CN114280936A - 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 invention discloses an organic pollutant treatment cloud edge collaborative optimization intelligent management and control system. Providing a low-energy-consumption dynamic process flow design for organic pollutant treatment on the edge side, and establishing a process steady-state model, a dynamic model and a control system design thereof by using flow simulation software; an acrylic acid organic pollutant treatment optimization management and control APP module is established at the center cloud based on an industrial operating system and is used for visually monitoring, optimizing and controlling the treatment process of organic pollutants. And performing bidirectional data transmission between the edge side and the center cloud by taking OPC Server software as a data transfer station to realize bidirectional data transmission between an edge side dynamic model and the center cloud, wherein the bidirectional data transmission comprises cooperative optimization control of data signals such as dynamic simulation data, decision variable write-back, PID parameter setting, working condition emergency braking and the like. The platform established by the system can be used for process optimization, working condition simulation and early warning, and worker training and remote control.
Description
Technical Field
The invention relates to the field of flow design simulation, multi-objective optimization and industrial operation system APP development, in particular to acrylic acid organic pollutant treatment process flow design, acrylic acid organic pollutant treatment optimization management control APP development and cloud edge collaborative optimization management control system establishment for acrylic acid organic pollutant treatment.
Background
With the rapid development of industrial production, organic pollutants with difficult degradability and larger pollution are always difficult problems in the chemical industry. The problem of treating organic pollutants is also gradually paid extensive attention by the academic world, and how to treat the organic pollutants in a harmless way to enable the organic pollutants to reach the national emission standard becomes a difficult problem to be solved urgently in the field. The green production is always the industrial production mode pursued by professionals in the chemical field at present. The waste water generated in the production process of acrylic acid has high organic matter concentration, contains various organic matters such as acrylic acid, acetic acid, formaldehyde, acrolein, methyl acrylate, ethyl acrylate and the like, has complex components and high toxicity, and thus, the treatment of the waste water of acrylic acid and esters thereof is very difficult. Networking and intellectualization are a new prospect in the current industrial field, and how to realize industrial operation automation, intelligent optimization, energy conservation, consumption reduction and remote control becomes a practical problem to be solved urgently.
Disclosure of Invention
The invention provides a cloud-edge collaborative optimization intelligent management and control system for treating organic pollutants, aiming at the existing technical problems.
The purpose of the invention can be realized by the following technical scheme:
the utility model provides a cloud limit collaborative optimization intelligence management and control system that organic pollutant was administered, this system includes that the edge side organic pollutant faces oxygen schizolysis and administers flow design and dynamic model establishment, central high in the clouds organic pollutant administers and optimizes the management and control APP module and establish and both data real-time transmission in edge side and central high in the clouds, and the concrete process of this system is as follows:
(1) aiming at the treatment process of the acrylic acid organic pollutants, the flow design of a heat exchanger, a fluidized bed reactor, a fixed bed reactor and a gas-liquid separator is carried out by adopting the temporary oxygen cracking treatment technology;
(2) based on a reaction kinetics equation and the process flow design in the step (1), firstly constructing an acrylic acid organic pollutant treatment steady-state model 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 dynamic model is transmitted to collector software by using OPC Server software, and then the data is imported into a central cloud, namely an industrial operating system, by using the collector software.
(4) Designing a UI (user interface) of an acrylic acid organic pollutant treatment optimization management and control system on an industrial operation system; establishing an acrylic acid organic pollutant treatment optimization control APP module, setting 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 on the control 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 dynamic model at the edge side, a differential evolution algorithm is adopted to carry out multi-objective optimization calculation on the dynamic model, the optimal optimization operation variable is obtained, and the function is integrated into a real-time optimization control of an intelligent optimization interface.
(5) And (4) writing back data to the edge side dynamic model by using an instruction signal obtained after the acrylic acid organic pollutant treatment optimization management control APP through collector software and OPC Server software, and realizing the data bidirectional transmission of the edge side dynamic model and the center cloud optimization management control APP together with the step (3).
