CN114280936B - Cloud edge collaborative optimization intelligent management and control system for organic pollutant treatment - Google Patents
Cloud edge collaborative optimization intelligent management and control system for organic pollutant treatment Download PDFInfo
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Abstract
The application discloses an intelligent control system for cloud edge collaborative optimization for organic pollutant treatment. The method comprises the steps of providing a low-energy consumption dynamic process flow design for organic pollutant treatment at the edge side, and establishing a process steady-state model, a dynamic model and a control system design thereof by using flow simulation software; and creating an acrylic acid organic pollutant treatment optimization management and control APP module based on an industrial operation system at a central cloud end, wherein the APP module is used for visually monitoring, optimizing and controlling the treatment process of the organic pollutants. And the OPC Server software is used as a data transfer station to perform bidirectional data transmission between the edge side and the central cloud, so that bidirectional data transmission between the edge side dynamic model and the central cloud is realized, and the collaborative optimization control of data signals including dynamic simulation data, decision variable write-back, PID parameter setting, working condition emergency braking and the like is realized. The platform set up by the system can be used for optimizing the flow, simulating and early warning working conditions, training staff and remotely controlling.
Description
Technical Field
The application relates to the field of flow design simulation, multi-objective optimization and APP development of an industrial operation system, in particular to acrylic acid organic pollutant treatment process flow design, acrylic acid organic pollutant treatment optimization management and control APP development and cloud edge collaborative optimization management and control system establishment of acrylic acid organic pollutant treatment.
Background
With the high-speed development of industrial production, organic pollutants with difficult degradation property and high pollution are always difficult problems puzzling the chemical industry. The problem of treating organic pollutants is also widely paid attention to in the academic circles, and how to harmlessly treat the organic pollutants to reach the national emission standard becomes a problem to be solved in the field. Green production is always the industrial production mode pursued by professionals in the chemical industry field in the current age. The waste gas and wastewater generated in the production process of acrylic acid has higher concentration of organic matters, contains various organic matters such as acrylic acid, acetic acid, formaldehyde, acrolein, methyl acrylate, ethyl acrylate and the like, has complex components and higher toxicity, and makes the treatment of the acrylic acid and the ester wastewater very difficult. Networking and intellectualization are a new prospect in the current industrial field, and how to realize industrial operation automation, intelligent optimization, energy saving and consumption reduction and remote control becomes a real problem to be solved urgently.
Disclosure of Invention
The application provides a cloud edge collaborative optimization intelligent management and control system for organic pollutant treatment aiming at the technical problems.
The aim of the application can be achieved by the following technical scheme:
the cloud edge collaborative optimization intelligent management and control system for organic pollutant treatment comprises edge side organic pollutant aerobic cracking treatment flow design and dynamic model establishment, center cloud end organic pollutant treatment optimization management and control APP module creation and edge side and center cloud end data real-time transmission, and the system comprises the following specific processes:
(1) Aiming at the acrylic acid organic pollutant treatment process, adopting an oxygen-induced cracking treatment technology to carry out flow design of a heat exchanger, a fluidized bed reactor, a fixed bed reactor and a gas-liquid separator;
(2) Based on a reaction kinetic equation and the process flow design in the step (1), firstly constructing a steady-state model for treating the acrylic acid organic pollutants by using flow simulation software, then designing an acrylic acid organic pollutant control system by adopting a multivariable control method, and finally constructing a dynamic model for treating the acrylic acid organic pollutants at the edge side by using the flow simulation software again;
(3) The simulation data of the dynamic model is transmitted to the collector software by using OPC Server software, and then the collector software is used for importing the data into the central cloud, namely the industrial operating system.
(4) An acrylic acid organic pollutant treatment optimization control system UI interface is designed on an industrial operating system; an acrylic acid organic pollutant treatment optimization control APP module is established, and a control interface is provided with a process parameter real-time data interface, a monitoring interface, an intelligent optimization interface, a feeding fluctuation interface, a pollution emission real-time VOC and COD monitoring interface, wherein the intelligent optimization interface is added with a real-time optimization control. Aiming at the problems of total energy consumption and reactor efficiency of the edge side dynamic model, a differential evolution algorithm is adopted to perform multi-objective optimization calculation on the problem, an optimal optimization operation variable is obtained, and the function is integrated into a real-time optimization control of an intelligent optimization interface.
(5) And (3) realizing data write-back to the edge side dynamic model through collector software and OPC Server software by using an instruction signal obtained after the APP is controlled and optimized by using the acrylic acid organic pollutants, and realizing data bidirectional transmission of the edge side dynamic model and the APP by using the central cloud optimization and control together with the step (3).
