Naphthalene water reducer production operation control method and control device

Abstract

The invention provides a naphthalene water reducer production operation control method and control device, and belongs to the technical field of concrete admixtures. The naphthalene water reducer production operation control method comprises the following steps: S1, setting various types of naphthalene water reducers and a plurality of production formulas respectively corresponding to the various types of naphthalene water reducers; s2, matching the actual type with various types of naphthalene water reducing agents to obtain an actual production formula corresponding to the actual type; and S3, monitoring the reaction kettle in real time according to the production process, controlling the temperature of the reaction kettle, and controlling corresponding production equipment and / or production materials to execute corresponding production operation when the temperature of the reaction kettle is matched with a corresponding reaction condition in one production process. The automatic operation rate of the device is improved through one-key start control, process formula management, temperature curve control and safety protection interlocking, manual operation links are reduced, and the stability, reliability, safety and automation of the device are improved.

Description

Technical Field

[0001] The present invention relates to the technical field of concrete admixtures, and in particular to a naphthalene-based water reducing agent production and operation control method and a control device. Background Art

[0002] Naphthalene-based water reducers are the most widely used water reducers in China. The general production process of naphthalene-based water reducers or homologous dispersants is to use industrial naphthalene and sulfuric acid for sulfonation reaction, and then condense with formaldehyde to generate naphthalenesulfonic acid formaldehyde condensate, and finally neutralize with alkali solution to generate the corresponding naphthalene-based water reducer. Due to the sharp rise in the supply price of the main raw material industrial naphthalene, water reducer manufacturers have begun to gradually improve the production process and reduce costs. At present, the most common practice is to use cheap naphthalene homologous series to replace industrial naphthalene, such as methylnaphthalene, naphthalene oil, washing oil, acenaphthene, anthracene oil, etc. At the same time, with the further improvement of the requirements of high-performance concrete for the water-reducing performance, dispersing performance and slump retention performance of high-efficiency water reducers, people pay more and more attention to the modification and compounding of naphthalene-based water reducers, resulting in a variety of preparation methods for naphthalene-based water reducers. The existing patents for the production of naphthalene-based water reducers are mainly aimed at the improvement of naphthalene-based water reducer production equipment, or the preparation method of modified naphthalene-based water reducers, or the simple command control of key parameters such as feed and temperature during the production process. In the existing technology of naphthalene-based water reducers and their homologous dispersants production processes, they are all intermittent manual or semi-automatic production operations, and no overall automatic control solution for the naphthalene-based water reducer production process has been found. Summary of the invention

[0003] In order to solve the above problems, the embodiments of the present application provide a naphthalene-based water reducer production operation control method and control device.

[0004] In a first aspect, the present application provides a naphthalene-based water reducer production operation control method, comprising the following steps: S1: setting a plurality of types of naphthalene-based water reducers and a plurality of production formulas corresponding to the plurality of types of naphthalene-based water reducers, wherein the production formulas include a plurality of production processes that are run in sequence, production equipment corresponding to a production process, production materials corresponding to a production process, material amounts corresponding to production materials in a production process, and reaction conditions corresponding to a production process, wherein the production equipment includes a reactor; S2: obtaining the actual type of the current naphthalene-based water reducer, respectively retrieving multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, matching the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; S3: When all the production equipment are connected according to the set connection method and the production start instruction is obtained, the corresponding multiple production processes are obtained according to the actual production formula and the corresponding production operations are performed in sequence according to the order of the multiple production processes. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction conditions in a production process, the corresponding production equipment and / or production materials are controlled to perform the corresponding production operation.

[0005] Preferably, step S1 specifically includes: S11: Set various types of naphthalene-based water reducers; S12: selecting a type of naphthalene-based water reducer from a plurality of types of naphthalene-based water reducers; S13: setting the production formula of the naphthalene-based water reducer of this type; S14: Return to step S12 until the production formulas corresponding to all types of naphthalene-based water reducers are set.

[0006] Step S13 specifically includes: S131: Set the production equipment used in the production formula; S132: Setting the type, properties and amount of raw materials used in the production formula; S133: setting specific operation steps of melting, sulfonation, hydrolysis, condensation, neutralization and drying in the production formula; S134: setting corresponding process parameters in multiple production processes, wherein the process parameters include material preparation weight, material preparation temperature, material feeding weight, material feeding time, reaction temperature, reaction acid concentration, reaction material viscosity, reaction time, discharge temperature, and discharge time.

[0007] Preferably, monitoring and controlling the real-time temperature of the reactor according to the production process in step S3 includes: obtaining the corresponding process parameters of the reactor in a preset operation stage according to the actual production formula, detecting the real-time temperature of the reactor in the preset operation stage, obtaining corresponding PID control information according to the process parameters and the real-time temperature, and controlling the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

[0008] Preferably, obtaining the process parameters corresponding to the reactor in different operation stages according to the actual production formula specifically includes: dividing the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtaining the process parameters corresponding to the reactor in each temperature control operation stage according to the multiple production processes; setting corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and operating the reactor in sequence according to the multiple production processes corresponding to the jump conditions of each temperature control operation stage, and outputting the corresponding preset temperature control operation stage when the reactor is in a temperature control operation stage and meets the jump conditions corresponding to the temperature control operation stage; obtaining the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage in which the reactor is located.

[0009] Preferably, detecting the real-time temperature of the reactor in the preset operation stage, and obtaining the corresponding PID control information according to the process parameters and the real-time temperature specifically includes: the process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage, and planning the target temperature curve corresponding to the temperature control operation stage according to the initial temperature, the end temperature, and the time setting of the temperature control operation stage; detecting multiple continuous real-time temperatures of the reactor in the temperature control operation stage, obtaining the temperature change rate corresponding to the temperature control operation stage according to the multiple continuous real-time temperatures, obtaining the temperature setting value of the reactor at the first preset time according to the target temperature curve, obtaining the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time, and inputting the temperature difference and the temperature change rate into the PID controller to obtain the corresponding PID control information.

[0010] Preferably, step S3 also includes: monitoring the real-time operating status of the production equipment, safely interlocking the alarm information and troubleshooting operations of the production equipment, and issuing an alarm message and executing corresponding troubleshooting operations when the real-time operating status of the production equipment matches the fault information.

