KR100911688B1 - APD method control and monitoring device and method - Google Patents

Abstract

APID (Advaced Phased Isolation Ditch) for sewage treatment system including a sewage treatment site facility having a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facility in real time according to a set target value. A method for controlling and monitoring a method, comprising: a data storage unit for storing measurement and operation data of the sewage treatment site facility transmitted from the site control device; Based on the measurement and operation data of the sewage treatment site facilities, grasp the progress of nitrification and denitrification of the bioreactor, and operation mode control for setting and switching the section of anaerobic, anaerobic, and aerobic processes in the bioreactor. APID method control including a process control module for determining the residence time for each process, controlling the dissolved oxygen concentration in the aerobic process, inlet location of the sewage and return sludge, and a target value for performing the flow rate control and transmitting the target value to the field control device. And a monitoring device is provided.

Description

APD method control and monitoring device and method thereof {APPARATUS AND METHOD FOR CONTROLLING AND MONOTORING USING ADVANCED PHASED ISOLATION DITCH}

The present invention relates to an APID (Advaced Phased Isolation Ditch) control and monitoring apparatus and method thereof, and in detail, reflects the change in the reaction of the biological reactor by receiving measurement and operation data of the sewage treatment site equipment equipped with the biological reactor. The present invention relates to an APID method control and monitoring apparatus and method for performing automatic real-time operation by determining a target value for operating mode setting control, aeration / non-aeration section control, dissolved oxygen concentration control, and sludge conveyance control for a biological reactor. .

In general, the advanced sewage treatment method divides anaerobic tank (process), anoxic tank (process), and aerobic tank (process).

Anaerobic tank (process) induces the release of phosphorus by using organic substances present in the sewage, and anaerobic tank (process) denitrification using organic substances present in the sewage from the nitrate nitrogen produced through nitrification in the aerobic tank (process) The aerobic tank (process) plays a role of removing organic substances, nitrogen and phosphorus by oxidizing and nitrifying some of the organic substances removed from the anaerobic tank (process) and anoxic tank (process), and excessive ingestion of phosphorus.

Most of the existing methods apply the inflow of sewage into the anaerobic tank only. However, in this case, as most organic materials are used for denitrification and phosphorus release in the anaerobic tank (process), the total nitrogen removal efficiency was low due to the lack of organic materials in the anoxic tank (process).

In order to solve this problem, split inflow into anaerobic tank and anaerobic tank has been developed. In case of split inflow into anaerobic tank (process) and anoxic tank (process), the denitrification rate is increased by using organic substances present in the sewage even in the anaerobic tank (process), compared to the method which flows into anaerobic tank (process) only. This was improved.

However, dividing the inlet (anaerobic: anoxic tank, 6: 4 or 5: 5, and so on) ratio is presented there is driving on the basis of experience and once a day the water quality analysis result of the analysis of most of the operators, of the PO in the anaerobic tank ₄₃ -P (step) If the concentration is low, it is judged that there is a lack of carbon source necessary for phosphorus release, and the inflow to the anaerobic tank (process) is increased. If NO ₃ ^-- N is high in the anaerobic tank (process), it is determined that the carbon source is insufficient. Increase the flow rate into) or decrease the internal transfer rate.

However, this is a result of using the previous data, which does not accurately reflect the current situation and does not significantly improve the processing performance.

In order to solve this problem, first of all, in order to accurately monitor the state in the bioreactor, each reactor (process) has ammonia nitrogen (NH ₄ ⁺ -N), nitrate nitrogen (NO ₃ ^-- N), phosphate phosphorus ( PO ₄₃ -P) A water quality measuring instrument should be installed to establish a control system to monitor the amount of pollutants in the reactor in real time.

However, in the general sewage advanced treatment method, each water quality measuring instrument should be installed for each process, which requires a huge initial investment and maintenance cost. Therefore, in order to effectively control the minimized water meter, it is necessary to simultaneously apply the temporal partitioning and the spatial partitioning method, rather than the spatial partitioning in the conventional reactor.

In addition, the conventional sewage treatment apparatus provides a monitoring and control system through real-time water quality monitoring, but since the system for checking the abnormality of the monitoring and control system is not established, the reliability of the monitoring and control system is very low.

The problem to be solved by the present invention is to provide an apparatus and method for controlling and monitoring the APID method for effective sewage treatment by monitoring the nitrification process and the denitrification process in a reaction tank in real time.

According to an aspect of the present invention, a sewage treatment system comprising a sewage treatment site facility equipped with a biological reaction tank consisting of two intermittent aeration tanks, a site control device for controlling the sewage treatment site facilities in real time according to a set target value. An apparatus for controlling and monitoring an Advanced Phased Isolation Ditch (APID) method, the apparatus comprising: a data storage configured to store measurement and operation data of the sewage treatment site equipment transmitted from the field control device; Based on the measurement and operation data of the sewage treatment site facilities, grasp the progress of nitrification and denitrification of the bioreactor, and operation mode control for setting and switching the section of anaerobic, anaerobic, and aerobic processes in the bioreactor. APID method control including a process control module for determining the residence time for each process, the dissolved oxygen concentration in the aerobic process, the inlet location of the sewage and return sludge and the target value for performing the flow rate control, and transmits it to the field control device; A monitoring device is provided.

Preferably, the APID method control and monitoring device HMI for providing an interface for reporting the operating status and process control status of the sewage treatment process, the user setting function for the target value or parameters related to the process control (Human-Machine Interface) further includes a processing module.

Preferably, the process control module may check the validity of the measurement and operation data received from the field control device, and if it is determined that there is an error in the network connection with the field control device, the previously transmitted target value Instruct the site control device to perform a stand-alone mode of controlling the sewage treatment site facility based on the control.

Preferably, the process control module, the operation mode control module for determining a target value for a plurality of operation mode control to perform the switching of the time and mode of the nitrification and denitrification section of the aeration and non-aeration section in the biological reactor ; Aeration / Aeration section control module for determining a target value for performing aeration / non-aeration control according to the number of aeration section of the biological reactor to change the residence time of the anaerobic / anaerobic / aerobic process; A dissolved oxygen concentration control module for determining a target value for controlling the amount of air supplied to maintain and control the oxygen concentration when the biological reactor is abandoned; And a sludge conveying control module for determining a target value for controlling the flow rate and conveying position of the conveying sludge in order to maintain the MLSS concentration of the bioreactor.

Preferably, the operation mode control module measures the concentration of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the aeration and aeration intervals, the aeration / aeration state cross-distribution logic Extract data through and perform time and mode switching between nitrification and denitrification intervals based on the extracted data.

Preferably, the aeration / aeration period control module is a sum of ammonia nitrogen and nitrate through the measurement of the concentration of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) of the biological reactor Calculate the ratio of nitrogen sum and control the aeration / aeration period according to the number of aeration cycles of the bioreactor according to the preset sum of ammonia nitrogen and nitrate nitrogen sum to change the residence time of anaerobic, anaerobic, and aerobic processes.

Preferably, the dissolved oxygen concentration control module is configured to set the dissolved oxygen concentration target value (set-point) and the maximum value according to the ammonia nitrogen concentration of the abandoned zone through ammonia nitrogen concentration and dissolved oxygen concentration measurement value of the abandoned zone. After determining the allowable dissolved oxygen concentration sequentially, the dissolved oxygen concentration in the aeration section is controlled.

Preferably, the sludge conveyance control module determines the flow rate according to the conveyed sludge concentration or the conveyed rate by using the inflow flow rate, conveyed sludge flow rate, conveyed MLSS concentration, discharge water turbidity, final sedimentation sludge interface measurement value, and the sludge interface of the final settling basin The conveyance rate is corrected using the turbidity of the over discharge water and the conveyance position is controlled according to the operation mode.