In some specific technical schemes, the design of the acrylic acid organic pollutant treatment process flow in the technical scheme mainly comprises 4 stages of a heat exchanger preheating stage, a fluidized bed reactor catalytic reaction stage, a fixed bed reactor catalytic reaction stage, a gas-liquid separator gas-liquid separation stage and the like:
the first stage is a heat exchanger preheating stage, firstly air is introduced, and the reaction heat release of the fluidized bed reactor and the fixed bed reactor is used for heating the air and the two-phase organic pollutants to reach the preset temperature of the reactor;
the 2 nd stage is a catalytic reaction stage of the fluidized bed reactor, the introduced gas-liquid two-phase organic pollutants are mixed with air and then enter the fluidized bed reactor, catalytic oxygen-induced cracking occurs in the reactor under the action of a catalyst, the organic pollutants are converted into carbon dioxide, water and other pollution-free substances, a Cu/Ce catalyst is filled, and the particle size distribution of the catalyst is 900-180 mu m;
the 3 rd stage is a fixed bed reactor catalytic reaction stage, unreacted reactant and reactant after the second stage catalytic reaction are introduced into the fixed bed reactor for deep catalytic reaction, a large amount of heat is generated in the two-step reaction and is used for vaporizing the reactant and the product, and the residual heat is used for preheating the feed through a heat exchange stage so as to reduce energy consumption and enable the initial materials to quickly reach the reaction temperature;
the 4 th stage is a condensation separator stage for realizing gas-liquid separation, and condensate discharged from the bottom and tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard 80mgO 2 Per liter and exhaust emission standard 120mg/m 3 。
In the technical scheme of the application, the dynamic model construction for the treatment of the acrylic acid organic pollutants in the technical scheme comprises the following main catalytic reaction and reaction kinetic parameters of the treatment of the acrylic acid organic pollutants:
K＝4.18×10 21 ,E＝186834kJ/kmol
K＝6.6568×10 10 ,E＝101236kJ/kmol
K＝5.4694×10 23 ,E＝187833kJ/kmol
the mass fractions (%) of the components of the feed stream A, B, C, D are shown in table 1.
TABLE 1
| A (air) | B (waste gas) | C (waste water 1) | D waste water (2) | |
| Nitrogen gas | 0.7800 | 0.7795 | 0 | 0 |
| Oxygen gas | 0.2299 | 0.2098 | 0 | 0 |
| Carbon dioxide | 0.0001 | 0 | 0 | 0 |
| Water and its preparation method | 0 | 0 | 0.9450 | 0 |
| Carbon monoxide | 0 | 0.0042 | 0 | 0 |
| Propylene | 0 | 0.0015 | 0 | 0 |
| Propane | 0 | 0.0028 | 0 | 0 |
| N-butanol | 0 | 0 | 0.0450 | 0.4498 |
| Ethylene glycol | 0 | 0 | 0 | 0.1500 |
| Tert-butanol | 0 | 0 | 0 | 0.3500 |
| Acrylic acid | 0 | 0 | 0 | 0.0500 |
| Formaldehyde | 0 | 0.0020 | 0 | 0 |
| Acetic acid | 0 | 0 | 0.0100 | 0 |
The steady state model is built by using process simulation software in combination with the process flow design, and the process design unit parameters are shown in table 2.
TABLE 2
In a fourth aspect, the acrylic acid organic pollutant treatment dynamic model in the technical scheme is established. After a steady-state simulation system of the acrylic acid organic pollutant treatment process is constructed by adopting process simulation software, a valve and a fluid pump are additionally arranged, the size of each device is regulated, and the like, a control system is designed by adopting a multivariable control method, and different controllers are arranged at different devices and flow sections and are converted into a dynamic model.
The feeding proportion is controlled to be that a proportion controller FC (101, 102, 103, 104) is arranged between the air feeding and the two-phase organic pollutant feeding, and the output of the controller is the valve opening of a feeding valve in a dynamic model;
the pressure control is that a pressure controller PC (204) is arranged in a gas-liquid flash tank, and the pressure controller PC (201, 202, 203) is arranged between a fluidized bed and a fixed bed reactor, and the output of the controller is the valve opening of a pressure control valve in a dynamic model;
the liquid level control is that a liquid level controller LC (401) is arranged for the gas-liquid flash tank, and the output of the controller is the valve opening of a liquid level control valve in the dynamic model;
the temperature control is to set self-feedback temperature controllers TC (301, 302) in the reactor, and set heat transfer controllers TC (303, 304) in the reactor, wherein the output of the controllers is the valve opening of a temperature control valve in a dynamic model.
