CN105938375A - Control method of flow of reducing agent in flue gas SNCR denitration process - Google Patents
Control method of flow of reducing agent in flue gas SNCR denitration process Download PDFInfo
- Publication number
- CN105938375A CN105938375A CN201610377549.1A CN201610377549A CN105938375A CN 105938375 A CN105938375 A CN 105938375A CN 201610377549 A CN201610377549 A CN 201610377549A CN 105938375 A CN105938375 A CN 105938375A
- Authority
- CN
- China
- Prior art keywords
- nox
- reducing agent
- concentration
- flue gas
- control method
- 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
Classifications
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D11/00—Control of flow ratio
- G05D11/02—Controlling ratio of two or more flows of fluid or fluent material
- G05D11/13—Controlling ratio of two or more flows of fluid or fluent material characterised by the use of electric means
- G05D11/131—Controlling ratio of two or more flows of fluid or fluent material characterised by the use of electric means by measuring the values related to the quantity of the individual components
- G05D11/133—Controlling ratio of two or more flows of fluid or fluent material characterised by the use of electric means by measuring the values related to the quantity of the individual components with discontinuous action
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/79—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- General Physics & Mathematics (AREA)
- Automation & Control Theory (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a control method of a flow of a reducing agent in a flue gas SNCR denitration process. The reducing agent is sprayed into a flue gas, SNCR denitration is performed on the flue gas, and a nitrogen oxide in the flue gas is restored. The control method of the flow of the reducing agent in a denitration control system comprises the following steps: taking ammonia water as the reducing agent for example, a flue gas flow Q in a chimney and a nitrogen oxide concentration [NOx]2 in the chimney are acquired, and by use of a formula (1) shown in the descriptions, a reducing agent flow calculation value SV is calculated; and a determining formula is set according to the flow calculation value and an actually measured value, and through determining conditions, a denitration control system automatically adjusts an initial NOx concentration [NOx]1 and the reducing agent flow calculation value SV so as to enable the actually measured NOx concentration [NOx]2 to be continuously close to a target NOx concentration [NOx]3 and the actually measured flow of the reducing agent to be continuously close to a calculation flow.
Description
Technical field
The present invention relates to computational methods and the control technology of a kind of denitrification reducing agent; it is especially applicable to SNCR (the selective non-catalytic reduction of cement clinker production line, water-tube boiler, coal-burning boiler; SNCR) metering method of the reducing agent of denitrating flue gas, belongs to environmental conservation and Chemical Engineering automation control area.
Background technology
SNCR gas denitrifying technology refers under the effect without catalyst, reducing agent is sprayed in suitable temperature window, nitrogen oxides in flue gas is reduced to water and the nitrogen being safe from harm, is the most commonly used technology of utilization in domestic and international cement furnace, water-tube boiler, coal-fired plant flue gas denitration engineering.
Patent ZL2014 2 0199444.8 provides reductant metering and the control technology of a kind of cement clinker production line SNCR denitrating flue gas, this technology calculate basis be utilize clinker line kiln tail C1 level preheater outlet the oneth CEMS, the first ammonia table and kiln tail chimney the 2nd CEMS, the second ammonia table major parameter as input quantity, metering ammonia flow.Only configuring the 2nd CEMS and the data of the second ammonia table at kiln tail chimney compared to conventional, promptness and elegance being obtained for of metering are substantially improved.
But, current reality three problems of existence: first, owing to the suitable monitoring site operating mode of C1 level preheater outlet is severe: flue-gas temperature is up to 320-350 DEG C, and negative pressure is up to 100g/m up to-6kPa, dust3(coal-burning power plant 30g/m above3It is high dirt), a CEMS and the first ammonia table type selecting difficulty, cost height, the most all of grog line denitration engineering has configuration；Second, even if being configured with a CEMS and the first ammonia table, due to mount point position bad working environments, equipment failure rate is high, and table meter maintenance workload is big, is slightly not good at, and data use value is little；3rd, the enterprise of actual disposition SNCR denitration system, either clinker manufacturing enterprise, water-tube boiler, coal-burning power plant, regular situation is the most only configured with CEMS and ammonia table at kiln tail chimney.