Preferably, the biological reaction tank consists of a first intermittent aeration tank consisting of three sections (Tank3b, Tank3a, Tank 1), and a second intermittent aeration tank consisting of three sections (Tank3c, Tank3d, Tank2), and the Tank3b Tank3c are connected to each other via a flow path; The operation mode control module selectively operates the A, B, C, D operation mode, the A operation mode is a flow path in which sewage flows into Tank1 and flows out of Tank2 through Tank3, and Tank1 performs aeration process. And, Tank2 is a pattern to be operated in the aeration process, the B operation mode is a flow path in which sewage flows into Tank3c and outflows from Tank2, Tank1 is a pattern to be abandoned, Tank2 is a pattern to be operated in a non-aeration process, the C operation Mode is a flow path in which sewage flows into Tank2 and flows out of Tank1 through Tank3, Tank1 is a pattern for operating in aeration process and Tank2 in aeration process, and the D operation mode flows sewage into Tank3b and flows out of Tank1. As a flow path, Tank1 is a pattern to operate in aeration process and Tank2 in aeration process.

Preferably, the biological reaction tank consists of a first intermittent aeration tank consisting of three sections (Tank3b, Tank3a, Tank 1), and a second intermittent aeration tank consisting of three sections (Tank3c, Tank3d, Tank2), and the Tank3b Tank3c are connected to each other via a flow path; The aeration / non-aeration section control module, the sum of ammonia nitrogen and nitrate nitrogen through the measurement of the concentration of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) of Tank1 and Tank2 The ratio is calculated to control the aeration / aeration period of the tank 3 according to the number of aeration sections of the tank 3 according to a preset ratio of the sum of ammonia nitrogen and the nitrate nitrogen.

According to another aspect of the present invention, there is provided a sewage treatment system including a sewage treatment site facility equipped with a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facilities in real time according to a set target value. Advanced Phased Isolation Ditch (APID) method control and monitoring method for the nitriding and denitrification of the biological reactor in the biological reactor based on the measurement and operation data of the sewage treatment site equipment transmitted from the field control device Determining the degree; Operation mode control for setting and converting the anaerobic / anaerobic / aerobic process section in the biological reactor by reflecting the progress of nitrification and denitrification of the biological reactor, residence time for each process, dissolved oxygen concentration control in the aerobic process, An APID method control and monitoring method is provided that includes determining a target value for performing inflow of sewage and conveying sludge and a target value for performing flow control to the field control device.

Preferably, the APID method control and monitoring method further comprises the step of validating the measurement and operation data received from the field control device.

Preferably, the APID method control and monitoring method, if it is determined that there is an error in the network connection with the site control device, based on the previously transmitted target value to control the sewage treatment site facilities in a single operation mode Instructing the field control device to perform.

Preferably, the determination of the target value comprises: determining a target value for controlling a plurality of operation modes such that switching between the time and mode of the nitrification and denitrification sections of the aeration and aeration sections in the biological reactor is possible; Determining a target value for the aeration / aeration period control according to the number of aeration sections of the bioreactor to change the residence time of the anaerobic / anaerobic / aerobic process; Determining a target value for controlling the amount of air supplied to maintain and control the oxygen concentration upon aeration of the bioreactor; Determining a target value for controlling the flow rate and conveying position of the conveying sludge to maintain the MLSS concentration of the bioreactor.

Preferably, the step of controlling the plurality of operation modes, aeration / ratio by measuring the concentration of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the aeration and aeration period Abandoned state cross-distribution logic extracts data and performs nitrification and denitrification interval time and mode switching based on the extracted data.

Preferably, the step for giving the / a non-giving control section, the bioreactors set of ammonium nitrogen (NH ₄ ⁺ -N) and nitrate (NO ₃ ^- -N) total ammonium nitrogen through the concentration measurement value By calculating the ratio of the sum of nitric acid and nitric acid, the aeration / aeration period is controlled according to the number of aeration stages of the bioreactor according to the pre-set ratio of ammonia nitrogen and nitrate nitrogen. Change it.

Preferably, the step for controlling the amount of air, the dissolved oxygen concentration target value (set-point) according to the ammonia nitrogen concentration of the aeration zone previously set through the ammonia nitrogen concentration and dissolved oxygen concentration measurement value of the aeration zone And the maximum allowable dissolved oxygen concentration are determined sequentially and then the dissolved oxygen concentration in the aeration section is controlled.

Preferably, the step for controlling the flow rate and conveying position of the conveying sludge, the flow rate according to the conveyed sludge concentration or conveyance rate using the inflow flow rate, conveyed sludge flow rate, conveyed MLSS concentration, effluent turbidity, final sediment sludge interface measurement value The transport rate is corrected using the sludge interface of the final settling basin and the turbidity of the discharged water, and the transport position is controlled according to the operation mode.

Preferably, the biological reaction tank consists of a first intermittent aeration tank consisting of three sections (Tank3b, Tank3a, Tank 1), and a second intermittent aeration tank consisting of three sections (Tank3c, Tank3d, Tank2), and the Tank3b Tank3c are connected to each other via a flow path; The plurality of operation modes include A, B, C, D operation mode, the A operation mode is a flow path in which sewage flows into Tank1 and flows out of Tank2 via Tank3, Tank1 performs aeration process, Tank2 is a pattern that is operated in the aeration process, the B operation mode is a flow path in which sewage flows into Tank3c and exits from Tank2, Tank1 is a pattern that is operated in aeration process, Tank2 is a non-aeration process, the C operation mode is Sewage flows into Tank2 and flows out of Tank1 through Tank3, Tank1 is a pattern to operate in aeration process and Tank2 is aeration process, and the D operation mode is a flow path in which sewage flows into Tank3b and flows out of Tank1 Tank1 is a pattern to operate in aeration process, Tank2 aeration process.

Preferably, the biological reaction tank is composed of a first intermittent aeration tank consisting of three sections (Tank3b, Tank3a, Tank 1), and a second intermittent aeration tank consisting of three sections (Tank3c, Tank3d, Tank2), the Tank3- b and Tank3-c are connected to each other via a flow path; The step of controlling the aeration / aeration period, the sum of ammonia nitrogen and nitrate through the measurement of the concentration of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) of the Tank1 and Tank2 The ratio of the sum of nitrogen is calculated to control the aeration / aeration of the tank 3 according to the number of aeration sections of the tank 3 according to a preset ammonia nitrogen sum and the nitrate nitrogen sum ratio.

According to the present invention, by receiving the measurement and operation data of the sewage treatment plant facilities, monitoring the operation of the sewage treatment plant facilities and field control device and reflecting the trend of reaction changes in the bioreactor, the operation mode control and abandonment of the biological reactor Real-time automatic operation can be performed by determining the target value for the control of the non-aeration section, the dissolved oxygen concentration control, and the sludge conveyance control.

Accordingly, the ripple effect of increasing the design technology of the sewage treatment plant is expected by providing quantitative design basic data based on the data acquired by real-time bioreactor control, and through the operation of scientific and rational sewage treatment plant using the system, Can be improved.

In addition, by laying the foundation for combining advanced information and communication technology and environmental technology, it is possible to promote technology development and expand its utilization in the field of environmental informatization, and as this control technology is incorporated into various domestic construction methods, automation execution units of sewage treatment plants The ripple effect is expected to extend the scope of application and to improve the accuracy of on-line water meters.

In addition, it is possible to improve the water quality of the surrounding streams and prevent eutrophication of the discharged water by maintaining stable and high-efficiency organic and suspended substances, nitrogen and phosphorus treatment performance throughout the year.

  In addition, when managing the sewage treatment plant using the sewage treatment system according to the present invention, it is possible to reduce the maintenance cost of the sewage treatment plant and maintain stable discharge water quality throughout the year through quantitative and qualitative scientific analysis, management, and control.

In addition, according to the present invention, stable discharge water quality is maintained throughout the year to improve the water quality of the discharge stream and decrease the frequency of side effects of the discharge area, thereby creating a hydrophilic environment, and thus, it is expected that the formation of a blue network is easy.

