CN112723542B - Enhanced denitrification system and method suitable for high sludge concentration - Google Patents
Enhanced denitrification system and method suitable for high sludge concentration Download PDFInfo
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- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
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- C02F3/30—Aerobic and anaerobic processes
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- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
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Abstract
The invention discloses a system and a method for enhanced denitrification suitable for high sludge concentration, belonging to the technical field of sewage treatment, wherein an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane pool zone are communicated in sequence; dissolved oxygen concentrations of the aerobic zone I, the micro-anoxic zone and the aerobic zone II are respectively controlled by a DO automatic control method; the sludge concentration of an aerobic zone I, a micro-anoxic zone and an aerobic zone II is detected in real time to control the discharge amount of the residual sludge in the membrane pool zone; adjusting the carbon source adding amount and the reflux ratio of the secondary reflux and the tertiary reflux by detecting orp values of the anaerobic zone, the anoxic zone and the micro-anoxic zone in real time; PID control operation is carried out through the total phosphorus target value and the total phosphorus actual value of the water outlet point, so that PAC feeding is dynamically controlled, and the aim of meeting the denitrification requirement that the total nitrogen of the outlet water is less than 10mg/L can be fulfilled by aiming at an AAO/AO + MBR system which has low water inlet load, unbalanced carbon-nitrogen ratio and small floor area.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a reinforced denitrification system and method suitable for high sludge concentration.
Background
The inlet water quality and the water temperature of the current urban sewage treatment plant have large variation range, and the problem of variation of the concentration of Total Nitrogen (TN) and chemical oxygen demand (CODcr) of the inlet water is particularly obvious under the influence of factors such as seasons, resident life styles and the like. When Total Nitrogen (TN) of inlet water is higher, carbon-nitrogen ratio (C/N) is low, and total nitrogen effluent standard is improved, the traditional anaerobic/anoxic/aerobic (AAO) process is difficult to meet denitrification requirement, and has higher consumption of carbon source.
In the face of the change of the concentration of the inlet water quality and the change of the water temperature, the combination of the biochemical tanks in a fixed mode is difficult to meet, if the aerobic part of the tank bodies in the biochemical tanks can be switched between an anoxic state and an aerobic state and is matched with a return system in mixed liquid, the problem that the outlet water standard cannot be guaranteed due to the high concentration of Total Nitrogen (TN) of the inlet water and the fluctuation of the inlet water quality and the water temperature can be solved.
Disclosure of Invention
In view of the above, in order to solve the above problems in the prior art, the present invention aims to provide an enhanced denitrification system and method suitable for high sludge concentration, so as to achieve the purpose of meeting the denitrification requirement that the total nitrogen of the effluent is less than 10mg/L for an AAO/AO + MBR system with low intake load, unbalanced carbon-nitrogen ratio and small floor area.
The technical scheme adopted by the invention is as follows: an enhanced nitrogen removal system suitable for high sludge concentration, comprising:
the anaerobic zone and the anoxic zone are respectively provided with a water inlet point;
the water inlet of the water inlet point is treated by an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane pool zone which are communicated in sequence, and then the water is denitrified and discharged;
wherein the membrane pool area returns the sludge to the aerobic area I through primary return; the micro anoxic zone reflows nitrified liquid to the anoxic zone through secondary reflux; and the anoxic zone returns anoxic liquid to the anaerobic zone through three-stage reflux.
The invention also provides an enhanced denitrification method suitable for high sludge concentration, which comprises the following steps:
sequentially communicating an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane pool zone, wherein the anaerobic zone and the anoxic zone are respectively used as water inlet points, and the membrane pool zone is used as a water outlet point and a discharge point of excess sludge;
dissolved oxygen concentrations of an aerobic zone I, a micro-anoxic zone and an aerobic zone II are respectively controlled by a DO automatic control method;
the sludge concentration of an aerobic zone I, a micro-anoxic zone and an aerobic zone II is detected in real time to control the discharge amount of the residual sludge in the membrane pool zone;
the membrane pool zone returns sludge to the aerobic zone I through primary reflux, the micro-anoxic zone returns nitrifying liquid to the anoxic zone through secondary reflux, and the anoxic zone returns anoxic liquid to the anaerobic zone through tertiary reflux;
the carbon source adding amount and the reflux ratio of the secondary reflux to the tertiary reflux are adjusted by detecting the orp values of the anaerobic zone, the anoxic zone and the micro anoxic zone in real time.
Further, the enhanced nitrogen removal method also comprises the following steps:
PID control operation is carried out through the total phosphorus target value and the total phosphorus actual value of the water outlet point so as to carry out dynamic control on PAC adding, and the power consumption and the PAC medicine consumption of the adding pump are saved through reasonably controlling the adding amount of PAC.
Further, the PAC adding control method comprises the following steps:
s101: setting a total phosphorus target value of a water outlet point and acquiring a total phosphorus actual value of the water outlet point;
s102: performing PID control operation according to the total phosphorus target value and the total phosphorus actual value;
s103: according to PID control operation, PAC adding concentration is obtained, and the PAC adding dosage needing to be added is calculated, wherein the calculation formula is as follows:
s104: performing PI control operation according to the calculated PAC dosage;
s105: dynamically controlling a feeding pump corresponding to PAC feeding according to PI control operation;
in the above, the PAC adding dosage is determined according to the calculation method of the PAC adding concentration, so that the dynamic adding of the PAC adding dosage in combination with the liquid amount is realized, and the automatic control of the PAC adding is completed.
Further, the method of the DO automatic control method includes:
s201: setting a dissolved oxygen target value of a zone to be controlled, and acquiring a dissolved oxygen actual value of the zone to be controlled;
s202: performing PID control operation according to the dissolved oxygen target value and the dissolved oxygen actual value;
s203: performing fan guide vane control or fan frequency control on the fan through PID control operation;
s204: revising and correcting the operation control of the fan according to the correction compensation to obtain the air supply amount of the fan corresponding to the area to be controlled;
wherein the zones to be controlled are an aerobic zone I, a micro-anoxic zone and an aerobic zone II; so as to realize the automatic control of the reasonable air supply quantity of the aerobic zone I, the micro-anoxic zone and the aerobic zone II.
Further, the method of the DO automatic control method further comprises:
s205: each zone to be controlled is correspondingly provided with a valve for controlling the aeration quantity;
s206: respectively obtaining a dissolved oxygen target value and a dissolved oxygen actual value of each zone to be controlled, and carrying out PI control operation;
s207: adjusting the opening of each valve according to the result of PI control operation;
the automatic control of dissolved oxygen in an aerobic zone of a biochemical pool is completed through the combined action of a fan and a valve, and the problem of limitation of a butterfly valve, a plunger valve and the like on nonlinear control of air volume regulation is solved.
Further, DO online instruments are installed at the tail ends of the aerobic zone I, the micro-anoxic zone and the aerobic zone II, and the dissolved oxygen actual values of the aerobic zone I, the micro-anoxic zone and the aerobic zone II are respectively obtained through the DO online instruments;
the dissolved oxygen target value of the aerobic zone I is set to be between 1 and 2mg/l, the dissolved oxygen target value of the aerobic zone II is set to be between 2 and 3mg/l, and the dissolved oxygen target value of the micro anoxic zone is set to be between 0.3 and 0.6 mg/l;
because the DO of the aerobic zone I, the micro anoxic zone and the aerobic zone II is controlled in a reasonable range, the anoxic retention time can be increased to promote the denitrification effect, and meanwhile, the low dissolved oxygen nitrification liquid in the micro anoxic zone flows back to the front-section anoxic zone to provide more favorable denitrification conditions for denitrification.
Further, detecting the sludge concentration of an aerobic zone I, a micro-anoxic zone and an aerobic zone II respectively in real time through an online mlss detector;
when the sludge concentration is higher than a target value, increasing the discharge of the excess sludge; when the sludge concentration is lower than the target value, reducing the discharge of the excess sludge;
the sludge concentration of the aerobic zone I, the micro-anoxic zone and the aerobic zone II is adjusted and controlled by discharging the excess sludge.
Furthermore, the sludge concentration of the aerobic zone I and the micro anoxic zone is controlled to be 10000-12000 mg/l, and the sludge concentration of the aerobic zone II is controlled to be 12000-15000 mg/l, so that the high sludge concentration of the system is maintained, the high sludge load is kept with higher sludge activity, the sludge discharge of the system is reduced, the growth rate and the generation time of the system are increased, the sludge concentration is as high as possible, the growth is as slow as possible, and the system is more favorable for denitrification.
Further, an online orp detector is used for detecting orp values of the anaerobic zone, the anoxic zone and the micro-anoxic zone in real time respectively;
if the value of the anaerobic zone orp is larger than the target value, reducing the reflux ratio of the three-stage reflux; if the value of the anaerobic zone orp is less than the target value, the reflux ratio of the three-stage reflux is increased;
if the orp values of the anoxic zone and the micro-anoxic zone are both larger than the target value, reducing the reflux ratio of the secondary reflux or increasing the carbon source adding amount of a water inlet point; otherwise, increasing the reflux ratio of the secondary reflux or reducing the carbon source adding amount of a water inlet point;
the method realizes the accurate control of the ORP value on the anaerobic zone, the anoxic zone and the micro-anoxic zone, and the ORP value is used as a real-time control parameter to adjust the reflux ratio of the system and the carbon source adding amount, thereby not only strengthening the biological denitrification, but also effectively controlling the carbon source adding amount.
Furthermore, the oxidation-reduction potential of the anaerobic zone is between-400 mv and-200 mv, the oxidation-reduction potential of the anoxic zone I is between-200 mv and-100 mv, and the oxidation-reduction potential of the anoxic zone II is between-150 mv and-80 mv, so that the reflux ratio of the system and the carbon source adding amount can be adjusted to a reasonable range.
The invention has the beneficial effects that:
1. by adopting the enhanced nitrogen removal system suitable for high sludge concentration provided by the invention, the micro anoxic zone and the aerobic zone II are arranged in the process flow, nitrification and denitrification reactions can synchronously occur in the micro anoxic zone, the nitrified liquid flows back to the anoxic zone, the adverse effect on denitrification of the front-section anoxic zone is extremely small, and the enhanced nitrification reaction is performed in the aerobic zone II, so that the nitrogen removal capability of the system can be enhanced while effluent ammonia nitrogen is up to the standard under the condition of limited hydraulic retention time.
2. The enhanced denitrification method suitable for high sludge concentration provided by the invention adopts an automatic control program, can automatically control DO of an oxygen I area, a micro anoxic area and an aerobic II area within a reasonable range, maintains the high sludge concentration of the system by automatically controlling the sludge concentration of the aerobic I area, the micro anoxic area and the aerobic II area, keeps higher sludge activity due to high sludge load, reduces sludge discharge amount, growth rate and generation time of the system, ensures that the sludge concentration is as high as possible and grows as slow as possible, improves denitrification capability, and simultaneously accurately controls the anaerobic area, the anoxic area and the micro anoxic area by using ORP value to adjust reflux ratio and carbon source addition amount in each level of the system, not only enhances biological denitrification, but also effectively controls carbon source addition amount.
Drawings
FIG. 1 is a process flow diagram of an enhanced denitrification system suitable for high sludge concentration provided by the present invention;
FIG. 2 is a logic diagram of the control of the feed water flow compensation in the enhanced denitrification process for high sludge concentration according to the present invention;
FIG. 3 is a logic diagram of the control of the ammonia nitrogen overrun compensation in the enhanced denitrification process for high sludge concentration according to the present invention;
FIG. 4 is a control logic diagram of DO overrun compensation in the enhanced denitrification process for high sludge concentration provided by the present invention;
FIG. 5 is a control logic diagram of pipe pressure override compensation in the enhanced denitrification process for high sludge concentration provided by the present invention;
FIG. 6 is a control logic diagram of the fan current compensation in the enhanced denitrification process for high sludge concentration according to the present invention.
Detailed Description
Reference will now be made in detail to embodiments of the present application, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar modules or modules having the same or similar functionality throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present application and are not to be construed as limiting the present application. On the contrary, the embodiments of the application include all changes, modifications and equivalents coming within the spirit and terms of the claims appended hereto.
Explanation of technical terms
And (3) PID control algorithm: the control deviation is formed according to the given value and the actual output value, the deviation is combined in proportion, integral and differential through linearity to form the control quantity, the controlled object is controlled, the formula is as follows:
and PI control algorithm: the control deviation is formed according to the given value and the actual output value, the proportion and the integral of the deviation are linearly combined to form a control quantity, and a controlled object is controlled, wherein the formula is as follows:
in the above formula, e (t) is a deviation signal of the control system, also referred to as an input signal of the controller, and a given target value r (t) is deviated from an actual output value c (t): e (t) = r (t) -c (t);
kp is a proportional coefficient which reflects the deviation signal e (t) of the control system in proportion;
u (t) is an output signal of the PID controller; p is a proportional operator; ti is an integral coefficient; td is a differential coefficient; kd is the differential gain of the differential coefficient.
Example 1
Specifically, the present embodiment provides an enhanced nitrogen removal system suitable for high sludge concentration, which includes: an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane tank zone, as shown in figure 1, the specific design is as follows:
and water inlet points are respectively arranged in the anaerobic zone and the anoxic zone so as to effectively utilize the carbon source, and the utilization rate of the denitrifying bacteria to the carbon source can be increased.
The inlet water of the water inlet point is treated by an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane pool zone which are sequentially communicated, and then is denitrified to be discharged; the membrane pool zone is used for refluxing the sludge to the aerobic zone I through primary reflux so as to realize the reflux of the high-concentration and high-DO (dissolved oxygen concentration) sludge in the membrane pool zone to the front end of the aerobic zone I, so that a certain DO (dissolved oxygen concentration) is provided for aerobic nitrification reaction, and meanwhile, compared with the traditional A2O process, the reflux point position does not influence the anaerobic phosphorus release and anoxic denitrification effect.
Will little anoxic zone through the second grade backward flow with the terminal liquid of nitrifying in little anoxic zone backward flow to the front end in anoxic zone, at this moment, the content of dissolved oxygen is not high in the liquid of nitrifying, compares the advantage that the liquid of traditional nitrification refluxes and is: does not damage the anoxic environment and is more beneficial to denitrification reaction.
And returning the anoxic liquid at the tail end of the anoxic zone to the anaerobic zone through three-stage reflux to maintain a certain sludge concentration for anaerobic phosphorus release.
As the primary reflux, the secondary reflux and the tertiary reflux are arranged in the process system, the denitrification effect can be effectively enhanced within a short hydraulic retention time.
In this embodiment, the micro-anoxic zone is understood to be a part of the anoxic zone, and the DO (dissolved oxygen concentration) in the micro-anoxic zone is controlled to be about 0.4mg/l during normal operation, so that the removal rate of total nitrogen in the biochemical system can be improved by about 18% without adding a carbon source. Meanwhile, an aerobic zone II is arranged behind the micro-anoxic zone, so that the ammonia nitrogen can reach the standard stably.
Example 2
On the basis of the enhanced nitrogen removal system provided in embodiment 1, the embodiment also provides an enhanced nitrogen removal method suitable for high sludge concentration, which aims to address an AAO/AO + MBR system with low intake load, unbalanced carbon-nitrogen ratio and small floor area, and can meet the requirement that the total nitrogen of the effluent is less than 10 mg/L. The enhanced nitrogen removal method comprises the following steps:
the anaerobic zone, the anoxic zone, the aerobic zone I, the micro-anoxic zone, the aerobic zone II and the membrane tank zone are communicated in sequence, the anaerobic zone and the anoxic zone are respectively used as water inlet points, and the membrane tank zone is used as a water outlet point and a discharge point of excess sludge. During operation, the process flow is automatically controlled and divided into the following parts (the sequence does not represent the step sequence):
(1) PAC dosing dynamics control
Carrying out PID control operation through the total phosphorus target value and the total phosphorus actual value of the water outlet point to carry out dynamic PAC (total phosphorus) adding control on PAC adding, wherein the PAC adding control method comprises the following steps:
s101: setting a total phosphorus target value of a water outlet point and acquiring a total phosphorus actual value of the water outlet point;
s102: and carrying out PID control operation according to the total phosphorus target value and the total phosphorus actual value, wherein the PID control algorithm is as follows:
and PID control operation forms control deviation according to the total phosphorus target value and the total phosphorus actual value, linearly combines the deviation according to the proportion (Kp), the integral (Ti) and the differential (Td) to form control quantity, solves the PAC adding concentration, loads a PID control algorithm into a PID controller, and performs PID operation to obtain the PAC adding concentration to be added.
S103: and (3) obtaining PAC adding concentration according to PID control operation, and calculating the PAC adding dosage needing to be added, wherein the calculation formula is as follows:
the relation conversion of PAC adding dosage, PAC adding concentration and liquid quantity is realized through the formula, so that the needed PAC adding dosage is obtained, the dependence of a PAC adding control system on historical data is solved, and the complexity of the system is reduced;
s104: performing PI control operation according to the calculated PAC adding dosage (namely the PAC adding dosage target value), wherein the PI control algorithm is as follows:
the PI control operation forms a control deviation according to a PAC dosing medicine amount target value and a PAC dosing medicine amount actual value, the proportion (Kp) and the integral (Ti) of the deviation form a control amount through linear combination, a controlled object (the control part is a dosing pump) is controlled, a PI control algorithm is loaded in a PI controller, and the operation frequency of the dosing pump is controlled through the PI controller;
s105: the operation frequency of the PAC adding pump is obtained according to PI control operation so as to dynamically control the adding pump corresponding to PAC adding, the PAC adding problem caused by the fixed frequency is solved, and dynamic control can be realized by adding through fixed flow.
S106: and (4) carrying out intermittent feeding of the feeding pump according to total phosphorus compensation operation to finally obtain proper feeding amount and feeding time.
The total phosphorus compensation operation is: when the PAC automatic adding control system is switched from manual operation to automatic operation, the program needs to carry out PAC adding stable control because the total phosphorus value may have fluctuation, so that the PAC automatic adding control can be stably transited by switching from manual operation to automatic operation, and the phenomena of frequent starting and stopping and non-ideal and sudden large total phosphorus control can not occur.
(2) DO (dissolved oxygen) control section
Dissolved oxygen concentrations of an aerobic zone I, a micro-anoxic zone and an aerobic zone II are respectively controlled by a DO automatic control method, the aerobic zone I, the micro-anoxic zone and the aerobic zone II are named as zones to be controlled, and the DO automatic control method comprises the following steps:
s201: setting a dissolved oxygen target value of a zone to be controlled, acquiring a dissolved oxygen actual value of the zone to be controlled, installing DO online instruments at the tail ends of the aerobic zone I, the micro-anoxic zone and the aerobic zone II during actual application, and respectively acquiring the dissolved oxygen actual values of the aerobic zone I, the micro-anoxic zone and the aerobic zone II through the DO online instruments.
S202: carrying out PID control operation according to the dissolved oxygen target value and the dissolved oxygen actual value, wherein the PID control operation formula is as follows:
the PID control operation constitutes a control deviation from the dissolved oxygen target value and the dissolved oxygen actual value, linearly combines the deviation in proportion (Kp), integral (Ti) and derivative (Td) to constitute a control quantity, controls a controlled object (the control unit is a fan), loads a PID control algorithm into a PID controller, and controls the operation of the fan by the PID controller.
S203: and performing guide vane control or fan frequency control on the fan according to a calculation result of PID control operation, namely generating a control instruction of the opening of the guide vane or the fan frequency of the fan by the PID controller, and performing guide vane control or fan frequency control on the fan by the control instruction.
S204: revising and correcting the operation control of the fan according to the correction compensation so as to finally obtain the air supply volume suitable for the aerobic zone of the biochemical pool, which specifically comprises the following steps: and carrying out process combination on the result of PID control operation, dividing data of different results into different levels, and carrying out control revision and deviation correction according to inflow compensation, ammonia nitrogen overrun compensation, starting and stopping fan air volume linking compensation, DO overrun compensation, pipe pressure overrun compensation and fan current compensation.
S205: each zone to be controlled is correspondingly provided with a valve for controlling the aeration quantity of the zone to be controlled, and the aeration quantity of the zone to be controlled is determined by the opening size of the valve; the air supply quantity provided by the fan is redistributed according to different air demand quantities of all zones to be controlled (namely an aerobic zone I, a micro-anoxic zone and an aerobic zone II) under the control of all valves so as to meet the air demand quantities of all the zones to be controlled;
s206: respectively obtaining the dissolved oxygen target value and the dissolved oxygen actual value of each zone to be controlled, and carrying out PI control operation, wherein the PI control algorithm is as follows:
the PI control operation constitutes a control deviation from a dissolved oxygen target value and a dissolved oxygen actual value, linearly combines a proportion (Kp) and an integral (Ti) of the deviation to constitute a control amount, controls a controlled object (the controlled part is a valve), and controls the opening degree of the valve by loading a PI control algorithm into a PI controller.
S207: adjusting the opening of each valve according to the result of PI control operation; the air demand of the area to be controlled is adapted by adjusting the valve opening, so that the linear control of the air demand in the area to be controlled is realized.
The DO (dissolved oxygen) control part completes the automatic control of the dissolved oxygen of the aerobic I area, the micro anoxic area and the aerobic II area through the combined action of the fan and the valve, finally the dissolved oxygen concentration of the aerobic I area is controlled to be between 1 and 2mg/l, the dissolved oxygen concentration of the aerobic II area is controlled to be between 2 and 3mg/l, and the dissolved oxygen concentration of the micro anoxic area is controlled to be between 0.3 and 0.6mg/l, so that the denitrification residence time can be prolonged, and the low dissolved oxygen nitrified liquid in the area flows back to the front-section anoxic area, thereby providing more favorable denitrification conditions for denitrification.
In the above, the inflow compensation, the ammonia nitrogen overrun compensation, the start-stop blower air volume engagement compensation, the DO overrun compensation, the pipe pressure overrun protection compensation and the blower current protection compensation are respectively explained as follows:
and (3) compensation of inflow flow: after the abnormal flow value is processed by the data processing system, the inflow water flow value is dynamically judged, when the inflow water flow fluctuation is obviously larger or smaller, the guide vane or the frequency of the fan is adjusted in advance to make up for the defect that the biochemical tank dissolution automatic control is not timely caused by the fluctuation of the inflow water, so that the impact of the inflow water fluctuation on the biochemical tank dissolution oxygen control is reduced, and the control effect is further influenced, as shown in fig. 2.
And (3) ammonia nitrogen overrun compensation: after the abnormal ammonia nitrogen value is processed by the data processing system, the output ammonia nitrogen is subjected to overrun judgment, and when the output ammonia nitrogen value exceeds a preset value, the air volume needs to be increased, so that the guide vane or the frequency of the fan is adjusted to supplement oxygen lacking due to insufficient ammonia nitrogen reaction in the aerobic zone, and the standard reaching requirement of the ammonia nitrogen output water is met, as shown in fig. 3.
DO overrun compensation: after the abnormal dissolved oxygen value is processed by the data processing system, the dissolved oxygen of the biochemical pool is subjected to overrun judgment, and when the dissolved oxygen of the biochemical pool exceeds a preset value, the air volume needs to be reduced, so that the guide vane or the frequency of the fan is increased; when the dissolved oxygen in the biochemical pool is lower than the preset value, the air quantity needs to be increased, so that the guide vane of the fan is reduced or the frequency is adjusted. The dissolved oxygen exceeding will cause over-aeration or insufficient aeration of the biochemical pool, and in order to make up for the untimely control and meet the requirements of dissolved oxygen control, the control adjustment of emergency is performed, as shown in fig. 4.
Pipe pressure overrun compensation: after the abnormal pressure value of the fan air supply pipe is processed through the data processing system, the pressure of the fan air supply pipe is subjected to overrun judgment, and when the pressure of the fan air supply pipe exceeds a preset value, the air quantity needs to be reduced, so that the guide vane or the frequency of the fan is adjusted. In order to ensure the stable operation of the fan, the air pipe pressure exceeds a limit value, so that potential safety hazards exist, other fans with small outlet pressure can also be caused to generate surging, the opening or frequency of guide vanes of the fan is reduced at the moment, and the safety of a fan pipeline system is ensured, as shown in fig. 5.
And (3) fan current compensation: after the abnormal fan current value is processed by the data processing system, the fan current overrun judgment is carried out, and when the fan current value exceeds a preset value, the air volume needs to be reduced, so that the guide vane or the frequency of the fan is adjusted. The stable operation of the fan cannot exceed the rated power of the fan, and in order to protect the normal use of the fan, the protection action is carried out in time when the current of the fan exceeds the limit value, as shown in fig. 6.
Starting and stopping fan air volume linking compensation: the fan is when starting or stopping appearing, and the amount of wind can change, and this kind of change can arouse the dissolved oxygen fluctuation in biochemical pond, and is unfavorable to biochemical pond dissolved oxygen automatic control, in order to solve this problem, formulates and stops fan amount of wind linking compensation, and when making the fan appear starting to stop, reduces the undulant impact to biochemical pond dissolved oxygen of amount of wind, makes the amount of wind before and after the change of fan platform number can link up.
(3) Sludge concentration control section
Respectively detecting the sludge concentration of an aerobic zone I, a micro-anoxic zone and an aerobic zone II in real time by an online mlss detector;
when the sludge concentration is higher than a target value, increasing the discharge of the excess sludge; when the sludge concentration is lower than the target value, reducing the discharge of the excess sludge; the functional relationship between the sludge concentration and the discharge of excess sludge during the adjustment is:
wherein, the concentration of the mixed liquid sludge in the biochemical pool is gMLSS/L; Δ X — total solids of sludge discharged daily in units of: gVSS/d; v-volume of the aeration reaction tank, unit is: m is a unit of 3 (ii) a θ -sludge age (mean biosolids retention time) in units of: d;
the sludge concentration of the aerobic zone I, the micro anoxic zone and the aerobic zone II is adjusted and controlled by discharging the residual sludge in the membrane tank zone. Finally, the sludge concentration of the aerobic zone I and the micro-anoxic zone is controlled between 10000 and 12000mg/l, and the sludge concentration of the aerobic zone II is controlled between 12000 and 15000 mg/l.
(4) Reflux ratio control section
The membrane pool area returns the sludge to the aerobic area I through primary reflux, the micro anoxic area returns the nitrifying liquid to the anoxic area through secondary reflux, and the anoxic area returns the anoxic liquid to the anaerobic area through tertiary reflux;
and adjusting the carbon source adding amount and the reflux ratio of the secondary reflux and the tertiary reflux by detecting the orp values of the anaerobic zone, the anoxic zone and the micro-anoxic zone in real time. The method specifically comprises the following steps:
s301: detecting orp values of an anaerobic zone, an anoxic zone and a micro-anoxic zone in real time respectively by an online orp detector;
s302: correspondingly adjusting according to the instrument display value of the online orp detector, and reducing the reflux ratio of the three-stage reflux (namely reducing the number or frequency of reflux pumps on the three-stage reflux) if the value of the anaerobic zone orp is larger than a target value; if the value of the anaerobic zone orp is less than the target value, the reflux ratio of the three-stage reflux is increased (namely, the number or the frequency of reflux pumps on the three-stage reflux is increased);
s303: if the orp values of the anoxic zone and the micro-anoxic zone are both larger than the target value, reducing the reflux ratio of the secondary reflux (namely reducing the number or frequency of reflux pumps on the secondary reflux) or increasing the carbon source adding amount of a water inlet point; otherwise, increasing the reflux ratio of the second-stage reflux (i.e. increasing the number or frequency of reflux pumps on the third-stage reflux) or reducing the carbon source dosage of the water inlet point, which is specifically divided into several cases:
a. the orp values of the anoxic zone and the micro anoxic zone are both smaller than the target value, the carbon source adding amount of a water inlet point is generally reduced;
b. and if the orp value of the anoxic zone is less than the target value and the orp value of the micro-anoxic zone is greater than the target value, synchronously increasing the reflux ratio of the secondary reflux and reducing the carbon source adding amount of a water inlet point.
Wherein the orp value is the redox potential, in the above, in an anaerobic zone: -400 to-200 mv, anoxic zone: -200 to-100 mv: micro-anoxic zone: -150 to-80 mv are target values for orp, respectively.
Be equipped with the backwash pump respectively on the route of one-level backward flow, second grade backward flow and tertiary backward flow, come control corresponding reflux ratio through the frequency or the quantity of adjusting the backwash pump, at this reflux ratio control part, the control range who finally realizes the reflux ratio does: the reflux ratio of the first-stage reflux is 300-400, the reflux ratio of the second-stage reflux is 200-400, and the reflux ratio of the third-stage reflux is 50-300.
In the enhanced nitrogen removal method of the embodiment, nutrient salts can be added in a targeted manner to culture and domesticate microbial strains with specific biochemical effects, and the microbial strains can be used for removing nitrogen and phosphorus in a biochemical system, such as microorganisms of aerobic denitrification and denitrifying phosphorus accumulating bacteria.
It should be noted that, in the description of the present application, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Further, in the description of the present application, the meaning of "a plurality" means at least two unless otherwise specified.
Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and the scope of the preferred embodiments of the present application includes other implementations in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present application.
It should be understood that portions of the present application may be implemented in hardware, software, firmware, or a combination thereof. In the above embodiments, various steps or methods may be implemented in software or firmware stored in a memory and executed by a suitable instruction execution system. For example, if implemented in hardware, as in another embodiment, any one or combination of the following techniques, which are known in the art, may be used: a discrete logic circuit having a logic gate circuit for implementing a logic function on a data signal, an application specific integrated circuit having an appropriate combinational logic gate circuit, a Programmable Gate Array (PGA), a Field Programmable Gate Array (FPGA), or the like.
It will be understood by those skilled in the art that all or part of the steps carried by the method for implementing the above embodiments may be implemented by hardware related to instructions of a program, which may be stored in a computer readable storage medium, and when the program is executed, the program includes one or a combination of the steps of the method embodiments.
In addition, functional units in the embodiments of the present application may be integrated into one processing module, or each unit may exist alone physically, or two or more units are integrated into one module. The integrated module can be realized in a hardware mode, and can also be realized in a software functional module mode. The integrated module, if implemented in the form of a software functional module and sold or used as a stand-alone product, may also be stored in a computer readable storage medium.
The storage medium mentioned above may be a read-only memory, a magnetic or optical disk, etc.
In the description herein, reference to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the application. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Although embodiments of the present application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present application, and that variations, modifications, substitutions and alterations may be made to the above embodiments by those of ordinary skill in the art within the scope of the present application.
