CN103034208B - Thermal generation unit denitration electricity price method for supervising - Google Patents
Thermal generation unit denitration electricity price method for supervising Download PDFInfo
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- 230000005611 electricity Effects 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000003546 flue gas Substances 0.000 claims abstract description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 36
- 229910021529 ammonia Inorganic materials 0.000 claims description 18
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 17
- 239000004202 carbamide Substances 0.000 claims description 17
- 238000005259 measurement Methods 0.000 claims description 16
- 230000002829 reductive effect Effects 0.000 claims description 16
- 238000010790 dilution Methods 0.000 claims description 15
- 239000012895 dilution Substances 0.000 claims description 15
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000000197 pyrolysis Methods 0.000 claims description 8
- 238000013461 design Methods 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 4
- 230000004143 urea cycle Effects 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 2
- 230000003068 static effect Effects 0.000 claims description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 9
- 238000004458 analytical method Methods 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000011835 investigation Methods 0.000 description 5
- 230000002146 bilateral effect Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical class [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910001369 Brass Inorganic materials 0.000 description 1
- 241001269238 Data Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000010951 brass Substances 0.000 description 1
- 238000000738 capillary electrophoresis-mass spectrometry Methods 0.000 description 1
- 238000007405 data analysis Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000001595 flow curve Methods 0.000 description 1
- 238000004868 gas analysis Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Abstract
The invention discloses a kind of Thermal generation unit denitration electricity price method for supervising, comprise the following steps: 1) calculate denitrification apparatus operational percentage, denitrification apparatus operational percentage is within the scope of assessment period, denitrating flue gas facility puts into operation the number percent of time divided by the assessment period time, described assessment period is exert oneself after genset starts to reach 50% of nominal output and start to drop to exerting oneself before unit trip time period 50% of nominal output, and the denitrating flue gas facility time of putting into operation is the difference of denitrating system start-up time and idle time; 2) denitration electricity price is calculated: M=T × P
e× (1-e) × a.The phenomenon that the present invention effectively prevent the denitration facility that not put into operation while electricity power enterprise enjoys denitration electricity price occurs.
Description
Technical field
The present invention relates to a kind of Thermal generation unit denitration electricity price method for supervising, realize, to effective management of coal unit denitration facility operation, belonging to automatic control technology of power system field.
Background technology
Denitrating flue gas is one of effective measures controlling power plant's discharged nitrous oxides, and at present, large coal-fired power plant all requires to install denitrification apparatus, and must install CEMS, monitors pollutants such as flue gas NOxes before and after denitration.Owing to not yet realizing at present the real-time monitoring run denitrification apparatus, even if cause occurring that part generate electricity enterprise has installed the phenomenon that denitrification apparatus also may not put into operation and occurred, do not play should have effect to effectively controlling oxides of nitrogen.
At present, domesticly see the research had denitration electricity price, but be all confined to put into operation the research that denitration facility causes cost of electricity-generating to increase to electricity power enterprise, do not relate on the basis of denitration electricity price, the examination of denitration electricity price is carried out to electricity power enterprise, this model is monitored and information management system in real time based on the coal unit denitrating flue gas developed, with chimney inlet nitrogen oxides concentration, nitrous oxides concentration is imported and exported in denitration, blower fan/pump electric current, the monitoring parameters such as reductive agent flow are analysis factor, to denitrating system operational percentage, denitration efficiency, the indexs such as concentration of emission are carried out adding up and are analyzed, establish perfect denitration electricity price examining model, implement supervision for related governmental departments and provide practicable technical measures, the phenomenon that effectively prevent the denitration facility that not put into operation while electricity power enterprise enjoys denitration electricity price occurs.
Summary of the invention
Technical matters to be solved by this invention is for rational, practicable method for supervising is formulated in the enforcement of denitration electricity price, preventing do not put into operation while the enjoying denitration electricity price phenomenon of denitration facility of electricity power enterprise from occurring, providing technical support for implementing supervision and management.
