discharge the downstream products. The settler is also connected to the regenerator through a second pipeline to recycle the catalyst to the regenerator. A second control valve is provided on the second pipeline.

[0014] Further, the multistage fluidized circulation reaction system further includes a cyclone separator, both ends of which are communicated with the regenerator. The cyclone separator is used to separate the gas and the catalyst.

[0015] Further, the multistage fluidized circulation reaction system further includes a storage tank for storing the catalyst. The storage tank is connected to the regenerator through a third pipeline. A third control valve is provided on the third pipeline.

[0016] Further, the multistage fluidized circulation reaction system further includes:

[0017] The first flowmeter is used to detect the flow rate of the first reaction gas;

[0018] The first pressure sensor is used to detect the pressure inside the regenerator;

[0019] The first temperature sensor is used to detect the temperature inside the regenerator;

[0020] The second flowmeter is used to detect the flow rate of the second reaction gas;

[0021] The second pressure sensor is used to detect the pressure inside the riser reactor;

[0022] The second temperature sensor is used to detect the temperature inside the riser reactor.

[0023] Further, the materials of the first light-transmitting area and the second light-transmitting area are quartz.

[0024] Further, both the first heater and the second heater are heating jackets.

[0025] Further, both the first heater and the second heater are set to be liftable.

[0026] In particular, an embodiment of the present invention further provides a heating control method for the multi-stage fluidized circulation reaction system described in any one of the above, including:

[0027] Detect the first current temperature in the regenerator, the second current temperature in the riser reactor, and the current light intensity;

[0028] Control the target heating power and target height of the first heater according to the changes in the first current temperature and light intensity;

[0029] Control the target heating power and target height of the second heater according to the changes in the second current temperature and light intensity.

[0030] Furthermore, in the step of controlling the target heating power and target height of the first heater according to the changes in the first current temperature and light intensity, the control target is to minimize the sum of the power required for the changes in the target heating power and height of the first heater.

[0031] Furthermore, determine the target heating power and target height of the first heater according to the following formula:

[0032]

[0033] Q l = k1 * I * (h - h1);

[0034] Q h = k2 * P1 * h1;

[0035] P2 = k3 * (h a - h1);

[0036] Wherein, Q re is the required heat corresponding to the reaction temperature, I is the current light intensity, I a is the changed light intensity, h is the height of the first light-transmitting area, h1 is the height of the first heater covering the first light-transmitting area currently, h a is the target height of the first heater, Q l is the heat provided by the current light, k1 is the light power coefficient, Q h is the heat provided by the first heater currently, P1 is the power of the first heater currently, k2 is the heating power coefficient, P2 is the power required for the first heater to rise from h1 to h a , and k3 is the lifting power coefficient.

[0037] According to the first aspect of the present invention, a multi-stage fluidized circulation reaction system is provided. Through the coupled design of a fluidized bed (i.e., the form in the regenerator) and a riser reactor, the efficient progress of the chemical looping reaction and the recycling of the catalyst are realized. This system can couple a gas-solid fluidized bed (i.e., the regenerator) and a riser reactor, enabling the reaction gas to come into full contact with the catalyst, and having the advantages of high mass transfer and heat transfer efficiency.

[0038] Furthermore, since the regenerator and the riser reactor are respectively provided with a light-transmitting area and a heater, the synergistic effect of light and heat can be fully exerted, and at the same time, the pain points of the existing photo-thermal fluidized bed reactor that cannot be applied to the chemical looping reaction can be solved, such as the problem of chemical looping reaction for ammonia synthesis.

[0039] Furthermore, this system can also realize the coupling processes such as catalyst reaction-regeneration, endothermic-exothermic, etc., and is applicable to chemical looping catalytic processes in various scenarios such as photocatalysis, thermal catalysis, and photo-thermal synergistic catalysis, and is suitable for large-scale production.

