Method and device for establishing riser and fluidized bed series reactor model

Abstract

The invention discloses a riser and fluidized bed series reactor model building method and device, and the method comprises the following steps: S1, carrying out the lumped division of raw materials and products according to the lumped kinetics principle and industrial actual demands; establishing a reaction network according to the divided lumps; s2, establishing a reaction kinetic model according to the reaction network; s3, constructing a prediction model according to the kinetic model, predicting the content of each raw material set through the properties of the raw materials, substituting the content into the prediction model, and predicting the yield of each product set; the kinetic model in S2 comprises a riser reactor kinetic model and a fluidized bed reactor kinetic model; the prediction model in the step S3 comprises a riser reactor prediction model and a fluidized bed reactor prediction model, and both the riser reactor prediction model and the fluidized bed reactor prediction model introduce a catalyst carbon determination function to represent the influence of the catalyst carbon determination function on the yield. According to the invention, the product prediction result is more accurate.

Description

Technical Field

[0001] The present invention relates to the technical field of catalytic cracking, and specifically relates to a method and device for establishing a riser and fluidized bed series reactor model. Background Art

[0002] The riser reactor has the advantages of high operating linear velocity, good conveying performance, low backmixing degree, high reaction efficiency, easy control of target products, etc. The fluidized bed reactor has the advantages of high mass and heat transfer efficiency. The riser and fluidized bed series reactor combines the advantages of both, that is, it retains the characteristics of high reaction intensity of the riser reactor and utilizes the advantage of the reaction depth of the fluidized bed reactor, achieving high conversion rate of raw materials and ensuring high selectivity of target products. To give full play to the advantages of the riser reactor and the fluidized bed reactor, a model of the series reactor is established to guide the complementary advantages of the riser and fluidized bed reactors.

[0003] In the prior art, the following are several representative kinetic models of the riser and fluidized bed series reactor:

[0004] The reaction device model established in the "New Catalytic Cracking MIP Lumping Reaction Kinetics Model" proposed by Duan Liangwei, Sun Peng, Weng Huixin, etc. in 2012;

[0005] The reaction device model established in the "Heavy Oil Catalytic Cracking MIP Process Lumping Kinetics Model" proposed by Jiang Hongbo, Zhong Guijiang, Ning Hui, etc. in 2010;

[0006] The reaction device model established in the "Numerical Simulation of MIP Riser Reaction Process Based on Multi-Scale Model" proposed by Lubona, Cheng Congli, Lu Weimin, etc. in 2013;

[0007] The patent applied by the present applicant in 2019 provides a method and device for establishing a catalytic cracking model (Patent No.: CN110648729A). A catalyst deactivation correction parameter is introduced in this catalytic cracking model to characterize its influence on the results. Among them, t c is the residence time of the catalyst in the riser, β is the catalyst deactivation constant, and the residence time of the catalyst in the riser reactor is a fixed value, making the catalyst deactivation correction parameter in the catalytic cracking model of the riser reactor also a fixed value, which cannot reflect the change of catalyst activity in the axial direction of the riser reactor. However, in the actual production process, the fixed carbon of the catalyst continuously increases from the inlet to the outlet of the riser reactor, resulting in the continuous change of catalyst activity along the axial direction of the riser. Therefore, the prediction result of the above formula is inaccurate. Summary of the Invention

[0008] To solve the problem of low accuracy in predicting the overall yield of each product in the prior art, the present invention provides a method and device for establishing a riser and fluidized bed series reactor model, introducing a catalyst fixed carbon function, and further considering the influence of catalyst activity change on the prediction result, so that the prediction result is more accurate.

[0009] To achieve the above object, the specific solution adopted by the present invention is: a method for establishing a riser and fluidized bed series reactor model, comprising the following steps:

[0010] S1. According to the lumping kinetics principle and industrial actual requirements, lump and divide the raw materials and products; establish a reaction network according to the divided lumps;

[0011] S2. Establish a reaction kinetics model according to the reaction network;

[0012] S3. Construct a prediction model according to the kinetics model, predict the content of each raw material lump through the raw material properties, and substitute it into the prediction model to predict the yield of each product lump. The kinetics model in the S1 includes a riser reactor kinetics model and a fluidized bed reactor kinetics model; the prediction model in the S3 includes a riser reactor prediction model and a fluidized bed reactor prediction model. The catalyst fixed carbon function is introduced into both the riser reactor prediction model and the fluidized bed reactor prediction model to characterize its influence on the yield. The catalyst fixed carbon function in the riser reactor prediction model is:

[0013] θ(C Riser ) = exp(-k W ·C Riser )

[0014] Wherein, C Riser is the fixed carbon of the catalyst in the riser reactor (w%), and k W is the fixed carbon influence constant of the catalyst;

[0015]

[0016] Wherein, y CK is the fraction of coke in the riser reactor, and R CO is the catalyst-oil ratio in the riser reactor;

[0017] The catalyst fixed carbon function in the fluidized bed reactor prediction model is:

[0018] θ(C Bed ) = exp(-k W ·C Bed )

[0019] Wherein, C Bed is the fixed carbon of the catalyst in the fluidized bed reactor (w%), and k Wis the influence constant of catalyst carbon content;

[0020]

[0021] Among them, R CO represents the catalyst-to-oil ratio in the fluidized bed reactor, y CK，Riser，out is the coke fraction at the outlet of the riser reactor, and β is the influence degree of reactor structure, reaction conditions, and feedstock oil properties on the catalyst carbon content.