In addition, according to the present invention, it is possible to replace the control algorithm, which is developed to be suitable for the domestic situation with the pure domestic technology and accompanying the existing foreign sewage altitude treatment method with the domestic technology, and based on the long-term field application results of the sewage altitude treatment method. By securing the excellence and database the know-how accumulated in the operation process, it is possible to secure competitiveness of comparative advantage over foreign technology in overseas markets such as Southeast Asia, Central Asia, and China. It is estimated.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a block diagram showing a sewage treatment system according to an embodiment of the present invention. Referring to FIG. 1, a sewage treatment site facility 200 installed at a sewage treatment site, a site control device 400 for controlling the operation of the sewage treatment site facility 200, and the site control device 400. It is configured to include an APID method control and monitoring device 600 to work with.

The sewage treatment site facilities 200 are various structures or various devices installed on the site for sewage treatment. The sewage treatment site facility 200 includes a biological reaction tank in which water is introduced into an anaerobic tank state, an anoxic state, or an aerobic state, and the opening and closing of the discharge part is adjusted to change the flow of the flow path. The bioreactor consists of two intermittent aeration tanks communicating with each other without internal partitions, and performs nitrification and denitrification processes. In addition, the sewage treatment site facility 200 includes a sedimentation tank and a blower, a valve, a pump, and a fan for controlling the flow of sewage and conveying sludge by subdividing each intermittent aeration tank into a plurality of sections. In addition, a measuring instrument for measuring the water quality of the biological reactor and signal transmission lines for receiving a driving signal from the outside are included.

The on-site control device 400 controls the sewage treatment site facility 200 in real time at the sewage treatment site to perform an operation for sewage treatment. The field control device 400 is performed based on the set target value. The field control device 400 may be implemented by, for example, a programmable logic controller (PLC), and includes control logic for real-time control of the sewage treatment site facility 200. The field control device 400 performs a control to turn on / off the operations given to the respective facilities in the field facility 200 according to the set target value.

The field control device 400 may perform a single operation mode or a linked operation mode. Here, the single operation mode is used as a relative concept of the interlocking operation mode, it may also be called a backup mode. The site control device 400 may control the operation of the sewage treatment site facility 200 in conjunction with the APID method control and monitoring device 600. When the site control apparatus 400 performs the interlocking operation mode, the site control apparatus 400 receives a target value from the APID method control and monitoring apparatus 600 and controls the sewage treatment site facility 200 according to the target value. In addition, the on-site control device 400 has its own or previously linked with the APID method control and monitoring device 600 on the basis of the target value received at the time of interworking with the APID method control and monitoring device 600. Operation of the sewage treatment site facility 200 may be controlled. In the general case, the field control device 400 performs the interlocking operation mode. In the special case, for example, when the communication with the APID method control and monitoring device 600 is not smooth, the field control device 400 performs the single operation mode. However, the present invention is not limited thereto and may be modified as much as necessary.

The field control device 400 operates the biological reactor based on a target value or a predetermined target value received from the APID method control and monitoring device 600.

The field control device 400 records the water quality measurement data measured in real time from the bioreactor and the operation data of the bioreactor in units of time and transmits them to the APID method control and monitoring device 600.

The APID method control and monitoring device 600 determines the target value to be used in the field control device 400 in real time and transmits it to the field control device 400 so that automatic operation of the sewage treatment site facilities is continuously performed. To be performed.

The target value includes operating mode control for setting and converting an anaerobic, anaerobic and aerobic process in the bioreactor, residence time control for each process, dissolved oxygen concentration control in an aerobic process, and inflow location of sewage and conveying sludge. The value determined by the APID method control and monitoring device 600 to perform the flow control. The target value is calculated and determined according to the progress of nitrification or denitrification in the biological reactor.

The APID method control and monitoring device 600 receives the measurement and operation data of the sewage treatment site facility 200 from the field control device 400 to determine the progress of nitrification or denitrification in the biological reactor. . The determination of the target value in the APID method control and monitoring apparatus 600 is made based on a predetermined process. As the target value is determined by reflecting the progress of nitrification and denitrification in the bioreactor in real time, dynamic operation control may be performed on the sewage treatment plant 200.

FIG. 2 is a perspective view schematically showing a biological reactor in a sewage treatment plant in a sewage treatment system according to an embodiment of the present invention shown in FIG. 1, and FIG. 3 is a sewage treatment system according to an embodiment of the present invention. Figure 4 is a schematic view showing the sewage treatment plant facilities, Figure 4 is a cross-sectional view showing the interior of the biological reaction tank according to an embodiment of the present invention.

In the sewage treatment plant 200, two intermittent aeration tanks 210 and 220 (bulk liquid) constitute one biological reactor as shown in FIGS. Each intermittent aeration tank (210, 220) is formed to communicate with each other flow paths (216, 226) is to flow the sewage between each other. In addition, the inlet (211, 212, 221, 222) and the discharge portion for discharging the sewage treated in the intermittent aeration tank (210, 220) to the upper and lower in the intermittent aeration tank (210, 220) 214 and 224 are connected. To this end, each of the intermittent aeration tank (210, 220) is formed with an inlet or outlet for connecting to the inlet (211, 212, 221, 222) and the outlet (214, 224).

In addition, the inlets 211, 212, 221, 222 are connected to the upper and lower ends of the intermittent aeration tanks 210, 220, respectively, and are opened and closed at the outlets of the inlets 211, 212, 221, 222. The means 270 is installed, and controls the open state of the discharge parts (214, 224) through the control of the opening and closing means (270).

A bioreactor consisting of two intermittent aeration tanks 210 and 220 is used, and is divided into three sections (Tank 1, Tank 2, Tank 3) on the operation side, and Tank 3 is again divided into four sections (Tank3a, Tank3b, Tank3c, and Tank3d), the residence time of anaerobic, anaerobic, and aerobic processes is controlled by abandonment / aeration of each zone within the intermittent aeration tank according to the inflow load. It is connected via a flow path between Tank3b and Tank3c for sewage flow. In order to apply intermittent aeration to each tank, it is installed to enable individual control.

The opening and closing means 270 is an electric sluice, connected to a cylinder 272 having a rod 274 movable up and down, and to a rod 274 of the cylinder 272, and having the inlets 211, 212, 221, A shield plate 276 that shields the outlet of 222.

In addition, the lower part of each intermittent aeration tank (210, 220) is provided with a diffuser 230 for supplying air. The diffuser 230 selectively supplies air to each of the intermittent aeration tanks 210 and 220, and accordingly, the intermittent aeration tanks 210 and 220 may be changed to any one of an anaerobic state, an anaerobic state, and an aerobic state. Can be. In addition, the intermittent aeration tanks 210 and 220 may coexist in an anaerobic state, anoxic state, and aerobic state by controlling the air injection position supplied from the diffuser 230.

In addition, the diffuser 230 may be provided in plurality, preferably installed to face the inlet (211, 212, 221, 222). Accordingly, the corresponding diffuser 230 is positioned below the inlets 211, 212, 221, and 222.

In addition, a main air supply pipe 232 for supplying air is connected to the diffuser 230, and a blower 236 is installed in the main air supply pipe 232 to supply air. In addition, a valve means 234 for controlling the amount of air supplied is installed at the connection portion between the diffuser 230 and the main air supply pipe 232. The valve means 234 may be composed of an electric needle valve (Electric Needle Value), an electric butterfly valve (Electric Butterfly Value), an electric ball valve (Electric Ball Value), respectively by adjusting the valve means 234 The amount of air supplied to the diffuser 230 can be controlled. Therefore, the sewage treatment site facility 200 is air supplied to each part of the intermittent aeration tanks 210 and 220 through the diffuser 230 even without stopping the operation of the blower 236. The supply can be cut off or adjusted.

In addition, a flow adjusting tank (not shown) may be installed at an inlet of the inlets 211, 212, 221, and 222 of the intermittent aeration tanks 210 and 220 to adjust a flow rate of the sewage raw water. Accordingly, a certain amount of flow rate can always be supplied to the intermittent aeration tanks 210 and 220.

