A modeling method and device for catalytic cracking oxygen-depleted regeneration system

Abstract

The present invention discloses a modeling method and device for a catalytic cracking oxygen-depleted regeneration system, and relates to the technical field of catalytic cracking. The modeling method for a catalytic cracking oxygen-depleted regeneration system includes: establishing a charring reaction kinetic model, establishing an oxygen-depleted regeneration system correction model, and establishing a regenerator steady-state model. After establishing the charring reaction kinetic model, the oxygen-depleted regeneration system correction model is established to effectively correct the reaction rate. For the oxygen-depleted regeneration system, the accuracy of the prediction of the regenerated flue gas composition can be effectively improved, and the catalyst carbon can be determined more accurately, which is of great significance for guiding the optimized operation of the catalytic cracking oxygen-depleted regeneration device.

Description

Technical Field

[0001] The present invention relates to the technical field of catalytic cracking, and in particular to a modeling method and a device for a catalytic cracking oxygen-depleted regeneration system. Background Art

[0002] The construction scale of catalytic cracking units tends to be larger, which reduces energy consumption and operating costs overall. This is an inevitable trend. The oxygen-depleted regeneration technology has low air consumption indicators, which can effectively reduce the size of the regenerator and reduce the power of the main fan, which is conducive to the manufacture of large units. Therefore, it has been widely used in large catalytic cracking units.

[0003] The catalytic cracking oxygen-depleted regeneration system model can guide technicians to optimize the operation of the device, reduce the main air consumption, and improve the regeneration efficiency. Usually, the catalytic cracking regeneration system model consists of a char kinetic model and a regenerator model. The char kinetic model equation is as follows:

[0004] ;

[0005] In the formula, Indicates A reaction; Indicates Reaction rate, unit ; is the reaction rate constant; Indicates the molar concentration of C element, H element or CO, unit ; Indicates that in O 2 The molar concentration, unit ; is a constant.

[0006] The regenerator model equation is as follows:

[0007] ;

[0008] In the formula, Indicates the height of the regenerator, in m; Indicates the bed There is no relative distance at the cross section; Represents the cross-sectional area of ​​the regenerator, in units ; It represents the molar flow rate of each gas component, in units of .

[0009] For the oxygen component, the equation for the change of its molar flow rate along the height of the regenerator is as follows:

[0010] ;

[0011] For the oxygen-poor regeneration system, the oxygen content is generally 0-2v%. Due to the reduction of main air consumption and insufficient oxygen content, when predicting the flue gas composition of the oxygen-poor regeneration system according to the above formula, the oxygen content in the flue gas may be calculated to be less than 0v%, which seriously affects the prediction accuracy of the regeneration system model. At present, no scholars have paid attention to this problem.

[0012] In view of this, the present invention is proposed. Summary of the invention

[0013] The object of the present invention is to provide a modeling method and device for a catalytic cracking oxygen-depleted regeneration system, aiming to accurately predict the composition of regeneration flue gas under oxygen-depleted regeneration conditions.

[0014] The present invention is achieved in that:

[0015] The present invention provides a modeling method for a catalytic cracking oxygen-depleted regeneration system, comprising:

[0016] Establish a kinetic model for the charring reaction: The char attached to the surface of the deactivated catalyst mainly contains carbon and hydrogen. During the combustion reaction, carbon is oxidized to generate carbon monoxide and carbon dioxide, hydrogen is oxidized to generate water, and carbon monoxide generated by the carbon reaction will continue to be oxidized to generate carbon dioxide. Kinetic models are established based on these four reactions.

[0017] Establish a correction model for the oxygen-poor regeneration system: calibrate the reactions of carbon burning, hydrogen burning and CO combustion respectively;

[0018] Establishing a steady-state model of the regenerator: Establishing a steady-state model of the regenerator based on the corrected char reaction kinetics model and the process flow of the catalytic regeneration system.

[0019] The present invention also provides a model building device for implementing the above-mentioned modeling method, including a model building module, wherein the model building module is used to build a scorching reaction kinetic model, an oxygen-deficient regeneration system correction model and a regenerator steady-state model.

