CN113707227A - Carbon-three-liquid phase hydrogenation reactor control method and system - Google Patents
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Abstract
The invention discloses a method and a system for controlling a carbon-three-liquid phase hydrogenation reactor. The control method of the carbon-three-liquid phase hydrogenation reactor comprises the following steps: carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data; analyzing and fitting the classified statistical data to obtain analysis fitting data, wherein the analysis fitting is based on an optimization mode, an operation rule set and the obtained real-time operation data analysis fitting of the carbon three liquid phase hydrogenation catalyst; establishing a state space model based on the characteristics of the carbon three liquid phase hydrogenation catalyst; obtaining control parameters based on the state space model and the analysis fitting data; obtaining gain scheduling data based on the analysis fitting data; and generating a control instruction based on the control parameter and the gain scheduling data. The method and the system can achieve the aim of obtaining the optimal yield of the propylene.
Description
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-three-liquid phase 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.
In the ethylene cracking device, naphtha and other liquid hydrocarbon raw materials are subjected to steam cracking and separation, and the carbon-three fraction contains propylene, propane and a small amount of propyne and propadiene (MAPD for short), wherein the MAPD content is about 1-5 percent (volume). In propylene polymerization, MAPD reduces the activity of polypropylene catalysts, affecting the product quality of polymer grade propylene. To remove MAPD from the carbon trisection, catalytic selective hydrogenation and solvent absorption methods are currently used in the industry to remove MAPD. The carbon three liquid phase catalytic hydrogenation method has simple process flow and no environmental pollution, so the application of the catalytic hydrogenation method is increasingly common.
The carbon-three liquid phase hydrogenation reactor unit is an important device of a propylene unit recovery system, and selectively hydrogenates MAPD in the carbon-three fraction to propylene under the action of a catalyst. MAPD, if hydrogenated excessively, will produce propane, oligomers and polymers, resulting in loss of propylene; if the hydrogenation effect of MAPD is not good, the concentration of MAPD at the outlet of the reactor is not controlled in the index requirement range, which causes the unqualified product of propylene and influences the production of downstream devices, so the purity and yield of the propylene product are directly influenced by the operation quality of the hydrogenation reactor.
The carbon three liquid phase hydrogenation catalyst generally adopts transition metals such as palladium, nickel and the like as active components, reaction thermodynamic parameters, surface adsorption and desorption reaction rates and process sensitivity of different catalysts are different, and the optimal performance of the catalyst can be ensured by targeted adjustment and optimization.
At present, the production control of the carbon-liquid phase hydrogenation reactor is generally manually regulated and controlled, and technicians manually regulate and control related parameters. Due to the long cracking and separating flow, complex process and limited labor, the carbon-liquid phase hydrogenation reactor cannot be monitored in real time and adjusted and optimized in an expert level. When unstable conditions such as material composition, pressure, temperature, flow, hydrogen fluctuation and the like occur in a carbon-three hydrogenation system, the stability recovery is very slow by only depending on the liquid phase 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 at the outlet of a reactor and excessive hydrogenation of propylene are easy to cause, and the yield of the propylene product and the separation effect of a rectifying tower are influenced.
Disclosure of Invention
In view of this, the invention provides a method and a system for controlling a carbon-three liquid phase hydrogenation reactor, which at least solve the problem of poor yield of propylene in the prior art.
In a first aspect, the present invention provides a method for controlling a carbon three liquid phase hydrogenation reactor, comprising:
carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
analyzing and fitting the classified statistical data to obtain analysis fitting data, wherein the analysis fitting is based on an optimization mode, an operation rule set and the obtained real-time operation data analysis fitting of the carbon three liquid phase hydrogenation catalyst;
establishing a state space model based on the characteristics of the carbon three liquid phase hydrogenation catalyst;
obtaining control parameters based on the state space model and the analysis fitting data;
obtaining gain scheduling data based on the analysis fitting data;
and generating a control instruction based on the control parameter and the gain scheduling data.