nullIn a word，SNCR flue gas denitrification system is different from SCR flue gas denitrification system，Owing to there is no initial NOx concentration before denitrating system，Can only be according to the Gas Parameters of kiln tail chimney as payment foundation，And patent ZL2014 2 0199444.8 have employed the initial concentration of supposition for calculating ammonia flow，One is set，Do not rechange，In actual motion，Variation and the persistence of the time of operation due to operating mode，The change of operating mode and combustion raw material causes initial NOx concentration to be to be continually changing in fact，Although patent ZL2014 2 0199444.8 is by K1 temperature corrected parameter、K2 the escaping of ammonia corrected parameter、K3 is automatically generated (E/F) by the ratio valve system of theoretical denitration rate and actual denitration rate and is adjusted，These fine setting parametrical faces are to there is the problem adjusted not in time when fluctuating widely.
Additionally, for indivedual initial NOx concentration far beyond scope of design (higher than 1000mg/m3Or less than 300mg/m3) time, owing to regulation valve does not operates in optimal open range, history curve is caused to occur abnormal: such as: after denitration, NOx emission concentration is still above actual ammonia flow already below target setting value, the ammonia flow of calculating, illustrates that original corrected parameter is unsatisfactory for extreme operating condition condition.
It is necessary to find new computational methods, to ensure that denitrating system can cover the various operating modes being likely to occur with gamut.
Summary of the invention
The present invention provides the control method of reducing agent flow during a kind of flue gas SNCR denitration, surveys NOx concentration after controlling denitration infinitely while target NOx value convergence, and actual ammonia aqua stream flux is infinitely to calculated value convergence.
During a kind of flue gas SNCR denitration, the control method of reducing agent flow, sprays into amino reductive in flue gas, and flue gas carries out SNCR denitration, the nitrogen oxides in reduction flue gas, and in denitration control system, the control method of reducing agent flow includes:
As a example by reducing agent is as ammonia, gathers in chimney nitrous oxides concentration in flue gas flow Q and chimney and (be [NOx] 1 before denitration, be [NOx] after spraying ammonia2), utilize formula (1) to be calculated reducing agent flow rate calculation value SV:
Wherein:
SV: ammonia flow rate calculation value (units/kg/h)；
PV: ammonia flow measured value (units/kg/h), can be read by the ammonia aqua stream gauge within denitration switch board, coordinate flow control valve, control actual ammonia aqua stream flux infinitely to value of calculation convergence；
Q: kiln tail chimney smoke flow (unit Nm3/h)；
[NOx]1: initial NOx concentration (unit mg/Nm3), it being manually entered, system default is 800mg/m3, it is possible to according to practical condition at 400-1200mg/m3In the range of any assignment.
[NOx]2: actual measurement NOx concentration (unit mg/Nm3), signal takes from kiln tail chimney CEMS, denitrating system put into operation after value, survey as NO, actual measurement NOx concentration [NOx]2For surveying NO conversion for NO under the dry state of mark2At 10%O2Data under content.
[NOx]3: target NOx controlled concentration (unit mg/Nm3), artificially input；According to " cement industry atmosphere pollutants emission standards " (GB4915-2013): if environmental protection regulatory requirements controls NOx emission concentration 320mg/Nm3Hereinafter, it is usually arranged as 220～300mg/Nm according to debugging situation3If environmental protection regulatory requirements controls NOx emission concentration 400mg/Nm3Hereinafter, it is usually arranged as 300～380mg/Nm according to debugging situation3；According to " emission standard of air pollutants for boilers " (GB13271-2013), setting value 20-100mg/m less than effluent standard limit value3, it is adaptable to clinker line denitration engineering and coal-burning boiler denitration engineering.
C: ammonia mass concentration (wt%), is manually entered according to entering factory's ammonia concn, concentration 15-25wt%；
NSR: ammonia nitrogen mol ratio；According to target denitration rate ηTargetSystem automatically generates:
Reducing agent flow rate calculation value SV is substituted into and judges formula as follows:
Wherein, PV: ammonia flow measured value, units/kg/h；
By decision condition, denitration control system adjusts initial NOx concentration [NOx] automatically1, reducing agent flow rate calculation value SV is adjusted, allows and survey NOx concentration [NOx]2Constantly convergence target NOx concentration [NOx]3, reducing agent measured discharge constantly levels off to calculated flow rate.