[0022] As an optimized scheme of the above method for establishing a riser and fluidized bed series reactor model: The prediction model of the riser reactor in S3 is:

[0023]

[0024] Among them, X Riser = x Riser / H Riser is the dimensionless relative distance at the x Riser section in the bed layer, H Riser represents the height of the riser reactor, x Riser represents the distance from the riser inlet into the reactor, y i is the mass fraction of each component, M i is the average relative molecular weight of the i-th lumping in the riser reactor, Y Riser is the mass fraction vector of each lumping component in the riser reactor, S WH is the true weight hourly space velocity, y i is the mass fraction of the i-th lumping, K is the reaction rate constant matrix in the riser reactor, exp(-k W ·C Riser ) is the catalyst carbon content function of the riser reactor, and P is the pressure (Pa) in the riser reactor.

[0025] As another optimized scheme of the above method for establishing a riser and fluidized bed series reactor model: The kinetic model of the riser reactor in S2 is:

[0026]

[0027] Among them, X Riser = x Riser / H Riser is the dimensionless relative distance at the x Riser section in the bed layer, H Riser represents the height of the riser reactor, x Riser represents the distance from the riser inlet into the reactor, a = [a1,..., a 17 T is the lumping component concentration vector, θ(C​Riser ) represents the function of catalyst fixed carbon in the riser reactor, S WH is the true weight hourly space velocity, a i is the concentration of the i-th lumping (molesi / g gas), K is the reaction rate constant matrix in the riser reactor, and P is the pressure (Pa) in the riser reactor.

[0028] As another optimization scheme of the above method for establishing a riser and fluidized bed series reactor model: The kinetic model of the riser reactor is obtained based on the continuity equation and reaction rate of the riser reactor:

[0029] The continuity equation is:

[0030]

[0031] Among them, ρ represents the density of the oil-gas mixture (g / cm 3 ), t represents the reaction time, G v represents the mass flow rate of the oil-gas cross-section (g / (cm 2 ·h)), x Riser represents the distance from the riser inlet into the reactor, a i is the concentration of the i-th lumping (molesi / g gas), R i represents the reaction rate of the i-th lumping, n r is the number of reactions in the riser reactor, v i，j is the stoichiometric coefficient of the i-th lumping in reaction j, r j represents the rate of the j-th reaction, and P is the pressure (Pa) in the riser reactor;

[0032] The reaction rate is:

[0033]

[0034] Among them, θ(C Riser ) is the function of the influence of catalyst fixed carbon in the riser reactor on the reaction rate, k j is the reaction rate constant of reaction j (cm 3 / (g·h)), ρ c is the catalyst density relative to the volume of the riser reactor (g / cm 3 ), ε is the void fraction, P is the system pressure (Pa) of the riser reactor, R is the gas constant (8.314 J / (mol·K)), and T is the system temperature (K) in the riser reactor.

[0035] As another optimization scheme of the above method for establishing a riser and fluidized bed series reactor model: The prediction model of the fluidized bed reactor is:

[0036]

[0037] Among them, X Bed = x Bed / H Bed is the dimensionless relative distance at the x bed cross-section in the fluidized bed layer, x bed is the distance from the fluidized bed inlet into the fluidized bed reactor, H bed is the height of the fluidized bed reactor, C bed is the fixed carbon of the catalyst in the fluidized bed reactor, k W is the fixed carbon influence constant of the catalyst in the fluidized bed (cm 3 / (g / h)), P is the system pressure in the fluidized bed reactor, R is the gas constant (8.314 J / (mol·K)), T is the system temperature in the fluidized bed reactor (K), S WH is the true weight hourly space velocity, y i is the mass fraction of each component, M i is the average relative molecular weight of the i-th lumping in the fluidized bed reactor, K is the reaction rate constant matrix in the fluidized bed reactor, Y Riser is the mass fraction vector of each lumping component.

[0038] As another optimization scheme of the above method for establishing a riser and fluidized bed series reactor model: the lumping of the raw materials is as follows. The raw oil in the riser reactor and the fluidized bed reactor is divided into three layers, namely the residue layer, the wax oil layer, and the diesel oil layer, according to the distillation range, and further subdivided into 11 raw material lumpings, namely the residue layer paraffin lumping, the residue layer naphthene lumping, the residue layer aromatic lumping, the aromatic lumping in gum and asphalt, the wax oil layer paraffin lumping, the wax oil layer naphthene lumping, the wax oil layer aromatic lumping, the diesel oil layer paraffin lumping, the diesel oil layer naphthene lumping, the diesel oil layer single-ring aromatic lumping, and the diesel oil layer multi-ring aromatic lumping; the products are divided into 6 lumpings, namely the gasoline paraffin lumping, the gasoline olefin lumping, the gasoline naphthene lumping, the gasoline aromatic lumping, the gas lumping, and the coke lumping.

[0039] As another optimization scheme of the above method for establishing a riser and fluidized bed series reactor model: the reaction network in S2 is as follows:

[0040] Establish reactions between the residue layer paraffin lumping and the wax oil layer paraffin lumping, the diesel paraffin lumping, and the coke lumping respectively;

[0041] Establish reactions between the residue layer naphthene lumping and the diesel naphthene lumping, the wax oil layer naphthene lumping, and the coke lumping respectively;

[0042] Establish reactions between the aromatics lumps in the residue oil layer and the aromatics lumps in the gas oil layer, the coke lumps, and the aromatics lumps with more than two rings in the diesel oil layer respectively;

[0043] Establish reactions between the aromatics lumps in the resin and asphaltene and the aromatics lumps in the gas oil layer and the coke lumps respectively;

[0044] Establish reactions between the paraffin lumps in the gas oil layer and the gas lumps, the paraffin lumps in the diesel oil, the paraffin lumps in the gasoline, the olefin lumps in the gasoline, and the coke lumps respectively;

[0045] Establish reactions between the naphthene lumps in the gas oil layer and the paraffin lumps in the gasoline, the gas lumps, the olefin lumps in the gasoline, the naphthene lumps in the diesel oil, the naphthene lumps in the gasoline, and the coke lumps respectively;

