CN110658797B - Optimization control method of hydrogen chloride synthesis furnace system - Google Patents

Optimization control method of hydrogen chloride synthesis furnace system Download PDF

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CN110658797B
CN110658797B CN201911030200.0A CN201911030200A CN110658797B CN 110658797 B CN110658797 B CN 110658797B CN 201911030200 A CN201911030200 A CN 201911030200A CN 110658797 B CN110658797 B CN 110658797B
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hydrogen
chlorine
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hydrogen chloride
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CN110658797A (en
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彭辉
李雯
张海峰
付雷
方知涵
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Central South University
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    • G—PHYSICS
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    • G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
    • G05B19/00—Programme-control systems
    • G05B19/02—Programme-control systems electric
    • G05B19/418—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS], computer integrated manufacturing [CIM]
    • G05B19/41865—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS], computer integrated manufacturing [CIM] characterised by job scheduling, process planning, material flow
    • G—PHYSICS
    • G05—CONTROLLING; REGULATING
    • G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
    • G05B2219/00—Program-control systems
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    • Y02P90/02—Total factory control, e.g. smart factories, flexible manufacturing systems [FMS] or integrated manufacturing systems [IMS]

Abstract

The invention discloses an optimization control method of a hydrogen chloride synthesis furnace system, which aims at a chlorine hydrogen flow regulation control system which has a plurality of hydrogen chloride synthesis furnaces and can measure the gas flow at the inlet of the hydrogen chloride synthesis furnace and is based on the manual on-line hydrogen chloride purity measurement, the method considers the coupling condition of flow and pressure existing in the flow joint regulation of the plurality of synthesis furnaces, an outer ring adopts a flow distribution optimization strategy with chlorine-hydrogen ratio control and total flow constraint, the flow is distributed according to the chlorine-hydrogen ratio, the stability of the flow of a chlorine and hydrogen main buffer tank is ensured at the same time, and the set values of the hydrogen and chlorine flow are optimized on line for the plurality of synthesis furnaces; and a PID flow control strategy is adopted in the inner ring, and pressure feedforward compensation is introduced to improve the robustness of the system. The invention combines the flow distribution optimization strategy with the chlorine-hydrogen ratio control strategy and the PID flow control strategy with the pressure feedforward compensation strategy to realize the optimal control of a plurality of hydrogen chloride synthesizing furnace systems.

Description

Optimization control method of hydrogen chloride synthesis furnace system
Technical Field
The invention relates to the technical field of optimization strategies and automatic control, and relates to an optimization control method of a hydrogen chloride synthesis furnace system.
Background
Hydrogen chloride is one of the most basic raw materials in the chemical industry and is also an important raw material for synthesizing vinyl chloride, and is an upstream process for producing polyvinyl chloride. And the hydrogen from the hydrogen buffer tank and the chlorine from the chlorine buffer tank are combusted in the synthesis furnace to generate hydrogen chloride gas. The synthesis furnace is an important device for generating hydrogen chloride gas, and the proportion of hydrogen and chlorine at the inlet of the synthesis furnace is the key for influencing the purity of hydrogen chloride at the outlet of the synthesis furnace and determining whether the hydrogen chloride can be safely produced. When hydrogen and chlorine are in chemical reaction in a synthesis furnace, the excess chlorine can cause the explosion of the synthesis furnace or a gas transmission pipeline, the excess hydrogen can cause the problems of high energy consumption, low raw material utilization rate and the like, the hydrogen and chlorine proportioning of the synthesis furnace is accurately controlled, the raw material utilization rate is improved, and the production risk is reduced, so that the method is an urgent problem to be solved in the chlorine and hydrogen synthesis process in the chlor-alkali industry at home and abroad.