Optionally, the method further includes modifying the state space model based on the acquired real-time operation data.
Optionally, the modifying the state space model based on the acquired real-time operation data is that:
and performing least square model correction on the state space model.
Optionally, the state space model is:
a linear time-varying space model of the reaction state of the carbon three liquid phase hydrogenation constructed based on the reaction process of the simulated carbon three liquid phase hydrogenation catalyst;
the parameters for constructing the state linear time-varying space model comprise:
the method comprises the following steps of measuring the temperature of different positions and outlets of a catalyst bed layer in a hydrogenation reactor, the hydrogen flow, the inlet temperature and the circulating material flow of the hydrogenation reactor, the MAPD concentration, the propylene selectivity, the reaction activity and the MAPD conversion rate at the outlet of the hydrogenation reactor, the hydrogen concentration, the carbon-carbon three feeding quantity and the reaction pressure at the inlet of the hydrogenation reactor, and time-varying model parameters of the catalyst deactivation characteristics.
Optionally, the linear time-varying spatial model of the reaction state is:
wherein,
the PV1(k), PV2(k), PV3(k) and PV4(k) are respectively the temperature of the upper part, the middle part, the lower part and the outlet of a catalyst bed layer in the carbon-three hydrogenation reactor;
MV1(k), MV2(k) and MV3(k) are the hydrogen flow, reactor inlet temperature and recycle stream flow, respectively, as the manipulated variables;
CV1(k), CV2(k), CV3(k) and CV4(k) are reactor outlet MAPD concentration, propylene selectivity, reactivity and MAPD conversion, respectively, as output variables;
DV1(k), DV2(k), and DV3(k) are inlet hydrogen concentration, carbon three feed rate, and reaction pressure, respectively, as disturbance variables; a, (t), B, (t), C (t), D (t), E (t), F (t) are all time-varying model parameters of catalyst deactivation characteristics.
Optionally, the propylene selectivity calculation formula is:
and/or the presence of a gas in the gas,
the calculation formula of the reactivity is as follows:
and/or the presence of a gas in the gas,
the calculation formula of the MAPD conversion rate is as follows:
optionally, in the generating of the control instruction based on the control parameter and the gain scheduling data,
adopting a state feedback control structure, solving a feedback control rate K (u is KX) by controlling MVC3 through minimum covariance constraint, and enabling an index
Minimum;
wherein r isj、qiWeight values, Σ, representing the system input and output variances, respectivelyyiSum ΣujAre respectively the system steady stateOutput and input covariance matrix sigmaySum ΣuThe ith, j element on the diagonal of (1).
Optionally, the optimization mode of the carbon three liquid phase hydrogenation catalyst comprises:
the control method comprises a catalyst initial-stage operation control mode, a catalyst final-stage operation control mode, a catalyst stabilization-stage operation control model, a high MAPD conversion rate control mode, an outlet MAPD concentration pilot control mode or a propylene selectivity pilot control mode.
Optionally, the carbon three liquid phase hydrogenation catalyst comprises a carrier, and a main active component and a cocatalyst component loaded on the carrier;
the main active component is at least one selected from Pd, Ni, Pt, Rh and Ru; the content of the main active component is preferably 0.05-0.8 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the cocatalyst component is selected from at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, a halogen family system, an alkali metal family system and an alkaline earth metal family system; the content of the cocatalyst is preferably 0.01-1.0 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the carrier of the carbon three-liquid phase hydrogenation catalyst is at least one selected from alumina, molecular sieve, silica, gallium oxide, titanium oxide and activated carbon.
In a second aspect, the present invention provides a carbon three liquid phase hydrogenation reactor control system comprising: the system comprises a state space model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluating module, a controller module and an online correction module;
the state space model module is used for establishing a state space model based on the characteristics of the carbon three-liquid phase hydrogenation catalyst and obtaining control parameters based on the state space model and the analysis fitting data;
the expert knowledge base module is used for analyzing and fitting the classified statistical data to obtain analysis fitting data, and the analysis fitting is analysis fitting based on an optimization mode, an operation rule set and the obtained real-time operation data of the carbon three liquid phase hydrogenation catalyst;
the gain scheduling module is used for acquiring gain scheduling data based on the analysis fitting data;
the soft measurement module and the analysis and evaluation module are used for carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
the controller module is used for generating a control instruction based on the control parameter and the gain scheduling data;
and the online correction module is used for correcting the state space model based on the acquired real-time operation data.