[0011] In a second aspect, the present application provides a naphthalene-based water reducer production operation control device, comprising: A formula setting component is used to set multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers; the production formula includes multiple production processes that run in sequence, production equipment corresponding to one production process, production materials corresponding to one production process, material dosage corresponding to the production materials in one production process, and reaction conditions corresponding to one production process, and the production equipment includes a reactor; A formula matching component is used to obtain the actual type of the current naphthalene-based water reducer, respectively retrieve multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, and match the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; The production control component is used to obtain the corresponding multiple production processes according to the actual production formula and execute the corresponding production operations in the order of the multiple production processes when all the production equipment are connected according to the set connection method and the production start instruction is obtained. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction conditions in a production process, the corresponding production equipment and / or production materials are controlled to execute the corresponding production operation.

[0012] Preferably, the production control component includes The temperature curve management module is used to obtain the corresponding process parameters of the reactor in the preset operation stage according to the actual production formula; The temperature curve control module is used to detect the real-time temperature of the reactor in the preset operation stage, obtain the corresponding PID control information according to the process parameters and the real-time temperature, and control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

[0013] Preferably, the temperature curve management module includes A stage division unit is used to divide the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtain the corresponding process parameters of the reactor in each temperature control operation stage according to the multiple production processes; The stage jump unit is used to set corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and according to the corresponding jump conditions of each temperature control operation stage, the reactor is operated in sequence according to its corresponding multiple production processes, and when the reactor is in a temperature control operation stage and meets the corresponding jump conditions of the temperature control operation stage, the corresponding preset temperature control operation stage is output; The parameter acquisition unit is used to acquire the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage of the reactor.

[0014] Preferably, the temperature curve control module includes The process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage; A curve planning unit is used to plan a target temperature curve corresponding to the temperature control operation stage according to the initial temperature, end temperature and time setting of the temperature control operation stage; A detection unit, used to detect a plurality of continuous real-time temperatures of the reactor in the temperature control operation stage; A calculation and acquisition unit, used to obtain the temperature change rate corresponding to the temperature control operation stage according to a plurality of continuous real-time temperatures, obtain the temperature setting value of the reactor at the first preset time according to the target temperature curve, and obtain the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time; A PID information acquisition unit, used to input the temperature difference and the temperature change rate into the PID controller to obtain corresponding PID control information; The control unit is used to control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

[0015] The beneficial effects of the present invention are as follows: a plurality of production formulas corresponding to a plurality of types of naphthalene-based water reducers are set, an actual production formula corresponding to the current naphthalene-based water reducer is obtained according to the actual type of the current naphthalene-based water reducer, a plurality of corresponding production processes are obtained according to the actual production formula, corresponding production operations are sequentially performed in the order of the plurality of production processes, a reactor is monitored in real time according to the production process and the temperature of the reactor is controlled, when the temperature of the reactor matches the corresponding reaction condition in a production process, corresponding production equipment and / or production materials are controlled to perform corresponding production operations, and a multi-formula production process of the naphthalene-based water reducer is fully automatically controlled, and in the process of using industrial naphthalene or its homologues as production raw materials to produce a naphthalene-based water reducer or its homologues dispersant with multiple formulas, automatic operation of steps such as material preparation, material mixing, reaction, and material transfer of a reaction device and a one-key switching formula function for production scheduling are provided, the utilization rate and production efficiency of the equipment are improved, tasks and resources are reasonably allocated, production costs are reduced, manual operation links are reduced, energy consumption and labor intensity are reduced, and the influence of human factors on product quality is reduced, which is conducive to the stability of product quality. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0017] Figure 1 A schematic diagram of a process for controlling the production and operation of a naphthalene-based water-reducing agent provided in an embodiment of the present application; Figure 2 A schematic diagram of the structure of a naphthalene-based water-reducing agent production and operation control device provided in an embodiment of the present application; Figure 3A schematic diagram of a one-key start control panel for a sulfonation reaction in a naphthalene-based water-reducing agent production and operation control method provided in an embodiment of the present application; Figure 4 A schematic diagram of a one-button start control panel for a condensation reaction in a naphthalene-based water-reducing agent production and operation control method provided in an embodiment of the present application; Figure 5 A schematic diagram of a process recipe management panel in a naphthalene-based water-reducing agent production operation control method provided in an embodiment of the present application; Figure 6 A schematic diagram of a process recipe selection panel in a naphthalene-based water-reducing agent production operation control method provided in an embodiment of the present application; Figure 7 A schematic diagram of a sulfonation reaction temperature curve control panel in a naphthalene-based water-reducing agent production operation control method provided in an embodiment of the present application; Figure 8 A schematic diagram of a condensation reaction temperature curve control panel in a naphthalene-based water reducer production operation control method provided in an embodiment of the present application. DETAILED DESCRIPTION

[0018] The technical solutions in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application.

[0019] In the following introduction, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance. The following introduction provides multiple embodiments of the present application, and different embodiments can be replaced or combined, so the present application can also be considered to include all possible combinations of the same and / or different embodiments recorded. Therefore, if one embodiment includes features A, B, and C, and another embodiment includes features B and D, then the present application should also be considered to include embodiments containing one or more of all other possible combinations of A, B, C, and D, although the embodiment may not be clearly recorded in the following text.

[0020] The following description provides examples and does not limit the scope, applicability or examples set forth in the claims. Changes may be made to the functions and arrangements of the elements described without departing from the scope of the present application. Various processes or components may be appropriately omitted, substituted or added to each example. For example, the described method may be performed in an order different from the order described, and various steps may be added, omitted or combined. In addition, features described in some examples may be combined in other examples.

[0021] See also Figure 1 , 3 -8. In an embodiment of the present application, the method comprises the following steps: S1: setting a plurality of types of naphthalene-based water reducers and a plurality of production formulas corresponding to the plurality of types of naphthalene-based water reducers; the production formulas include a plurality of production processes that run in sequence, production equipment corresponding to a production process, production materials corresponding to a production process, material amounts corresponding to production materials in a production process, and reaction conditions corresponding to a production process, and the production equipment includes a reactor; S2: obtaining the actual type of the current naphthalene-based water reducer, respectively retrieving multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, matching the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; S3: When all the production equipment are connected according to the set connection method and the production start instruction is obtained, the corresponding multiple production processes are obtained according to the actual production formula and the corresponding production operations are performed in sequence according to the order of the multiple production processes. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction conditions in a production process, the corresponding production equipment and / or production materials are controlled to perform the corresponding production operation.

