Control method and system for carbon dihydrogenation reactor

Abstract

The present invention discloses a control method and system for a carbon two hydrogenation reactor. The automatic control method of the carbon two hydrogenation reactor includes: obtaining the operation data and operating data of the carbon two hydrogenation reactor; classifying and counting the operation data and operating data to obtain real-time statistical data; fitting and calculating the real-time statistical data through the carbon two hydrogenation load distribution model to obtain the operating parameter setting value; and controlling the carbon two hydrogenation reactor based on the operating parameter setting value. The method and system disclosed in the present invention fit the real-time statistical data through the carbon two hydrogenation load distribution model to obtain the operating parameter setting value, and control the carbon two hydrogenation reactor based on the operating parameter setting value, so as to realize automatic control of the carbon two hydrogenation reactor, optimize the reactor control parameters, and achieve the purpose of reducing energy and material consumption while extending the full life cycle of the catalyst.

Description

Technical Field

[0001] The present invention belongs to the field of petrochemical industry, and more specifically, relates to a control method and system for a carbon dihydrogenation reactor. Background Art

[0002] Ethylene technology is the leading technology in petrochemical industry, and the level of ethylene technology is regarded as an important indicator of the development level of a country's petrochemical industry. The trienes (ethylene, propylene, butadiene) produced by ethylene cracking units are the basic raw materials of the petrochemical industry, and the level of triene production is the main indicator of the development level of a country's petrochemical industry.

[0003] After the liquid hydrocarbon raw materials such as naphtha in the ethylene cracking unit are steam cracked and separated, the carbon two fraction contains ethylene, ethane, and a small amount of acetylene, and the acetylene content is about 0.5% to 3% (volume). In the downstream polymerization reaction, the presence of acetylene will poison the polyolefin promoter. In order to obtain polymerization-grade ethylene, acetylene must be removed. The widely used method for removing acetylene is catalytic selective hydrogenation. The removal of acetylene in the carbon two fraction mainly adopts two processes: solvent absorption method and catalytic selective hydrogenation method.

[0004] Since the catalytic selective hydrogenation process is simple, has low energy consumption, no environmental pollution, can increase the yield of the target product, and with the continuous improvement of the performance of new high-efficiency hydrogenation catalysts, the application of hydrogenation is becoming more and more common, becoming the most commonly used economical and simple method. According to different process routes, it can be divided into two types: pre-hydrogenation and post-hydrogenation. The post-hydrogenation process is suitable for separation processes mainly including sequential separation, pre-depropanization and post-hydrogenation, and pre-de-ethanization and post-hydrogenation. They are the process of adding an appropriate amount of hydrogen to the remaining pure carbon two fractions after the light fractions such as hydrogen, CO, and methane and heavy fractions such as carbon three or carbon four or above contained in the cracked gas for hydrogenation.

[0005] The C2 hydrogenation reactor unit is an important part of ethylene product refining. It converts acetylene in the C2 fraction into ethylene by selective hydrogenation under the action of a catalyst. If acetylene is over-hydrogenated to produce ethane, ethylene loss will occur; or acetylene undergoes polymerization to produce oligomers or even polymers, which will affect the reactor life cycle; or if the acetylene hydrogenation activity is poor, the volume content of acetylene at the reactor outlet cannot be controlled within the index requirements, making the product ethylene unqualified. These will have a direct impact on ethylene products and the downstream industrial chain. Therefore, the operation of the C2 hydrogenation reactor will play a vital role in both corporate benefits and national economy and people's livelihood.

[0006] The catalyst for carbon dihydrogenation generally uses palladium-based precious metals as the active component, and the production suppliers include Sinopec Catalyst Company, CLARIANT Company, PHILLIPS Company, etc. The reaction thermodynamic parameters, surface adsorption and desorption reaction rates, and process sensitivity of catalysts of different manufacturers are different, and targeted adjustments and optimizations are needed to ensure their best performance.

[0007] At present, the production control of the C2 hydrogenation reactor generally adopts manual control, and the technicians manually adjust and control the relevant parameters. Due to the lengthy cracking and separation process, complex technology, and limited personnel energy, it is impossible to monitor and adjust the C2 hydrogenation reactor in real time. When the C2 hydrogenation system has unstable conditions such as material composition, pressure, temperature, flow, and hydrogen fluctuations, it is very slow to restore stability by relying solely on the hydrogenation system itself. The superposition phenomenon caused by multiple fluctuations makes the system in a metastable state for a long time, which is easy to cause leakage of acetylene and ethylene loss at the reactor outlet, affecting the product ethylene yield and the separation effect of the distillation tower.

[0008] At present, most C2 hydrogenation reactors are operated by manual experience and manual adjustment. In order to ensure that the acetylene in the ethylene product is removed to a qualified level, it is easy to cause excessive hydrogenation in the single-stage or final-stage C2 hydrogenation reactor, making the volume content of acetylene in the final hydrogenation product tend to 0 ppm, resulting in a large loss of ethylene. This leads to the problem of low ethylene selectivity in the C2 hydrogenation reactor. Summary of the invention

[0009] In view of this, the present invention provides a control method and system for a carbon dihydrogenation reactor, which at least solves the problems of high energy and material consumption and short life cycle of the catalyst in the prior art.

[0010] In a first aspect, the present invention provides a method for controlling a carbon dihydrogenation reactor, comprising:

[0011] Obtaining the operation data and operating data of the C2 hydrogenation reactor;

[0012] Classify and count the running data and operation data to obtain real-time statistical data;

[0013] The operating parameter setting values ​​are obtained by fitting and calculating the real-time statistical data through the C2 hydrogenation load distribution model;

[0014] The carbon dihydrogenation reactor is controlled based on the operating parameter set values.

[0015] Optionally, the C2 hydrogenation load distribution model includes a set value model for acetylene hydrogenation conversion amount and a set value model for outlet acetylene volume content;

[0016] The set value model of the acetylene hydrogenation conversion amount is:

[0017]

[0018] In the formula, Y n is the set value of the acetylene hydrogenation conversion amount in the nth bed; F n (X) is the hydrogenation distribution function of the nth bed, where n = 1, 2,... (N - 1); X is the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor; N is the total number of beds in the C2 hydrogenation reactor; a i is the section number influence factor, associated with the total number of beds N, where i = 1, 2,... (N - 1);

[0019] The set value model of the outlet acetylene volume content is:

[0020]

[0021] In the formula, M n out is the set value of the outlet acetylene volume content in the nth bed, where n = 1, 2,... (N - 1); Y k is the set value of the acetylene hydrogenation conversion amount in the kth bed, where k = 1, 2,... n.

