CN114446404A - Control method and system for carbon dioxide hydrogenation reactor - Google Patents

Abstract

The invention discloses a control method and a control system for a carbon dioxide hydrogenation reactor. The automatic control method of the carbon dioxide hydrogenation reactor comprises the following steps: acquiring operation data and operation data of a carbon dioxide hydrogenation reactor; performing classified statistics on the operation data and the operation data to obtain real-time statistical data; fitting and calculating the real-time statistical data through a carbon dioxide hydrogenation load distribution model to obtain an operation parameter set value; controlling the carbon dioxide hydrogenation reactor based on the operating parameter set value. According to the method and the system disclosed by the invention, the operation parameter set value is obtained by fitting and calculating the real-time statistical data through the carbon two hydrogenation load distribution model, the carbon two hydrogenation reactor is controlled based on the operation parameter set value, the automatic control of the carbon two hydrogenation reactor is realized, the operation parameters of the reactor are optimized, and the purposes of reducing the energy and material consumption and prolonging the full-life operation period of the catalyst are achieved.

Description

Control method and system for carbon dioxide hydrogenation reactor

Technical Field

The invention belongs to the field of petrochemical industry, and particularly relates to a control method and a control system for a carbon dioxide hydrogenation reactor.

Background

Ethylene technology is the leading technology of petrochemical industry, and the ethylene technology level is regarded as an important mark for measuring the development level of the petrochemical industry in China. Trienes (ethylene, propylene, butadiene) produced by an ethylene cracking device are basic raw materials of petrochemical industry, and the high and low yield of the trienes is a main mark for measuring the development level of the national petrochemical industry.

After the liquid hydrocarbon raw materials such as naphtha and the like in the ethylene cracking device are subjected to steam cracking and separation, the carbon-two fraction contains ethylene, ethane and a small amount of acetylene, and the content of the acetylene is about 0.5-3 percent (volume). In downstream polymerization reactions, the presence of acetylene poisons the polyolefin promoters and must be removed to obtain polymer grade ethylene. The acetylene removal method widely used at present is a catalytic selective hydrogenation method. The acetylene in the carbon dioxide fraction is removed by two processes, namely a solvent absorption method and a catalytic selective hydrogenation method.

The catalytic selective hydrogenation method has the advantages of simple process flow, less energy consumption and no environmental pollution, can increase the yield of target products, and becomes the most common economic and simple method at present along with the continuous improvement of the performance of novel efficient hydrogenation catalysts and the increasing popularity of the hydrogenation method. According to different process routes, the method can be divided into pre-hydrogenation and post-hydrogenation. The post-hydrogenation process is suitable for separation processes mainly comprising sequential separation, pre-depropanization and post-hydrogenation, pre-deethanization and post-hydrogenation and the like, and is a process of adding a proper amount of hydrogen into the remaining pure carbon two-fraction for hydrogenation after light fractions containing hydrogen, CO, methane and the like and heavy fractions containing three or more carbon atoms and the like in the pyrolysis gas.

The carbon hydrogenation reactor unit is an important link for refining ethylene products, and is used for selectively hydrogenating acetylene in the carbon-containing fraction into ethylene under the action of a catalyst. Ethylene loss if excess hydrogenation of acetylene to ethane results; or acetylene is polymerized to generate oligomers or even high polymers, which affects the service cycle of the reactor; if the acetylene hydrogenation activity is not good, the volume content of the acetylene at the outlet of the reactor cannot be controlled within the index requirement range, and the ethylene product is unqualified, which can directly affect the ethylene product and a downstream industrial chain, so that the operation quality of the carbon dioxide hydrogenation reactor plays a vital role in both enterprise benefit and national civilization.

The carbon dioxide hydrogenation catalyst generally adopts palladium noble metal as an active component, and the production suppliers comprise China petrochemical catalyst company, Clariant company, PHILIPS company and the like. The thermodynamic parameters, the surface adsorption and desorption reaction rates and the process sensitivity of each brand of catalyst of each manufacturer are different, and the optimal performance can be ensured by targeted adjustment and optimization.

At present, the production control of the carbon dioxide hydrogenation reactor generally adopts manual regulation and control, and technicians manually regulate and control related parameters. Because the cracking separation process is long, the process is complex, the energy of personnel is limited, and the carbon dioxide hydrogenation reactor cannot be monitored, adjusted and optimized in real time. When the carbon dioxide hydrogenation system has unstable conditions such as material composition, pressure, temperature, flow, hydrogen fluctuation and the like, the stability recovery is very slow by the hydrogenation system, and the superposition phenomenon generated by multiple fluctuations makes the system in a metastable state for a long time, so that acetylene leakage and ethylene loss at the outlet of the reactor are easily caused, and the ethylene yield and the separation effect of the rectifying tower are influenced.

At present, most of the operations of the carbon dioxide hydrogenation reactors adopt a method of manual experience and manual adjustment, and in order to ensure that acetylene in ethylene products is removed to be qualified, excessive hydrogenation of the carbon dioxide hydrogenation reactor in a single-stage bed or a last-stage bed is easily caused, so that the volume content of the acetylene in the final hydrogenation product tends to 0ppm, and the ethylene loss is large. Thereby causing a problem of low ethylene selectivity of the carbohydrogenator.

Disclosure of Invention

In view of the above, the invention provides a control method and a control system for a carbon dioxide hydrogenation reactor, which at least solve the problems of high energy and material consumption and short full-life operation cycle of a catalyst in the prior art.

In a first aspect, the present invention provides a method for controlling a carbon dioxide hydrogenation reactor, comprising:

acquiring operation data and operation data of a carbon dioxide hydrogenation reactor;

performing classified statistics on the operation data and the operation data to obtain real-time statistical data;

fitting and calculating the real-time statistical data through a carbon dioxide hydrogenation load distribution model to obtain an operation parameter set value;

controlling the carbon dioxide hydrogenation reactor based on the operating parameter set value.

Optionally, the carbon dioxide hydrogenation load distribution model comprises a set value model of acetylene hydrogenation conversion amount and a set value model of outlet acetylene volume content;

the set value model of the acetylene hydrogenation conversion amount is as follows:

in the formula, Y_nThe preset value of the hydrogenation conversion amount of the acetylene in the nth section bed; f_n(X) is the nth stage bed hydrogenation distribution function, where N is 1, 2, … (N-1); x is the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor; n is the total number of segments of the carbon two hydrogenation reactor; a is_iIs a segment number influence factor, associated with the total number of segments N, where i ═ 1, 2, … (N-1);

the set value model of the volume content of the outlet acetylene is as follows:

in the formula, M_{n out}Is a set value of the volume content of acetylene at the outlet of the nth section of the bed, wherein n is equal to1，2，…(N-1)；Y_kIs the set value of the acetylene hydrogenation conversion amount of the k-th bed, wherein k is 1, 2, … n.