[0040] According to the second aspect of the present invention, a heating control method for the above multi-stage fluidized circulation reaction system is also provided. By calibrating in advance the relationship between each power and heat, the corresponding calibration coefficient is determined, and then with the goal of minimizing the sum of the target heating power of each heater and the power required for height change, the target heating power and target height of each heater are obtained, so as to achieve the purpose of keeping the reaction temperature constant and minimizing the input power, thereby reducing the input energy consumption and saving energy while ensuring the efficient progress of the reaction. Description of the Drawings

[0041] Figure 1 It is a schematic structural diagram of a multi-stage fluidized circulation reaction system according to an embodiment of the present invention;

[0042] Figure 2 It is a flowchart of a heating control method for a multi-stage fluidized circulation reaction system according to an embodiment of the present invention;

[0043] Reference Signs:

[0044] 100 - multi-stage fluidized circulation reaction system, 10 - regenerator, 11 - first light-transmitting area, 20 - riser reactor, 30 - settler, 40 - storage tank, 50 - first pipeline, 51 - first control valve, 60 - second pipeline, 61 - second control valve, 70 - cyclone separator, 80 - third pipeline, 81 - third control valve. Detailed Embodiments

[0045] To make the above objects, features, and advantages of the present application more apparent and understandable, the following provides a detailed description of the specific embodiments of the present application with reference to the accompanying drawings. Many specific details are set forth in the following description to facilitate a full understanding of the present application. However, the present application can be implemented in many other ways different from those described herein, and those skilled in the art can make similar improvements without departing from the connotation of the present application. Therefore, the present application is not limited by the specific embodiments disclosed below.

[0046] It should be noted that when a component is referred to as being "fixed to" or "disposed on" another component, it can be directly on the other component or there can also be an intermediate component. When a component is considered to be "connected" to another component, it can be directly connected to the other component or there may be an intermediate component at the same time. The terms "vertical", "horizontal", "upper", "lower", "left", "right" and similar expressions used in the specification of the present application are only for illustrative purposes and do not represent the only implementation manner.

[0047] In addition, the terms "first" and "second" are only used for descriptive purposes and cannot be understood as indicating or implying relative importance or implicitly specifying the quantity of the indicated technical features. Thus, the features defined with "first" and "second" may explicitly or implicitly include at least one of such features. In the description of the present application, the meaning of "a plurality" is at least two, such as two, three, etc., unless otherwise specifically and clearly defined.

[0048] In the present application, unless otherwise clearly specified and limited, the first feature being "on" or "under" the second feature can be that the first feature is in direct contact with the second feature, or the first feature is indirectly in contact with the second feature through an intermediate medium. Moreover, the first feature being "above", "over" and "on top of" the second feature can be that the first feature is directly above or obliquely above the second feature, or only indicates that the first feature has a higher horizontal height than the second feature. The first feature being "under", "beneath" and "underneath" the second feature can be that the first feature is directly below or obliquely below the second feature, or only indicates that the first feature has a lower horizontal height than the second feature.

[0049] Unless otherwise defined, all technical and scientific terms used in the specification of the present application have the same meaning as commonly understood by those skilled in the technical field to which the present application pertains. The terms used in the specification of the present application are only for the purpose of describing specific embodiments and are not intended to limit the present application. The term "and / or" used in the specification of the present application includes any and all combinations of one or more of the related listed items.