Due to the actual production requirements, when the chlorine or hydrogen flow of any synthesis furnace needs to be adjusted in the hydrogen chloride synthesis process, the judgment of field operation workers is mainly relied on, the workers adopt a manual control mode, the opening degree of a regulating valve of the gas flow is modified by a strategy of inductive trial adjustment, namely, the opening degree of a valve position is set on an operation interface of a control system to adjust the gas flow in a pipeline, and the next operation is determined by the flow change of a hydrogen and chlorine control object. When the chlorine or hydrogen flow of any synthesis furnace changes, due to the strong coupling among the gas supply loops of the synthesis furnaces, the disordered competition phenomenon occurs in the chlorine or hydrogen pipelines of different synthesis furnaces, and finally the long-period oscillation fluctuation of a control system is caused, thereby having adverse effects on the overall stability of the system and the quality of the hydrogen chloride gas.
Every synthesizer hydrogen and chlorine gas flow in the current chlor-alkali workshop synthesis process are mainly manual regulation, realize through the mode that sets up the valve aperture promptly, in order to guarantee the hydrogen chloride purity in the safety in production, adopt the ratio control strategy between hydrogen flow and the chlorine gas flow, nevertheless because the fluctuation of chlorine buffer tank and hydrogen buffer tank and house steward pressure, every synthesizer receives the influence of parallel line flow and pressure fluctuation, lead to the unable effective operation of ratio control, and then lead to the fluctuation problem of chlorine gas flow and the actual ratio of hydrogen gas flow in the hydrogen chloride synthesis process. The research on the optimization control technology of the chlorine flow and the hydrogen flow of a plurality of synthesis furnaces has important theoretical significance and urgent practical needs.
Disclosure of Invention
The invention aims to solve the technical problem that the prior art is insufficient, and provides an optimal control method of a hydrogen chloride synthesis furnace system, which can more quickly and accurately realize the control of a plurality of hydrogen chloride synthesis furnace systems.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: an optimized control method of a hydrogen chloride synthesis furnace system comprises the following steps:
1. the hydrogen buffer tank and the chlorine buffer tank simultaneously provide hydrogen and chlorine for a plurality of synthesis furnaces, each synthesis furnace is provided with two inlets, an electric regulating valve is arranged in front of each inlet, and a gas flow detector is arranged behind each valve;
2. setting parameters such as the total number of the synthetic furnace, the expected hydrogen chloride purity value at the outlet of the synthetic furnace, the total hydrogen chloride yield and the like in an upper computer;
3. the upper computer is used for measuring the purity value of the hydrogen chloride on line based on measurable flow information of the inlet of the hydrogen chloride synthesis furnace and manual work of each synthesis furnace according to set parameters, and optimizing set values of hydrogen flow and chlorine flow for each synthesis furnace on line under the condition of ensuring small-range change of the flow of the hydrogen and chlorine total buffer tanks so as to achieve that the actual purity of the hydrogen chloride at the outlet of each synthesis furnace reaches a desired value;
4. each synthesis furnace enters PID flow closed-loop control after obtaining set values of hydrogen and chlorine flow, the input of a controller is the error between a flow set value and an actual flow value, a control variable is the opening degree of a valve, and the measurable gas flow at the inlet of the hydrogen chloride synthesis furnace is used as a feedback signal;
5. the PID flow closed-loop control system of each synthesis furnace can be disturbed by the change of gas pressure, and the influence of the pressure disturbance of the pipeline on the flow is compensated by adopting feed-forward regulation;
6. the hydrogen and chlorine flow information detected by the flowmeter is not only fed back to the PID flow closed-loop system, but also serves as an input parameter to be transmitted to an optimization program of the upper computer, and the operation of 3) -6) is repeated after the upper computer obtains the hydrogen chloride purity information measured manually on line.
The number of the hydrogen chloride synthesis furnaces input in the step 2 determines the total flow of hydrogen and chlorine optimized by the upper computer, the expected hydrogen chloride purity value of the synthesis furnaces and the total hydrogen chloride yield of all the synthesis furnaces depend on the actual production process requirements, and the constraint range of the optimization program of the upper computer is influenced.