[0022] Optionally, the set value of the outlet acetylene volume content of the last bed is M end out , M end out is the specified constant Ω, and the value range of Ω is 0 < Ω < 1 ppm.

[0023] Optionally, the value range of the total number of beds N of the C2 hydrogenation reactor is: an integer of 1 < N < 6;

[0024] The value range of the volume content X of acetylene in the total inlet material of the C2 hydrogenation reactor is: 0.3% ≤ X ≤ 5.5%.

[0025] F n (X) has nothing to do with the total number of beds of the reactor and is related to the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor.

[0026] Optionally, after the step of obtaining the set value of the operating parameter by fitting and calculating the real-time statistical data through the C2 hydrogenation load distribution model module, it further includes:

[0027] Optimizing the set value of the operating parameter, and the optimizing the set value of the operating parameter includes:

[0028] Establishing a functional relationship between the acetylene hydrogenation conversion amount of each bed and the selected operating parameter through the C2 hydrogenation load distribution model, and the functional relationship is as follows:

[0029] Y = G(R, T, M in ) + ΔE(Fl, P),

[0030] Where, Y is the acetylene conversion amount of each reactor, R is the volume ratio of hydrogen to acetylene at the inlet of each reactor, T is the material temperature at the inlet of each reactor, M in The volume content of acetylene at the inlet of each section of the reactor; Fl and P are the material flow rate and pressure at the inlet of the C2 hydrogenation reactor respectively. Fl and P are disturbance variables, which are related to the upstream incoming materials of the C2 hydrogenation reactor. G is the control function of the hydrogenation activity of each section of the reactor; ΔE is the disturbance compensation function of the hydrogenation activity of each section of the reactor.

[0031] Optionally, the optimizing the setting value of the operating parameter further includes:

[0032] A functional relationship is established between the material temperature at the inlet of each bed and the set value of the hydrogen-acetylene ratio, and the functional relationship is:

[0033] R n =G′(T n )+ΔE(Fl,P),

[0034] R end =G′(T end )+ΔE(Fl,P),

[0035] R n is the set value of the volume content ratio of hydrogen to acetylene at the inlet of the nth stage bed, T n is the set value of the material temperature at the inlet of the nth stage bed; where n = 1, 2, ... (N-1); R end， T end are the volume ratio of hydrogen to acetylene in the inlet of the last stage bed and the inlet material temperature, respectively; G′ is the temperature control function of the hydrogenation activity of each stage reactor.

[0036] Optionally, the optimizing the setting value of the operating parameter further includes:

[0037] The functional relationship between the acetylene selectivity of each bed and the selected operating parameters is established as follows:

[0038] S=Q(R,T,M in , M out )+ΔR(Fl,P),

[0039] Where S is the ethylene selectivity of each bed, R is the volume ratio of hydrogen to acetylene at the inlet of each bed, T is the material temperature at the inlet of each bed, M in Acetylene volume content at each bed inlet, M out The volume content of acetylene at the outlet of each bed; Fl and P are the material flow and pressure at the inlet of the C2 hydrogenation reactor respectively, Fl and P are disturbance variables, which are related to the upstream incoming material of the C2 hydrogenation reactor, Q is the control function of the selectivity of each reactor section; ΔR is the disturbance compensation function of the selectivity of each reactor section.

[0040] Optionally, the optimizing the setting value of the operating parameter further includes:

[0041] The functional relationship between the set value of the material temperature at the inlet of each bed and the ethylene selectivity is established. The functional relationship is as follows:

[0042] S n =Q′(T n )+ΔR(Fl,P),

[0043] S end =Q′(T end )+ΔR(Fl,P),

[0044] In the formula, S n , S end are the ethylene selectivity of the nth bed and the last bed, T n , T end are the set values ​​of the inlet material temperature of the nth bed and the last bed, respectively; wherein n=1, 2, ... (N-1), and Q′ is the selective temperature control function of each bed.

[0045] Optionally, the optimizing the setting value of the operating parameter further includes:

[0046] Acquire the inlet temperature setting value corresponding to the maximum value of ethylene selectivity obtained by establishing a functional relationship between the inlet material temperature setting value of each bed and the ethylene selectivity;

[0047] Obtaining a set value of the volume content ratio of hydrogen to acetylene obtained by establishing a functional relationship between the material temperature at the inlet of each bed section and the set value of the hydrogen-acetylene ratio;

[0048] The obtained inlet temperature setting value and hydrogen to acetylene volume content ratio setting value corresponding to the maximum value of ethylene selectivity are returned to the C2 hydrogenation load distribution model, thereby assigning values ​​to the operating parameters corresponding to the setting value of the acetylene hydrogenation conversion amount of each bed section and the setting value of the acetylene volume content at the outlet of each bed section.

[0049] In a second aspect, the present invention provides a control system for a carbon dihydrogenation reactor, using any control method described in the first aspect, comprising:

[0050] C2 hydrogenation load distribution model module, expert knowledge base module, gain scheduling module, soft measurement module, analysis and evaluation module, control module and online correction module;

[0051] The output end of the soft measurement module is electrically connected to the input end of the analysis and evaluation module, the expert knowledge base module and the C2 hydrogenation load distribution model module respectively, the expert knowledge base module is communicatively connected to the C2 hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected to the input end of the gain scheduling module, the output end of the C2 hydrogenation load distribution model module is electrically connected to the input end of the control module, and the output end of the gain scheduling module is electrically connected to the input end of the control module;

[0052] The analysis and operation data of the C2 hydrogenation reactor are classified and statistically calculated by the soft measurement module and the analysis and evaluation module, and then transmitted to the C2 hydrogenation load distribution model module for fitting calculation, so as to obtain the operation parameter setting value;

[0053] The expert knowledge base optimizes the operating parameter setting values ​​using an optimization mode and an operating rule set to obtain optimized operating parameter setting values;

[0054] The gain scheduling module and the control module control the C2 hydrogenation reactor based on the optimized operating parameter set values.

[0055] Optionally, the operating rule set includes boundary limitations on control parameters, a selected operating parameter adjustment order, a selected operating parameter adjustment frequency and / or a selected operating parameter adjustment amplitude.

