Process water system control method and device, storage medium and processor

Abstract

The invention relates to the field of chemical engineering, and discloses a process water system control method and device, a storage medium and a processor, and the method comprises the steps: obtaining the real-time flue gas flow, the real-time flue gas temperature, the real-time flushing water amount of a demister and the real-time spraying amount corresponding to a slurry circulating pump; inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time flushing water amount of the demister and the real-time spraying amount into a preset model to obtain the real-time flue gas evaporation amount of the desulfurizing absorption tower; determining the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system and the real-time water amount carried in gypsum discharged by the desulfurization system; and controlling the liquid level in the process water tank based on the real-time water consumption and the incoming water flow of the process water tank in the process water system. Based on the scheme, the process water of the desulfurization system can be guaranteed, and the situation of water supply interruption of the desulfurization system is avoided, so that the desulfurization process can be safely and stably carried out for a long time.

Description

Technical Field

[0001] The present invention relates to the field of chemical technology, and in particular to a process water system control method, a process water system control device, a machine-readable storage medium and a processor. Background Art

[0002] The wet flue gas desulfurization process usually involves a desulfurization system and a process water system, and flue gas desulfurization is achieved based on the cooperation between the desulfurization system and the process water system. The desulfurization system includes wet flue gas desulfurization related equipment, such as a desulfurization absorption tower, a slurry circulation pump, etc. The process water system is used to provide the desulfurization system with water used in the desulfurization process, such as water used for flushing the demister and water used to compensate for water loss in the desulfurization process.

[0003] In practical applications, the desulfurization system is generally operated under variable conditions, and the load changes are relatively drastic, resulting in large changes in process water consumption. Therefore, how to reasonably control the process water system is crucial for the long-term safe and stable operation of the desulfurization process. However, the current control method of the process water system cannot meet the needs of long-term safe and stable operation of the desulfurization process. Summary of the invention

[0004] The purpose of the present invention is to overcome the problem that the control method of the process water system in the prior art cannot meet the requirements of long-term safe and stable desulfurization process, and to provide a process water system control method, device, storage medium and processor.

[0005] In order to achieve the above object, the present invention provides a process water system control method in a first aspect, comprising:

[0006] Obtain real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume and real-time spray volume corresponding to the slurry circulation pump;

[0007] The real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume are input into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower;

[0008] Determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system;

[0009] Based on the real-time water consumption and the inflow flow of the process water tank in the process water system, the liquid level in the process water tank is controlled.

[0010] In an embodiment of the present application, the preset model is constructed based on the historical flue gas flow, historical flue gas temperature, historical demister flushing water volume, historical spray volume corresponding to the slurry circulation pump, and historical flue gas evaporation volume of the desulfurization absorption tower.

[0011] In the embodiment of the present application, the real-time water volume carried in the gypsum discharged from the desulfurization system is obtained based on the following formula:

[0012] H2Op=Hp×Wp×Sp×Dp×A×10 -3 ;

[0013] Among them, H2Op is the real-time water volume carried in the gypsum discharged from the desulfurization system, in m 3 / h; Hp is the real-time thickness of gypsum discharged from the desulfurization system, in m; Wp is the real-time width of gypsum discharged from the desulfurization system, in m; Sp is the real-time speed of the vacuum belt conveyor, in m / h; Dp is the real-time density of gypsum discharged from the desulfurization system, in kg / m 3 ; A is the real-time mass percentage of water in gypsum discharged from the desulfurization system.

[0014] In an embodiment of the present application, controlling the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system includes:

[0015] If the ratio of the incoming water flow rate to the real-time water consumption is less than 1, controlling the liquid level in the process water tank to a first liquid level;

[0016] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 1 but less than 2, controlling the liquid level in the process water tank to a second liquid level;

[0017] If the ratio of the incoming water flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is greater than a third liquid level, shut off the incoming water to the process water tank;

[0018] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is less than a fourth liquid level, turning on the incoming water of the process water tank;

[0019] Among them, the liquid level heights in the process water tank are from high to low: the third liquid level, the first liquid level, the second liquid level, and the fourth liquid level.

[0020] In an embodiment of the present application, the process water system includes a process water jellyfish pipeline, a plurality of process water tanks and a plurality of process water branch pipelines; the plurality of process water tanks correspond to the plurality of process water branch pipelines one by one, and the process water in each process water tank is respectively transported to the process water jellyfish pipeline through the corresponding process water branch pipeline, and is transported to the desulfurization system through the process water jellyfish pipeline, and each process water branch pipeline is provided with a process water pump; the control method also includes:

[0021] Obtaining the operating current of each process water pump, and calculating the average operating current based on the operating current of each process water pump;

[0022] The outlet pressure of each process water pump is controlled based on the target pressure, and the operating current of each process water pump is controlled based on the average operating current.

[0023] In the embodiment of the present application, the control method further includes:

[0024] The outlet pressure of each process water pump and the operating current of each process water pump are controlled alternately.

[0025] In the embodiment of the present application, the control method further includes:

[0026] Obtain the real-time operating frequency of each process water pump, and determine the rated current corresponding to each process water pump at its respective real-time operating frequency;

[0027] Based on the real-time operating current of each process water pump and the rated current corresponding to each process water pump, the current deviation value corresponding to each process water pump is calculated;

[0028] According to the current deviation value corresponding to each process water pump, the blockage condition of each process water branch pipeline is determined.

[0029] A second aspect of the present invention provides a process water system control device, comprising:

[0030] An acquisition module is used to obtain real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume, and real-time spray volume corresponding to the slurry circulation pump;

[0031] A prediction module, used for inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower;

[0032] A water consumption calculation module, used to determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system;

[0033] The control module is used to control the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system.

[0034] A third aspect of the present application provides a processor configured to execute the above-mentioned process water system control method.

[0035] A fourth aspect of the present application provides a machine-readable storage medium having instructions stored thereon, which, when executed by a processor, configure the processor to execute the above-mentioned process water system control method.