[0020] The present invention also provides an electronic device, comprising a processor and a memory, wherein the memory stores computer-readable instructions, and when the computer-readable instructions are executed by the processor, the steps in the above-mentioned modeling method are executed.

[0021] The present invention also provides a readable storage medium on which a computer program is stored. When the computer program is executed by a processor, the steps in the above modeling method are executed.

[0022] The present invention has the following beneficial effects: after establishing the kinetic model of the charring reaction, a correction model of the oxygen-depleted regeneration system is established to effectively correct the reaction rate. For the oxygen-depleted regeneration system, the accuracy of the prediction of the regeneration flue gas composition can be effectively improved, thereby more accurately determining the carbon content of the catalyst, which is of great significance for guiding the optimized operation of the catalytic cracking oxygen-depleted regeneration device. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the embodiments are briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without creative work.

[0024] Figure 1 The effect of the main air volume on the smoke outlet composition in Example 1;

[0025] Figure 2 The effect of the main air volume on the carbon content of the regenerated catalyst in Example 1;

[0026] Figure 3 This is the effect of the main air volume on the smoke outlet composition in comparative example 1;

[0027] Figure 4 This is the effect of the main air volume on the carbon content of the regenerated catalyst in Comparative Example 1;

[0028] Figure 5 This is the effect of the main air volume on the smoke outlet composition in comparative example 2;

[0029] Figure 6 This is the effect of the main air volume on the carbon content of the regenerated catalyst in Comparative Example 2;

[0030] Figure 7 This is the effect of the main air volume on the smoke outlet composition in comparative example 3;

[0031] Figure 8 This is the effect of the main air volume on the carbon content of the regenerated catalyst in comparative example 3;

[0032] Fig. 9 This is the effect of the main air volume on the smoke outlet composition in comparative example 4;

[0033] Fig.10 This is the effect of the main air volume on the carbon content of the regenerated catalyst in comparative example 4. DETAILED DESCRIPTION

[0034] In order to make the purpose, technical scheme and advantages of the embodiments of the present invention clearer, the technical scheme in the embodiments of the present invention will be described clearly and completely below. If the specific conditions are not specified in the embodiments, they are carried out according to conventional conditions or conditions recommended by the manufacturer. If the manufacturer of the reagents or instruments used is not specified, they are all conventional products that can be purchased commercially.

[0035] The inventors found that the reason why the oxygen content in the flue gas was calculated to be less than 0v% during the prediction was mainly because: as the oxygen content in the system decreased linearly, the charring rate in the regenerator did not decrease linearly. When the oxygen content was about to drop below 0.5v%, the charring rate decreased exponentially with the decrease in oxygen content. The existing regeneration system model cannot simulate this phenomenon.

[0036] To address this problem, the inventor creatively introduced a correction model to significantly improve the accuracy of flue gas composition prediction. An embodiment of the present invention provides a modeling method for a catalytic cracking oxygen-depleted regeneration system, comprising the following steps:

[0037] S1. Establishing the kinetic model of charring reaction

[0038] The coke attached to the surface of the deactivated catalyst is a mixture that mainly contains carbon (C) and hydrogen (H). During the combustion reaction, carbon is oxidized to produce CO and CO 2 , hydrogen is oxidized to form H 2 O, the CO generated by the carbon element reaction will continue to be oxidized to generate CO 2 , kinetic models are established based on these four reactions. When describing the kinetics of the char burning reaction, elements such as nitrogen (N) and sulfur (S) in the coke are ignored, and only carbon burning and hydrogen burning reactions are considered. The char burning reaction rate is a function of the molar concentration of coke and the molar concentration of oxygen.