The parameter being manually set is needed to have: initial NOx concentration [NOx]1,[NOx]1Adjustment increment Delta, target NOx setting value [NOx]3, it is both placed on man-machine exchange operation interface.
The present invention is by actual measurement NOx concentration and the contrast of target NOx concentration and calculates ammonia demand and the contrast of actual measurement ammonia usage amount, is jointly provided with four kinds of operating modes, under the conditions of nominal situation, automatically adjusts according to computing formula ammonia vol；When operating condition fluctuation or beyond when designing category (being characterized primarily by exhaust gas volumn and NOx concentration), then there will be and be judged to exception, system is according to the initial NOx concentration increment given, adjust initial NOx concentration, and iteration can not be stopped, until judge that operating mode, as normal, surveyed NOx concentration and fluctuated with target NOx concentration, ammonia actual amount continues convergence with calculating consumption, to dynamic equilibrium.
Each supposition operating mode is described as follows:
Operating mode one: actual measurement NOx concentration is < during target NOx concentration, system is in running status up to standard, ammonia demand (value of calculation) reduces, the calculated flow rate that system is obtained by formula (1) should be less than measured discharge, when measured discharge is drawn close to calculated flow rate, actual motion reduces the consumption of reducing agent, saves operating cost.If there is value of calculation on the contrary more than measured value, the initial NOx concentration that explanation system set originally is bigger than normal, and therefore, system automatically adjusts initial NOx concentration and reduces, and makes reducing agent calculated flow rate decline.This judges and the meeting of calculating ceaselessly iteration, until being judged to nominal situation, initial NOx then keeps dynamic stability, the measured discharge of system call interception reducing agent and calculated flow rate infinite tendency, and whole system keeps dynamic stability.
Operating mode two: during actual measurement NOx concentration ＜ target NOx concentration, system is in running status up to standard, and the calculated flow rate SV that system is obtained by formula (1) should be less than measured discharge PV, so operating mode two is nominal situation.When measured discharge is drawn close to calculated flow rate, actual motion reduces the consumption of reducing agent, save operating cost.
Operating mode three: during actual measurement NOx concentration ＞ target NOx concentration, system is it is possible that exceed standard, now, ammonia demand (value of calculation) increases in theory, the calculated flow rate SV that system is obtained by formula (1) should be more than measured discharge PV, when measured discharge is drawn close to calculated flow rate, increase the consumption of reducing agent, it is ensured that operation up to standard.If occurring value of calculation SV ＜ measured value PV on the contrary in actual motion, the initial NOx concentration that explanation system set originally is less than normal, and now, by above-mentioned decision condition, system automatically adjusts initial NOx concentration and raises, and makes reducing agent calculated flow rate raise.Decision process and initial NOx concentration assignment procedure can ceaselessly iteration, until being judged to nominal situation, initial NOx then keeps dynamic stability, the measured discharge of system call interception reducing agent and calculated flow rate infinite tendency, and whole system keeps dynamic stability.
Operating mode four: during actual measurement NOx concentration ＞ target NOx concentration, system is it is possible that exceed standard, now, ammonia demand (value of calculation) increases in theory, the calculated flow rate SV that system is obtained by formula (1) should ＞ measured discharge PV, when measured discharge is drawn close to calculated flow rate, increase the consumption of reducing agent, it is ensured that operation up to standard.If actual motion coincide, initial NOx concentration keeps initial value, does not changes, and system keeps dynamic equilibrium.
The method application process of the present invention need the parameter being manually entered to have: NOx initial concentration, NOx target discharge concentration and NOx initial concentration increments of change, input authority opens to user on main operation interface, system gives initial value according to design parameter debugging situation, and user the most artificially can adjust according to practical operation situation.