And 3, an optimization algorithm for online combined adjustment of the hydrogen and chlorine flow set values at the inlets of the plurality of hydrogen chloride synthesis furnaces comprises the following specific implementation steps:
1) determining the number of the synthesis furnaces as n in the upper computer, and calculating a formula according to the purity of the hydrogen chloride and the proportion of the hydrogen chloride
Figure BDA0002249926150000021
Wherein K is the ratio of the hydrogen flow to the chlorine flow, C is the purity of the hydrogen chloride, and the expected value of the purity of the hydrogen chloride of the synthesis furnace is converted into the expected ratio K of the hydrogen flow to the chlorine flowpTotal yield of ChCalculating the total flow of the hydrogen buffer tank as
Figure BDA0002249926150000031
The total flow rate of the chlorine buffer tank is
Figure BDA0002249926150000032
2) And collecting flow data of hydrogen and chlorine at the inlet of each synthesis furnace and the manually tested hydrogen chloride purity data. The detected flow data is Q1],Q[2],…Q[2n]Wherein Q < 1 >],Q[2]…Q[n]The hydrogen flow rate from the 1 st to the n th synthesis furnaces, Q [ n + 1%],Q[n+2],…Q[2n]The chlorine flow rate from the 1 st to the n-th synthesis furnaces. Calculating the ratio of the hydrogen and chlorine flows according to the data of the hydrogen and chlorine flows
Figure BDA0002249926150000033
Collecting the hydrogen chloride purity data measured manually on line, and converting the data into the ratio r of the hydrogen to chlorine flow of each synthesis furnace based on manual measurementp[i]，i＝1,2…,n；
3) Recording the adjustment quantity of hydrogen and chlorine flow of each synthesis furnace as x [1], x [2], … x [2n ], and establishing an objective function of the flow joint distribution optimization of a plurality of synthesis furnaces:
f(x)＝kg(x)+(1-k)h(x)
wherein the content of the first and second substances,
Figure BDA0002249926150000034
Figure BDA0002249926150000035
；
k is an adjustable weight value, g (x) is the square sum of the adjustment quantity of the hydrogen and chlorine flow of each synthesis furnace, and h (x) is the square sum of the hydrogen flow difference and the chlorine flow difference of every two synthesis furnaces in n synthesis furnaces.
4) The total flow of the hydrogen buffer tank and the total flow of the chlorine buffer tank are required to be changed only in a small range, so that the total flow of the hydrogen and the total flow of the chlorine after being adjusted by an optimization algorithm should meet the following requirements:
Figure BDA0002249926150000036
wherein1And2the allowable variation of the total flow of hydrogen and the total flow of chlorine.
5) The hydrogen-chlorine ratio r is obtained according to manual on-line detectionp[i]Desired ratio k of flow of hydrogen and chlorinepAnd a hydrogen-hydrogen ratio r [ i ] obtained based on the detected flow rate value]And designing ratio constraint conditions in an optimization algorithm. The hydrogen-chlorine flow ratio adjustment quantity of each synthesis furnace is recorded as t [ i ]]Get it
Figure BDA0002249926150000041
The hydrogen-hydrogen ratio adjustment constraint of each synthesis furnace in the optimization algorithm is as follows:
Figure BDA0002249926150000042
wherein the content of the first and second substances,
Figure BDA0002249926150000043
in the above formula, β is an adjustable control strength parameter, and α is a small offset.