Optionally, the real-time operation data is classified and counted by the soft measurement module and the analysis and evaluation module, and then is output to the expert knowledge base module and the online correction module.
The method comprises the steps of carrying out classification statistics, analysis fitting on operation data of the hydrogenation reactor, and generating a control instruction based on a state space model and gain scheduling data to control the carbon-liquid phase hydrogenation reactor. Different controls are carried out aiming at different carbon three liquid phase hydrogenation catalysts, and the maximum efficiency of the carbon three liquid phase hydrogenation catalyst is exerted, so that the aim of obtaining the optimal propylene yield is fulfilled.
The automatic control of the carbon-three-liquid phase hydrogenation reactor is realized under the condition of actual production fluctuation by establishing a state space model and assisting expert knowledge. The optimal propylene yield is obtained by combining the minimum covariance constraint control and the gain scheduling method, and the full life operation cycle of the catalyst is prolonged while the consumption of energy and materials is reduced.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
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 carbon three liquid phase hydrogenation reactor control process according to one embodiment of the present invention;
FIG. 2 illustrates a functional block diagram of state feedback control according to one embodiment of the present invention;
FIG. 3 illustrates a functional block diagram of a carbon three liquid phase hydrogenation reactor control system according to an embodiment of the present invention;
FIG. 4 shows a schematic comparison of hydrogen distribution changes before and after commissioning of a carbon three liquid phase hydrogenation reactor control system according to an embodiment of the present invention;
FIG. 5 shows a graphical comparison of propylene selectivity before and after commissioning of a carbon three liquid phase hydrogenation reactor control system according to an embodiment of the present invention;
FIG. 6 shows a schematic of a prior art carbon three liquid phase hydrogenation unit process;
wherein, the reaction system comprises a 1-C3 hydrogenation reactor and a 2-condenser.
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 first embodiment is as follows:
as shown in fig. 1, a method for controlling a carbon three-liquid phase hydrogenation reactor comprises,
step S101: carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
the operational data is based on the user's operation of the hydrogenation reactor. The method specifically comprises the composition and content of materials before and after a carbon three-liquid phase hydrogenation reactor, the composition and content of the top of a depropanizer or the composition and content of the bottom of a deethanizer and the composition and content of a circulating carbon three material, and the content changes of the catalyst on-line operation time, the material flow, the reaction temperature, the pressure, hydrogen before and after the reaction, the carbon three composition, the carbon four composition, water and the like.
The classification statistics is that the numerical values and the trends of the composition and the content of each material are obtained based on the data of the composition and the content of the materials before and after the C-T liquid phase hydrogenation reactor, the composition and the content of the top of the depropanizer, or the composition and the content of the bottom of the deethanizer, and the composition and the content of the circulating C-T material after filtration.
And obtaining the catalytic performances of the catalyst, such as the operation life, the activity, the propylene selectivity, the MAPD conversion rate, the MAPD tolerance and the like, based on the online operation time, the material flow, the reaction temperature, the pressure, the hydrogen, the carbon three composition, the carbon four composition, the water and other content change data before and after the reaction.
Step S102: analyzing and fitting the classified statistical data to obtain analysis fitting data, wherein the analysis fitting is based on an optimization mode, an operation rule set and the obtained real-time operation data analysis fitting of the carbon three liquid phase hydrogenation catalyst;
step S103: establishing a state space model based on the characteristics of the carbon three liquid phase hydrogenation catalyst;
step S104: obtaining control parameters based on the state space model and the analysis fitting data;
step S105: obtaining gain scheduling data based on the analysis fitting data;
step S106: and generating a control instruction based on the control parameter and the gain scheduling data.