In some specific technical schemes, the process flow design for treating the acrylic acid organic pollutants in the technical scheme mainly comprises 4 stages, namely 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, air is firstly introduced, the heat exchanger is used for releasing heat of the reaction of the fluidized bed reactor and the fixed bed reactor so as to heat the air and the two-phase organic pollutants to reach the preset temperature of the reactor;
the 2 nd stage is a fluidized bed reactor catalytic reaction stage, the introduced gas-liquid two-phase organic pollutants are mixed with air and then enter the fluidized bed reactor, catalytic oxygen cracking is carried out in the reactor under the action of a catalyst, the organic pollutants are converted into carbon dioxide, water and other pollution-free substances, and the Cu/Ce catalyst is filled, and the particle size distribution of the catalyst is 900-;
the 3 rd stage is a catalytic reaction stage of the fixed bed reactor, unreacted materials and reactants after the catalytic reaction in the second stage are introduced into the fixed bed reactor for deep catalytic reaction, a large amount of heat is generated by the two-step reaction and is used for vaporizing the reactants and the products, and the residual heat is used for preheating feeding materials 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 the condensate discharged from the bottom and the tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard of 80mgO2The emission standard of the exhaust gas and the L is 120mg/m3。
In the technical scheme of the invention, the acrylic acid organic pollutant treatment dynamic model in the technical scheme is constructed, and the main catalytic reaction and reaction kinetic parameters of acrylic acid organic pollution treatment are as follows:
K＝4.18×1021,E＝186834kJ/kmol
K＝6.6568×1010,E＝101236kJ/kmol
K＝5.4694×1023,E＝187833kJ/kmol
the mass fraction (%) of the A, B, C, D components of the feed stream is 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 (W) | 0 | 0 | 0.9450 | 0 |
| |
0 | 0.0042 | 0 | 0 |
| Propylene (PA) | 0 | 0.0015 | 0 | 0 |
| |
0 | 0.0028 | 0 | 0 |
| N- |
0 | 0 | 0.0450 | 0.4498 |
| |
0 | 0 | 0 | 0.1500 |
| Tert- |
0 | 0 | 0 | 0.3500 |
| |
0 | 0 | 0 | 0.0500 |
| Formaldehyde (I) | 0 | 0.0020 | 0 | 0 |
| |
0 | 0 | 0.0100 | 0 |
The steady state model was established using flow simulation software in conjunction with the process design, with the process design unit parameters as shown in table 2.
TABLE 2
In a fourth aspect, the establishment of the acrylic acid organic pollutant treatment dynamic model in the technical scheme is provided. 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 sizes of all equipment are specified, and the like, a control system is designed by adopting a multivariable control method, and different controllers are arranged at different equipment and flow sections and are converted into a dynamic model.
The feeding proportion control is characterized in that a proportion controller FC (101, 102, 103, 104) is arranged between air feeding and 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 the gas-liquid flash tank, the pressure controllers PC (201, 202 and 203) are arranged between the fluidized bed and the fixed bed reactor, and the output of the controllers is the valve opening of a pressure control valve in the dynamic model;
the liquid level control is that a liquid level controller LC (401) is arranged in the gas-liquid flash tank, and the output of the controller is the valve opening of a liquid level control valve in a dynamic model;
the temperature control is carried out by providing a self-feedback type temperature controller TC (301, 302) in the reactor, and providing a heat transfer controller TC (303, 304) in the reactor, the output of which is the valve opening of the temperature control valve in the dynamic model.
The tuning parameters and the action directions of the controllers at each control site are shown in Table 3
TABLE 3
| Proportional gain | Integration time (min) | Direction of action | |
| FC101 | 0.5 | 0.3 | Inverse direction |
| FC102 | 0.5 | 0.3 | Inverse direction |
| FC103 | 0.5 | 0.3 | Inverse direction |
| FC104 | 0.5 | 0.3 | Inverse direction |
| PC201 | 20 | 12 | Is just |
| PC202 | 20 | 12 | Is just |
| PC203 | 20 | 12 | Is just |
| PC204 | 20 | 12 | Is just |
| TC301 | 5 | 0.5 | Inverse direction |
| TC302 | 5 | 0.5 | Inverse direction |
| TC303 | 5 | 0.5 | Inverse direction |
| TC304 | 5 | 0.5 | Inverse direction |
| LC401 | 2 | 9999 | Is just |
The technical scheme of the invention is as follows: and (3) transmitting data from the edge side dynamic model to a central cloud industrial operating system: dynamic simulation data are 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 method comprises the following specific steps:
(1) and (6) deriving dynamic model data. Firstly, after the setting of a dynamic model is finished, exporting variables needing to be read and written to OPC Server software;
(2) and collecting data by collector software. And then, acquiring the derived dynamic model data in the OPC Server software through collector software, and setting the derived simulation data in the collector to be capable of being read, written and stored in real time.