[0022] In the embodiment of the present application, in the production process, it involves defining, tracking and controlling different formulas of naphthalene-based water reducers. For naphthalene-based water reducers of different formulas, the production equipment used, the types of materials, properties and dosages used, the production process, and the reaction conditions are all different. Different equipment, materials, processes, and parameter compositions correspond to the formulas of naphthalene-based water reducers, where the processes include manual activities (manual confirmation, manual feeding, etc.) and automatic activities (DCS / PLC control implementation). Formulas are introduced to achieve standardization of the production process of naphthalene-based water reducers. According to the production plan, batches can be created by selecting the corresponding formula, and batches can be started and stopped with one key, effectively reducing the frequency of operations. In order to improve the stability and safety of the production process, ensure the uniformity of product quality, improve the yield of the target product, improve the processing capacity of the production device, and reduce the operating cost of the production process, the production process of naphthalene-based water reducers is autonomously operated and controlled, and the refined control and management of the production process are completed to stabilize product quality and ensure safe production.

[0023] In an embodiment of the present application, step S3 specifically includes: according to a production process, respectively obtaining corresponding production equipment or production materials or reaction conditions; if the first production equipment corresponding to the production process and the first production operation corresponding to the first production equipment are obtained according to the production process, then the first production equipment is controlled to perform the first production operation; if the production material corresponding to the production process, the actual usage corresponding to the production material, and the second production operation corresponding to the production material are obtained according to the production process, then the production material with the actual usage is controlled to perform the second production operation; if the preset reaction conditions corresponding to the production process and the second production equipment and the third production operation corresponding to the preset reaction conditions are obtained according to the production process, then the real-time reaction conditions of the second production equipment are obtained, and when the real-time reaction conditions match the preset reaction conditions, the second production equipment is controlled to perform the third production operation.

[0024] In the embodiment of the present application, a process embodiment of preparing naphthalenesulfonate water reducer is provided by using industrial naphthalene as the main raw material through the synthetic route of melting naphthalene → sulfonation → hydrolysis → condensation → neutralization → filtration → drying → product. An autonomous operation monitoring system for the production process of naphthalene-based water reducer is proposed. The synthetic process is to use industrial naphthalene or its homologues, concentrated sulfuric acid, formaldehyde and liquid alkali as the main raw materials, and to melt naphthalene, sulfonation reaction, hydrolysis reaction, condensation reaction, neutralization reaction to form liquid high-efficiency water reducer, and then dry to obtain naphthalene-based high-efficiency water reducer or its homologue dispersant product.

[0025] The following is a description of the production process for a naphthalene-based water reducer preparation method: Melt industrial naphthalene in a naphthalene melting kettle, and accurately add naphthalene into the sulfonation reactor. When the reaction temperature reaches the formula temperature requirement, start to drip sulfuric acid for sulfonation. During the sulfuric acid dripping process, control the material heating rate, control the dripping time according to the type of sulfuric acid, and control the maximum reaction temperature according to the type of naphthalene. After the sulfuric acid is dripped, control the material insulation temperature and insulation time according to the type of naphthalene; after the insulation is completed, first cool to the hydrolysis water temperature, slowly add hydrolysis water, stir evenly, and discharge the material to the condensation reactor. Before starting the condensation, the material in the reactor needs to be cooled to the formaldehyde addition temperature before starting to drip formaldehyde for condensation reaction. The dripping process controls the reaction time and the maximum reaction temperature; after the formaldehyde is dripped, start the insulation reaction, and control the insulation time, insulation temperature and appropriate amount of water during the insulation process to adjust the material viscosity. After the insulation reaction is completed, add an appropriate amount of wastewater to dilute and stir evenly, discharge the material to the neutralization tank, and add liquid alkali while discharging the material for neutralization reaction to obtain a liquid product.

[0026] In an embodiment of the present application, the plurality of production equipment may respectively be a naphthalene feed pump, a sulfuric acid metering tank, a clean water metering tank, a sulfonation reactor, a formaldehyde metering tank, a wastewater metering tank, a condensation reactor, a liquid alkali metering tank, and a neutralization tank. The instrument configuration related to the production equipment may include a reactor internal thermometer, a reactor pressure gauge, a reactor jacket inlet and outlet thermometers, a reactor nitrogen cut-off valve, a reactor steam regulating and cut-off valve, a reactor hydrophobic cut-off valve, a reactor circulating water inlet regulating valve, a reactor circulating water outlet cut-off valve, a reactor exhaust cut-off valve, a reactor drain cut-off valve, a reactor compressed air regulating and cut-off valve, a reactor sulfonation vent valve, a reactor sulfonation vent purge valve, a reactor feed vent valve, a reactor sulfonation feed vent purge valve, a reactor naphthalene feed cut-off valve, a reactor sulfuric acid feed regulating and cut-off valve, a reactor clean water feed cut-off valve, a reactor discharge valve, a reactor emergency discharge valve, and a reactor discharge steam purge valve. During the production of naphthalene-based water reducers, strict quality control of the reaction process is required. First, the raw materials need to be tested and the dosage determined according to their purity and quality. Secondly, the temperature, pressure, stirring speed and reaction time during the reaction need to be controlled to ensure that the reactants react fully. The key steps that affect product performance are sulfonation and condensation reactions. Due to the violent reactions, the operating conditions are relatively high. The operating conditions are also related to the safety of the process. The autonomous operation system for the production of naphthalene-based water reducers refers to improving the autonomous operation rate of the device through one-button start control, process formula management, temperature curve control, and safety interlocking, effectively reducing the number of operations and alarms, and improving the stability, reliability, safety and automation of the device.

[0027] In the embodiments of the present application, the prior art production processes of naphthalene-based water reducers and homologous dispersants thereof are all operated in intermittent manual or semi-automatic production. This patent provides a one-key start control method for a naphthalene-based water reducer production device. According to the naphthalene-based water reducer production formula process flow, the production formula process is constructed, and the real-time monitoring and operation of the on-site equipment is realized through program judgment or manual confirmation of the flowchart steps. The standardized process can not only help the operator replace the unconventional and manual operations in the production process of naphthalene-based water reducers with automatic program control, reduce misoperation, but also minimize the production fluctuations caused by differences in operator levels.

[0028] In the embodiment of the present application, the related program design of one-key start is: 1. Sulfonation automation operation steps: 1.1 "Preparing"; 1.2 "Preparing materials"; 1.3 "Nitrogen replacement, adding naphthalene"; 1.4 "Heating before adding sulfuric acid"; 1.5 "Adding sulfuric acid, keeping warm"; 1.6 "Cooling down"; 1.7 "Adding clean water"; 1.8 "Stirring, discharging materials"; 1.9 "Reaction is completed"; 2 Detailed description of sulfonation automation operation steps: 2.1 “Preparing” automation step description: After initialization, the valve will automatically reset and the step will enter preparation. You can start the one-key automatic program at any time.