In addition, the discharge portion (214, 224) of the intermittent aeration tank (210, 220) is provided with a water level control device (280) for adjusting the opening and closing of the discharge portion (214, 224) to change the flow of the flow path. Therefore, the intermittent aeration tanks 210 and 220 may naturally lower the nitrified sewage to an oxygen-free (trough) state through adjustment of the water level control device 280 to obtain an internal transport effect with less power.

The water level adjusting device 280 adjusts the opening and closing by adjusting the opening heights of the discharge parts 214 and 224, and changes the flow of the flow path by adjusting the flow rate flowing over the discharge parts 214 and 224. do. To this end, the water level control device 280 includes shielding means for blocking the opening, and height adjustment means for adjusting the height of the shielding means.

5 is a block diagram illustrating an APID method control and monitoring apparatus in a sewage treatment system according to an embodiment of the present invention.

Referring to FIG. 5, the APID method control and monitoring apparatus 600 according to an embodiment of the present invention includes a data storage unit 610 for storing various data for sewage treatment, a process control module 630, and an HMI. Processing module 640.

The data storage unit 610 stores measurement and operation data of the sewage treatment site facility 200 transmitted from the field control device 400 and data for setting a target value.

The measurement data includes measurement data such as concentration measurement data of NH ₄ , NO ₃ , MLSS, PO ₄ , and dissolved oxygen in the biological reaction tank, sludge level, air flow rate, pressure, turbidity, return flow rate, influent flow rate, and the like.

The operation data includes operation data such as a blower, a control valve (inflow branch control valve, air branch control valve, conveying sludge branch control valve), a level control device, a surplus sludge pump, a conveying sludge pump, an inflow pump, and the like.

The data for setting the target value include data related to denitrification / nitrification conditions, dissolved oxygen and loading conditions, MLSS concentration and return flow conditions.

The process control module 630 determines various target values for controlling the nitrification process and the denitrification process (DN) by reflecting the change of reaction in the biological reactor.

The target values include target values for operating mode control, aeration / non-aeration section control, dissolved oxygen concentration control, and sludge conveyance control for the biological reactor of the sewage treatment plant facility 200.

The calculation of the target values is determined by denitrification / nitrification conditions, dissolved oxygen and loading conditions, MLSS concentration and return flow conditions. The process control module 630 performs a validity check on the data stored in the data storage 610 and then calculates a target value based on the valid data.

Nitrification is a process in which ammonia nitrogen is oxidized to nitrous acid and nitric acid by nitrifying microorganisms under aerobic conditions, and is classified into ammonia oxidation process and nitrite oxidation process as shown in the following formulas.

Here, the theoretical total oxygen demand for oxidizing ammonia to nitric acid is about 4.57 gO ₂ / gN, and the amount of oxygen required for the ammonia oxidation and nitrite oxidation steps is 3.43 gO ₂ -N and 1.14 gO ₂ / gN, respectively. to be. At this time, the nitrifying microorganism uses carbon dioxide gas in the wastewater as an inorganic carbon source, and the alkalinity of the wastewater occurs due to hydrogen ions (H ⁺ ) generated during the nitrification process. Theoretically, an alkalinity of 7.14 mg (as CaCO ₃ ) is required to oxidize 1 mg NO ₄ ⁺ -N.

Inorganic carbon is required for cell synthesis during nitrification. At this time, most of the energy obtained from the oxidation of nitrogen is consumed to reduce carbon dioxide to cells. The stoichiometry of cell synthesis can be expressed by [Formula 2], wherein the yields of ammonia oxidizing bacteria and nitrite oxidizing bacteria are 0.08g-VSS / g-NH ₄ ⁺ -N and 0.05g-VSS / g-NO _{2-, respectively} ^. -N applies. Here, C ₅ H ₇ NO ₂ means nitrifying bacteria.

In general, nitrification is known to be mainly due to chemoautotrophic bacteria. Among the microorganisms involved in nitrification, Nitrosomonas sp. Is a representative microorganism that oxidizes ammonia to hydroxyl nitrite via hydroxylamine. Other types include Nitrosospira briensis, Nitrosococcus nitrous, and Nitrosolobus multiformis. Nitrobacter sp. Is the major microorganism that oxidizes nitrous acid to nitric acid. The marine microorganisms Nitrosospina gracilis and Nitrosococcus mobils are also known.

The denitrification (DN) process can be carried out in all forms of anoxic suspended growth and anoxic attached growth, the conditions of the denitrification reaction being deficient in dissolved oxygen concentrations and the presence of sufficient nitrates. Depends on the presence Biological denitrification generally begins with a complete nitrification reaction. However, the microorganisms involved in the nitrification process change the nitrification pathway according to the nitrogen type in the influent wastewater. In high concentration ammonia wastewater, the nitrobacter is caused by the non-ionized ammonia (NH ₃ : free ammonia) and nitrite (HNO ₃ : free nirous acid). Inhibition of nitrification results in nitrite build-up. The microorganisms involved in the denitrification process are random heterotrophic microorganisms, which require the maintenance of anoxic state in the reactor and organic carbon source, which is an electron donor, and methanol is the most important electron donor for economic reasons. It is used. When methanol is used as the electron donor, the denitrification reaction is as follows.

_{NO 3 + 1 / 3CH 3 OH} → NO 2 - + 1 / 3CO 2 + 2 / 3H 2 O

^{_{NO 2 - + 1 / 2CH 3}} OH → 1 / 2N 2 + 1 / 2CO 2 + 1 / 2H 2 O + OH -

_{NO 3 + 5 / 6CH 3 OH} → 1 / 2N 2 + 5 / 6CO 2 + 7 / 6H2 O + OH -

It is known that methanol for denitrification requires about 25 to 30% of cell synthesis of denitrification microorganisms, and the general denitrification reaction of nitrates considering cell synthesis is proposed as follows based on actual research. have.

NO ₃ + 1.08CH ₃ OH + 0.24H ₂ CO ₃ → 0.056C ₅ H ₇ NO ₂ + 0.47N ₂ + 1.68H ₂ O + HCO

^{_{NO 2 - + 0.67CH 3 OH +}} 0.53H 2 CO 3 → 0.004C 5 H 7 NO 2 + 0.48N 2 + 1.23H 2 O + HCO

O ₂ + 0.93 CH ₃ OH + 0.056 H ₂ CO ₃ → 0.056 C ₅ H ₇ NO ₂ + 1.04 N ₂ + 0.59 H ₂ O + 0.56 HCO

When the nitric acid is reduced to N ₂ gas in the denitrification reaction, carbon acid and bicarbonate are produced. Denitrification of 1 mg NO ₃ ^-- N produces an alkalinity of about 2.3 to 3.0 mg / L, which in turn increases the pH of the reactor. In the environmental conditions for biological denitrification, dissolved oxygen concentration is a decisive variable. In general, the dissolved oxygen concentration is hindered by the denitrification reaction when the dissolved oxygen concentration is 0.2 mg / L or more and denitrification at the dissolved oxygen concentration of 0.13 mg / L. Some reports have stopped responding. Since the presence of dissolved oxygen inhibits the enzyme system for denitrification, the dissolved oxygen concentration is preferably zero or very low. Denitrification rate in the denitrification process can be described by the following formula (5).

U'RDN (T) = RDN (T) K (T-20) (1-DO)

here,

U'RDN (T): Total denitrification rate

RDN (T): Specific denitrifiction rate, kgNO ₃ -N / kgMLVSS.

T: temperature, ℃

DO: concentration of dissolved oxygen in the reaction tank, mg / L

K: temperature constant, 1.09 (range: 1.03 ~ 1.1)

Formula 5 indicates that the denitrification rate is zero when the dissolved oxygen concentration is 1.0 mg / L. The temperature for the denitrification reaction is similar to other biological processes and can be reacted in the range of 0 to 50 ° C. In the wastewater treatment, denitrification is generally performed at a temperature in the range of 5 to 30 ° C., but the optimum reaction temperature is known to be 35 to 50 ° C. In addition, the reaction rate in the range of 5 ~ 10 ℃ is about 1.5 ~ 2.0 times as 10 ℃ increase and the denitrification reaction was reported to be stopped at the water temperature of about 3 ℃.