[0036] Through the above technical scheme, including: obtaining the real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume and real-time spray volume corresponding to the slurry circulation pump; inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spray volume into the preset model to obtain the real-time flue gas evaporation of the desulfurization absorption tower; determining the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation, the real-time wastewater volume discharged by the desulfurization system and the real-time water volume carried in the gypsum discharged by the desulfurization system; based on the real-time water consumption and the inflow of water in the process water tank in the process water system, controlling the liquid level in the process water tank. Based on the scheme provided in the embodiment of the present application, the process water of the desulfurization system can be guaranteed to avoid the interruption of water supply to the desulfurization system, which is conducive to the long-term safe and stable operation of the desulfurization process.

[0037] Other features and advantages of the embodiments of the present application will be described in detail in the subsequent specific implementation section. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] The accompanying drawings are used to provide a further understanding of the embodiments of the present application and constitute a part of the specification. Together with the following specific implementations, they are used to explain the embodiments of the present application, but do not constitute a limitation on the embodiments of the present application. In the accompanying drawings:

[0039] Figure 1 A schematic diagram of a process water system control method according to an embodiment of the present application is schematically shown;

[0040] Figure 2 A schematic diagram of a process flow of another process water system control method according to an embodiment of the present application is shown;

[0041] Figure 3 A schematic diagram of a process flow of another process water system control method according to an embodiment of the present application is shown;

[0042] Figure 4 The structure block diagram of a process water system control device according to an embodiment of the present application is schematically shown;

[0043] Figure 5 The internal structure of a computer device according to an embodiment of the present application is schematically shown.

[0044] Description of Reference Numerals

[0045] 410 - acquisition module; 420 - prediction module; 430 - water consumption calculation module; 440 - control module; A01 - processor; A02 - network interface; A03 - internal memory; A04 - display screen; A05 - input device; A06 - non-volatile storage medium; B01 - operating system; B02 - computer program. DETAILED DESCRIPTION

[0046] In order to make the purpose, technical scheme and advantages of the embodiments of the present application clearer, the technical scheme 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. It should be understood that the specific implementation methods described herein are only used to illustrate and explain the embodiments of the present application, and are not used to limit the embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of this application.

[0047] If there are descriptions involving "first", "second", etc. in the embodiments of the present application, the descriptions of "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or suggesting their relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In addition, the technical solutions between the various embodiments can be combined with each other, but they must be based on the ability of ordinary technicians in the field to implement them. When the combination of technical solutions is contradictory or cannot be implemented, it should be deemed that such a combination of technical solutions does not exist and is not within the scope of protection required by this application.

[0048] As described in the background technology, the wet flue gas desulfurization process usually involves a desulfurization system and a process water system, and flue gas desulfurization is achieved based on the cooperation between the desulfurization system and the process water system. Among them, the desulfurization system includes wet flue gas desulfurization related equipment, such as a desulfurization absorption tower, a slurry circulation pump, etc., and the process water system is used to provide the desulfurization system with water used in the desulfurization process, such as the water used for flushing the demister, and the water used to compensate for water loss in the desulfurization process. In actual applications, the desulfurization system generally operates under variable conditions, and the load changes are relatively drastic, resulting in large changes in the amount of process water used. Therefore, how to reasonably control the process water system is crucial for the long-term safe and stable operation of the desulfurization process. However, the current control method of the process water system cannot meet the needs of long-term safe and stable operation of the desulfurization process.

[0049] In view of this, an embodiment of the present application provides a process water system control method, such as Figure 1 As shown, the process water system control method may include the following steps:

[0050] Step 101, obtaining the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spray volume corresponding to the slurry circulation pump.

[0051] Wherein, the real-time flue gas flow rate and the real-time flue gas temperature can be measured at the flue gas inlet of the absorption tower.

[0052] Step 102, inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower.

[0053] The preset model can be used to characterize the correspondence between the flue gas evaporation amount of the desulfurization absorption tower and the flue gas flow rate, flue gas temperature, demister flushing water volume, and the spray volume corresponding to the slurry circulation pump. Furthermore, after obtaining the real-time flue gas flow rate, real-time flue gas temperature, real-time demister flushing water volume, and real-time spray volume corresponding to the slurry circulation pump under the current working conditions, the flue gas evaporation amount corresponding to the current flue gas flow rate, current flue gas temperature, current demister flushing water volume, and current spray volume can be obtained based on this correspondence. Among them, the flue gas evaporation amount is specifically the flow rate of water vapor discharged with the flue gas, and the real-time demister flushing water volume is specifically the flushing water flow rate. The slurry circulation pump is arranged on the slurry circulation pipeline between the desulfurization absorption tower kettle and the desulfurization absorption tower spray layer. The real-time spray volume corresponding to the slurry circulation pump is specifically the real-time spray volume corresponding to the slurry circulation pump in operation, and the spray volume is specifically the spray flow rate.

[0054] Since the flue gas evaporation amount of the desulfurization absorption tower is mainly related to the flue gas flow rate, flue gas temperature, demister flushing water volume, and the corresponding spraying amount of the slurry circulation pump, the embodiment of the present application establishes a corresponding relationship between the flue gas flow rate, flue gas temperature, demister flushing water volume, the corresponding spraying amount of the slurry circulation pump, and the flue gas evaporation amount of the desulfurization absorption tower.

[0055] In specific implementation, the preset model can be constructed based on the historical flue gas flow, historical flue gas temperature, historical demister flushing water volume, historical spray volume corresponding to the slurry circulation pump, and historical flue gas evaporation volume of the desulfurization absorption tower. Among them, the historical flue gas flow, historical flue gas temperature, historical demister flushing water volume, historical spray volume, and historical flue gas evaporation volume of the desulfurization absorption tower correspond to the same historical period. In specific implementation, the historical data of this historical period can be extracted from the DCS, and then the preset model can be obtained through neural network modeling and training. Considering that the demister flushing water volume may not be directly recorded in the DCS, but the switch state of the demister flushing valve is recorded. The demister flushing time can reflect the demister flushing water volume (the demister flushing water volume is proportional to the flushing time), and the demister flushing time is related to the switch state of the demister flushing valve. Therefore, in practical applications, the switch state of the demister flushing valve corresponding to the historical period can be extracted from the DCS, and then the historical demister flushing water volume of this historical period can be obtained.