Initial NOx concentration automatically adjusts increment and is defaulted as 20mg/m3, at 10-50mg/m3In the range of adjustable, authority opening to user, arrange value bigger time, adjustment amplitude is big, response is fast, but may result in frequently adjustment, and system stability is the best, arrange value less time, it is little that initial NOx concentration adjusts amplitude automatically, low-response, and system sensitivity is not good enough, cement production enterprise or station boiler enterprise can be adjusted according to the production status load fluctuation situation of oneself, it is proposed that setting value is 10mg/m3、20mg/m3、30mg/m3、40mg/m3、50mg/m3, it is not recommended that setting excessive, otherwise system stability is the best.As preferably, it is proposed that increment is set to 20-30mg/m3。
Initial NOx can obtain denitrating system is out of service when, and denitrating system then cannot obtain after putting into operation, and typically can no longer be adjusted by meansigma methods during being defaulted as design load or debugging, automatically adjusted after being judged by system condition after setting.
Target NOx concentration is due to the fluctuation of system loading, actual measurement NOx concentration should be run in the fluctuation of surrounding target NOx concentration, for ensureing the reliable and stable operation up to standard of denitrating system, the maximum of actual measurement NOx concentration is necessarily less than standard limited value discharge standard, therefore, it is less than standard NOx emission concentration limit that general recommendations arranges target NOx concentration, default setting value 30mg/m less than standard value3, typically less 20-100mg/m than standard value3In the range of adjustable.
Described reducing agent is ammonia or carbamide, illustrates in the present invention as a example by ammonia.
SNCR gas denitrifying technology is different from SCR denitration; its initial NOx emission concentration then cannot characterize after denitrating system puts into operation; initial NOx concentration is associated with dore furnace/index such as furnace exit temperature, clinker; anticipation adjustment is carried out by corrected parameter; run relatively stable when steady load; but when load fluctuation is relatively big or beyond scope of design, due to less than normal to the correction amplitude of initial NOx concentration, usually there will be control malfunctioning.
The computational methods of the SNCR denitrating flue gas reducing agent consumption that the present invention provides and control technology, ammonia theory demands amount SV is tried to achieve by computing formula listed by the present invention, compare with denitration control system actual measurement ammonia flow PV, joint objective NOx concentration and the comparison of actual measurement NOx concentration, operating mode is judged, adjusts reducing agent flow, and realize when adapting to operating mode substantial deviation design load initial NOx concentration is constantly modified.
In the present invention, all Gas Parameters all deliver to denitration control system, for realizing automatically controlling, the computing formula of reducing agent flow rate calculation value SV of the present invention and judgement formula are enrolled original denitration control system, according to computing formula (1) and judgement formula, by the aperture of denitration control system regulation reducing agent flow valve, to adjust the measured discharge infinite tendency value of calculation of reducing agent.
The present invention calculates and is mainly used in clinker line denitration engineering and coal-burning boiler denitration engineering with modification method.
When being applied to clinker line denitration engineering, can solve described in technical background C1 level outlet be not provided with CEMS, correction factor can not meet too low or too high initial NOx concentration for the correction amplitude of initial NOx emission concentration, by arranging decision condition, initial NOx emission concentration is allowed constantly to adjust according to operating mode, generate new initial NOx emission concentration and as input parameter, for ensureing the stability of denitrating system, the amplitude of adjustment and the frequency are also crucial, are a kind of brand-new computational methods.When being applied to coal-burning boiler denitration engineering, without too much temperature parameter, it is only necessary to basic chimney CEMS data, and the effusion meter of denitrating system reduction assignment subsystem configuration, regulation valve, metering and the adjustment of reducing agent is realized by PID calculating and comparing.
The present invention solve the initial NOx concentration of SNCR denitration control system can not value in real time, the technological gap that load fluctuation is big or super scope of design unusual service condition regulation is malfunctioning.Compared with existing apparatus, the invention have the advantages that:
(1) judge that the abnormal conditions in formula illustrate that the primary operating parameter of denitrating system is far beyond design category (initial NOx concentration is excessive or too small), cause system regulation malfunctioning, by judging and adjusting, denitration control system is made to remain to Effective Regulation reducing agent consumption after beyond design category；
(2) conventionally calculation formula is by temperature, CO, clinker (or boiler load) etc. includes computing formula in, as auxiliary control parameter, but in part of cement factory or power plant, these auxiliary control parameters are inconspicuous with the dependency of initial NOx concentration, particularly during reciprocal action, leading regulation and control parameter is not easy to distinguish, above-mentioned parameter is no longer included in the correction factor as computing formula by the present invention, but directly by true measurable NOx actual discharge concentration and NOx goal setting concentration, reducing agent calculated flow rate and reducing agent actual flow are compared, if after finding that control is malfunctioning, adjust initial NOx concentration, the continuous iteration of process judged and adjust, until regulation and control are in dynamic equilibrium, decrease uncertain factor；
(3) about setting and the difficult point of tracking always SNCR denitrating flue gas, the present invention setting by decision condition of initial NOx concentration, solve the drawback that the set-point of immesurable initial NOx concentration is fixing, allow system be in dynamic equilibrium all the time.