Optionally, the method further includes modifying the state space model based on the acquired real-time operation data.
Before analyzing and fitting or correcting the state space model, the obtained real-time operation data is classified and counted. In particular, the state space model is corrected on line.
Optionally, the modifying the state space model based on the acquired real-time operation data is that:
and performing least square model correction on the state space model.
Optionally, the state space model is:
a linear time-varying space model of the reaction state of the carbon three liquid phase hydrogenation constructed based on the reaction process of the simulated carbon three liquid phase hydrogenation catalyst;
the parameters for constructing the state linear time-varying space model comprise:
the method comprises the following steps of measuring the temperature of different positions and outlets of a catalyst bed layer in a hydrogenation reactor, the hydrogen flow, the inlet temperature and the circulating material flow of the hydrogenation reactor, the MAPD concentration, the propylene selectivity, the reaction activity and the MAPD conversion rate at the outlet of the hydrogenation reactor, the hydrogen concentration, the carbon-carbon three feeding quantity and the reaction pressure at the inlet of the hydrogenation reactor, and time-varying model parameters of the catalyst deactivation characteristics.
The state linear time-varying space model specifically comprises the following steps:
wherein,
for the state vector, PV1(k), PV2(k), PV3(k) and PV4(k) are respectively the upper, middle, lower and outlet temperatures of the catalyst bed in the carbon-three hydrogenation reactor;
MV1(k), MV2(k) and MV3(k) are the hydrogen flow, reactor inlet temperature and recycle stream flow, respectively, as the manipulated variables;
CV1(k), CV2(k), CV3(k) and CV4(k) are reactor outlet MAPD concentration, propylene selectivity, reactivity and MAPD conversion, respectively, as output variables;
DV1(k), DV2(k), and DV3(k) are inlet hydrogen concentration, carbon three feed rate, and reaction pressure, respectively, as disturbance variables; a, (t), B, (t), C (t), D (t), E (t), F (t) are all time-varying model parameters of catalyst deactivation characteristics.
Optionally, the propylene selectivity calculation formula is:
the calculation formula of the reactivity is as follows:
the calculation formula of the MAPD conversion rate is as follows:
optionally, in the generating of the control instruction based on the control parameter and the gain scheduling data,
as shown in fig. 2, a state feedback Control structure is adopted, and a feedback Control rate K (u ═ KX) is solved by Minimum Covariance constraint Control MVC3(Minimum Variance Covariance Constrained Control), so as to enable an index
Minimum;
wherein r isj、qiWeight values, Σ, representing the system input and output variances, respectivelyyiSum ΣujRespectively, the system steady state output and input covariance matrix sigmaySum ΣuThe ith, j element on the diagonal of (1).
Optionally, the optimization mode of the carbon three liquid phase hydrogenation catalyst comprises:
a catalyst initial operation control mode, a catalyst final operation control mode, a catalyst stabilization period operation control model, a high MAPD conversion rate control mode, an outlet MAPD concentration pilot control mode, a propylene selectivity pilot control mode and the like.
Optionally, the carbon three liquid phase hydrogenation catalyst comprises a carrier, and a main active component and a cocatalyst component loaded on the carrier;
the main active component is at least one selected from Pd, Ni, Pt, Rh and Ru; the content of the main active component is preferably 0.05-0.8 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the cocatalyst component is selected from at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, a halogen family system, an alkali metal family system and an alkaline earth metal family system; the content of the cocatalyst is preferably 0.01-1.0 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the carrier of the carbon three-liquid phase hydrogenation catalyst is at least one selected from alumina, molecular sieve, silica, gallium oxide, titanium oxide and activated carbon.