Tuning parameters and action directions of the controllers of all control sites are shown in Table 3
TABLE 3 Table 3
| Proportional gain | Integration time (min) | Direction of action | |
| FC101 | 0.5 | 0.3 | Reverse-rotation |
| FC102 | 0.5 | 0.3 | Reverse-rotation |
| FC103 | 0.5 | 0.3 | Reverse-rotation |
| FC104 | 0.5 | 0.3 | Reverse-rotation |
| PC201 | 20 | 12 | Positive direction |
| PC202 | 20 | 12 | Positive direction |
| PC203 | 20 | 12 | Positive direction |
| PC204 | 20 | 12 | Positive direction |
| TC301 | 5 | 0.5 | Reverse-rotation |
| TC302 | 5 | 0.5 | Reverse-rotation |
| TC303 | 5 | 0.5 | Reverse-rotation |
| TC304 | 5 | 0.5 | Reverse-rotation |
| LC401 | 2 | 9999 | Positive direction |
The technical scheme of the application is as follows: and transmitting data of the edge side dynamic model to a central cloud industrial operating system: the dynamic simulation data is transmitted to the collector software by using OPC Server software, and then the collector software is used for importing the data into an example template of an industrial operating system, and the specific steps are as follows:
(1) And (5) deriving dynamic model data. Firstly, after finishing the setting of a dynamic model, exporting variables required to be read and written to OPC Server software;
(2) And (5) data acquisition by the collector software. And then the acquired dynamic model data which is exported in the OPC Server software is acquired through the collector software, and the exported simulation data is arranged in the collector to be read, written and stored in real time.
(3) The data is accessed into the acrylic acid organic pollutant treatment and optimization management APP, the industrial operation system and the collector software are subjected to authentication management, and after the authentication management is finished, each piece of data in the collector is transmitted to the industrial operation system for classification and renaming.
The technical scheme of the application is as follows: acrylic acid organic pollutant governance control system UI interface: and building an acrylic acid organic pollutant treatment optimization management and control APP in an industrial operation system APP designer, issuing a Web version, and embedding the Web version into the platform in a webpage component module form through an industrial operation system.
In the technical scheme of the application, aiming at an edge side dynamic process model, a real-time multi-objective optimization method based on a differential evolution algorithm is adopted: in order to solve the problem of the reaction efficiency of the reactor, the ratio of the contents of organic pollutants in the fluidized bed and fixed bed catalytic cracking reactors of the two-phase catalytic cracking reactor is used as a first objective function F (1) and a second objective function F (2).
F(1)＝V1＝m 1a /m 1b (1)
F(2)＝V2＝m 2a /m 2b (2)
Wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutant in the fluidized bed reactor, and m 1a Is the content, m before the acrylic acid organic pollutant enters the fluidized bed reactor 1b Is the content of acrylic acid organic pollutant after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency, m of the acrylic acid organic pollutant in the fixed bed reactor 2a The content, m of the acrylic acid organic pollutant before entering a fixed bed reactor 2b Is the content of acrylic acid organic pollutant after flowing out of the fixed bed reactor.
To solve the problem of total process energy consumption, the total process energy consumption is used as a third objective function F (3). The specific total energy consumption calculation formula is as follows:
∑P＝P f +P c +P p +P r1 +P r2 (3)
wherein ΣP, P f ,P c ,P p ,P r1 ,P r2 The total energy consumption effective power of the organic pollution control flow in the acrylic acid industrial production, the effective power of each flash tank, the effective power of each water pump, the effective power of the air compressor, the effective power of the fluidized bed reactor temperature regulating device and the effective power of the fixed bed reactor temperature regulating device are respectively shown.
The power of each device is effective power, the total power consumption is the sum of the total power of each device, and if the power efficiency of a flash tank is 70%, the power efficiency of a water pump is 65%, the efficiency of an air compressor is 60%, the efficiency of a fluidized bed reactor temperature regulating device is 75%, and the efficiency of a fixed bed reactor temperature regulating device is 65%.
Wherein Σp1 represents the total energy consumption and power of the organic pollution control process in the industrial production of acrylic acid.
In order to meet the national pollution emission standard, the COD and the VOC content of the treated wastewater are used as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80(5)
0≤G(2)＝VOC≤120 (6)
wherein COD and VOC represent the COD of the wastewater and the VOC content of the waste gas respectively.
The feed ratio of both air and acrylic acid organic contaminants, fluidized bed reactor temperature and fixed bed reactor temperature were used as decision variables. Expression (1), (2), and (4) are used as objective functions, and expression (5) and (6) are used as constraints.
And (3) iteratively solving the maximum value of the objective functions F (1) and F (2) and the minimum value of F (3) by adopting a differential evolution algorithm method. The parameters of the differential evolution algorithm are: population size np=50, variance factor f=0.63, crossover probability cr=0.32, maximum number of iterations gmax=100.
The data in the technical scheme is written back to the edge side dynamic model. And the command signal obtained after the acrylic acid organic pollutant is used for controlling and optimizing the APP is subjected to data write-back to the edge side dynamic model through the collector software and the OPC Server software, so that the data bidirectional transmission of the edge side dynamic model and the central cloud optimizing and controlling APP is realized.
Based on the technical scheme, the intelligent control platform for the acrylic acid organic pollutant treatment is realized by integrating the acrylic acid organic pollutant treatment process development design, the dynamic model setting and the industrial operation system, and various application scenes and simulation fluctuation provide a simulation operation platform which is closer to the actual performance of the industrial intelligent system.
It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the application as claimed.