[0029] 2.2 "Material preparation" automation step description: It is used for the batching process of sulfuric acid, industrial naphthalene and clean water in the metering tank. The feed weight is determined by the formula. When the one-key automatic start is on, if the actual weight is greater than the set weight, the high-level tank batching will skip the material preparation step and go to the next step.

[0030] 2.3 Explanation of the automated steps of “Nitrogen replacement and heating”: Nitrogen replacement must be carried out before feeding the reactor. The nitrogen filling time is determined according to the actual production situation. After the nitrogen replacement is completed, heating begins. When the heating weight reaches half of the set value, the stirring of the reactor starts automatically until heating is completed.

[0031] 2.4 "Temperature adjustment before sulfuric acid addition" automation step description: Due to the different sulfuric acid concentrations used in different formulas, the material temperature in the reactor before adding sulfuric acid is also different. The specific temperature is given in the formula, and the steam or cold water is automatically started to adjust the temperature to the temperature at which sulfuric acid can be added according to the given temperature and the actual temperature.

[0032] 2.5 “Add sulfuric acid, keep warm” automation step description: The sulfuric acid addition time and the heat preservation time are given by the formula. The program automatically controls the temperature in the reactor. When the heat preservation time is over, a button “end temperature control and discharge” will appear in the automation pop-up box. The operator manually determines whether the downstream condensation reactor can be fed, otherwise the sulfonation reactor will remain in the heat preservation stage.

[0033] 2.6 “Cooling down” automated step description: In this stage, cooling water is automatically used to cool down the machine in preparation for adding fresh water. The cooling temperature is given by the recipe.

[0034] 2.7 “Add clean water” automated step description: Add clean water according to the weight of the formula into the reactor for dilution. While adding clean water, cool the water to reduce the temperature.

[0035] 2.8 “Stirring and discharging” automated steps: When the temperature in the reactor reaches the cooling temperature, after standing and stirring for a period of time, first open the discharge valve, and allow the material in the reactor to flow into the condensation reactor for a certain period of time, then open the discharge steam pressure valve to press the material into the condensation reactor.

[0036] 2.9 “Reaction End” Automation Step Description: After the discharge is completed, wait for the next start. After the discharge is completed, the program will automatically jump to the pause state, and the step prompt will be “Reaction End”.

[0037] 3. Condensation automation operation steps: 3.1 “Preparing”; 3.2 “Preparing”; 3.3 “Adding clean water during preparing”; 3.4 “Lowering the temperature to the temperature for adding formaldehyde”; 3.5 “Adding formaldehyde, keeping warm and controlling the temperature”; 3.6 “Discharging”; 3.7 “Opening the pressure valve to discharge”; 3.8 “Condensation reaction is completed”.

[0038] 4 Detailed description of the condensation automation operation steps: 4.1 “Preparing” automation step description: After initialization, the valve will automatically reset and the step will enter preparation. You can start the one-key automatic program at any time.

[0039] 4.2 “Mixing” automation step description: The high-level tank mixes ingredients according to the formula settings. When the one-key automatic start is on, if the actual weight is greater than the set weight, the high-level tank batching will skip the preparation step and go to the next step.

[0040] 4.3 “Add clean water during batching” automation step description: When the batching is completed, the amount of clean water to be added is controlled according to the formula, and the amount is given by the formula.

[0041] 4.4 “Cooling down to the temperature for adding formaldehyde” automated step description: Before adding formaldehyde, the material temperature in the condensation kettle needs to be lowered to below the set value, which is given by the recipe.

[0042] 4.5 "Adding formaldehyde, keeping warm, and controlling temperature" automation step description: Control the formaldehyde dripping time, dripping temperature, keeping warm time, keeping warm temperature, and control the condensation kettle motor current ampere to control viscosity, and perform automatic control according to the pre-set settings. When the reaction is completed, a button "Temperature control ends and discharge" will appear in the automation pop-up box. The operator manually determines whether the discharge can be performed, otherwise the reactor will remain in the viscosity control stage.

[0043] 4.6 “Discharging” automation steps description: This stage mainly involves blowing out the discharging pipeline to ensure that the pipeline is unobstructed.

[0044] 4.7 "Open the steam pressure valve to discharge" automation step description: The discharge process controls the total amount of water added, the time for uniform stirring, the time for pressing, the time for purging, and the weight of flushing water. After the purging is completed, enter the discharge stage. During the discharge, press and hold the "discharge time" in the automation pop-up box. During the discharge process, open the pressure valve to ensure that the pressure in the reactor is greater than the "pressing" pressure in the automation pop-up box. When the discharge time is completed, add the wastewater of the "flushing weight" in the automation pop-up box to flush the pipeline. After the wastewater cleaning pipeline is completed, purge for a certain period of time.

[0045] 4.8 “Condensation reaction completed” automated step description: Condensation discharge is completed and waiting for the next start.

[0046] In one possible implementation, step S1 specifically includes: S11: Set various types of naphthalene-based water reducers; S12: selecting a type of naphthalene-based water reducer from a plurality of types of naphthalene-based water reducers; S13: setting the production formula of the naphthalene-based water reducer of this type; S14: Return to step S12 until the production formulas corresponding to all types of naphthalene-based water reducers are set.

[0047] Step S13 specifically includes: S131: Set the production equipment used in the production formula; S132: Setting the type, properties and amount of raw materials used in the production formula; S133: setting specific operation steps of melting, sulfonation, hydrolysis, condensation, neutralization and drying in the production formula; S134: setting corresponding process parameters in multiple production processes, wherein the process parameters include material preparation weight, material preparation temperature, material feeding weight, material feeding time, reaction temperature, reaction acid concentration, reaction material viscosity, reaction time, discharge temperature, and discharge time.

[0048] In the embodiment of the present application, the formula definition can be completed in the configuration period, allowing the user to define and describe different configuration options of the nylon-based water reducer formula, mainly for configuring the key equipment, materials, steps and process parameters that affect the product performance. In the operation period, the corresponding nylon-based water reducer formula can be simply selected, and the control parameters of the formula can be replaced with one click and imported into the control program, which is conducive to the execution of the production plan and the creation of batch production.

[0049] In one possible implementation mode, monitoring and controlling the real-time temperature of the reactor according to the production process in step S3 includes: obtaining corresponding process parameters of the reactor in a preset operation stage according to the actual production formula, detecting the real-time temperature of the reactor in the preset operation stage, obtaining corresponding PID control information according to the process parameters and the real-time temperature, and controlling the corresponding regulating valve to perform corresponding adjustment actions according to the PID control information to control the temperature of the reactor.