[0056] Optionally, the selected operating parameters include:

[0057] Inlet material pressure, inlet material flow rate, hydrogen volume content in the inlet material of each bed section, inlet material temperature of each bed section, volume content ratio of hydrogen to acetylene at the inlet of each bed section and / or bed temperature rise of each bed reactor.

[0058] Optionally, the carbon two hydrogenation reactor does not need to be equipped with a hydrogenation moderator, and the hydrogenation moderator includes crude hydrogen and CO;

[0059] and / or

[0060] The invention relates to a process for removing acetylene by hydrogenation from ethylene refining applied to the separation process of an ethylene cracking unit. The separation process includes a sequential separation process, a process of removing propanation first and then hydrogenation, and a process of removing ethane first and then hydrogenation.

[0061] Optionally, the inlet material of the carbon two hydrogenation reactor includes ethylene, ethane and acetylene, and also includes at least one of hydrogen, methane, propylene and propane;

[0062] and / or

[0063] The carbon two hydrogenation catalyst added to the carbon two hydrogenation reactor includes: at least one of Pd, Ni, Pt, Rh, and Ru, with a content of 0.01-0.5wt%;

[0064] The promoter includes at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halogen family, alkali metal family, and alkaline earth metal family, and the content is 0.01-1.0wt%;

[0065] The carrier includes at least one of aluminum oxide, molecular sieve, silicon oxide, gallium oxide, titanium oxide and activated carbon.

[0066] The present invention obtains operating parameter setting values ​​by fitting real-time statistical data through a carbon two hydrogenation load distribution model, controls the carbon two hydrogenation reactor based on the operating parameter setting values, realizes automatic control of the carbon two hydrogenation reactor, optimizes the reactor control parameters, thereby reducing energy and material consumption while extending the full life cycle of the catalyst. BRIEF DESCRIPTION OF THE DRAWINGS

[0067] Exemplary embodiments of the present invention will be described in more detail with reference to the accompanying drawings.

[0068] Figure 1 A flow chart showing a method for controlling a carbon dihydrogenation reactor according to an embodiment of the present invention is shown;

[0069] Figure 2 A principle block diagram of a control system of a carbon dihydrogenation reactor according to an embodiment of the present invention is shown;

[0070] Figure 3 A schematic diagram of a process flow of a carbon dihydrogenation reactor according to an embodiment of the present invention is shown;

[0071] Figure 4 A comparison diagram of operating parameter changes after adopting the control method of the carbon two hydrogenation reactor of this embodiment is shown;

[0072] in:

[0073] 1-first stage bed reactor, 2-last stage bed reactor, 3-ethylene distillation tower. DETAILED DESCRIPTION

[0074] The specific embodiments of the present invention are described in detail below. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention, and are not used to limit the present invention.

[0075] The present invention will be further described below in conjunction with embodiments, but the scope of the present invention is not limited to these embodiments.

[0076] The carbon dihydrogenation reactor in this embodiment includes a multi-stage bed reactor.

[0077] Embodiment 1:

[0078] like Figure 1 As shown, a control method for a carbon dihydrogenation reactor comprises:

[0079] Step S101: Acquire running data and operation data of a carbon two hydrogenation reactor;

[0080] In specific application scenarios, running data and operation data are obtained through various sensors installed on the carbon dihydrogenation reactor.

[0081] Step S102: classify and count the running data and operation data to obtain real-time statistical data;

[0082] Step S103: fitting and calculating the real-time statistical data through the C2 hydrogenation load distribution model to obtain the operating parameter setting value;

[0083] Step S104: Controlling the carbon two hydrogenation reactor based on the operating parameter setting values.

[0084] Optionally, the C2 hydrogenation load distribution model includes a set value model for acetylene hydrogenation conversion amount and a set value model for outlet acetylene volume content;

[0085] The set value model of the acetylene hydrogenation conversion amount is:

[0086]

[0087] Where Y n is the set value of acetylene hydrogenation conversion amount in the nth stage bed; F n (X) is the hydrogenation distribution function of the nth stage bed, wherein n=1, 2, ... (N-1); X is the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor; N is the total number of stages of the C2 hydrogenation reactor; a i is the segment number impact factor, which is associated with the total number of segments N, where i = 1, 2, ... (N-1);

[0088] The set value model of the outlet acetylene volume content is:

[0089]

[0090] Where M n out is the set value of the acetylene volume content at the outlet of the nth stage bed, where n = 1, 2, ... (N-1); Y k is the set value of the acetylene hydrogenation conversion amount of the kth bed, where k = 1, 2, ...n.

[0091] Optionally, the acetylene volume content at the outlet of the last stage bed is set to M end out , M end out To specify the constant Ω, the value range of Ω is 0<Ω<1ppm.

[0092] Optionally, the total number of stages N of the C2 hydrogenation reactor ranges from: an integer of 1 < N < 6;

[0093] The volume content X of acetylene in the total inlet material of the C2 hydrogenation reactor ranges from: 0.3% ≤ X ≤ 5.5%.

[0094] F n (x) is independent of the total number of reactor stages and is related to the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor.

[0095] Optionally, after the step of obtaining the set value of the operating parameter by fitting and calculating the real-time statistical data through the C2 hydrogenation load distribution model module, the following is further included:

[0096] Optimizing the set value of the operating parameter, and the optimization of the set value of the operating parameter includes:

[0097] Establishing a functional relationship between the acetylene hydrogenation conversion amount of each bed and the selected operating parameters through the C2 hydrogenation load distribution model, and the functional relationship is as follows:

[0098] Y = G(R, T, M in ) + ΔE(Fl, P) (3),

[0099] In the formula, Y is the acetylene conversion amount of each stage reactor, R is the volume content ratio of hydrogen to acetylene at the inlet of each stage reactor, T is the temperature of the inlet material of each stage reactor, M in The volume content of acetylene at the inlet of each stage reactor; Fl and P are respectively the flow rate and pressure of the inlet material of the C2 hydrogenation reactor. Fl and P are disturbance variables and are related to the upstream feed of the C2 hydrogenation reactor. G is the control function of the hydrogenation activity of each stage reactor; ΔE is the disturbance compensation function of the hydrogenation activity of each stage reactor.