[0050] Figure 1 It is a schematic structural diagram of a multi-stage fluidized circulation reaction system 100 according to an embodiment of the present invention. As Figure 1As shown, in one embodiment, the multi-stage fluidized circulation reaction system 100 includes a regenerator 10, a first heater (not shown), a riser reactor 20, a second heater (not shown), and a settling zone 30. The regenerator 10 is used to introduce a catalyst and a first reaction gas (see Figure 1 at location A). The catalyst forms a fluidized bed layer under the action of the first reaction gas and is regenerated. The regenerator 10 is provided with a first light-transmitting region 11 for transmitting light. That is to say, the catalyst mentioned in this application is a catalyst in a solid particle state, and the regenerator 10 is used to regenerate the catalyst. The first heater is used to heat the regenerator 10. The riser reactor 20 is connected to the regenerator 10 through a first pipeline 50 to introduce the catalyst. A first control valve 51 is provided on the first pipeline 50. The riser reactor 20 is also used to introduce a second reaction gas (see Figure 1 at location B) to produce downstream products (see Figure 1 at location C). The riser reactor 20 is provided with a second light-transmitting region for transmitting light, and the second light-transmitting region can be the side wall of the riser. The first light-transmitting region 11 and the second light-transmitting region here can be quartz light windows or other common light-transmitting methods, which are not limited herein. The second heater is used to heat the riser reactor 20. The first heater and the second heater can be heating jackets sleeved on the regenerator 10 or heating wires fixedly wound on the outside of the regenerator 10, etc., which are not limited herein. The settling zone 30 is connected to the riser reactor 20 and is used to settle the catalyst and discharge the downstream products. The settling zone 30 is also connected to the regenerator 10 through a second pipeline 60 to return the catalyst to the regenerator 10. A second control valve 61 is provided on the second pipeline 60. The catalyst, the first reaction gas, and the second reaction gas here can be adjusted according to the target reaction, which is not limited herein. For example, the catalyst here can be an iron-based or ruthenium-based catalyst (Fe / K / Al2O3, Ru / C), the first reaction gas can be N2 or air + O2 or a small amount of H2, which is used to remove impurities on the catalyst surface and regenerate the active sites, and the second reaction gas can be N2 and H2 to produce NH3 under high temperature and high pressure. The catalyst can also be Ni / Al2O3, Cu / ZnO / Al2O3, Fe / Mn / K / C, the first reaction gas can be CO2 and H2 (or air), which is used for carbon deposition oxidation and heat treatment, and the second reaction gas can be CO and H2 (CO2 and H2) to carry out chain growth reactions to produce alkanes, alcohols, or olefins, etc. Or, the catalyst is Co3Mo3N, the first reaction gas is H2 and N2, and the second reaction gas is CO2 and H2 to produce CO and high-concentration NH3.

[0051] This embodiment provides a multistage fluidized bed circulation reaction system 100. Through the coupled design of a fluidized bed (i.e., the form in the regenerator 10) and a riser reactor 20, the efficient progress of the chemical looping reaction and the recycling of the catalyst are realized. This system can couple a gas-solid fluidized bed (i.e., the regenerator 10) and a riser reactor 20, enabling the reaction gas to fully contact the catalyst, and having the advantages of high mass transfer and heat transfer efficiency.

[0052] Furthermore, since the regenerator 10 and the riser reactor 20 are respectively provided with a light-transmitting area and a heater, the synergistic effect of light and heat can be fully exerted, and at the same time, the pain points of the existing photo-thermal fluidized bed reactor that cannot be applied to the chemical looping reaction can be solved, such as the problem of chemical looping reaction for ammonia synthesis.

[0053] In addition, this system can also realize the coupled processes such as catalyst reaction-regeneration, endothermic-exothermic, etc., and is applicable to the chemical looping catalytic processes in various scenarios such as photocatalysis, thermal catalysis, and photo-thermal synergistic catalysis, and is suitable for large-scale production.

[0054] In a further embodiment, as Figure 1 shown, the multistage fluidized bed circulation reaction system 100 further includes a cyclone separator 70, both ends of which are connected to the regenerator 10. The cyclone separator 70 is used to separate gas and catalyst.

[0055] In this embodiment, by setting the cyclone separator 70, the separation of catalyst solid particles and reaction gas can be effectively carried out, so that the catalyst is continuously separated and then re-enters the regenerator 10 for regeneration, realizing the efficient activation of the catalyst. For example, when using Co3Mo3N to produce ammonia, the removal of the passivation layer on the catalyst surface and the replenishment of surface nitrogen and hydrogen species can be realized.