Claims (5)
1. An enhanced nitrogen removal method suitable for high sludge concentration is characterized by comprising the following steps:
the anaerobic zone, the anoxic zone, the aerobic zone I, the micro-anoxic zone, the aerobic zone II and the membrane tank zone are communicated in sequence, the anaerobic zone and the anoxic zone are respectively used as water inlet points, and the membrane tank zone is used as a water outlet point and a discharge point of excess sludge;
dissolved oxygen concentrations of the aerobic zone I, the micro-anoxic zone and the aerobic zone II are respectively controlled by a DO automatic control method;
the sludge concentration of an aerobic zone I, a micro-anoxic zone and an aerobic zone II is detected in real time to control the discharge amount of the residual sludge in the membrane pool zone;
the membrane pool zone returns sludge to the aerobic zone I through primary reflux, the micro-anoxic zone returns nitrifying liquid to the anoxic zone through secondary reflux, and the anoxic zone returns anoxic liquid to the anaerobic zone through tertiary reflux;
adjusting the carbon source adding amount and the reflux ratio of the secondary reflux to the tertiary reflux by detecting the orp values of the anaerobic zone, the anoxic zone and the micro anoxic zone in real time;
the DO automatic control method comprises the following steps:
s201: setting a dissolved oxygen target value of a zone to be controlled, and acquiring a dissolved oxygen actual value of the zone to be controlled;
s202: carrying out PID control operation according to the dissolved oxygen target value and the dissolved oxygen actual value;
s203: performing fan guide vane control or fan frequency control on the fan through PID control operation;
s204: revising and correcting the operation control of the fan according to the correction compensation to obtain the air supply amount of the fan corresponding to the area to be controlled;
wherein the zones to be controlled are an aerobic zone I, a micro-anoxic zone and an aerobic zone II;
the method of the DO autonomous method further comprises:
s205: each zone to be controlled is correspondingly provided with a valve for controlling the aeration quantity;
s206: respectively obtaining a dissolved oxygen target value and a dissolved oxygen actual value of each zone to be controlled, and carrying out PI control operation;
s207: adjusting the opening of each valve according to the result of PI control operation;
installing DO online instruments at the tail ends of the aerobic zone I, the micro-anoxic zone and the aerobic zone II, and respectively acquiring the dissolved oxygen actual values of the aerobic zone I, the micro-anoxic zone and the aerobic zone II through the DO online instruments;
the dissolved oxygen target value of the aerobic I area is set to be between 1 and 2mg/l, the dissolved oxygen target value of the aerobic II area is set to be between 2 and 3mg/l, and the dissolved oxygen target value of the micro-anoxic area is set to be between 0.3 and 0.6 mg/l;
detecting orp values of an anaerobic zone, an anoxic zone and a micro-anoxic zone in real time respectively by an online orp detector;
if the value of the anaerobic zone orp is larger than the target value, reducing the reflux ratio of the three-stage reflux; if the value of the anaerobic zone orp is less than the target value, the reflux ratio of the three-stage reflux is increased;
if the orp values of the anoxic zone and the micro-anoxic zone are both larger than the target value, reducing the reflux ratio of the secondary reflux or increasing the carbon source adding amount of a water inlet point; otherwise, increasing the reflux ratio of the secondary reflux or reducing the carbon source adding amount of a water inlet point;
the oxidation-reduction potential of the anaerobic zone is-400 to-200 mv, the oxidation-reduction potential of the anoxic zone is-200 to-100 mv, and the oxidation-reduction potential of the micro-anoxic zone is-150 to-80 mv;
the nitrification and denitrification reactions are synchronously generated in the micro-anoxic zone.
2. The enhanced nitrogen removal method for high sludge concentration according to claim 1, further comprising:
and carrying out PID control operation through the total phosphorus target value and the total phosphorus actual value of the water outlet point to dynamically control PAC addition.
3. The enhanced denitrification method for high sludge concentration according to claim 2, wherein the PAC dosage control method comprises the following steps:
s101: setting a total phosphorus target value of a water outlet point and acquiring a total phosphorus actual value of the water outlet point;
s102: performing PID control operation according to the total phosphorus target value and the total phosphorus actual value;
s103: according to PID control operation, PAC adding concentration is obtained, and the PAC adding dosage needing to be added is calculated, wherein the calculation formula is as follows:
s104: performing PI control operation according to the calculated PAC dosage;
s105: and dynamically controlling an adding pump corresponding to PAC adding according to PI control operation.
4. The enhanced denitrification method for high sludge concentration as claimed in claim 1, wherein the sludge concentrations of the aerobic zone I, the micro-anoxic zone and the aerobic zone II are respectively detected in real time by an on-line mlss detector;
when the sludge concentration is higher than a target value, increasing the discharge of the excess sludge; when the sludge concentration is lower than the target value, reducing the discharge of the excess sludge;
and adjusting and controlling the sludge concentration of an aerobic I area, a micro-anoxic area and an aerobic II area through the discharge of excess sludge, wherein the sludge concentration of the aerobic I area and the micro-anoxic area is controlled to be 10000-12000mg/l, and the sludge concentration of the aerobic II area is controlled to be 12000-15000mg/l.
5. An enhanced nitrogen removal system for high sludge concentration used in the method of any one of claims 1 to 4, comprising:
the anaerobic zone and the anoxic zone are respectively provided with a water inlet point;
the inlet water of the water inlet point is treated by an anaerobic zone, an anoxic zone, an aerobic zone I, a micro-anoxic zone, an aerobic zone II and a membrane pool zone which are sequentially communicated, and then is denitrified to be discharged;
wherein, the membrane pool zone reflows the sludge to an aerobic zone I through primary reflow; the micro anoxic zone reflows nitrified liquid to the anoxic zone through secondary reflux; the anoxic zone returns anoxic liquid to the anaerobic zone through three-stage reflux.
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