Therefore, the process control module 630 includes an operation mode control module 631, an aeration / non-aeration section control module 632, a dissolved oxygen control module 633, and a sludge conveyance control module 634.

6 to 9 are views for explaining the operation of the driving mode control module according to an embodiment of the present invention.

Referring to FIG. 6, the driving mode control module 631 may include a data validation module 631a, a denitrification / nitridation region detection module 631b, and a driving mode and a running time setting module 631c.

The data validation module 631a validates the concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the bioreactor received from the field control device 400. Only verified data is passed to the denitrification / nitridation area detection module 631b.

The denitrification / nitridation area detection module 631b is based on the HMI operator setting input and ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ) in the aeration and aeration sections received from the data validation module 631a. ^- extracts the data through a given up / non-giving cross-state distribution logic for the concentration of -N).

The operation mode and time setting module 631c utilizes the data extracted through the denitrification / nitridation area detection module 631b based on the HMI operator setting input for the nitrification and denitrification section time correction and the phase shift time correction. The calculated calculation value is calculated. This calculated value is used to correct the correlation between ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) for each aeration / aeration period in the basic operation mode. Set the section and determine the target value for converting to the operation mode that inflows sewage into the non-aeration section. The target value determined as described above is the driving mode control target value, and is converted to a predetermined signal type (for example, a mode mode code signal type) and then outputted to the field control device 400. Therefore, the driving mode code signal includes information for setting the driving mode setting and the running time.

In the reaction tank of the method described in the above-described nitrification and denitrification process and the chemical reaction scheme, the reaction relationship and the flow of the process are inferred by the simple reaction scheme shown in FIG. Variables to be applied in the setting of the operation mode are ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N).

In the correlation between ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N), ammonia nitrogen (NH ₄ ⁺ -N) decreases when the aeration process is performed in the reactor. The acidic nitrogen (NO ₃ ^-- N) is increased and the nitrification process starts and is approaching the end point, whereas the ammonia nitrogen (NH ₄ ⁺ -N) is increased and the nitric acid (NO ₃ -N) is increased. ^The decrease in -N) may be inferred by the introduction of organic carbon sources (such as influent sewage and sludge inflows) and approaching the end point due to denitrification.

Determination of the correlation lines between concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N), which are control variables to change each operation mode, based on the sewage treatment trial run or Lab reactor operation data Done. For example, if the end point of the mode is an ammonia concentration of a mg / L and a nitrate nitrogen concentration of b mg / L, the relationship threshold at which each concentration change in a mode switches the mode of the reactor (a For example, it can be applied to switch to the next mode immediately when the data is reached or b mg / L) is entered or beyond the range.

The operation mode and the progress time setting module 631c set the bioreactor by selecting one operation mode among A, B, C, and D operation modes as shown in FIG. 9. The inflow and flow of sewage, the outflow of treated sewage, and aeration and no aeration sections are set for each operation mode.

Operation mode and time setting module 631c is a section of Tank3 (Tank3a, Tank3b, Tank3c, Tank3d) by the nitrification and denitrification state of Tank1 or Tank2 executing the aeration process according to A, B, C, D operation modes. Anaerobic and aerobic processes (non-aeration process) to denitrate nitrate nitrogen and to remove residual organic substances and to induce nitrification and excess intake of phosphorus (aeration process) to help release phosphorus in sewage inflow. Set the operation mode.

The operation mode and the time setting module 631c basically set each operation mode at a predetermined time interval (for example, one hour), but the inflow water quality introduced into the bioreactor, the microbial state of the bioreactor, and the outflow from the bioreactor The operating time of each mode can be adjusted according to the conditions of the effluent quality and the sludge interface of the final settling basin.

A operation mode is a flow path in which sewage flows into Tank1 and flows out of Tank2 through Tank3, Tank1 performs aeration process, and Tank2 operates in aeration process.

When the operating mode is set, sewage flows into the rear of Tank1 with return sludge. At this time, up to the section of Tank1 and Tank3a is aeration state, the influent and conveying sludge is introduced into an oxygen-free state where the air supply is stopped. The tank3b, tank3c, tank3d and tank2 sections are maintained in aerobic conditions with abandonment, and the influent and return sludges are moved in a plug-flow form without stirring, and finally maintain the aerobic state. The treated water is discharged to the final settling basin.

B operation mode is a flow path in which sewage flows into Tank3c and flows out of Tank2. Tank1 is a pattern in which aeration process and Tank2 are operated by aeration process.

When the B operation mode is set, the inflow of sewage and conveying sludge to Tank1 according to the B operation mode is stopped, and the sewage and conveying sludge flows into Tank3c. At this time, Tank_c maintains an oxygen-free state in which air supply is stopped, and the remaining aeration tank sections Tank1, Tank2, Tank3a, Tank3b, and Tank3d are supplied with air to maintain an exhalation state.

C operation mode is a flow path in which sewage flows into Tank2 and flows out of Tank1 through Tank3, where Tank1 is an aeration process and Tank2 is a non-aeration process.

When the C operation mode is set, the sewage and return sludge flow in the B operation mode is interrupted, and the sewage and return sludge flows into the rear end of Tank2 in a symmetrical manner with the A operation mode, and Tank2 and Tank3d are switched to aerobic operation to be anaerobic. It is operated under the condition. Tank3a, Tank3b, Tank3c and Tank1 are maintained in aerobic aeration conditions, and the inflow of sewage and conveyed sludge is moved to a plug-flow form in which no agitation is carried out and finally treated while maintaining an aerobic state. Drain the water to the final settling basin.

D operation mode is a flow path in which sewage flows into Tank3b and flows out of Tank1, where Tank1 is the aeration process and Tank2 is the aeration process.

When the D operation mode is set, the inflow of sewage and conveying sludge in the C operation mode is stopped, and the sewage and conveying sludge flows into Tank3b. At this time, Tank_b maintains an oxygen-free state in which the air supply is stopped, and the remaining aeration tank sections Tank1, Tank2, Tank3a, Tank3c, and Tank3d are supplied with air to maintain an aerobic state, and the final effluent flows into the aerobic state.

The operation mode and the progress time setting module 631c variably set the processing time for each operation mode according to the load amount of the influent, and accordingly, the processing time for each operation mode may be lengthened or omitted.

10 to 14 are diagrams for explaining the aeration / aeration interval control module according to an embodiment of the present invention.

Referring to FIG. 10, the abandonment / aeration section control module 632 includes a data validation module 632a, a denitrification / nitridation state detection module 632b, and a grid driver calculation and correction module 632c.

The data validation module 632a validates the concentrations of ammonia nitrogen (NH ₄ ⁺ -N), nitrate nitrogen (NO ₃ ^-- N), and phosphate phosphorus in the bioreactor received from the field control device 400. Only validated data is transmitted to the denitrification / nitridation state detection module 632b.

Denitrification / Nitrification Status Detection Module 632b uses ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) concentration measurements in Tank1 and Tank2 based on the MHI operator setting inputs. Calculate the ratio of sum and nitrate nitrogen, and control the aeration / aeration period of Tank3 according to the number of abandonment sections of Tank3 according to the pre-set ratio of ammonia nitrogen and nitrate nitrogen. Change the time.

In the bioreactor, the O _{2 content} is constantly operated in relation to ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N). The denitrification / nitrification state detection module 632b can infer a ratio relationship.

Since the amount of organic matter in the influent sewage is an important factor limiting the removal performance of nitrogen and phosphorus in the sewage treatment process, it is necessary to utilize the small amount of organic matter as effectively as possible and to increase the nitrogen removal efficiency by inducing endogenous denitrification of microorganisms.

In order to implement this, APID method uses ammonia nitrogen (NH ₄ ⁺ -N) which can represent the state of Tank1 and 2 reactors to control parameters of Tank3 to enable dynamic plug (variability of aeration and aeration). The use of nitrate nitrogen (NO ₃ ^-- N) ratios allows the scope of nitrification and denitrification to be expanded.