(3) Data access acrylic acid organic pollutant treatment optimization management control APP firstly performs authentication management on an industrial operation system and collector software, and after the authentication management is completed, each piece of data in a collector is transmitted to the industrial operation system for classification and renaming.
The technical scheme of the invention is as follows: acrylic acid organic pollutant administers management and control system UI interface: establishing acrylic acid organic pollutant treatment optimization management control APP in an industrial operation system APP designer, releasing a Web version, and embedding the Web version into the platform through an industrial operation system in a webpage component module mode.
In the technical scheme of the invention, aiming at the dynamic process model at the edge side, the real-time multi-objective optimization method based on the differential evolution algorithm comprises the following steps: in order to solve the problem of reactor reaction efficiency, the catalytic reaction efficiency of a fluidized bed and a fixed bed reactor of a two-phase catalytic cracking reactor is taken as a first objective function F (1) and a second objective function F (2) according to the ratio of the content of each organic pollutant in unit time.
F(1)＝V1＝m1a/m1b (1)
F(2)＝V2＝m2a/m2b (2)
Wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutants in the fluidized bed reactor, m1aM is the content of acrylic acid organic pollutants before entering a fluidized bed reactor1bThe content of acrylic acid organic pollutants after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency of acrylic acid organic pollutants in a fixed bed reactor, m2aM is the content of acrylic acid organic pollutants before entering a fixed bed reactor2bIs the content of acrylic acid organic pollutants after flowing out of the fixed bed reactor.
In order to solve the problem of total energy consumption of the process, the total process energy consumption is taken as a third objective function F (3). The specific total energy consumption calculation formula is as follows:
∑P＝Pf+Pc+Pp+Pr1+Pr2 (3)
wherein, Σ P, Pf,Pc,Pp,Pr1,Pr2Respectively shows the total energy consumption effective power of an organic pollution treatment process in the industrial production of acrylic acid, 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 temperature regulating equipment of a fluidized bed reactor and the effective power of temperature regulating equipment of a fixed bed reactor.
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 flash tank power efficiency is 70%, the water pump power efficiency is 65%, the air compressor efficiency is 60%, the fluidized bed reactor temperature regulating device efficiency is 75%, and the fixed bed reactor temperature regulating device efficiency is 65%.
Wherein, the sigma P1 represents the total energy consumption of the organic pollution treatment process in the acrylic acid industrial production.
In order to meet the national emission standard, the COD of the treated wastewater and the VOC content of the waste gas are taken as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80 (5)
0≤G(2)＝VOC≤120 (6)
wherein, COD and VOC respectively represent COD of the waste water and VOC content in the waste gas.
The feed ratio of air to organic contaminants of acrylic acid, the fluidized bed reactor temperature and the fixed bed reactor temperature were used as decision variables. Expressions (1), (2) and (4) are used as objective functions, and expressions (5) and (6) are used as constraint conditions.
And (3) carrying out iterative solution on the maximum values of the objective functions F (1) and F (2) and the minimum value of the objective function F (3) by adopting a differential evolution algorithm method. The parameters of the differential evolution algorithm are as follows: the population size NP is 50, the variation factor F is 0.63, the crossover probability CR is 0.32, and the maximum number of iterations GMAX is 100.
The data in the technical scheme is written back to the edge side dynamic model. And writing back data of the instruction signal obtained after the acrylic acid organic pollutant treatment optimization management control APP to the edge side dynamic model through collector software and OPC Server software, and realizing data bidirectional transmission of the edge side dynamic model and the center cloud optimization management control APP together.
Based on the technical scheme, the intelligent optimization management and control platform for acrylic acid organic pollutant treatment is realized by combining acrylic acid organic pollutant treatment process development and design, dynamic model setting and an industrial operation system, and a simulation operation platform which is closer to the reality is provided for the performance of the industrial intelligent system by various application scenes and simulation fluctuation.
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.
The process simulation software is commercial engineering software products of Aspen Plus software and Aspen Plus Dynamics software of the American Isthis technology, Inc.
The OPC Server software is the OPC Server software of MatrikonOPC Industrial control software company of Canada.
The collector software is supOS data collection software of Zhejiang blue-and-erect industry Internet information technology Limited.
