CN105892504A - Thermal power plant denitration ammonia supplying automatic return circuit control method and system - Google Patents
Thermal power plant denitration ammonia supplying automatic return circuit control method and system Download PDFInfo
- Publication number
- CN105892504A CN105892504A CN201510459723.2A CN201510459723A CN105892504A CN 105892504 A CN105892504 A CN 105892504A CN 201510459723 A CN201510459723 A CN 201510459723A CN 105892504 A CN105892504 A CN 105892504A
- Authority
- CN
- China
- Prior art keywords
- concentration value
- control loop
- ammonia
- value
- side outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a thermal power plant denitration ammonia supplying automatic return circuit control method and system. An ammonia supplying automatic return circuit consists of a master control return circuit and an auxiliary control return circuit, the master control return circuit fulfills an adjusting function while NOx concentration of an exit of an SCR reactor is used as a process value, the auxiliary control return circuit comprises a plurality of single control return circuits, and each single control return circuit fulfills an adjusting function while an ammonia supplying flow quantity is used as a process value. The beneficial effects of the thermal power plant denitration ammonia supplying automatic return circuit control method and system are that via a plurality of function relations, influence exerted on the automatic control return circuit by disturbance caused by change of parameters such as boiler loads, entrance NOx concentration, exit NOx concentration and the like can be eliminated or minimized; the ammonia supplying automatic return circuit can be enabled to respond in advance to adjust rapidly and eliminate influence caused by the disturbance, and an aim of accurate control can be attained.
Description
Technical field
The present invention relates to denitration and supply ammonia technical field, in particular to the denitration of a kind of thermal power plant for ammonia certainly
The control method in dynamic loop and control system.
Background technology
Along with China environmental protection law, rule and standard increasingly strict, gas denitrifying technology is the most extensive
It is applied to most Coal-fired group.The NO that burning is producedxControl method mainly has control before burning
3 classes are controlled after system, burning control and burn.Control before burning bunker coal is converted into low nitrogen fuel exactly,
But its difficulty is very big, and cost is the highest, and engineer applied is few；In burning control refer to improve combustion system and
Production technology, uses low NOxCombustion technology, reduces NO in stovexGrowing amount, the method expense is relatively low, but
Due to the limitation of low-NO_x combustion technology in stove so that NOxControl effect unsatisfactory；After burning, control is
Refer at flue afterbody De-NO_x, by the NO in flue gasxIt is changed into harmless N2Or useful fertilizer,
Because it has the advantages such as technology maturation, denitration efficiency are high, reliable, it is the most most widely used
General NOxControl technology.
In the fired power generating unit of China, the SCR of control mode after having the denitrification apparatus employing of more than 92% to burn
(Selective Catalytic Reduction, selective catalytic reduction) denitrating technique, this technology is by ammonia
Class reducing agent sprays in flue gas, under the effect of catalyst selectively with NOxCarry out reduction reaction, by cigarette
NO in gasxIt is converted into N2And H2O。
Conventional denitrification reducing agent has liquefied ammonia, ammonia and 3 kinds of carbamide.The investment of liquefied ammonia, transport and usage charges
With minimum, but liquefied ammonia belongs to dangerous materials, it is necessary to have strict safety assurance and fire prevention measure, its transport and
Storage relates to local statues and labour hygiene standard；Ammonia transportation volume is huge, transport and carrying cost
The highest；Carbamide is a kind of safe graininess agricultural fertilizer, without transport and storage problem, but ammonia system processed
Complexity, initial investment is bigger.
Denitrating system is in running, if reducing agent sprays into very few, can cause NOxDischarge exceeds standard, and sends out
The environmental protection facing great number is punished by electricity enterprise；If reducing agent sprays into too much, not only result in reducing agent
Waste, increases operating cost, but also can increase the escapement ratio of ammonia, and then it is stifled to be greatly increased air preheater
The risk of plug.Therefore, thermal power plant is guaranteeing NOxWhile emission compliance, denitrating system to be strengthened
Reliability of operation, seriality and economy.Wherein, the reducing agent straying quatity of denitrating system is accurately controlled
(hereinafter referred to as ammonia amount) becomes the key avoided discharge beyond standards, effectively reduce operating cost.
From the point of view of the ruuning situation of current domestic denitrating system, the control for ammonia amount is generally adopted by denitrating system
By basic control mode, i.e. fixed molar ratio control mode (Constant Mole Ratio Control).?
Under this control mode, system is according to fixing NH3/NOxNO in mol ratio removing flue gasx.Perform for ammonia regulation
The process values (PV) that the confession ammonia flow of mechanism controls as single loop PID, the confession ammonia stream of each actuator
Amount setting value (SP) Computing Principle is as follows:
(1)NOxMass flow=flue gas flow × entrance NOxConcentration；
(2) reducing agent mass flow=NOxMass flow × ammonia nitrogen mol ratio × conversion coefficient；
(3)
This control strategy is setting value adjustable unity loop control strategy, its control principle block diagram such as Fig. 1
Shown in.Wherein, the numerical value of flue gas flow can be directly obtained by flowmeter survey, it is possible to according to boiler
The theoretical value that load is corresponding obtains.
Also there is partial denitrification system that A side, B side reaction device are respectively adopted the controlling party of double PID bunch grade adjustment
Formula realizes the control for ammonia amount.Main PID regulator regulation denitration efficiency or SCR reactor outlet NOx
Concentration (hereinafter referred to as exports NOxConcentration), secondary PID regulator regulation is for ammonia flow.In order to make automatically to return
Road can quickly respond when load change, strengthens the stability of automatic loop, this bunch grade adjustment loop
Generally also can introduce boiler load as feed-forward signal.The principle frame of unilateral double PID bunch grade adjustment control mode
Figure is as shown in Figure 2.
The control strategy of fixed molar ratio is feasible in theory, but during reality is applied, past
Automatic loop is caused to put into instability, often toward because of reasons such as exhaust gas volumn fluctuation are excessive, governing response is slow
Occur that reducing agent sprays into very few or sprays into too much phenomenon, have a strong impact on the operation steady in a long-term of denitrating system,
Not only increase the working strength of operations staff, but also considerably increase operating cost.