[0039] The reaction equations for carbon to be oxidized to form carbon monoxide and carbon dioxide and hydrogen to be oxidized to form water are as follows:

[0040] (1)

[0041] (2)

[0042] (3)

[0043] In the formula , , The carbon element is oxidized to form CO and CO respectively. 2 and H element is oxidized to H 2 The reaction rate at O, in units ;

[0044] The three reactions (1)-(3) all occur in the dense phase bed, and the calculation formula is as follows:

[0045] (4)

[0046] (5)

[0047] (6)

[0048] In the formula, is the reaction rate constant, in units of ;

[0049] Indicates the generated CO 2 The molar ratio of CO, in units ;

[0050] Indicates the density of catalyst particles in the dense phase region, unit ;

[0051] represents the volume fraction of dense-phase bed catalyst;

[0052] Indicates the coke content on the catalyst, unit ;

[0053] Indicates the molar molecular mass of carbon, unit ;

[0054] Indicates the molar molecular mass of hydrogen, unit ;

[0055] is the molar ratio of hydrogen to carbon in coke;

[0056] Indicated in Gas composition in the area The molar concentration, unit , The area is a dense bed D or a dilute bed F, and the gas composition CO, CO 2 , H 2 O, O 2 or N 2 ;

[0057] In formula (4) and formula (5), The value of can be calculated by the empirical formula, and T represents the dense phase bed temperature in the regenerator:

[0058] (7)

[0059] In formulas (4)-(6), according to Determine the relationship:

[0060] represents the volume fraction of mixed gas in the dense bed, and The calculation formula is as follows:

[0061] (8)

[0062] (9)

[0063] In the formula, It represents the volume flow rate of gas in the dense phase, in units of , which is related to the main air flow entering the regenerator; It represents the cross-sectional area of ​​the dense phase bed of the regenerator;

[0064] The reaction rate constant can be calculated according to the Arrhenius equation as follows:

[0065] (10)

[0066] Where R represents the ideal gas constant, 8.314 ; and represent the pre-exponential factor and activation energy of the reaction respectively; Indicates the reference regeneration temperature.

[0067] The CO generated by the carbon element reaction is further oxidized to form CO 2 The reaction will occur in both the dense phase bed and the dilute phase zone; when it occurs in the dense phase bed, the reaction equation and reaction rate calculation formula are as follows:

[0068]

[0069] (11)

[0070] Molar concentration of gas in dense phase The calculation formula is as follows:

[0071] (12)

[0072] In the formula, It represents the molar flow rate of each gas component in the dense phase, in units of ; It represents the volume flow rate of gas in the dense phase, in units of .

[0073] There is no scorching reaction in the freeboard zone, only the oxidation reaction of CO. Therefore, the reaction rate of the oxidation reaction of CO in the freeboard zone is as follows:

[0074] (13)

[0075] It represents the molar concentration of each gas component in the dilute phase, in units of , the calculation formula is as follows:

[0076] (14)

[0077] In the formula, It represents the molar flow rate of each gas component, in units of .

[0078] S2. Establishment of the correction model of the oxygen-poor regeneration system

[0079] The charring reaction kinetic model is corrected to make the prediction data of flue gas composition more accurate. When the oxygen content of the system is high, the charring and CO combustion rates in the regenerator decrease linearly with the decrease of oxygen content; when the oxygen content of the system is low, the charring and CO combustion rates in the regenerator decrease linearly with the decrease of oxygen content.

[0080] The embodiment of the present application proposes an equation for correcting the burning rate according to the oxygen content of the system, and corrects the burning rates of carbon, hydrogen and CO respectively. Among them, the reaction of carbon combustion to generate carbon monoxide adopts Correction is made for the reaction of carbon combustion to produce carbon dioxide using Correction is made for the reaction of carbon monoxide burning to produce carbon dioxide. Make corrections;

[0081] in, ; ; .

[0082] It should be noted that as the oxygen content decreases to 0v%, Increase, , decreases to 0, and As the oxygen content decreases, C is more likely to generate CO when burned. Correction of this reaction; as the oxygen content decreases, it becomes more difficult for C to burn to produce CO 2 , so we use Correct the reaction; as the oxygen content decreases, it becomes more difficult for CO to burn to form CO 2 However, this reaction is more difficult to carry out than the direct combustion of C to produce CO2 The response is low, so the Correcting the reaction. The inventors calibrated the three reactions precisely by accurately selecting the correction parameters, thereby improving the accuracy of the smoke composition prediction.