The industrial operating system is a supOS industrial operating system of the Zhejiang blue-and-tall industry internet information technology limited company.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present application and, together with the description, serve to explain the principles of the application and are not to be construed as limiting the application.
FIG. 1 is a general architecture of the present invention.
FIG. 2 is a steady-state model diagram of the acrylic acid organic pollutant treating process flow.
FIG. 3 is a control diagram of a dynamic model of an acrylic acid organic pollutant treatment process flow.
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 wastewater. FC101, FC102, FC103 and FC104 are all feed ratio controllers; PC201, PC202, PC203 and PC204 are all pressure controllers; TC301, TC302, TC303 and TC304 are all temperature controllers; LC401 is a level controller.
Fig. 4 is a diagram of the steps of the authentication management of the industrial operating system and the collector software.
FIG. 5 is a diagram of APP for optimizing and controlling treatment and control of acrylic acid organic pollutants in an industrial operation system.
FIG. 6 is a flowchart of a differential evolution algorithm suitable for an edge-side dynamic model.
Detailed Description
The invention is further illustrated by the following examples, without limiting the scope of the invention:
it should be noted that the terms "first," "second," and the like in this application are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the application described herein are capable of operation in sequences other than those illustrated or otherwise described herein. The embodiments described in the following exemplary embodiments do not represent all embodiments consistent with the present application. Rather, they are merely examples of apparatus and methods consistent with certain aspects of the present application, as detailed in the appended claims.
Referring to fig. 2, the design simulation of the steady-state flow of acrylic acid organic pollutant treatment is shown. The main organic pollutants in the process for preparing acrylic acid by using the mainstream propylene two-step oxidation method at present are acrylic acid, acetic acid, formaldehyde, acrolein, methyl acrylate, ethyl acrylate and the like. The process design of the treatment process of the acrylic acid organic pollutants is mainly divided into four stages, namely 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, air is firstly introduced, the heat exchanger is used for carrying out reaction heat release of the fluidized bed reactor and the fixed bed reactor so as to heat the air and the two-phase organic pollutants to reach the preset temperature of the reactor;
the second stage is a fluidized bed reactor catalytic reaction stage, wherein introduced gas-liquid two-phase organic pollutants and air are mixed and then enter the fluidized bed reactor, catalytic oxygen cracking is carried out in the reactor under the action of a catalyst, the organic pollutants are converted into carbon dioxide, water and other pollution-free substances, and the Cu/Ce catalyst is filled, and the particle size distribution of the catalyst is 180 mu m;
the third stage is a fixed bed reactor catalytic reaction stage, unreacted materials and reactants after the catalytic reaction in the second stage are introduced into the fixed bed reactor for deep catalytic reaction, the two-step reaction generates a large amount of heat for vaporizing the reactants and the products, and the residual heat preheats the feeding materials through a heat exchange stage so as to reduce the energy consumption and enable the initial materials to quickly reach the reaction temperature;
the fourth stage is a condensation separator stage for realizing gas-liquid separation, and the condensate discharged from the bottom and the tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard of 80mgO2The emission standard of the exhaust gas and the L is 120mg/m3。
And (3) constructing a steady-state model for treating acrylic acid organic pollutants. The main catalytic reaction and reaction kinetic parameters for treating the organic pollution of the acrylic acid are as follows:
K＝4.18×1021,E＝186834kJ/kmol
K＝6.6568×1010,E＝101236kJ/kmol
K＝5.4694×1023,E＝187833kJ/kmol
the mass fraction (%) of the A, B, C, D components of the feed stream is shown in Table 1
TABLE 1
The steady-state model is established by using process simulation software in combination with process design, and the parameters of the process design units are shown in Table 2
TABLE 2
As shown in fig. 3, the establishment of a dynamic model for treating the edge side acrylic acid organic pollutants. 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 sizes of all equipment are specified, and the like, a control system is designed by adopting a multivariable control method, and different controllers are arranged at different equipment and flow sections and are converted into a dynamic model.
The feeding proportion control is characterized in that a proportion controller FC (101, 102, 103, 104) is arranged between air feeding and 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 the gas-liquid flash tank, the pressure controllers PC (201, 202 and 203) are arranged between the fluidized bed and the fixed bed reactor, and the output of the controllers is the valve opening of a pressure control valve in the dynamic model;
the liquid level control is that a liquid level controller LC (401) is arranged in the gas-liquid flash tank, and the output of the controller is the valve opening of a liquid level control valve in a dynamic model;
the temperature control is carried out by providing a self-feedback type temperature controller TC (301, 302) in the reactor, and providing a heat transfer controller TC (303, 304) in the reactor, the output of which is the valve opening of the temperature control valve in the dynamic model.