[0050] In an embodiment of the present application, process parameters are obtained, corresponding PID control information is obtained based on the process parameters and the real-time temperature, and the regulating valve is controlled to perform a regulating action based on the PID control information, thereby achieving precise control of the temperature of the reactor.

[0051] In one possible implementation, obtaining the process parameters corresponding to the reactor in different operating stages according to the actual production formula specifically includes: dividing the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtaining the process parameters corresponding to the reactor in each temperature control operation stage according to the multiple production processes; setting corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and operating the reactor in sequence according to the multiple production processes corresponding to the jump conditions of each temperature control operation stage, and outputting the corresponding preset temperature control operation stage when the reactor is in a temperature control operation stage and meets the jump conditions corresponding to the temperature control operation stage; obtaining the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage in which the reactor is located.

[0052] In the embodiment of the present application, the temperature curves of reactors with different formulations are different. The temperature control operation stages are divided according to the types of heating, insulation and cooling in multiple production processes, so that the entire production process can be divided into several temperature control operation stages according to the temperature rise type. At the same time, the single-stage temperature control operation stage will be further subdivided according to the operating process, reaction characteristics, control indicators, etc., which is conducive to fine control, so as to achieve fine control by further subdividing each temperature control operation stage according to control needs; after the temperature control operation stage is divided, the sequential control method is adopted to configure the jump conditions, jump targets and work tasks according to the temperature curve subdivision situation, so as to achieve automatic jump when the stage jump conditions are met. Go to the next stage and execute the corresponding operation instructions. The jump conditions are mainly divided into temperature, time, manual confirmation signal or compound conditions, etc. Each temperature control operation stage includes the corresponding stage parameters, each temperature control operation stage includes the stage name, number, temperature setting, time setting, valve setting, optimization algorithm parameter setting, support for the definition of parameter items and the support of the modification interface at the design time, and the stage parameters are provided for the subsequent planning of the target temperature curve. It is implemented by the parameter management module and will automatically call the stage parameters according to the current stage; in the temperature control operation stage, the control display stage number, temperature setting value, stage operation time, temperature change curve, valve control output, confirmation operation, fault alarm and other prompts. The purpose of the division is to construct a target temperature curve connected by multiple sections.

[0053] In one possible implementation mode, detecting the real-time temperature of the reactor in the preset operation stage, and obtaining corresponding PID control information according to the process parameters and the real-time temperature specifically includes: the process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage, and planning a target temperature curve corresponding to the temperature control operation stage according to the initial temperature, the end temperature, and the time setting of the temperature control operation stage; detecting multiple continuous real-time temperatures of the reactor in the temperature control operation stage, obtaining the temperature change rate corresponding to the temperature control operation stage according to the multiple continuous real-time temperatures, obtaining the temperature setting value of the reactor at the first preset time according to the target temperature curve, obtaining the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time, and inputting the temperature difference and the temperature change rate into the PID controller to obtain corresponding PID control information.

[0054] In the embodiment of the present application, a basic target curve is planned according to the initial temperature, end temperature and time setting of the temperature control operation stage, reflecting the target value of the main control parameter of the production process; then, the local shape of the basic target curve is optimized in combination with excellent batch production data and operating experience, that is, a target curve that meets the on-site production is planned; finally, a functional relationship between temperature and time is used: Proposed Parameter value of Timing the phases, is the initial time setting (usually 0), To set the time for the termination phase, is the initial temperature setting, is the termination temperature setting, and is the real-time temperature value. By collecting multiple continuous real-time temperature values, the internal algorithm determines the temperature waveform, which is divided into rising, falling, peak, trough and other states, and calculates the temperature change rate to calibrate the speed of temperature change. According to the specific process conditions, the input and output parameters of the controller are defined. The input signals of the controller are kettle temperature, kettle pressure, inlet and outlet temperature of the heat exchange structure, temperature and pressure of the heat exchange medium, and feed amount. The output signals are temperature regulation, pressure regulation and material regulation. In order to improve the quality and accuracy of the collected data, preprocessing of the data defined by the parameters is provided, including data cleaning, outlier removal, data smoothing and data normalization, etc., to provide a basis for subsequent controller optimization calculations. When developing the model, the appropriate parameter processing strategy should be selected according to specific needs and scenarios. The control algorithm and expert experience library are configured according to the specific process conditions. For the actuator that is a regulating valve, the fuzzy control PID control algorithm is mostly used. The corresponding fuzzy rules are clarified according to expert experience, and specific PID built-in parameters are calculated in real time to improve the controller's adaptability to on-site industrial scenarios. According to the current temperature setting value, temperature difference, and temperature change rate, the fuzzy rule table is configured to calculate the PID parameters Kp, Ki, and Kd. For actuators that are cut-off valves, the fuzzy control plus PWM (pulse width modulation) control method is mostly used. The output PID control quantity OUT is normalized and converted into a PWM duty cycle signal. The continuous output waveform is adjusted by opening and closing. By adjusting the duty cycle, a series of pulse output signals with equal amplitude and unequal width are output to control the temperature cut-off, pressure cut-off, and material cut-off switches. In addition, some expert strategies are added to integrate engineering experience and the experience of skilled operators into the control plan to solve some special working conditions and situations that require rapid response. Optimization controller: According to the operation characteristics and control requirements of sulfonation and condensation reactors, fuzzy multivariable control technology is combined with expert experience, with variables such as stirring frequency, steam opening, cold water opening as manipulated variables, and temperature, pressure, jacket outlet temperature, etc. in the reactor as controlled variables, and stage jump, parameter setting, curve formulation, parameter preprocessing, and optimization algorithm function block examples as means to overcome lag and interference factors and achieve stable control and optimization of temperature and pressure in the reactor. In order to ensure the smooth operation of the actuator, the switching between the on-site manual control output and the autonomous operation control system output must be non-disturbance, the on-site manual control output and the autonomous operation control system output track each other, and the actuator output is non-disturbance during the control mode switching process.

[0055] In one feasible implementation, step S3 also includes: monitoring the real-time operating status of the production equipment, safely interlocking the alarm information and troubleshooting operations of the production equipment, and issuing an alarm message and executing corresponding troubleshooting operations when the real-time operating status of the production equipment matches the fault information.