And the control strategy of double PID bunch grade adjustment, it is adjusted although with double PID adjustment device, introduces again
Boiler load feed-forward signal, improves the control effect of automatic loop to a certain extent, but due to also
Do not eliminate the impact that other interference factors bring, yet suffer from actual application the amplitude of accommodation bigger than normal,
The problems such as regulating cycle is long.
The ontological properties of eliminating denitration CEMS equipment fault and adjustment actuating mechanism etc. are to for ammonia automatic loop
Impact, by Systematic Analysis, cause the main cause for ammonia automatic loop regulation quality difference to conclude
For following some:
(1) flue gas flow parameter is inaccurate.In actual applications, either directly measure obtain by instrument
, the theoretical value corresponding according further to boiler load obtains, and obtained flue gas flow data all cannot be accurate
The really real change situation of flue gas flow in reflection actual condition.The cigarette obtained especially by instrument measurement
Throughput, even instrument itself is working properly, its measured value also can frequent fluctuation, cause regulation
Output valve fluctuates frequently up and down, the most real flue gas flow increasing (can by boiler load and
Entrance NOxThe change of concentration judges), and the measured value of instrument is reducing or is being basically unchanged, and then cause
The when of should increasing reducing agent straying quatity, regulation output does not the most increase so that controls effect and pays no attention to very much
Think.And the flue gas flow obtained according to the theoretical value that boiler load is corresponding is also inaccurate, because i.e.
Making in the case of boiler load is identical, produced by different as-fired coal matter and combustion conditions, exhaust gas volumn is also
It is different.
(2) automatic loop response is slow.This causes due to process system itself, because chemical reaction
Need the regular hour, the reason that process pipe, installations and facilities are arranged in addition so that just sprayed into goes back
Former dose can not participate in reduction reaction at once, and needs a few minutes just can make outlet NO even more for a long timexConcentration
Reduce.In this case, if the regulation effect for ammonia automatic loop strengthened, will result in overshoot；
On the contrary, if declines will be regulated, the phenomenon that control lag, automatic loop do not catch up with is arisen that.
(3) automatic loop interference factor is more.During boiler load variation, the big amplitude variation of exhaust gas volumn can be caused
Change so that the NO of SCR reactor inletxMeasure fluctuation therewith, and then cause the regulation of automatic loop defeated
Go out upper and lower frequent fluctuation.It addition, when boiler load is substantially steady, as-fired coal matter and the change of firing optimization
Change, also can make the NO of SCR reactor inletxAmount changes, and then affects the regulating effect of automatic loop.
CEMS system external, when carrying out the periodic maintenance task such as automatic back blow, calibration, can be passed by CEMS equipment
Defeated data interlock keeps, different equipment manufacturers, and CEMS safeguards that the required time is the most different automatically,
Some CEMS equipment only needs to make data keep 1～3 minute, and have then needs holding data more than 10 minutes；
For for ammonia automatic loop, the numerical value after holding is exactly a definite value, if for a long time according to this number
Value automatically adjusts, and the CEMS data once kept are released, and the numerical bias before and after release is often
Very big, this will result in the disturbance of phase step type；If locking keeps PID while CEMS data keep
The output valve of actuator, then after the data of holding are released, can cause automatic loop to vibrate equally, from
Dynamic loop generally requires and is lot more time to be adjusted to stable state, even it sometimes appear that deviation is excessive, cannot
Adjust the phenomenon of returning.
Summary of the invention
For solving the problems referred to above, it is an object of the invention to provide a kind of elimination interference factor, reach accurate
The thermal power plant's denitration controlling purpose supplies control method and the control system of ammonia automatic loop.
The invention provides a kind of thermal power plant denitration control method for ammonia automatic loop, for ammonia automatic loop
Being made up of main control loop and auxiliary control loop, described main control loop takes the outlet NO of SCR reactorxConcentration is made
Being adjusted for process values, described auxiliary control loop includes that multiple single control loop, each single control loop take for ammonia
Flow is adjusted as process values, specifically includes step:
Step 1, boiler load obtains the required of correspondence under different load by the first function F1 (X) and supplies ammonia amount
Radix；
Step 2, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation by the first analog quantity alternative module, and described first analog quantity two is selected
The outlet NO of one module outputxConcentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
Step 3, the outlet NO that will obtain in step 2xConcentration value is exported by the 3rd function F3 (X)
NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and by described first output
Compensating parameter participates in regulation computing as feed-forward signal；
Step 4, the outlet NO that the PID regulator of described main control loop will obtain in step 2xConcentration value
Being adjusted computing with the described first output compensating parameter obtained in step 3, the output valve after computing is led to
Cross the second function F2 (X) and obtain the required correction factor for ammonia amount；
Step 5, the correction factor that the cardinal sum step 4 step 1 obtained obtains is multiplied and obtains for ammonia amount value；
Step 6, obtains different speed by the percentage speed variation of described boiler load by the 5th function F5 (X)
The second output compensating parameter that degree rate of change is corresponding；
Step 7, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second analog quantity two
A module is selected to carry out Selecting operation, after the value of described second analog quantity alternative module output is as selecting
Entrance NOxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value passes through the 4th function F4 (X)
Obtain the 3rd output compensating parameter that different percentage speed variations is corresponding；
Step 8, obtains described second output compensating parameter and described 3rd output compensating parameter with step 5
Confession ammonia amount value be added, obtain actually required confession ammonia amount, and distribute to this digital average to put into automatic
For ammonia adjustment actuating mechanism, obtain each actuator for ammonia flow setting value, as in auxiliary control loop
The confession ammonia flow setting value of the PID regulator in each single control loop；
Step 9, by the confession for ammonia flow with the PID regulator in each single control loop in each single control loop
Ammonia flow setting value is adjusted computing, obtains each ammonia that supplies for ammonia adjustment actuating mechanism and regulates flow.