[0083] S3. Establishing a steady-state model of the regenerator

[0084] According to the corrected char reaction kinetic model and the process flow of the catalytic regeneration system, the steady-state model of the regenerator is established. In the process of establishing the steady-state model of the regenerator, the steady-state model of the regenerator is a set of ordinary differential equations. 2 , H 2 O, O 2 、N 2 Content to determine the coke content in the regenerated catalyst.

[0085] Material balance is performed on the gas in the dense bed. The height of the dense bed in the regenerator is set to remain unchanged. According to the correction equation, the equation for the rate of change of the molar flow rate of each gas component in the dense bed of the regenerator along the axial direction is as follows:

[0086] (15)

[0087] (16)

[0088] (17)

[0089] (18)

[0090] (19)

[0091] In the formula, Indicates the height of dense phase bed, unit is m;

[0092] Indicates the cross-sectional area of ​​the regenerator dense phase bed, in m 2 .

[0093] The initial values ​​of the molar flow rates of each component are calculated as follows:

[0094] (20)

[0095] (twenty one)

[0096] (twenty two)

[0097] (twenty three)

[0098] (twenty four)

[0099] In the formula, Indicates air mass flow rate, unit ;

[0100] Indicates the mass of air molecules, unit .

[0101] For the gas in the dilute phase area, all of them come from the dense phase area, including CO, CO generated by the charring reaction. 2 , H 2 O, the molar flow rate of each component is calculated as follows:

[0102] (25)

[0103] (26)

[0104] (27)

[0105] (28)

[0106] (29)

[0107] In the formula, Indicates the height of the dilute phase zone, in m;

[0108] According to the continuity of gas flow, the gas molar flow rate at the entrance of the dilute phase zone is equal to the gas molar flow rate at the exit of the dense phase zone. The calculation formula is as follows:

[0109] (30)

[0110] (31)

[0111] (32)

[0112] (33)

[0113] (34)

[0114] In the above formula It represents the molar flow rate of each gas component at the entrance of the dilute phase zone, in units of ; It represents the molar flow rate of each gas component at the outlet of the dense phase zone, in units of ;

[0115] The ratio of each gas component in the flue gas is calculated by the following formula:

[0116] (35)

[0117] In the formula, It represents the molar flow rate of each gas component in the regenerator flue gas, in units of ;

[0118] The calculation formula for the coke content of the semi-regenerated catalyst after repeated regeneration is as follows:

[0119] (36).

[0120] It should be added that other operations and conditions related to modeling that are not disclosed in the embodiments of the present invention can refer to the relevant contents of the prior art and will not be elaborated in detail here.

[0121] An embodiment of the present invention provides a model building device for implementing the above-mentioned modeling method, including a model building module, wherein the model building module is used to build a scorching reaction kinetic model, an oxygen-deficient regeneration system correction model and a regenerator steady-state model.

[0122] An embodiment of the present invention further provides an electronic device, including a processor and a memory, wherein the memory stores computer-readable instructions, and when the computer-readable instructions are executed by the processor, the steps in the above-mentioned modeling method are executed.

[0123] In some embodiments, the electronic device includes a modeling device, a processor, a memory, a storage controller, a peripheral interface, an input and output unit, an audio unit, a display unit, and the like.

[0124] Specifically, the memory, storage controller, processor, peripheral interface, input / output unit, audio unit, and display unit are electrically connected to each other directly or indirectly to achieve data transmission or interaction. The modeling device includes at least one software function module that can be stored in the memory in the form of software or firmware or fixed in the operating system (OS) of the modeling device. The processor is used to execute the executable modules stored in the memory, including software function modules or computer programs.

[0125] The memory may be, but is not limited to, a random access memory (RAM), a read-only memory (ROM), a programmable read-only memory (PROM), an erasable read-only memory (EPROM), an electrically erasable read-only memory (EEPROM), etc. The memory is used to store programs, and the processor executes the corresponding program after receiving the execution instruction. The method executed by the server defined by the flow process involved in this application can be applied to the processor or implemented by the processor.

[0126] The processor can be an integrated circuit chip with signal processing capabilities. The above-mentioned processor can be a general-purpose processor, including a central processing unit (CPU), a network processor (NP), etc.; it can also be a digital signal processor (DSP), an application-specific integrated circuit (ASIC), a field-programmable gate array (FPGA) or other programmable logic devices, discrete gate or transistor logic devices, and discrete hardware components.