[0056] In the embodiments of the present application, the present application provides a method for setting a workshop alarm value and a workshop automation safety interlock and safety measures. Multiple production equipment may include a sulfonation reactor, a stirring element in the reactor, and a parking system. The fault information may be the upper temperature limit of the sulfonation reactor, the upper temperature limit of the sulfonation reactor, the temperature threshold of the sulfonation reactor, the sulfuric acid flow threshold of the sulfonation reactor, the jacket cooling water inlet threshold of the sulfonation reactor, and a stirring fault of the stirring element in the reactor; key supervision processes: the temperature and pressure of the sulfonation reactor are set with a high limit alarm, and the high and high limit interlock closes the sulfuric acid feed cut-off valve, closes the steam feed cut-off valve, automatically opens the cooling water inlet and outlet valves, and opens the two vent pipe cut-off valves at the same time; the temperature and sulfuric acid flow in the sulfonation reactor, the jacket cooling water inlet valve of the sulfonation reactor, and the stirring current in the reactor are interlocked; the stirring fault alarm is alarmed, and the feed and steam are cut off interlocked, and the cooling water is automatically opened; there is an emergency parking system, press the interlock to cut off the feed and steam, and automatically open the cooling water; the safety release system, the sulfonation reactors are equipped with bursting discs, the bursting pressure is set, and the bursting pipe is connected to the sulfonation tank.

[0057] In the embodiment of the present application, SIL rating: the sulfonation reactor is designed with two remote thermometers and two pressure transmitters, which are interlocked with the sulfuric acid feed cut-off valve, steam feed cut-off valve, and vent pipe cut-off valve respectively; the sulfuric acid feed regulating valve opening is adjusted according to the reactor temperature to control the reaction temperature; a cut-off valve is added to the naphthalene feed pipeline of the sulfonation reactor, and is interlocked with the sulfuric acid pipeline cut-off valve; naphthalene is added first, and then sulfuric acid is added dropwise to prevent the wrong order of material addition. HAZOP analysis: During the sulfonation reaction, each reactor's automatic feed valve is interlocked to prevent other reactors from entering the reactor during the charging process; the sulfonation reactor is set to interlock the stirring and sulfuric acid regulating valve, and set the current alarm; during condensation, the formaldehyde feed regulating valve is set to automatic control and interlocked with the temperature; the condensation reactor is set to interlock the stirring and formaldehyde regulating valve, and set the current alarm. Other settings are made by yourself: the sulfuric acid dripping regulating valve during sulfonation and the formaldehyde dripping regulating valve during condensation are set to have inconsistent feedback or fault alarm; nitrogen replacement is installed in the sulfonation and condensation reactors; the two sulfonation large release (venting) cut-off valves are interlocked, and at least one of them is open at the same time; the condensation reactor is equipped with two remote thermometers and a pressure transmitter, and the high-limit interlock cuts off the formaldehyde feed, opens the wastewater feed, cuts off the steam feed, and automatically opens the cooling water; a bursting disc is installed in the condensation, the bursting pressure is set, and the bursting pipe is connected to the sulfonation tank; when low negative pressure occurs in the sulfonation reactor, the nitrogen pipeline cut-off valve is opened to replenish nitrogen; when high negative pressure occurs, the steam pipeline regulating valve is opened to replenish steam.

[0058] In the embodiments of the present application, in the field of naphthalene-based water reducer production technology, the present application realizes automatic control and monitoring of the naphthalene-based water reducer preparation process through one-key start control, multi-formula management, temperature curve control and process safety interlocking, ensures product stability and production safety, and autonomous operation control of multi-formula production of naphthalene-based water reducer.

[0059] The following will be combined with the attached Figure 2 , a naphthalene-based water reducer production and operation control device provided in the embodiment of the present application is introduced in detail. It should be noted that the attached Figure 2 A naphthalene-based water-reducing agent production and operation control device is shown, which is used to execute the present application Figure 1 For the convenience of explanation, only the part related to the embodiment of the present application is shown. For the specific technical details not disclosed, please refer to the present application. Figure 1 The embodiment shown.

[0060] See also Figure 2 , Figure 2 Schematic diagram of a naphthalene-based water-reducing agent production and operation control device provided in an embodiment of the present application. Figure 2 As shown, the device comprises The formula setting part 201 is used to set multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers; the production formula includes multiple production processes that run in sequence, production equipment corresponding to one production process, production materials corresponding to one production process, material dosage corresponding to the production materials in one production process, and reaction conditions corresponding to one production process, and the production equipment includes a reactor; The formula matching component 202 is used to obtain the actual type of the current naphthalene-based water reducer, respectively retrieve multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, and match the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; The production control component 203 is used to obtain the corresponding multiple production processes according to the actual production formula and execute the corresponding production operations in sequence according to the order of the multiple production processes when all the production equipment are connected according to the set connection method and the production start instruction is obtained. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction condition in a production process, the corresponding production equipment and / or production materials are controlled to execute the corresponding production operation.

[0061] In one embodiment, the production control component 203 includes The temperature curve management module is used to obtain the corresponding process parameters of the reactor in the preset operation stage according to the actual production formula; The temperature curve control module is used to detect the real-time temperature of the reactor in the preset operation stage, obtain the corresponding PID control information according to the process parameters and the real-time temperature, and control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

[0062] In the embodiments of the present application, sulfonation and condensation reactions are typical intermittent production processes, which have typical strong time-varying, nonlinear and large hysteresis characteristics. In addition, the fine chemical industry requires high process precision, and conventional control methods are difficult to accurately control the temperature. For intermittent reactors, the present application provides a reactor temperature control solution that can solve the temperature control problem during sulfonation and condensation reactions. The reactor temperature curve optimization control solution includes a temperature curve management module and a temperature curve control module. The temperature curve management module is responsible for managing multiple parameters of the process curve, and the temperature curve control module is responsible for accurately controlling the reactor temperature.

[0063] In one possible implementation, the temperature curve management module includes A stage division unit is used to divide the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtain the corresponding process parameters of the reactor in each temperature control operation stage according to the multiple production processes; The stage jump unit is used to set corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and according to the corresponding jump conditions of each temperature control operation stage, the reactor is operated in sequence according to its corresponding multiple production processes, and when the reactor is in a temperature control operation stage and meets the corresponding jump conditions of the temperature control operation stage, the corresponding preset temperature control operation stage is output; The parameter acquisition unit is used to acquire the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage of the reactor.