[0046] Establish reactions between the aromatics lumps in the gas oil layer and the gas lumps, the single - ring aromatics lumps in the diesel oil layer, the aromatics lumps with more than two rings in the diesel oil layer, the aromatics lumps in the gasoline, and the coke lumps respectively;

[0047] Establish reactions between the paraffin lumps in the diesel oil and the gas lumps, the paraffin lumps in the gasoline, the olefin lumps in the gasoline, and the coke lumps respectively;

[0048] Establish reactions between the naphthene lumps in the diesel oil and the paraffin lumps in the gasoline, the gas lumps, the olefin lumps in the gasoline, the naphthene lumps in the gasoline, and the coke lumps respectively;

[0049] Establish reactions between the single - ring aromatics lumps in the diesel oil layer and the gas lumps, the aromatics lumps in the gasoline, and the coke lumps respectively;

[0050] Establish a reaction between the aromatics lumps with more than two rings in the diesel oil layer and the coke lumps;

[0051] Establish reactions between the paraffin lumps in the gasoline and the gas lumps and the coke lumps respectively;

[0052] Establish reactions between the olefin lumps in the gasoline and the paraffin lumps in the gasoline, the gas lumps, and the coke lumps respectively;

[0053] Establish reactions between the naphthene lumps in the gasoline and the gas lumps, the aromatics lumps in the gasoline, and the coke lumps respectively;

[0054] Establish reactions between the aromatics lumps in the gasoline and the gas lumps and the coke lumps respectively.

[0055] An establishment device for a riser and fluidized bed tandem catalytic cracking reaction model, the establishment device includes a modeling module that models using the above - mentioned riser and fluidized bed tandem catalytic cracking reaction model.

[0056] An electronic device includes a processor and a memory, the memory stores computer - readable instructions, when the computer - readable instructions are executed by the processor, it can run the above - mentioned prediction model.

[0057] A readable storage medium stores a computer program thereon. When the computer program is executed by a processor, the steps of the above-mentioned establishment method are run.

[0058] Compared with the prior art, the present invention has the following beneficial effects:

[0059] The present invention provides a method for establishing a riser and fluidized bed series reactor model. A catalyst fixed carbon function is introduced into the prediction model to characterize the influence of the change of catalyst activity on the prediction model. Among them, the introduction of the catalyst fixed carbon function in the riser reactor prediction model shows the change of catalyst activity in its axial direction. The catalyst enters the fluidized bed reactor after reaction in the riser reactor and further accumulates carbon in the fluidized bed reactor. The degree of carbon accumulation is affected by the reactor structure, reaction conditions and feedstock oil properties. Therefore, β is introduced into the catalyst fixed carbon function in the fluidized bed reactor prediction model to make the prediction results of the overall yields of each product more accurate. Specific embodiments

[0060] The technical solution of the present invention will be further elaborated in detail below in conjunction with specific embodiments. For the parts not detailedly recorded and disclosed in the following embodiments of the present invention, they should all be understood as the prior art known or should be known to those skilled in the art.

[0061] Example 1

[0062] A method for establishing a riser and fluidized bed series reactor model includes the following steps:

[0063] S1. According to the lumping kinetics principle and industrial actual requirements, lump the raw materials and products; establish a reaction network according to the lumps divided.

[0064] The lumping of raw materials is as follows: according to the distillation range, the feedstock oil in the riser reactor and the fluidized bed reactor is divided into three layers: the residue oil layer, the wax oil layer, and the diesel oil layer. Each layer is further divided into paraffins, naphthenes, and aromatics according to the structural group composition. Considering that most of the aromatics in gum and asphalt exist as polycyclic aromatics, and their cracking performance is different from that of the aromatics lumped in the residue oil layer, they are therefore separately lumped as aromatics in gum and asphalt. Considering that there are significant differences in the cracking performance of the aromatic carbon in monocyclic aromatics and polycyclic aromatics in the diesel oil layer, the diesel oil layer is divided into a monocyclic aromatic lumped group and a polycyclic aromatic lumped group in the diesel oil layer. That is, the raw material lumping is refined into 11 raw material lumped groups, namely the paraffin lumped group in the residue oil layer, the naphthene lumped group in the residue oil layer, the aromatic lumped group in the residue oil layer, the aromatic lumped group in gum and asphalt, the paraffin lumped group in the wax oil layer, the naphthene lumped group in the wax oil layer, the aromatic lumped group in the wax oil layer, the paraffin lumped group in the diesel oil layer, the naphthene lumped group in the diesel oil layer, the monocyclic aromatic lumped group in the diesel oil layer, and the polycyclic aromatic lumped group in the diesel oil layer above two rings. The products are divided into 6 lumped groups, namely the paraffin lumped group in gasoline, the olefin lumped group in gasoline, the naphthene lumped group in gasoline, the aromatic lumped group in gasoline, the gas lumped group, and the coke lumped group.

[0065] The chemical reactions in the riser reactor and the fluidized bed reactor are parallel-consecutive reactions. Diesel and gasoline are both reaction products and reactants, while gas and coke are the final products. The chemical reactions mainly involve the cracking of heavy components to produce light components. In the reactions of the residue oil layer cracking to produce the wax oil layer and the diesel oil layer, and the wax oil layer cracking to produce the diesel oil layer, paraffins can only crack to produce paraffins, naphthenes can only crack to produce naphthenes, and aromatics can only crack to produce aromatics; for the residue oil layer, the wax oil layer, and the diesel oil layer, there is no interaction between the lumped groups in the same layer; the residue oil layer cannot directly produce gas and gasoline. Based on this, the reaction network includes 17 lumped groups and 50 reactions.