As a further improvement on the present invention, in step 2, described first analog quantity alternative module output
Outlet NOxConcentration value is A side outlet NOxConcentration value and B side outlet NOxMaximum in concentration value
Value or A side outlet NOxConcentration value and B side outlet NOxMinima in concentration value or A side outlet NOx
Concentration value and B side outlet NOxThe meansigma methods of concentration value.
As a further improvement on the present invention, in step 7, described second analog quantity alternative module output
Entrance NOxConcentration value is A side entrance NOxConcentration value and B side entrance NOxMaximum in concentration value
Value or A side entrance NOxConcentration value and B side entrance NOxMinima in concentration value or A side entrance NOx
Concentration value and B side entrance NOxThe meansigma methods of concentration value.
Present invention also offers a kind of thermal power plant denitration control system for ammonia automatic loop, automatically return for ammonia
Route main control loop and auxiliary control loop are constituted, and described main control loop takes the outlet NO of SCR reactorxConcentration
Being adjusted as process values, described auxiliary control loop includes that multiple single control loop, each single control loop take confession
Ammonia flow is adjusted as process values, specifically includes:
First computing module, boiler load obtains under different load corresponding required by the first function F1 (X)
Radix for ammonia amount；
Judge to select module, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation by the first analog quantity alternative module, and described first analog quantity two is selected
The outlet NO of one module outputxConcentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
First compensating module, by the described outlet NO judging to select module outputxConcentration value passes through the 3rd letter
Number F3 (X) obtains exporting NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and
Described first output compensating parameter is participated in regulation computing as feed-forward signal；
First adjustment module, the PID regulator of described main control loop judges to select module output by described
Outlet NOxThe described first output compensating parameter obtained in concentration and described first compensating module is adjusted
Computing, the output valve after computing obtains the required correction factor for ammonia amount by the second function F2 (X)；
Second computing module, the first adjustment module described in the cardinal sum obtain described first computing module obtains
To correction factor be multiplied and obtain for ammonia amount value；
Second compensating module, is obtained the percentage speed variation of described boiler load not by the 5th function F5 (X)
The second output compensating parameter that same percentage speed variation is corresponding；
3rd compensating module, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second mould
Analog quantity alternative module carries out Selecting operation, and the value of described second analog quantity alternative module output is as choosing
Entrance NO after selectingxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value passes through the 4th letter
Number F4 (X) obtains the 3rd output compensating parameter that different percentage speed variations is corresponding；
3rd computing module, by described second output compensating parameter and described 3rd output compensating parameter and institute
State the confession ammonia amount value addition that the second computing module obtains, obtain actually required confession ammonia amount, and by this numerical value
It is averagely allocated to put into automatically for ammonia adjustment actuating mechanism, obtains each actuator and set for ammonia flow
Value, as the confession ammonia flow setting value of the PID regulator in single control loop each in auxiliary control loop；
Second adjustment module, adjusting each single control loop with the PID in each single control loop for ammonia flow
The ammonia flow setting value that supplies of joint device is adjusted computing, obtains each adjusting for ammonia for ammonia adjustment actuating mechanism
Amount of restriction.
As a further improvement on the present invention, described judgement selects in module, and described first analog quantity two is selected
The outlet NO of one module outputxConcentration value is A side outlet NOxConcentration value and B side outlet NOxConcentration
Maximum in value or A side outlet NOxConcentration value and B side outlet NOxMinima in concentration value or A
Side outlet NOxConcentration value and B side outlet NOxThe meansigma methods of concentration value.
As a further improvement on the present invention, in described 3rd compensating module, described second analog quantity two is selected
The entrance NO of one module outputxConcentration value is A side entrance NOxConcentration value and B side entrance NOxConcentration
Maximum in value or A side entrance NOxConcentration value and B side entrance NOxMinima in concentration value or A
Side entrance NOxConcentration value and B side entrance NOxThe meansigma methods of concentration value.
The invention have the benefit that by multiple functional relationships, by boiler load, entrance NOxConcentration,
Outlet NOxThe impact of automatic control loop is eliminated or drops to by the disturbance caused by the Parameters variation such as concentration
Minimum, it can make, for ammonia automatic loop early response, quickly to regulate, and eliminates the impact that disturbance brings,
Reach the purpose accurately controlled.
Accompanying drawing explanation
Fig. 1 is the theory diagram of fixed molar ratio control mode；
Fig. 2 is the theory diagram of unilateral double PID bunch grade adjustment control mode；
Fig. 3 is the control method for ammonia automatic loop of a kind of thermal power plant denitration described in the embodiment of the present invention
Flow chart；
Fig. 4 is the main control loop theory diagram described in the embodiment of the present invention；
Fig. 5 is the auxiliary control circuit theory block diagram described in the embodiment of the present invention；
Fig. 6 is the biasing debugging functions theory diagram described in the embodiment of the present invention；
Fig. 7 is the control system for ammonia automatic loop of a kind of thermal power plant denitration described in the embodiment of the present invention
Structured flowchart.
Detailed description of the invention
Below by specific embodiment and combine accompanying drawing the present invention is described in further detail.