[0056] In one embodiment, the multistage fluidized bed circulation reaction system 100 further includes a storage tank 40 for storing the catalyst. The storage tank 40 is connected to the regenerator 10 through a third pipeline 80, and a third control valve 81 is provided on the third pipeline 80. The multistage fluidized bed circulation reaction system 100 further includes a first flowmeter, a first temperature sensor, a second flowmeter, a second pressure sensor, and a second temperature sensor. The first flowmeter is used to detect the flow rate of the first reaction gas. The first pressure sensor is used to detect the pressure in the regenerator 10. The first temperature sensor is used to detect the temperature in the regenerator 10. The second flowmeter is used to detect the flow rate of the second reaction gas. The second pressure sensor is used to detect the pressure in the riser reactor 20. The second temperature sensor is used to detect the temperature in the riser reactor 20. The materials of the first light-transmitting area 11 and the second light-transmitting area are quartz.

[0057] In a further embodiment, both the first heater and the second heater are heating jackets, and both are arranged to be liftable. For example, they are both driven by a motor-driven lead screw mechanism, or a rack and pinion mechanism, etc. Here, there is no limitation on the lifting drive mechanism of the heating jacket, as long as the heating jacket can be controllably lifted. Here, the lifting mechanisms of the two heating jackets, the first flowmeter, the first temperature sensor, the second flowmeter, the second pressure sensor, the second temperature sensor, the first control valve 51, the second control valve 61, and the third control valve 81 can all be connected to the controller to achieve automatic control of the reaction.

[0058] Taking the catalyst as Co3Mo3N, the first reaction gas as H2 and N2, and the second reaction gas as CO2 and H2 as an example, the control process of the multi-stage fluidized circulation reaction system 100 includes the following steps:

[0059] S1: Transfer the catalyst. Control the third control valve 81 to open to connect the storage tank 40 and the regenerator 10, so that Co3Mo3N in the storage tank 40 is transferred to the regenerator 10 through the third pipeline 80, and close the third control valve 81 after introducing the required amount of Co3Mo3N. At this time, the catalyst is in a state of surface oxidation and contains C species.

[0060] S2: Pretreat the catalyst. Introduce a mixture of N2 and H2 with a preset flow rate into the regenerator 10, with a ratio of 1:3, until Co3Mo3N is in a suspended fluidized state, and at the same time turn on the first heater and the cyclone separator 70. At this time, the gas blows the catalyst in the regenerator 10 through the cyclone separator 70 to complete gas-solid separation, and the catalyst flows back into the regenerator 10 to complete the cycle, so as to remove the passivation layer on the catalyst surface, supplement the surface nitrogen and hydrogen species, and realize the activation of the catalyst.

[0061] S3: Start the ammonia synthesis reaction. Introduce a high flow rate of CO2 and H2 into the riser reactor 20, with a ratio of 1:3. After the gas flow is stable, open the first control valve 51 on the first pipeline 50, so that the catalyst flows into the riser reactor 20, and enters the settling zone 30 under the action of the gas flow of the CO2 and H2 mixture. At the same time, turn on the second heater to provide the heat required for the reaction temperature. The CO2-induced hydrogenation of nitrogen and hydrogen species to produce NH3 and the CO2 hydrogenation reaction are carried out in the riser reactor 20. After the catalyst reacts in the riser reactor 20, it flows into the settling zone 30. Due to the rapid widening of the pipe diameter in the gas flow direction, the catalyst quickly settles, and the product gas and the unreacted gas flow out from the top outlet of the settling zone 30 for product separation.

[0062] S4: Catalyst regeneration. Open the second control valve 61 on the second pipeline 60 to allow the catalyst in the settling zone 30 to flow into the regenerator 10 through the second pipeline 60 for catalyst regeneration. The regeneration process includes the replenishment of nitrogen and hydrogen species and the removal of CO2 hydrogenation intermediate species. The catalyst at this time is fresh Co3Mo3NH containing x species. x form.

[0063] S5: Achieve cyclic reaction. Close the third control valve 81, open the first control valve 51 and the second control valve. The catalyst can circulate between the regenerator 10, the riser reactor 20, and the settling zone 30 through the first pipeline 50 and the second pipeline 60 to achieve the stable production of NH3 and CO2 hydrogenation products (C1 products), that is, to achieve the steady-state production of chemical-looping ammonia synthesis products.