[0066] The reaction network is as follows: reactions are established between the paraffin lumped group in the residue oil layer and the paraffin lumped group in the wax oil layer, the paraffin lumped group in diesel, and the coke lumped group respectively;

[0067] reactions are established between the naphthene lumped group in the residue oil layer and the naphthene lumped group in diesel, the naphthene lumped group in the wax oil layer, and the coke lumped group respectively;

[0068] reactions are established between the aromatic lumped group in the residue oil layer and the aromatic lumped group in the wax oil layer, the coke lumped group, and the polycyclic aromatic lumped group in the diesel oil layer above two rings respectively;

[0069] reactions are established between the aromatic lumped group in gum and asphalt and the aromatic lumped group in the wax oil layer and the coke lumped group respectively;

[0070] reactions are established between the paraffin lumped group in the wax oil layer and the gas lumped group, the paraffin lumped group in diesel, the paraffin lumped group in gasoline, the olefin lumped group in gasoline, and the coke lumped group respectively;

[0071] The naphthene lumps in the wax oil layer are respectively reacted with the paraffin lumps in gasoline, the gas lumps, the olefin lumps in gasoline, the naphthene lumps in diesel, the naphthene lumps in gasoline and the coke lumps;

[0072] The aromatic lumps in the wax oil layer are respectively reacted with the gas lumps, the single-ring aromatic lumps in the diesel layer, the multi-ring aromatic lumps in the diesel layer, the aromatic lumps in gasoline and the coke lumps;

[0073] The paraffin lumps in diesel are respectively reacted with the gas lumps, the paraffin lumps in gasoline, the olefin lumps in gasoline and the coke lumps;

[0074] The naphthene lumps in diesel are respectively reacted with the paraffin lumps in gasoline, the gas lumps, the olefin lumps in gasoline, the naphthene lumps in gasoline and the coke lumps;

[0075] The single-ring aromatic lumps in the diesel layer are respectively reacted with the gas lumps, the aromatic lumps in gasoline and the coke lumps;

[0076] The multi-ring aromatic lumps in the diesel layer are reacted with the coke lumps;

[0077] The paraffin lumps in gasoline are respectively reacted with the gas lumps and the coke lumps;

[0078] The olefin lumps in gasoline are respectively reacted with the paraffin lumps in gasoline, the gas lumps and the coke lumps;

[0079] The naphthene lumps in gasoline are respectively reacted with the gas lumps, the aromatic lumps in gasoline and the coke lumps;

[0080] The aromatic lumps in gasoline are respectively reacted with the gas lumps and the coke lumps.

[0081] S2. Establish a reaction kinetic model according to the reaction network; the kinetic model includes a riser reactor kinetic model and a fluidized bed reactor kinetic model.

[0082] The riser reactor kinetic model is obtained based on the continuity equation and reaction rate of the riser reactor:

[0083] The reaction rate of the chemical reaction in the riser reactor is:

[0084]

[0085] Among them, θ(C Riser ) is the influence function of the catalyst carbon content in the riser reactor on the reaction rate, k j is the reaction rate constant of reaction j (cm 3 / (g·h)), ρc is the catalyst density relative to the volume of the riser reactor (g / cm 3), where ε is the void fraction, P is the system pressure (Pa) in the riser reactor, R is the gas constant (8.314 J / (mol·K)), and T is the system temperature (K) in the riser reactor.

[0086] The reaction rate constant of reaction j in the riser reactor is:

[0087]

[0088] Among them, A j is the pre-exponential factor, E j is the activation energy, R is the gas constant (8.314 J / (mol·K)), and T is the system temperature (K) in the riser reactor.

[0089] For the i-th lumping in the riser reactor, its reaction rate equation is:

[0090]

[0091] Among them, n r is the number of reactions in the riser reactor, v i，j is the stoichiometric coefficient of the i-th lumping in reaction j, and r j represents the rate of the j-th reaction.

[0092] The continuity equation of chemical reactions in the riser reactor is:

[0093]

[0094] Among them, ρ represents the density of the oil-gas mixture (g / cm 3 ), t represents the reaction time, G v represents the mass flow rate of the oil-gas cross-section (g / (cm 2 ·h)), x Riser represents the distance from the riser inlet into the reactor, a i is the concentration of the i-th lumping (molesi / g gas), R i represents the reaction rate of the i-th lumping, n r is the number of reactions in the riser reactor, v i，j is the stoichiometric coefficient of the i-th lumping in reaction j, and r j represents the rate of the j-th reaction, and P is the pressure (Pa) in the riser reactor.

[0095] The kinetic model of the riser reactor is:

[0096]

[0097] Among them, X Riser = x Riser / HRiser The dimensionless relative distance H at the cross-section in the x-direction of the bed layer Riser represents the height of the riser reactor, x Riser represents the distance from the inlet of the riser reactor into the reactor, a = [a1,..., a Riser 17 T is the vector of lumped component concentrations, θ(C Riser ) represents the catalyst carbon function in the riser reactor, S WH is the true weight hourly space velocity, a i is the concentration of the i-th lumped component (molesi / g gas), K is the reaction rate constant matrix in the riser reactor, and P is the pressure in the riser reactor (Pa).

[0098] Among them, θ(C Riser ) = exp(-k W ·C Riser ), C Riser is the catalyst carbon content (w%) in the riser reactor, and k W is the catalyst carbon influence constant.

[0099] The kinetic model of the fluidized bed reactor is obtained based on the continuity equation and reaction rate of the fluidized bed reactor:[[]]

[0100] The reaction rate of the chemical reaction in the fluidized bed reactor is:[[]]

[0101]

[0102] Among them, θ(C Bed ) is the influence function of the catalyst carbon content on the reaction rate in the fluidized bed reactor, k j is the reaction rate constant of reaction j (cm 3 / (g·h)), ρ c is the catalyst density relative to the volume of the fluidized bed reactor (g / cm 3 ), ε is the void fraction, P is the system pressure in the fluidized bed reactor (Pa), R is the gas constant (8.314 J / (mol·K)), and T is the system temperature in the fluidized bed reactor (K).