The flow simulation software is Aspen Plus software and Aspen Plus Dynamics software which are commercial engineering software products of America Ainshiu technologies Co.
The OPC Server software is OPC Server software of MatrikonOPC Industrial control software company of Canada.
The collector software is supOS data collection software of Zhejiang blue android industry Internet information technology Co.
The industrial operating system is a supOS industrial operating system of Zhejiang blue-Zhejiang industrial Internet information technology Co.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the application and together with the description, serve to explain the principles of the application and do not constitute a undue limitation on the application.
Fig. 1 is a schematic diagram of the overall architecture of the present application.
FIG. 2 is a steady-state model diagram of an acrylic acid organic pollutant treatment process flow.
FIG. 3 is a dynamic model control chart of the acrylic acid organic pollutant treating process.
1: a mixing tank a;2: a mixing tank b;3, a fluidized bed reactor; 4: a heat exchanger; 5: a fixed bed reactor a;
6: a fixed bed reactor b;7, flash tank, A: acrylic acid organic waste gas; b: air; c: acrylic acid organic wastewater; d: acrylic acid organic waste water. FC101, FC102, FC103 and FC104 are all feed ratio controllers; PC201, PC202, PC203, PC204 are pressure controllers; TC301, TC302, TC303, TC304 are temperature controllers; LC401 is a liquid level controller.
FIG. 4 is a diagram of steps for authentication management of industrial operating system and collector software.
FIG. 5 is a chart of an APP for optimizing and controlling the treatment of acrylic acid organic pollutants in an industrial operation system.
FIG. 6 is a flow chart of a differential evolution algorithm suitable for use with the edge side dynamic model.
Detailed Description
The application is further illustrated below with reference to examples, but the scope of the application is not limited thereto:
it should be noted that the terms "first," "second," and the like herein are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate such that the embodiments of the application described herein may be implemented in sequences other than those illustrated or otherwise described herein. The implementations described in the following exemplary examples do not represent all implementations consistent with the application. Rather, they are merely examples of apparatus and methods consistent with aspects of the application as detailed in the accompanying claims.
As shown in fig. 2, the design simulation of the steady-state flow of the acrylic acid organic pollutant treatment. The main organic pollutants in the two-step oxidation method for preparing acrylic acid by using the main current propylene are acrylic acid, acetic acid, formaldehyde, acrolein, methyl acrylate, ethyl acrylate and the like. The design of the process flow for treating the acrylic acid organic pollutants mainly comprises four stages of a heat exchanger preheating stage, a fluidized bed reactor catalytic reaction stage, a fixed bed reactor catalytic reaction stage and a gas-liquid separator gas-liquid separation stage:
the first stage is a heat exchanger preheating stage, firstly introducing air, and heating the air and the two-phase organic pollutants by using the heat exchanger to react and release heat of the fluidized bed reactor and the fixed bed reactor to reach the preset temperature of the reactor;
the second stage is a catalytic reaction stage of a fluidized bed reactor, the introduced gas-liquid two-phase organic pollutants are mixed with air and then enter the fluidized bed reactor, catalytic oxygen-induced cracking occurs in the reactor under the action of a catalyst, the organic pollutants are converted into carbon dioxide, water and other pollution-free substances, a Cu/Ce catalyst is filled, and the particle size distribution of the catalyst is 900-180 mu m;
the third stage is a fixed bed reactor catalytic reaction stage, unreacted reactant and reactant after the second stage catalytic reaction are introduced into the fixed bed reactor for deep catalytic reaction, a large amount of heat is generated in the two-step reaction and is used for vaporizing the reactant and the product, and the residual heat is used for preheating the feed through a heat exchange stage so as to reduce energy consumption and enable the initial materials to quickly reach the reaction temperature;
the fourth stage is to realize gas-liquid separation in the condensation separator stage, wherein condensate discharged from the bottom and tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard 80mg/L and the waste gas discharge standard 120mg/m 3 。
And (3) constructing a steady-state model for treating the acrylic acid organic pollutants. The main catalytic reaction and reaction kinetic parameters of the acrylic acid organic pollution treatment are as follows:
K＝4.18×10 21 ,E＝186834kJ/kmol
K＝6.6568×10 10 ,E＝101236kJ/kmol
K＝5.4694×10 23 ,E＝187833kJ/kmol
the mass fractions (%) of the components of the feed stream A, B, C, D are shown in Table 1
TABLE 1
The steady state model is established by using flow simulation software in combination with the process flow design, and the parameters of the process design unit are shown in Table 2
TABLE 2
As shown in fig. 3, the dynamic model of the edge side acrylic acid organic pollutant treatment is established. After a steady-state simulation system of the acrylic acid organic pollutant treatment process is constructed by adopting process simulation software, a valve and a fluid pump are additionally arranged, the size of each device is regulated, and the like, a control system is designed by adopting a multivariable control method, and different controllers are arranged at different devices and flow sections and are converted into a dynamic model.