6) Setting the lower and upper limits of hydrogen flow and chlorine flow at the inlet of each synthesis furnace, and setting the lower limit of the hydrogen flow asHUpper bound of
Figure BDA0002249926150000044
The lower bound of the chlorine flow isLUpper bound of
Figure BDA0002249926150000045
The optimized flow set point must satisfy the following conditions:
Figure BDA0002249926150000046
7) obtaining the objective function of the optimized flow setting of the multiple synthesis furnaces according to the steps 4), 5) and 6) and meeting the following constraint conditions:
Figure BDA0002249926150000051
8) solving the following parameter optimization problem according to the objective function in the step 3) and the constraint condition in the step 7)
Figure BDA0002249926150000052
Figure BDA0002249926150000053
Obtaining the optimal adjustment x 1 of hydrogen and chlorine flow of all synthesis furnaces]～x[2n]And outputting the set values Q of the hydrogen and chlorine flow rates of all the synthesis furnacest[1]～Qt[2n]The hydrogen flow rate set value is: qt[i]＝Q[i]+x[i]I is 1,2 …, n, the chlorine flow set point is: qt[i+n]＝Q[i+n]+x[i+n]，i＝1,2…,n。
Step 4, adopting a PID closed-loop control strategy, wherein the hydrogen flow closed-loop control strategy is the same as the chlorine flow control strategy, taking hydrogen as an example, and the hydrogen flow set value of each synthesis furnace is Qt[i]The hydrogen flow value detected by the flowmeter is Q [ i ]]Deviation is e [ i]＝Qt[i]-Q[i]The controlled quantity is the valve opening u [ i ]]Obtained according to the PID control principleThe valve opening is:
Figure BDA0002249926150000061
and 5, pressure feedforward compensation control in step 5. A first-order inertia plus pure hysteresis model is established through the valve and flow characteristics, and the transfer function is as follows:
Figure BDA0002249926150000062
K0is a proportionality coefficient, θ0For pure lag time, τ0Is the time constant of inertia. The pressure fluctuation is used as disturbance quantity, a first-order inertia plus pure hysteresis model is established according to the corresponding flow variation quantity, and the transfer function is as follows:
Figure BDA0002249926150000063
K1is a proportionality coefficient, θ0For pure lag time, τ0Is an inertia time constant, represented by G0(s) and G1(s) obtaining a feedforward compensation controller Gn(s)：
Figure BDA0002249926150000064
The parameters in the controller may be estimated from the actual sampled data.
Compared with the prior art, the invention has the beneficial effects that: the invention considers the coupling condition of flow and pressure existing in the flow combined regulation of a plurality of synthesis furnaces, the outer ring adopts a flow distribution optimization strategy with chlorine-hydrogen ratio control and total flow constraint, the flow is distributed according to the chlorine-hydrogen ratio, the stability of the flow of the chlorine and hydrogen total buffer tank is ensured at the same time, and the set values of the flow of the hydrogen and the chlorine are optimized for the plurality of synthesis furnaces on line; and a PID flow control strategy is adopted in the inner ring, and pressure feedforward compensation is introduced to improve the robustness of the system. The invention combines the flow distribution optimization strategy with the chlorine-hydrogen ratio control strategy and combines the PID flow control strategy with the pressure feedforward compensation strategy to realize the control of a plurality of hydrogen chloride synthesizing furnace systems more quickly and accurately.
Drawings
FIG. 1 is a block diagram of a hydrogen and chlorine flow distribution system for a synthesis furnace;
FIG. 2 is a schematic diagram of the hydrogen chloride optimization control system of the present invention.
Detailed Description
Fig. 1 shows a structure diagram of a hydrogen-chlorine flow distribution system of a synthesis furnace, the system mainly comprises 1 hydrogen buffer tank, 1 chlorine buffer tank, 2 pressure gauges, 16 valves, 16 flow meters, 8 synthesis furnaces and the like, and the pressure of the buffer tanks is kept stable in the flow regulation process. In the schematic diagram of the hydrogen chloride optimization control system shown in fig. 2, the upper computer needs to receive the collected hydrogen chloride purity information and the inlet flow information displayed by the actual flow detector, and then the upper computer is set to 16 loop output flow set values and enters the closed-loop control of each flow loop. The specific working flow comprises the following steps:
1. the hydrogen buffer tank and the chlorine buffer tank simultaneously provide hydrogen and chlorine for a plurality of synthesis furnaces, each synthesis furnace is provided with two inlets, an electric regulating valve is arranged in front of each inlet, and a gas flow detector is arranged behind each valve;
2. setting parameters such as the total number of the synthetic furnace, the expected hydrogen chloride purity value at the outlet of the synthetic furnace, the total hydrogen chloride yield and the like in an upper computer;
3. the upper computer is used for measuring the purity value of the hydrogen chloride on line based on measurable flow information of the inlet of the hydrogen chloride synthesis furnace and manual work of each synthesis furnace according to set parameters, and optimizing set values of hydrogen flow and chlorine flow for each synthesis furnace on line under the condition of ensuring small-range change of the flow of the hydrogen and chlorine total buffer tanks so as to achieve that the actual purity of the hydrogen chloride at the outlet of each synthesis furnace reaches a desired value;
4. each synthesis furnace enters PID flow closed-loop control after obtaining set values of hydrogen and chlorine flow, the input of a controller is the error between a flow set value and an actual flow value, a control variable is the opening degree of a valve, and the measurable gas flow at the inlet of the hydrogen chloride synthesis furnace is used as a feedback signal;
5. the PID flow closed-loop control system of each synthesis furnace can be disturbed by the change of gas pressure, and the influence of the pressure disturbance of the pipeline on the flow is compensated by adopting feed-forward regulation;
6. the hydrogen and chlorine flow information detected by the flowmeter is not only fed back to the PID flow closed-loop system, but also serves as an input parameter to be transmitted to an optimization program of the upper computer, and the operation of 3-6 times is repeated after the upper computer obtains the hydrogen chloride purity information measured manually on line.
The number of the hydrogen chloride synthesis furnaces input in the step 2 determines the total flow of hydrogen and chlorine optimized by the upper computer, the expected hydrogen chloride purity value of the synthesis furnaces and the total hydrogen chloride yield of all the synthesis furnaces depend on the actual production process requirements, and the constraint range of the optimization program of the upper computer is influenced.
And 3, an optimization algorithm for online combined adjustment of the hydrogen and chlorine flow set values at the inlets of the plurality of hydrogen chloride synthesis furnaces comprises the following specific implementation steps:
1) determining the number of synthesis furnaces to be 8 in the upper computer, and calculating a formula according to the purity of the hydrogen chloride and the proportion of the hydrogen chloride
Figure BDA0002249926150000071
Wherein K is the ratio of the hydrogen flow to the chlorine flow, C is the purity of the hydrogen chloride, and the expected value of the purity of the hydrogen chloride of the synthesis furnace is converted into the expected ratio K of the hydrogen flow to the chlorine flowpTotal yield of ChCalculating the total flow of the hydrogen buffer tank as
Figure BDA0002249926150000081
The total flow rate of the chlorine buffer tank is
Figure BDA0002249926150000082
2) And collecting flow data of hydrogen and chlorine at the inlet of each synthesis furnace and the manually tested hydrogen chloride purity data. The detected flow data is Q1],Q[2],…Q[16]Wherein Q < 1 >],Q[2]…Q[8]The hydrogen flow rate of the 1 st to 8 th synthesis furnaces, Q9],Q[10],…Q[16]The chlorine flow rate of the 1 st to 8 th synthesis furnaces. Calculating the flow rates of hydrogen and chlorine according to the flow rate data of hydrogen and chlorineRatio of
Figure BDA0002249926150000083
Collecting the hydrogen chloride purity data measured manually on line, and converting the data into the ratio r of the hydrogen to chlorine flow of each synthesis furnace based on manual measurementp[i]，i＝1,2…,8；
3) Recording the adjustment quantity of hydrogen and chlorine flow of each synthesis furnace as x [1], x [2], … x [16], and establishing an objective function of the flow joint distribution optimization of a plurality of synthesis furnaces:
f(x)＝kg(x)+(1-k)h(x)
wherein the content of the first and second substances,
Figure BDA0002249926150000084
Figure BDA0002249926150000085
；
k is an adjustable weight value, g (x) is the square sum of the adjustment quantity of the hydrogen and chlorine flow of each synthesis furnace, and h (x) is the square sum of the hydrogen flow difference and the chlorine flow difference of every two synthesis furnaces in 8 synthesis furnaces.