[0103] The reaction rate constant of reaction j in the fluidized bed reactor is:[[]]

[0104]

[0105] Among them, A j is the pre-exponential factor, E j is the activation energy, R is the gas constant (8,314 J / (mol·K)), and T is the system temperature in the fluidized bed reactor (K). ​​

[0106] The continuity equation for the chemical reaction in the fluidized bed reactor is as follows:

[0107]

[0108] Among them, ρ represents the density of the oil-gas mixture (g / cm 3 ), t represents the reaction time, G v represents the mass flow rate of the oil-gas cross-section (g / (cm 2 ·h)), x Bed represents the distance from the inlet of the fluidized bed into the reactor, a i is the concentration of the i-th lumping (molesi / g gas), R i represents the reaction rate of the i-th lumping, n r is the number of reactions in the fluidized bed reactor, v i，j is the stoichiometric coefficient of the i-th lumping in the j-th reaction, r j represents the rate of the j-th reaction, and P is the pressure in the fluidized bed reactor (Pa).

[0109] The kinetic model of the fluidized bed reactor is as follows:

[0110]

[0111] Among them, X Bed = x Bed / H Bed is the dimensionless relative distance at the x bed section in the fluidized bed layer, x bed is the distance from the inlet of the fluidized bed into the fluidized bed reactor, H bed is the height of the fluidized bed reactor, C bed is the fixed carbon of the catalyst in the fluidized bed reactor, a = [a1,..., a 17 T is the lumped component concentration vector, θ(C Bed ) represents the catalyst fixed carbon function in the fluidized bed reactor, S WH is the true weight hourly space velocity, a i is the concentration of the i-th lumping (molesi / g gas), K is the reaction rate constant matrix in the fluidized bed reactor, and P is the pressure in the fluidized bed reactor (Pa).

[0112] Among them, θ(C Bed ) = exp(-k W ·C Bed ), C Bed is the fixed carbon of the catalyst in the fluidized bed reactor (w%), and k W is the catalyst fixed carbon influence constant.

[0113] ​S3. Construct a prediction model based on the kinetic model, predict the content of each feedstock lumping through the feedstock properties, and substitute it into the prediction model to predict the yields of each product lumping. The prediction model includes a riser reactor prediction model and a fluidized bed reactor prediction model. Both the riser reactor prediction model and the fluidized bed reactor prediction model introduce a catalyst carbon content function to characterize its influence on the yield.

[0114] The prediction model of the riser reactor is:

[0115]

[0116] where X Riser = x Riser / H Riser is the dimensionless relative distance at the x Riser cross-section in the bed layer, H Riser represents the height of the riser reactor, x Riser represents the distance from the riser inlet into the reactor, y i is the mass fraction of each component, M i is the average relative molecular weight of the i-th lumping in the riser reactor, Y Riser is the mass fraction vector of each lumping component in the riser reactor, S WH is the true weight hourly space velocity, y i is the mass fraction of the i-th lumping, K is the reaction rate constant matrix in the riser reactor, exp(-k W ·C Riser ) is the catalyst carbon content function in the riser reactor, and P is the pressure (Pa) in the riser reactor.

[0117] The mass fraction vector of each lumping component in the riser reactor is:

[0118] Y Riser = [y HP , y HN , y HA , y FA , y MP , y MN , y MA , y LP , y LN , y LA , y LHA , y GP , y GO , y GN , y GA , y GS , y CK T

[0119] where y HP ​is the mass fraction of paraffin lumps in the residue oil layer, y HN is the mass fraction of naphthene lumps in the residue oil layer, y HA is the mass fraction of aromatic lumps in the residue oil layer, y FA is the mass fraction of aromatic lumps in the gum-asphalt, y MP is the mass fraction of paraffin lumps in the gas oil layer, y MN is the mass fraction of naphthene lumps in the gas oil layer, y MA is the mass fraction of aromatic lumps in the gas oil layer, y LP is the mass fraction of paraffin lumps in the diesel oil layer, y LN is the mass fraction of naphthene lumps in the diesel oil layer, y LA is the mass fraction of single-ring aromatic lumps in the diesel oil layer, y LHA is the mass fraction of multi-ring aromatic lumps in the diesel oil layer, y GP is the mass fraction of paraffin lumps in the gasoline, y GO is the mass fraction of olefin lumps in the gasoline, y GN is the mass fraction of naphthene lumps in the gasoline, y GA is the mass fraction of aromatic lumps in the gasoline, y GS is the mass fraction of gas lumps, y CK is the mass fraction of coke lumps, and T is the temperature (K) in the riser reactor.

[0120] The catalyst carbon content in the riser reactor is:

[0121]

[0122] where y CK is the fraction of coke in the riser reactor, and R CO is the catalyst-to-oil ratio in the riser reactor. The oil-gas flow rate in the riser reactor is high and the residence time is short, so backmixing can be ignored. Therefore, the riser reactor can be regarded as a plug flow reactor. The catalyst carbon content changes along the axial direction of the riser reactor, which makes the value of the catalyst carbon content function change along the axial direction of the riser reactor. According to the prediction model, the fraction of products in the riser reactor can be accurately calculated.