[0100] The C2 hydrogenation load distribution model expression 3 shows that the change in the acetylene conversion amount of each stage reactor is affected by multiple factor variables such as the volume content of acetylene at the inlet of each stage reactor, the temperature of the inlet material of the reactor, the volume content ratio of hydrogen to acetylene at the inlet, and the flow rate and pressure of the inlet material of the reactor. Among them, the flow rate and pressure of the inlet material of the reactor are affected by the upstream unit operation and cannot be adjusted in the C2 hydrogenation unit. In the actual production process, the flow rate and pressure of the inlet material are generally used as compensation variables to correct the function. In the expressions 1 and 2 of the C2 hydrogenation load distribution model, a functional relationship is established between the acetylene conversion amount of each stage reactor and the volume content of acetylene at the inlet of each stage reactor based on the C2 hydrogenation reaction characteristics and reactor design optimization. Therefore, a bivariate functional relationship between Y and R and T can be formed.

[0101] Optionally, the optimization of the set value of the operating parameter further includes:

[0102] A functional relationship is established between the material temperature at the inlet of each bed and the set value of the hydrogen-acetylene ratio, and the functional relationship is:

[0103] R n =G′(T n )+ΔE(Fl,P) (4),

[0104] R end =G′(T end )+ΔE(Fl,P) (5),

[0105] R n is the set value of the volume content ratio of hydrogen to acetylene at the inlet of the nth stage bed, T n is the set value of the material temperature at the inlet of the nth stage bed; where n = 1, 2, ... (N-1); R end , T end are the volume ratio of hydrogen to acetylene in the inlet of the last stage bed and the inlet material temperature, respectively; G′ is the temperature control function of the hydrogenation activity of each stage reactor.

[0106] The nth stage bed setting value Y is calculated based on the real-time device data through expressions 1 and 2 of the C2 hydrogenation load distribution model. n 、M n or / and end bed Y end 、M end , and these set values ​​Y n 、M n or / and and Y end 、M end Substitute the constant coefficient into Expression 3 to establish a functional relationship between the set values ​​of the inlet material temperature of the nth bed or / and the hydrogen-acetylene ratio, as shown in Expressions 4 and 5.

[0107] Optionally, the optimizing the setting value of the operating parameter further includes:

[0108] The functional relationship between the acetylene selectivity of each bed and the selected operating parameters is established as follows:

[0109] S=Q(R,T,M in , M out )+ΔR(Fl,P) (6),

[0110] Where S is the ethylene selectivity of each bed, R is the volume ratio of hydrogen to acetylene at the inlet of each bed, T is the material temperature at the inlet of each bed, M in Acetylene volume content at each bed inlet, M outThe volume content of acetylene at the outlet of each bed; Fl and P are the material flow and pressure at the inlet of the C2 hydrogenation reactor respectively, Fl and P are disturbance variables, which are related to the upstream incoming material of the C2 hydrogenation reactor, Q is the control function of the selectivity of each reactor section; ΔR is the disturbance compensation function of the selectivity of each reactor section.

[0111] Optionally, the optimizing the setting value of the operating parameter further includes:

[0112] The functional relationship between the set value of the material temperature at the inlet of each bed and the ethylene selectivity is established. The functional relationship is as follows:

[0113] S n =Q'(T n )+ΔR(Fl,P) (7),

[0114] S end =Q'(T end )+ΔR(Fl,P) (8),

[0115] In the formula, S n , S end are the ethylene selectivity of the nth bed and the last bed, T n , T end are the set values ​​of the inlet material temperature of the nth bed and the last bed, respectively; wherein n=1, 2, ... (N-1), and Q′ is the selective temperature control function of each bed.

[0116] Optionally, the optimizing the setting value of the operating parameter further includes:

[0117] Acquire the inlet temperature setting value corresponding to the maximum value of ethylene selectivity obtained by establishing a functional relationship between the inlet material temperature setting value of each bed and the ethylene selectivity;

[0118] Obtaining a set value of the volume content ratio of hydrogen to acetylene obtained by establishing a functional relationship between the material temperature at the inlet of each bed section and the set value of the hydrogen-acetylene ratio;

[0119] The obtained inlet temperature setting value and hydrogen to acetylene volume content ratio setting value corresponding to the maximum value of ethylene selectivity are returned to the C2 hydrogenation load distribution model, thereby assigning values ​​to the operating parameters corresponding to the setting value of the acetylene hydrogenation conversion amount of each bed section and the setting value of the acetylene volume content at the outlet of each bed section.

[0120] That is, by calculating by Expression 7 and Expression 8, we can get the S of the nth bed n and / or terminal bed S end When it is the maximum value, the corresponding inlet temperature setting value T n Smax and T end Smax , and the hydrogen-acetylene ratio setting value R is calculated by expression 4 and expression 5 n Smax and Rend Smax , returns the C2 hydrogenation load distribution model module to the nth bed setting value Y n 、M n or / and end bed Y end 、M end The corresponding operation parameter assignment.

[0121] The selected operating parameters of the carbon dioxide hydrogenation reactor include the inlet material pressure, the inlet material flow rate, the volume content of hydrogen in the inlet material of each bed section, the inlet material temperature of each bed section, the volume content ratio of hydrogen to acetylene in the inlet of each bed section, and the bed temperature rise of each bed section reactor, preferably the inlet material temperature of each bed section and the volume content ratio of hydrogen to acetylene in the inlet of each bed section.

[0122] Embodiment 2:

[0123] A control system for a carbon dihydrogenation reactor, using a control method according to an embodiment, comprising:

[0124] C2 hydrogenation load distribution model module, expert knowledge base module, gain scheduling module, soft measurement module, analysis and evaluation module, control module and online correction module;

[0125] The output end of the soft measurement module is electrically connected to the input end of the analysis and evaluation module, the expert knowledge base module and the C2 hydrogenation load distribution model module respectively, the expert knowledge base module is communicatively connected to the C2 hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected to the input end of the gain scheduling module, the output end of the C2 hydrogenation load distribution model module is electrically connected to the input end of the control module, and the output end of the gain scheduling module is electrically connected to the input end of the control module;

[0126] The analysis and operation data of the C2 hydrogenation reactor are classified and statistically calculated by the soft measurement module and the analysis and evaluation module, and then transmitted to the C2 hydrogenation load distribution model module for fitting calculation, so as to obtain the operation parameter setting value;

[0127] The expert knowledge base optimizes the operating parameter setting values ​​using an optimization mode and an operating rule set to obtain optimized operating parameter setting values;

[0128] The gain scheduling module and the control module control the C2 hydrogenation reactor based on the optimized operating parameter set values.

[0129] Optionally, the operating rule set includes boundary limitations on control parameters, a selected operating parameter adjustment order, a selected operating parameter adjustment frequency and / or a selected operating parameter adjustment amplitude.