The tuning parameters and the action directions of the controllers at each control site are shown in Table 3
TABLE 3
| Proportional gain | Integration time (min) | Direction of action | |
| FC101 | 0.5 | 0.3 | Inverse direction |
| FC102 | 0.5 | 0.3 | Inverse direction |
| FC103 | 0.5 | 0.3 | Inverse direction |
| FC104 | 0.5 | 0.3 | Inverse direction |
| PC201 | 20 | 12 | Is just |
| PC202 | 20 | 12 | Is just |
| PC203 | 20 | 12 | Is just |
| PC204 | 20 | 12 | Is just |
| TC301 | 5 | 0.5 | Inverse direction |
| TC302 | 5 | 0.5 | Inverse direction |
| TC303 | 5 | 0.5 | Inverse direction |
| TC304 | 5 | 0.5 | |
| LC401 | |||
| 2 | 9999 | Is just |
And after the establishment of the dynamic model for treating the edge side acrylic acid organic pollutants is completed, transmitting data of the edge side dynamic model to the central cloud industrial operating system. Dynamic simulation data are 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 method comprises the following specific steps:
1) in the process simulation software, Variables to be read and written are derived by using a sub tool bar 'On Line Links …' under 'Tools' in the tool bar, wherein a first Input Variables column is an Input variable, and a second Output Variables column is an Output variable. Eable at the lower part of the page is selected as On.
2) The OPC Server software can realize the reading and writing of each variable parameter of the process in the process simulation software. And exporting the edited variables needing to be read and written in the steps to a label page of an acrylic acid organic pollutant treatment process flow 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 process simulates data, and the data can be correctly and stably read and written.
3) And collecting data from OPC Server software by using data collector software. The method for realizing the data acquisition of the OPC Server acrylic acid organic pollutant treatment process flow needs three steps, wherein the first step is the establishment of an acquisition source point, and the establishment method comprises the following steps: (1) clicking a < + newly-added button of a 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 button < change >, expanding the OPC server, and inputting < OPA service address > as 'localhost'; (4) < OPC DA service option > is selected as "opc.simulation.1"; (5) automatically generating an OPC server path; (6) clicking a radio button of the protocol version, and selecting a protocol version V2.0 corresponding to the OPC server; (7) selecting a disconnection reconnection mode, and selecting disconnection reconnection by default; (8) selecting reconnection interval as 30 s; (9) the clock source selects the local time; (10) setting the delay request to 5 s; (11) setting the updating rate to 1000 ms; (12) setting the read-write state as read-write; (13) click the < save > button.
The second step is the introduction of the collection site, and the specific implementation way is as follows: the OPC drives the batch import function of the support bit number, after the source point information is configured, (1) clicking to enter a [ bit number batch import ] tab, and expanding bit number batch import information; (2) clicking < enumerate bit number >, the system will enumerate the bit number information corresponding to the source point automatically; (3) selecting a bit number to be introduced, namely a variable needing to be read and written in a label page of an acrylic acid organic pollutant treatment process flow in OPC Server software, and clicking < introduction >; (4) the "tag management" page will import all the bit numbers of the source point.
And the third step is that the collector is accessed into an industrial operation system. As shown in fig. 4, the operation steps of accessing the industrial operating system are as follows: (1) entering an administrator setting page, and acquiring new authentication of clicking < + > buttons under a node management/authentication management page; inputting name, responsible person, company address, company name and description, clicking a < generation > button to automatically generate UUID, selecting a common collector for type selection, clicking < determination > and setting an authentication state as 'to be accessed'; (2) at the collector software end, a system information management/system configuration management page is used for inputting a name, an industrial operating system server address, a UUID generated by the industrial operating system end, a communication port 32568, a data uploading mode is TCP, a < save > button is clicked, and an 'operation success' dialog box is popped up; collecting a node management/state management page at an industrial operating system end, and checking that the authentication state is 'to be audited'; (3) after information is expanded, clicking an agreement button to agree with the access of a collector; displaying the connection state of the collector software end to display the connection success; the authentication management state at the industrial operating system end shows that the authentication is approved and the authentication is finished; (4) and clicking a collector row to expand a source point state tab under an industrial operating system [ collection node management/state management ], so that the source point state of the collector can be checked. Managing a data acquisition device; (5) and the object instance binds the data source to acquire data.