[0123] The prediction model of the fluidized bed reactor is:

[0124]

[0125] where X Bed = x Bed / H Bed is the dimensionless relative distance at the x bed section in the fluidized bed layer, x bed is the distance from the fluidized bed inlet into the fluidized bed reactor, and H bedis the height of the fluidized bed reactor, C bed is the fixed carbon of the catalyst in the fluidized bed reactor, k W is the fixed carbon influence constant of the catalyst in the fluidized bed (cm 3 / (g / h)), P is the system pressure in the fluidized bed reactor, R is the gas constant (8.314 J / (mol·K)), T is the system temperature in the fluidized bed reactor (K), S WH is the true weight hourly space velocity, y i is the mass fraction of each component, M i is the average relative molecular weight of the i-th lumping in the fluidized bed reactor, K is the reaction rate constant matrix in the fluidized bed reactor, Y Bed is the mass fraction vector of each lumped component in the fluidized bed reactor.

[0126] Y Bed = [y HP , y HN , y HA , y FA , y MP , y MN , y MA , y LP , y LN , y LA , y LHA , y GP , y GO , y GN , y GA , y GS , y CK T

[0127] Among them, y HP is the mass fraction of the paraffin lumping in the residue oil layer, y HN is the mass fraction of the naphthene lumping in the residue oil layer, y HA is the mass fraction of the aromatic lumping in the residue oil layer, y FA is the mass fraction of the aromatic lumping in the gum asphalt, y MP is the mass fraction of the paraffin lumping in the gas oil layer, y MN is the mass fraction of the naphthene lumping in the gas oil layer, y MA is the mass fraction of the aromatic lumping in the gas oil layer, y LP is the mass fraction of the paraffin lumping in the diesel oil layer, y LN is the mass fraction of the naphthene lumping in the diesel oil layer, y LA is the mass fraction of the single-ring aromatic lumping in the diesel oil layer, y LHA is the mass fraction of the multi-ring aromatic lumping in the diesel oil layer above two rings, y GP is the mass fraction of the gasoline paraffin lumping, y GO is the mass fraction of the gasoline olefin lumping, y​GN is the mass fraction of the gasoline naphthene lumps, y GA is the mass fraction of the gasoline aromatic lumps, y GS is the mass fraction of the gas lumps, y CK is the mass fraction of the coke lumps, and T is the temperature (K) in the fluidized bed reactor.

[0128] The fixed carbon of the catalyst in the fluidized bed reactor is:

[0129]

[0130] Among them, R CO represents the catalyst-oil ratio in the fluidized bed reactor, y CK，Riserout is the coke fraction at the outlet of the riser reactor, and β is the influence degree of reactor structure, reaction conditions, and feedstock oil properties on the fixed carbon of the catalyst. In the fluidized bed reactor, the oil and gas move upward axially in a plug flow, that is, the catalyst moves in a completely mixed flow in the fluidized bed reactor, and the catalyst activity remains stable in the fluidized bed reactor. Therefore, C Bed is a constant value, but not equal to the fixed carbon of the catalyst at the outlet of the riser (C Riser，out ). The catalyst leaves the riser reactor and enters the fluidized bed reactor to continue catalytic cracking, and it further accumulates carbon, and the degree of carbon accumulation is affected by reactor structure, reaction conditions, and feedstock oil properties.

[0131] In this embodiment, the product composition of the fluidized bed reactor is the same as the outlet product composition of the riser reactor.

[0132] Example 2

[0133] An apparatus for establishing a riser and fluidized bed series catalytic cracking reaction model, the establishing apparatus includes a modeling module that uses the riser and fluidized bed series catalytic cracking reaction model described in Example 1 for modeling.

[0134] Example 3

[0135] An electronic device includes a processor and a memory, and the memory stores computer-readable instructions. When the computer-readable instructions are executed by the processor, the above evaluation method can be run.

[0136] In this embodiment, the electronic device includes a modeling device, a processor, a memory, a storage controller, a peripheral interface, an input / output unit, an audio unit, and a display unit, etc.

[0137] 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.

[0138] 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.

[0139] 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.

[0140] 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.

[0141] 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.

[0142] Example 4

[0143] A readable storage medium stores a computer program, and when the computer program is executed by a processor, the steps of the above-mentioned evaluation method are executed.

[0144] In order to verify the effect of the present invention, the following experimental examples are carried out:

[0145] Experimental Example

[0146] According to the method of Example 1, a prediction model of the riser reactor and a prediction model of the fluidized bed reactor were established. The parameters in the models were fitted according to the test data. The properties of the test feedstock oil are shown in Table 1, the product distribution is shown in Table 2, and the average relative error between the fitted values and the test values calculated through Example 1 is shown in Table 3.

[0147] Comparative Example 1

[0148] This Comparative Example 1 is a reaction device model established based on the "New Catalytic Cracking MIP Lumping Reaction Kinetics Model" proposed by Duan Liangwei, Sun Peng, Weng Huixin, etc. in 2012. The parameters in the model were fitted according to the same test data as in the experimental example. The comparison between the fitted values and the test values calculated is shown in Table 3 below.

[0149] Comparative Example 2

[0150] This Comparative Example 2 is a reaction device model established based on the "Lumping Kinetics Model of Heavy Oil Catalytic Cracking MIP Process" proposed by Jiang Hongbo, Zhong Guijiang, Ning Hui, etc. in 2010. The parameters in the model were fitted according to the same test data as in the experimental example. The comparison between the fitted values and the test values calculated is shown in Table 3 below.

[0151] Comparative Example 3

[0152] This Comparative Example 3 is a reaction device model established based on the "Numerical Simulation of MIP Riser Reaction Process Based on Multi-Scale Model" proposed by Lu Bona, Cheng Congli, Lu Weimin, etc. in 2013. The parameters in the model were fitted according to the same test data as in the experimental example. The comparison between the fitted values and the test values calculated is shown in Table 3 below.

[0153] Comparative Example 4

[0154] This comparative example uses a kinetic model established by a catalytic cracking model establishment method (Patent No.: CN110648729A) to construct a product prediction model. The parameters in the model were fitted according to the same test data as in the experimental example. The comparison between the fitted values and the test values calculated is shown in Table 3 below.