For solving the problems of the technologies described above, the invention provides a kind of Thermal generation unit denitration electricity price method for supervising, it is characterized in that, comprise the following steps:
1) denitrification apparatus operational percentage is calculated: denitrification apparatus operational percentage is within the scope of assessment period, denitrating flue gas facility puts into operation the number percent of time divided by the assessment period time, described assessment period is exert oneself after genset starts to reach 50% of nominal output and start to drop to exerting oneself before unit trip time period specified 50%, the denitrating flue gas facility time of putting into operation is the difference of denitrating system start-up time and idle time
The criterion of denitrating system start-up time is:
11) for SCR(Select Catalytic Reduction, selective catalytic reduction) mode:
During using liquefied ammonia as reductive agent, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the 100mg/m of concentration
3;
Little hourly value >=the lower threshold of arbitrary dilution air electric current (lower limit is 5A);
(lower limit is 5kg/h (7.1m to the little hourly value>=lower threshold of arbitrary side spray ammonia flow
3/ h));
The little hourly value of unit denitration efficiency (the getting both sides mean value of bilateral denitrification apparatus) >=50%;
During urea pyrolysis technique, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the 100mg/m of concentration
3;
40% of the little hourly value of urea pyrolysis electric heater running current >=specified;
Little hourly value >=the lower threshold of urea cycle pump motor current (lower limit is 5A);
The little hourly value of unit denitration efficiency (the getting both sides mean value of bilateral denitrification apparatus) >=50%;
12) for SNCR(Select Non-catalytic Reduction, SNCR method) mode, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the design load of concentration;
Arbitrary dilution water pump operation signal=1;
(lower limit is 5kg/h (0.01m to arbitrary region urea flow hour average>=lower threshold
3/ h));
13) for Circulating Fluidized Bed Boiler, meet following condition simultaneously:
Install equipment for denitrifying flue gas additional;
Little hourly value≤the 200mg/m of chimney inlet NOx concentration
3;
Denitrating system stoppage in transit signal criterion is:
For SCR(Select Catalytic Reduction, selective catalytic reduction) mode:
When liquefied ammonia is as reductive agent, meet one of following condition:
Chimney entrance NO
xconcentration little hourly value > 100mg/m
3;
All dilution air electric currents little hourly value < lower threshold (lower limit is 5A);
(lower limit is 5kg/h (7.1m to two side spray ammonia flows little hourly value < lower threshold
3/ h));
The little hourly value of unit denitration efficiency (the getting both sides mean value of bilateral denitrification apparatus) < 50%;
Urea pyrolysis technique, meets one of following condition:
Chimney entrance NO
xconcentration little hourly value > 100mg/m
3;
Urea pyrolysis electric heater running current little hourly value < specified 40%;
Urea cycle pump motor current little hourly value < lower threshold (lower limit is 5A);
The little hourly value of unit denitration efficiency (the getting both sides mean value of bilateral denitrification apparatus) < 50%;
With SNCR(Select Non-catalytic Reduction, SNCR method) mode time, meet one of following condition:
Chimney entrance NO
xconcentration little hourly value > design load;
All dilution water pump operation signal=0;
(lower limit is 5kg/h (0.01m to all regions urea flow hour average < lower threshold
3/ h));
For Circulating Fluidized Bed Boiler: install equipment for denitrifying flue gas additional and chimney inlet nitrogen oxides concentration little hourly value > 200mg/m
3;
2) denitration efficiency is calculated:
For SCR(Select Catalytic Reduction, selective catalytic reduction) mode: get the NO after denitrification apparatus import and exiting flue gas analytic system measurement conversion
xconcentration (coal-burning boiler excess air coefficient gets 1.4),
wherein NOx is for conversion is to 6%O
2under concentration, NOx
actual measurement, O
2 actual measurementsbe respectively actual measurement NO
xconcentration, O
2concentration;
Then denitration efficiency is:
wherein NOx
import, NOx
outletbe respectively denitrification apparatus enter,
The NOx of outlet converts concentration;
For SNCR(Select Non-catalytic Reduction, SNCR method) mode, do not examine denitration efficiency;
3) NOx emission concentration is calculated: get the NOx concentration (coal-burning boiler excess air coefficient gets 1.4) after the conversion of chimney import flue gas analysis systematic survey,
The data that analysis meter reads are the dry concentration values of mark: 1 μm of ol/mol(1ppm), according to GB13223-2003;
4) flow velocity conversion: all to convert to when all flue gas flow rates make weighted mean mark state under flow velocity,
Wherein: V is actual measurement flue gas flow rate, V
0for flow velocity under mark state; P is actual measurement flue gas static pressure; T is actual measurement flue-gas temperature; X is actual measurement smoke moisture;
5) denitration electricity price is calculated: M=T × P
e× (1-e) × a
Wherein: M is subsidy electricity price, Wan Yuan;
T is denitrification apparatus operational percentage, %;
P
efor checking energy, ten thousand kWh;
E is station service power consumption rate, in 6%;
A is that unit electricity allowance is used: SCR denitration principle: 0.008 yuan/kWh;
SNCR denitration principle: 0.006 yuan/kWh.