(4) computing formula no longer includes the parameters such as temperature, CO, clinker (or boiler load) in, and instrument arrangement can simplify, hardware fault rate can reduce, and controls malfunctioning situation and have also been obtained effectively solution.
Accompanying drawing explanation
Fig. 1 is cement clinker production line SNCR denitration reducing agent control system hardcore distribution of facilities figure.
Fig. 2 is coal-burning boiler SNCR denitration reducing agent control system hardcore distribution of facilities figure.
Fig. 3 is SNCR denitration reducing agent control system composition schematic diagram in Fig. 1 and Fig. 2.
Fig. 4 is the abnormal conditions figure occurred according to original computing formula in embodiment 1.
Reference shown in figure is:
1-reductant metering and control system 2-reducing agent dispensing cabinet 3-Pt100 temperature probe
4-dore furnace 5-CO analyser 6-conditioning Tower
7-waste heat boiler 8-electric cleaner 9-raw mill
10-chimney the escaping of ammonia analyser 11-chimney CEMS analyser 12-chimney the escaping of ammonia is popped one's head in
13-chimney CEMS pops one's head in 14-kiln tail chimney 15-boiler
16-economizer 17-SCR reactor 18-air preheater
19-cleaner unit 20-desulfurizing tower
Detailed description of the invention
The present invention is further illustrated with embodiment below in conjunction with the accompanying drawings.
[embodiment one]
As shown in Figure 1, specification is the SNCR denitration reductant metering system of daily output 5000t clinker production line dore furnace, uses ammonia as reducing agent.Dore furnace is provided with Pt100 temperature probe, the outlet of C1 level preheater is provided with CO analyser, and signal delivers to denitrating system, and its denitration control system composition diagram is as shown in Figure 3.
Before denitrification apparatus is built, for environmental protection regulatory requirements, being provided with chimney CEMS, fume indication has: flue gas flow, NOx, SO2, dust, temperature, humidity, O2.When carrying out the transformation of SNCR denitrating flue gas, the same layer add chimney the escaping of ammonia detector of chimney CEMS sampling probe, all Gas Parameters all deliver to denitration control system.
Ammonia volume input data has: the flue gas flow (425681Nm of chimney CEMS3/ h), NOx initial concentration owner be manually entered according to design parameter and debugging situation that (it is 550mg/Nm that system gives default value3)；After being manually entered denitration, target NOx controlled concentration (is implemented ground and is performed " the new standard of cement industry air pollution emission (GB4915-2013) " emission limit standard, NOx emission concentration limit 400mg/m3, manually arranging target NOx emission concentration is 370mg/Nm3。
According to original computing formula, in fact it could happen that the abnormal conditions shown in Fig. 4, target NOx concentration is set as 370mg/m3, actual measurement NOx is 257.4370mg/m3, actual measurement ammonia vol SV is 197.4370L/h, and ammonia amount of calculation is 216.8L/h, according to logic, surveys NOx concentration ＜ target NOx concentration, and amount of calculation SV of ammonia should be less than measured value PV, coincide with the unusual condition of operating mode one.Its reason essentially consists in: initial NOx concentration does not rechanges once input, after stopping denitrating system, finds that initial NOx concentration is at 360-580mg/m3, it is far smaller than initial NOx concentration 800mg/m of design3With initial NOx concentration 650mg/m set3, to such an extent as to after actual measurement NOx concentration is already less than target NOx concentration, ammonia theory demands amount SV that system-computed goes out is on the contrary more than measured discharge, to such an extent as to system down.