Optionally, the volume content set value of acetylene at the outlet of the last bed is M_{end out}，M_{end out}To specify the constant Ω, the value range of Ω is 0<Ω<1ppm。

Optionally, the value range of the total number N of the carbon dioxide hydrogenation reactor is as follows: 1< N < 6;

the value range of the volume content X of acetylene in the total inlet material of the carbon hydrogenation reactor is as follows: x is more than or equal to 0.3 percent and less than or equal to 5.5 percent.

F_n(X) is independent of the total number of the reactor sections and is related to the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor.

Optionally, after the step of obtaining the set value of the operation parameter by performing fitting calculation on the real-time statistical data through the carbon dioxide hydrogenation load distribution model module, the method further includes:

optimizing the operating parameter set point, the optimizing the operating parameter set point comprising:

establishing a functional relation for the acetylene hydrogenation conversion amount of each section of bed and the selected operation parameters through the carbon dioxide hydrogenation load distribution model, wherein the functional relation is as follows:

Y＝G(R，T，M_in)+ΔE(Fl，P)，

in the formula, Y is the acetylene conversion amount of each reactor section, R is the volume content ratio of hydrogen to acetylene at the inlet of each reactor section, T is the material temperature at the inlet of each reactor section, and M is_inThe volume content of acetylene at the inlet of each reactor section; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbo-hydrogenation reactor, and G is a control function of the hydrogenation activity of each section of reactor; and the delta E is a disturbance compensation function of the hydrogenation activity of each reactor section.

Optionally, the optimizing the operation parameter setting value further includes:

establishing a function relation between the material temperature at the inlet of each section of the bed and the set value of the hydrogen alkyne ratio, wherein the function relation is as follows:

R_n＝G′(T_n)+ΔE(Fl，P)，

R_end＝G′(T_end)+ΔE(Fl，P)，

R_nis the volume content ratio set value of the hydrogen and the acetylene at the inlet of the nth section of the bed, T_nIs the material temperature set value at the inlet of the nth section of bed; wherein N is 1, 2, … (N-1); r is_end，T_endThe volume content ratio of the hydrogen and the acetylene at the inlet of the last stage bed and the inlet material temperature and inlet material temperature set values are respectively, and G' is a temperature control function of the hydrogenation activity of each stage of reactor.

Optionally, the optimizing the operation parameter setting value further includes:

and establishing a functional relationship between the acetylene selectivity of each section of the bed and the selected operation parameters, wherein the functional relationship is as follows:

S＝Q(R，T，M_in，M_out)+ΔR(Fl，P)，

wherein S is the ethylene selectivity of each section of bed, R is the volume content ratio of hydrogen to acetylene at the inlet of each section, T is the material temperature at the inlet of each section of bed, and M is_inVolume content of acetylene at the entrance of each bed, M_outThe volume content of acetylene at the outlet of each section of bed; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbo-hydrogenation reactor, and Q is a selective control function of each section of the reactor; Δ R disturbance compensation function for each stage reactor selectivity.

Optionally, the optimizing the operation parameter setting value further includes:

establishing a functional relation between the set value of the temperature of the material at the inlet of each section of the bed and the selectivity of the ethylene, wherein the functional relation is as follows:

S_n＝Q′(T_n)+ΔR(Fl，P)，

S_end＝Q′(T_end)+ΔR(Fl，P)，

in the formula, S_n、S_endEthylene selectivity, T, for the n-th and last-stage beds, respectively_n、T_endRespectively setting the material temperature at the inlet of the nth section bed and the material temperature at the inlet of the last section bed; wherein N is 1, 2, … (N-1),q' is a temperature control function of the selectivity of each section of bed.

Optionally, the optimizing the operation parameter setting value further includes:

acquiring inlet temperature set values corresponding to the maximum ethylene selectivity values obtained by establishing a functional relation between the inlet material temperature set values of all sections of beds and the ethylene selectivity;

obtaining a hydrogen and acetylene volume content ratio set value obtained by establishing a functional relation between the inlet material temperature of each section of bed and the hydrogen-acetylene ratio set value;

and returning the inlet temperature set value and the hydrogen-acetylene volume content ratio set value corresponding to the maximum ethylene selectivity value to the carbon-two hydrogenation load distribution model, thereby assigning the operating parameters corresponding to the acetylene hydrogenation conversion amount set value of each section of bed and the acetylene volume content set value of each section of bed outlet.

In a second aspect, the present invention provides a control system for a carbon dioxide hydrogenation reactor, using the control method according to any one of the first aspects, comprising:

the device comprises a carbon dioxide hydrogenation load distribution model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluation module, a control module and an online correction module;

the output end of the soft measurement module is respectively and electrically connected with the input ends of an analysis evaluation module, an expert knowledge base module and a carbon dioxide hydrogenation load distribution model module, the expert knowledge base module is in communication connection with the carbon dioxide hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected with the input end of the gain scheduling module, the output end of the carbon dioxide hydrogenation load distribution model module is electrically connected with the input end of the control module, and the output end of the gain scheduling module is electrically connected with the input end of the control module;

after the analysis and operation data of the carbon dioxide hydrogenation reactor are subjected to classified statistical calculation through the soft measurement module and the analysis and evaluation module, the analysis and operation data are transmitted to the carbon dioxide hydrogenation load distribution model module for fitting calculation, so that an operation parameter set value is obtained;

the expert knowledge base optimizes the operation parameter set value by adopting an optimization mode and an operation rule set to obtain an optimized operation parameter set value;

the gain scheduling module and the control module control the carbon dioxide hydrogenation reactor based on the optimized operating parameter set value.

Optionally, the operation rule set includes a boundary definition for the manipulation parameter, a selected operation parameter adjustment order, a selected operation parameter adjustment frequency, and/or a selected operation parameter adjustment magnitude.

Optionally, the selecting the operating parameter includes:

the pressure of the inlet material, the flow rate of the inlet material, the volume content of hydrogen in the inlet material of each section of bed, the temperature of the inlet material of each section of bed, the volume content ratio of hydrogen and acetylene at the inlet of each section of bed and/or the temperature rise of the bed layer of each section of bed reactor.