Embodiment 1, as it is shown on figure 3, a kind of thermal power plant denitration of the embodiment of the present invention is for ammonia automatic loop
Control method, is made up of main control loop and auxiliary control loop for ammonia automatic loop, and main control loop takes SCR reaction
The outlet NO of devicexConcentration is adjusted as process values, and auxiliary control loop includes multiple single control loop, each
Single control loop takes and is adjusted as process values for ammonia flow, specifically includes step:
Step 1, boiler load obtains the required of correspondence under different load by the first function F1 (X) and supplies ammonia amount
Radix；
Step 2, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation, the first analog quantity alternative mould by the first analog quantity alternative module
Block output A side outlet NOxConcentration value and B side outlet NOxMaximum in concentration value or A side outlet
NOxConcentration value and B side outlet NOxMinima in concentration value or A side outlet NOxConcentration value and B side
Outlet NOxThe meansigma methods of concentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
Step 3, the outlet NO that will obtain in step 2xConcentration value is exported by the 3rd function F3 (X)
NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and the first output is compensated
Parameter participates in regulation computing as feed-forward signal；
Step 4, the outlet NO that the PID regulator of main control loop will obtain in step 2xConcentration value and step
The the first output compensating parameter obtained in rapid 3 is adjusted computing, and the output valve after computing passes through the second letter
Number F2 (X) obtains the required correction factor for ammonia amount；
Step 5, the correction factor that the cardinal sum step 4 step 1 obtained obtains is multiplied and obtains for ammonia amount value；
Step 6, obtains different speed by the percentage speed variation of boiler load by the 5th function F5 (X) and becomes
The second output compensating parameter that rate is corresponding；
Step 7, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second analog quantity two
A module is selected to carry out Selecting operation, the second analog quantity alternative module output A side entrance NOxConcentration value and
B side entrance NOxMaximum in concentration value or A side entrance NOxConcentration value and B side entrance NOxConcentration
Minima in value or A side entrance NOxConcentration value and B side entrance NOxThe meansigma methods of concentration value is as choosing
Entrance NO after selectingxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value passes through the 4th letter
Number F4 (X) obtains the 3rd output compensating parameter that different percentage speed variations is corresponding；
Step 8, the confession ammonia amount that the second output compensating parameter and the 3rd output compensating parameter are obtained with step 5
Value is added, and obtains actually required confession ammonia amount, and distributes to this digital average put into automatically for ammonia tune
Joint actuator, obtains each actuator and supplies ammonia flow setting value, as single control each in auxiliary control loop
The confession ammonia flow setting value of the PID regulator in loop；
Step 9, by the confession for ammonia flow with the PID regulator in each single control loop in each single control loop
Ammonia flow setting value is adjusted computing, obtains each ammonia that supplies for ammonia adjustment actuating mechanism and regulates flow.
As shown in Figure 4 and Figure 5, boiler load determines correspondence under different load by the first function F1 (X)
The required radix for ammonia amount.In Fig. 4,Represent percentage speed variation.The PID regulator of main control loop with
Outlet NOxConcentration is adjusted computing as process variable, and its output valve determines institute by the second function F2 (X)
Need to be for the correction factor of ammonia amount.Radix is multiplied with correction factor and can obtain actually required confession ammonia amount, then
This digital average is distributed to the automatic actuator of each input, returns as single control each in auxiliary control loop
The confession ammonia flow setting value of the PID regulator in road.Outlet NOxThe percentage speed variation of concentration passes through the 3rd
Function F3 (X) determines the first output compensating parameter that different percentage speed variations is corresponding, and as feed-forward signal
Participate in regulation computing.Entrance NOxThe percentage speed variation of concentration determines different speed by the 4th function F4 (X)
The 3rd output compensating parameter that degree rate of change is corresponding；The percentage speed variation of boiler load passes through the 5th function
F5 (X) determines the second output compensating parameter that different percentage speed variations is corresponding.
Wherein, the first function F1 (X), the second function F2 (X), the 3rd function F3 (X), the 4th function F4 (X)
Parameter value such as table 1 with the 5th function F5 (X).In first function F1 (X), X is boiler load, Y
For the required radix for ammonia amount.In second function F2 (X), X is master control PID regulator output valve, and Y is
The required correction factor for ammonia amount.In 3rd function F3 (X), X is outlet NOxThe percentage speed variation of concentration,
Y is the first output compensating parameter.In 4th function F4 (X), X is entrance NOxThe percentage speed variation of concentration,
Y is the 3rd output compensating parameter.In 5th function F5 (X), X is the percentage speed variation of boiler load, Y
It it is the second output compensating parameter.The 3rd function F3 (X), the 4th function F4 (X) and the 5th function at table 1
In the value of the X of F5 (X), positive number represents the percentage speed variation of rising, the velocity variations that negative number representation declines
Rate.
By the first function F1 (X), the second function F2 (X), the 3rd function F3 (X), the 4th function F4 (X)
With the 5th function F5 (X), can be by boiler load, entrance NOxConcentration, outlet NOxThe disturbances such as concentration because of
The impact of automatic control loop is eliminated or is preferably minimized by element.
Table 1
| Parameter | F1(X) | F2(X) | F3(X) | F4(X) | F5(X) |
| X1 | 0 | 0 | -1.0 | -1.0 | -1.0 |
| Y1 | 0 | 0.5 | -1 | -40 | -10 |
| X2 | 250 | 100 | -0.8 | -0.8 | -0.8 |
| Y2 | 60 | 1.5 | -0.8 | -30 | -8 |
| X3 | 300 | -0.6 | -0.6 | -0.6 | |
| Y3 | 70 | -0.6 | -20 | -6 | |
| X4 | 350 | -0.4 | -0.4 | -0.4 | |
| Y4 | 100 | -0.4 | -10 | -4 | |
| X5 | 400 | -0.2 | -0.2 | -0.2 | |
| Y5 | 110 | -0.2 | -5 | -2 | |
| X6 | 450 | 0 | 0 | 0 | |
| Y6 | 120 | 0 | 0 | 0 | |
| X7 | 500 | 0.2 | 0.2 | 0.2 | |
| Y7 | 130 | 0.2 | 10 | 3 | |
| X8 | 550 | 0.4 | 0.4 | 0.4 | |
| Y8 | 150 | 0.4 | 20 | 6 | |
| X9 | 600 | 0.6 | 0.6 | 0.6 | |
| Y9 | 160 | 0.6 | 30 | 9 | |
| X10 | 650 | 0.8 | 0.8 | 0.8 | |
| Y10 | 170 | 0.8 | 40 | 12 | |
| X11 | 700 | 1 | 1 | 1 | |
| Y11 | 180 | 1 | 50 | 15 |
The problem safeguarded for the calibration of CEMS system at regular intervals, can use the control model that multilamellar selects,
Use A side outlet, B side outlet NO the most under normal circumstancesxConcentration passes through the first analog quantity alternative module
Carrying out output valve, the process values as the PID regulator of main control loop participates in regulation computing；When A side outlet
When CEMS system calibration is safeguarded, then select B side outlet NOxConcentration is as main control loop PID regulator
Process values；In like manner, when B side outlet CEMS system calibration is safeguarded, then select A side outlet NOx
Concentration is as the process values of main control loop PID regulator.Because entrance CEMS system calibration is safeguarded this plan
Control loop impact slightly is the least, therefore does not considers.For A side outlet, B side outlet CEMS system
The situation that calibration is safeguarded, adjustable outlet CEMS system at regular intervals may be occurred to calibrate the time safeguarded simultaneously,
The timing node that two side outlet CEMS system calibrations of staggering are safeguarded, it is to avoid two side outlet CEMS systems are same
Time safeguard situation occur.