[0056] In the embodiment of the present application, the flue gas evaporation amount of the desulfurization absorption tower can be regarded as a function of the flue gas flow rate, the flue gas temperature, the demister flushing water volume and the spray volume corresponding to the slurry circulation pump, as shown in the following formula (1):

[0057] Evp=f(Tin,Fin,Fcp,Fme) (1);

[0058] In the above formula (1), Evp is the flue gas evaporation amount of the desulfurization absorption tower, m 3 / h; f() represents function; Tin is flue gas temperature, unit is ℃; Fin is flue gas flow, unit is m 3 / h; Fcp is the spray volume corresponding to the slurry circulation pump, unit is m 3 / h; Fme is the demister flushing water volume, unit is m 3 / h.

[0059] Considering that there may be multiple desulfurization systems (one desulfurization system corresponds to one desulfurization absorption tower), the process water system is a common system that supplies water to multiple desulfurization systems at the same time. Therefore, in specific implementation, the real-time flue gas evaporation of the desulfurization absorption towers corresponding to each desulfurization system can be obtained according to the above scheme. For example, if there are two desulfurization systems, one desulfurization system corresponds to one desulfurization absorption tower, then the real-time flue gas evaporation corresponding to the two desulfurization towers can be obtained according to the above scheme.

[0060] Step 103, determining the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged from the desulfurization system, and the real-time water amount carried in the gypsum discharged from the desulfurization system.

[0061] Among them, the real-time wastewater volume discharged from the desulfurization system can be directly obtained through the online flow measurement point of DCS.

[0062] In the embodiment of the present application, the real-time amount of water carried in the gypsum discharged from the desulfurization system can be obtained based on the following formula (2):

[0063] H2Op=Hp×Wp×Sp×Dp×A×10 -3 (2);

[0064] In the above formula (2), H2Op is the real-time water content in the gypsum discharged from the desulfurization system, in units of m 3 / h; Hp is the real-time thickness of gypsum discharged from the desulfurization system, in m; Wp is the real-time width of gypsum discharged from the desulfurization system, in m; Sp is the real-time speed of the vacuum belt conveyor, in m / h; Dp is the real-time density of gypsum discharged from the desulfurization system, in kg / m 3 ; A is the real-time mass percentage of water in gypsum discharged from the desulfurization system.

[0065] In practical applications, the real-time thickness of the gypsum and the real-time speed of the vacuum belt conveyor can be obtained through the DCS online measurement point. The width of the gypsum is usually a fixed value and can be obtained through previous actual measurements, that is, the gypsum width obtained from previous actual measurements can be used as the real-time thickness of the gypsum. The density of the gypsum is usually a fixed value and can be obtained through previous actual measurements, that is, the gypsum density obtained from previous actual measurements can be used as the real-time density of the gypsum. The mass percentage of water in the gypsum is also usually a fixed value and can be obtained through previous actual measurements, that is, the mass percentage of water obtained from previous actual measurements can be used as the real-time mass percentage of water in the gypsum. For example, if the mass percentage of water in the gypsum obtained from previous actual measurements is 10%, then A in the above formula (2) can be set to 10%.

[0066] In the embodiment of the present application, the sum of the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system can be used as the real-time water consumption of the desulfurization system, as shown in the following formula (3):

[0067] C=Evp+H2Ow+H2Op (3);

[0068] In the above formula (3), C is the real-time water consumption of the desulfurization system, in m 3 / h; H2Ow is the real-time wastewater discharged from the desulfurization system, in m 3 / h.

[0069] In the case of multiple desulfurization systems, the real-time water consumption corresponding to each desulfurization system can be obtained according to the above scheme.

[0070] It can be understood that the real-time water consumption of the desulfurization system obtained based on the above scheme is the theoretical real-time water consumption of the desulfurization system. That is, the embodiment of the present application can predict the real-time water consumption of the desulfurization system, based on which the process water system can be controlled in advance and in time to ensure the process water of the desulfurization system, thereby alleviating the lag of the control of the process water system in the prior art to a certain extent.

[0071] Step 104: Control the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system.

[0072] In the embodiment of the present application, the controlling of the liquid level in the process water tank based on the real-time water consumption and the inflow flow of the process water tank in the process water system may include: if the ratio of the inflow flow to the real-time water consumption is less than 1, controlling the liquid level in the process water tank to a first liquid level; if the ratio of the inflow flow to the real-time water consumption is greater than or equal to 1 but less than 2, controlling the liquid level in the process water tank to a second liquid level; if the ratio of the inflow flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is greater than a third liquid level, closing the inflow of the process water tank; if the ratio of the inflow flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is less than a fourth liquid level, opening the inflow of the process water tank. The liquid level height corresponding to the third liquid level is higher than the liquid level height corresponding to the first liquid level, the liquid level height corresponding to the first liquid level is higher than the liquid level height corresponding to the second liquid level, and the liquid level height corresponding to the second liquid level is higher than the liquid level height corresponding to the fourth liquid level. That is, the liquid level heights in the process water tank are, from high to low, the third liquid level, the first liquid level, the second liquid level, and the fourth liquid level.

[0073] The inflow flow rate of the process water tank is specifically the flow rate of water supplied to the process water tank. The process water tank is usually provided with a corresponding water supply pipeline to supply water to the process water tank, and the water supply pipeline is provided with a process water supply valve. In specific implementation, the inflow flow rate used for comparison with the real-time water consumption can be specifically the flow rate corresponding to the maximum opening of the process water supply valve.

[0074] Then, the ratio of the incoming water flow rate to the real-time water consumption is specifically the ratio of the flow rate corresponding to the maximum opening of the process water replenishment valve to the real-time water consumption. In practical applications, the ratio of the flow rate corresponding to the maximum opening of the process water replenishment valve to the real-time water consumption can be obtained based on the following formula (4):

[0075] K = Fmax / C (4);

[0076] In the above formula (4), K is the ratio of the flow rate corresponding to the maximum opening of the process water supply valve to the real-time water consumption, which can also be called the liquid level compensation coefficient; Fmax is the flow rate corresponding to the maximum opening of the process water supply valve, in units of m 3 / h.