The control parameters of the Dynamic Plug are the concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the reaction tank.Ammonia nitrogen (NH ₄ ⁺ -N) in the reaction tank is nitrate nitrogen (NO If it is higher than ₃ ^-- N, it means that the current concentration of ammonia nitrogen (NH ₄ ⁺ -N) in the reaction tank to increase the volume of the aerobic process to perform nitrification (see Fig. 10), on the contrary If the ratio of nitrate nitrogen (NO ₃ ^-- N) in the high, this means that the volume of the anaerobic process should be denitrogenated through endogenous denitrification of the microorganisms (see Figure 13).

This ratio can be calculated based on the operator's experience, the operation of the biological reactor is shown in FIG. Referring to FIG. 14, non-aeration / aeration is set at a ratio of 1: 3, 1: 1, 3: 1, 7: 1.

At the aeration condition of each mode, the organic matter is removed and the nitrification process is performed in which ammonia nitrogen (NH ₄ ⁺ -N) is converted to nitrate nitrogen (NO ₃ ^-- N). Acidic nitrogen (NO ₃ ^-- N) is the carbon source as part of the organic material introduced, and denitrification of nitric acid (NO ₃ ^-- N) by the sludge returned in the biological reaction tank. All influent flows into the aerobic zone to cause denitrification and low concentrations of nitrate nitrogen to allow sludge to have good sedimentability.

The operation mode measures the concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ -N) between the aeration and non-aeration devices, and calculates the time and process due to the position shift of nitrification and denitrification through mutual distribution logic. The process progress and end point are extracted by calculation and logic, and it is applied to set the aeration / aeration section of Tank 1 and 2 based on the extracted logic and convert it into the operation mode that inflows sewage into the aeration section.

Grid operator calculation and correction module 632c is based on the MHI operator setting input and operation mode values, and the ammonia nitrogen (NH ₄ ⁺ -N) and nitrogen nitrate (NO) progressed by the process of Tank 1 and Tank 2 ₃ ^-- N) From the concentration measurement, the mutual ratio calculated by the denitrification / nitridation state detection module 632b is determined by determining the number of abandoned or anaerobic sections of Tank 3 according to the process state (ratio) of Tank 1 or Tank 2. The residence time of the anaerobic / anaerobic / aerobic process can be changed.

The grid operator calculation and correction module 632c promises in advance the correction of the control signal according to the activation of the aeration state and the change of position of the aeration condition. The signal is converted into a signal form (eg, Grid Code) and transmitted to the field control device 400.

15 to 17 are views for explaining the dissolved oxygen control module according to an embodiment of the present invention.

Referring to FIG. 15, the dissolved oxygen control module 633 according to an embodiment of the present invention includes a data validity verification module 633a, a load target DO setting module 633b, and a tank selection module 633c.

The data validation module 633a verifies the validity of the ammonia nitrogen, the nitrate nitrogen, and the air volume dissolved oxygen received from the field control device 400 and transfers only the verified data to the DO target value setting module 633b for each load.

The tank selection module 633c selects a tank in which abandonment is in progress based on the operation mode information, and sets the DO concentration control target value by the DO target value setting module 633b for each load together with the information of the selected tank. To be sent).

Referring to FIGS. 16 and 17, the DO target value setting module 633b for each load determines a target value for controlling the amount of air supplied to maintain and control the oxygen concentration when the tanks 1 and 2 are abandoned. Oxygen must be supplied for the respiratory action of microorganisms and biological treatment of sewage, and operation is required to supply air through a blower that supplies air for sufficient mixing to float the solids in the bioreactor.

The DO target value setting module 633b for each load determines the dissolved oxygen concentration set-point and the maximum allowable value according to the ammonia nitrogen concentration of the abandoned aeration section through the ammonia nitrogen concentration and the dissolved oxygen concentration measurement value of the aeration zone. The dissolved oxygen concentration is determined sequentially to control the dissolved oxygen concentration of the aeration section Tank1 or 2 using PID control.

The DO target value setting module 633b for each load is determined by calculating an appropriate dissolved oxygen target value based on ammonia nitrogen, nitrate nitrogen, and air content dissolved oxygen in the bioreactor.

Since nitrification is carried out in a biological reactor

NH ₄ Volume + O ₂ Volume-> NO ₃ Volume

Since the control relationship and flow are inferred by the simple reaction of, the target to be controlled is O ₂ (or dissolved oxygen DO) and the necessary relation variables of control are NH ₄ and NO ₃ .

In addition, ammonia (NH ₄ ) (reaction amount), oxygen (requirement amount), and nitrate (output amount) are based on quantitative chemical reactions, and NH ₄ , NO _3, and DO meters are installed in the control system. It can be measured, and by the measured NH ₄ and NO ₃ can be inferred the amount of oxygen required at the time of aeration.

Furthermore, since the reaction flows from left to right in the reaction equation, NH ₄ and NO ₃ are inversely operated by the reaction equation of consumption and output. In other words, NH ₄ is decreased and NO ₃ is increased by the O ₂ consumption reaction.

From this mutual reaction relationship, the required O ₂ demand amount can be set by NH ₄ and NO ₃ . DO load curve of the required amount of each of the NH ₄ NO ₃ and DO requirements by one electron is proportional NO ₃ is in inverse proportion.

Each load curve has a theoretical linear curve, but it has a nonlinear proportional curve due to actual operational factors such as season, time, load, water content ratio, microbial activity, water temperature and climate. In addition, the plotting of each nonlinear proportional curve plots the target value based on data obtained during the initial trial operation of the influent sewage of the wastewater treatment plant.

OUR (Oxygen Uptake Rate) is the rate at which microorganisms use oxygen in the process of microorganisms combining NH ₄ (ammonia nitrogen) and oxygen in the reactor and converting it into NO ₃ (nitric acid nitrate) (biological water treatment process). As the oxygen intake rate can be used as a measure of the activity of the microorganism. In order to apply the oxygen intake rate to the process, it is necessary to consider the unit microorganisms, and represents the amount of oxygen consumed by the unit microorganisms during the unit time. Oxygen uptake rate is proportional to the oxidation of COD and ammonia, and can be used as a data to determine the final quality of the effluent depending on the load conditions.

Oxygen consumption by microorganisms is directly related to biomass increases and metabolic processes associated with substrate degradation are associated with respiratory rate. Since it is impossible to measure this respiration rate in the microorganism itself, it is measured from the water or wastewater containing the microorganism. The applied respiratory rate calculation can be calculated by indirect method by dissolved oxygen (DO) measurement as follows.

Oxygen uptake rate per unit time = O ₂ supply per unit time-DO change per unit time

As a result, the oxygen consumption rate (oxygen uptake rate) by the microorganism can be calculated.

18 and 20 are diagrams for explaining the sludge conveyance control module according to an embodiment of the present invention.

Referring to FIG. 18, the sludge conveyance control module 634 according to an embodiment of the present invention may include a data validation module 634a, a target concentration and conveyance flow rate 634b, a PID operation module 634c, and a conveyance position detection module. 634d.

The data validation module 634a verifies the validity of the return flow rate, the influent flow rate, the return MLSS, the reactor MLSS, and the sludge interface, and delivers only the validated data to the target concentration and return flow rate module 634b.

The target concentration and return flow module 634b uses the return sludge flow rate, influent flow rate, return MLSS concentration, effluent turbidity (reaction tank MLSS), and final settling sludge interface measurements to maintain the MLSS concentration of the bioreactor, or The flow rate is determined according to the conveyance rate.

The conveyed sludge flow rate control performed by the target concentration and conveyed flow rate module 634b has two important purposes. Returning the sludge to the reactor where the active biological process is taking place and maintaining the sludge in the settling tank at a suitable height to avoid excess sludge in the effluent stream. The return sludge flow control allows to maintain a constant sludge concentration in the reactor and to maintain a sludge balance.