[0127] The peripheral interface couples various input / output devices to the processor and the memory. The peripheral interface, the processor, and the memory controller may be implemented in a single chip or may be implemented in separate chips.

[0128] The input and output unit, audio unit and display unit are all existing technologies. For example, the input and output unit is used to provide input data to the user to enable the user to interact with the server (or local terminal), and can be a mouse, keyboard, etc.; the audio unit provides an audio interface to the user, which may include one or more microphones, one or more speakers and an audio circuit; the display unit provides an interactive interface (such as a user operation interface) between the electronic device and the user or is used to display image data for the user's reference.

[0129] An embodiment of the present invention further provides a readable storage medium on which a computer program is stored. When the computer program is executed by a processor, the steps in the above-mentioned modeling method are executed.

[0130] The features and performance of the present invention are further described in detail below in conjunction with the embodiments.

[0131] Example 1

[0132] The modeling method provided in the embodiment of the present invention is used to predict the regenerator flue gas outlet composition and the regenerated catalyst carbon content, referring to equations (1)-(36). The specific parameters are as follows:

[0133] Assume that the regeneration system is in thermal equilibrium, the flow rate of the regenerated catalyst is 200 kg / s, the carbon content of the regenerated catalyst is 1.0 w%, and the dense phase temperature is 690 °C. Predict the effect of the main air volume on the flue gas outlet composition.

[0134] The influence of main air volume on the smoke outlet composition is shown in Figure 1 ,like Figure 1 As shown, when the main air volume is less than 9.0m 3 / kg coke, the oxygen content in the flue gas is close to 0v%. As the main air volume decreases, the oxygen content in the flue gas decreases, and the oxygen content is greater than 0. When the main air volume is greater than 9m 3 / kg coke, as the main air volume increases, the oxygen content in the flue gas increases, the carbon monoxide content decreases, and the carbon dioxide content first increases and then decreases.

[0135] The effect of main air volume on carbon content of regenerated catalyst is shown in Figure 2 It can be seen that when the main air volume is greater than 11 m3 / kg coke, the carbon content of the regenerated catalyst can be reduced to below 1w%.

[0136] Comparative Example 1

[0137] The only difference from Example 1 is that the conventional regeneration system model is used to predict the flue gas composition and the regenerated catalyst carbon. The conventional regeneration system model does not introduce a correction function compared to the model in Example 1. , and .

[0138] The influence of the main air volume on the flue gas outlet composition is shown in Figure 3 The effect of main air volume on the carbon content of regenerated catalyst is shown in Figure 4 .

[0139] like Figure 3 and Figure 4 As shown, when the main air volume is greater than 9m 3 / kg coke, the flue gas composition and regenerated catalyst carbon content can be calculated. 3 / kg coke, the oxygen content in the flue gas is calculated to be less than 0v%. The right side of the equations (15)-(18) has ,when , a complex number will be calculated, so the calculation result is meaningless. 3 / kg coke, the trend of flue gas composition and regeneration agent carbon content changing with main air volume is roughly the same as that in Example 1.

[0140] Comparative Example 2

[0141] The only difference from Example 1 is that the correction function uniformly adopts .

[0142] The influence of the main air volume on the flue gas outlet composition is shown in Figure 5 The effect of main air volume on the carbon content of regenerated catalyst is shown in Figure 6 .

[0143] like Figure 5 and Figure 6 As shown, when the main air volume is greater than 11.5m 3 / kg coke, the flue gas composition and regenerated catalyst carbon content can be calculated. 3 / kg coke, the calculated oxygen content in the flue gas is less than 0v%. This is due to the correction function The combustion rate of C and CO is increased, that is, the oxygen consumption rate is increased. Compared with the comparative example 1 and the conventional regeneration system model, the oxygen consumption is greater under the same main air volume.

[0144] Comparative Example 3

[0145] The only difference from Example 1 is that the correction function uniformly adopts .

[0146] The influence of the main air volume on the flue gas outlet composition is shown in Figure 7 The effect of main air volume on the carbon content of regenerated catalyst is shown in Figure 8 .