[0077] When the liquid level compensation coefficient K is less than 1, it means that the water balance between the current desulfurization system and the process water system has been destroyed, and the real-time water consumption of the desulfurization system is large. At this time, the liquid level in the process water tank can be controlled at a higher level (i.e., the first liquid level) to meet the water supply of the desulfurization system. In specific control, PID can be used to control the liquid level of the process water tank according to the first liquid level. In practical applications, in response to the liquid level compensation coefficient K being less than 1, an alarm can also be issued, and the above control measures can be taken in time to avoid water outages in the desulfurization system.

[0078] When 1≤K<2, it means that there is a risk of the water balance between the current desulfurization system and the process water system being destroyed. At this time, the liquid level in the process water tank can be controlled at the middle liquid level (i.e., the second liquid level) to meet the water supply of the desulfurization system and avoid the destruction of the water balance. In specific control, PID can be used to control the liquid level of the process water tank according to the second liquid level.

[0079] When K≥2, it means that the water supply mode of the current process water system can basically meet the water demand of the desulfurization system. At this time, the liquid level in the process water tank can be intermittently controlled, that is, if the liquid level in the process water tank is greater than the third liquid level, the water inlet of the process water tank is closed (that is, the process water replenishment valve is closed), and if the liquid level in the process water tank is less than the fourth liquid level, the water inlet of the process water tank is opened (that is, the process water replenishment valve is opened).

[0080] In practical applications, the specific heights of the first liquid level, the second liquid level, the third liquid level and the fourth liquid level can be set according to actual conditions. For example, if the full load level of the process water tank is 6m, the first liquid level can be set to 5m, the second liquid level can be set to 3m, the third liquid level can be set to 5.5m, and the fourth liquid level can be set to 2m.

[0081] In addition, in the actual control process, the above three control strategies can be automatically switched according to the change of the liquid level compensation coefficient K.

[0082] Considering that the process water system may include multiple process water tanks, the process water in each process water tank is transported to the process water pipe through its corresponding process water branch, and then transported to the desulfurization end by the process water pipe. In order to reasonably control the liquid level in each process water tank, in the specific implementation, the real-time water consumption of the desulfurization end can be divided by the number of process water tanks to obtain the average real-time water consumption of a single process water tank. Then, for any process water tank, the liquid level in the process water tank is controlled according to the average real-time water consumption and the water flow rate of the process water tank; the specific control process can refer to the above content and will not be repeated here. Among them, when the desulfurization end includes a desulfurization system, the real-time water consumption of the desulfurization end is the real-time water consumption of this desulfurization system; when the desulfurization end includes multiple desulfurization systems, the real-time water consumption of the desulfurization end is the sum of the real-time water consumption of multiple desulfurization systems.

[0083] It can be understood that the process water system control method provided by the above embodiment of the present application includes: obtaining the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spray volume corresponding to the slurry circulation pump; inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spray volume into a preset model to obtain the real-time flue gas evaporation of the desulfurization absorption tower; determining the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation, the real-time wastewater volume discharged by the desulfurization system and the real-time water volume carried in the gypsum discharged by the desulfurization system; and controlling the liquid level in the process water tank based on the real-time water consumption and the inflow flow of the process water tank in the process water system. Based on the scheme provided by the embodiment of the present application, the process water of the desulfurization system can be guaranteed to avoid the interruption of the water supply of the desulfurization system, which is conducive to the long-term safe and stable operation of the desulfurization process.

[0084] In the prior art, only intermittent control is usually used for the liquid level in the process water tank, and the process water replenishment valve is generally interlocked and switched according to the liquid level, that is, when the liquid level in the process water tank is higher than a certain value, the process water replenishment valve is interlocked and closed, and when the liquid level in the process water tank is lower than a certain value, the process water replenishment valve is interlocked and opened. This control method provides intermittent water supply to the process water tank instead of continuous water supply, which is prone to water shortage in the process water tank, making it difficult to ensure the process water for the desulfurization system, and prone to water supply interruption in the desulfurization system. Based on the solution provided in the above embodiment of the present application, the liquid level in the process water tank is dynamically matched with the real-time water consumption of the desulfurization system, which can ensure the process water for the desulfurization system and avoid water supply interruption in the desulfurization system.

[0085] In actual applications, the process water system may include a process water jelly pipe, multiple process water tanks, and multiple process water branch pipes; the multiple process water tanks correspond to the multiple process water branch pipes one by one, and the process water in each process water tank is transported to the process water jelly pipe through the corresponding process water branch pipes, and then transported to the desulfurization system through the process water jelly pipes. A process water pump is provided on each process water branch pipe, and each process water pump is usually a water pump of the same model and power. In this case, since it is usually difficult to achieve complete symmetry in the pipeline layout and the individual differences of each process water pump, it is difficult to ensure that the output of each process water pump is exactly the same even if the operating frequency is the same, which often causes some process water pumps to have a larger output and other process water pumps to have a smaller output, and then a water grabbing situation occurs. This water grabbing situation will affect the control effect of the control method in the above embodiment, which is not conducive to the long-term safe and stable operation of the desulfurization process. Moreover, as time went by, the water grabbing situation became more and more serious, gradually changing to a situation where some process water pumps were overloaded while other process water pumps had almost no flow, causing cavitation of the process water pumps and seriously affecting the stable and safe operation of the process water pumps.

[0086] Thus, in one embodiment, if Figure 2 As shown, the process water system control method provided in the embodiment of the present application further includes step 201 and step 202, which are specifically as follows:

[0087] Step 201 : acquiring the operating current of each process water pump, and calculating the average operating current based on the operating current of each process water pump.

[0088] The average operating current is specifically an arithmetic average operating current.