% Flow (Control Volume) = (Return Flow) / Inflow Sewage) + F (MLSS Change)

However, F (MLSS variation) is a return flow adjustment function due to MLSS variation

The PID operation module 364d controls the conveying pump of the field facility by transmitting the field control device 400 by adjusting the conveying flow rate (%) signal so that the target conveying flow rate determined by the target concentration and conveying flow rate module 634b is maintained. It is used to

The conveying position detecting module 634d detects a position at which the sludge should be conveyed in the bioreactor based on the HMI operator setting input, and transmits the sludge valve to the field control device 400 as a RAS distribution control target value to provide the conveying sludge valve of the field facility. Used to control

The RAS distribution performed by the conveyance position detection module 634d is to effectively assist in the activation of sludge and improved denitrification and phosphorus release by maintaining the MLSS concentration uniformly in the biological reactor and conveying the short cycle. For example, as shown in FIG. 20, inflow of an anaerobic process may improve phosphorus removal efficiency, inflow of anoxic process may improve nitrogen removal efficiency, and aerobic process inflow may improve nitrification and organic matter removal efficiency.

The distribution method can be applied to the method of returning to the sewage inflow tank determined at each operation mode (simultaneous inflow) and to the method of returning to Tank3b and Tan3c sections regardless of the operation mode (shear inflow). RAS return location = F (TN, OUR) can be represented.

That is, the conveying position detecting module 634d determines the conveying position by the N-load state by TN (= NH ₄ + NH ₃ ) and the MLSS state by the result of nitrification / denitrification by OUR.

21 and 22 are screen diagrams for describing an HMI processing module according to an embodiment of the present invention.

The Human-Machine Interface (HMI) processing module 640 provides a user interface for a user. The HMI processing module 640 allows a user to know the operation status and process control status of the sewage treatment process, and provides an interface for directly setting target values or parameters related to process control.

To this end, the HMI processing module 640 may provide, for example, a facility management menu, an information management menu, an internet monitoring control menu, an automatic operation execution menu, a unified messaging service menu, and the like.

The facility management menu may provide information on facility history management and maintenance history of sewage treatment site facilities. The information management menu may provide information for comprehensively managing the operating situation of the sewage treatment site. The Internet surveillance control menu provides a function to monitor and control the sewage treatment site facilities in real time using the Internet. The automatic operation execution menu provides a function to monitor / control the treatment efficiency of the bioreactor. The unified messaging service menu provides a function of transmitting an on-site alert to an administrator by SMS, e-mail, or fax.

As illustrated in FIG. 21, the HMI processing module 640 is hierarchically configured to provide screen information. The HMI processing module 640 allows an operator to display the operation state and process of the sewage treatment facility through a menu display method for each component. Make management more effective.

The HMI processing module 640 may be constructed using, for example, commercial package software running on Xindow XP so as to facilitate addition and modification to quickly grasp the operation state of the entire sewage treatment process and perform necessary control functions.

The HMI processing module 640 may provide a trend chart displaying a real-time operating situation of the entire process and a temporal change of the main measurement through a processing diagram. The operator can immediately see the operating situation by looking at the trend chart.

In addition, the HMI processing module 640 changes the operation mode, the inflow water level, the various flow rates, and the water quality measurement values by double-clicking the corresponding object element so as to set the automatic operation mode and the manual operation mode. Trend charts can be viewed and can be implemented to allow manual operation of valves and pumps and to change set points.

In addition, as shown in FIG. 22, the HMI processing module 640 collectively displays a sewage treatment plant schematic diagram, an aeration tank screen, and measurement values of a measuring device on a basic menu screen for the operation and operation of the entire process. An analog screen, a digital screen that shows the operation status of valves and pumps collectively, and a real-time trend and past trend screen that show the temporal change of measured values can be implemented.

1 is a block diagram showing a sewage treatment system according to an embodiment of the present invention.

FIG. 2 is a perspective view schematically illustrating a bioreactor provided in a sewage treatment site facility in a sewage treatment system according to an embodiment of the present invention shown in FIG. 1.

Figure 3 is a schematic diagram showing the sewage treatment plant facilities in the sewage treatment system according to an embodiment of the present invention.

Figure 4 is a cross-sectional view showing the interior of the biological reactor of the sewage treatment site facilities according to an embodiment of the present invention.

5 is a block diagram illustrating an APID method control and monitoring apparatus in a sewage treatment system according to an embodiment of the present invention.

6 to 9 are views for explaining the operation of the driving mode control module according to an embodiment of the present invention.

10 to 14 are diagrams for explaining the aeration / aeration interval control module according to an embodiment of the present invention.

15 to 17 are views for explaining the dissolved oxygen control module according to an embodiment of the present invention.

18 to 20 are diagrams for explaining the sludge conveyance control module according to an embodiment of the present invention.

21 and 22 are screen diagrams for describing an HMI processing module according to an embodiment of the present invention.

Claims (21)