4) The total flow of the hydrogen buffer tank and the total flow of the chlorine buffer tank are required to be changed only in a small range, so that the total flow of the hydrogen and the total flow of the chlorine after being adjusted by an optimization algorithm should meet the following requirements:
Figure BDA0002249926150000086
wherein1And2the allowable variation of the total flow of hydrogen and the total flow of chlorine.
5) The hydrogen-chlorine ratio r is obtained according to manual on-line detectionp[i]Desired ratio k of flow of hydrogen and chlorinepAnd a hydrogen-hydrogen ratio r [ i ] obtained based on the detected flow rate value]And designing ratio constraint conditions in an optimization algorithm. The hydrogen-chlorine flow ratio adjustment quantity of each synthesis furnace is recorded as t [ i ]]Get it
Figure BDA0002249926150000091
The hydrogen-hydrogen ratio adjustment constraint of each synthesis furnace in the optimization algorithm is as follows:
Figure BDA0002249926150000092
wherein the content of the first and second substances,
Figure BDA0002249926150000093
in the above formula, β is an adjustable control strength parameter, and α is a small offset.
6) Setting the lower and upper limits of hydrogen flow and chlorine flow at the inlet of each synthesis furnace, and setting the lower limit of the hydrogen flow asHUpper bound of
Figure BDA0002249926150000094
The lower bound of the chlorine flow isLUpper bound of
Figure BDA0002249926150000095
The optimized flow set point must satisfy the following conditions:
Figure BDA0002249926150000096
7) obtaining the objective function of the optimized flow setting of the multiple synthesis furnaces according to the steps 4), 5) and 6) and meeting the following constraint conditions:
Figure BDA0002249926150000101
8) solving the following parameter optimization problem according to the objective function in the step 3) and the constraint condition in the step 7):
Figure BDA0002249926150000102
Figure BDA0002249926150000103
obtaining the optimal adjustment x 1 of hydrogen and chlorine flow of all synthesis furnaces]～x[16]And outputting the set values Q of the hydrogen and chlorine flow rates of all the synthesis furnacest[1]～Qt[16]The hydrogen flow rate set value is: qt[i]＝Q[i]+x[i]I is 1,2 …,8, the chlorine flow set point is: qt[i+8]＝Q[i+8]+x[i+8]，i＝1,2…,8。
Step 4, adopting a PID closed-loop control strategy, wherein the hydrogen flow closed-loop control strategy is the same as the chlorine flow control strategy, taking hydrogen as an example, and the hydrogen flow set value of each synthesis furnace is Qt[i]The hydrogen flow value detected by the flowmeter is Q [ i ]]Deviation is e [ i]＝Qt[i]-Q[i]The controlled quantity is the valve opening u [ i ]]According to the PID control principle, the valve opening can be obtained as follows:
Figure BDA0002249926150000111
and 5, pressure feedforward compensation control in step 5. A first-order inertia plus pure hysteresis model is established through the valve and flow characteristics, and the transfer function is as follows:
Figure BDA0002249926150000112
K0is a proportionality coefficient, θ0For pure lag time, τ0Is the time constant of inertia. The pressure fluctuation is used as disturbance quantity, a first-order inertia plus pure hysteresis model is established according to the corresponding flow variation quantity, and the transfer function is as follows:
Figure BDA0002249926150000113
K1is a proportionality coefficient, θ0For pure lag time, τ0Is an inertia time constant, represented by G0(s) and G1(s) obtaining feedforward compensation controlSystem ware Gn(s)：
Figure BDA0002249926150000114
The parameters in the controller may be estimated from the actual sampled data.