Optionally, the carbon dioxide hydrogenation reactor does not need to be matched with a hydrogenation moderator, and the hydrogenation moderator comprises crude hydrogen and CO;

and/or

The process for refining ethylene and removing acetylene by hydrogenation is applied to the separation process of an ethylene cracking device, and the separation process comprises a sequential separation process, a front depropanization and rear hydrogenation process and a front deethanization and rear hydrogenation process.

Optionally, the inlet material of the carbon hydrogenation reactor comprises ethylene, ethane and acetylene, and further comprises at least one of hydrogen, methane, propylene and propane;

and/or

The carbon dioxide hydrogenation catalyst added by the carbon dioxide hydrogenation reactor comprises: at least one of Pd, Ni, Pt, Rh and Ru, the content is 0.01-0.5 wt%;

the cocatalyst comprises at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halide series, alkali metal series and alkaline earth metal series, and the content is 0.01-1.0 wt%;

the carrier comprises at least one of alumina, molecular sieve, silicon oxide, gallium oxide, titanium oxide and active carbon.

According to the invention, the operation parameter set value is obtained by fitting and calculating the real-time statistical data through the carbon dioxide hydrogenation load distribution model, the carbon dioxide hydrogenation reactor is controlled based on the operation parameter set value, the automatic control of the carbon dioxide hydrogenation reactor is realized, and the reactor control parameters are optimized, so that the energy and material consumption is reduced, and the full-life operation cycle of the catalyst is prolonged.

Drawings

Exemplary embodiments of the present invention will be described in more detail by referring to the accompanying drawings.

FIG. 1 shows a flow diagram of a method of controlling a carbo-hydrogenation reactor according to one embodiment of the invention;

FIG. 2 illustrates a functional block diagram of a control system for a carbo-hydrogenation reactor according to one embodiment of the present invention;

FIG. 3 shows a schematic diagram of a carbon two hydrogenation reactor process flow according to one embodiment of the present invention;

FIG. 4 is a graph showing a comparison of the change in operating parameters after the control method for a carbon dioxide hydrogenation reactor according to this example;

wherein:

1-first-stage bed reactor, 2-last-stage bed reactor and 3-ethylene rectifying tower.

Detailed Description

The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

The present invention will be further described with reference to the following examples, but the scope of the present invention is not limited to these examples.

The carbo-hydrogenation reactor in this example comprises a multi-stage bed reactor.

The first embodiment is as follows:

as shown in fig. 1, a method for controlling a carbon hydrogenation reactor includes:

step S101: acquiring operation data and operation data of a carbon dioxide hydrogenation reactor;

in a specific application scenario, operational data and operational data are obtained by various sensors mounted on the carbon dioxide hydrogenation reactor.

Step S102: performing classified statistics on the operation data and the operation data to obtain real-time statistical data;

step S103: fitting and calculating the real-time statistical data through a carbon dioxide hydrogenation load distribution model to obtain an operation parameter set value;

step S104: controlling the carbon dioxide hydrogenation reactor based on the operating parameter set value.

Optionally, the carbon dioxide hydrogenation load distribution model comprises a set value model of acetylene hydrogenation conversion amount and a set value model of outlet acetylene volume content;

the set value model of the acetylene hydrogenation conversion amount is as follows:

in the formula, Y_nThe preset value of the hydrogenation conversion amount of the acetylene in the nth section bed; f_n(X) is the nth stage bed hydrogenation distribution function, where N is 1, 2, … (N-1); x is the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor; n is the total number of segments of the carbon two hydrogenation reactor; a is_iIs a segment number influence factor, associated with the total number of segments N, where i ═ 1, 2, … (N-1);

the set value model of the volume content of the outlet acetylene is as follows:

in the formula, M_{n out}Is the set point for the volume content of acetylene at the N-th bed outlet, wherein N is 1, 2, … (N-1); y is_kIs the set value of the acetylene hydrogenation conversion amount of the k-th bed, wherein k is 1, 2, … n.

Optionally, the volume content set value of acetylene at the outlet of the last bed is M_{end out}，M_{end out}To specify the constant Ω, Ω is taken to be in the range of 0<Ω<1ppm。

Optionally, the value range of the total number N of the carbon dioxide hydrogenation reactor is as follows: 1< N < 6;

the value range of the volume content X of acetylene in the total inlet material of the carbon hydrogenation reactor is as follows: x is more than or equal to 0.3 percent and less than or equal to 5.5 percent.

F_n(x) Independent of the total number of the reactor sections and the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor.

Optionally, after the step of obtaining the set value of the operation parameter by performing fitting calculation on the real-time statistical data through the carbon dioxide hydrogenation load distribution model module, the method further includes:

optimizing the operating parameter set point, the optimizing the operating parameter set point comprising:

establishing a functional relation for the acetylene hydrogenation conversion amount of each section of bed and the selected operation parameters through the carbon dioxide hydrogenation load distribution model, wherein the functional relation is as follows:

Y＝G(R，T,M_in)+ΔE(Fl,P) (3),

in the formula, Y is the acetylene conversion amount of each reactor section, R is the volume content ratio of hydrogen to acetylene at the inlet of each reactor section, T is the material temperature at the inlet of each reactor section, and M is_inThe volume content of acetylene at the inlet of each reactor section; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbo-hydrogenation reactor, and G is a control function of the hydrogenation activity of each section of reactor; and the delta E is a disturbance compensation function of the hydrogenation activity of each reactor section.

The carbon dioxide hydrogenation load distribution model expression 3 shows that the acetylene conversion amount change of each reactor section is influenced by multi-factor variables such as the volume content of acetylene at the inlet of each reactor section, the temperature of materials at the inlet of the reactor, the volume content ratio of inlet hydrogen to acetylene, the flow rate and pressure of the materials at the inlet of the reactor and the like. Wherein the reactor inlet feed flow and pressure are affected by upstream unit operation and cannot be adjusted for operation in the carbon-two hydrogenation unit. In an actual production process, the inlet material flow and pressure are typically corrected as compensation variables to a function. And establishing a functional relation between the acetylene conversion amount of each section of reactor and the volume content of acetylene at the inlet of each section of reactor based on the carbon dioxide hydrogenation reaction characteristics and the design optimization of the reactor in expression 1 and expression 2 of the carbon dioxide hydrogenation load distribution model. Thus, a bivariate functional relationship of Y to R and T can be formed.

