KR101871931B1 - Operating method of integrated nitrogen control system of wastewater disposal equipment - Google Patents

Abstract

The present invention provides an operating method for an integrated nitrogen control system of a wastewater and sewage disposal facility, capable of stably treating sewage and wastewater and economically operating a disposal facility by reducing energy consumption. According to the present invention, the operating method for an integrated nitrogen control system of a wastewater and sewage disposal facility includes: a TN desired value setting step of setting a desired value of total nitrogen which is a sum of nitrate nitrogen and ammonia nitrogen; an NH_4-N desired value and an NO_3-N desired value setting step of individually setting the desired value of the nitrate nitrogen and the desired value of the ammonia nitrogen; an NH_4-N measuring step of measuring the amount of the ammonia nitrogen in real time in an aerobic zone; a comparison step of comparing the desired value of the ammonia nitrogen in the NH_4-N desired value and the NO_3-N desired value setting step and the amount of the ammonia nitrogen measured in the real time in the NH_4-N measuring step; a first transferring step of transferring sludge from the aerobic zone to a first anaerobic zone in a case that it is determined in the comparison step that the measured value of the ammonia nitrogen is smaller than the desired value of the ammonia nitrogen which is set; and a second transferring step of transferring the sludge of a second anaerobic zone to the first anaerobic zone in a case that it is determined in the comparison step that the measured value of the ammonia nitrogen is larger than or is the same as the desired value of the ammonia nitrogen which is set.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of operating an integrated nitrogen control system of a wastewater treatment plant,

More particularly, the present invention relates to an integrated nitrogen control system and method for operating a wastewater treatment plant, which can reduce energy consumption, maximize the denitrification and denitrification, To an operation method of an integrated nitrogen control system of a wastewater treatment facility.

Generally, the removal of nitrogen from sewage and wastewater occurs through nitrification of ammonia nitrogen (aerobic condition) followed by denitrification (anoxic condition) reaction, releasing gas form (N ₂ ) into the atmosphere, Nitrogen is released to the water system untreated. This nitrification is a nitrification microorganism that oxidizes ammonia nitrogen to nitrate nitrogen by using oxygen as an electron donor. It is essential to apply the blower to supply oxygen to the reaction tank.

On the other hand, denitrification is a reaction in which oxidized nitroxides are reduced to nitrogen gas by denitrifying microorganisms under anoxic conditions, and takes place under anaerobic conditions in which free oxygen is not present, and organic matter is essentially consumed. In order to supply the organic matter for the denitrification, it is economical to dispose the anoxic tank in front of the oxic tank to efficiently use the organic matter in the influent water for denitrification.

For this reason, the oxidized nitroxide needs to be internally transported from the aerobic tank to the anoxic tank, and the nitrogen removal efficiency is changed by the internal recycle rate. Further, when the nitrogen removal efficiency is inadequate due to the lack of organic substances required for denitrification, Do.

However, the conventional nitrogen control system and method are problematic in that the characteristics of inflow sewage and wastewater change according to seasonal, regional, and time zone, and skilled operators do not actively cope with such changes, In contrast, when the concentration of the inflow sewage and wastewater is low and the inflow is low, the aeration amount, the internal transfer amount, and the external carbon source injection amount become excessive, which causes a problem that energy consumption is unnecessarily consumed.

Korean Patent Publication No. 10-2012-0079899

The present invention relates to an apparatus and a method for measuring nitrogen oxides (NOx) and nitrogen oxides (NOx) for nitrogen removal, in which dissolved oxygen (DO) for nitrification, internal transport of nitrate, and external carbon source injection are measured and integrated in real- The present invention provides a method for operating an integrated nitrogen control system of a wastewater treatment facility capable of stable treatment of sewage and wastewater by controlling the operation of the wastewater treatment plant and operating the treatment plant economically by reducing energy consumption.

According to an aspect of the present invention, there is provided an apparatus for anaerobic digestion, comprising: a first anoxic tank in which lower and wastewater are introduced and denitrification proceeds in an anaerobic atmosphere; An anaerobic tank in which treated water treated in an anoxic tank flows in and an outflow reaction of the treated water proceeds in an anaerobic state; and an anaerobic tank disposed in a rear of the anaerobic tank for introducing the treated water treated in the anaerobic tank, A second anoxic tank disposed in the rear of the oxic tank to allow the treated water treated in the oxic tank to flow in and the denitrification reaction of the treated water proceeds in an anaerobic atmosphere; An aeration section including a blower, and a first half for conveying the sludge of the aerobic tank to the first anoxic tank A second transfer section for transferring the sludge of the second anoxic tank to the first anoxic tank, an external carbon source supply section for injecting an external carbon source into the second anoxic tank, The amount of dissolved oxygen and the amount of ammonia nitrogen in the aerobic tank and the amount of nitrate nitrogen in the second anoxic tank are respectively connected to the second transport unit and the external carbon source supply unit to correspond to the dissolved oxygen amount, the ammonia nitrogen amount and the nitrate nitrogen amount And an integrated nitrogen control section for controlling an amount of air blown by the blower, an inner transport of the first transport section, and an inner transport of the second transport section, wherein the ammonia nitrogen and the nitrogen A TN target value setting step (S10) in which a target value of total nitrogen which is the sum of the acid nitrogen is set; Setting a NH ₄ -N target value and a NO ₃ -N target value (S20) in which a target value of the ammonia nitrogen and a target value of the nitrate nitrogen are respectively set; An NH ₄ -N measurement step (S 30) in which the ammonia nitrogen amount is measured in real time in the oxic tank; Comparison step in which the NH ₄ a measurement in real time, the ammonia in the measurement step -N sex nitrogen content and the NH ₄ NO ₃ -N target value and the target value of the ammonium nitrogen in the comparison set -N target value setting step (S40); The internal conveyance by the first conveyance unit is performed and the internal conveyance by the second conveyance unit is performed when the measured value of the ammonia nitrogen amount is found to be smaller than the set value of the set ammonia nitrogen in the comparison step (S60); Wherein when the ammonia nitrogen measurement value is found to be equal to or greater than a target value of the set ammonia nitrogen in the comparison step, the internal conveyance by the second conveyance unit is carried out and the internal conveyance by the first conveyance unit (S90); A NO ₃ -N target value changing step of changing the target value of the nitrate nitrogen to a lower value when it is confirmed in the comparing step that the measured ammonia nitrogen amount is equal to or greater than the set target ammonia nitrogen value (S70); A NO ₃ -N measuring step (S 100) in which the nitrate nitrogen amount is measured in real time in the second anoxic oxygen; And a step (S110) of adjusting an internal transport amount in the second transport step corresponding to a rate of change with respect to a change amount of the nitrate nitrogen amount measured from the NO ₃ -N measurement step, wherein the NO ₃ -N target value in the target value of the target value of the nitrate nitrogen is, the NH ₄ NO ₃ -N -N target value and target value setting nitrate nitrogen (NO ₃ -N) set in the step (S20) in the change step (S70), The ammonia nitrogen (NH ₄ -N) measured in the NH ₄ -N measurement step (S 30) is subtracted from the NH ₄ -N target value and the NO ₃ -N target value setting step S20) the operating method of the ammonium nitrogen (NH ₄ -N) wastewater treatment plant integrated control system of the nitrogen is changed to a value obtained by adding a target value of the set is provided in the.

The operation method of the integrated nitrogen control system of the wastewater treatment facility may include adjusting the internal transport amount in the first transport step to correspond to the rate of change of the amount of ammonia nitrogen measured from the H ₄ -N measurement step, And adjusting the amount of external carbon source injected into the second anoxic tank by the external carbon source supply unit corresponding to a rate of change of the amount of nitrate nitrogen measured from the NO ₃ -N measurement step.

The operation method of the integrated nitrogen control system of the wastewater treatment facility is characterized in that when the measured value of the ammonia nitrogen amount is smaller than the target value of the set ammonia nitrogen in the comparison step, And a step S50 of maintaining the amount of air to be maintained.

The operation method of the integrated nitrogen control system of the wastewater treatment facility is characterized in that when the ammonia nitrogen amount measurement value is found to be equal to or greater than the target value of the ammonia nitrogen set in the comparison step, that further comprises a blowing air volume increasing step (S80), in step increases the blowing air volume air volume may be adjusted corresponding to the rate of change of the change amount of said ammonium nitrogen content measured by the measurement step H ₄ -N.

The integrated nitrogen control system and operating method of the wastewater treatment facility according to the present invention provides the following effects.

First, the operating parameters of each reactor are measured and integrated in real time, and based on this, the supply of dissolved oxygen (DO) for nitrification of the aeration tank for nitrogen removal, the internal return of the aerobic tank, the internal return of the second anoxic tank, By integrating control of external carbon source injection, stable treatment of sewage and wastewater is possible, and it is possible to operate economical treatment plant by reducing energy consumption, and it is easy to maintain by maintaining target TN value at a certain level.

Second, by optimally adjusting the aeration amount (blowing amount) in response to the fluctuation of the inflow load of the sewage and the wastewater, it is possible to reduce the power consumption, minimize the energy consumption, shorten the trouble period and normalize the DO And stable water quality can be secured.

Third, it is possible to minimize the energy consumption by reducing the power ratio by optimally controlling the amount of internal transportation, increasing denitrification efficiency, inducing denitrification of the first anoxic tank, and minimizing energy consumption.

Fourthly, it is possible to optimize the amount of external carbon source injection to minimize the energy consumption by reducing the cost of medicines, to induce denitrification of residual nitrate after internal transportation, to enable stable operation, and to enhance complete denitrification and induction of phosphorus. Also, it is possible to prevent problems such as untreated COD leakage in the effluent water due to excessive carbon source injection.

Fifth, when the measured value of the ammonia nitrogen in the aerobic tank is compared with the target value, if the target value is larger than the measured value, the sludge of the aerobic tank is internally transported to the first anoxic tank. If the target value is less than or equal to the measured value, 2 sludge in the anoxic tank is changed to be transported to the first anoxic tank, the treatment plant can be economically operated.

Sixth, the calculation of the three arithmetic mean values of the measured values and the rate of change with respect to the change amount are reflected in the control, thereby preventing the malfunction of the system caused by the noise or error of the measuring instrument and precisely coping with the state of the reactor.

1 is a block diagram illustrating an integrated nitrogen control system of a wastewater treatment facility in accordance with an embodiment of the present invention.
2 is a block diagram showing a control flow of the integrated nitrogen control unit of the integrated nitrogen control system of the wastewater treatment facility of FIG.
Fig. 3 is a block diagram showing another embodiment of the integrated nitrogen control system of the wastewater treatment plant of Fig. 1; Fig.
FIG. 4 is a flow chart illustrating a nitrification control flow of an oxic tank in an integrated nitrogen control system operation method of a wastewater treatment facility according to an embodiment of the present invention.
5 is a flow chart showing a flow of denitrification control in a second anoxic tank in the method of operating an integrated nitrogen control system of a wastewater treatment facility according to an embodiment of the present invention.
FIG. 6 is a flow chart showing the flow of denitrification control in the integrated nitrogen control system operating method of the bottom water treatment plant according to another embodiment of the present invention.

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

1 to 3, an integrated nitrogen control system (hereinafter, referred to as 'integrated nitrogen control system') of a wastewater treatment facility according to an embodiment of the present invention includes a first anoxic tank 30 arranged in sequence, 40, the aerobic tank 50, the second anoxic tank 60, the membrane separation tank 70, the aeration section 51, the first transport section 52, the second transport section 62, An external carbon source supply unit 64, a third transport unit 72, and an integrated nitrogen control unit 80. [

In the first anoxic tank (30), denitrification reaction proceeds in an oxygen-free atmosphere due to the inflow of waste water and wastewater. The screen unit 10 and the flow rate adjusting tank 20 are sequentially disposed in front of the first anoxic tank 30 so that the lower and wastewater are filtered through the screen unit 10, Stored in the flow rate adjusting tank 20, and supplied to the first anoxic tank 30.

The anaerobic tank 40 is disposed in the rear of the first anoxic tank 30 so that the treated water treated in the first anoxic tank 30 flows into the anaerobic tank 40 and is treated in the anaerobic state The number of the blowout reaction proceeds. The anaerobic tank 40 is disposed in front of the aerobic tank 50 so as to allow the aerobic tank 50 to consume excessive phosphorus and to induce excessive intake of phosphorus from the aerobic tank 50 do.

According to the above description, the integrated nitrogen control system may be arranged such that the first anoxic tank 30 is disposed at a front end of the anaerobic tank 40, nitrate nitrogen (NO ₃ -N) is supplied from the first anoxic tank 30 to a nitrogen gas (N ₂ ) to remove nitric acid before it is introduced into the anaerobic tank 40, so that the release of phosphorus in the anaerobic tank 40 is more likely to occur.

The aerobic tank (50) is disposed behind the anaerobic tank (40), and the treated water treated in the anaerobic tank (40) flows in. In the exhaust atmosphere, excessive intake of phosphorus in the treated water and ammonia in NO ₂ and NO ₃ The nitrification reaction proceeds. The aerobic tank 50 includes an aeration unit 51 and the aeration unit 51 includes an aeration fan for supplying oxygen to the aerobic tank 50. On the other hand, the sludge in the oxic tank (50) is internally transported to the first anoxic tank (30) through the first transport section (52).

The second anoxic tank 60 is disposed at the rear of the oxic tank 50 so that the treated water treated in the oxic tank 50 flows into the oxic tank 50. The denitrification reaction of the treated water proceeds in an anaerobic atmosphere, Lt; RTI ID = 0.0 > denitrification < / RTI > The second anoxic tank 60 is configured to internally transport sludge and dissolved oxygen of the second anoxic tank 60 to the first anoxic tank 30 through the second transport unit 62.

In the second anoxic tank 60, a large amount of organic matter is consumed in the previous process, and an external carbon source is injected to enhance the denitrification efficiency.

The external carbon source supply unit 64 injects an external carbon source into the second anoxic tank 60 and may be injected through an external carbon injection unit including a known injection nozzle and an injection line.

The separation membrane tank 70 is disposed behind the second anoxic tank 60 and receives the treated water treated in the second anoxic tank 60 to filter suspended substances and the like of the treated water, Pull out and discharge. Here, a known filtration screen or the like can be applied to the separation membrane tank 70, and a detailed description thereof will be omitted.

Meanwhile, in the integrated nitrogen control system, the separation of the aerobic tank 50 and the separation membrane bath 70 can be prevented by removing the separation membrane during the separation membrane cleaning of the separation membrane bath 70, It is possible to carry out in-house cleaning and maintenance is convenient.

The third transfer part 72 serves to transfer the treated water from the separation membrane bath 70 to the oxic tank 50 and supplies the sludge and dissolved oxygen of the separation membrane bath 70 to the oxic tank 50 Thereby eliminating the dissolved oxygen in the separation membrane bath 70. The aerobic tank 50 can reduce the amount of the aerobic tank 50 to be aerated by removing the organic matter or performing the nitrification by utilizing the dissolved dissolved oxygen Energy consumption can be minimized.

The integrated nitrogen control unit 80 is connected to the aeration unit 51, the first transport unit 52, the second transport unit 62, and the external carbon source supply unit 64, The amount of dissolved oxygen and the amount of ammonia nitrogen in the first anoxic tank 50 and the amount of nitrate nitrogen in the second anoxic tank 60 are respectively measured and the amount of blown air of the blower and the amount of nitrate The sludge internal transfer amount of the first transfer section 52 and the sludge internal transfer amount of the second transfer section 62 and the external carbon source injection amount of the second anoxic tank 60 are optimally controlled.

Specifically, the integrated nitrogen control unit 80 measures and verifies in real time the amount of change in the amount of dissolved oxygen, the amount of ammonia nitrogen, and the amount of nitrate nitrogen, which are nitrogen removal factors, and determines, based on the rate of change, The amount of the internal carbon carrier, and the amount of the external carbon source injected, respectively, to improve the nitrogen removal efficiency.

In addition, the integrated nitrogen control unit 80 can actively control according to the rate of change of state of each reaction vessel as well as predictive control by controlling based on the rate of change of each parameter described above, The nitrogen removal efficiency can be improved and efficient operation can be performed.

3 is a view showing another embodiment of the integrated nitrogen control system. In comparison with the integrated nitrogen control system of FIG. 1, when the meter for measuring nitrate nitrogen is not the second anoxic tank 60 And the other configuration is substantially the same as that of the integrated nitrogen control system of FIG. The integrated nitrogen control system measures the amount of nitrate nitrogen in the treated water in the separation membrane bath 70 so that the integrated nitrogen control unit 80 controls the amount of dissolved oxygen and ammonia nitrogen in the aerobic tank 50, 70) In accordance with the nitrate nitrogen amount of the treated water, the blowing amount of the blower, the internal conveying system, the internal conveyance amount and the external carbon source injection amount are optimally controlled in an integrated manner. Here, the nitrate nitrogen amount of the treatment water in the separation membrane bath 70 is similar to the nitrate nitrogen amount of the second anoxic tank 60 because it is the target of the treated water after the denitrification of the second anoxic tank 60 is completed , And there is no interference by the MLSS, it is possible to obtain a more accurate measurement value.

According to the above, the integrated nitrogen control system is configured to measure and integrate the operation parameters of each reaction tank in real time and to supply dissolved oxygen (DO) for nitrification of the oxic tank 50 for nitrogen removal, The internal transportation of the first anoxic tank 50, the internal transportation of the second anoxic tank 60, and the external carbon source injection are optimally controlled in an integrated manner, whereby stable treatment of sewage and wastewater is possible, It is economical because it can reduce usage and external carbon source cost.

Hereinafter, a method of operating an integrated nitrogen control system of a wastewater treatment plant using the integrated nitrogen control system will be described. Detailed description of each component of the integrated nitrogen control system will be omitted.

The integrated nitrogen control system operating method is characterized in that the amount of blowing of the oxic tank (50), the internal transport system, the internal transport amount of the oxic tank (50), the internal transport amount of the second anoxic tank (60) So that effective denitrification is induced and energy consumption is minimized.

First, let us examine the air flow rate control.

The optimal control of the amount of air blown in the oxic tank 50 is performed by measuring the amount of dissolved oxygen of the oxic tank 50 by measuring the dissolved oxygen amount of the oxic tank 50 a plurality of times in real time and measuring the rate of change of the dissolved oxygen amount And controls the optimum air blowing amount of the oxic tank 50 correspondingly.

In other words, the optimal air flow rate control of the oxic tank 50 is performed by setting the set dissolved oxygen required for the operation, measuring the dissolved oxygen of the oxic tank 50 a plurality of times in real time, Wherein dissolved oxygen of the aerobic tank (50) is set to the set dissolved oxygen when the current dissolved oxygen is in a set range with respect to the set dissolved oxygen as compared with the current dissolved oxygen and the set dissolved oxygen required for the operation, And controls the blowing amount through PID control so as to become dissolved oxygen.

The step of controlling the optimum air blowing amount of the oxic tank 50 may include adjusting the proportional control element value according to the rate of change with respect to the change amount of dissolved oxygen in the oxic tank 50 by checking the change amount of dissolved oxygen in the oxic tank 50, If the change rate of the change amount of the dissolved oxygen is larger than 0, the rate of decrease of the dissolved oxygen is determined to be abrupt, and the proportional control element value is increased by 18% to 22%, preferably 20% .

The step of controlling the optimum air blowing amount of the oxic tank 50 may be performed by checking the change amount of dissolved oxygen of the oxic tank 50 and adjusting the proportional control element value according to the change rate, ', It is preferable to determine that the rate of decrease of dissolved oxygen is smooth and to increase the proportional control element value by 8% to 12%, preferably by 10%, which is variable.

As described above, the blowing rate control of the oxic tank 50 can minimize the energy consumption by adjusting the aeration amount according to the situation as described above. By controlling the rate of change of the dissolved oxygen amount change amount, the trouble period can be shortened, It is possible to secure stable water quality through normalization.

Hereinafter, an embodiment of the air flow rate control method will be described with reference to FIG.

First, the dissolved oxygen (DO) of the oxic tank 50 is measured every minute (D _PV ). At this time, the arithmetic average value of the three times dissolved oxygen is determined as the present dissolved oxygen for eliminating errors and noise of the meter, Likewise, the measurement value of dissolved oxygen is averaged three times immediately before it is recognized as dissolved oxygen.

Equation 1

^{_{DO n '= (DO n-}} 2 + DO n-1 + DO n) / 3, ex) DO 3' = (DO 1 + DO 2 + DO 3) / 3,

Then, the set oxygen demand (DO _set ) required for operation is compared with the current dissolved oxygen, and the blowing amount for operating the set DO (DO _set ) is PID control. At this time, And adjusts the proportional control element value (K _p ) according to the rate of change with respect to the amount of change as shown in Equation (3).

Equation 2

DO DO _n ^' = DO ^' _n- DO ^' _{n -1} , ex) △ DO ₅ ^' = DO ₅ ^' _- DO ₄ ^'

Equation 3

△ DO _n ^'' = DELTA DO _n ^' _- DELTA DO _n-1 ^' _, ex) △ DO ₅ ^'' = △ DO ₅ ^' _- △ DO ₄ ^'

Controls the aeration rate according to the above, and if the dissolved oxygen is less than the DO _set , the aeration amount is increased through the rotation speed control.

For example, Δ DO _n ^" (rate of change of dissolved oxygen change) > 0, then a determination that suddenly the dissolved oxygen rate of decrease is proportional to the control element values (K _p) to improve ^{_{20%, △ DO n ''}} ≤ 0 is determined that the dissolved oxygen rate of decrease is gradual and proportional control factor values (K _p) 10%.

Next, the control of the internal conveyance amount of the second anoxic tank 60 will be described.

The optimum control of the internal transfer amount is performed by setting a desired set nitrate nitrogen and by measuring the nitrate nitrogen amount of the second anoxic tank 60 a plurality of times in real time to obtain an arithmetic mean value of the nitrate nitrogen amount measured plural times, And determining the nitrate nitrogen as the acid nitrate, and when the present nitrate nitrogen is in the range set for the target nitrate nitrogen to be set as compared with the present nitrate nitrogen and the target nitrate nitrogen to be set, ) Is controlled by PID control so that the nitrate nitrogen of the nitrate nitrogen corresponds to the set nitrate nitrogen. That is, the optimal control of the internal transport amount of the second anoxic tank 60 is performed by measuring and confirming the amount of change of the present nitrate nitrogen, adjusting the proportional control element value according to the rate of change with respect to the change amount of the nitrate nitrogen amount And controls the optimum internal conveyance amount conveyed from the second anoxic tank (60) to the first anoxic tank (30) (see Fig. 5).

The external carbon source injection amount control is performed by measuring the amount of nitrate nitrogen in the second anoxic tank (60) by measuring the nitrate nitrogen amount of the second anoxic tank (60) in real time plural times, Wherein the control unit controls the optimal amount of the external carbon source injected to the second anoxic tank (60) according to the rate of change, and injects the external carbon source into the second anoxic tank (60) according to the set amount of injection when the current nitrate nitrogen is higher than the set nitrate nitrogen And the injection of the external carbon source is stopped by the injection stopping tank to be described later (see FIG. 5).

The step of controlling the amount of internal transfer of the second anoxic tank (60) comprises: determining an arithmetic average value of the nitrate nitrogen amount measured plural times in the second anoxic tank (60) as the current nitrate nitrogen, The amount of internal transfer of the second anoxic tank (60) is controlled through PID control so that the nitrate nitrogen of the second anoxic tank (60) corresponds to the set nitrate nitrogen as compared with the target set nitrate nitrogen.

The step of controlling the amount of internal transfer of the second anoxic tank (60) may include the steps of: determining a change amount of the current nitrate nitrogen and adjusting a proportional control element value according to the change rate, wherein the rate of change of the nitrate nitrogen is & , It is judged that the rate of denitrification is rapid and the amount of internal transfer is increased by 18% to 22%, preferably by 20%.

The step of controlling the amount of internal transfer of the second anoxic tank (60) may include the steps of: checking a change amount of the current nitrate nitrogen and adjusting a proportional control element value according to the change rate, wherein the rate of change of the nitrate nitrogen is' 0 ', it is preferable to determine that the denitration reduction rate is gentle and increase the internal transport amount by 8% to 12%, preferably 10%. However, it is preferable that the optimum control design and the capacity of the integrated nitrogen control system Of course.

The step of controlling the internal transport amount of the second anoxic tank (60) increases the internal transport amount and returns to the initially set internal transport amount when the present nitrate nitrogen reaches the set nitrate nitrogen.

Hereinafter, an embodiment of the internal conveyance amount control method of the second anoxic tank 60 will be described with reference to FIG.

First, the NO ₃ -N of the second anoxic tank (or the discharged water tank) is measured every minute (N _PV ), and the measured value of NO ₃ -N is calculated as shown in Equation 4 for the error and noise removal of the meter three times the average will be recognized as a current NO ₃ -N an arithmetic mean of NO ₃ -N.

Equation 4

^{_{NO 3 -N n '= (NO}} 3 -N n -2 + NO 3 -N n -1 + NO 3 -N n) / 3, ex) NO 3 -N 3' = (NO 3 -N 1 + NO ₃ -N ₂ + NO ₃ -N ₃ ) / 3,

In this case, since the NO ₃ -N instrument is installed at the end of the second anoxic tank 60 (before the separation membrane tank 70), the nitrification and denitrification are completed. Therefore, even if the instrument is installed in the discharge water tank, NO ₃ -N Because there is no interference by MLSS when installing the instrument, it is possible to obtain a more accurate measurement value.

Then, the change amount of NO ₃ -N is checked, the proportional control element value K _p is adjusted according to the change rate (see Equations 5 and 6), and the target setting NO ₃ -N (N _Set ) And compares it with current NO ₃ -N.

Equation 5

NO ₃ -N _n ^' = NO ₃ -N ^' _n -NO ₃ -N ^' _{n -1} , ex) NO ₃ -N ₅ ^' = NO ₃ -N ₅ ^' - NO ₃ -N ₄ ^'

Equation 6

NO ₃ -N _n ^" = NO ₃ -N _n ^' - NO ₃ -N _n-1 ^' _, ex) &Quot; NO ₃ -N ₅ ^" = ^" NO ₃ -N ₅ ^' - NO ₃ -N ₄ ^'

After the comparison, if NO ₃ -N is larger than N _Set , the amount of conveyance is increased by controlling the internal conveying pump rotation speed, and the amount of internal conveyance is adjusted within the range of 100 to 300%. If ΔNO ₃ -N _n ^'' > 0, it is determined that the rate of denitrification is abrupt, the internal transport amount is increased by 20%, and if ΔNO ₃ -N _n ^'' ≤0, Increase the amount by 10%. It goes without saying that the amount of internal transportation of the second anoxic tank 60 may vary depending on the optimum control design and the capacity of the integrated nitrogen control system.

At this time, when the NO ₃ -N reaches N _Set at the present time while increasing the inner carry amount, it returns to the initially set inner carry amount.

The step of controlling the amount of the external carbon source injects the external carbon source into the second anoxic tank 60 according to the set amount of injection when the present nitrate nitrogen is higher than the set nitrate nitrogen.

More specifically, in the step of controlling the external carbon source injection amount, when the value (mg / L) obtained by subtracting the set nitrate nitrogen from the present nitrate nitrogen exceeds 5, the external carbon source is continuously injected.

On the other hand, when the value (mg / L) obtained by subtracting the set nitrate nitrogen from the present nitrate nitrogen is equal to or less than 5, the external carbon source is intermittently injected, and the intermittent cycle is subtracted from the value (mg / L) The smaller the number, the longer the intermittent cycle.

Next, the control of the external carbon source injection amount will be described.

The step of controlling the amount of external carbon source injection stops the external carbon source injection according to the injection stop condition. The injection stop condition is a condition in which the measurement value of the nitrate nitrogen of the second anoxic tank 60 is measured to be equal to or lower than the set nitrate nitrogen and the condition that the pH of the second anoxic tank 60 is changed, (nitrate apex) or a change in the oxidation-reduction potential (ORP) to detect a nitrate knee, and a case where there is no time variation of the nitrate nitrogen of the second anoxic tank 60 .

On the other hand, the external carbon source is intended to induce denitrification of the remaining nitrogen oxides using an external carbon source after internal transportation. On the other hand, the consumption amount of methanol (CH ₃ OH) generally used when an external carbon source is injected for removing nitrate nitrogen after the maximum internal feed rate of 300% is calculated is shown in Equation (7).

Equation 7

= 3.68 g/gMethanol requirement =

= 3.68 g / g

= 0.156gVSS/gbCODYn =

= 0.156 g VSS / gbCOD

Here, Yn, Y, Kd, SRT and VSS are respectively the net microorganism synthesis coefficient, the microorganism synthesis coefficient, the endogenous respiration coefficient, the sludge residence time, and the volatile suspended material.

The injection of the external carbon source is performed when the target setting NO ₃ -N (N _Set ) is set to 5 mg / L and the present NO ₃ -N _n ^' is higher than the set value (N _Set ) The operation time of the injection pump is assumed.

Here, if NO ₃ -N _n ^' -N _Set > 5, the chemical injection pump is continuously injected, and 3 <NO ₃ -N _n ^' -N _Set &Lt; 5, the chemical injection pump is stopped for 5 minutes / 1 minute, and NO ₃ -N _n ^' -N _Set &Lt; 3, the chemical injection pump is operated with a 5 minute injection / 5 minute stop.

On the other hand, when the external carbon source is injected at a rate equal to or greater than the denitration amount, it is possible to cause an increase in the residual COD of the effluent and unnecessary consumption of the chemicals occurs. When the measured value of the second anoxic tank NO ₃ -N is measured to be equal to or lower than the set value (N _Set ) or when the nitrate apex is detected by sensing the change of the second anoxic tank pH, (Nitrate knee) is detected by detecting a change in the oxidation-reduction potential of the second anoxic tank NO ₃ -N, or there is no time variation of the second anoxic tank NO ₃ -N.

Here, nitrate knee is an ORP bending point when denitrification is complete and no more nitrate or nitrite is present. This is caused by sulfate-reduction dp that produces sulfide, while sulfide is 0.07 mg sulfide / L increases the ORP of 100mV. When the denitrification progresses under anaerobic conditions, the ORP increases. However, since the denitrification point is seen as ΔNO ₃ -N _n ^'' ≥ 0 at the increasing trend, it can be regarded as the time when the denitrification is completed.

In the anoxic condition, the pH is decreased by the carbon dioxide formation in the early stage, but the pH decrease is canceled as the OH ^- ion is generated by the denitrification. However, at the end of the denitrification, the pH begins to decrease, leading to a pH peak point called the nitrate apex. At this time, since the denitrification by the external carbon source is considered to be completed, the external carbon source injection is stopped.

Hereinafter, an embodiment of a transport system including the second transport section 62 and the third transport section 72 but not including the first transport section 52 will be described.

The third conveying unit 72 is for conveying the high MLSS and dissolved oxygen of the separation membrane bath 70 to the oxic tank 50 and the second conveying unit 62 is for performing denitrification in the second anoxic tank 60 And to reduce the dissolved oxygen concentration for complete denitrification in the first anoxic tank (30).

Thus, the second transporting section 62 and the third transporting section 72 are formed in the two-stage denitrification process (first anoxic-anaerobic-aerobic-second anoxic-membrane separation tank 70) And 1.5Q to 2.5Q from the separation membrane bath 70 to the oxic tank 50 and from the second anoxic tank 60 to the first anoxic tank 30 to form the 2 to 3Q transportation process .

The third conveying part 72 is provided with a high MLSS (about 9,000 mg / L to 11,000 mg / L) and a high dissolved oxygen concentration (about 4 mg / L or more) of the separation membrane bath 70 in the oxic tank 50 in the range of 1.5 to 2.5 Q carrier, the pollutant can be removed even with a small HRT in the aerobic tank 50 (high MLSS maintenance), and the advantage of saving the amount of blowing of the oxic tank 50 due to the high dissolved oxygen concentration of the separation membrane bath 70 have.

The second transporting unit 62 firstly denitrifies nitrified oxides in the oxic tank 50 in the second anoxic tank 60 and finally transports the nitrified oxide in the second anoxic tank 30 for 2 to 3Q to induce complete denitrification. do. At this time, together with the MLSS transport of the second anoxic tank (60), the dissolved oxygen concentration is almost zero, and the denitrification efficiency can be expected to be much higher than that carried out directly in the oxic tank (50). In addition, the near-zero dissolved oxygen concentration and complete denitrification contribute to the increase in the efficiency of the inhalation of the anaerobic tank (40).

When the internal return rate is increased to increase the nitrogen removal efficiency, the denitrification in the anoxic tank is not performed properly due to the high dissolved oxygen concentration of the oxic tank 50, and the denitrification of the nitric oxide is carried out in the anaerobic tank 40), the denitrification occurs in the anaerobic tank 40 (denitrifying microorganism dominant, anaerobic microbial erosion). On the other hand, the first transport section 62 maintains a high feed rate and increases the nitrogen removal efficiency. At the same time, the nitrate and dissolved oxygen concentrations, which are the inhibiting elements of the in-outflow, are maintained close to zero in the anaerobic tank 40, .

FIG. 6 is a flow chart showing the flow of denitrification control in the integrated nitrogen control system operation method of the bottom water treatment plant according to another embodiment of the present invention using the integrated nitrogen control system of the wastewater treatment facility shown in FIG. 6, the driving system control method of the integrated nitrogen wastewater treatment plants, TN and the target value setting step (S10), NH ₄ -N and NO ₃ -N target value and target value setting step (S20), NH ₄ and -N measurement step (S30), NH ₄ -N and NH ₄ -N measurement value and comparing (S40) for comparing the target value, and the blowing air volume holding step (S50), and the first transfer step (S60), NO ₃ -N target value changing step S70, a blowing amount increasing step S80, a second conveying step S90, a NO ₃ -N measuring step S100, an inner conveying amount and an outer carbon source injection amount adjusting step S110).

In TN target value setting step (S10) ammonium nitrogen (NH ₄ -N) and the total sum of the nitrate nitrogen (NO ₃ -N): the target value of (Total Nitrogen TN) are set.

In the NH ₄ -N target value and NO ₃ -N target value setting step S20, the target value of ammonia nitrogen (NH ₄ -N) and the target value of nitrate nitrogen (NO ₃ -N) are respectively set. The target value of the ammonia nitrogen (NH ₄ -N) and the target value of the nitrate nitrogen (NO ₃ -N) in the NH ₄ -N target value and the NO ₃ -N target value setting step S20 are set in the TN target value setting step (S10), the target value of total nitrogen is set automatically. Since the ammonia nitrogen is changed into nitrate nitrogen, the ammonia nitrogen can be sufficiently removed to control the generated nitrate nitrogen to an external carbon source, and thus the final total nitrogen concentration can be controlled. Therefore, the target value of ammonia nitrogen It is set lower than the acid nitrogen target value. In the present embodiment, the target value of ammonia nitrogen is automatically set to 20% of TN target value, and the target value of nitrate nitrogen is automatically set to 60% of TN target value. However, the present invention is not limited to this no.

In the NH ₄ -N measurement step S30, the amount of ammonia nitrogen (NH ₄ -N) in the oxic tank 50 is measured in real time. This will be described in detail as follows. Ammonium nitrogen in the aerobic tank (50) (NH ₄ -N) is currently ammonium nitrogen arithmetic mean value of three times ammonium nitrogen (NH ₄ -N) for the measurement, at which time error and noise removal of the instrument per 1 minute ( NH ₄ -N), and the measured value of ammonia nitrogen (NH ₄ -N) is averaged three times immediately before as ammonia nitrogen (NH ₄ -N) as shown in Equation (8).

Equation 7

^{_{NH 4 -N n '= (NH}} 4 -N n-2 + NH 4 -N n-1 + NH 4 -N n) / 3, ex) NH 4 -N 3' = (NH 4 -N 1 + NH ₄ -N ₂ + NH ₄ -N ₃ ) / 3,

Comparing (S40) the amount of NH ₄ NO ₃ -N -N target value and target value setting in NH ₄ -N ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 is measured in real time in the measurement step (S30) the target value of the ammonium nitrogen (NH ₄ -N) set in the step (S20) is compared. In the comparing step (S40), the measured ammonium nitrogen (NH ₄ -N) ammonium nitrogen (NH ₄ -N), if a large air volume, the target value holding step (S50) and a first conveying step of the set than the amount of ( S60) is performed and, when changing the target value of the ammonium nitrogen (NH ₄ -N) set at more than the amount of ammonium nitrogen (NH ₄ -N measurement) or equal to the target value, the NO ₃ -N step (S70) , A blowing amount increasing step (S80), and a second conveying step (S90) are performed.

In the blowing amount maintenance step (S50), the blowing amount supplied to the oxic tank (50) is kept unchanged.

In the first conveying step S60, only the first conveying section 52 out of the first conveying section 52 and the second conveying section 62 operates so that the sludge of the oxic tank 50 is conveyed to the first anoxic tank 30 do.

In the NO ₃ -N target value changing step (S 70), the target value of nitrate nitrogen (NO ₃ -N) is automatically changed. The target value of the nitrate nitrogen (NO ₃ -N) in the NO ₃ -N target value changing step (S 70) is set to the NH ₄ -N target value and the nitrate nitrogen NO set in the NO ₃ -N target value setting step S 20 ₃ -N). In this embodiment, at the target value of the nitrate nitrogen (NO ₃ -N) set in the NH ₄ -N target value and the NO ₃ -N target value setting step S 20, subtracting the measured value of NH ₄ -N measured ammonium nitrogen (NH ₄ -N) in the aerobic tank measured in the step (S30) and, NH ₄ -N target value and the NO ₃ -N in the target value setting step (S20) And the target value of the set ammonia nitrogen (NH ₄ -N) is added. Namely, the target value of the ammonia nitrogen (NH ₄ -N) set in the NH ₄ -N target value and the NO ₃ -N target value setting step S20 is A, the NH ₄ -N target value and the NO ₃ -N The target value of the nitrate nitrogen (NO ₃ -N) set in the target value setting step (S20) is referred to as B, the ammonia nitrogen (NH ₄ -N) in the oxic tank measured in the NH ₄ -N measurement step (S30) The target value of the nitrate nitrogen (NO ₃ -N) is changed to B- (CA) in the NO ₃ -N target value changing step S 70.

To increase the air volume step (S80) blowing air volume supplied to the aerobic tank 50 is increased based on the change of the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50, specifically to them as follows. The amount of control of the air volume in the air volume increasing step (S80) is aerobic tank 50 of the ammonium nitrogen (NH ₄ -N) in ammonium nitrogen (NH ₄ -N) aerobic tank 50, a plurality of times in real-time by measuring the amount of And controls the blowing amount of the oxic tank 50 in accordance with the rate of change with respect to the amount of change in the amount of ammonia nitrogen (NH ₄ -N).

In other words, the air volume control in the aerobic tank 50 in the air volume increasing step (S80), the ammonium nitrogen in the aerobic tank 50 (NH ₄ -N), a plurality of times to measure in real time a plurality of times measured ammonium nitrogen (NH ₄ after the defined as the arithmetic average value of dissolved oxygen -N), through the PID control so that the target value of the ammonium nitrogen (NH ₄ -N) is set, the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 Control the blowing amount.

Blowing air volume increasing step (S80) is to determine the amount of change of the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 is controlled in accordance with the rate of change in proportion to the amount of change of the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 but by adjusting the component values control the blowing air volume of the aerobic tank 50, the ammonium nitrogen (NH ₄ -N) is greater ammonium nitrogen (NH ₄ -N) than the zero rate of change of the amount of change is found to suddenly increase And raises the proportional control element value by 18% to 22%, preferably 20%.

In addition, the blowing air volume increasing step (S80) is to determine the amount of change of the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 depending on the rate of change of the amount of change of the ammonium nitrogen (NH ₄ -N) in the aerobic tank 50 proportional control, but adjusts the component values, the ammonium nitrogen (NH ₄ -N) equal to the rate of change of the amount of change less than or equal to zero ammonium nitrogen (NH ₄ -N) and is determined to gradually increase the proportion of control It is desirable to raise the element value by 8% to 12%, preferably by 10%, which is variable.

As described above, the blowing rate control of the oxic tank 50 can minimize the energy consumption by adjusting the aeration amount according to the situation as described above, and can be controlled based on the rate of change of the amount of change in ammonia nitrogen (NH ₄ -N) , It is possible to shorten the trouble period and secure stable water quality through normalization of ammonia nitrogen (NH ₄ -N).

At this time, PID control is performed by comparing the target values of ammonia nitrogen (NH ₄ -N) and ammonia nitrogen (NH ₄ -N). At this time, the change amount of dissolved oxygen is checked as shown in Equation (8) The proportional control element value (K _p ) is adjusted according to the rate of change with respect to the reference value.

Equation 8

NH ₄ -N _n ^' = NH ₄ -N ^' _n -NH ₄ -N ^' _n-1 , ex) ? NH ₄ -N ₅ ^' = ^{_{NH 4 -N 5 '- NH 4}} -N 4'

Equation 9

? H ₄ -N _n ^'' = ? H ₄ -N _n ^' _- ? H ₄ -N _n-1 ^' _, ex) △ DO ₅ ^'' = ? H ₄ -N ₅ ^' _- ? H ₄ -N ₄ ^'

For example, ΔH ₄ -N _n ^" (the rate of change of the amount of nitrogen in ammonia) > 0, it is judged that the ammonia nitrogen is abruptly increased and the proportional control element value (K _p ) is improved by 20%. If ΔH ₄ -N _n ^'' ≤ 0, it is judged that the ammonia nitrogen is gently increased, Increase the control element value (K _p ) by 10%.

In the second conveying step S90, only the second conveying part 62 of the first conveying part 52 and the second conveying part 62 operates to convey the sludge of the second anoxic tank 60 to the first anoxic tank 30 Lt; / RTI &gt;

In the NO ₃ -N measurement step S100, the amount of nitrate nitrogen (NO ₃ -N) in the second anoxic tank 60 is measured in real time. Since this is the same as the description of Equation 4 and FIG. 5, detailed description thereof will be omitted.

In the inner transfer amount and the outer carbon source injection amount adjustment step S110, the inner transfer amount in the first transfer step S60, the inner transfer amount in the second transfer step S90, and the outer carbon source to the second anoxic tank 60 The dosage is adjusted.

First, the control of the amount of sludge in the aerobic tank 50 to be transported to the first anoxic tank 30 in the first transportation step (S60) will be described as follows.

A first internal conveyance amount of the conveyance control step (S60) is, H ₄ -N measurement step (S30) the ammonium nitrogen (H ₄ -N) and set ammonium nitrogen (H ₄ -N) measured in real time And controls the internal conveyance amount through PID control so that the ammonia nitrogen (H ₄ -N) of the oxic tank 50 corresponds to the target value. That is, the optimal control of the internal transport amount of the oxic tank 50 is performed by measuring and confirming the change amount of the present ammonia nitrogen amount, adjusting the proportional control element value according to the rate of change with respect to the change amount of the ammonia nitrogen amount, 50) to the first anoxic tank (30).

In the step of controlling the amount of internal transfer of the oxic tank 50, the amount of change of the ammonia nitrogen is checked and the value of the proportional control element is adjusted according to the rate of change. If the rate of change of the amount of ammonia nitrogen is larger than 0, Is determined to increase sharply, and the internal conveyance amount is increased by 18% to 22%, preferably by 20%.

The step of controlling the amount of internal transfer of the oxic tank 50 may be performed by checking the change amount of the present ammonia nitrogen (see Equation 8), adjusting the proportional control element value according to the change rate, 9) is less than or equal to '0', it is determined that the ammonia nitrogen is gradually increased, and it is preferable to increase the internal transportation amount by 8% to 12%, preferably by 10% Of course, can be varied depending on the optimum control design and the capacity of the integrated nitrogen control system.

The step of controlling the internal conveying amount of the oxic tank (50) increases the internal conveying amount and returns to the initially set internal conveying amount when the current ammonia nitrogen reaches the target value.

The adjustment of the internal conveyance amount in the second conveying step S90 and the adjustment of the external carbon source injection amount to the second anoxic tank 60 are the same as those described above with reference to FIG. 5, so a detailed description thereof will be omitted.

While the present invention has been described with reference to exemplary embodiments, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, but, on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims. Accordingly, the true scope of the present invention should be determined by the technical idea of the appended claims.

10: Screen unit 20: Flow regulator
30: First anoxic tank 40: Anaerobic tank
50: aerobic tank 51:
52: first transport section 60: second anoxic tank
62 ... second transport section 64: external carbon source supply section
70: Membrane tank 72: Second transfer section
80: Integrated nitrogen control unit

Claims (6)

A first anoxic tank in which a waste water and a wastewater are introduced and a denitrification reaction proceeds in an anaerobic atmosphere; and a second anoxic tank disposed behind the first anoxic tank and having been treated in the first anoxic tank, Wherein the anaerobic tank is disposed downstream of the anaerobic tank and the treated water treated in the anaerobic tank is introduced into the anaerobic tank and the nitrification reaction of the treated water proceeds in an exhalation atmosphere; An aeration unit including a second anoxic tank into which treated water flows and an denitrification reaction of the treated water proceeds in an anoxic atmosphere, and an aerator for aeration to supply oxygen by the aerobic tank; and a sludge tank And a second anoxic tank for supplying the sludge to the first anoxic tank, An outer carbon source supply unit for injecting an outer carbon source into the second anoxic tank; and a second carbon monoxide tank connected to the aeration unit, the first transport unit, the second transport unit, and the outer carbon source supply unit, And an amount of ammonia nitrogen and an amount of nitrate nitrogen of the second anoxic tank are measured to determine a blowing amount of the blower corresponding to the amount of dissolved oxygen, the amount of ammonia nitrogen, and the amount of nitrate nitrogen, A method for operating an integrated nitrogen control system of a wastewater treatment plant, comprising an integrated nitrogen control unit for controlling the internal transfer of the components,
A TN target value setting step (S10) in which a target value of total nitrogen which is a sum of the ammonia nitrogen and the nitrate nitrogen is set;
Setting a NH ₄ -N target value and a NO ₃ -N target value (S20) in which a target value of the ammonia nitrogen and a target value of the nitrate nitrogen are respectively set;
An NH ₄ -N measurement step (S 30) in which the ammonia nitrogen amount is measured in real time in the oxic tank;
Comparison step in which the NH ₄ a measurement in real time, the ammonia in the measurement step -N sex nitrogen content and the NH ₄ NO ₃ -N target value and the target value of the ammonium nitrogen in the comparison set -N target value setting step (S40);
The internal conveyance by the first conveyance unit is performed and the internal conveyance by the second conveyance unit is performed when the measured value of the ammonia nitrogen amount is found to be smaller than the set value of the set ammonia nitrogen in the comparison step (S60);
Wherein when the ammonia nitrogen measurement value is found to be equal to or greater than a target value of the set ammonia nitrogen in the comparison step, the internal conveyance by the second conveyance unit is carried out and the internal conveyance by the first conveyance unit (S90);
A NO ₃ -N target value changing step of changing the target value of the nitrate nitrogen to a lower value when it is confirmed in the comparing step that the measured ammonia nitrogen amount is equal to or greater than the set target ammonia nitrogen value (S70);
A NO ₃ -N measuring step (S 100) in which the nitrate nitrogen amount is measured in real time in the second anoxic oxygen; And
The internal transport amount in the second transport step and the external carbon source injection amount to the second anoxic tank by the external carbon source supply unit are controlled in accordance with the rate of change with respect to the change amount of the nitrate nitrogen amount measured from the NO ₃ -N measurement step (S110)
In the setting of the NH ₄ -N target value and the NO ₃ -N target value, the target value of the ammonia nitrogen is set to be lower than the nitrate nitrogen target value,
In the NO ₃ -N target value changing step S 70, the target value of the nitrate nitrogen is set to the nitrate nitrogen (NO ₃ - N target value) set in the NH ₄ -N target value and the NO ₃ -N target value setting step (S 20) in the target value of N), the NH ₄ -N subtracting the measured value of the ammonium nitrogen (NH ₄ -N) in the said aerobic tank measured by the measurement step (S30), and the NH ₄ NO ₃ -N target value, and changed to -N target value setting step (S20) is set ammonium nitrogen obtained by adding a target value of (NH ₄ -N) in value, and,
The internal transport amount is increased by 18% to 22% when the change rate of the change amount of the nitrate nitrogen measurement value is greater than 0 in the step of adjusting the internal transport amount in the second transport step, When the change rate of the change amount is less than or equal to '0', the internal carry amount is increased by 8% to 12%, and when the measured value of nitrate nitrogen reaches the target value when the internal carry amount is increased,
In the step of controlling the external carbon source injection amount, when the value (mg / L) obtained by subtracting the target value of the nitrate nitrogen from the measured nitrate nitrogen is greater than 5, the external carbon source is continuously injected, Wherein the external carbon source is injected intermittently when the value (mg / L) obtained by subtracting the target value of the nitrate nitrogen from the measurement value of the acid nitrogen is 5 or less, and the measurement value of the nitrate nitrogen is set to a target value The method of operating an integrated nitrogen control system of a wastewater treatment plant wherein external carbon source injection is interrupted. The method according to claim 1,
The NH ₄ -N said ammonia measured by the measuring step in response to the property change rate with respect to variation of the nitrogen content of the first conveying step of wastewater treatment equipment, which further comprises the step (S110) is adjusted the amount of internal recycle of nitrogen from the integrated control system Operating method. delete The method according to claim 1,
(S50) in which the amount of air supplied to the oxic tank is kept unchanged when it is determined that the measured value of the ammonia nitrogen amount is smaller than the target value of the set ammonia nitrogen in the comparing step A method of operating an integrated nitrogen control system of a treatment facility. The method according to claim 1,
(S80) in which the amount of ammonia nitrogen to be supplied to the oxic tank is increased when it is determined that the measured ammonia nitrogen amount is equal to or greater than a target value of the set ammonia nitrogen in the comparison step A method of operating an integrated nitrogen control system of a plant. The method of claim 5,
Wherein the blowing amount in the step of increasing the blowing amount is adjusted in accordance with a rate of change with respect to a change amount of the ammonia nitrogen amount measured from the NH ₄ -N measurement step.

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