Operation conditions in view of A side reaction device, B side reaction device may be different, thus cause both sides
Actual needs ammonia amount inconsistent；If the simplest mean allocation, arise that a certain side reaction device also
Former dose sprays into too much phenomenon.Therefore, each actuator stream is obtained total for ammonia flow mean allocation
After amount setting value, and before this setting value enters each single control loop PID regulator, add biasing
Debugging functions, can realize A side reaction device and B side reaction device is on-demand for ammonia, it is to avoid unilateral reactor overspray
Situation occur.As shown in Figure 6, principle of operation is as follows for the theory diagram of the biasing debugging functions of the present invention:
CGao Xuan=Max (CA side, CB side)；
Δ1=CGao Xuan-CA side；
Δ2=CGao Xuan-CB side；
Wherein: CA sideFor A side outlet NOx concentration value, CB sideFor B side outlet NOx concentration value.
Logic is selected to select the two by height A side outlet NOx concentration value, B side outlet NOx concentration value
In maximum, this value is done with A side outlet NOx concentration value and B side outlet NOx concentration value respectively
Difference draws Δ1And Δ2.If Δ1＜ 1, then A side is not revised for ammonia amount, i.e. A side is repaiied for ammonia amount
On the occasion of for 0；If Δ1＞ 1, then determine different Δs according to the 6th function F6 (X)1The A side that value is corresponding
Decrement for ammonia amount.In like manner, if Δ2＜ 1, then B side is not revised for ammonia amount, i.e. B side is for ammonia amount
Correction value be 0；If Δ2＞ 1, then determine different Δs according to the 7th function F7 (X)2Value correspondence
B side is for the decrement of ammonia amount.The output valve of the 6th function F6 (X) and the 7th function F7 (X) respectively with master control
Each actuator that loop is tried to achieve is added for ammonia flow setting value, thus obtains revised each execution
Mechanism is for ammonia flow setting value.The parameter value such as table 2 of the 6th function F6 (X) and the 7th function F7 (X).
Table 2
| Parameter | F6(X) | F7(X) |
| X1 | 1 | 1 |
| Y1 | 0 | 0 |
| X2 | 5 | 5 |
| Y2 | -10 | -10 |
| X3 | 10 | 10 |
| Y3 | -20 | -20 |
| X4 | 20 | 20 |
| Y4 | -25 | -25 |
| X5 | 30 | 30 |
| Y5 | -30 | -30 |
| X6 | 40 | 40 |
| Y6 | -35 | -35 |
In table 2, in the 6th function F6 (X), X is Δ 1, and the Δ 1 that Y is different is worth the A side of correspondence and supplies
The decrement of ammonia amount.In 7th function F7 (X), X is Δ 2, and the Δ 2 that Y is different is worth the B side of correspondence
Decrement for ammonia amount.
Owing in urea method denitrating technique, A side reaction device entrance and B side reaction device inlet duct are manually to adjust
Section door, therefore these biasing debugging functions are generally only applicable to liquid ammonia process for caustic soda purification denitrating technique.
Embodiment 2, as it is shown in fig. 7, present invention also offers the denitration of a kind of thermal power plant for ammonia automatic loop
Control system, is made up of main control loop and auxiliary control loop for ammonia automatic loop, and main control loop takes SCR reaction
The outlet NO of devicexConcentration is adjusted as process values, and auxiliary control loop includes multiple single control loop, each
Single control loop takes and is adjusted as process values for ammonia flow, specifically includes:
First computing module, boiler load obtains under different load corresponding required by the first function F1 (X)
Radix for ammonia amount；
Judge to select module, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation, the first analog quantity alternative mould by the first analog quantity alternative module
Block output A side outlet NOxConcentration value and B side outlet NOxMaximum in concentration value or A side outlet
NOxConcentration value and B side outlet NOxMinima in concentration value or A side outlet NOxConcentration value and B side
Outlet NOxThe meansigma methods of concentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
First compensating module, will determine that the outlet NO selecting module outputxConcentration value passes through the 3rd function
F3 (X) obtains exporting NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and will
First output compensating parameter participates in regulation computing as feed-forward signal；
First adjustment module, the PID regulator of main control loop will determine that the outlet NO selecting module outputx
The the first output compensating parameter obtained in concentration and the first compensating module is adjusted computing, defeated after computing
Go out value and obtain the required correction factor for ammonia amount by the second function F2 (X)；
Second computing module, the correction that cardinal sum the first adjustment module obtained by the first computing module obtains
Multiplication obtains for ammonia amount value；
Second compensating module, obtains different by the percentage speed variation of boiler load by the 5th function F5 (X)
The second output compensating parameter that percentage speed variation is corresponding；
3rd compensating module, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second mould
Analog quantity alternative module carries out Selecting operation, the second analog quantity alternative module output A side entrance NOxDense
Angle value and B side entrance NOxMaximum in concentration value or A side entrance NOxConcentration value and B side entrance
NOxMinima in concentration value or A side entrance NOxConcentration value and B side entrance NOxConcentration value average
It is worth as the entrance NO after selectingxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value is led to
Cross the 4th function F4 (X) and obtain the 3rd output compensating parameter that different percentage speed variations is corresponding；
3rd computing module, by the second output compensating parameter and the 3rd output compensating parameter and the second computing mould
The confession ammonia amount value that block obtains is added, and obtains actually required confession ammonia amount, and distributes to this digital average throw
Enter automatically for ammonia adjustment actuating mechanism, obtain each actuator and supply ammonia flow setting value, as auxiliary control
In loop, the PID regulator in each single control loop supplies ammonia flow setting value；
Second adjustment module, adjusting each single control loop with the PID in each single control loop for ammonia flow
The ammonia flow setting value that supplies of joint device is adjusted computing, obtains each adjusting for ammonia for ammonia adjustment actuating mechanism
Amount of restriction.