Optionally, the optimizing the operation parameter setting value further includes:

establishing a function relation between the material temperature at the inlet of each section of the bed and the set value of the hydrogen alkyne ratio, wherein the function relation is as follows:

R_n＝G′(T_n)+ΔE(Fl，P) (4)，

R_end＝G′(T_end)+ΔE(Fl，P) (5)，

R_nis the volume content ratio set value of the hydrogen and the acetylene at the inlet of the nth section of the bed, T_nIs the material temperature set value at the inlet of the nth section of bed; wherein N is 1, 2, … (N-1); r_end，T_endThe volume content ratio of the hydrogen and the acetylene at the inlet of the last stage bed and the inlet material temperature and inlet material temperature set values are respectively, and G' is a temperature control function of the hydrogenation activity of each stage of reactor.

Calculating the set value Y of the nth section of bed according to the real-time device data through the expression 1 and the expression 2 of the carbon two hydrogenation load distribution model_n、M_nOr/and end bed Y_end、M_endAnd these set values Y_n、M_nOr/and Y_end、M_endAnd bringing the constant value coefficient into an expression 3, and establishing a functional relation between the inlet material temperature of the nth section bed or/last section bed and the set value of the hydrogen acetylene ratio, wherein the functional relation is specifically shown as an expression 4 and an expression 5.

Optionally, the optimizing the operation parameter setting value further includes:

and establishing a functional relationship between the acetylene selectivity of each section of the bed and the selected operation parameters, wherein the functional relationship is as follows:

S＝Q(R，T，M_in，M_out)+ΔR(Fl，P) (6)，

wherein S is the ethylene selectivity of each section of bed, R is the volume content ratio of hydrogen to acetylene at the inlet of each section, T is the material temperature at the inlet of each section of bed, and M is_inInlet B of each section of bedVolume content of alkyne, M_outThe volume content of acetylene at the outlet of each section of bed; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbo-hydrogenation reactor, and Q is a selective control function of each section of the reactor; Δ R disturbance compensation function for each stage reactor selectivity.

Optionally, the optimizing the operation parameter setting value further includes:

establishing a functional relation between the set value of the temperature of the material at the inlet of each section of the bed and the selectivity of the ethylene, wherein the functional relation is as follows:

S_n＝Q'(T_n)+ΔR(Fl,P) (7),

S_end＝Q'(T_end)+ΔR(Fl，P) (8),

in the formula, S_n、S_endEthylene selectivity, T, for the n-th and last-stage beds, respectively_n、T_endRespectively setting the inlet material temperature of the nth section bed and the inlet material temperature of the last section bed; where N is 1, 2, … (N-1), and Q' is the temperature control function of the selectivity of each bed.

Optionally, the optimizing the operation parameter setting value further includes:

acquiring inlet temperature set values corresponding to the maximum ethylene selectivity values obtained by establishing a functional relation between the inlet material temperature set values of all sections of beds and the ethylene selectivity;

obtaining a hydrogen and acetylene volume content ratio set value obtained by establishing a functional relation between the inlet material temperature of each section of bed and the hydrogen-acetylene ratio set value;

and returning the inlet temperature set value and the hydrogen-acetylene volume content ratio set value corresponding to the maximum ethylene selectivity value to the carbon-two hydrogenation load distribution model, thereby assigning the operating parameters corresponding to the acetylene hydrogenation conversion amount set value of each section of bed and the acetylene volume content set value of each section of bed outlet.

Namely, the nth section of bed S is obtained by calculating the expression 7 and the expression 8_nAnd/or end bed S_endAt maximum, the corresponding inlet temperature set value T_{n Smax}And T_{end Smax}And pass through the watchCalculating a hydrogen alkyne ratio set value R by an expression 4 and an expression 5_{n Smax}And R_{end Smax}Returning to the carbon dioxide hydrogenation load distribution model module as the nth section bed set value Y_n、M_nOr/and end bed Y_end、M_endAnd assigning corresponding operating parameters.

The selected operating parameters of the carbon dioxide hydrogenation reactor comprise inlet material pressure, inlet material flow, volume content of hydrogen in the inlet material of each section of bed, inlet material temperature of each section of bed, volume content ratio of hydrogen to acetylene at the inlet of each section of bed and bed layer temperature rise of each section of bed reactor, and preferably the inlet material temperature of each section of bed and the volume content ratio of hydrogen to acetylene at the inlet of each section of bed.

Example two:

a control system for a carbo-hydrogenation reactor, using an embodiment of a control method, comprising:

the device comprises a carbon dioxide hydrogenation load distribution model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluation module, a control module and an online correction module;

the output end of the soft measurement module is respectively and electrically connected with the input ends of an analysis evaluation module, an expert knowledge base module and a carbon dioxide hydrogenation load distribution model module, the expert knowledge base module is in communication connection with the carbon dioxide hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected with the input end of the gain scheduling module, the output end of the carbon dioxide hydrogenation load distribution model module is electrically connected with the input end of the control module, and the output end of the gain scheduling module is electrically connected with the input end of the control module;

after the analysis and operation data of the carbon dioxide hydrogenation reactor are subjected to classified statistical calculation through the soft measurement module and the analysis and evaluation module, the analysis and operation data are transmitted to the carbon dioxide hydrogenation load distribution model module for fitting calculation, so that an operation parameter set value is obtained;

the expert knowledge base optimizes the set values of the operation parameters by adopting an optimization mode and an operation rule set to obtain the optimized set values of the operation parameters;

the gain scheduling module and the control module control the carbon dioxide hydrogenation reactor based on the optimized operating parameter set value.

Optionally, the operation rule set includes a boundary definition for the manipulation parameter, a selected operation parameter adjustment order, a selected operation parameter adjustment frequency, and/or a selected operation parameter adjustment magnitude.

Optionally, the selecting the operating parameter includes:

the pressure of the inlet material, the flow rate of the inlet material, the volume content of hydrogen in the inlet material of each section of bed, the temperature of the inlet material of each section of bed, the volume content ratio of hydrogen and acetylene at the inlet of each section of bed and/or the temperature rise of the bed layer of each section of bed reactor.

Optionally, the carbon dioxide hydrogenation reactor does not need to be matched with a hydrogenation moderator, and the hydrogenation moderator comprises crude hydrogen and CO;

and/or

The process for refining ethylene and removing acetylene by hydrogenation is applied to the separation process of an ethylene cracking device, and the separation process comprises a sequential separation process, a front depropanization and rear hydrogenation process and a front deethanization and rear hydrogenation process.