[0064] In the embodiment of the present application, the temperature curve management module mainly includes the following functions: stage segmentation: according to the process operation flow, the entire production process is divided into several stages, and according to the control needs, each stage is further subdivided into stages to form a temperature control operation stage, so as to achieve refined control; stage connection: using the sequential control method, the jump conditions, jump targets and work tasks are configured according to the temperature curve segmentation, so that when the stage jump conditions are met, it automatically jumps to the next temperature control operation stage and executes the corresponding operation instructions; stage parameters: each stage includes the stage name, number, temperature setting, time setting, valve setting, optimization algorithm parameter setting, and supports the definition of parameter items at design time and the support of modification interface; stage operation: the operation process will display the number of stages, temperature setting value, stage operation time, total operation time, temperature change curve, valve control output, confirmation operation, fault alarm and other prompts.

[0065] In one embodiment, the temperature curve control module includes The process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage; A curve planning unit is used to plan a target temperature curve corresponding to the temperature control operation stage according to the initial temperature, end temperature and time setting of the temperature control operation stage; A detection unit, used to detect a plurality of continuous real-time temperatures of the reactor in the temperature control operation stage; A calculation and acquisition unit, used to obtain the temperature change rate corresponding to the temperature control operation stage according to a plurality of continuous real-time temperatures, obtain the temperature setting value of the reactor at the first preset time according to the target temperature curve, and obtain the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time; A PID information acquisition unit, used to input the temperature difference and the temperature change rate into the PID controller to obtain corresponding PID control information; The control unit is used to control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

[0066] In the embodiment of the present application, the temperature curve control module is responsible for the implementation of the intermittent reactor temperature curve optimization control algorithm. The algorithm used is fuzzy control or improved fuzzy multivariable control mode, which minimizes the dependence on the system model and accommodates multiple influencing factors. The reactor temperature control algorithm is executed on the basis of stage segmentation. Unlike the continuous production process, the actuators of each stage of the intermittent production process are different, and the control strategies or control parameters are also different. With the help of expert experience and optimization calculation and other technical means, a set of temperature optimization control composite algorithms are formed for the specific equipment and processes on site, and finally the temperature curve control requirements of the intermittent reaction device are realized.

[0067] In an embodiment of the present application, the initial temperature, final temperature, and time settings of each stage in the curve drawing unit can form a temperature curve with time as the horizontal axis and temperature as the vertical axis. The shape of the temperature curve from the initial temperature to the final temperature can be a straight line or a parabola. At this time, we can determine the functional relationship between temperature and time. The current temperature curve setting value can be calculated by the stage timing. The curve drawing unit is used to calculate the temperature curve setting value and input it into the temperature curve control module as the target input. The curve drawing unit combines the specific process parameter control requirements. The key parameters are the initial temperature, end temperature, time setting, etc. A basic target curve is planned according to the initial temperature, end temperature, and time setting of the temperature control operation stage, reflecting the target values ​​of the main control parameters of the production process; then, combined with excellent batch production data and operating experience, the local shape of the basic target curve is optimized, that is, a target curve that meets the on-site production is planned; finally, through a functional relationship between temperature and time: Proposed Parameter value of Timing the phases, is the initial time setting (usually 0), For stage time setting, is the initial temperature setting, is the termination temperature setting, and is the real-time temperature value. The calculation acquisition unit is used to monitor the current temperature change trend. According to the current temperature setting value, temperature difference, temperature change rate and fuzzy rule table, the PID information acquisition unit calculates the PID parameters Kp, Ki, and Kd.

[0068] In the embodiment of the present application, the PID information acquisition unit can define the input and output parameters of the controller according to the specific conditions of the process. The input signals of the controller are the kettle temperature, kettle pressure, inlet and outlet temperatures of the heat exchange structure, temperature and pressure of the heat exchange medium, and feed amount. The output signals are temperature regulation, pressure regulation, and material regulation. The data defined by the parameters can be preprocessed, including data cleaning, outlier removal, data smoothing, and data normalization, to provide a basis for subsequent controller optimization calculations. The control algorithm and expert experience library can be configured according to the specific conditions of the process. For actuators that are regulating valves, a fuzzy control PID control algorithm is adopted. The corresponding fuzzy rules are clarified based on expert experience, and specific PID built-in parameters are calculated in real time to improve the controller's adaptability to on-site industrial scenarios. For actuators that are cut-off valves, fuzzy control plus PWM (pulse width modulation) control methods are mostly used. According to the operation characteristics and control requirements of the sulfonation and condensation reactors, the control unit adopts a combination of fuzzy multivariable control technology and expert experience, with variables such as stirring frequency, steam opening, and cold water opening as manipulated variables, and the temperature, pressure, and jacket outlet temperature in the reactor as controlled variables. It uses stage jump, parameter setting, curve formulation, parameter preprocessing, and optimization algorithm function block examples as means to overcome lag and interference factors and achieve stable control and optimization of the temperature and pressure in the reactor. The temperature curve control module also includes a disturbance-free switching unit. To ensure the smooth operation of the actuator, the switching between the on-site manual control output and the autonomous operation control system output must be disturbance-free. The on-site manual control output and the autonomous operation control system output track each other. During the control mode switching process, the actuator output is disturbance-free.

[0069] The contents described above may be implemented individually or in combination in various ways, and these variations are all within the protection scope of the present invention.

[0070] It should be noted that, in the description of the present application, the terms "upper end", "lower end" and "bottom end" indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of the application is usually placed when in use, and are only for the convenience of describing the present application and simplifying the description, rather than indicating or implying that the device referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present application. Moreover, the terms "include", "comprise" or any other variant thereof are intended to cover non-exclusive inclusion, so that a process, method, article or device comprising a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article or device. In the absence of further restrictions, the elements defined by the sentence "includes a ..." do not exclude the presence of other identical elements in the process, method, article or device comprising the elements.

[0071] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit them. Although the present invention has been described in detail with reference to the above embodiments, a person skilled in the art should understand that the technical solutions described in the above embodiments can still be modified, or some of the technical features can be replaced by equivalents; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A naphthalene-based water reducer production operation control method, characterized in that: The steps include: S1: setting a plurality of types of naphthalene-based water reducers and a plurality of production formulas corresponding to the plurality of types of naphthalene-based water reducers, wherein the production formulas include a plurality of production processes that are run in sequence, production equipment corresponding to a production process, production materials corresponding to a production process, material amounts corresponding to production materials in a production process, and reaction conditions corresponding to a production process, wherein the production equipment includes a reactor; S2: obtaining the actual type of the current naphthalene-based water reducer, respectively retrieving multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, matching the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; S3: When all the production equipment are connected according to the set connection method and the production start instruction is obtained, the corresponding multiple production processes are obtained according to the actual production formula and the corresponding production operations are performed in sequence according to the order of the multiple production processes. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction conditions in a production process, the corresponding production equipment and / or production materials are controlled to perform the corresponding production operation.