[0147] like Figure 7 As shown, within the main air volume range investigated, the flue gas oxygen content increases from 4v% to 8v%, which is much greater than 0. The trend of flue gas composition changing with the main air volume is inconsistent with that of Comparative Example 1.

[0148] like Figure 8 As shown, as the main air volume increases to 15m 3 / kg coke, the carbon content of the regeneration agent is reduced to about 0.25w%, and the regeneration effect is poor, which is inconsistent with Comparative Example 1.

[0149] Comparative Example 4

[0150] The only difference from Example 1 is that the correction function uniformly adopts .

[0151] The influence of the main air volume on the flue gas outlet composition is shown in Fig. 9 The effect of main air volume on the carbon content of regenerated catalyst is shown in Fig.10 .

[0152] like Fig. 9 Shown and Fig.10 As shown, the trends of flue gas composition and regeneration agent carbon content as the main air volume changes are similar to those of Comparative Example 3, but inconsistent with Comparative Example 1.

[0153] By comparing Example 1 with Comparative Examples 1, 2, 3 and 4, it can be seen that only by adopting the correction model proposed in the present invention can the flue gas composition and regeneration agent carbon content obtained by the model prediction be the same as the conventional regenerator model with the trend of the change of the main air volume, and at the same time, the flue gas composition and regeneration catalyst carbon content can be predicted when the oxygen content in the system is insufficient, which has guiding significance for the design and optimization operation of the regenerator.

[0154] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A modeling method for a catalytic cracking oxygen-depleted regeneration system, characterized in that: include: Establish a kinetic model for the charring reaction: The char attached to the surface of the deactivated catalyst mainly contains carbon and hydrogen. During the combustion reaction, carbon is oxidized to generate carbon monoxide and carbon dioxide, hydrogen is oxidized to generate water, and carbon monoxide generated by the carbon reaction will continue to be oxidized to generate carbon dioxide. Kinetic models are established based on these four reactions. Establish a correction model for the oxygen-poor regeneration system: calibrate the reactions of carbon burning and CO combustion respectively; Establishing a steady-state model of the regenerator: Establishing a steady-state model of the regenerator based on the corrected char reaction kinetic model and the process flow of the catalytic regeneration system; In the process of establishing the correction model of the oxygen-poor regeneration system, the reaction of carbon combustion to generate carbon monoxide is adopted Correction is made for the reaction of carbon combustion to produce carbon dioxide using Correction is made for the reaction of carbon monoxide burning to produce carbon dioxide. Make corrections; in, ; ； ； In the process of establishing the steady-state model of the regenerator, the steady-state model of the regenerator is a set of ordinary differential equations, and the coke content in the regenerated catalyst is determined by calculating the contents of CO, CO2, H2O, O2, and N2 in the flue gas; Material balance is performed on the gas in the dense bed. The height of the dense bed in the regenerator is set to remain unchanged. According to the correction equation, the equation for the rate of change of the molar flow rate of each gas component in the dense bed of the regenerator along the axial direction is as follows: （15） （16） （17） （18） （19） In the formula, Indicates the height of dense phase bed, unit is m; Indicates the cross-sectional area of ​​the regenerator dense phase bed, in m 2 ; is the reaction rate constant, in units of ; Indicates the molar ratio of generated CO2 and CO, in units ; Indicates the density of catalyst particles in the dense phase region, unit ; represents the volume fraction of dense-phase bed catalyst; Indicates the coke content on the catalyst, unit ; Indicates the molar molecular mass of carbon, unit ; Indicates the molar molecular mass of hydrogen, unit ; is the molar ratio of hydrogen to carbon in coke; Indicated in Gas composition in the area The molar concentration, unit , The area is a dense bed D or a dilute bed F, and the gas composition CO, CO2, H2O, O2 or N2; It represents the volume flow rate of gas in the dense phase, in units of ; The initial values ​​of the molar flow rates of each component are calculated as follows: （20） （21） （22） （23） （24） In the formula, Indicates air mass flow rate, unit ; Indicates the mass of air molecules, unit ; For the gas in the dilute phase area, all of them come from the dense phase area, including CO, CO2, and H2O generated by the charring reaction. The molar flow rate of each component is calculated as follows: （25） （26） （27） （28） （29） In the formula, Indicates the height of the dilute phase zone, in m; According to the continuity of gas flow, the gas molar flow rate at the entrance of the dilute phase zone is equal to the gas molar flow rate at the exit of the dense phase zone. The calculation formula is as follows: （30） （31） （32） （33） （34） In the above formula It represents the molar flow rate of each gas component at the entrance of the dilute phase zone, in units of ; It represents the molar flow rate of each gas component at the outlet of the dense phase zone, in units of .