After using the computational methods of the present invention, the initial NOx concentration increment of artificial input is 25mg/m3, by the decision condition that computational methods are attached, initial NOx concentration constantly adjusts, until being reduced to 480mg/m3Time, value of calculation SV ＜ measured value PV, valve opening reduces, and resumed controlling is normal, it is to avoid the invalid of ammonia adds.
Nominal situation is the most, then not illustrate.
[embodiment two]
As shown in Figure 2, specification is the SNCR denitration reductant metering system of the CFBB (CFB) of 130 ton hour, uses ammonia as reducing agent.Being provided with Pt100 temperature probe and CO analyser at burner hearth economizer, signal delivers to denitrating system, and its denitration control system composition diagram is as shown in Figure 3.
Before denitrification apparatus is built, for environmental protection regulatory requirements, being provided with chimney CEMS, fume indication has: flue gas flow, NOx, SO2, dust, temperature, humidity, O2.After carrying out SNCR denitrating flue gas transformation, the same layer add chimney the escaping of ammonia detector of chimney CEMS sampling probe, all Gas Parameters all deliver to denitration control system.
Ammonia volume input data has: the flue gas flow (165681Nm of chimney CEMS3/ h), NOx initial concentration owner is rule of thumb manually entered and (is defaulted as 250mg/Nm3)；After being manually entered denitration, target NOx controlled concentration (is implemented ground and is performed " the new standard of thermal power plant's air pollution emission (GB13223-2011) " emission limit standard, NOx emission concentration limit 100mg/m especially3, manually arranging target NOx emission concentration is 80mg/Nm3, thus can calculate theoretical denitration rate is 68%, and control system will automatically generate the NSR=1.8 of correspondence, and system can effectively realize ammonia Flow-rate adjustment and the change of initial NOx concentration.
The foregoing is only the case that is embodied as of patent of the present invention, but the technical characteristic of patent of the present invention is not limited thereto, any those skilled in the relevant art are in the field of the invention, and change or the modification made all are contained among the scope of the claims of the present invention.
Claims (9)
1. a control method for reducing agent flow during flue gas SNCR denitration, sprays in flue gas
Enter reducing agent, flue gas carried out SNCR denitration, the nitrogen oxides in reduction flue gas, it is characterised in that
Reducing agent flow rate calculation value SV is:
Wherein:
SV: reducing agent flow rate calculation value, units/kg/h；
Q: flue gas flow in kiln tail chimney, unit Nm3/h；
[NOx]1: initial NOx concentration, unit mg/Nm3；
[NOx]2: actual measurement NOx concentration, unit mg/Nm in kiln tail chimney3。
[NOx]3: target NOx controlled concentration, unit mg/Nm3；
C: reducing agent mass concentration, wt%；
NSR: ammonia nitrogen mol ratio；Reducing agent flow rate calculation value SV is substituted into and judges formula as follows:
Wherein, PV: reducing agent flow measured value, units/kg/h；
By decision condition, adjust initial NOx concentration [NOx]1, to reducing agent flow rate calculation value SV
It is adjusted, allows and survey NOx concentration [NOx] after denitration2Constantly convergence target NOx concentration [NOx]3,
Reducing agent measured discharge PV constantly levels off to calculated flow rate SV.
2. control method as claimed in claim 1, it is characterised in that described initial NOx concentration
[NOx]1For 400-1200mg/m3。
Control method the most according to claim 1, it is characterised in that judge [NOx] in formula1
Increment Delta is set as 10mg/m3～50mg/m3。
Control method the most according to claim 1, it is characterised in that judge [NOx] in formula1
Increment Delta is set as 10mg/m3、20mg/m3、30mg/m3、40mg/m3、50mg/m3。
Control method the most according to claim 1, it is characterised in that described reducing agent is ammonia
Or carbamide, reductant concentration 15-25wt%.
Control method the most according to claim 1, it is characterised in that described target NOx controls
Concentration [NOx]320-100mg//m is limited less than industry discharge3。
Control method the most according to claim 1, it is characterised in that described actual measurement NOx concentration
[NOx]2For surveying NO conversion for NO under the dry state of mark2At 10%O2Data under content.
8. control method application in clinker line denitration engineering as claimed in claim 1.