[0155] From the comparison of the data in Table 3, it can be seen that the relative error of the product distribution in the experimental example is significantly smaller than that in Comparative Example 1, Comparative Example 2, Comparative Example 3, and Comparative Example 4, indicating that the modeling method proposed by the present invention has higher prediction accuracy. Table 1 Properties of Feedstock Oil Project Feedstock Oil 1 Feedstock Oil 2 Feedstock Oil 3 <![CDATA[Density, (20 °C, kg / m 3 )]]> 923.1 916.7 899.4 <![CDATA[Viscosity, (100 °C, mm 2 / s)]]> 13.5 11.2 6.8 Carbon Residue, w% 3.12 2.08 0.59 Molecular Weight, kg / kmol 500 488 464 H, w% 11.8 11.9 12.1 Saturated Hydrocarbon Content, w% 50.3 61.3 68.0 Aromatics + Resins + Asphaltenes Content, w% 49.7 38.7 32.0 Content below 350°C, w% 1.8 3.6 5.5 Content above 500°C, w% 30.8 20.1 3.6 Table 2 Product Distribution

[0156] Table 3 Average relative error between test values and fitted values Project Experimental Example Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 Product Distribution, w% Dry Gas 2.01 3.97 4.49 5.24 3.65 Liquefied Gas 1.76 4.51 4.19 4.46 3.50 Gasoline 0.11 1.18 1.79 2.08 1.35 Diesel 0.92 2.28 2.74 3.95 2.32 Slurry Oil 1.65 5.19 5.28 5.88 4.26 Coke 1.50 3.95 4.18 4.67 3.31

[0157] The foregoing description of the disclosed embodiments enables those skilled in the art to practice or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Thus, the invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A method for establishing a riser and fluidized bed reactor series model, comprising the following steps: S1. According to the lumping kinetics principle and industrial actual requirements, lump and divide the raw materials and products; establish a reaction network based on the divided lumps; S2. Establish a reaction kinetics model according to the reaction network; S3. Construct a prediction model according to the kinetics model, predict the content of each raw material lump through the properties of the raw materials, and substitute it into the prediction model to predict the yields of each product lump; characterized in that: the kinetics model in S2 includes a riser reactor kinetics model and a fluidized bed reactor kinetics model; the prediction model in S3 includes a riser reactor prediction model and a fluidized bed reactor prediction model. The catalyst fixed carbon function is introduced into both the riser reactor prediction model and the fluidized bed reactor prediction model to characterize its influence on the yield. The catalyst fixed carbon function in the riser reactor prediction model is: θ(C Riser ) = exp(-k W ·C Riser ) Among them, C Riser is the fixed carbon content (w%) of the catalyst in the riser reactor, and k W is the influence constant of the fixed carbon content of the catalyst; where y CK is the fraction of coke in the riser reactor, and R CO is the catalyst-to-oil ratio in the riser reactor; The catalyst fixed carbon function in the fluidized bed reactor prediction model is: θ(C Bed ) = exp(-k W ·C Bed ) Among them, C Bed is the fixed carbon (w%) of the catalyst in the fluidized bed reactor, and k W is the influence constant of the fixed carbon of the catalyst; Among them, R CO represents the catalyst-to-oil ratio in the fluidized bed reactor, y CK,Riser,out is the coke fraction at the outlet of the riser reactor, and β is the influence degree of reactor structure, reaction conditions, and feedstock oil properties on the catalyst carbon deposition.

2. The method for establishing a riser and fluidized bed tandem catalytic cracking reaction model according to claim 1, wherein: The prediction model of the riser reactor in S3 is: Among them, X Riser = x Riser / H Riser The dimensionless relative distance at the x Riser cross-section in the bed layer, and H Riser represents the riser reactor height, and y i is the mass fraction of each component, and x Riser represents the distance from the riser inlet into the reactor, and M i is the average relative molecular weight of the i-th lumping in the riser reactor, and Y Riser is the mass fraction vector of each lumping component in the riser reactor, and S WH is the true weight hourly space velocity, K is the reaction rate constant matrix in the riser reactor, and exp(-k W ·C Riser ) is the catalyst carbon content function in the riser reactor, and P is the pressure (Pa) in the riser reactor.

3. The method for establishing a riser and fluidized bed tandem catalytic cracking reaction model according to claim 1, wherein: The kinetics model of the riser reactor in S2 is: Among them, X Riser = x Riser / H Riser The dimensionless relative distance at the x Riser cross-section in the bed, H Riser represents the height of the riser reactor, x Riser represents the distance from the riser inlet into the reactor, a = [a1,..., a 17 T is the vector of lumped component concentrations, θ(C Riser ) represents the catalyst coke deposition function in the riser reactor, S WH is the true weight hourly space velocity, a i is the concentration of the i-th lumped component (molesi / g gas), K is the reaction rate constant matrix in the riser reactor, and P is the pressure (Pa) in the riser reactor.​ 4. The method for establishing a riser and fluidized bed tandem catalytic cracking reaction model according to claim 1, wherein: The kinetics model of the riser reactor is obtained based on the continuity equation and reaction rate of the riser reactor: The continuity equation is: Among them, ρ represents the density of the oil-gas mixture (g / cm 3 ), t represents the reaction time, G v represents the mass flow rate of the oil-gas cross-section (g / (cm 2 ·h)), x Riser represents the distance from the riser inlet into the reactor, a i is the concentration of the i-th lumping (molesi / g gas), R i represents the reaction rate of the i-th lumping, n r is the number of reactions in the riser reactor, v i,j is the stoichiometric coefficient of the i-th lumping in the j-th reaction, r j represents the rate of the j-th reaction; The reaction rate is: Among them, θ(C Riser ) is the influence function of the catalyst carbon content in the riser reactor on the reaction rate, k j is the reaction rate constant of reaction j (cm 3 / (g·h)), ρ c is the catalyst density relative to the volume of the riser reactor (g / cm 3 ), ε is the void fraction, P is the system pressure of the riser reactor (Pa), R is the gas constant (8.314 J / (mol·K)), and T is the system temperature in the riser reactor (K).