[0130] Optionally, the selected operating parameters include:

[0131] Inlet material pressure, inlet material flow rate, hydrogen volume content in the inlet material of each bed section, inlet material temperature of each bed section, volume content ratio of hydrogen to acetylene at the inlet of each bed section and / or bed temperature rise of each bed reactor.

[0132] Optionally, the carbon two hydrogenation reactor does not need to be equipped with a hydrogenation moderator, and the hydrogenation moderator includes crude hydrogen and CO;

[0133] and / or

[0134] The invention relates to a process for removing acetylene by hydrogenation from ethylene refining applied to the separation process of an ethylene cracking unit. The separation process includes a sequential separation process, a process of removing propanation first and then hydrogenation, and a process of removing ethane first and then hydrogenation.

[0135] Optionally, the inlet material of the carbon two hydrogenation reactor includes ethylene, ethane and acetylene, and also includes at least one of hydrogen, methane, propylene and propane;

[0136] and / or

[0137] The carbon two hydrogenation catalyst added to the carbon two hydrogenation reactor includes: at least one of Pd, Ni, Pt, Rh, and Ru, with a content of 0.01-0.5wt%;

[0138] The promoter includes at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halogen family, alkali metal family, and alkaline earth metal family, and the content is 0.01-1.0wt%;

[0139] The carrier includes at least one of aluminum oxide, molecular sieve, silicon oxide, gallium oxide, titanium oxide and activated carbon.

[0140] like Figure 2As shown, the control system is located in a server connected to the distributed control system, i.e., the DCS system, of the C2 hydrogenation reactor. The control module is located at the bottom layer of the modular automatic control system of the C2 hydrogenation reactor, and is connected to the DCS system through the OPC Server, directly issuing optimized control signals and commands to the DCS; the gain scheduling module is also located at the bottom layer of the system, providing the control module with the gain and frequency of each adjustment parameter; the soft measurement module and the C2 hydrogenation load distribution model module are located at the middle layer of the modular automatic control system of the C2 hydrogenation reactor, wherein the C2 hydrogenation load distribution model module provides the main optimized control parameter setting values ​​for the bottom control module through model calculation and solution; the expert knowledge base module and the analysis and evaluation module are both located at the top layer of the modular automatic control system of the C2 hydrogenation reactor, and the expert knowledge base module combines the operation data trends provided by the soft measurement and analysis and evaluation modules, and optimizes the operation parameter setting values ​​calculated by the C2 hydrogenation load distribution model module using the optimization mode and the operation rule set, and returns them to the C2 hydrogenation load distribution model module for data correction, and directs the gain scheduling module to implement automatic control.

[0141] like Figure 3 As shown, the carbon two hydrogenation reactor includes a first-stage bed reactor, a last-stage bed reactor and an ethylene distillation tower. Other stage bed reactors can be arranged between the first-stage bed reactor and the last-stage bed reactor as required.

[0142] In this embodiment, the soft measurement module monitors in real time the composition and content of materials before and after the carbon dioxide hydrogenation reactor, the composition of the top of the deethanizer tower, and the composition and content of materials at the top and bottom of the ethylene distillation tower. The real-time data is filtered and input into the soft measurement model to measure the values ​​and trends of the composition and content of each material.

[0143] The analysis and evaluation module monitors in real time the online operation time of the catalyst, material flow, reaction temperature, pressure, changes in the contents of hydrogen, carbon II composition, carbon III composition, water, etc. before and after the reaction, and inputs the real-time data into the analysis and evaluation model to measure the catalyst's operating life, activity, ethylene selectivity, acetylene conversion rate and other performance.

[0144] The ethylene selectivity is calculated as follows:

[0145]

[0146] The reactivity is as follows:

[0147]

[0148] The acetylene conversion rate is calculated as follows:

[0149]

[0150] The operation optimization modeling method for the C2 hydrogenation reactor aims to obtain the best ethylene selectivity. Through the C2 hydrogenation load distribution model module, fitting calculations are performed on real-time data to give the set values of operation parameters. Then, through the expert knowledge base, the set values of operation parameters calculated by the model are optimized using the optimization mode and operation rule set, and then the control module and gain scheduling module are commanded to implement automatic control. The analysis and operation data of the C2 hydrogenation reactor are classified and statistically calculated through the soft measurement module and analysis and evaluation module, and then enter the C2 hydrogenation load distribution model module and expert knowledge base module for fitting calculations.

[0151] More specifically, the C2 hydrogenation load distribution model is established based on the simulation of the C2 hydrogenation reaction process and the optimization of reactor design, and the expression is as follows:

[0152]

[0153] In the formula, Y n is the set value of the acetylene hydrogenation conversion amount in the nth bed, F n (X) is the hydrogenation distribution function of the nth bed; where n = 1, 2,... (N - 1); X is the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor; N is the total number of beds of the C2 hydrogenation reactor; a i is the section number influence factor, affected by the total number of beds N, where i = 1, 2,... (N - 1).

[0154]

[0155] In the formula, M n out is the set value of the acetylene volume content at the outlet of the nth bed, where n = 1, 2,... (N - 1); Y k is the set value of the acetylene hydrogenation conversion amount in the kth bed, where k = 1, 2,... n.

[0156] The set value M of the acetylene volume content at the outlet of the last bed of the C2 hydrogenation reactor end out is a specified constant Ω, and the value range of Ω is 0 < Ω < 1 ppm.

[0157] In the C2 hydrogenation load distribution model, N is the total number of beds of the multi-bed C2 hydrogenation reactor, and its value range is: an integer of 1 < N < 6; X is the volume content of acetylene at the total inlet of the reactor, and its value range is 0.3% ≤ X ≤ 5.5%; F n (X) is the hydrogenation distribution function of the nth bed, which is not affected by the total number of reactor beds and is only related to the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor, where n = 1, 2,... (N - 1); Y nis the set value of the acetylene hydrogenation conversion amount of the nth bed calculated by the model, which is calculated by the multi-bed acetylene hydrogenation load distribution model, where n=1, 2, ... (N-1).