Therefore, bidirectional data transmission between the edge dynamic model and the central cloud industrial operating system can be completed.
As shown in fig. 5, an acrylic acid organic pollutant treatment optimization management and control system is newly built on an industrial operation system platform. Establishing acrylic acid organic pollutant treatment optimization management control APP in an industrial operation system APP designer, releasing a Web version, and embedding the Web version into the platform through an industrial operation system in a webpage component module mode. The control interface is provided with a real-time data interface for each parameter of the process, a monitoring interface, an intelligent optimization interface, a feeding fluctuation interface, a pollution emission real-time VOC and COD monitoring interface. When setting a real-time data interface, a monitoring interface, a feeding fluctuation interface and a pollution emission real-time VOC and COD monitoring interface of each parameter of the process, firstly calling a self-contained control of an industrial operating system, and then debugging for use. 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 dynamic model at the edge side, a differential evolution algorithm is adopted to carry out multi-objective optimization calculation on the dynamic model, the 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 reactor reaction efficiency, the catalytic reaction efficiency of a fluidized bed and a fixed bed reactor of a two-phase catalytic cracking reactor is taken as a first objective function F (1) and a second objective function F (2) according to the ratio of the content of each organic pollutant before and after reaction in unit time.
F(1)＝V1＝m1a/m1b (1)
F(2)＝V2＝m2a/m2b (2)
Wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutants in the fluidized bed reactor, m1aM is the content of acrylic acid organic pollutants before entering a fluidized bed reactor1bThe content of acrylic acid organic pollutants after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency of acrylic acid organic pollutants in a fixed bed reactor, m2aM is the content of acrylic acid organic pollutants before entering a fixed bed reactor2bIs the content of acrylic acid organic pollutants after flowing out of the fixed bed reactor.
In order to solve the problem of total energy consumption of the process, the total process energy consumption is taken as a third objective function F (3). The specific total energy consumption calculation formula is as follows:
∑P＝Pf+Pc+Pp+Pr1+Pr2 (3)
wherein, Σ P, Pf,Pc,Pp,Pr1,Pr2Respectively shows the total energy consumption effective power of an organic pollution treatment process in the industrial production of acrylic acid, 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 temperature regulating equipment of a fluidized bed reactor and the effective power of temperature regulating equipment of a fixed bed reactor.
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 flash tank power efficiency is 70%, the water pump power efficiency is 65%, the air compressor efficiency is 60%, the fluidized bed reactor temperature regulating device efficiency is 75%, and the fixed bed reactor temperature regulating device efficiency is 65%.
Wherein, the sigma P1 represents the total energy consumption of the organic pollution treatment process in the acrylic acid industrial production.
In order to meet the national emission standard, the COD of the treated wastewater and the VOC content of the waste gas are taken as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80 (5)
0≤G(2)＝VOC≤120 (6)
wherein, COD and VOC respectively represent COD of the waste water and VOC content in the waste gas.
The feed ratio of air to organic contaminants of acrylic acid, the fluidized bed reactor temperature and the fixed bed reactor temperature were used as decision variables. Expressions (1), (2) and (4) are used as objective functions, and expressions (5) and (6) are used as constraint conditions.
As shown in fig. 6, the maximum values of the objective functions F (1), F (2) and the minimum value of F (3) are iteratively solved by using a differential evolution algorithm method. The parameters of the differential evolution algorithm are as follows: the population size NP is 50, the variation factor F is 0.63, the crossover probability CR is 0.32, and the maximum number of iterations GMAX is 100.
And (3) supposing that optimization operation is performed every five minutes, after iterative operation of the multi-objective optimization algorithm, the optimal decision variable is written back to the decision variable port of the dynamic acrylic acid organic pollutant treatment model on the edge side through the bidirectional data transmission channel, so that real-time optimization is completed. Namely, the acrylic acid organic pollutant treatment optimization management control APP carries out real-time optimization on the process performance change caused by flow fluctuation and equipment lag effect, and writes back the process performance change to the acrylic acid organic pollutant dynamic model on the edge side to carry out a new cycle of acrylic acid organic pollutant process simulation operation.