2. A naphthalene-based water reducer production operation control method as claimed in claim 1, characterized in that: Step S1 specifically includes: S11: Set various types of naphthalene-based water reducers; S12: selecting a type of naphthalene-based water reducer from a plurality of types of naphthalene-based water reducers; S13: Setting the production formula of the naphthalene-based water reducer; S14: Return to step S12 until the production formulas corresponding to all types of naphthalene-based water reducers are set; Step S13 specifically includes: S131: Set the production equipment used in the production formula; S132: Setting the type, properties and amount of raw materials used in the production formula; S133: setting specific operation steps of melting, sulfonation, hydrolysis, condensation, neutralization and drying in the production formula; S134: setting corresponding process parameters in multiple production processes, wherein the process parameters include material preparation weight, material preparation temperature, material feeding weight, material feeding time, reaction temperature, reaction acid concentration, reaction material viscosity, reaction time, discharge temperature, and discharge time.

3. A naphthalene-based water reducer production operation control method as claimed in claim 1 or 2, characterized in that: In step S3, monitoring and controlling the real-time temperature of the reactor according to the production process includes: obtaining the corresponding process parameters of the reactor in a preset operation stage according to the actual production formula, detecting the real-time temperature of the reactor in the preset operation stage, obtaining corresponding PID control information according to the process parameters and the real-time temperature, and controlling the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

4. The naphthalene-based water reducer production operation control method according to claim 3, characterized in that: Obtaining the process parameters corresponding to the reactor in different operation stages according to the actual production formula specifically includes: dividing the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtaining the process parameters corresponding to the reactor in each temperature control operation stage according to the multiple production processes; setting corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and operating the reactor in sequence according to the corresponding multiple production processes according to the jump conditions corresponding to each temperature control operation stage, and outputting the corresponding preset temperature control operation stage when the reactor is in a temperature control operation stage and meets the jump conditions corresponding to the temperature control operation stage; obtaining the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage in which the reactor is located.

5. A naphthalene-based water reducer production operation control method as claimed in claim 4, characterized in that: Detecting the real-time temperature of the reactor in the preset operation stage, and obtaining corresponding PID control information according to the process parameters and the real-time temperature specifically includes: the process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage, and planning a target temperature curve corresponding to the temperature control operation stage according to the initial temperature, the end temperature, and the time setting of the temperature control operation stage; detecting multiple continuous real-time temperatures of the reactor in the temperature control operation stage, obtaining the temperature change rate corresponding to the temperature control operation stage according to the multiple continuous real-time temperatures, obtaining the temperature setting value of the reactor at the first preset time according to the target temperature curve, obtaining the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time, and inputting the temperature difference and the temperature change rate into the PID controller to obtain corresponding PID control information.

6. A naphthalene-based water reducer production operation control method as claimed in claim 1 or 2, characterized in that: Step S3 also includes: monitoring the real-time operating status of the production equipment, safely interlocking the alarm information and troubleshooting operations of the production equipment, and issuing an alarm message and executing corresponding troubleshooting operations when the real-time operating status of the production equipment matches the fault information.

7. A naphthalene-based water reducer production operation control device, characterized in that: include A formula setting component is used to set multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers; the production formula includes multiple production processes that run in sequence, production equipment corresponding to one production process, production materials corresponding to one production process, material dosage corresponding to the production materials in one production process, and reaction conditions corresponding to one production process, and the production equipment includes a reactor; A formula matching component is used to obtain the actual type of the current naphthalene-based water reducer, respectively retrieve multiple types of naphthalene-based water reducers and multiple production formulas corresponding to the multiple types of naphthalene-based water reducers, and match the actual type with the multiple types of naphthalene-based water reducers to obtain the actual production formula corresponding to the actual type; The production control component is used to obtain the corresponding multiple production processes according to the actual production formula and execute the corresponding production operations in the order of the multiple production processes when all the production equipment are connected according to the set connection method and the production start instruction is obtained. The reactor is monitored in real time according to the production process and the temperature of the reactor is controlled. When the temperature of the reactor matches the corresponding reaction conditions in a production process, the corresponding production equipment and / or production materials are controlled to execute the corresponding production operation.

8. A naphthalene-based water-reducing agent production and operation control device as claimed in claim 7, characterized in that: The production control component includes The temperature curve management module is used to obtain the corresponding process parameters of the reactor in the preset operation stage according to the actual production formula; The temperature curve control module is used to detect the real-time temperature of the reactor in the preset operation stage, obtain the corresponding PID control information according to the process parameters and the real-time temperature, and control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

9. A naphthalene-based water-reducing agent production and operation control device as claimed in claim 8, characterized in that: The temperature curve management module includes A stage division unit is used to divide the entire production process of the reactor into multiple temperature control operation stages according to multiple production processes, and obtain the corresponding process parameters of the reactor in each temperature control operation stage according to the multiple production processes; The stage jump unit is used to set corresponding jump conditions for each temperature control operation stage according to the process parameters of two adjacent temperature control operation stages, and according to the corresponding jump conditions of each temperature control operation stage, the reactor is operated in sequence according to its corresponding multiple production processes, and when the reactor is in a temperature control operation stage and meets the corresponding jump conditions of the temperature control operation stage, the corresponding preset temperature control operation stage is output; The parameter acquisition unit is used to acquire the process parameters corresponding to the temperature control operation stage according to the preset temperature control operation stage of the reactor.

10. A naphthalene-based water-reducing agent production and operation control device as claimed in claim 8, characterized in that: The temperature curve control module includes The process parameters include the initial temperature of the temperature control operation stage, the end temperature of the temperature control operation stage, and the time setting of the temperature control operation stage; A curve planning unit is used to plan a target temperature curve corresponding to the temperature control operation stage according to the initial temperature, end temperature and time setting of the temperature control operation stage; A detection unit, used to detect a plurality of continuous real-time temperatures of the reactor in the temperature control operation stage; A calculation and acquisition unit, used to obtain the temperature change rate corresponding to the temperature control operation stage according to a plurality of continuous real-time temperatures, obtain the temperature setting value of the reactor at the first preset time according to the target temperature curve, and obtain the temperature difference according to the temperature setting value and the real-time temperature of the reactor at the first preset time; A PID information acquisition unit, used to input the temperature difference and the temperature change rate into the PID controller to obtain corresponding PID control information; The PID control unit is used to control the corresponding regulating valve to perform corresponding regulating actions according to the PID control information to control the temperature of the reactor.

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