APID (Advaced Phased Isolation Ditch) for sewage treatment system including a sewage treatment site facility having a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facility in real time according to a set target value. As a method control and monitoring device, A data storage unit for storing measurement and operation data of the sewage treatment site equipment transmitted from the field control device; Based on the measurement and operation data of the sewage treatment site facilities, grasp the progress of nitrification and denitrification of the bioreactor, and operation mode control for setting and switching the section of anaerobic, anaerobic, and aerobic processes in the bioreactor. It includes a process control module for determining the target value for performing the residence time control for each process, the dissolved oxygen concentration control in the aerobic process, the inlet location and flow control of the sewage and return sludge, and transmits to the field control device, The process control module APID method control and monitoring device for validating the measurement and operation data received from the field control device. The method according to claim 1, It further includes a human-machine interface (HMI) treatment module that provides an interface for reporting the operating status and process control status of the sewage treatment process, and a user setting function for a target value or parameter related to the process control. APID process control and monitoring device. delete The method according to claim 1, If it is determined that there is an error in the network connection with the site control device, the process control module is configured to perform a single operation mode for controlling the sewage treatment site facility based on a previously transmitted target value. Directing APID method control and monitoring device. APID (Advaced Phased Isolation Ditch) for sewage treatment system including a sewage treatment site facility having a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facility in real time according to a set target value. As a method control and monitoring device, A data storage unit for storing measurement and operation data of the sewage treatment site equipment transmitted from the field control device; Based on the measurement and operation data of the sewage treatment site facilities, grasp the progress of nitrification and denitrification of the bioreactor, and operation mode control for setting and switching the section of anaerobic, anaerobic, and aerobic processes in the bioreactor. It includes a process control module for determining the target value for performing the residence time control for each process, the dissolved oxygen concentration control in the aerobic process, the inlet location and flow control of the sewage and return sludge, and transmits to the field control device, The process control module, An operation mode control module configured to determine a target value for controlling a plurality of operation modes such that switching between time and mode of the nitrification and denitrification sections of the aeration and non-aeration sections in the biological reactor is possible; Aeration / Aeration section control module for determining a target value for performing aeration / aeration control according to the number of aeration section of the biological reactor to change the residence time of the anaerobic / anaerobic / aerobic process; A dissolved oxygen concentration control module for determining a target value for controlling the amount of air supplied to maintain and control the oxygen concentration when the biological reactor is abandoned; And a sludge conveyance control module for determining a target value for controlling the flow rate and conveyance position of the conveying sludge in order to maintain the MLSS concentration of the bioreactor. The method according to claim 5, The operation mode control module measures the concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the aeration and aeration periods, and provides data through the aeration / aeration state cross-distribution logic. APID process control and monitoring device that performs extraction and nitrification section time and mode switching based on the extracted data. The method according to claim 5, The aeration / non-aeration zone control module calculates the ratio of sum of ammonia nitrogen and nitrate nitrogen through the measurement of concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the bioreactor. APID method control and monitoring to change the residence time of anaerobic, anaerobic, and aerobic processes by controlling the aeration / aerobic sections according to the number of aeration sections of the bioreactor according to the pre-set ratio of ammonia nitrogen and nitrate nitrogen Device. The method according to claim 5, The dissolved oxygen concentration control module is a dissolved oxygen concentration set-point and the maximum allowable dissolved oxygen concentration according to the ammonia nitrogen concentration of the aeration section previously set through the ammonia nitrogen concentration and dissolved oxygen concentration measurement value of the aeration zone. APID method control and monitoring device for controlling the dissolved oxygen concentration in the abandoned section after sequentially determining. The method according to claim 5, The sludge conveyance control module determines the flow rate according to the conveyed sludge concentration or conveyance rate by using the inflow flow rate, conveyed sludge flow rate, conveyed MLSS concentration, discharge water turbidity, and final settling sludge interface measurement value, and the turbidity of the sludge interface and discharge water of the final settling basin. APID method control and monitoring device for correcting the conveyance rate by using and to control the transport position in accordance with the operation mode. The method according to claim 6, The biological reaction tank comprises a first intermittent aeration tank consisting of three sections Tank3b, Tank3a, and Tank 1, and a second intermittent aeration tank consisting of three sections Tank3c, Tank3d, and Tank2, wherein the Tank3b and Tank3c form a flow path. Connected to each other through; The operation mode control module selectively operates A, B, C, D operation mode, The A operation mode is a flow path in which sewage flows into Tank1 and flows out of Tank2 through Tank3, Tank1 performs aeration process, and Tank2 is a pattern operated by aeration process. The B operation mode is a flow path in which sewage flows into Tank3c and flows out of Tank2, Tank1 is a pattern of aeration, Tank2 is operated by aeration process, The C operation mode is a flow path in which sewage flows into Tank2 and flows out of Tank1 through Tank3, where Tank1 is a pattern of operating in aeration process and Tank2 in aeration process. The D operation mode is a flow path in which sewage flows into Tank3b and flows out of Tank1, where Tank1 is a non-aeration process and Tank2 is a pattern for operating in aeration process. The method according to claim 7, The biological reaction tank is composed of a first intermittent aeration tank consisting of three sections Tank3b, Tank3a, and Tank1, and a second intermittent aeration tank consisting of three sections Tank3c, Tank3d, and Tank2. Connected to each other; The abandonment / aeration interval control module, The ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) concentration measurement values of the Tank 1 and Tank ₂ are calculated to calculate the ratio of the sum of the ammonia nitrogen and the nitrate nitrogen, and the previously set ammonia nitrogen APID method control and monitoring device for controlling the aeration / aeration period of the tank 3 according to the number of aeration section of the tank 3 according to the sum and the ratio of the nitrate nitrogen sum. APID (Advaced Phased Isolation Ditch) for sewage treatment system including a sewage treatment site facility having a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facility in real time according to a set target value. As a method control and monitoring method, Determining the progress of nitrification and denitrification of the biological reaction tank in the biological reaction tank based on the measurement and operation data of the sewage treatment site equipment transmitted from the field control device; Operation mode control for setting and converting sections of anaerobic, anaerobic, and aerobic processes in the biological reactor by reflecting the progress of nitrification and denitrification of the biological reactor, residence time control for each process, and dissolved oxygen concentration control in the aerobic process Determining a target value for performing the inflow position and flow control of the sewage and conveying sludge, and transmitting to the field control device, Validating the measurement and operation data transmitted from the field control device APID method control and monitoring method further comprising. delete The method according to claim 12, If it is determined that there is an error in network connection with the site control device, instructing the site control device to perform a single operation mode for controlling the sewage treatment site facilities based on a previously transmitted target value. APID method control and monitoring methods, including. APID (Advaced Phased Isolation Ditch) for sewage treatment system including a sewage treatment site facility having a biological reaction tank consisting of two intermittent aeration tanks, and a site control device for controlling the sewage treatment site facility in real time according to a set target value. As a method control and monitoring method, Determining the progress of nitrification and denitrification of the biological reaction tank in the biological reaction tank based on the measurement and operation data of the sewage treatment site equipment transmitted from the field control device; Operation mode control for setting and converting sections of anaerobic, anaerobic, and aerobic processes in the biological reactor by reflecting the progress of nitrification and denitrification of the biological reactor, residence time control for each process, and dissolved oxygen concentration control in the aerobic process Determining a target value for performing the inflow position and flow control of the sewage and conveying sludge, and transmitting to the field control device, The determination of the target value, Determining a target value for controlling a plurality of operation modes so that switching between time and mode of nitrification and denitrification in the aeration and non-aeration sections can be performed in the biological reactor; Determining a target value for the aeration / aeration period control according to the number of aeration sections of the bioreactor to change the residence time of the anaerobic / anaerobic / aerobic process; Determining a target value for controlling the amount of air supplied to maintain and control the oxygen concentration upon aeration of the bioreactor; Determining a target value for controlling the flow rate and conveying position of the conveying sludge in order to maintain the MLSS concentration of the bioreactor. The method according to claim 15, Steps for controlling the plurality of driving modes, By measuring the concentrations of ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) in the aeration and aeration sections, the data are extracted through the aeration and aeration state cross-distribution logic, and the extracted data is extracted. APID method control and monitoring method comprising performing a nitrification and denitrification interval time and mode switching based. The method according to claim 15, The step for controlling the abandonment / aeration period The ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) concentration measurement values of the bioreactor are calculated to calculate the ratio of the sum of ammonia nitrogen and nitrate nitrogen, and the preset ammonia nitrogen sum APID method control and monitoring method to change the residence time of anaerobic, anaerobic, and aerobic processes by controlling the aeration / aeration period according to the number of aeration sections of the bioreactor according to the ratio of the nitrate and nitrogen nitrate. The method according to claim 15, The step for controlling the amount of air, After measuring the ammonia nitrogen concentration and dissolved oxygen concentration in the aeration zone, the set-point and the maximum allowable dissolved oxygen concentration according to the ammonia nitrogen concentration in the aeration zone were determined in advance. APID method control and monitoring method to control the dissolved oxygen concentration of. The method according to claim 15, Steps for controlling the flow rate and conveying position of the conveying sludge, The flow rate is determined according to the return sludge concentration or the return rate using measured inflow, return sludge flow rate, return MLSS concentration, discharge water turbidity, and final settling sludge interface, and the return rate is corrected using the sludge interface of the final settling basin and turbidity of the discharge water. APID method control and monitoring method for controlling the return position according to the driving mode. The method according to claim 16, The biological reaction tank comprises a first intermittent aeration tank consisting of three sections Tank3b, Tank3a, and Tank 1, and a second intermittent aeration tank consisting of three sections Tank3c, Tank3d, and Tank2, wherein the Tank3b and Tank3c form a flow path. Connected to each other through; The plurality of operation modes include A, B, C, D operation mode, The A operation mode is a flow path in which sewage flows into Tank1 and flows out of Tank2 through Tank3, Tank1 performs aeration process, and Tank2 is a pattern operated by aeration process. The B operation mode is a flow path in which sewage flows into Tank3c and flows out of Tank2, Tank1 is a pattern of aeration, Tank2 is operated by aeration process, The C operation mode is a flow path in which sewage flows into Tank2 and flows out of Tank1 through Tank3, Tank1 is a pattern of aeration process, and Tank2 is a pattern of aeration process. The D operation mode is a flow path in which sewage flows into Tank3b and flows out of Tank1, where Tank1 is a non-aeration process and Tank2 is a pattern for operating in aeration process. The method according to claim 17, The biological reactor consists of a first intermittent aeration tank consisting of three sections Tank3b, Tank3a, and Tank 1, and a second intermittent aeration tank consisting of three sections Tank3c, Tank3d, and Tank2. The tank3-b and Tank3- c are connected to each other via a flow path; The step for controlling the abandonment / aeration period, The ammonia nitrogen (NH ₄ ⁺ -N) and nitrate nitrogen (NO ₃ ^-- N) concentration measurement values of the Tank 1 and Tank ₂ are calculated to calculate the ratio of the sum of the ammonia nitrogen and the nitrate nitrogen, and the previously set ammonia nitrogen APID method control and monitoring method for controlling the aeration / aeration of the tank 3 according to the number of aeration section of the tank 3 according to the ratio of the sum and the nitrate nitrogen sum.

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