9. control method application in coal-burning boiler denitration engineering as claimed in claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610377549.1A CN105938375B (en) | 2016-05-31 | 2016-05-31 | A kind of flue gas SNCR denitration restores the control method of agent flux in the process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610377549.1A CN105938375B (en) | 2016-05-31 | 2016-05-31 | A kind of flue gas SNCR denitration restores the control method of agent flux in the process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105938375A true CN105938375A (en) | 2016-09-14 |
| CN105938375B CN105938375B (en) | 2018-12-11 |
Family
ID=57151640
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610377549.1A Active CN105938375B (en) | 2016-05-31 | 2016-05-31 | A kind of flue gas SNCR denitration restores the control method of agent flux in the process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105938375B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109806913A (en) * | 2019-03-12 | 2019-05-28 | 上海三融环保工程有限公司 | A kind of denitrating catalyst and preparation method thereof applied to cement plant |
| CN110180347A (en) * | 2019-05-31 | 2019-08-30 | 芜湖富春染织股份有限公司 | A kind of denitration of boiler smoke method |
| CN110652856A (en) * | 2019-08-26 | 2020-01-07 | 光大环保技术研究院（南京）有限公司 | SNCR control system based on model |
| CN111135683A (en) * | 2020-02-27 | 2020-05-12 | 上海三融环保工程有限公司 | SNCR (selective non-catalytic reduction) out-of-stock automatic control method and system |
| CN111974212A (en) * | 2020-09-19 | 2020-11-24 | 北京首钢国际工程技术有限公司 | Flue gas denitration system of air gas preheating steel rolling heating furnace |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977705A (en) * | 2014-04-23 | 2014-08-13 | 浙江省环境保护科学设计研究院 | Reducing agent metering for cement clinker production line SNCR flue gas denitration and control system and method thereof |
| CN104809341A (en) * | 2015-04-23 | 2015-07-29 | 西安西热电站信息技术有限公司 | Method for calculating reducing agent flow of SCR (Selective Catalytic Reduction) denitrification system in real time |
-
2016
- 2016-05-31 CN CN201610377549.1A patent/CN105938375B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977705A (en) * | 2014-04-23 | 2014-08-13 | 浙江省环境保护科学设计研究院 | Reducing agent metering for cement clinker production line SNCR flue gas denitration and control system and method thereof |
| CN104809341A (en) * | 2015-04-23 | 2015-07-29 | 西安西热电站信息技术有限公司 | Method for calculating reducing agent flow of SCR (Selective Catalytic Reduction) denitrification system in real time |
Non-Patent Citations (5)
| Title |
|---|
| HOSSAIN K A ET AL.: "Application of selective non-catalytic reduction of NOx in small-scale combustion systems", 《ATMOSPHERIC ENVIRONMENT》 * |
| 周荣等: "水泥窑炉SNCR烟气脱硝技术的工程应用分析", 《水泥》 * |
| 周荣等: "水泥窑炉SNCR脱硝工程优化设计的探讨", 《水泥》 * |
| 王凡等: "我国工业烟气SCR_SNCR脱硝技术与还原剂用量平衡", 《环境工程技术学报》 * |
| 贾瑞文等: "SNCR脱硝***模块控制原理及控制方法", 《四川建材》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109806913A (en) * | 2019-03-12 | 2019-05-28 | 上海三融环保工程有限公司 | A kind of denitrating catalyst and preparation method thereof applied to cement plant |
| CN109806913B (en) * | 2019-03-12 | 2022-05-31 | 南京信融环保新材料有限公司 | Denitration catalyst applied to cement plant and preparation method thereof |
| CN110180347A (en) * | 2019-05-31 | 2019-08-30 | 芜湖富春染织股份有限公司 | A kind of denitration of boiler smoke method |
| CN110652856A (en) * | 2019-08-26 | 2020-01-07 | 光大环保技术研究院（南京）有限公司 | SNCR control system based on model |
| CN110652856B (en) * | 2019-08-26 | 2022-07-22 | 光大环保技术研究院（南京）有限公司 | SNCR control system based on model |
| CN111135683A (en) * | 2020-02-27 | 2020-05-12 | 上海三融环保工程有限公司 | SNCR (selective non-catalytic reduction) out-of-stock automatic control method and system |
| CN111974212A (en) * | 2020-09-19 | 2020-11-24 | 北京首钢国际工程技术有限公司 | Flue gas denitration system of air gas preheating steel rolling heating furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105938375B (en) | 2018-12-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105938375A (en) | Control method of flow of reducing agent in flue gas SNCR denitration process | |
| CN108380043B (en) | Selective ammonia injection regulation control method for SCR (Selective catalytic reduction) denitration device | |
| CN107561941B (en) | Full-working-condition standard-reaching emission control method for thermal power generating unit denitration system | |
| CN105797576B (en) | Denitration ammonia injection control method for coal-fired unit | |
| US5286458A (en) | Injection type non-catalyst denitrogen oxide process control system | |
| CN105148727B (en) | Thermal generation unit denitration optimal control method and system | |
| CN103752170B (en) | A kind of tangential firing pulverized-coal fired boiler SCR system denitration running optimizatin method | |
| CN105920997B (en) | A kind of coal-burning boiler denitrating system that burnout degree is coupled with SNCR and method | |
| CN108664006A (en) | It is a kind of that ammonia optimization method and system are intelligently sprayed based on the SCR denitration of zonal control and Dynamic matrix control | |
| CN109092035A (en) | A kind of device and its working method for adjusting denitration spray ammonia flow adding feedforward based on cascade PID | |
| CN103831016B (en) | Denitrification operation optimization method of SCR (selective catalytic reduction) system of W flame boiler | |
| CN113266843B (en) | Combustion optimization method, system and device for coal-fired boiler | |
| CN110501901B (en) | SCR ammonia injection regulation optimization method based on full-load accurate denitration requirement | |
| CN103759277A (en) | Intelligent soot blowing closed-loop control method, device and system for coal-fired power station boiler | |
| US8783013B2 (en) | Feedforward selective catalytic reduction system for turbine engines | |
| CN112569785A (en) | SCR ammonia injection control system and method based on ammonia escape monitoring | |
| CN209020167U (en) | A kind of device for adjusting denitration spray ammonia flow adding feedforward based on cascade PID | |
| CN103977705A (en) | Reducing agent metering for cement clinker production line SNCR flue gas denitration and control system and method thereof | |
| CN110038426A (en) | A kind of frequency modulation type is intelligent to control ammonia system and method | |
| CN110479061A (en) | SNCR control system and method based on fire box temperature field information | |
| CN108816043A (en) | A kind of denitration device and its autocontrol method | |
| CN114307627B (en) | Denitration adjusting method based on theoretical ammonia consumption | |
| CN214635434U (en) | SCR ammonia injection control system based on ammonia escape monitoring | |
| CN206045790U (en) | A kind of low-nitrogen discharged three-stage control system of coal unit | |
| JPH0263524A (en) | Method for controlling amount of nh3 to be injected into exhaust gas denitrification device |
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 | ||
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 310007 No. 109 Tianmu Mountain Road, Hangzhou, Zhejiang, Xihu District Co-patentee after: ZHEJIANG HUANKE ENVIRONMENT TECHNOLOGY CO.,LTD. Patentee after: Zhejiang Institute of ecological environmental science design and research Address before: 310007 No. 109 Tianmu Mountain Road, Hangzhou, Zhejiang, Xihu District Co-patentee before: ZHEJIANG HUANKE ENVIRONMENT TECHNOLOGY Co.,Ltd. Patentee before: ENVIRONMENTAL RESEARCH AND DESIGN INSTITUTE OF ZHEJIANG PROVINCE |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200820 Address after: 310007 No. 109 Tianmu Mountain Road, Hangzhou, Zhejiang, Xihu District Co-patentee after: ZHEJIANG HUANKE ENVIRONMENT RESEARCH INSTITUTE Co.,Ltd. Patentee after: Zhejiang Institute of ecological environmental science design and research Address before: 310007 No. 109 Tianmu Mountain Road, Hangzhou, Zhejiang, Xihu District Co-patentee before: ZHEJIANG HUANKE ENVIRONMENT TECHNOLOGY Co.,Ltd. Patentee before: Zhejiang Institute of ecological environmental science design and research |