[0158] The C2 hydrogenation load distribution model establishes a functional relationship between the acetylene hydrogenation conversion amount and the main operating parameters of each reactor stage, and its expression is as follows:

[0159] Y=G(R,T,M in )+ΔE(Fl,P),

[0160] Where, Y is the acetylene conversion amount of each reactor, R is the volume ratio of hydrogen to acetylene at the inlet of each reactor, T is the material temperature at the inlet of each reactor, M in The volume content of acetylene at the inlet of each section of the reactor; Fl and P are the material flow rate and pressure at the inlet of the C2 hydrogenation reactor respectively. Fl and P are disturbance variables, which are affected by the upstream material of the C2 hydrogenation reactor. G is the control function of the hydrogenation activity of each section of the reactor; ΔE is the disturbance compensation function of the hydrogenation activity of each section of the reactor.

[0161] The expression of the C2 hydrogenation load distribution model shows that the change in the acetylene conversion amount of each section of the reactor is affected by multiple variables such as the acetylene volume content at the inlet of each section of the reactor, the material temperature at the inlet of the reactor, the ratio of the volume content of hydrogen to acetylene at the inlet, and the material flow rate and pressure at the inlet of the reactor. Among them, the material flow rate and pressure at the inlet of the reactor are affected by the operation of the upstream unit and cannot be adjusted in the C2 hydrogenation unit. In the actual production process, the inlet material flow rate and pressure are generally used as compensation variables to correct the function. In the expression of the C2 hydrogenation load distribution model, a functional relationship is established between the acetylene conversion amount of each section of the reactor and the acetylene volume content at the inlet of each section of the reactor based on the reaction characteristics of C2 hydrogenation and the optimization of reactor design. Therefore, a two-variable functional relationship between Y and R and T can be formed.

[0162] The nth stage bed setting value Y is calculated based on the real-time device data through the expression 1 and expression 2 of the carbon 2 hydrogenation load distribution model. n 、M n or / and end bed Y end 、M end , and these set values ​​Y n 、M n or / and and Y end 、M end Substitute the fixed value coefficient into Expression 3 to establish a functional relationship between the set value of the inlet material temperature of the nth bed or / the last bed and the hydrogen-acetylene ratio, and the expression is as follows:

[0163] R n =G'(T n )+ΔE(Fl,P),

[0164] R end =G'(T end )+ΔE(Fl,P),

[0165] In the formula, R n is the set value of the volume content ratio of hydrogen to acetylene at the inlet of the nth stage bed, T n is the set value of the material temperature at the inlet of the nth stage bed; where n = 1, 2, ... (N-1); R end , T end , are the volume ratio of hydrogen to acetylene and the inlet material temperature of the last stage bed, respectively, and G′ is the temperature control function of the hydrogenation activity of each stage reactor.

[0166] The expert optimization module includes an optimization mode and an operation rule set, which guides the C2 hydrogenation load distribution model module and the gain scheduling module after data optimization fitting. The optimization mode adopted by the expert optimization module establishes a functional relationship between the acetylene selectivity of each bed and the main operating parameters, and its expression is as follows:

[0167] S=Q(R,T,M in , M out )+ΔR(Fl,P),

[0168] Where S is the ethylene selectivity of each reactor, R is the volume ratio of hydrogen to acetylene at the inlet of each reactor, T is the material temperature at the inlet of each reactor, M in Acetylene volume content at the inlet of each reactor, M out The volume content of acetylene at the outlet of each section of the reactor; Fl and P are the material flow and pressure at the inlet of the C2 hydrogenation reactor respectively. Fl and P are disturbance variables, which are affected by the upstream material of the C2 hydrogenation reactor. Q is the control function of the selectivity of each section of the reactor; ΔR is the disturbance compensation function of the selectivity of each section of the reactor.

[0169] In the optimization mode of the expert optimization module, the carbon two hydrogenation load distribution model expression 1 and expression 2 are used to calculate the nth stage bed setting value Y n 、M n Or / and the final bed setting value Y end 、M end Substitute the given coefficients into expressions 4, 5 and 6 to establish a functional relationship between the set value of the inlet material temperature of the nth bed or / and the last bed and the ethylene selectivity, as shown below:

[0170] S n =Q′(T n )+ΔR(Fl,P),

[0171] S end =Q′(T end )+ΔR(Fl,P),

[0172] In the formula, S n , S end are the ethylene selectivity of the nth bed and the last bed, T n , T end are the set values ​​of the inlet material temperature of the nth bed and the last bed, respectively; where n = 1, 2, ... (N-1), and Q' is the temperature control function of the selectivity of each bed.

[0173] The expert optimization module uses Expression 7 and Expression 8) to calculate and obtain the nth bed S n and / or terminal bed S end When it is the maximum value, the corresponding inlet temperature setting value T n Smax and T end Smax , and the hydrogen-acetylene ratio setting value R is calculated by expression 4 and expression 5) n Smax and R end Smax , returns the C2 hydrogenation load distribution model module to the nth bed setting value Y n 、M n or / and end bed Y end 、M end The corresponding operation parameter assignment.

[0174] The operating rule set in the expert optimization module includes boundary limits for control parameters such as inlet material temperature of each section, inlet acetylene and hydrogen volume content, material flow rate, pressure, etc.; adjustment order, frequency and amplitude of main operating parameters such as hydrogen-acetylene ratio and inlet material temperature; adjustment compensation coefficients for main operating parameters of the reactor when poisons such as CO, water, sulfur and methanol are introduced; formula for the decay of ethylene selectivity over time during the catalyst operation cycle, etc.

[0175] 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 C2 hydrogenation load distribution model module.

[0176] The main operating parameters of the carbon dioxide hydrogenation reactor in the operation optimization modeling method of the carbon dioxide hydrogenation reactor include the inlet material pressure, the inlet material flow rate, the volume content of hydrogen in the inlet material of each bed section, the inlet material temperature of each bed section, the volume content ratio of hydrogen to acetylene in the inlet of each bed section, and the temperature rise of the bed layer of each bed reactor, preferably the inlet material temperature of each bed section and the volume content ratio of hydrogen to acetylene in the inlet of each bed section.

[0177] The modeling method for optimizing the operation of a C2 hydrogenation reactor does not require the addition of crude hydrogen, CO or other hydrogenation moderators.

[0178] The optimization modeling method for the operation of the carbon two hydrogenation reactor is applied to the process of ethylene refining and hydrogenation to remove acetylene in the separation process of the ethylene cracking unit. The separation process includes a sequential separation process, a pre-depropanization and then hydrogenation process, a pre-de-ethanization and then hydrogenation process, etc.

[0179] The composition of the inlet material of the carbon two hydrogenation reactor contains at least ethylene, ethane, acetylene, and also includes at least one of hydrogen, methane, propylene and propane.

[0180] The concentrations are expressed in volume percentage, and the flow rates are expressed in mass flow rates.

[0181] The main active component of the carbon dihydrogenation catalyst is at least one of Pd, Ni, Pt, Rh and Ru, with a content of 0.01-0.5wt%; the co-catalyst includes at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halogen family, alkali metal family, alkaline earth metal family, etc., with a content of 0.01-1.0wt%; the carrier is at least one of aluminum oxide, molecular sieve, silicon oxide, gallium oxide, titanium oxide, activated carbon, etc.

[0182] The control system uses C# language to implement the design of iterative learning control software. The software includes data acquisition part, data storage and learning control algorithm part. The control system software uses OPC technology to communicate with the DCS system of the C2 hydrogenation unit, reads real-time process variable data, and realizes the optimization control of the C2 hydrogenation reactor through write operation. The data storage part can store historical data.

[0183] By utilizing the knowledge framework of C2 hydrogenation reaction principle and reactor design optimization, combined with the long-term evaluation test results of the catalyst in the industrial side line, a C2 hydrogenation load distribution model was established and supplemented by the expert knowledge base optimization model, and the automatic control of the C2 hydrogenation reactor was realized under the actual production fluctuation conditions. With the optimal ethylene yield as the goal, the reactor control parameters were fully optimized, reducing energy and material consumption while extending the full life cycle of the catalyst.

[0184] Embodiment three:

[0185] The modular automatic control system of the C2 hydrogenation reactor was established. This included constructing a C2 hydrogenation load distribution model; establishing an expert knowledge base to use the deep knowledge of the catalyst combined with gain scheduling to design the rules for switching the local controller model. The control system used C# language to write the expert control software, and tested the reliability of the software.

[0186] The method of the present invention is applied to the C2 hydrogenation reaction control unit of the olefin plant: the modular automatic control system of the C2 hydrogenation reactor is connected to the device DCS through the OPC Server, various process conditions are optimized and adjusted, and the adjustment target is provided to the DCS system in real time to realize automatic control of the C2 hydrogenation reactor.

[0187] Figure 4 The changes of various process parameters of the hydrogen dosage of the C2 hydrogenation reactor after the automatic control system was put into use are given.

[0188] The commissioning of the C2 hydrogenation reactor control system has significantly improved ethylene selectivity. Under the same reactor, catalyst and feed composition conditions, the introduction of the automatic control system can increase the average ethylene selectivity from 42.3% before commissioning to 57.6% after commissioning, an increase of 15.3 percentage points, and the efficiency-enhancing effect is very obvious.

[0189] Comparative Example:

[0190] An olefin plant with an annual output of 800,000 tons of ethylene has a total of 15 cracking furnaces, which can process various cracking raw materials from ethane to hydrogenation tail oil. The separation process of the plant adopts a sequential separation process. The carbon two hydrogenation reactor is located between the cold zone deethanizer and the ethylene distillation tower. The carbon two fraction obtained from the top of the deethanizer tower is heat exchanged to the required temperature through the cooler (or preheater), and then enters the hydrogenation reactor through the raw material dryer, mixed with hydrogen in the pipeline, and enters the reactor catalytic bed for selective hydrogenation reaction. The plant's carbon two hydrogenation process is designed with a double-stage bed, with a heat exchanger between the stages, two in operation and one in standby. The process flow is as follows Figure 2 As shown. The normal operation of the carbon two hydrogenation reactor in this plant is manually adjusted by the operator. The inlet acetylene of the carbon two hydrogenation reactor is 0.9-1.0mol%, and the outlet acetylene is required to be less than 1ppm. The catalyst is the BC-H-20B catalyst developed by Sinopec Beijing Chemical Research Institute.

[0191] The comparison results show that the introduction of the method and system of the present invention can significantly improve the ethylene yield and reduce the hydrogen consumption compared with the manual control of the original factory.

[0192] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

[0193] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

Claims

1. A method for controlling a carbon dihydrogenation reactor, characterized in that: include: Obtaining the operation data and operating data of the C2 hydrogenation reactor; Classify and count the running data and operation data to obtain real-time statistical data; The operating parameter setting values ​​are obtained by fitting and calculating the real-time statistical data through the C2 hydrogenation load distribution model; Controlling the carbon two hydrogenation reactor based on the operating parameter set value; The C2 hydrogenation load distribution model includes a set value model for acetylene hydrogenation conversion amount and a set value model for outlet acetylene volume content; The set value model of the acetylene hydrogenation conversion amount is: Where Y n is the set value of acetylene hydrogenation conversion amount in the nth stage bed; F n (X) is the hydrogenation distribution function of the nth stage bed, wherein n=1, 2, ... (N-1); X is the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor; N is the total number of stages of the C2 hydrogenation reactor; a i is the segment number impact factor, which is associated with the total number of segments N, where i = 1, 2, ... (N-1); The set value model of the outlet acetylene volume content is: Where M n out is the set value of the acetylene volume content at the outlet of the nth stage bed, where n = 1, 2, ... (N-1); Y k is the set value of the acetylene hydrogenation conversion amount of the kth stage bed, where k = 1, 2, ... n; After the step of fitting and calculating the real-time statistical data to obtain the operating parameter setting value through the C2 hydrogenation load distribution model module, the method further includes: Optimizing the operating parameter setting value, wherein the optimizing the operating parameter setting value comprises: The carbon two hydrogenation load distribution model is used to establish a functional relationship between the acetylene hydrogenation conversion amount of each bed and the selected operating parameters. The functional relationship is as follows: Y=G(R,T,M in )+ΔE(Fl,P), Where, Y is the acetylene conversion amount of each reactor, R is the volume ratio of hydrogen to acetylene at the inlet of each reactor, T is the material temperature at the inlet of each reactor, M in The volume content of acetylene at the inlet of each section of the reactor; Fl and P are the material flow rate and pressure at the inlet of the C2 hydrogenation reactor respectively. Fl and P are disturbance variables, which are related to the upstream incoming materials of the C2 hydrogenation reactor. G is the control function of the hydrogenation activity of each section of the reactor; ΔE is the disturbance compensation function of the hydrogenation activity of each section of the reactor.

2. The control method of a carbon dihydrogenation reactor according to claim 1, characterized in that: The acetylene volume content at the outlet of the last stage bed is set to M end out , M end out To specify the constant Ω, the value range of Ω is 0<Ω<1ppm.

3. The control method of a carbon dihydrogenation reactor according to claim 1, characterized in that: The total number of stages N of the carbon dihydrogenation reactor is in the range of an integer of 1<N<6; The value range of the acetylene volume content X in the total inlet material of the carbon dihydrogenation reactor is: 0.3%≤X≤5.5%; F n (X) has nothing to do with the total number of reactor stages, but is related to the volume content of acetylene in the total inlet material of the C2 hydrogenation reactor.

4. The control method of a carbon dihydrogenation reactor according to claim 1, characterized in that: The optimizing the setting value of the operating parameter further comprises: A functional relationship is established between the material temperature at the inlet of each bed and the set value of the hydrogen-acetylene ratio, and the functional relationship is: R n =G′(T n )+ΔE(Fl,P), R end =G′(T end )+ΔE(Fl,P), R n is the set value of the volume content ratio of hydrogen to acetylene at the inlet of the nth stage bed, T n is the set value of the material temperature at the inlet of the nth stage bed; where n = 1, 2, ... (N-1); R end , T end are the volume ratio of hydrogen to acetylene in the inlet of the last stage bed and the inlet material temperature, respectively; G′ is the temperature control function of the hydrogenation activity of each stage reactor.

5. The control method of a carbon dihydrogenation reactor according to claim 4, characterized in that: The optimizing the setting value of the operating parameter further comprises: The functional relationship between the acetylene selectivity of each bed and the selected operating parameters is established as follows: S=Q(R,T,M in ,M out )+ΔR(Fl,P), Where S is the ethylene selectivity of each bed, R is the volume ratio of hydrogen to acetylene at the inlet of each bed, T is the material temperature at the inlet of each bed, M in Acetylene volume content at each bed inlet, M out The volume content of acetylene at the outlet of each bed; Fl and P are the material flow and pressure at the inlet of the C2 hydrogenation reactor respectively, Fl and P are disturbance variables, which are related to the upstream incoming material of the C2 hydrogenation reactor, Q is the control function of the selectivity of each reactor section; ΔR is the disturbance compensation function of the selectivity of each reactor section.

6. The control method of a carbon dihydrogenation reactor according to claim 5, characterized in that: The optimizing the setting value of the operating parameter further comprises: The functional relationship between the set value of the material temperature at the inlet of each bed and the ethylene selectivity is established. The functional relationship 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 end are the ethylene selectivity of the nth bed and the last bed, T n , T end are the set values ​​of the inlet material temperature of the nth bed and the last bed, respectively; wherein n=1, 2, ... (N-1), and Q′ is the selective temperature control function of each bed.

7. The control method of a carbon dihydrogenation reactor according to claim 6, characterized in that: The optimizing the setting value of the operating parameter further comprises: Acquire the inlet temperature setting value corresponding to the maximum value of ethylene selectivity obtained by establishing a functional relationship between the inlet material temperature setting value of each bed and the ethylene selectivity; Obtaining a set value of the volume content ratio of hydrogen to acetylene obtained by establishing a functional relationship between the material temperature at the inlet of each bed section and the set value of the hydrogen-acetylene ratio; The obtained inlet temperature setting value and hydrogen to acetylene volume content ratio setting value corresponding to the maximum value of ethylene selectivity are returned to the C2 hydrogenation load distribution model, thereby assigning values ​​to the operating parameters corresponding to the setting value of the acetylene hydrogenation conversion amount of each bed section and the setting value of the acetylene volume content at the outlet of each bed section.

8. A control system for a carbon dihydrogenation reactor, using the control method according to any one of claims 1 to 7, characterized in that: include: C2 hydrogenation load distribution model module, expert knowledge base module, gain scheduling module, soft measurement module, analysis and evaluation module, control module and online correction module; The output end of the soft measurement module is electrically connected to the input end of the analysis and evaluation module, the expert knowledge base module and the C2 hydrogenation load distribution model module respectively, the expert knowledge base module is communicatively connected to the C2 hydrogenation load distribution model module, the output end of the expert knowledge base module is electrically connected to the input end of the gain scheduling module, the output end of the C2 hydrogenation load distribution model module is electrically connected to the input end of the control module, and the output end of the gain scheduling module is electrically connected to the input end of the control module; The analysis and operation data of the C2 hydrogenation reactor are classified and statistically calculated by the soft measurement module and the analysis and evaluation module, and then transmitted to the C2 hydrogenation load distribution model module for fitting calculation, so as to obtain the operation parameter setting value; The expert knowledge base optimizes the operating parameter setting values ​​using an optimization mode and an operating rule set to obtain optimized operating parameter setting values; The gain scheduling module and the control module control the C2 hydrogenation reactor based on the optimized operating parameter set values.

9. The control system of the carbon dihydrogenation reactor according to claim 8, characterized in that: The operating rule set includes boundary definitions for control parameters, a selected operating parameter adjustment order, a selected operating parameter adjustment frequency, and / or a selected operating parameter adjustment amplitude.

10. The control system of the carbon dihydrogenation reactor according to claim 9, characterized in that: The selected operating parameters include: Inlet material pressure, inlet material flow rate, hydrogen volume content in the inlet material of each bed section, inlet material temperature of each bed section, volume content ratio of hydrogen to acetylene at the inlet of each bed section and / or bed temperature rise of each bed reactor.

11. The control system of the carbon dihydrogenation reactor according to claim 8, characterized in that: The carbon two hydrogenation reactor does not need to be equipped with a hydrogenation moderator, and the hydrogenation moderator includes crude hydrogen and CO; and / or The invention relates to a process for removing acetylene by hydrogenation from ethylene refining applied to the separation process of an ethylene cracking unit. The separation process includes a sequential separation process, a process of removing propanation first and then hydrogenation, and a process of removing ethane first and then hydrogenation.

12. The control system of the carbon dihydrogenation reactor according to claim 8, characterized in that: The inlet materials of the carbon dihydrogenation reactor include ethylene, ethane and acetylene. Also includes at least one of hydrogen, methane, propylene, and propane; and / or The carbon two hydrogenation catalyst added to the carbon two hydrogenation reactor includes: at least one of Pd, Ni, Pt, Rh, and Ru, with a content of 0.01-0.5wt%; The promoter includes at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, halogen family, alkali metal family, and alkaline earth metal family, and the content is 0.01-1.0wt%; The carrier includes at least one of aluminum oxide, molecular sieve, silicon oxide, gallium oxide, titanium oxide and activated carbon.

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