2. The modeling method according to claim 1, characterized in that: The reaction equations for carbon to be oxidized to form carbon monoxide and carbon dioxide and hydrogen to be oxidized to form water are as follows: （1） （2） （3） In the formula , , Respectively represent the reaction rates when carbon is oxidized to form CO, CO2 and H is oxidized to form H2O, in units of ; All three reactions occur in a dense phase bed, and the calculation formula is as follows: （4） （5） （6） In the formula, is the reaction rate constant, in units of ; Indicates the molar ratio of generated CO2 and CO, in units ; Indicates the density of catalyst particles in the dense phase region, unit ; represents the volume fraction of dense-phase bed catalyst; Indicates the coke content on the catalyst, unit ; Indicates the molar molecular mass of carbon, unit ; Indicates the molar molecular mass of hydrogen, unit ; is the molar ratio of hydrogen to carbon in coke; Indicated in Gas composition in the area The molar concentration, unit , The area is a dense bed D or a dilute bed F, and the gas composition CO, CO2, H2O, O2 or N2; In formula (4) and formula (5), The value of is determined according to the dense bed temperature T in the regenerator: （7） In formulas (4)-(6), according to Determine the relationship: represents the volume fraction of mixed gas in the dense bed, and The calculation formula is as follows: （8） （9） In the formula, It represents the volume flow rate of gas in the dense phase, in units of , which is related to the main air flow entering the regenerator; It represents the cross-sectional area of ​​the dense phase bed of the regenerator; The reaction rate constant can be calculated according to the Arrhenius equation as follows: （10） Where R represents the ideal gas constant, 8.314 ; and represent the pre-exponential factor and activation energy of the reaction respectively; Indicates the reference regeneration temperature.

3. The modeling method according to claim 2, characterized in that: The CO generated by the carbon element reaction is further oxidized to form CO2, which occurs in both the dense phase bed and the dilute phase zone; When it occurs in a dense phase bed, the reaction equation and reaction rate calculation formula are as follows: （11） Molar concentration of gas in dense phase The calculation formula is as follows: （12） In the formula, It represents the molar flow rate of each gas component in the dense phase, in units of ; It represents the volume flow rate of gas in the dense phase, in units of ; There is no scorching reaction in the dilute phase zone, so the reaction rate of CO oxidation reaction in the dilute phase zone is as follows: （13） It represents the molar concentration of each gas component in the dilute phase, in units of , the calculation formula is as follows: （14） In the formula, It represents the molar flow rate of each gas component in the dilute phase region, in units of .

4. The modeling method according to claim 1, characterized in that: The ratio of each gas component in the flue gas is calculated by the following formula: （35） In the formula, It represents the molar flow rate of each gas component in the regenerator flue gas, in units of ; The calculation formula for the coke content of the semi-regenerated catalyst after repeated regeneration is as follows: （36）。 5. A model building device for implementing the modeling method according to any one of claims 1 to 4, characterized in that: It includes a model building module, which is used to build a scorch reaction kinetic model, an oxygen-deficient regeneration system correction model and a regenerator steady-state model.

6. An electronic device, characterized in that: The invention comprises a processor and a memory, wherein the memory stores computer-readable instructions, and when the computer-readable instructions are executed by the processor, the steps in the modeling method according to any one of claims 1 to 4 are executed.

7. A readable storage medium having a computer program stored thereon, characterized in that: When the computer program is executed by a processor, the steps of the modeling method according to any one of claims 1 to 4 are executed.

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