The management and 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 variables exceeding a 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 manually setting material disturbance on a control interface, and after three minutes, restoring each parameter to a stable state again without working condition alarm. No matter whether the feeding fluctuation is added or not, the VOC content in the waste gas and the COD value in the waste liquid both meet the national emission requirements, and the comparison before and after the feeding fluctuation is shown in the following table. The invention can effectively overcome the disturbance of the feeding components and the flow rate by multi-loop control and multi-objective optimization aiming at the dynamic model at the edge side and normal operation of the working condition.
The above description explains the invention in detail in terms of process flow design, process variable multi-objective optimization, process flow dynamic design, simulated data transmission, intelligent optimization management and control platform establishment, and the like. But the invention can not only treat the acrylic acid organic pollutant, but also develop similar chemical production and byproduct resource utilization.
The exemplary embodiments of the present invention are described in terms of a series of steps or devices. However, the present invention 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, may be performed in an order different from the order in the embodiments, or may be performed simultaneously.
Other embodiments of the present application will be apparent to those skilled in the art from consideration of the specification and practice of the invention disclosed herein. This application is intended to cover any variations, uses, or adaptations of the invention 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 invention pertains. It is intended that the specification and examples be considered as exemplary only.
It will be understood that the present application is not limited to the precise arrangements described above and shown in the drawings and that various modifications and changes may be made without departing from the scope thereof. The scope of the application is limited only by the appended claims.
Claims (5)
1. The utility model provides a cloud limit collaborative optimization intelligence management and control system that organic pollutant was administered which this characterized in that: the system comprises the steps of designing the edge side organic pollutant aerobic cracking treatment process and establishing a dynamic model, establishing a center cloud organic pollutant treatment optimization management control APP module and transmitting data of the edge side and the center cloud in real time, wherein the specific process is as follows:
(1) aiming at the treatment process of the acrylic acid organic pollutants, the flow design of a heat exchanger, a fluidized bed reactor, a fixed bed reactor and a gas-liquid separator is carried out by adopting the temporary oxygen cracking treatment technology;
(2) based on a reaction kinetics equation and the process design in the step (1), firstly constructing an acrylic acid organic pollutant treatment steady-state model by using process 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 process simulation software again;
(3) analog data of an OPC Server software dynamic model is transmitted to collector software, and then the collector software is used for importing the data into a central cloud, namely an industrial operating system;
(4) designing a UI (user interface) of an acrylic acid organic pollutant treatment optimization management and control system on an industrial operation system; establishing an acrylic acid organic pollutant treatment optimization control APP module, wherein a control interface is provided with a real-time data interface, a monitoring interface, an intelligent optimization interface, a feeding fluctuation interface, a pollution emission real-time VOC (volatile organic compound) and COD (chemical oxygen demand) monitoring interface of each parameter of the process, and a real-time optimization control is added to the intelligent optimization interface; aiming at the problems of total energy consumption and reactor efficiency of the dynamic model at the edge side, carrying out multi-objective optimization calculation on the dynamic model by adopting a differential evolution algorithm to obtain an optimal optimization operation variable, and integrating the function into a real-time optimization control of an intelligent optimization interface;
(5) and (4) writing back data to the edge side dynamic model by using an instruction signal obtained after the acrylic acid organic pollutant treatment optimization management control APP through collector software and OPC Server software, and realizing the data bidirectional transmission of the edge side dynamic model and the center cloud optimization management control APP together with the step (3).