[0089] Step 202: Control the outlet pressure of each process water pump based on the target pressure, and control the operating current of each process water pump based on the average operating current.

[0090] Among them, the target pressure is for the process jellyfish pipeline. When the pressure of the process jellyfish pipeline deviates from the target pressure, the outlet pressure of each process water pump can be adjusted to make the pressure of the process jellyfish pipeline reach or approximately reach the target pressure.

[0091] In an embodiment of the present application, the operating current of each process water pump is controlled based on the average operating current, which can be specifically: adjusting the operating current of each process water pump to the average operating current. That is, for a process water pump whose operating current is greater than the average operating current, its operating current can be reduced, and then its operating frequency and output can be reduced. For a process water pump whose operating current is less than the average operating current, its operating current can be increased, and then its operating frequency and output can be increased. When making specific adjustments, a PID method can be adopted for adjustment.

[0092] The operating current of a process water pump can often measure its output capacity, and the same operating current usually means the same output. Therefore, in the embodiment of the present application, by adjusting the operating current of each process water pump to the average operating current, the operating current of each process water pump can be made the same, and thus the output of each process water pump can be made the same.

[0093] It can be understood that by adopting the above scheme, the outlet pressure of each process water pump is controlled based on the target pressure, and the operating current of each process water pump is controlled based on the average operating current. This can not only control the operating frequency of each process water pump to be the same, but also control the output of each process water pump to be the same, thereby avoiding the occurrence of water grabbing, which is beneficial to the long-term safe and stable implementation of the desulfurization process and the stable and safe operation of each process water pump.

[0094] Considering that the dynamic inertia of the two control objects, outlet pressure and operating current, are relatively close, if they are adjusted at the same time, it is easy to cause system data oscillation, and it is difficult to achieve the expected control effect. Therefore, in the specific implementation, the outlet pressure of each process water pump and the operating current of each process water pump can be controlled alternately. That is, the outlet pressure of each process water pump is controlled in the previous period, the operating current of each process water pump is controlled in the next period, and then the outlet pressure of each process water pump is controlled... In this way, the control is carried out alternately. In this way, the occurrence of data oscillation can be avoided.

[0095] In actual applications, each process water branch pipeline is equipped with a filter screen upstream of the process water pump. If the filter screen is blocked and not handled in time, it will cause insufficient actual output of the process water pump, and in severe cases, it will cause cavitation. Figure 3 As shown, the process water system control method provided in the embodiment of the present application may also include:

[0096] Step 301, obtaining the real-time operating frequency of each process water pump, and determining the rated current corresponding to each process water pump at its respective real-time operating frequency.

[0097] In the absence of water grabbing, the operating frequency and operating current of the process water pump generally have a relatively fixed corresponding relationship, which can usually be represented by a current frequency curve, that is, one operating frequency corresponds to one current (which can be called the rated current). Since each process water pump is of the same model and power, the current-frequency function relationship is also the same. Furthermore, after obtaining the real-time operating frequency of each process water pump, the rated current corresponding to each process water pump at its respective real-time operating frequency can be determined based on the functional relationship or the curve.

[0098] Step 302: Calculate the current deviation value corresponding to each process water pump based on the real-time operating current of each process water pump and the rated current corresponding to each process water pump.

[0099] In specific implementation, for each process water pump, the real-time operating current of the process water pump may be subtracted from the rated current corresponding to the process water pump to obtain the current deviation value corresponding to the process water pump.

[0100] Step 303, determining the blockage status of each process water branch pipeline according to the current deviation value corresponding to each process water pump.

[0101] Specifically, the process water pump has the same rated current at the same operating frequency. Then, when the current deviation value is larger, it means that the current is smaller, and the blockage is more serious. Based on this rule, the process water branch pipeline with more serious blockage can be screened out from each process water branch pipeline, and a blockage warning can be issued to remind relevant personnel to deal with it in time.

[0102] In actual applications, it may happen that the process water pump still supplies excessive water to the desulfurization system at the lowest frequency. Therefore, a reflux pipe is usually provided in the process water system, the inlet of the reflux pipe is connected to the process water branch pipe, the outlet of the reflux pipe is connected to the process water tank, and a reflux valve is provided on the reflux pipe to cause part of the process water in the process water branch pipe to flow back to the process water tank. In the case of multiple process water tanks, multiple process water branch pipes and multiple process water pumps, each process water branch pipe is generally provided with a corresponding reflux pipe. In the existing operation process, the reflux pipe in the process water system is usually set to a normally open state, resulting in high energy consumption of the process water pump in the process water system. Therefore, in the case where the process water system includes multiple process water tanks, multiple process water branch pipes and multiple process water pumps, and each process water branch pipe is provided with a corresponding reflux pipe, the process water system control method provided in the embodiment of the present application may also include:

[0103] When the real-time water consumption C of the desulfurization system is equal to the maximum flow of a process water pump (the error can be ±5%), the actual water supply is not enough to meet the water supply demand due to the opening of the reflux pipeline. At this time, the reflux valve can be closed to cut off the reflux and only a single process water pump can be turned on. In this way, the maximum water supply of a single process water pump can be achieved, avoiding the use of dual pump operation, and reducing the energy consumption of the process water pump in the process water system.

[0104] When the real-time water consumption C of the desulfurization system is equal to the maximum flow of the process water pump (the error can be ±5%), the reflux valve can be closed to cut off the reflux, and only two process water pumps can be turned on. In this way, the water supply can be maximized, the operation of three pumps can be avoided, and the energy consumption of the process water pump in the process water system can be reduced.

[0105] By analogy, when the real-time water consumption C of the desulfurization system is equal to the maximum flow of an integer number of process water pumps (the error can be ±5%), the reflux valve can be closed to cut off the reflux, and the corresponding number of process water pumps can be opened.

[0106] When the real-time water consumption C of the desulfurization system is not equal to the maximum flow of an integer number of process water pumps, the reflux mode can be used, that is, the reflux valve can be opened. In addition, in actual control, the process water pump outlet pressure can be used as the control target, and the PID control method can be used to control the water supply, so as to ensure smooth water supply and low energy consumption. In actual applications, the process water pump outlet pressure can be specifically controlled to be around 0.5MPa.