The regulating effect for ammonia automatic loop of the present invention is excellent, for safe and stable, the warp of denitrating system
Ji operation provides guarantee.The control method of the present invention can reach every Con trolling index, the most satisfied
The requirement of SCR denitration Automated condtrol, for SCR denitration system, has stronger versatility and practicality
Property.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for this
For the technical staff in field, the present invention can have various modifications and variations.All spirit in the present invention and
Within principle, any modification, equivalent substitution and improvement etc. made, should be included in the protection of the present invention
Within the scope of.
Claims (6)
1. the control method of thermal power plant's denitration confession ammonia automatic loop, it is characterised in that automatically return for ammonia
Route main control loop and auxiliary control loop are constituted, and described main control loop takes the outlet NO of SCR reactorxConcentration
Value is adjusted as process values, and described auxiliary control loop includes that multiple single control loop, each single control loop take
It is adjusted as process values for ammonia flow, specifically includes step:
Step 1, boiler load obtains the required of correspondence under different load by the first function F1 (X) and supplies ammonia amount
Radix；
Step 2, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation by the first analog quantity alternative module, and described first analog quantity two is selected
The outlet NO of one module outputxConcentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOx concentration value
Process values as the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOx concentration value
Process values as the PID regulator of main control loop；
Step 3, the outlet NO that will obtain in step 2xConcentration value is exported by the 3rd function F3 (X)
NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and by described first output
Compensating parameter participates in regulation computing as feed-forward signal；
Step 4, the outlet NO that the PID regulator of described main control loop will obtain in step 2xConcentration value
Being adjusted computing with the described first output compensating parameter obtained in step 3, the output valve after computing is led to
Cross the second function F2 (X) and obtain the required correction factor for ammonia amount；
Step 5, the correction factor that the cardinal sum step 4 step 1 obtained obtains is multiplied and obtains for ammonia amount value；
Step 6, obtains different speed by the percentage speed variation of described boiler load by the 5th function F5 (X)
The second output compensating parameter that degree rate of change is corresponding；
Step 7, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second analog quantity two
A module is selected to carry out Selecting operation, after the value of described second analog quantity alternative module output is as selecting
Entrance NOxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value passes through the 4th function F4 (X)
Obtain the 3rd output compensating parameter that different percentage speed variations is corresponding；
Step 8, obtains described second output compensating parameter and described 3rd output compensating parameter with step 5
Confession ammonia amount value be added, obtain actually required confession ammonia amount, and distribute to this digital average to put into automatic
For ammonia adjustment actuating mechanism, obtain each actuator for ammonia flow setting value, as in auxiliary control loop
The confession ammonia flow setting value of the PID regulator in each single control loop；
Step 9, by the confession for ammonia flow with the PID regulator in each single control loop in each single control loop
Ammonia flow setting value is adjusted computing, obtains each ammonia that supplies for ammonia adjustment actuating mechanism and regulates flow.
Control method the most according to claim 1, it is characterised in that in step 2, described first
The outlet NO of analog quantity alternative module outputxConcentration value is A side outlet NOxConcentration value and B side outlet
NOxMaximum in concentration value or A side outlet NOxConcentration value and B side outlet NOxIn concentration value
Little value or A side outlet NOxConcentration value and B side outlet NOxThe meansigma methods of concentration value.
Control method the most according to claim 1, it is characterised in that in step 7, described second
The entrance NO of analog quantity alternative module outputxConcentration value is A side entrance NOxConcentration value and B side entrance
NOxMaximum in concentration value or A side entrance NOxConcentration value and B side entrance NOxIn concentration value
Little value or A side entrance NOxConcentration value and B side entrance NOxThe meansigma methods of concentration value.