The feeding proportion is controlled to be that a proportion controller FC (101, 102, 103, 104) is arranged between the air feeding and the two-phase organic pollutant feeding, and the output of the controller is the valve opening of a feeding valve in a dynamic model;
the pressure control is that a pressure controller PC (204) is arranged in a gas-liquid flash tank, and the pressure controller PC (201, 202, 203) is arranged between a fluidized bed and a fixed bed reactor, and the output of the controller is the valve opening of a pressure control valve in a dynamic model;
the liquid level control is that a liquid level controller LC (401) is arranged for the gas-liquid flash tank, and the output of the controller is the valve opening of a liquid level control valve in the dynamic model;
the temperature control is to set self-feedback temperature controllers TC (301, 302) in the reactor, and set heat transfer controllers TC (303, 304) in the reactor, wherein the output of the controllers is the valve opening of a temperature control valve in a dynamic model.
Tuning parameters and action directions of the controllers of all control sites are shown in Table 3
TABLE 3 Table 3
| Proportional gain | Integration time (min) | Direction of action | |
| FC101 | 0.5 | 0.3 | Reverse-rotation |
| FC102 | 0.5 | 0.3 | Reverse-rotation |
| FC103 | 0.5 | 0.3 | Reverse-rotation |
| FC104 | 0.5 | 0.3 | Reverse-rotation |
| PC201 | 20 | 12 | Positive direction |
| PC202 | 20 | 12 | Positive direction |
| PC203 | 20 | 12 | Positive direction |
| PC204 | 20 | 12 | Positive direction |
| TC301 | 5 | 0.5 | Reverse-rotation |
| TC302 | 5 | 0.5 | Reverse-rotation |
| TC303 | 5 | 0.5 | Reverse-rotation |
| TC304 | 5 | 0.5 | Reverse-rotation |
| LC401 | 2 | 9999 | Positive direction |
After the establishment of the dynamic model for treating the acrylic acid organic pollutants at the edge side is completed, the data transmission from the dynamic model at the edge side to the central cloud industrial operation system is carried out. The dynamic simulation data is transmitted to the collector software by using OPC Server software, and then the collector software is used for importing the data into an example template of an industrial operating system, and the specific steps are as follows:
1) In the flow simulation software, a sub toolbar "On Line Links …" under the "Tools" in the toolbar is used to export the Variables required to be read and written, and an Input variable is taken as an Input variable, and an Output variable is taken as an Output variable. The table below the page is selected to be On.
2) OPC Server software can realize the reading and writing of each variable parameter of the flow in the flow simulation software. And exporting the edited variables required to be read and written in the steps to an acrylic acid organic pollutant treatment process flow label page of the OPC Server. The corresponding OPC Server tag page ID 'acrylic acid organic pollutant treatment process flow' can be opened through OPC Explorer software, and the data export and write-back functions are observed. The test run flow simulates data, and the data can be correctly and stably read and written.
3) Data is collected from the OPC Server software using data collector software. The data acquisition of the OPC Server acrylic acid organic pollutant treatment process flow is realized by three steps, wherein the first step is that a collector source point is established, and the establishment method is as follows: (1) Clicking a < + > new adding button of the source point management information interface, and expanding source point information configuration; (2) Inputting a source point name ASA, selecting OPCDA by a drive name, and expanding information required to be input by the drive according to the selected drive name by a system; (3) Clicking the < change > button, expanding the OPC server, and inputting the < OPA service address > as "localhost"; (4) < OPC DA service selection > is selected as "OPC.Simulation.1"; (5) automatically generating an OPC server path; (6) Clicking a radio button of a protocol version, and selecting a protocol version V2.0 corresponding to the OPC server; (7) Selecting a mode of disconnection reconnection, and selecting the disconnection reconnection by default; (8) selecting a reconnection interval of 30s; (9) clock source selection "local time"; (10) setting the delay request to 5s; (11) setting the update rate to 1000ms; (12) setting a read-write state as read-write; (13) clicking on the < save > button.
The second step is the introduction of the acquisition site, and the specific implementation way is as follows: the OPC driver supports a bit number batch import function, and after the source point information is configured, the OPC driver (1) clicks into a [ bit number batch import ] tab, and expands bit number batch import information; (2) Clicking < enumerate the number of bits >, the system will enumerate the number of bits information that this source point corresponds automatically; (3) Selecting a bit number to be imported, namely a variable which needs to be read and written in a label page of an acrylic acid organic pollutant treatment process flow in OPC Server software, and clicking < import >; (4) The "tag management" page will import all the bit numbers for the source point.