Example two:
as shown in fig. 3, a carbon three liquid phase hydrogenation reactor control system comprises: the system comprises a state space model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluating module, a controller module and an online correction module;
the state space model module is used for establishing a state space model based on the characteristics of the carbon three-liquid phase hydrogenation catalyst and obtaining control parameters based on the state space model and the analysis fitting data;
the expert knowledge base module is used for analyzing and fitting the classified statistical data to obtain analysis fitting data, and the analysis fitting is analysis fitting based on an optimization mode, an operation rule set and the obtained real-time operation data of the carbon three liquid phase hydrogenation catalyst;
the gain scheduling module is used for acquiring gain scheduling data based on the analysis fitting data;
the soft measurement module and the analysis and evaluation module are used for carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
the controller module is used for generating a control instruction based on the control parameter and the gain scheduling data;
and the online correction module is used for correcting the state space model based on the acquired real-time operation data.
Optionally, the real-time operation data is classified and counted by the soft measurement module and the analysis and evaluation module, and then is output to the expert knowledge base module and the online correction module.
In this embodiment, the design of iterative learning control software is implemented using C # language. The software comprises a data acquisition part, a data storage and learning control algorithm part. The control system software uses OPC technology to communicate with the DCS system of the carbon hydrogenation reactor, reads real-time process variable data and realizes the optimized control of the carbon hydrogenation reactor through writing operation. The data storage section is capable of storing history data.
The control system of the carbon-three-liquid phase hydrogenation reactor is positioned in a server connected with a Distributed Control System (DCS) of the carbon-three-liquid phase hydrogenation reactor. The controller module is positioned at the bottom layer of a control system of the carbon-liquid phase hydrogenation reactor, is connected with the DCS through an OPC Server and directly issues an optimization control signal and a command to the DCS; the gain scheduling module is also positioned at the bottom layer of the control system of the carbon-liquid phase hydrogenation reactor and provides the gain and the frequency of each adjusting parameter for the controller module; the state space model module and the online correction module are positioned in the middle layer of the carbon-liquid phase hydrogenation reactor control system, wherein the state space model module provides main optimized control parameters for the bottom layer controller module through model calculation solution; the online correction module corrects the calculation method in the state space model module according to the trend of the running data; the expert knowledge base module, the soft measurement module and the analysis and evaluation module are all positioned at the top layer of the control system of the carbon-liquid phase hydrogenation reactor, and the expert knowledge base module optimizes and adjusts the state space model module and the gain scheduling module by combining the operation data trend and the catalyst performance state value provided by the soft measurement and analysis and evaluation module.
The carbon three-liquid phase hydrogenation reactor control system monitors the composition and content of materials before and after the carbon three-liquid phase hydrogenation reactor, the composition and content of the top of a depropanizer or the composition and content of the bottom of a deethanizer and the composition and content of the circulating carbon three-material in real time, and the real-time data are filtered and input into a soft measurement model to obtain the numerical values and trends of the composition and content of each material.
The control system of the carbon-three-liquid phase hydrogenation reactor monitors the online operation time of the catalyst, the material flow, the reaction temperature, the pressure, the content changes of hydrogen, carbon-three composition, carbon-four composition, water and the like before and after reaction in real time, and inputs the real-time data into an analysis and evaluation model to obtain the catalytic performances of the catalyst, such as the operation life, the activity, the propylene selectivity, the MAPD conversion rate, the MAPD tolerance and the like.
The expert knowledge base module adopts a carbon three liquid phase hydrogenation catalyst optimization mode and an operation rule set, data after fitting with real-time operation data are output to the state space model module and the gain scheduling module,
in a specific application scenario, the method for controlling a carbon three liquid phase hydrogenation reactor is applied to a carbon three liquid phase hydrogenation reaction control unit of the olefin plant: the control system of the carbon-three liquid phase hydrogenation reactor is connected with a DCS through an OPC Server, each process condition is optimized and adjusted, and the adjustment target is provided for the DCS in real time, so that the automatic control of the carbon-three hydrogenation reactor is realized.
FIG. 4 shows a comparison of the hydrogen distribution of the hydrocarbon three-hydrogenation reactor before and after the automatic control system is put into operation. Before the control system is put into use, the hydrogen distribution amount is 1373NM3/hr (the fluctuation range is-13.6% -18.2%); after the control system is put into operation, the hydrogen distribution amount is 1291NM3/hr (the fluctuation amplitude is +/-11.4%), and the hydrogen distribution amount and the fluctuation amplitude are obviously reduced compared with the prior art. The control system has good effect on optimizing hydrogen distribution.
FIG. 5 is a graph showing a comparison of the propylene selectivity before and after the system was dosed. The use of the carbon three liquid phase hydrogenation reactor control system significantly improves propylene selectivity. Under the conditions of the same reactor, catalyst, feed composition and the like, an automatic control system is introduced, so that the average propylene selectivity can be improved from 53.5 percent before the dosage to 72.9 percent after the dosage, the selectivity is improved by 19.4 percent, and the synergistic effect is very obvious.
Comparative example:
in the prior art, olefin plants producing 80 million tons of ethylene every year share 15 cracking furnaces, and can process various cracking raw materials from ethane to hydrogenation tail oil and the like, and 40 million tons of propylene are produced every year. The separation process of the plant adopts a sequential separation flow, a C-III hydrogenation reactor is positioned between a hot zone depropanizing tower and a propylene rectifying tower, C-III fraction obtained from the top of a high-pressure depropanizing tower is subjected to heat exchange by a cooler (or a preheater) to reach a required temperature, is subjected to pressure rise by a feed pump, enters the hydrogenation reactor through a raw material dearsenizer, is mixed with hydrogen in a pipeline, and enters a reactor catalytic bed layer for selective hydrogenation reaction, and the C-III hydrogenation process of the plant is a liquid phase hydrogenation process, as shown in figure 6. The normal operation of the carbon-liquid phase hydrogenation reactor of the plant is manually adjusted.
The comparison results show that: compared with the manual control of the original factory, the automatic control modeling method obviously improves the yield of propylene and reduces the consumption of hydrogen.
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 (11)
1. A control method for a carbon three-liquid phase hydrogenation reactor is characterized by comprising the following steps:
carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
analyzing and fitting the classified statistical data to obtain analysis fitting data, wherein the analysis fitting is based on an optimization mode, an operation rule set and the obtained real-time operation data analysis fitting of the carbon three liquid phase hydrogenation catalyst;
establishing a state space model based on the characteristics of the carbon three liquid phase hydrogenation catalyst;
obtaining control parameters based on the state space model and the analysis fitting data;
obtaining gain scheduling data based on the analysis fitting data;
and generating a control instruction based on the control parameter and the gain scheduling data.
2. The carbon three liquid phase hydrogenation reactor control method of claim 1, further comprising: and correcting the state space model based on the acquired real-time operation data.
3. The carbon three liquid phase hydrogenation reactor control method of claim 2, wherein said modifying said state space model based on said obtained real time operational data is:
and performing least square model correction on the state space model.
4. The carbon three liquid phase hydrogenation reactor control method of claim 1, wherein the state space model is:
a linear time-varying space model of the reaction state of the carbon three liquid phase hydrogenation constructed based on the reaction process of the simulated carbon three liquid phase hydrogenation catalyst;
the parameters for constructing the state linear time-varying space model comprise:
the method comprises the following steps of measuring the temperature of different positions and outlets of a catalyst bed layer in a hydrogenation reactor, the hydrogen flow, the inlet temperature and the circulating material flow of the hydrogenation reactor, the MAPD concentration at the outlet of the hydrogenation reactor, the propylene selectivity, the reaction activity, the MAPD conversion rate, the hydrogen concentration at the inlet of the hydrogenation reactor, the carbon-three feeding amount, the reaction pressure and time-varying model parameters of the catalyst deactivation characteristics.
5. The carbon three-liquid phase hydrogenation reactor control method according to claim 4, wherein the reaction state linear time-varying spatial model is:
wherein,
the PV1(k), PV2(k), PV3(k) and PV4(k) are respectively the temperature of the upper part, the middle part, the lower part and the outlet of a catalyst bed layer in the carbon-three hydrogenation reactor;
MV1(k), MV2(k) and MV3(k) are the hydrogen flow, reactor inlet temperature and recycle stream flow, respectively, as the manipulated variables;
CV1(k), CV2(k), CV3(k) and CV4(k) are reactor outlet MAPD concentration, propylene selectivity, reactivity and MAPD conversion, respectively, as output variables;
DV1(k), DV2(k), and DV3(k) are inlet hydrogen concentration, carbon three feed rate, and reaction pressure, respectively, as disturbance variables; a, (t), B, (t), C (t), D (t), E (t), F (t) are all time-varying model parameters of catalyst deactivation characteristics.
6. The carbon three liquid phase hydrogenation reactor control method as recited in claim 4, wherein the propylene selectivity calculation formula is:
and/or the presence of a gas in the gas,
the calculation formula of the reactivity is as follows:
and/or the presence of a gas in the gas,
the calculation formula of the MAPD conversion rate is as follows:
7. the carbon three liquid phase hydrogenation reactor control method of claim 1, wherein in said generating control commands based on said control parameters and gain scheduling data,
adopting a state feedback control structure, solving a feedback control rate K (u is KX) by controlling MVC3 through minimum covariance constraint, and enabling an index
Minimum;
wherein r isj、qiWeight values, Σ, representing the system input and output variances, respectivelyyiSum ΣujRespectively, the system steady state output and input covariance matrix sigmaySum ΣuThe ith, j element on the diagonal of (1).
8. The carbon three liquid phase hydrogenation reactor control method as recited in claim 1, wherein the optimization mode of the carbon three liquid phase hydrogenation catalyst comprises:
the control method comprises a catalyst initial-stage operation control mode, a catalyst final-stage operation control mode, a catalyst stabilization-stage operation control model, a high MAPD conversion rate control mode, an outlet MAPD concentration pilot control mode or a propylene selectivity pilot control mode.
9. The carbon three liquid phase hydrogenation reactor control method as recited in claim 1, wherein the carbon three liquid phase hydrogenation catalyst comprises a carrier and a main active component and a cocatalyst component loaded thereon;
the main active component is at least one selected from Pd, Ni, Pt, Rh and Ru; the content of the main active component is preferably 0.05-0.8 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the cocatalyst component is selected from at least one of Ag, Cu, Au, La, Ce, Ga, Pb, W, Mo, a halogen family system, an alkali metal family system and an alkaline earth metal family system; the content of the cocatalyst is preferably 0.01-1.0 wt% based on the weight of the carbon three liquid phase hydrogenation catalyst;
the carrier of the carbon three-liquid phase hydrogenation catalyst is at least one selected from alumina, molecular sieve, silica, gallium oxide, titanium oxide and activated carbon.
10. A carbon three liquid phase hydrogenation reactor control system, comprising: the system comprises a state space model module, an expert knowledge base module, a gain scheduling module, a soft measurement module, an analysis evaluating module, a controller module and an online correction module;
the state space model module is used for establishing a state space model based on the characteristics of the carbon three-liquid phase hydrogenation catalyst and obtaining control parameters based on the state space model and the analysis fitting data;
the expert knowledge base module is used for analyzing and fitting the classified statistical data to obtain analysis fitting data, and the analysis fitting is analysis fitting based on an optimization mode, an operation rule set and the obtained real-time operation data of the carbon three liquid phase hydrogenation catalyst;
the gain scheduling module is used for acquiring gain scheduling data based on the analysis fitting data;
the soft measurement module and the analysis and evaluation module are used for carrying out classified statistics on the operation data of the hydrogenation reactor to obtain classified statistical data;
the controller module is used for generating a control instruction based on the control parameter and the gain scheduling data;
and the online correction module is used for correcting the state space model based on the acquired real-time operation data.
11. The carbon three liquid phase hydrogenation reactor control system of claim 10, wherein the real-time operation data is classified and counted by the soft measurement module and the analysis and evaluation module, and then output to the expert knowledge base module and the online correction module.
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