[0107] When the non-reflux operation mode is adopted, that is, when the reflux valve is closed, it is considered that the real-time water consumption C of the desulfurization system may be biased, which may cause the outlet pressure of the process water pump to be too high or too low. Taking the outlet pressure of 0.5MPa as the control target as an example, if the outlet pressure is higher than 0.6MPa and maintained for more than 1 minute, in order to ensure the safe operation of the process water pump and ensure that the process water pump will not be blocked, the reflux valve can be put into automatic mode; if the outlet pressure is lower than 0.4MPa and maintained for more than 1 minute, the spare process water pump can be automatically started (in actual application, one more process water pump is usually set as a spare) and switched to the reflux control mode.

[0108] It can be understood that the above scheme can reduce the energy consumption of the process water pump in the process water system while ensuring the process water of the desulfurization system, thereby improving the economic benefits.

[0109] Based on the same inventive concept, Figure 4 As shown, Figure 4 The structural block diagram of a process water system control device according to an embodiment of the present application is schematically shown. In one embodiment, a process water system control device 400 is provided, including an acquisition module 410, a prediction module 420, a water consumption calculation module 430 and a control module 440, wherein:

[0110] An acquisition module 410 is used to acquire real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume, and real-time spray volume corresponding to a slurry circulation pump;

[0111] The prediction module 420 is used to input the real-time flue gas flow rate, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower;

[0112] The water consumption calculation module 430 is used to determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system;

[0113] The control module 440 is used to control the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system.

[0114] In one embodiment, the preset model is constructed based on historical flue gas flow, historical flue gas temperature, historical demister flushing water volume, historical spray volume corresponding to the slurry circulation pump, and historical flue gas evaporation volume of the desulfurization absorption tower.

[0115] In one embodiment, the prediction module 420 is used to obtain the real-time water content carried in the gypsum discharged from the desulfurization system based on the following formula:

[0116] H2Op=Hp×Wp×Sp×Dp×A×10 -3 ;

[0117] Among them, H2Op is the real-time water volume carried in the gypsum discharged from the desulfurization system, in m 3 / h; Hp is the real-time thickness of gypsum discharged from the desulfurization system, in m; Wp is the real-time width of gypsum discharged from the desulfurization system, in m; Sp is the real-time speed of the vacuum belt conveyor, in m / h; Dp is the real-time density of gypsum discharged from the desulfurization system, in kg / m 3 ; A is the real-time mass percentage of water in gypsum discharged from the desulfurization system.

[0118] In one embodiment, the control module 440 is used to control the liquid level in the process water tank to a first liquid level if the ratio of the incoming water flow rate to the real-time water consumption is less than 1;

[0119] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 1 but less than 2, controlling the liquid level in the process water tank to a second liquid level;

[0120] If the ratio of the incoming water flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is greater than a third liquid level, shut off the incoming water to the process water tank;

[0121] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is less than a fourth liquid level, turning on the incoming water of the process water tank;

[0122] Among them, the liquid level heights in the process water tank are from high to low: the third liquid level, the first liquid level, the second liquid level, and the fourth liquid level.

[0123] In one embodiment, the process water system includes a process water jelly pipeline, multiple process water tanks and multiple process water branch pipelines; the multiple process water tanks correspond one-to-one to the multiple process water branch pipelines, and the process water in each process water tank is transported to the process water jelly pipeline through its corresponding process water branch pipeline, and transported to the desulfurization system via the process water jelly pipeline, and a process water pump is provided on each process water branch pipeline; the control module 440 is also used to obtain the operating current of each process water pump, and calculate the average operating current based on the operating current of each process water pump; the outlet pressure of each process water pump is controlled based on the target pressure, and the operating current of each process water pump is controlled based on the average operating current.

[0124] In one embodiment, the control module 440 is used to alternately control the outlet pressure of each process water pump and the operating current of each process water pump.

[0125] In one embodiment, the process water system control device 400 further includes a blockage determination module, which is used to obtain the real-time operating frequency of each process water pump and determine the rated current corresponding to each process water pump at the respective real-time operating frequency;

[0126] Based on the real-time operating current of each process water pump and the rated current corresponding to each process water pump, the current deviation value corresponding to each process water pump is calculated;

[0127] According to the current deviation value corresponding to each process water pump, the blockage condition of each process water branch pipeline is determined.

[0128] The process water system control device includes a processor and a memory. The acquisition module 410, prediction module 420, water consumption calculation module 430 and control module 440 are all stored in the memory as program units, and the processor executes the above program modules stored in the memory to implement corresponding functions.

[0129] The processor contains a kernel, which calls the corresponding program unit from the memory. One or more kernels can be set, and the kernel parameters can be adjusted to achieve fast and efficient modeling and calculation at the full chip scale.

[0130] The memory may include non-permanent memory in a computer-readable medium, random access memory (RAM) and / or non-volatile memory, such as read-only memory (ROM) or flash RAM, and the memory includes at least one memory chip.

[0131] An embodiment of the present application provides a machine-readable storage medium on which a program is stored. When the program is executed by a processor, the above-mentioned process water system control method is implemented.

[0132] In one embodiment, a computer device is provided. The computer device may be a terminal, and its internal structure diagram may be as follows: Figure 5 As shown. The computer device includes a processor A01, a network interface A02, a display screen A04, an input device A05 and a memory (not shown in the figure) connected through a system bus. Among them, the processor A01 of the computer device is used to provide computing and control capabilities. The memory of the computer device includes an internal memory A03 and a non-volatile storage medium A06. The non-volatile storage medium A06 stores an operating system B01 and a computer program B02. The internal memory A03 provides an environment for the operation of the operating system B01 and the computer program B02 in the non-volatile storage medium A06. The network interface A02 of the computer device is used to communicate with an external terminal through a network connection. When the computer program is executed by the processor A01, a process water system control method is implemented. The display screen A04 of the computer device can be a liquid crystal display or an electronic ink display, and the input device A05 of the computer device can be a touch layer covered on the display screen, or a button, trackball or touchpad set on the computer device housing, or an external keyboard, touchpad or mouse, etc.