Optionally, the inlet material of the carbon hydrogenation reactor comprises ethylene, ethane and acetylene, and also comprises at least one of hydrogen, methane, propylene and propane;

and/or

The carbon dioxide hydrogenation catalyst added by the carbon dioxide hydrogenation reactor comprises: at least one of Pd, Ni, Pt, Rh and Ru, the content is 0.01-0.5 wt%;

the cocatalyst comprises at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halide series, alkali metal series and alkaline earth metal series, and the content is 0.01-1.0 wt%;

the carrier comprises at least one of alumina, molecular sieve, silicon oxide, gallium oxide, titanium oxide and active carbon.

As shown in fig. 2, the control system is located in a server connected to the distributed control system of the carbon hydrogenation reactor, i.e. the DCS system. The control module is positioned at the bottom layer of the modularized automatic control system of the carbon dioxide hydrogenation reactor, is connected with the DCS through the OPC Server and directly issues an optimized control signal and a command to the DCS; the gain scheduling module is also positioned at the bottom layer of the system and provides the gain and the frequency of each adjusting parameter for the control module; the soft measurement module and the carbon dioxide hydrogenation load distribution model module are positioned in the middle layer of the modularized automatic control system of the carbon dioxide hydrogenation reactor, wherein the carbon dioxide hydrogenation load distribution model module provides a main optimized control parameter set value for the bottom layer control module through model calculation solution; the expert knowledge base module and the analysis and evaluation module are both positioned at the top layer of the modularized automatic control system of the carbon dioxide hydrogenation reactor, the expert knowledge base module optimizes the operation parameter set value calculated by the carbon dioxide hydrogenation load distribution model module by adopting an optimization mode and an operation rule set in combination with the operation data trend provided by the soft measurement and analysis and evaluation module, then returns the operation parameter set value to the carbon dioxide hydrogenation load distribution model module for data correction, and instructs the gain scheduling module to implement automatic control.

As shown in FIG. 3, the carbohydrogenation reactor comprises a first-stage bed reactor, a last-stage bed reactor and an ethylene rectifying tower. Wherein other section bed reactors can be arranged between the first section bed reactor and the last section bed reactor according to the requirement.

In this embodiment, the soft measurement module monitors the composition and content of the materials before and after the carbon dioxide hydrogenation reactor, the composition of the top of the deethanizer, and the composition and content of the materials at the top and bottom of the ethylene rectification tower in real time, and filters the real-time data and inputs the filtered data into the soft measurement model to measure the values and trends of the composition and content of each material.

The analysis and evaluation module monitors the online operation time of the catalyst, the material flow, the reaction temperature, the pressure, the content changes of hydrogen, carbon two, carbon three, water and the like before and after the reaction in real time, and inputs the real-time data into the analysis and evaluation model to measure the performance of the catalyst, such as the operation life, the activity, the ethylene selectivity, the acetylene conversion rate and the like.

The ethylene selectivity calculation is as follows:

the reactivity was as follows:

the acetylene conversion calculation formula is as follows:

the optimized modeling method for the operation of the carbon dioxide hydrogenation reactor aims at obtaining the optimal ethylene selectivity, the operation parameter set value is obtained by fitting and calculating real-time data through the carbon dioxide hydrogenation load distribution model module, the operation parameter set value is calculated and optimized through the expert knowledge base by adopting an optimization mode and an operation rule set, the control module and the gain scheduling module are commanded to implement automatic control, and the analysis and operation data of the carbon dioxide hydrogenation reactor enter the carbon dioxide hydrogenation load distribution model module and the expert knowledge base module for fitting and calculation after being classified and counted and calculated through the soft measurement module and the analysis and evaluation module.

More specifically, the carbon dioxide hydrogenation load distribution model is established based on the simulation of the carbon dioxide hydrogenation reaction process and the optimization of the reactor design, and the expression is as follows:

in the formula, Y_nIs a set value of the acetylene hydrogenation conversion amount of the nth bed, F_n(X) is the nth stage bed hydrogenation distribution function; wherein N is 1, 2, … (N-1); x is the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor; n is the total number of segments of the carbon two hydrogenation reactor; a is_iThe factor is the influence factor of the number of segments and is influenced by the total number of segments N, wherein i is 1, 2, … (N-1).

In the formula, M_{n out}Is the set point for the volume content of acetylene at the N-th bed outlet, wherein N is 1, 2, … (N-1); y is_kIs the set point for the hydroconversion of acetylene to the kth bed, where k is 1, 2, … n.

Volume content set value M of acetylene at outlet of tail bed of carbon hydrogenation reactor_{end out}To specify the constant Ω, the value range of Ω is 0<Ω<1ppm。

N is the total bed number of stages of multistage bed carbo-hydrogenator in the carbo-hydrogenator load distribution model, and its value range is: 1<N<An integer of 6; x is the volume content of acetylene at the total inlet of the reactor, and the value range of X is more than or equal to 0.3% and less than or equal to 5.5%; f_n(X) is the nth stage bed hydrogenation distribution function, which is independent of the total number of stages in the reactor and is related only to the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor, wherein N is 1, 2, … (N-1); y is_nAnd calculating the set value of the N-th section bed acetylene hydrogenation conversion amount obtained by the model calculation according to a multi-section bed acetylene hydrogenation load distribution model, wherein N is 1, 2, … (N-1).

The carbon dioxide hydrogenation load distribution model establishes a functional relationship between the acetylene hydrogenation conversion amount and main operation parameters of each section of reactor, and the expression is as follows:

Y＝G(R，T，M_in)+ΔE(Fl，P)，

in the formula, Y is the acetylene conversion amount of each reactor section, R is the volume content ratio of hydrogen to acetylene at the inlet of each reactor section, T is the material temperature at the inlet of each reactor section, and M is_inThe volume content of acetylene at the inlet of each reactor section; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbon hydrogenation reactor, Fl and P are disturbance variables and are influenced by the upstream incoming material of the carbon hydrogenation reactor, and G is a control function of the hydrogenation activity of each section of reactor; and the delta E is a disturbance compensation function of the hydrogenation activity of each reactor section.