2. The cloud-edge collaborative optimization intelligent management and control system for organic pollutant remediation of claim 1, wherein: the treatment process design of the acrylic acid organic pollutants in the step (1) is mainly divided into 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, air is firstly introduced, the heat exchanger is used for carrying out reaction heat release of the fluidized bed reactor and the fixed bed reactor so as to heat the air and the two-phase organic pollutants to reach the preset temperature of the reactor;
the second stage is a fluidized bed reactor catalytic reaction stage, the introduced gas-liquid two-phase organic pollutants are mixed with air and then enter the fluidized bed reactor, and catalytic oxygen cracking is carried out in the reactor under the action of a catalyst to convert the organic pollutants into carbon dioxide, water and other pollution-free substances;
the third stage is a fixed bed reactor catalytic reaction stage, unreacted materials and reactants after the catalytic reaction in the second stage are introduced into the fixed bed reactor for deep catalytic reaction, the two-step reaction generates a large amount of heat for vaporizing the reactants and the products, and the residual heat preheats the feeding materials through a heat exchange stage so as to reduce the energy consumption and enable the initial materials to quickly reach the reaction temperature;
the fourth stage is a condensation separator stage for realizing gas-liquid separation, and the condensate discharged from the bottom and the tail gas discharged from the top respectively need to reach the national wastewater direct discharge standard of 80mgO2The emission standard of the exhaust gas and the L is 120mg/m3。
3. The cloud-edge collaborative optimization intelligent management and control system for organic pollutant remediation of claim 1, wherein: in the step (3), dynamic analog data is transmitted to collector software by using OPC Server software, and then the collector software is used to import 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 the setting of a dynamic model is finished, exporting variables needing to be read and written to OPC Server software;
(2) acquiring data by collector software: then, acquiring the derived dynamic model data in OPC Server software through collector software, and setting the derived simulation data in a collector to be capable of being read, written and stored in real time;
(3) data access acrylic acid organic pollutant treatment optimization management control APP firstly performs authentication management on an industrial operating system and collector software, and after the authentication management is completed, each piece of data in a collector is transmitted to a central cloud industrial operating system.
4. The cloud-edge collaborative optimization intelligent management and control system for organic pollutant remediation of claim 1, wherein: and (4) establishing an acrylic acid organic pollutant treatment optimization management control APP in an industrial operating system APP designer, releasing a Web version, and embedding the Web version into the platform through the industrial operating system in a webpage component module mode.
5. The cloud-edge collaborative optimization intelligent management and control system for organic pollutant remediation of claim 1, wherein: 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 a fluidized bed of the two-phase catalytic cracking reactor and the catalytic reaction efficiency of a fixed bed reactor are used as a first objective function F (1) and a second objective function F (2) according to the ratio of the total organic pollutant content before and after reaction in unit time;
F(1)＝V1＝m1a/m1b (1)
F(2)＝V2＝m2a/m2b (2)
wherein V1 is the catalytic reaction efficiency of acrylic acid organic pollutants in the fluidized bed reactor, m1aM is the content of acrylic acid organic pollutants before entering a fluidized bed reactor1bThe content of acrylic acid organic pollutants after flowing out of the fluidized bed reactor; v2 is the catalytic reaction efficiency of acrylic acid organic pollutants in a fixed bed reactor, m2aM is the content of acrylic acid organic pollutants before entering a fixed bed reactor2bThe content of acrylic acid organic pollutants after flowing out of the fixed bed reactor;
in order to solve the problem of total energy consumption of the process, 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＝Pf+Pc+Pp+Pr1+Pr2 (3)
wherein, Σ P, Pf,Pc,Pp,Pr1,Pr2Respectively showing total energy consumption effective power of an organic pollution treatment process in the industrial production of acrylic acid, effective power of each flash tank, effective power of each water pump, effective power of an air compressor, effective power of temperature regulating equipment of a fluidized bed reactor and effective power of temperature regulating equipment of a fixed bed reactor;
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 flash tank power efficiency is 70%, the water pump power efficiency is 65%, the air compressor efficiency is 60%, the fluidized bed reactor temperature regulating device efficiency is 75%, and the fixed bed reactor temperature regulating device efficiency is 65%.
Wherein, the sigma P1 represents the total energy consumption and power of the organic pollution treatment process in the industrial production of acrylic acid;
in order to meet the national emission standard, the COD of the treated wastewater and the VOC content of the waste gas are taken as constraint variables G (1) and G (2):
0≤G(1)＝COD≤80 (5)
0≤G(2)＝VOC≤120 (6)
wherein, COD and VOC respectively represent COD of the waste water and VOC content in the waste gas;
taking the feeding ratio of air and acrylic acid organic pollutants, the temperature of a fluidized bed reactor and the temperature of a fixed bed reactor as decision variables, taking expressions (1), (2) and (4) as objective functions, and taking expressions (5) and (6) as constraint conditions;
and (3) carrying out iterative solution on the maximum values of the objective functions F (1) and F (2) and the minimum value of the objective function F (3) by adopting a differential evolution algorithm method. The parameters of the differential evolution algorithm are as follows: the population size NP is 50, the variation factor F is 0.63, the crossover probability CR is 0.32, and the maximum number of iterations GMAX is 100.
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