[0133] Those skilled in the art will understand that Figure 5 The structure shown in the figure is only a block diagram of a part of the structure related to the solution of the present application, and does not constitute a limitation on the computer device to which the solution of the present application is applied. The specific computer device may include more or fewer components than those shown in the figure, or combine certain components, or have a different arrangement of components.

[0134] In one embodiment, the process water system control device provided in the present application can be implemented in the form of a computer program. The computer program can be Figure 5 The computer device shown in the figure is run on the computer device. The memory of the computer device can store various program modules that constitute the intelligent scheduling device for construction tasks, such as: Figure 4 The acquisition module 410, prediction module 420, water consumption calculation module 430 and control module 440 are shown. The computer program composed of various program modules enables the processor to execute the steps of the process water system control method of each embodiment of the present application described in this specification.

[0135] Figure 5 The computer device shown can be Figure 4 The acquisition module 410, prediction module 420, water consumption calculation module 430 and control module 440 in the process water system control device shown execute the method.

[0136] The embodiment of the present application provides a device, which includes a processor, a memory, and a program stored in the memory and executable on the processor. When the processor executes the program, the following steps are implemented:

[0137] Obtain real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume and real-time spray volume corresponding to the slurry circulation pump;

[0138] The real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume are input into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower;

[0139] Determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system;

[0140] Based on the real-time water consumption and the inflow flow of the process water tank in the process water system, the liquid level in the process water tank is controlled.

[0141] In one embodiment, the preset model is constructed based on historical flue gas flow, historical flue gas temperature, historical demister flushing water volume, historical spray volume corresponding to the slurry circulation pump, and historical flue gas evaporation volume of the desulfurization absorption tower.

[0142] In one embodiment, the real-time amount of water carried in the gypsum discharged from the desulfurization system is obtained based on the following formula:

[0143] H2Op=Hp×Wp×Sp×Dp×A×10 -3 ;

[0144] Among them, H2Op is the real-time water volume carried in the gypsum discharged from the desulfurization system, in m 3 / h; Hp is the real-time thickness of gypsum discharged from the desulfurization system, in m; Wp is the real-time width of gypsum discharged from the desulfurization system, in m; Sp is the real-time speed of the vacuum belt conveyor, in m / h; Dp is the real-time density of gypsum discharged from the desulfurization system, in kg / m 3 ; A is the real-time mass percentage of water in gypsum discharged from the desulfurization system.

[0145] In one embodiment, the controlling the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system includes:

[0146] If the ratio of the incoming water flow rate to the real-time water consumption is less than 1, controlling the liquid level in the process water tank to a first liquid level;

[0147] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 1 but less than 2, controlling the liquid level in the process water tank to a second liquid level;

[0148] If the ratio of the incoming water flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is greater than a third liquid level, shut off the incoming water to the process water tank;

[0149] If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is less than a fourth liquid level, turning on the incoming water of the process water tank;

[0150] Among them, the liquid level heights in the process water tank are from high to low: the third liquid level, the first liquid level, the second liquid level, and the fourth liquid level.

[0151] In one embodiment, the process water system includes a process water jelly pipe, a plurality of process water tanks and a plurality of process water branch pipes; the plurality of process water tanks correspond to the plurality of process water branch pipes one by one, the process water in each process water tank is respectively transported to the process water jelly pipe through the corresponding process water branch pipes, and is transported to the desulfurization system through the process water jelly pipe, and each process water branch pipe is provided with a process water pump; the control method further includes:

[0152] Obtaining the operating current of each process water pump, and calculating the average operating current based on the operating current of each process water pump;

[0153] The outlet pressure of each process water pump is controlled based on the target pressure, and the operating current of each process water pump is controlled based on the average operating current.

[0154] In one embodiment, the control method further includes:

[0155] The outlet pressure of each process water pump and the operating current of each process water pump are controlled alternately.

[0156] In one embodiment, the control method further includes:

[0157] Obtain the real-time operating frequency of each process water pump, and determine the rated current corresponding to each process water pump at its respective real-time operating frequency;

[0158] Based on the real-time operating current of each process water pump and the rated current corresponding to each process water pump, the current deviation value corresponding to each process water pump is calculated;

[0159] According to the current deviation value corresponding to each process water pump, the blockage condition of each process water branch pipeline is determined.

[0160] Those skilled in the art will appreciate that the embodiments of the present application may be provided as methods, systems, or computer program products. Therefore, the present application may adopt the form of a complete hardware embodiment, a complete software embodiment, or an embodiment in combination with software and hardware. Moreover, the present application may adopt the form of a computer program product implemented in one or more computer-usable storage media (including but not limited to disk storage, CD-ROM, optical storage, etc.) that include computer-usable program code.

[0161] The present application is described with reference to the flowcharts and / or block diagrams of the methods, devices (systems), and computer program products according to the embodiments of the present application. It should be understood that each process and / or box in the flowchart and / or block diagram, as well as the combination of the processes and / or boxes in the flowchart and / or block diagram, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, a special-purpose computer, an embedded processor, or other programmable data processing device to generate a machine, so that the instructions executed by the processor of the computer or other programmable data processing device generate instructions for implementing the processes in the flowchart and / or block diagram. Figure 1 A process or multiple processes and / or boxes Figure 1 A device that provides the functions specified in a block or multiple blocks.

[0162] These computer program instructions may also be stored in a computer-readable memory capable of directing a computer or other programmable data processing device to operate in a specific manner, so that the instructions stored in the computer-readable memory produce an article of manufacture comprising an instruction device, which implements the process Figure 1 A process or multiple processes and / or boxes Figure 1 A function specified in one or more boxes.

[0163] These computer program instructions can also be loaded onto a computer or other programmable data processing device so that a series of operating steps are executed on the computer or other programmable device to produce a computer-implemented process, thereby providing instructions for implementing the process. Figure 1 A process or multiple processes and / or boxes Figure 1 The steps for the functions specified in one or more boxes.

[0164] In a typical configuration, a computing device includes one or more processors (CPU), input / output interfaces, network interfaces, and memory.

[0165] The memory may include non-permanent memory in a computer-readable medium, random access memory (RAM) and / or non-volatile memory in the form of read-only memory (ROM) or flash RAM. The memory is an example of a computer-readable medium.

[0166] Computer readable media include permanent and non-permanent, removable and non-removable media, and can be implemented by any method or technology to store information. Information can be computer readable instructions, data structures, program modules or other data. Examples of computer storage media include, but are not limited to, phase change memory (PRAM), static random access memory (SRAM), dynamic random access memory (DRAM), other types of random access memory (RAM), read-only memory (ROM), electrically erasable programmable read-only memory (EEPROM), flash memory or other memory technology, compact disk read-only memory (CD-ROM), digital versatile disk (DVD) or other optical storage, magnetic cassettes, magnetic tape magnetic disk storage or other magnetic storage devices or any other non-transmission media that can be used to store information that can be accessed by a computing device. As defined herein, computer readable media does not include temporary computer readable media (transitory media), such as modulated data signals and carrier waves.

[0167] It should also be noted that the terms "include", "comprises" or any other variations thereof are intended to cover non-exclusive inclusion, so that a process, method, commodity or device including 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, commodity or device. In the absence of more restrictions, the elements defined by the sentence "comprises a ..." do not exclude the existence of other identical elements in the process, method, commodity or device including the elements.

[0168] The above are only embodiments of the present application and are not intended to limit the present application. For those skilled in the art, the present application may have various changes and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included within the scope of the claims of the present application.

Claims

1. A process water system control method, characterized in that: The control method comprises: Obtain real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume and real-time spray volume corresponding to the slurry circulation pump; The real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume are input into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower; Determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system; Based on the real-time water consumption and the inflow flow of the process water tank in the process water system, the liquid level in the process water tank is controlled.

2. The process water system control method according to claim 1, characterized in that: The preset model is constructed based on the historical flue gas flow, the historical flue gas temperature, the historical demister flushing water volume, the historical spray volume corresponding to the slurry circulation pump, and the historical flue gas evaporation volume of the desulfurization absorption tower.

3. The process water system control method according to claim 1, characterized in that: The real-time water volume carried in the gypsum discharged from the desulfurization system is obtained based on the following formula: H2Op=Hp×Wp×Sp×Dp×A×10 -3 ; Among them, H2Op is the real-time water volume carried in the gypsum discharged from the desulfurization system, in m 3 / h; Hp is the real-time thickness of gypsum discharged from the desulfurization system, in m; Wp is the real-time width of gypsum discharged from the desulfurization system, in m; Sp is the real-time speed of the vacuum belt conveyor, in m / h; Dp is the real-time density of gypsum discharged from the desulfurization system, in kg / m 3 ; A is the real-time mass percentage of water in gypsum discharged from the desulfurization system.

4. The process water system control method according to claim 1, characterized in that: The controlling of the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system includes: If the ratio of the incoming water flow rate to the real-time water consumption is less than 1, controlling the liquid level in the process water tank to a first liquid level; If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 1 but less than 2, controlling the liquid level in the process water tank to a second liquid level; If the ratio of the incoming water flow to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is greater than a third liquid level, shut off the incoming water to the process water tank; If the ratio of the incoming water flow rate to the real-time water consumption is greater than or equal to 2, and the liquid level in the process water tank is less than a fourth liquid level, turning on the incoming water of the process water tank; Among them, the liquid level heights in the process water tank are from high to low: the third liquid level, the first liquid level, the second liquid level, and the fourth liquid level.

5. The process water system control method according to claim 1, characterized in that: The process water system includes a process water pipe, a plurality of process water tanks and a plurality of process water branch pipes; the plurality of process water tanks correspond to the plurality of process water branch pipes one by one, the process water in each process water tank is respectively transported to the process water pipe through the corresponding process water branch pipe, and is transported to the desulfurization system through the process water pipe, and each process water branch pipe is provided with a process water pump; the control method also includes: Obtaining the operating current of each process water pump, and calculating the average operating current based on the operating current of each process water pump; The outlet pressure of each process water pump is controlled based on the target pressure, and the operating current of each process water pump is controlled based on the average operating current.

6. The process water system control method according to claim 5, characterized in that: The control method further comprises: The outlet pressure of each process water pump and the operating current of each process water pump are controlled alternately.

7. The process water system control method according to claim 5, characterized in that: The control method further comprises: Obtain the real-time operating frequency of each process water pump, and determine the rated current corresponding to each process water pump at its respective real-time operating frequency; Based on the real-time operating current of each process water pump and the rated current corresponding to each process water pump, the current deviation value corresponding to each process water pump is calculated; According to the current deviation value corresponding to each process water pump, the blockage condition of each process water branch pipeline is determined.

8. A process water system control device, characterized in that: include: An acquisition module is used to obtain real-time flue gas flow, real-time flue gas temperature, real-time demister flushing water volume, and real-time spray volume corresponding to the slurry circulation pump; A prediction module, used for inputting the real-time flue gas flow, the real-time flue gas temperature, the real-time demister flushing water volume and the real-time spraying volume into a preset model to obtain the real-time flue gas evaporation volume of the desulfurization absorption tower; A water consumption calculation module, used to determine the real-time water consumption of the desulfurization system according to the real-time flue gas evaporation amount, the real-time wastewater amount discharged by the desulfurization system, and the real-time water amount carried in the gypsum discharged by the desulfurization system; The control module is used to control the liquid level in the process water tank based on the real-time water consumption and the water flow rate of the process water tank in the process water system.

9. A processor, characterized in that: The method is configured to execute the process water system control method according to any one of claims 1 to 7.

10. A machine-readable storage medium having instructions stored thereon, characterized in that: When the instructions are executed by a processor, the processor is configured to perform the process water system control method according to any one of claims 1 to 7.

Images