[0064] Among them, the reaction temperature of the riser reactor 20 and the regenerator 10 is any value between 200°C and 600°C, such as 200°C, 300°C, 400°C, 500°C, or 600°C, or any other value between 200°C and 600°C, which is not limited here. The superficial linear velocity of the first reaction gas is any value between 0.5 m / s and 2.0 m / s, such as the superficial linear velocity is 0.5 m / s, 0.8 m / s, 1 m / s, 1.5 m / s, 1.8 m / s, or 2.0 m / s, or any other value between 0.5 m / s and 2.0 m / s, which is not limited here. The bed density is 100 kg / m 3 -800 kg / m 3 any value, such as the bed density is 100 kg / m 3 、200 kg / m 3 、300 kg / m 3 、500 kg / m 3 、600 kg / m 3 、700 kg / m 3 or 800 kg / m 3 , or it can also be 100 kg / m 3 -800 kg / m 3Any other value among them is not restricted herein. The gas flow rates of N2 and H2 are any value in the range of 100 ml / min to 10000000 ml / min, such as 100 ml / min, 500 ml / min, 1000 ml / min, 2000 ml / min, 5000 ml / min, 10000 ml / min, 50000 ml / min, 100000 ml / min, 150000 ml / min, 500000 ml / min, 2000000 ml / min, 5000000 ml / min or 10000000 ml / min, or any other value in the range of 100 ml / min to 10000000 ml / min, which is not restricted herein. The ratio of the gas flow rates of N2 and H2 is any value in the range of 1:1 to 20, such as the ratio of 1:1, 1:3, 1:5, 1:10, 1:15 or 1:20, or any other value in the range of 1:1 to 20, which is not restricted herein. The gas flow rates of CO2 and H2 are 100 - 10000000 ml / min, such as 100 ml / min, 600 ml / min, 1200 ml / min, 2000 ml / min, 4000 ml / min, 10000 ml / min, 50000 ml / min, 100000 ml / min, 150000 ml / min, 500000 ml / min, 2000000 ml / min, 5000000 ml / min or 10000000 ml / min, or any other value in the range of 100 ml / min to 10000000 ml / min, which is not restricted herein. The ratio of the gas flow rates of CO2 and H2 is any value in the range of 1:1 to 20, such as the ratio of 1:1, 1:3, 1:5, 1:10, 1:15 or 1:20, or any other value in the range of 1:1 to 20, which is not restricted herein. The mass of the catalyst is any value in the range of 1 g to 1000000 g, such as the catalyst mass of 1 g, 50 g, 200 g, 1000 g, 5000 g, 10000 g, 100000 g, 500000 g or 1000000 g, or any other value in the range of 1 g to 1000000 g, which is not restricted herein. The particle size of the catalyst is any value in the range of 0.01 mm to 30 mm, such as the particle size of 0.01 mm, 0.1 mm, 1 mm, 2 mm, 5 mm, 10 mm, 20 mm or 30 mm, or any other value in the range of 0.01 mm to 30 mm, which is not restricted herein. The pressure in the regenerator 10 or the riser reactor 20 is any value in the range of 100 kPa to 30 MPa, such as the pressure of 100 kPa, 300 kPa, 500 kPa, 1 MPa, 5 MPa, 16 MPa, 20 MPa, 27 MPa or 30 MPa, and can also be any other value in the range of 100 kPa to 30 MPa, which is not restricted herein.The thickness of the quartz optical windows in the riser reactor 20 and the regenerator 10 is any value from 1 mm to 100 mm, such as 1 mm, 5 mm, 40 mm, 70 mm, 80 mm or 100 mm, or any other value within 1 mm - 100 mm, which is not limited herein.