5. The method for establishing a riser and fluidized bed tandem catalytic cracking reaction model according to claim 1, wherein: The prediction model of the fluidized bed reactor is: Among them, X Bed = x Bed / H Bed is the dimensionless relative distance at the x bed cross-section in the fluidized bed layer, x bed is the distance from the fluidized bed inlet into the fluidized bed reactor, H bed is the height of the fluidized bed reactor, C bed is the fixed carbon of the catalyst in the fluidized bed reactor, k W is the influence constant of the fixed carbon of the catalyst in the fluidized bed (cm 3 / (g / h)), P is the system pressure in the fluidized bed reactor, R is the gas constant (8.314 J / (mol·K)), T is the system temperature in the fluidized bed reactor (K), S WH is the true weight hourly space velocity, y i is the mass fraction of each component, M i is the average relative molecular weight of the i-th lumping in the fluidized bed reactor, K is the reaction rate constant matrix in the fluidized bed reactor, Y Bed is the mass fraction vector of each lumping component in the fluidized bed reactor.

6. The method for establishing a riser and fluidized bed series catalytic cracking reaction model according to claim 1, wherein: The lump division of the raw materials is as follows: the raw oil in the riser reactor and the fluidized bed reactor is divided into three layers of residue oil layer, wax oil layer and diesel oil layer according to the distillation range, and further subdivided into 11 raw material lumps, namely residue oil layer paraffin hydrocarbon lump, residue oil layer naphthene hydrocarbon lump, residue oil layer aromatic hydrocarbon lump, aromatic hydrocarbon lump in gum and asphaltene, wax oil layer paraffin hydrocarbon lump, wax oil layer naphthene hydrocarbon lump, wax oil layer aromatic hydrocarbon lump, diesel oil layer paraffin hydrocarbon lump, diesel oil layer naphthene hydrocarbon lump, diesel oil layer single-ring aromatic hydrocarbon lump and diesel oil layer polycyclic aromatic hydrocarbon lump above two rings; the products are divided into 6 lumps, namely gasoline paraffin hydrocarbon lump, gasoline olefin lump, gasoline naphthene hydrocarbon lump, gasoline aromatic hydrocarbon lump, gas lump and coke lump.

7. The method for establishing a riser and fluidized bed tandem catalytic cracking reaction model according to claim 6, wherein: The reaction network in S2 is: Establish reactions between the residue oil layer paraffin hydrocarbon lump and the wax oil layer paraffin hydrocarbon lump, diesel paraffin hydrocarbon lump and coke lump respectively; Establish reactions between the residue oil layer naphthene hydrocarbon lump and the diesel naphthene hydrocarbon lump, wax oil layer naphthene hydrocarbon lump and coke lump respectively; Establish reactions between the residue oil layer aromatic hydrocarbon lump and the wax oil layer aromatic hydrocarbon lump, coke lump and diesel oil layer polycyclic aromatic hydrocarbon lump above two rings respectively; Establish reactions between the aromatic hydrocarbon lump in gum and asphaltene and the wax oil layer aromatic hydrocarbon lump and coke lump respectively; Establish reactions between the wax oil layer paraffin hydrocarbon lump and the gas lump, diesel paraffin hydrocarbon lump, gasoline paraffin hydrocarbon lump, gasoline olefin lump and coke lump respectively; Establish reactions between the wax oil layer naphthene hydrocarbon lump and the gasoline paraffin hydrocarbon lump, gas lump, gasoline olefin lump, diesel naphthene hydrocarbon lump, gasoline naphthene hydrocarbon lump, gasoline aromatic hydrocarbon lump and coke lump respectively; Establish reactions between the wax oil layer aromatic hydrocarbon lump and the gas lump, diesel oil layer single-ring aromatic hydrocarbon lump, diesel oil layer polycyclic aromatic hydrocarbon lump above two rings, gasoline aromatic hydrocarbon lump and coke lump respectively; Reactions are established between the diesel paraffin lumps and the gas lumps, gasoline paraffin lumps, gasoline olefin lumps, and coke lumps respectively; Reactions are established between the diesel naphthene lumps and the gasoline paraffin lumps, gas lumps, gasoline olefin lumps, gasoline naphthene lumps, and coke lumps respectively; Reactions are established between the single-ring aromatic lumps in the diesel layer and the gas lumps, gasoline aromatic lumps, and coke lumps respectively; Reactions are established between the multi-ring aromatic lumps in the diesel layer and the coke lumps respectively; Reactions are established between the gasoline paraffin lumps and the gas lumps and coke lumps respectively; Reactions are established between the gasoline olefin lumps and the gasoline paraffin lumps, gas lumps, and coke lumps respectively; Reactions are established between the gasoline naphthene lumps and the gas lumps, gasoline aromatic lumps, and coke lumps respectively; Reactions are established between the gasoline aromatic lumps and the gas lumps and coke lumps respectively.

8. An apparatus for establishing a riser and fluidized bed series catalytic cracking reaction model, characterized in that: The establishing device includes a modeling module that models using the riser and fluidized bed series catalytic cracking reaction model described in any one of claims 1-7.

9. An electronic device, characterized in that: It includes a processor and a memory, and the memory stores computer-readable instructions. When the computer-readable instructions are executed by the processor, the prediction model described in any one of claims 1-7 can be run.

10. A readable storage medium, on which a computer program is stored, characterized in that: When the computer program is executed by the processor, the steps of the establishing method described in any one of claims 1-7 are run.

Images