The third step is that the collector is connected to the industrial operating system. As shown in fig. 4, the access industry operating system operates as follows: (1) Entering an administrator setting page, and clicking a < + > button to newly increase authentication under a collection node management/authentication management page; inputting a name, a responsible person, a company address, a company name and a description, clicking a < generation > button to automatically generate a UUID, selecting a type of a common collector, clicking a determination, and determining that an authentication state is to be accessed; (2) At the collector software end, a system information management/system configuration management page, an input name, an industrial operating system server address, a UUID generated by the input industrial operating system end, a communication port 32568, a data uploading mode TCP, clicking a < save > button, and popping up a dialogue box with successful operation; at the industrial operating system end, collecting a node management/state management page, and checking the authentication state as 'to be audited'; (3) After the information is unfolded, clicking a < agree > button to agree the acquisition unit to access; the connection state of the collector software end shows that the connection is successful; displaying 'checked' on the authentication management state of the industrial operating system end, and finishing authentication; (4) And clicking the collector row to expand the source point state tab under the industrial operating system [ collection node management/state management ], so that the source point state of the collector can be checked. Managing a data collector; (5) object instance binding data source acquisition data.
Therefore, the bidirectional transmission of the data of the edge side dynamic model and the data of the central cloud industrial operating system can be completed.
As shown in FIG. 5, an acrylic acid organic pollutant treatment optimizing and controlling system is newly built on an industrial operation system platform. And building an acrylic acid organic pollutant treatment optimization management and control APP in an industrial operation system APP designer, issuing a Web version, and embedding the Web version into the platform in a webpage component module form through an industrial operation system. The control interface is provided with a process parameter real-time data interface, a monitoring interface, an intelligent optimization interface, a feeding fluctuation interface, a pollution emission real-time VOC and COD monitoring interface. When the process parameters are set up in the real-time data interface, the monitoring interface, the feeding fluctuation interface and the pollution emission real-time VOC and COD monitoring interface, the control of the industrial operating system is called first, and then the industrial operating system is debugged and used. And the intelligent optimization interface is added with a real-time optimization control. Aiming at the problems of total energy consumption and reactor efficiency of the edge side dynamic model, a differential evolution algorithm is adopted to perform multi-objective optimization calculation on the problem, an optimal optimization operation variable is obtained, and the function is integrated into a real-time optimization control of an intelligent optimization interface.
In order to solve the problem of the reaction efficiency of the reactor, the ratio of the contents of organic pollutants before and after the reaction in unit time is used as a first objective function F (1) and a second objective function F (2) for the catalytic reaction efficiency of the fluidized bed and the fixed bed of the two-phase catalytic cracking reactor.
F(1)＝V1＝m 1a /m 1b (1)
F(2)＝V2＝m 2a /m 2b (2)
Wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutant in the fluidized bed reactor, and m 1a Is the content, m before the acrylic acid organic pollutant enters the fluidized bed reactor 1b Is the content of acrylic acid organic pollutant after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency, m of the acrylic acid organic pollutant in the fixed bed reactor 2a The content, m of the acrylic acid organic pollutant before entering a fixed bed reactor 2b Is the content of acrylic acid organic pollutant after flowing out of the fixed bed reactor.
To solve the problem of total process energy consumption, the total process energy consumption is used as a third objective function F (3). The specific total energy consumption calculation formula is as follows:
∑P＝P f +P c +P p +P r1 +P r2 (3)
wherein ΣP, P f ,P c ,P p ,P r1 ,P r2 Respectively represents the total energy consumption effective power of the organic pollution control flow in the acrylic acid industrial production, the effective power of each flash tank, the effective power of each water pump, the effective power of an air compressor, the effective power of the temperature regulating equipment of the fluidized bed reactor and the fixed bedThe reactor attemperation device is active.
The power of each device is effective power, the total power consumption is the sum of the total power of each device, and if the power efficiency of a flash tank is 70%, the power efficiency of a water pump is 65%, the efficiency of an air compressor is 60%, the efficiency of a fluidized bed reactor temperature regulating device is 75%, and the efficiency of a fixed bed reactor temperature regulating device is 65%.
Wherein Σp1 represents the total energy consumption and power of the organic pollution control process in the industrial production of acrylic acid.
In order to meet the national pollution emission standard, the COD and the VOC content of the treated wastewater are used as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80(5)
0≤G(2)＝VOC≤120 (6)
wherein COD and VOC represent the COD of the wastewater and the VOC content of the waste gas respectively.
The feed ratio of both air and acrylic acid organic contaminants, fluidized bed reactor temperature and fixed bed reactor temperature were used as decision variables. Expression (1), (2), and (4) are used as objective functions, and expression (5) and (6) are used as constraints.
As shown in fig. 6, the maximum value of the objective functions F (1), F (2) and the minimum value of F (3) are iteratively solved by adopting a differential evolution algorithm method. The parameters of the differential evolution algorithm are: population size np=50, variance factor f=0.63, crossover probability cr=0.32, maximum number of iterations gmax=100.
And (3) assuming that the optimization operation is carried out every five minutes, carrying out iterative operation by the multi-objective optimization algorithm, and writing the optimal decision variable back to an edge side acrylic acid organic pollutant treatment dynamic model decision variable port through a bidirectional data transmission channel so as to complete real-time optimization. The method is characterized in that the process performance change brought by the flow fluctuation and the equipment hysteresis effect is optimized in real time on the acrylic acid organic pollutant control APP, and the acrylic acid organic pollutant dynamic model on the edge side is written back to perform a new round of acrylic acid organic pollutant process simulation operation.
The control system is operated, and the acrylic acid treatment process flow is stably operated. The platform can monitor the change condition of main parameters of the whole process and alarm the variables exceeding the critical value. The platform can also calculate the total cost of the process flow in real time, and is provided with a working condition emergency disposal button. And setting material disturbance manually at a control interface, and recovering each parameter to a stable state after three minutes, wherein no working condition alarm occurs. Whether or not the feed fluctuation is added, the VOC content in the waste gas and the COD value in the waste liquid meet the national emission requirements, and the comparison between the feed fluctuation and the feed fluctuation is shown in the following table. According to the application, through multi-loop control and multi-objective optimization aiming at the edge side dynamic model, the working condition is normal, and the feeding components and flow disturbance can be effectively overcome.
The above description explains the application in detail in terms of process flow design, process variable multi-objective optimization, process flow dynamic design, analog data transmission, intelligent optimization management and control platform establishment, and the like. But the application not only can solve the problem of treatment of acrylic acid organic pollutants, but also can develop similar chemical production and byproduct recycling.
The exemplary embodiments mentioned in this disclosure describe some methods or systems based on a series of steps or devices. However, the present application is not limited to the order of the above-described steps, that is, the steps may be performed in the order mentioned in the embodiments, or may be performed in a different order from the order in the embodiments, or several steps may be performed simultaneously.
Other embodiments of the application will be apparent to those skilled in the art from consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of the application following, in general, the principles of the application and including such departures from the present disclosure as come within known or customary practice within the art to which the application pertains. The specification and examples are to be regarded in an illustrative manner only.
It is to be understood that the application is not limited to the precise arrangements and instrumentalities shown in the drawings, which have been described above, and that various modifications and changes may be effected without departing from the scope thereof. The scope of the application is limited only by the appended claims.
Claims (5)
1. Cloud edge collaborative optimization intelligent management and control system for organic pollutant treatment is characterized in that: the system comprises edge side organic pollutant aerobic pyrolysis treatment process design and dynamic model establishment, central cloud end organic pollutant treatment optimization management and control APP module creation and edge side and central cloud end data real-time transmission, and the specific process is as follows:
(1) Aiming at the acrylic acid organic pollutant treatment process, adopting an oxygen-induced cracking treatment technology to carry out flow design of a heat exchanger, a fluidized bed reactor, a fixed bed reactor and a gas-liquid separator;
(2) Firstly, constructing an acrylic acid organic pollutant treatment steady-state model based on a reaction kinetic equation and flow design in the step (1) by using flow simulation software, then designing an acrylic acid organic pollutant control system by adopting a multivariable control method, and finally constructing an edge side acrylic acid organic pollutant treatment dynamic model by using the flow simulation software again;
(3) The simulation data of the OPC Server software dynamic model is transmitted to the collector software, and then the collector software is used for importing the data into the central cloud, namely the industrial operating system;
(4) An acrylic acid organic pollutant treatment optimization control system UI interface is designed on an industrial operating system; an acrylic acid organic pollutant treatment optimization control APP module is established, and a control interface is provided with a process parameter real-time data interface, a monitoring interface, an intelligent optimization interface, a feeding fluctuation interface, a pollution emission real-time VOC and COD monitoring interface, wherein the intelligent optimization interface is added with a real-time optimization control; aiming at the problems of total energy consumption and reactor efficiency of the edge side dynamic model, performing multi-objective optimization calculation on the problem by adopting a differential evolution algorithm to obtain an optimal optimization operation variable, and integrating functions into a real-time optimization control of an intelligent optimization interface;
(5) And (3) realizing data write-back to the edge side dynamic model through collector software and OPC Server software by using an instruction signal obtained after the APP is controlled and optimized by using the acrylic acid organic pollutants, and realizing data bidirectional transmission of the edge side dynamic model and the APP by using the central cloud optimization and control together with the step (3).