The carbon dioxide hydrogenation load distribution model expression shows that the acetylene conversion amount change of each reactor is influenced by the volume content of acetylene at the inlet of each reactor, the temperature of the material at the inlet of the reactor, the volume content ratio of the hydrogen at the inlet to the acetylene, the flow rate and the pressure of the material at the inlet of the reactor and other multi-factor variables. Wherein the reactor inlet feed flow and pressure are affected by upstream unit operation and cannot be adjusted for operation in the carbon-two hydrogenation unit. In an actual production process, the inlet material flow and pressure are typically corrected as compensation variables to the function. And establishing a functional relation between the acetylene conversion amount of each section of reactor and the volume content of acetylene at the inlet of each section of reactor based on the carbon hydrogenation reaction characteristics and the optimization of reactor design in an expression of a carbon hydrogenation load distribution model. Thus, a bivariate functional relationship of Y to R and T can be formed.

Calculating the set value Y of the nth section of bed according to the data of a real-time device through the expression 1 and the expression 2 of the carbon dioxide hydrogenation load distribution model_n、M_nOr/and end bed Y_end、M_endAnd these set values Y_n、M_nOr/and Y_end、M_endBringing the constant value coefficient into an expression 3, and establishing a functional relation between the inlet material temperature of the nth section bed or/last section bed and the set value of the hydrogen acetylene ratio, wherein the expression is as follows:

R_n＝G'(T_n)+ΔE(Fl,P)，

R_end＝G'(T_end)+ΔE(Fl，P)，

in the formula, R_nIs the volume content ratio set value of the hydrogen and the acetylene at the inlet of the nth section of the bed, T_nIs the material temperature set value at the inlet of the nth section of bed; wherein N is 1, 2, … (N-1); r_end，T_endThe volume content ratio of the hydrogen and the acetylene at the inlet of the last stage bed and the inlet material temperature and inlet material temperature set values are respectively, and G' is a temperature control function of the hydrogenation activity of each stage of reactor.

The expert optimization module comprises an optimization mode and an operation rule set, and guides the carbon dioxide hydrogenation load distribution model module and the gain scheduling module after data optimization fitting. The expert optimization module adopts an optimization mode to establish a functional relation between the selectivity of acetylene and main operation parameters of each section of bed, and the expression is as follows:

S＝Q(R，T，M_in，M_out)+ΔR(Fl，P)，

wherein S is the selectivity of ethylene in each reactor section, and R is the hydrogen at the inlet of each reactor sectionVolume content ratio of acetylene, T is the inlet material temperature of each reactor section, M_inVolume content of acetylene at the inlet of each reactor section, M_outThe volume content of acetylene at the outlet of each reactor section; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are influenced by the upstream incoming material of the carbo-hydrogenation reactor, and Q is a selective control function of each section of the reactor; Δ R disturbance compensation function for each stage reactor selectivity.

In the expert optimization module optimization mode, the expressions 1 and 2 of the carbon dioxide hydrogenation load distribution model calculate the set value Y of the nth section of bed_n、M_nOr/and end bed set point Y_end、M_endSubstituting the given coefficient into expressions 4, 5 and 6 to obtain the function relationship between the inlet material temperature set value of the nth stage bed or/and the last stage bed and the selectivity of ethylene, wherein the expressions are as follows

S_n＝Q′(T_n)+ΔR(Fl，P)，

S_end＝Q′(T_end)+ΔR(Fl，P)，

In the formula, S_n、S_endEthylene selectivity for the n-th and last-stage beds, respectively, T_n、T_endRespectively setting the material temperature at the inlet of the nth section bed and the material temperature at the inlet of the last section bed; where N is 1, 2, … (N-1), and Q' is the temperature control function of the selectivity of each bed. .

Calculating by expression 7 and expression 8) in the expert optimization module to obtain the nth section of bed S_nAnd/or end bed S_endAt maximum, the corresponding inlet temperature set value T_{n Smax}And T_{end Smax}And calculating a hydrogen alkyne ratio set value R by an expression 4 and an expression 5)_{n Smax}And R_{end Smax}Returning to the carbon dioxide hydrogenation load distribution model module as the nth section bed set value Y_n、M_nOr/and end bed Y_end、M_endAnd assigning corresponding operating parameters.

The operation rule set in the expert optimization module comprises boundary limits of operation parameters such as inlet material temperature, inlet acetylene and hydrogen volume content, material flow, pressure and the like of each section; adjusting sequence, frequency and amplitude of main operation parameters such as hydrogen alkyne ratio, inlet material temperature and the like; the poisonous substances such as CO, water, sulfur, methanol and the like are introduced into the adjustment compensation coefficient of the main operation parameters of the reactor; the ethylene selectivity decays with time in the catalyst operation period, etc.

And the real-time operation data is processed by the soft measurement module and the analysis and evaluation module and then enters the expert knowledge base module and the carbon dioxide hydrogenation load distribution model module.

The main operating parameters of the carbon-two hydrogenation reactor in the optimized modeling method for the operation of the carbon-two hydrogenation reactor comprise inlet material pressure, inlet material flow, hydrogen volume content in the inlet material of each section of bed, inlet material temperature of each section of bed, volume content ratio of hydrogen and acetylene at the inlet of each section of bed, bed layer temperature rise of each section of bed reactor, preferably inlet material temperature of each section of bed and volume content ratio of hydrogen and acetylene at the inlet of each section of bed.

The operation optimization modeling method of the carbon dioxide hydrogenation reactor does not need to add hydrogenation moderators such as crude hydrogen, CO and the like.

The operation optimization modeling method of the carbon dioxide hydrogenation reactor is applied to a process for refining ethylene and removing acetylene by hydrogenation in a separation process of an ethylene cracking device, wherein the separation process comprises a sequential separation process, a front depropanization and rear hydrogenation process, a front deethanization and rear hydrogenation process and the like.

The inlet material of the carbon hydrogenation reactor at least comprises ethylene, ethane and acetylene, and also comprises at least one of hydrogen, methane, propylene and propane.

The concentration refers to the volume percentage content, and the flow refers to the mass flow.

The main active component of the carbon dioxide hydrogenation catalyst is at least one of Pd, Ni, Pt, Rh and Ru, and the content is 0.01-0.5 wt%; the cocatalyst comprises at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halogen series, alkali metal series, alkaline earth metal series, etc., and the content is 0.01-1.0 wt%; the carrier is at least one of alumina, molecular sieve, silicon oxide, gallium oxide, titanium oxide, active carbon and the like.