4. the control system of thermal power plant's denitration confession ammonia automatic loop, it is characterised in that automatically return for ammonia
Route main control loop and auxiliary control loop are constituted, and described main control loop takes the outlet NO of SCR reactorxConcentration
Being adjusted as process values, described auxiliary control loop includes that multiple single control loop, each single control loop take confession
Ammonia flow is adjusted as process values, specifically includes:
First computing module, boiler load obtains under different load corresponding required by the first function F1 (X)
Radix for ammonia amount；
Judge to select module, by judging the process values selecting to obtain the PID regulator of main control loop:
If A side outlet and B side outlet are all normal, then A side outlet NOxConcentration value and B side outlet
NOxConcentration value carries out Selecting operation by the first analog quantity alternative module, and described first analog quantity two is selected
The outlet NO of one module outputxConcentration value is as the process values of the PID regulator of main control loop；
If the CEMS system of A side outlet is safeguarded in calibration, then select B side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
If the CEMS system of B side outlet is safeguarded in calibration, then select A side outlet NOxConcentration value is made
Process values for the PID regulator of main control loop；
First compensating module, by the described outlet NO judging to select module outputxConcentration value passes through the 3rd letter
Number F3 (X) obtains exporting NOxFirst that the friction speed rate of change of concentration value is corresponding exports compensating parameter, and
Described first output compensating parameter is participated in regulation computing as feed-forward signal；
First adjustment module, the PID regulator of described main control loop judges to select module output by described
Outlet NOxThe described first output compensating parameter obtained in concentration and described first compensating module is adjusted
Computing, the output valve after computing obtains the required correction factor for ammonia amount by the second function F2 (X)；
Second computing module, the first adjustment module described in the cardinal sum obtain described first computing module obtains
To correction factor be multiplied and obtain for ammonia amount value；
Second compensating module, is obtained the percentage speed variation of described boiler load not by the 5th function F5 (X)
The second output compensating parameter that same percentage speed variation is corresponding；
3rd compensating module, A side entrance NOxConcentration value and B side entrance NOxConcentration value passes through the second mould
Analog quantity alternative module carries out Selecting operation, and the value of described second analog quantity alternative module output is as choosing
Entrance NO after selectingxConcentration value, by the entrance NO of outputxThe percentage speed variation of concentration value passes through the 4th letter
Number F4 (X) obtains the 3rd output compensating parameter that different percentage speed variations is corresponding；
3rd computing module, by described second output compensating parameter and described 3rd output compensating parameter and institute
State the confession ammonia amount value addition that the second computing module obtains, obtain actually required confession ammonia amount, and by this numerical value
It is averagely allocated to put into automatically for ammonia adjustment actuating mechanism, obtains each actuator and set for ammonia flow
Value, as the confession ammonia flow setting value of the PID regulator in single control loop each in auxiliary control loop；
Second adjustment module, adjusting each single control loop with the PID in each single control loop for ammonia flow
The ammonia flow setting value that supplies of joint device is adjusted computing, obtains each adjusting for ammonia for ammonia adjustment actuating mechanism
Amount of restriction.
Control system the most according to claim 4, it is characterised in that described judgement selects in module,
The outlet NO of described first analog quantity alternative module outputxConcentration value is A side outlet NOxConcentration value and
B side outlet NOxMaximum in concentration value or A side outlet NOxConcentration value and B side outlet NOxConcentration
Minima in value or A side outlet NOxConcentration value and B side outlet NOxThe meansigma methods of concentration value.
Control system the most according to claim 4, it is characterised in that in described 3rd compensating module,
The entrance NO of described second analog quantity alternative module outputxConcentration value is A side entrance NOxConcentration value and
B side entrance NOxMaximum in concentration value or A side entrance NOxConcentration value and B side entrance NOxConcentration
Minima in value or A side entrance NOxConcentration value and B side entrance NOxThe meansigma methods of concentration value.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510459723.2A CN105892504B (en) | 2015-07-30 | 2015-07-30 | The control method and control system of a kind of thermal power plant's denitration for ammonia automatic loop |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510459723.2A CN105892504B (en) | 2015-07-30 | 2015-07-30 | The control method and control system of a kind of thermal power plant's denitration for ammonia automatic loop |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105892504A true CN105892504A (en) | 2016-08-24 |
| CN105892504B CN105892504B (en) | 2018-08-31 |
Family
ID=57002035
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510459723.2A Active CN105892504B (en) | 2015-07-30 | 2015-07-30 | The control method and control system of a kind of thermal power plant's denitration for ammonia automatic loop |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105892504B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106215671A (en) * | 2016-09-09 | 2016-12-14 | 中国大唐集团科学技术研究院有限公司华中分公司 | A kind of thermal power plant denitration spray ammonia control method and device |
| CN106422709A (en) * | 2016-10-24 | 2017-02-22 | 大唐韩城第二发电有限责任公司 | Ammonia spraying regulation automatic control method for denitrification system of thermal power plant |
| CN106731829A (en) * | 2017-03-31 | 2017-05-31 | 华北电力大学（保定） | Suppress control system and method for the purging on thermal power plant's discharged nitrous oxides influence |
| CN107561941A (en) * | 2017-09-01 | 2018-01-09 | 华北电力大学（保定） | A kind of full working scope qualified discharge control method of fired power generating unit denitrating system |
| CN107803114A (en) * | 2017-12-04 | 2018-03-16 | 烟台龙源电力技术股份有限公司 | A kind of denitration control system and its control method and control device |
| CN107967003A (en) * | 2017-03-10 | 2018-04-27 | 邯郸学院 | For the SCR denitration Control Technique in circulating fluidized bed boiler |
| CN109343349A (en) * | 2018-11-01 | 2019-02-15 | 大唐环境产业集团股份有限公司 | A kind of SCR denitrating flue gas Optimal Control System and method based on ammonia spraying amount compensator |