2. The cloud edge collaborative optimization intelligent management and control system for organic pollutant remediation according to claim 1, wherein the system comprises: the design of the acrylic acid organic pollutant treatment flow in the step (1) mainly comprises four stages of a heat exchanger preheating stage, a fluidized bed reactor catalytic reaction stage, a fixed bed reactor catalytic reaction stage and a gas-liquid separator gas-liquid separation stage:
the first stage is a heat exchanger preheating stage, firstly introducing air, and heating the air and the two-phase organic pollutants by using the heat exchanger to react and release heat of the fluidized bed reactor and the fixed bed reactor to reach the preset temperature of the reactor;
the second stage is a catalytic reaction stage of the fluidized bed reactor, the introduced gas-liquid two-phase organic pollutants are mixed with air and then enter the fluidized bed reactor, catalytic oxygen-induced cracking occurs in the reactor under the action of a catalyst, and the organic pollutants are converted into pollution-free substances, wherein the pollution-free substances comprise carbon dioxide and water;
the third stage is a fixed bed reactor catalytic reaction stage, unreacted reactant and reactant after the second stage catalytic reaction are introduced into the fixed bed reactor for deep catalytic reaction, a large amount of heat is generated in the two-step reaction and is used for vaporizing the reactant and the product, and the residual heat is used for preheating the feed through a heat exchange stage so as to reduce energy consumption and enable the initial materials to quickly reach the reaction temperature;
the fourth stage is to realize gas-liquid separation in the condensation separator stage, wherein condensate discharged from the bottom and tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard 80mg/L and the waste gas discharge standard 120mg/m 3 。
3. The cloud edge collaborative optimization intelligent management and control system for organic pollutant remediation according to claim 1, wherein the system comprises: in the step (3), dynamic simulation data is transmitted to collector software by using OPC Server software, and then the collector software is used for importing the data into an example template of an industrial operating system, and the specific steps are as follows:
(1) Dynamic model data derivation: firstly, after finishing the setting of a dynamic model, exporting variables required to be read and written to OPC Server software;
(2) And (3) collector software data collection: then the data of the dynamic model which is exported in the OPC Server software is collected through the collector software, and the exported simulation data is set in the collector to be read, written and stored in real time;
(3) The data is accessed into the acrylic acid organic pollutant treatment and optimization management APP, the industrial operation system and the collector software are subjected to authentication management, and each piece of data in the collector is transmitted to the central cloud industrial operation system after the authentication management is finished.
4. The cloud edge collaborative optimization intelligent management and control system for organic pollutant remediation according to claim 1, wherein the system comprises: in the step (4), an acrylic acid organic pollutant treatment optimization management and control APP is established in an industrial operation system APP designer, a Web version is issued, and the APP is embedded into a platform through an industrial operation system in a webpage component module mode.
5. The cloud edge collaborative optimization intelligent management and control system for organic pollutant remediation according to claim 1, wherein the system comprises: in the step (4), the real-time multi-objective optimization method based on the differential evolution algorithm is used for solving the problem of the reaction efficiency of the reactor, so that the catalytic reaction efficiency of the fluidized bed and the fixed bed of the two-phase catalytic cracking reactor is used as a first objective function F (1) and a second objective function F (2) according to the ratio of the total organic pollutant contents before and after the reaction in unit time;
F(1)＝V1＝m 1a /m 1b (1)
F(2)＝V2＝m 2a /m 2b (2)
wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutant in the fluidized bed reactor, and m 1a Is the content, m before the acrylic acid organic pollutant enters the fluidized bed reactor 1b Is the content of acrylic acid organic pollutant after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency, m of the acrylic acid organic pollutant in the fixed bed reactor 2a The content, m of the acrylic acid organic pollutant before entering a fixed bed reactor 2b Is the content of acrylic acid organic pollutant after flowing out of the fixed bed reactor;
in order to solve the problem of total process energy consumption, the total process energy consumption is used as a third objective function F (3); the specific total energy consumption calculation formula is as follows:
∑P＝P f +P c +P p +P r1 +P r2 (3)
wherein ΣP, P f ,P c ,P p ,P r1 ,P r2 The total energy consumption effective power of the organic pollution control flow in the acrylic acid industrial production is respectively represented, and the effective power of each flash tank, the effective power of each water pump, the effective power of an air compressor, the effective power of the temperature regulating equipment of the fluidized bed reactor and the effective power of the temperature regulating equipment of the fixed bed reactor are respectively represented;
the power of each device is effective power, the total power consumption is the sum of the total power of each device, the power efficiency of the existing flash tank is 70%, the power efficiency of the water pump is 65%, the efficiency of the air compressor is 60%, the efficiency of the temperature regulating device of the fluidized bed reactor is 75%, and the efficiency of the temperature regulating device of the fixed bed reactor is 65%;
wherein Σp1 represents the total energy consumption power of the organic pollution control process in the industrial production of acrylic acid;
in order to meet the national pollution emission standard, the COD and the VOC content of the treated wastewater are used as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80(5)
0≤G(2)＝VOC≤120 (6)
wherein COD and VOC represent the COD of the wastewater and the VOC content in the waste gas respectively;
taking the feeding ratio of air and acrylic acid organic pollutants, the fluidized bed reactor temperature and the fixed bed reactor temperature as decision variables, taking expressions (1), (2) and (4) as objective functions and taking expressions (5) and (6) as constraint conditions;
carrying out iterative solution on the maximum value of the objective function F (1), the maximum value of the objective function F (2) and the minimum value of the objective function F (3) by adopting a differential evolution algorithm method, wherein the parameters of the differential evolution algorithm are as follows: population size np=50, variance factor f=0.63, crossover probability cr=0.32, maximum number of iterations gmax=100.
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