The control system uses C # language to realize the design of iterative learning control software. The software comprises a data acquisition part, a data storage and learning control algorithm part. And the control system software uses OPC technology to communicate with the DCS of the carbon dioxide hydrogenation device, reads real-time process variable data and realizes the optimized control of the carbon dioxide hydrogenation reactor through writing operation. The data storage section is capable of storing history data.

By utilizing the principle of the carbon dioxide hydrogenation reaction and the design optimization knowledge framework of the reactor, and combining the evaluation test result of the catalyst on the industrial side line length period, a carbon dioxide hydrogenation load distribution model is established and is assisted by an expert knowledge base optimization mode, and the automatic control of the carbon dioxide hydrogenation reactor is realized under the condition of actual production fluctuation. The optimal ethylene yield is taken as a target, the operation parameters of the reactor are comprehensively optimized, the energy and material consumption is reduced, and the full-life operation period of the catalyst is prolonged.

Example three:

and establishing a modularized automatic control system of the carbon hydrogenation reactor. Constructing a carbon dioxide hydrogenation load distribution model; and establishing an expert knowledge base, and designing a rule for switching the local controller model by combining deep knowledge of the catalyst with gain scheduling. The control system adopts C # language to compile expert control software and test the reliability of the software.

The method of the invention is applied to a carbon dioxide hydrogenation reaction control unit of the olefin plant: the modularized automatic control system of the carbon dioxide hydrogenation reactor is connected with a device DCS through an OPC Server, each process condition is optimized and adjusted, and an adjustment target is provided for the DCS in real time, so that the automatic control of the carbon dioxide hydrogenation reactor is realized.

FIG. 4 shows the variation of the technical parameters of the hydrogen distribution amount of the hydrogenation reaction vessel after the automatic control system is put into operation.

The commissioning of the carbohydrogenator control system significantly improves ethylene selectivity. Under the conditions of the same reactor, catalyst, feed composition and the like, an automatic control system is introduced, so that the average ethylene selectivity can be improved from 42.3 percent before the ethylene is put into use to 57.6 percent after the ethylene is put into use, the selectivity is improved by 15.3 percent, and the synergistic effect is very obvious.

Comparative example:

an olefin plant producing 80 ten thousand tons of ethylene in a year has 15 cracking furnaces, and can process various cracking raw materials from ethane to hydrogenated tail oil and the like. The separation process of the plant adopts a sequential separation flow, a carbon dioxide hydrogenation reactor is positioned between a cold zone deethanizer and an ethylene rectifying tower, and carbon dioxide fraction obtained from the top of the deethanizer exchanges heat to a required temperature through a cooler (or a preheater), enters the hydrogenation reactor through a raw material dryer, is mixed with hydrogen in a pipeline, and enters a catalytic bed of the reactor for selective hydrogenation reaction. The carbon dioxide hydrogenation process of the plant is designed into a double-section bed, a heat exchanger is arranged between sections, two sections are provided, one is provided, and the process flow is shown in figure 2. The carbon dioxide hydrogenation reactor of the plant is operated manually and manually for normal operation. The inlet acetylene of the carbo-hydrogenation reactor is 0.9-1.0 mol%, and the outlet acetylene is required to be less than 1 ppm. The catalyst is BC-H-20B catalyst developed by the Beijing chemical research institute of the Chinese petrochemical industry.

The comparison results show that: compared with the manual control of the original factory, the method and the system provided by the invention can obviously improve the ethylene yield and reduce the hydrogen consumption. .

Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

Claims (14)

1. A method for controlling a carbohydrogenator, comprising:

acquiring operation data and operation data of a carbon dioxide hydrogenation reactor;

performing classified statistics on the operation data and the operation data to obtain real-time statistical data;

fitting and calculating the real-time statistical data through a carbon dioxide hydrogenation load distribution model to obtain an operation parameter set value;

controlling the carbon dioxide hydrogenation reactor based on the operating parameter set value.

2. The control method of a carbon dioxide hydrogenation reactor as claimed in claim 1, wherein the carbon dioxide hydrogenation load distribution model comprises a set value model of acetylene hydrogenation conversion amount and a set value model of outlet acetylene volume content;

the set value model of the acetylene hydrogenation conversion amount is as follows:

in the formula, Y_nThe preset value of the hydrogenation conversion amount of the acetylene in the nth section bed; f_n(X) is the nth stage bed hydro-distribution function, where N is 1, 2, … (N-1); x is the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor; n is the total number of the carbon hydrogenation reactor; a is_iIs a segment number influence factor, associated with a total number of segments N, where i ═ 1, 2, … (N-1);

the set value model of the volume content of the outlet acetylene is as follows:

in the formula, M_{n out}Is the set point for the volume content of acetylene at the N-th bed outlet, wherein N is 1, 2, … (N-1); y is_kIs the set value of the acetylene hydrogenation conversion amount of the k-th bed, wherein k is 1, 2, … n.

3. According to the rightThe method for controlling a hydrogenation reactor for carbon dioxide as set forth in claim 2, wherein the set value of the volume content of acetylene at the outlet of the last-stage bed is M_{end out}，M_{end out}The value range of omega is more than 0 and less than 1ppm for a specified constant omega.

4. The method for controlling a carbo-hydrogenation reactor as recited in claim 2,

the value range of the total number N of the carbon dioxide hydrogenation reactor is as follows: n is more than 1 and less than 6;

the value range of the volume content X of acetylene in the total inlet material of the carbon hydrogenation reactor is as follows: x is more than or equal to 0.3 percent and less than or equal to 5.5 percent.

F_n(X) is independent of the total number of the reactor sections and is related to the volume content of acetylene in the total inlet material of the carbon hydrogenation reactor.

5. The method for controlling a carbon dioxide hydrogenation reactor according to claim 4, wherein the step of obtaining the set value of the operation parameter by the carbon dioxide hydrogenation load distribution model module through fitting calculation of the real-time statistical data further comprises:

optimizing the operating parameter set point, the optimizing the operating parameter set point comprising:

establishing a functional relation for the acetylene hydrogenation conversion amount of each section of bed and the selected operation parameters through the carbon dioxide hydrogenation load distribution model, wherein the functional relation is as follows:

Y＝G(R，T，M_in)+ΔE(Fl，P)，

wherein Y is the conversion amount of acetylene in each reactor, R is the volume content ratio of hydrogen to acetylene at the inlet of each reactor, T is the material temperature at the inlet of each reactor, and M is_inThe volume content of acetylene at the inlet of each reactor section; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbon hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbon hydrogenation reactor, and G is a control function of the hydrogenation activity of each section of reactor; and the delta E is a disturbance compensation function of the hydrogenation activity of each reactor section.

6. The method of controlling a carbo-hydrogenation reactor as recited in claim 5, wherein the optimizing the operating parameter set point further comprises:

establishing a function relation between the material temperature at the inlet of each section of the bed and the set value of the hydrogen alkyne ratio, wherein the function relation is as follows:

R_n＝G′(T_n)+ΔE(Fl，P)，

R_end＝G′(T_end)+ΔE(Fl，P)，

R_nis the volume content ratio set value of the hydrogen and the acetylene at the inlet of the nth section of the bed, T_nIs the material temperature set value at the inlet of the nth section of bed; wherein N is 1, 2, … (N-1); r_end，T_endThe volume content ratio of the hydrogen and the acetylene at the inlet of the last stage bed and the inlet material temperature and inlet material temperature set values are respectively, and G' is a temperature control function of the hydrogenation activity of each stage of reactor.

7. The method for controlling a carbo-hydrogenation reactor as recited in claim 6, wherein the optimizing the operating parameter set point further comprises:

and establishing a functional relationship between the acetylene selectivity of each section of the bed and the selected operation parameters, wherein the functional relationship is as follows:

S＝Q(R，T，M_in，M_out)+ΔR(Fl，P)，

wherein S is the ethylene selectivity of each section of bed, R is the volume content ratio of hydrogen to acetylene at the inlet of each section, T is the material temperature at the inlet of each section of bed, and M is_inVolume content of acetylene at the entrance of each bed, M_outThe volume content of acetylene at the outlet of each section of bed; fl and P are respectively the flow rate and pressure of the material at the inlet of the carbo-hydrogenation reactor, Fl and P are disturbance variables and are related to the upstream incoming material of the carbo-hydrogenation reactor, and Q is a selective control function of each section of the reactor; Δ R disturbance compensation function for each stage reactor selectivity.

8. The method for controlling a carbo-hydrogenation reactor as recited in claim 7, wherein the optimizing the operating parameter set point further comprises:

establishing a functional relation between the set value of the temperature of the material at the inlet of each section of the bed and the selectivity of the ethylene, wherein the functional relation is as follows:

S_n＝Q′(T_n)+ΔR(Fl，P)，

S_end＝Q′(T_end)+ΔR(Fl，P)，

in the formula, S_n、S_endEthylene selectivity, T, for the n-th and last-stage beds, respectively_n、T_endRespectively setting the material temperature at the inlet of the nth section bed and the material temperature at the inlet of the last section bed; where N is 1, 2, … (N-1), and Q' is the temperature control function of each section of bed selectivity.

9. The method for controlling a carbo-hydrogenation reactor as recited in claim 8, wherein the optimizing the operating parameter set point further comprises:

acquiring inlet temperature set values corresponding to the maximum ethylene selectivity values obtained by establishing a functional relation between the inlet material temperature set values of all sections of beds and the ethylene selectivity;

obtaining a hydrogen and acetylene volume content ratio set value obtained by establishing a functional relation between the inlet material temperature of each section of bed and the hydrogen-acetylene ratio set value;

and returning the inlet temperature set value and the hydrogen-acetylene volume content ratio set value corresponding to the maximum ethylene selectivity value to the carbon-two hydrogenation load distribution model, thereby assigning the operating parameters corresponding to the acetylene hydrogenation conversion amount set value of each section of bed and the acetylene volume content set value of each section of bed outlet.

10. A control system for a carbohydrogenator, using the control method according to any one of claims 1 to 9, characterized by comprising:

the device comprises a carbon dioxide hydrogenation load distribution model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluation module, a control module and an online correction module;

the output end of the soft measurement module is respectively and electrically connected with the input ends of an analysis evaluation module, an expert knowledge base module and a carbon dioxide hydrogenation load distribution model module, the expert knowledge base module is in communication connection with the carbon dioxide hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected with the input end of the gain scheduling module, the output end of the carbon dioxide hydrogenation load distribution model module is electrically connected with the input end of the control module, and the output end of the gain scheduling module is electrically connected with the input end of the control module;

after the analysis and operation data of the carbon dioxide hydrogenation reactor are subjected to classified statistical calculation through the soft measurement module and the analysis and evaluation module, the analysis and operation data are transmitted to the carbon dioxide hydrogenation load distribution model module for fitting calculation, so that an operation parameter set value is obtained;

the expert knowledge base optimizes the set values of the operation parameters by adopting an optimization mode and an operation rule set to obtain the optimized set values of the operation parameters;

the gain scheduling module and the control module control the carbon dioxide hydrogenation reactor based on the optimized operating parameter set value.

11. The control system for a carbon dioxide hydrogenation reactor as set forth in claim 10 wherein the set of operating rules comprises boundary definitions for handling parameters, selected operating parameter adjustment sequences, selected operating parameter adjustment frequencies, and/or selected operating parameter adjustment magnitudes.

12. The control system for a carbon dioxide hydrogenation reactor as set forth in claim 11 wherein the selected operating parameters comprise:

the pressure of the inlet material, the flow rate of the inlet material, the volume content of hydrogen in the inlet material of each section of bed, the temperature of the inlet material of each section of bed, the volume content ratio of hydrogen and acetylene at the inlet of each section of bed and/or the temperature rise of the bed layer of each section of bed reactor.

13. The control system for a carbo-hydrogenator reactor as set forth in claim 10 wherein the carbo-hydrogenator reactor is not formulated with a hydrogenation moderator comprising, crude hydrogen and CO;

and/or

The process for refining ethylene and removing acetylene by hydrogenation is applied to the separation process of an ethylene cracking device, and the separation process comprises a sequential separation process, a front depropanization and rear hydrogenation process and a front deethanization and rear hydrogenation process.

14. The control system for a carbo-hydrogenation reactor as defined in claim 10 wherein the carbo-hydrogenation reactor inlet feed comprises ethylene, ethane and acetylene,

at least one of hydrogen, methane, propylene and propane is also included;

and/or

The carbon dioxide hydrogenation catalyst added by the carbon dioxide hydrogenation reactor comprises: at least one of Pd, Ni, Pt, Rh and Ru, the content is 0.01-0.5 wt%;

the cocatalyst comprises at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halide series, alkali metal series and alkaline earth metal series, and the content is 0.01-1.0 wt%;

the carrier comprises at least one of alumina, molecular sieve, silicon oxide, gallium oxide, titanium oxide and active carbon.

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