[0065] Figure 2 It is a flowchart of the heating control method for the multi-stage fluidized circulation reaction system 100 according to an embodiment of the present invention. In one embodiment, in order to maximize the utilization of solar energy, the entire areas of the regenerator 10 and the riser reactor 20 are made of quartz material, that is, the entire areas are light-transmissive. The first heater and the second heater are respectively heating jackets sleeved on the outer peripheral sides of the regenerator 10 and the riser reactor 20. The regenerator 10 provides heat through natural light irradiation and / or the first heater, and the riser reactor 20 provides heat through natural light irradiation and / or the second heater. When the overlapping area between the heating jacket and the regenerator 10 increases, it means that the area of the first light-transmissive region 11 of the regenerator 10 decreases. The same principle applies to the riser reactor 20, and the target temperature is achieved through the coordinated cooperation of light irradiation and the heating jacket. For the multi-stage fluidized circulation reaction system 100 of this embodiment, the present application also provides a corresponding heating control method, as Figure 2 shown, the heating control method includes:

[0066] Step S100, detecting the first current temperature in the regenerator 10, the second current temperature in the riser reactor 20, and the current light intensity;

[0067] Step S200, controlling the target heating power and target height of the first heater according to the changes in the first current temperature and light intensity;

[0068] Step S300, controlling the target heating power and target height of the second heater according to the changes in the second current temperature and light intensity.

[0069] In one embodiment, in step S200, the control target is to minimize the sum of the power required for the target heating power and height change of the first heater. In step S300, the control target is to minimize the sum of the power required for the target heating power and height change of the second heater.

[0070] In one embodiment, the target heating power and target height of the first heater are determined according to the following formula:

[0071]

[0072] Q l = k1 * I * (h - h1) (2);

[0073] Q h = k2 * P1 * h1 (3);

[0074] P2 = k3 * (h a - h1) (4);

[0075] Wherein, Q re is the required heat corresponding to the reaction temperature, I is the current light intensity, I a is the changed light intensity (i.e., the light intensity measured after the light fluctuates), h is the height of the first light-transmitting area 11, h1 is the height of the current first heater covering the first light-transmitting area 11, h a is the target height of the first heater, Q l is the heat provided by the current light, k1 is the light power coefficient, Q h is the heat provided by the current first heater, P1 is the power of the current first heater, k2 is the heating power coefficient, P2 is the power required for the first heater to rise from h1 to h a and k3 is the power increase coefficient.

[0076] Formula (2) expresses the linear relationship between the light intensity and the heat provided by the light, formula (3) expresses the linear relationship between the power of the first heater and the heat it provides, formula (4) expresses the linear relationship between the power required for the first heater to rise and the increased heat after the rise. Among them, the light power coefficient k1, the heating power coefficient k2, and the power increase coefficient k3 can all be determined through calibration experiments. For example, for the light power coefficient k1, by changing the light intensity and then measuring the temperature change in the regenerator 10, the light power coefficient k1 can be obtained through multiple experimental values. The heating power coefficient k2 and the power increase coefficient k3 can also be obtained through similar calibration experiments, which are not limited here. When Q l and Q h are in J, the unit of I is mW / cm 2 , the units of h, h1, and h a are in cm, and the units of P1 and P2 are in kW, the unit of the light power coefficient k1 is J·cm / mW, the unit of the heating power coefficient k2 is J / kW·cm, and the unit of the power increase coefficient k3 is kW / cm. Of course, when Q l , I, h, and h1 adopt other units, the units of the light power coefficient k1, the heating power coefficient k2, and the power increase coefficient k3 can be adapted accordingly, which are not limited here.

[0077] After obtaining the light power coefficient k1, the heating power coefficient k2, and the power increase coefficient k3, assuming that the first heater is at the target height h a and the target heating power is P aWhen the sum of the target heating power of the first heater and the power required for height change is minimized, at this time, the heat Q provided by the first heater ha can be expressed as k2*P a *h a , and the heat Q provided by light irradiation la can be expressed as k1*I a *(h - h a ), Q ha +Q la =Q re , therefore, P a can be expressed as From this, formula (1) is obtained, and then the target height h that meets the conditions is calculated according to formula (1) a and the target heating power is P a .

[0078] Similarly, the target heating power and target height of the second heater can also be determined with reference to the foregoing formula, which will not be elaborated here.

[0079] The heating control method of the present application determines the corresponding calibration coefficients through the relationship between each power and heat calibrated in advance, and then takes the minimum sum of the target heating power of each heater and the power required for height change as the control target, and obtains the target heating power and target height of each heater, so as to achieve the purpose of keeping the reaction temperature constant and minimizing the input power, thereby reducing the input energy consumption and saving energy while ensuring the efficient progress of the reaction.