Claims (4)

1. An optimal control method of a hydrogen chloride synthesis furnace system is characterized by comprising the following steps:
1) setting the total number of the synthetic furnace, the expected purity value of the hydrogen chloride at the outlet of the synthetic furnace and the total yield of the hydrogen chloride;
2) according to the parameters set in the step 1), based on the measurable flow information of the hydrogen chloride synthesis furnace inlet and the manual online hydrogen chloride purity measurement of each synthesis furnace, the flow of the hydrogen total buffer tank and the flow of the chlorine total buffer tank are ensured to be in1And2under the condition of change in the range, the set values of the hydrogen flow and the chlorine flow are optimized for each synthesis furnace on line, so that the actual purity of the hydrogen chloride at the outlet of each synthesis furnace reaches the expected value; wherein1And2are all percentage numbers;
3) each synthesis furnace enters PID flow closed-loop control after obtaining set values of hydrogen and chlorine flow, and the influence of pipeline pressure disturbance on the flow is compensated by adopting feedforward regulation aiming at the problem that a PID flow closed-loop control system is subjected to pipeline pressure fluctuation, an input signal of the PID flow closed-loop control system is an error between a flow set value and an actual flow value, a control variable is a valve opening degree, a valve opening degree signal enables an inlet of the hydrogen chloride synthesis furnace to obtain corresponding gas flow, and the measurable gas flow at the inlet of the hydrogen chloride synthesis furnace is used as a feedback signal of the PID control system;
4) the gas flow at the inlet of the hydrogen chloride synthesis furnace is simultaneously used as one input signal of an upper computer, and the steps 2) to 4) are repeated when the upper computer obtains the hydrogen chloride purity information manually measured on line, namely a second input signal is obtained;
wherein, in the step 2), the following parameter optimization problem is solved to obtain the optimal adjustment quantity x 1 of the hydrogen and chlorine flow of all the synthesis furnaces]～x[2n]And output all the combinationsSet value Q of flow of hydrogen and chlorine in forming furnacet[1]～Qt[2n]：
Figure FDA0002675494440000021
Figure FDA0002675494440000022
Wherein the content of the first and second substances,Hthe lower limit of the hydrogen flow of a single synthesis furnace,
Figure FDA0002675494440000027
The upper limit of the hydrogen flow of a single synthesis furnace;Lthe lower limit of chlorine gas flow of a single synthesis furnace,
Figure FDA0002675494440000026
The upper limit of chlorine flow of a single synthesis furnace;1and2the allowable variation of the total flow of the hydrogen and the chlorine; k is an adjustable weight; chConverting the expected value of the purity of the hydrogen chloride of the synthesis furnace into the total yield of the hydrogen and chlorine flow; k is a radical ofpConverting the expected value of the purity of the hydrogen chloride of the synthesis furnace into an expected ratio of the flow of the hydrogen to the flow of the chlorine;
Figure FDA0002675494440000023
Q[1],Q[2]…Q[n]the hydrogen flow rate from the 1 st to the n th synthesis furnaces, Q [ n + 1%],Q[n+2],…Q[2n]Chlorine flow from the 1 st synthesis furnace to the nth synthesis furnace;
Figure FDA0002675494440000024
Figure FDA0002675494440000025
beta is more than 0 and less than 1, and alpha is more than 0; beta is a control intensity parameter, and alpha is an offset; set value Q of hydrogen gas flow ratet[i]＝Q[i]+x[i](ii) a Set value Q of chlorine flowt[i+n]＝Q[i+n]+x[i+n](ii) a g (x) is the square sum of the adjusted quantities of the hydrogen and chlorine flow rates of each synthesis furnace, and h (x) is the square sum of the difference of the hydrogen flow rates and the chlorine flow rate of every two synthesis furnaces of the n synthesis furnaces.
2. The optimal control method of a hydrogen chloride synthesis furnace system according to claim 1, wherein the parameter optimization problem formula obtaining process includes:
1) determining n synthesis furnaces in the upper computer, and according to the relational expression of the hydrogen chloride purity C and the hydrogen chloride ratio K
Figure FDA0002675494440000031
Converting the expected value of the purity of the hydrogen chloride of the synthesis furnace into the expected ratio k of the hydrogen to the chlorine flowpTotal yield of ChCalculating the total flow of the hydrogen buffer tank as
Figure FDA0002675494440000032
The total flow rate of the chlorine buffer tank is
Figure FDA0002675494440000033
2) Collecting flow data Q1 of hydrogen and chlorine at each synthetic furnace inlet],Q[2],…Q[2n]And calculating the ratio of hydrogen to chlorine flow rates based thereon
Figure FDA0002675494440000034
Collecting the hydrogen chloride purity data measured manually on line, and converting the data into the ratio r of the hydrogen to chlorine flow of each synthesis furnace based on manual measurementp[i]；
3) Recording the adjustment quantity of hydrogen and chlorine flow of each synthesis furnace as x [1], x [2], … x [2n ], and establishing an objective function of the flow joint distribution optimization of a plurality of synthesis furnaces: (x) kg (x) + (1-k) h (x); wherein the content of the first and second substances,
Figure FDA0002675494440000035
Figure FDA0002675494440000036
4) the total flow of hydrogen and the total flow of chlorine after being adjusted by the optimization algorithm meet the following requirements:
Figure FDA0002675494440000037
5) the hydrogen-chlorine ratio r is obtained according to manual on-line detectionp[i]Desired ratio k of flow of hydrogen and chlorinepAnd a hydrogen-hydrogen ratio r [ i ] obtained based on the detected flow rate value]Designing ratio constraint conditions in an optimization algorithm, and recording the hydrogen-hydrogen flow ratio adjustment quantity of each synthesis furnace as t [ i [ ]]Get it
Figure FDA0002675494440000038
6) Setting the lower and upper limits of hydrogen flow and chlorine flow at the inlet of each synthesis furnace, and setting the lower limit of the hydrogen flow asHUpper bound of
Figure FDA0002675494440000044
The lower bound of the chlorine flow isLUpper bound of
Figure FDA0002675494440000043
The optimized flow set value meets the following conditions:
Figure FDA0002675494440000041
7) obtaining the objective function of the optimized flow setting of the multiple synthesis furnaces according to the steps 4) to 6) and meeting the following constraint conditions:
Figure FDA0002675494440000042
8) obtaining the following parameter optimization problem according to the objective function in the step 3) and the constraint condition in the step 7):
Figure FDA0002675494440000051
Figure FDA0002675494440000052
3. the optimal control method for the hydrogen chloride synthesis furnace system according to claim 1, wherein in the step 3), the valve opening degree calculation formula is
Figure FDA0002675494440000053
Figure FDA0002675494440000054
Wherein the deviation e [ i ]]＝Qt[i]-Q[i]，Qt[i]Setting the hydrogen flow rate of each synthesis furnace; q [ i]Value of hydrogen flow, K, detected for the flowmeterpIs a proportionality coefficient, TiTo integrate the time constant, TdIs the differential time constant.
4. The optimal control method for the hydrogen chloride synthesis furnace system according to claim 1, wherein in the step 3), the compensation controller is adjusted in a feed-forward manner
Figure FDA0002675494440000055
Wherein the content of the first and second substances,
Figure FDA0002675494440000056
a transfer function of a first-order inertia plus pure hysteresis model established through the valve and flow characteristics;
Figure FDA0002675494440000057
to take pressure fluctuation as disturbance quantityThe transfer function of a first-order inertia plus pure lag model is established according to the flow variation; k0、K1Is a proportionality coefficient, θ0、θ1For pure lag time, τ0、τ1Is the time constant of inertia.
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