| CN110501901A (en) * | 2019-07-08 | 2019-11-26 | 华能南京金陵发电有限公司 | The SCR spray ammonia required based on the accurate denitration of full load adjusts the method optimized |
| CN111895489A (en) * | 2020-06-17 | 2020-11-06 | 天津国电津能滨海热电有限公司 | Enthalpy value calculation-based unit heat supply steam extraction flow measuring method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102000482A (en) * | 2010-11-15 | 2011-04-06 | 无锡科立泰科技有限公司 | System and method for controlling oxynitride removal |
| JP2011094572A (en) * | 2009-10-30 | 2011-05-12 | Mitsubishi Heavy Ind Ltd | Nox cleaning device for internal combustion engine |
| CN103574581A (en) * | 2013-11-15 | 2014-02-12 | 神华集团有限责任公司 | Thermal power generating unit NOx combustion optimization method and system |
| CN104793652A (en) * | 2015-04-21 | 2015-07-22 | 中电投河南电力有限公司技术信息中心 | Load dispatch curve based ammonia injection quantity adjustment method and system |
| CN104801180A (en) * | 2015-04-21 | 2015-07-29 | 中电投河南电力有限公司技术信息中心 | Ammonia spraying amount control method and system |
-
2015
- 2015-07-30 CN CN201510459723.2A patent/CN105892504B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011094572A (en) * | 2009-10-30 | 2011-05-12 | Mitsubishi Heavy Ind Ltd | Nox cleaning device for internal combustion engine |
| CN102000482A (en) * | 2010-11-15 | 2011-04-06 | 无锡科立泰科技有限公司 | System and method for controlling oxynitride removal |
| CN103574581A (en) * | 2013-11-15 | 2014-02-12 | 神华集团有限责任公司 | Thermal power generating unit NOx combustion optimization method and system |
| CN104793652A (en) * | 2015-04-21 | 2015-07-22 | 中电投河南电力有限公司技术信息中心 | Load dispatch curve based ammonia injection quantity adjustment method and system |
| CN104801180A (en) * | 2015-04-21 | 2015-07-29 | 中电投河南电力有限公司技术信息中心 | Ammonia spraying amount control method and system |
Non-Patent Citations (1)
| Title |
|---|
| 毛奕升: "烟气脱硝喷氨自动控制回路的优化", 《HUADIAN TECHNOLOGY》 * |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106215671A (en) * | 2016-09-09 | 2016-12-14 | 中国大唐集团科学技术研究院有限公司华中分公司 | A kind of thermal power plant denitration spray ammonia control method and device |
| CN106215671B (en) * | 2016-09-09 | 2018-10-16 | 中国大唐集团科学技术研究院有限公司华中分公司 | A kind of thermal power plant's denitration spray ammonia control method and device |
| CN106422709A (en) * | 2016-10-24 | 2017-02-22 | 大唐韩城第二发电有限责任公司 | Ammonia spraying regulation automatic control method for denitrification system of thermal power plant |
| CN107967003A (en) * | 2017-03-10 | 2018-04-27 | 邯郸学院 | For the SCR denitration Control Technique in circulating fluidized bed boiler |
| CN106731829A (en) * | 2017-03-31 | 2017-05-31 | 华北电力大学（保定） | Suppress control system and method for the purging on thermal power plant's discharged nitrous oxides influence |
| CN107561941A (en) * | 2017-09-01 | 2018-01-09 | 华北电力大学（保定） | A kind of full working scope qualified discharge control method of fired power generating unit denitrating system |
| CN107561941B (en) * | 2017-09-01 | 2021-06-29 | 华北电力大学（保定） | Full-working-condition standard-reaching emission control method for thermal power generating unit denitration system |
| CN107803114A (en) * | 2017-12-04 | 2018-03-16 | 烟台龙源电力技术股份有限公司 | A kind of denitration control system and its control method and control device |
| CN107803114B (en) * | 2017-12-04 | 2020-06-16 | 烟台龙源电力技术股份有限公司 | Denitration control system and control method and control device thereof |
| CN109343349A (en) * | 2018-11-01 | 2019-02-15 | 大唐环境产业集团股份有限公司 | A kind of SCR denitrating flue gas Optimal Control System and method based on ammonia spraying amount compensator |
| CN109343349B (en) * | 2018-11-01 | 2023-08-22 | 大唐环境产业集团股份有限公司 | SCR flue gas denitration optimal control system and method based on ammonia injection amount compensator |
| CN110501901A (en) * | 2019-07-08 | 2019-11-26 | 华能南京金陵发电有限公司 | The SCR spray ammonia required based on the accurate denitration of full load adjusts the method optimized |
| CN110501901B (en) * | 2019-07-08 | 2022-05-10 | 华能南京金陵发电有限公司 | SCR ammonia injection regulation optimization method based on full-load accurate denitration requirement |
| CN111895489A (en) * | 2020-06-17 | 2020-11-06 | 天津国电津能滨海热电有限公司 | Enthalpy value calculation-based unit heat supply steam extraction flow measuring method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105892504B (en) | 2018-08-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105892504B (en) | The control method and control system of a kind of thermal power plant's denitration for ammonia automatic loop | |
| CN106582284B (en) | The autocontrol method and system of fired power generating unit SCR denitration spray ammonia | |
| CN101842148B (en) | Adaptive control system for reagent distribution control in scr reactors | |
| CN104826492B (en) | Improvement method for selective catalytic reduction flue gas denitrification and ammonia injection control system | |
| CN104826493B (en) | A kind of control method of selective catalytic reduction flue gas denitrification system | |
| CN103752170B (en) | A kind of tangential firing pulverized-coal fired boiler SCR system denitration running optimizatin method | |
| CN106268239A (en) | The control method that the integration of thermal power plant's denitration control system separates | |
| CN105700570B (en) | SCR denitration control method for thermal power plant | |
| CN103268066B (en) | The optimization method that a kind of station boiler runs and device | |
| CN105045089A (en) | Boiler denitration control method based on outlet NOx content control and system thereof | |
| CN103831016B (en) | Denitrification operation optimization method of SCR (selective catalytic reduction) system of W flame boiler | |
| CN104801180A (en) | Ammonia spraying amount control method and system | |
| US9631776B2 (en) | Model-based controls for selective catalyst reduction systems | |
| CN107420874A (en) | A kind of ultra supercritical Coordinate Control of Fossil-fired Generating Sets | |
| CN110501901B (en) | SCR ammonia injection regulation optimization method based on full-load accurate denitration requirement | |
| CN102654776A (en) | Smoke denitration ammonia injection amount control method and device | |
| CN110263452A (en) | Flue gas Annual distribution characteristic analysis method, system and denitrating system in a kind of flue | |
| CN106292270B (en) | A kind of circulating fluidized bed boiler denitration automatic control device and its method | |
| CN105938375B (en) | A kind of flue gas SNCR denitration restores the control method of agent flux in the process | |
| CN104793652A (en) | Load dispatch curve based ammonia injection quantity adjustment method and system | |
| CN114307627B (en) | Denitration adjusting method based on theoretical ammonia consumption | |
| CN110479053A (en) | It is a kind of list pid loop add feed-forward regulation desulfurization for starch flow device and control method | |
| CN104147912A (en) | Flue-gas denitration method and device by mixing of selective non-catalytic reduction method SNCR and selective catalytic reduction method SCR | |
| CN103977705A (en) | Reducing agent metering for cement clinker production line SNCR flue gas denitration and control system and method thereof | |
| CN104678761A (en) | Total air volume advanced control-based denitration control method and system for thermal power unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |