Modeling method for BTX production process through hydrogenation reaction and catalytic cracking reaction

Abstract

The modeling method for the BTX production process through the hydrogenation reaction and the catalytic cracking reaction comprises the following steps that S1, according to the lumped kinetics principle, raw materials and products are subjected to lumped division, and a reaction network is established; s2, establishing a reaction kinetic model; s3, establishing a prediction model according to the dynamic model; in the step S1, establishment of the reaction network comprises establishment of a hydrogenation reaction network and establishment of a catalytic cracking reaction network. According to the method, the BTX yield prediction model is established, and the process conditions are optimized according to the prediction result, so that the BTX yield is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of BTX production, in particular to a modeling method for a BTX production process through hydrogenation reaction and catalytic cracking reaction. Background Art

[0002] Benzene, toluene, and xylene (BTX) are essential organic chemical raw materials in the petrochemical industry. BTX can be used to produce a variety of chemical products, including synthetic rubber, synthetic fibers, and synthetic resins, as well as a variety of fine chemicals. Currently, BTX production primarily involves catalytic reforming, aromatization of light hydrocarbons, and steam cracking of gasoline to produce BTX and reforming materials. However, the production of aromatics from low-quality catalytic diesel through hydrogenation and catalytic cracking is a new trend. Modeling this production process to improve BTX yields is crucial. Summary of the Invention

[0003] In order to establish a model for the process of producing BTX by hydrogenation reaction and catalytic cracking reaction of low-quality diesel, the present invention provides a modeling method for the process of producing BTX by hydrogenation reaction and catalytic cracking reaction, which can improve the yield of BTX.

[0004] In order to achieve the above object, the specific scheme adopted by the present invention is: a modeling method for the process of producing BTX by hydrogenation reaction and catalytic cracking reaction, comprising the following steps:

[0005] S1, according to the principle of lumped kinetics, the raw materials and products are lumped and divided and the reaction network is established;

[0006] S2, establish reaction kinetic model;

[0007] S3, establishing a prediction model based on the kinetic model;

[0008] In said S1, establishing the reaction network includes establishing a hydrogenation reaction network and establishing a catalytic cracking reaction network, wherein the establishment of the hydrogenation reaction network needs to be lumped and divided according to the distillation range and the reaction mechanism of the hydrogenation reaction, including: dividing the raw material of the hydrogenation reaction, the inferior catalytic diesel, into a lump of paraffins, a lump of cycloalkanes, a lump of monocyclic aromatics, and a lump of polycyclic aromatics, and dividing the products of the hydrogenation reaction into a lump of gas, a lump of light naphtha paraffins, a lump of light naphtha cycloalkanes, a lump of light naphtha monocyclic aromatics, and a lump of heavy naphtha;

[0009] The establishment of a catalytic cracking reaction network requires lumping and division according to the distillation range and reaction mechanism of the catalytic cracking reaction, including: dividing the raw materials of the catalytic cracking reaction into a lump of paraffins, a lump of cycloalkanes, a lump of monocyclic aromatics and a lump of polycyclic aromatics; and dividing the products of the catalytic cracking reaction into a lump of gas, a lump of light gasoline paraffins, a lump of light gasoline olefins, a lump of light gasoline cycloalkanes, a lump of light gasoline monocyclic aromatics, a lump of heavy gasoline and a lump of heavy components.

[0010] As an optimization of the modeling method of the BTX production process by the above-mentioned hydrogenation reaction and catalytic cracking reaction, the hydrogenation reaction network is:

[0011] The paraffin lump is respectively reacted with the gas lump and the naphtha paraffin lump;

[0012] The naphthene lump is respectively reacted with the gas lump, the naphtha paraffin lump, the paraffin lump and the naphtha naphthene lump;

[0013] The single-ring aromatic lump is respectively reacted with the naphthene lump, the gas lump, the naphtha single-ring aromatic lump and the heavy naphtha lump;

[0014] The multi-ring aromatic lump is respectively reacted with the single-ring aromatic lump;

[0015] The naphtha paraffin lump is reacted with the gas lump;

[0016] The naphtha naphthene lump is respectively reacted with the naphtha paraffin lump and the gas lump;

[0017] The naphtha single-ring aromatic lump is respectively reacted with the gas lump and the naphtha naphthene lump;

[0018] The heavy naphtha lump is reacted with the naphtha single-ring aromatic lump.

[0019] As another optimization of the modeling method of the BTX production process by the above-mentioned hydrogenation reaction and catalytic cracking reaction, the catalytic cracking reaction network is:

[0020] The paraffin lump is respectively reacted with the gas lump, the light gasoline paraffin lump, the light gasoline olefin lump and the heavy gasoline lump;

[0021] The naphthene lump is respectively reacted with the gas lump, the light gasoline paraffin lump, the light gasoline olefin lump, the light gasoline naphthene lump and the heavy gasoline lump;

[0022] The single-ring aromatic lump is respectively reacted with the gas lump, the heavy gasoline lump, the multi-ring aromatic lump and the light gasoline single-ring aromatic lump;

[0023] The multi-ring aromatic lump is reacted with the heavy component lump;

[0024] The heavy gasoline lump is reacted with the light gasoline single-ring aromatic lump;

[0025] The light gasoline paraffin lump is reacted with the gas lump;

[0026] The light gasoline olefin lump is respectively reacted with the gas lump and the light gasoline paraffin lump;

[0027] The light gasoline naphthene lump is respectively reacted with the gas lump and the light gasoline single ring aromatic lump;

[0028] The light gasoline single ring aromatic lump is respectively reacted with the gas and the heavy component lump.

[0029] Another optimization scheme of the modeling method of the BTX production process of the above-mentioned one hydrogenation reaction and catalytic cracking reaction: the kinetic model comprises a hydrogenation kinetic model and a catalytic cracking kinetic model.

[0030] Another optimization scheme of the modeling method of the BTX production process of the above-mentioned one hydrogenation reaction and catalytic cracking reaction: the hydrogenation reaction kinetic model is:

[0031]

[0032]

[0033]

[0034]

[0035]

[0036]

[0037]

[0038]

[0039]

[0040] Wherein, y is the mass content, and subscripts 1-9 are respectively a paraffin lump, a naphthene lump, a single ring aromatic lump, a multi-ring aromatic lump, a light naphtha paraffin lump, a light naphtha naphthene lump, a light naphtha single ring aromatic lump, a heavy naphtha lump and a gas lump; x = h / H is a dimensionless relative distance at the h cross section in the bed, h is the height from the hydrogenation reactor inlet to the cross section, H is the bed height of the hydrogenation reactor, P is the hydrogenation reaction pressure, R is the ideal gas constant, T is the hydrogenation reaction temperature, S WH is the true weight hourly space velocity, MW i is the molecular weight, and k is the reaction rate constant.

[0041] Another optimization scheme of the modeling method of the BTX production process of the above-mentioned one hydrogenation reaction and catalytic cracking reaction: the k is:

[0042]

[0043] wherein k0 is the pre-exponential factor of the hydrogenation reaction, E i is the activation energy of the hydrogenation reaction, T* is the reference reaction temperature, T is the hydrogenation reaction temperature, and R is the ideal gas constant.

[0044] As another optimization of the modeling method of the BTX production process by the hydrogenation reaction and the catalytic cracking reaction, the catalytic cracking kinetic model is:

[0045]

[0046]

[0047]

[0048]

[0049]

[0050]

[0051]

[0052]

[0053]

[0054]

[0055]

[0056] wherein y is the mass content, and subscripts 1-11 are respectively the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light gasoline paraffin lump, the light gasoline olefin lump, the light gasoline naphthene lump, the light gasoline single-ring aromatic lump, the heavy gasoline lump, the heavy component lump, and the gas lump; x = h / H is the dimensionless relative distance at the h cross section in the bed, h is the height from the catalytic cracking reactor inlet to the cross section, H is the bed height of the catalytic cracking reactor, P is the catalytic cracking reaction pressure, R is the ideal gas constant, T is the catalytic cracking reaction temperature, S WH is the true weight hourly space velocity, MW i is the molecular weight, k is the reaction rate constant, y i is the mass content of the i-th lump, in unit 1.

[0057] As another optimization of the modeling method of the BTX production process by the hydrogenation reaction and the catalytic cracking reaction, the prediction model comprises a hydrogen consumption prediction model of the hydrogenation reaction and a BTX yield prediction model.

[0058] As another optimization scheme of the modeling method of the BTX production process by the hydrogenation reaction and the catalytic cracking reaction, the hydrogen consumption prediction model is:

[0059]

[0060] wherein w H is the hydrogen consumption of the hydrogenation reaction, are the mass contents of the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light naphtha paraffin lump, the light naphtha naphthene lump, the light naphtha single-ring aromatic lump, the heavy naphtha lump and the gas lump at the outlet of the hydrogenation reactor, respectively, are the mass contents of the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light naphtha paraffin lump, the light naphtha naphthene lump, the light naphtha single-ring aromatic lump, the heavy naphtha lump and the gas lump at the inlet of the hydrogenation reactor, respectively.

[0061] As another optimization scheme of the modeling method of the BTX production process by the hydrogenation reaction and the catalytic cracking reaction, the BTX yield prediction model is:

[0062]

[0063] wherein, is the catalytic cracking diesel flow outside the system, kg / h, is the catalytic cracking diesel flow circulating in the system, kg / h, is the single-ring aromatic yield of the hydrogenation reaction, unit 1, is the hydrogenation catalytic diesel production of the hydrogenation reaction, unit kg / h, is the single-ring aromatic yield of the cracking reaction, unit 1.

[0064] Compared with the prior art, the present application has the following beneficial effects:

[0065] 1. The present application provides a modeling method of a BTX production process by a hydrogenation reaction and a catalytic cracking reaction, establishes a BTX yield prediction model, and optimizes process conditions according to the prediction results to improve the yield of BTX.

[0066] 2. In the present application, a hydrogen consumption prediction model is established according to the kinetic model of the hydrogenation reaction, the hydrogen consumption of the hydrogenation reaction is predicted, and process conditions are optimized according to the prediction results of the hydrogen consumption and the prediction results of the BTX yield, so as to improve the yield of BTX while reducing the hydrogen consumption. BRIEF DESCRIPTION OF DRAWINGS

[0067] Figure 1 is a combined process flow diagram of LCO hydrogenation reaction and catalytic cracking reaction;

[0068] Figure 2 is a hydrogenation reaction network;

[0069] Figure 3 is a catalytic cracking reaction network. DETAILED DESCRIPTION

[0070] The technical solutions of the present application are further described in detail below in combination with specific embodiments. The parts not described and disclosed in detail in the following embodiments of the present application should be understood as the prior art known or should be known by the skilled in the art.

[0071] EMBODIMENT

[0072] A modeling method of a BTX production process by hydrogenation reaction and catalytic cracking reaction, comprising the following steps:

[0073] S1, according to the principle of lumped kinetics, the raw materials and products are lumped and divided, and a reaction network is established, which includes the establishment of a hydrogenation reaction network and the establishment of a catalytic cracking reaction network.

[0074] Specifically:

[0075] S101, the raw materials and products are lumped and divided: the establishment of a hydrogenation reaction network requires lumped division according to the distillation range and the reaction mechanism of hydrogenation reaction. Specifically, the raw material of hydrogenation reaction is inferior catalytic cracking diesel oil (LCO), and its distillation range is 200-300℃. LCO is divided into paraffin (LP), naphthene (LN), single-ring aromatic hydrocarbon (LA) and multi-ring aromatic hydrocarbon (GA) according to group composition. The raw material of hydrogenation reaction, inferior catalytic cracking diesel oil, is divided into paraffin lump, naphthene lump, single-ring aromatic hydrocarbon lump and multi-ring aromatic hydrocarbon lump according to group composition. After hydrogenation reaction of inferior catalytic cracking diesel oil, hydrogenated naphtha, gas (GS) and hydrogenated catalytic diesel oil are obtained. Among them, hydrogenated naphtha is divided into light naphtha and heavy naphtha with 150℃ as the boundary, i.e. the products of hydrogenation reaction are divided into four groups according to the distillation range, namely gas (GS) (<35℃), light naphtha (35-150℃), heavy naphtha (HG) (150-200℃) and hydrogenated catalytic diesel oil (HLCO) (200-350℃), wherein light naphtha is divided into paraffin (GP), naphthene (GN) and single-ring aromatic hydrocarbon (GA). In summary, the products of hydrogenation reaction are divided into gas lump, light naphtha paraffin lump, light naphtha naphthene lump, light naphtha single-ring aromatic hydrocarbon lump and heavy naphtha lump.

[0076] The establishment of catalytic cracking reaction network needs to be divided according to the distillation range and the reaction mechanism of catalytic cracking reaction. In this embodiment, the distillation range of HLCO and the distillation range of LCO are similar, and HLCO is divided into paraffin (LP), naphthene (LN), single-ring aromatic (LA) and multi-ring aromatic (GA) according to the group composition, and it is considered that the paraffin, naphthene, single-ring aromatic and multi-ring aromatic of LCO are converted into the paraffin, naphthene, single-ring aromatic and multi-ring aromatic of HLCO through hydrogenation reaction, that is, the raw material of catalytic cracking reaction is divided into paraffin collection, naphthene collection, single-ring aromatic collection and multi-ring aromatic collection. The products of catalytic cracking reaction are gas (<35℃), light gasoline (35-150℃), heavy gasoline (HG) (150-200℃), LCO (200-350℃) and heavy component (HO) (>350℃), wherein the light gasoline is divided into paraffin (GP), olefin (GO), naphthene (GN) and single-ring aromatic (GA) catalytic cracking reaction product, and the product is divided into gas collection, light gasoline paraffin collection, light gasoline olefin collection, light gasoline naphthene collection, light gasoline single-ring aromatic collection, heavy gasoline collection and heavy component collection.

[0077] S102, the hydrogenation reaction network and the catalytic cracking reaction network are established. Specifically, in the hydrogenation reaction, the gas is the terminal product, and the naphtha is both the reactant and the product. In the reaction of generating naphtha in the diesel layer, the paraffin is cracked to generate paraffin and naphthene, and the single-ring aromatic is cracked to generate aromatic; in the diesel layer, there are reactions of hydrogenation of multi-ring aromatic to generate single-ring aromatic, hydrogenation of single-ring aromatic to generate naphthene, and hydrogenation of naphthene to generate paraffin; in the naphtha layer, there are reactions of hydrogenation of single-ring aromatic to generate naphthene and hydrogenation of naphthene to generate paraffin; based on the above, the hydrogenation reaction network is established:

[0078] The paraffin collection is respectively reacted with the gas collection and the light naphtha paraffin collection;

[0079] The naphthene collection is respectively reacted with the gas collection, the light naphtha paraffin collection, the paraffin collection and the light naphtha naphthene collection;

[0080] The single-ring aromatic collection is respectively reacted with the naphthene collection, the gas collection, the light naphtha single-ring aromatic collection and the heavy naphtha collection;

[0081] The multi-ring aromatic collection is respectively reacted with the single-ring aromatic collection;

[0082] The light naphtha paraffin collection is reacted with the gas collection;

[0083] The light naphtha naphthene collection is respectively reacted with the light naphtha paraffin collection and the gas collection;

[0084] The light naphtha monocyclic aromatic hydrocarbon cluster is respectively reacted with the gas cluster and the light naphtha naphthenes cluster;

[0085] The heavy naphtha cluster is reacted with the light naphtha monocyclic aromatic hydrocarbon cluster.

[0086] In the catalytic cracking reaction, gas, oil slurry and coke are end products, and gasoline is both a reactant and a product; in the diesel layer to gasoline layer reaction, paraffins are cracked to form paraffins, olefins and heavy gasoline, naphthenes are cracked to form paraffins, olefins, naphthenes and heavy gasoline, monocyclic aromatic hydrocarbons are cracked to form aromatic hydrocarbons and heavy gasoline; the diesel layer has a reaction of monocyclic aromatic hydrocarbons to form polycyclic aromatic hydrocarbons, and the gasoline layer has a reaction of olefins and naphthenes to form paraffins and aromatic hydrocarbons through hydrogen transfer; based on the above, the catalytic cracking reaction network is established:

[0087] The paraffin cluster is respectively reacted with the gas cluster, the light gasoline paraffin cluster, the light gasoline olefin cluster and the heavy gasoline cluster;

[0088] The naphthene cluster is respectively reacted with the gas cluster, the light gasoline paraffin cluster, the light gasoline olefin cluster, the light gasoline naphthene cluster and the heavy gasoline cluster;

[0089] The monocyclic aromatic hydrocarbon cluster is respectively reacted with the gas cluster, the heavy gasoline cluster, the polycyclic aromatic hydrocarbon cluster and the light gasoline monocyclic aromatic hydrocarbon cluster;

[0090] The polycyclic aromatic hydrocarbon cluster is reacted with the heavy component cluster;

[0091] The heavy gasoline cluster is reacted with the light gasoline monocyclic aromatic hydrocarbon cluster;

[0092] The light gasoline paraffin cluster is reacted with the gas cluster;

[0093] The light gasoline olefin cluster is respectively reacted with the gas cluster and the light gasoline paraffin cluster;

[0094] The light gasoline naphthene cluster is respectively reacted with the gas cluster and the light gasoline monocyclic aromatic hydrocarbon cluster;

[0095] The light gasoline monocyclic aromatic hydrocarbon is respectively reacted with the gas and the heavy component cluster.

[0096] S2, a reaction kinetics model is established, including establishing a hydrogenation kinetics model and establishing a catalytic cracking kinetics model.

[0097] The hydrogenation kinetics model is:

[0098]

[0099]

[0100]

[0101]

[0102]

[0103]

[0104]

[0105]

[0106]

[0107] wherein y is the mass content, unit 1, the subscripts 1-9 are respectively paraffin lump, naphthene lump, single-ring aromatic hydrocarbon lump, multi-ring aromatic hydrocarbon lump, light naphtha paraffin lump, light naphtha naphthene lump, light naphtha single-ring aromatic hydrocarbon lump, heavy naphtha lump and gas lump; x = h / H is the dimensionless relative distance at the cross section h in the bed, h is the height from the inlet of the hydrogenation reactor to the cross section, unit m; H is the bed height of the hydrogenation reactor, unit m; P is the hydrogenation reaction pressure, unit Pa; R is the ideal gas constant, R = 8.314 kJ / (kmol·K); T is the hydrogenation reaction temperature, unit K; S WH is the true weight hourly space velocity, unit g feed (oil + H2) / (h·g(catalyst)); MW i is the molecular weight, unit kg / kmol; k is the reaction rate constant, unit (m 3 / (kg catalyst·h).

[0108] The calculation formula of the above k is:

[0109]

[0110] wherein k0 is the pre-exponential factor of the hydrogenation reaction, E i is the activation energy of the hydrogenation reaction, T* is the reference reaction temperature, and R is the gas constant.

[0111] The catalytic cracking reaction kinetics model is:

[0112]

[0113]

[0114]

[0115]

[0116]

[0117]

[0118]

[0119]

[0120]

[0121]

[0122]

[0123] wherein y is the mass content, the subscripts 1-11 are the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light gasoline paraffin lump, the light gasoline olefin lump, the light gasoline naphthene lump, the light gasoline single-ring aromatic lump, the heavy gasoline lump, the heavy component lump and the gas lump, respectively; x = h / H is the dimensionless relative distance at the cross section h in the bed, h is the height from the inlet of the catalytic cracking reactor to the cross section, H is the bed height of the catalytic cracking reactor, P is the catalytic cracking reaction pressure, R is the ideal gas constant, T is the catalytic cracking reaction temperature, S is the cross-sectional area of the catalytic cracking reactor, and the units of x, h, H, P, R, T and S are dimensionless, m, m, m, Pa, J / mol / K, K and m2, respectively. WH is the true weight hourly space velocity, MW i is the molecular weight, k is the reaction rate constant, y i is the mass content in the i-th lump, and the unit is 1.

[0124] S3, establishing a prediction model according to the kinetic model, the prediction model comprising a hydrogen consumption prediction model of the hydrogenation reaction and a BTX yield prediction model.

[0125] According to the combined process of the hydrogenation reaction and the catalytic cracking reaction, the hydrogenation reaction kinetic model and the catalytic cracking reaction kinetic model are integrated, specifically, the initial value of the raw material in the hydrogenation reaction is:

[0126]

[0127]

[0128]

[0129]

[0130] wherein, is the LP mass content of the LCO hydrogenation feed, the unit is 1, is the LCO flow rate from outside the system, kg / h, is the LP mass content of the LCO from outside the system, the unit is 1, is the LCO flow rate circulating in the system, kg / h, LP mass content of LCO circulating in the system, unit 1, LN mass content of LCO in hydrogenation feed, unit 1, LN mass content of LCO from outside the system, unit 1, LN mass content of LCO circulating in the system, unit 1, LA mass content of LCO in hydrogenation feed, unit 1, LA mass content of LCO from outside the system, unit 1, LA mass content of LCO circulating in the system, unit 1, LHA mass content of LCO in hydrogenation feed, unit 1, LHA mass content of LCO from outside the system, unit 1, LHA mass content of LCO circulating in the system, unit 1.

[0131] The content of the catalytic cracking reaction raw material is calculated by the hydrogenation reaction kinetics model:

[0132]

[0133]

[0134]

[0135]

[0136] wherein, LP mass content of HLCO generated by hydrogenation reaction, unit 1, LP mass content of HLCO generated by hydrogenation reaction, unit 1, LN mass content of HLCO generated by hydrogenation reaction, unit 1, LA mass content of HLCO generated by hydrogenation reaction, unit 1, LHA mass content of HLCO generated by hydrogenation reaction, unit 1.

[0137] The monocyclic aromatic hydrocarbon content of light naphtha and the monocyclic aromatic hydrocarbon content of light petroleum can be obtained by the hydrogenation reaction and catalytic cracking reaction kinetics model, and the BTX yield can be calculated according to the contents of the two, that is, the prediction model of the BTX yield is obtained:

[0138]

[0139] wherein, LCO flow from outside the system, kg / h, LCO flow circulating in the system, kg / h, GA yield for hydrogenation reaction, unit 1, HLCO yield for hydrogenation reaction, unit kg / h, GA yield for cracking reaction, unit 1.

[0140] According to the prediction results, the process conditions are optimized to improve the yield of BTX.

[0141] The hydrogen consumption of the hydrogenation reaction is obtained by the hydrocarbon group composition of LCO before hydrogenation and the distribution of the product after hydrogenation, i.e., the hydrogen consumption prediction model is obtained:

[0142]

[0143] wherein, w H hydrogen consumption of the hydrogenation reaction, respectively, the mass content of the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light naphtha paraffin lump, the light naphtha naphthene lump, the light naphtha single-ring aromatic lump, the heavy naphtha lump and the gas lump at the outlet of the hydrogenation reactor, respectively, the mass content of the paraffin lump, the naphthene lump, the single-ring aromatic lump, the multi-ring aromatic lump, the light naphtha paraffin lump, the light naphtha naphthene lump, the light naphtha single-ring aromatic lump, the heavy naphtha lump and the gas lump at the inlet of the hydrogenation reactor.

[0144] According to the prediction results of the hydrogen consumption and the prediction results of the BTX yield, the process conditions are optimized to improve the yield of BTX while reducing the hydrogen consumption.

[0145] The above description of disclosed embodiments enables one of ordinary skill in the art to make or use the application. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein can be applied to other embodiments without departing from the spirit or scope of the application. Thus, the present application 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 modeling method for a BTX production process by hydrogenation reaction and catalytic cracking reaction, comprising the following steps: S1, according to the principle of lumped kinetics, the raw materials and products are lumped and divided and the reaction network is established; S2, establish reaction kinetic model; S3, establishing a prediction model based on the kinetic model; It is characterized in that: in said S1, establishing the reaction network includes establishing a hydrogenation reaction network and establishing a catalytic cracking reaction network, wherein the establishment of the hydrogenation reaction network needs to be lumped and divided according to the distillation range and the reaction mechanism of the hydrogenation reaction, including: dividing the raw material of the hydrogenation reaction, the inferior catalytic diesel, into a lump of paraffins, a lump of cycloalkanes, a lump of monocyclic aromatics and a lump of polycyclic aromatics, and dividing the products of the hydrogenation reaction into a lump of gas, a lump of light naphtha paraffins, a lump of light naphtha cycloalkanes, a lump of light naphtha monocyclic aromatics and a lump of heavy naphtha; The establishment of a catalytic cracking reaction network requires lumping and division according to the distillation range and reaction mechanism of the catalytic cracking reaction, including: dividing the raw materials of the catalytic cracking reaction into a lump of paraffins, a lump of cycloalkanes, a lump of monocyclic aromatics and a lump of polycyclic aromatics; and dividing the products of the catalytic cracking reaction into a lump of gas, a lump of light gasoline paraffins, a lump of light gasoline olefins, a lump of light gasoline cycloalkanes, a lump of light gasoline monocyclic aromatics, a lump of heavy gasoline and a lump of heavy components.

2. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 1, characterized in that: The hydrogenation reaction network is: Reactions are established between the paraffin aggregate and the gas aggregate and the light naphtha paraffin aggregate respectively; Reactions are established between the cycloalkanes aggregate and the gas aggregate, the light naphtha paraffins aggregate, the paraffins aggregate and the light naphtha cycloalkanes aggregate respectively; Reactions are established between the monocyclic aromatic hydrocarbons aggregate, the cycloalkanes aggregate, the gas aggregate, the light naphtha monocyclic aromatic hydrocarbons aggregate and the heavy naphtha aggregate respectively; The polycyclic aromatic hydrocarbons aggregates were reacted with the monocyclic aromatic hydrocarbons aggregates respectively; The light naphtha paraffin aggregate is reacted with the gas aggregate; The light naphtha cycloalkanes aggregate is reacted with the light naphtha paraffins aggregate and the gas aggregate respectively; The light naphtha monocyclic aromatic hydrocarbons aggregate is reacted with the gas aggregate and the light naphtha cycloalkanes aggregate respectively; A reaction is established between the heavy naphtha aggregate and the light naphtha monocyclic aromatic hydrocarbon aggregate.

3. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 1, characterized in that: The catalytic cracking reaction network is: The paraffinic hydrocarbons are set up to react with the gas mass, the light gasoline paraffinic hydrocarbons mass, the light gasoline olefinic hydrocarbons mass and the heavy gasoline mass respectively; the cycloalkanes are set up to react with the gas mass, the light gasoline paraffinic hydrocarbons mass, the light gasoline olefinic hydrocarbons mass, the light gasoline cycloalkanes mass and the heavy gasoline mass respectively; Reactions are established between the monocyclic aromatic hydrocarbons aggregate and the gas aggregate, heavy gasoline aggregate, polycyclic aromatic hydrocarbons aggregate and light gasoline monocyclic aromatic hydrocarbons aggregate respectively; Establishing a reaction between the aggregated PAHs and the aggregated recombinant components; Establishing a reaction between the aggregate of heavy gasoline and the aggregate of single-ring aromatic hydrocarbons in light gasoline; The light gasoline paraffin aggregate is reacted with the gas aggregate; The light gasoline olefins aggregate is reacted with the gas aggregate and the light gasoline paraffins aggregate respectively; The light gasoline cycloalkanes aggregate is reacted with the gas aggregate and light gasoline monocyclic aromatics respectively; The monocyclic aromatic hydrocarbons of light gasoline are reacted with gas and heavy components respectively.

4. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 1, characterized in that: The kinetic model includes a hydrogenation kinetic model and a catalytic cracking kinetic model.

5. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 4, characterized in that: The hydrogenation reaction kinetic model is: Where y is the mass content, subscripts 1-9 are the total paraffins, total cycloalkanes, total monocyclic aromatics, total polycyclic aromatics, total light naphtha paraffins, total light naphtha cycloalkanes, total light naphtha monocyclic aromatics, total heavy naphtha, and total gas, respectively; x = h / H is the dimensionless relative distance at the h section in the bed, h is the height from the hydrogenation reactor inlet to the cross section, H is the hydrogenation reactor bed height, P is the hydrogenation reaction pressure, R is the ideal gas constant, T is the hydrogenation reaction temperature, S WH is the true weight hourly space velocity, MW i is the molecular weight, k is the reaction rate constant, and the subscript i represents the i-th reaction in the reaction network.

6. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 5, characterized in that: The k is: Where k0 is the pre-exponential factor of the hydrogenation reaction, E i is the activation energy of the hydrogenation reaction, T* is the reference reaction temperature, T is the hydrogenation reaction temperature, and R is the ideal gas constant.

7. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 4, characterized in that: The catalytic cracking kinetic model is: Wherein, y is the mass content, subscripts 1-11 are the total paraffins, total cycloalkanes, total monocyclic aromatics, total polycyclic aromatics, total light gasoline paraffins, total light gasoline olefins, total light gasoline cycloalkanes, total light gasoline monocyclic aromatics, total heavy gasoline, total heavy components, and total gas, respectively; x = h / H is the dimensionless relative distance at the h-section in the bed, h is the height from the catalytic cracking reactor inlet to the cross section, H is the catalytic cracking reactor bed height, P is the catalytic cracking reaction pressure, R is the ideal gas constant, T is the catalytic cracking reaction temperature, S WH is the true weight hourly space velocity, MW i is the molecular weight, k is the reaction rate constant, y i is the mass content of the i-th lumped element, unit 1.

8. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 1, characterized in that: The prediction model includes a hydrogen consumption prediction model for hydrogenation reaction and a BTX yield prediction model.

9. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 8, characterized in that: The hydrogen consumption prediction model is: Among them, w H is the hydrogen consumption of the hydrogenation reaction, are the mass contents of the total paraffins, total cycloalkanes, total monocyclic aromatics, total polycyclic aromatics, total light naphtha paraffins, total light naphtha cycloalkanes, total light naphtha monocyclic aromatics, total heavy naphtha and total gas at the outlet of the hydrogenation reactor, respectively. They are the mass contents of total paraffins, total cycloalkanes, total monocyclic aromatics, total polycyclic aromatics, total light naphtha paraffins, total light naphtha cycloalkanes, total light naphtha monocyclic aromatics, total heavy naphtha and total gas at the inlet of the hydrogenation reactor.

10. The modeling method for a process of producing BTX by hydrogenation reaction and catalytic cracking reaction according to claim 8, characterized in that: The BTX yield prediction model is: in, is the catalytic cracking diesel flow rate from outside the system, kg / h, is the catalytic cracking diesel flow rate circulating in the system, kg / h, is the yield of monocyclic aromatic hydrocarbons in hydrogenation reaction, unit 1, is the hydrogenation catalytic diesel production in the hydrogenation reaction, in kg / h. is the yield of monocyclic aromatic hydrocarbons in cracking reaction, unit 1.

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