[0080] The above embodiments only represent several implementation manners of the present invention, and their descriptions are relatively specific and detailed, but they should not be construed as limiting the scope of the invention patent. It should be noted that for those of ordinary skill in the art, without departing from the concept of the present invention, several modifications and improvements can still be made, and these all belong to the protection scope of the present invention. Therefore, the protection scope of the invention patent should be subject to the appended claims.

Claims

1. A heating control method for a multi-stage fluidized cycle reaction system, characterized in that: The multi-stage fluidized circulation reaction system comprises: A regenerator, used for introducing a catalyst and a first reaction gas, wherein the catalyst forms a fluidized bed layer and is regenerated under the action of the first reaction gas, and the regenerator is provided with a first light-transmitting area for transmitting light; a first heater, for heating the regenerator; A riser reactor connected to the regenerator through a first pipeline for introducing the catalyst, the first pipeline being provided with a first control valve, the riser reactor being further used for introducing a second reaction gas to generate a downstream product, and the riser reactor being provided with a second light-transmitting area for transmitting light; a second heater for heating the riser reactor; A settler connected to the riser reactor for settling the catalyst and discharging the downstream product, the settler is also connected to the regenerator via a second pipeline to reflux the catalyst to the regenerator, and a second control valve is provided on the second pipeline; The first heater is a heating sleeve, and the first heater is arranged to be liftable; The heating control method comprises: detecting a first current temperature and a current light intensity in the regenerator; Controlling the target heating power and the target height of the first heater according to the changes of the first current temperature and the light intensity, with the sum of the target heating power of the first heater and the power required for the height change being minimized as a control target; The target heating power and target height of the first heater are determined according to the following formula: Q l =k1*I*(h-h1); Q h =k2*P1*h1; P2=k3*(h a -h1); Among them, Q re is the required heat corresponding to the reaction temperature, I is the current light intensity, and I a is the changed light intensity, h is the height of the first light-transmitting area, h1 is the height of the first heater currently covering the first light-transmitting area, and h a is the target height of the first heater, Q l is the heat provided by the current light, k1 is the light power coefficient, Q h is the heat currently provided by the first heater, P1 is the current power of the first heater, k2 is the heating power coefficient, and P2 is the power of the first heater increased from h1 to h a The power required, k3 improves the power coefficient.

2. The heating control method for a multi-stage fluidized cycle reaction system according to claim 1, characterized in that: The second heater is a heating sleeve, and the second heater is arranged to be liftable; The heating control method further comprises: detecting a second current temperature and a current light intensity in the riser reactor; The target heating power and the target height of the second heater are controlled according to changes in the second current temperature and the light intensity.

3. The heating control method for a multi-stage fluidized cycle reaction system according to claim 1, characterized in that: The multi-stage fluidized cycle reaction system further comprises a cyclone separator, both ends of which are connected to the regenerator, and the cyclone separator is used to separate the gas and the catalyst.

4. The heating control method for a multi-stage fluidized cycle reaction system according to claim 3, characterized in that: The multi-stage fluidized circulation reaction system also includes a storage tank for storing the catalyst. The storage tank is connected to the regenerator via a third pipeline. A third control valve is disposed on the third pipeline.

5. The heating control method for a multi-stage fluidized cycle reaction system according to claim 4, characterized in that: The multi-stage fluidized circulation reaction system also includes: A first flow meter, used to detect the flow rate of the first reaction gas; A first pressure sensor, used to detect the pressure in the regenerator; A first temperature sensor, used to detect the temperature in the regenerator; A second flow meter, used to detect the flow rate of the second reaction gas; a second pressure sensor for detecting the pressure in the riser reactor; The second temperature sensor is used to detect the temperature inside the riser reactor.

6. The heating control method for a multi-stage fluidized circulation reaction system according to any one of claims 1 to 5, characterized in that: The first light-transmitting region and the second light-transmitting region are made of quartz.

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