The beneficial effect that the present invention reaches: the phenomenon that the present invention effectively prevent the denitration facility that not put into operation while electricity power enterprise enjoys denitration electricity price occurs, after the invention process, denitration unit operation index significantly promotes, and discharged nitrous oxides concentration is reduced to 77.17mg/m3 from 155.48mg/m3; Denitration efficiency is promoted to 76.46% from 45.82%; Denitration operational percentage is promoted to 91.72% from 22.31%, is that completing of 12 oxides of nitrogen emission reduction targets plays positive facilitation.
Accompanying drawing explanation
Fig. 1 is the denitration inlet temperature curve map of different load section correspondence;
Fig. 2 is the motor current curve figure of the different load section correspondence of different capacitance grade unit;
Fig. 3 is the reductive agent flow curve figure of the different load section correspondence of different capacitance grade unit;
Fig. 4 is SCR denitration unit denitration inlet NOx concentration curve map.
Embodiment
Method of the present invention is applicable to the coal-fired denitration unit of more than 135MW, take genset as examination unit, with hour for substantially to examine the cycle, carries out the form of subsidy electricity price: namely when a certain hour satisfied examination condition, and this hour checking energy gives electricity price and subsidize.
The unit examination time:
Denitration inlet temperature:
SCR denitration mode needs to carry out under the effect of catalyzer, and the reaction needed of reductive agent and catalyzer just can reach best effect at a certain temperature.At present, the unit catalyzer possessing SCR mode denitration facility inside the province adopts V2O5/TiO2 mostly, and the optimal reaction temperature of this type catalyzer is about 310 DEG C.On the south system, 7 units such as heat (600MW), Nanjing, Huaneng Group (1000MW), brass hill China Resources (1000MW), state's electricity Jian Bi (1000MW) are target of investication and study, intensive investigation and analysis is carried out to denitration inlet temperature data in 2011 of target of investication and study, has been classified as follows shown in table according to different load section:
The denitration inlet temperature of table 1 different load section correspondence
Can be found out by above investigational data, when above 7 unit generation loads are greater than 50%, denitration inlet temperature is at least 310 DEG C, all can reach denitration optimal reaction temperature.
Generator power:
In conjunction with " coal-firing units gas desulfurization is monitored and infosystem in real time " of having put into operation, determine with accessed in system 41 power plant, 129 135MW and above unit for target of investication and study, intensive investigation and analysis was carried out to 2010 of target of investication and study and annual generator power data in 2011, has been classified as follows shown in table according to different load section:
The generator power of table 2 different load section correspondence
Can be found out by above investigational data, 129 135MW and above unit more than 98% time period generation load are all greater than 50% of rated load.
Dilution air electric current:
Because SNCR denitration mode adopts dilution water transport pump dilution water to dilute reductive agent, according to investigation situation, the Li Gang power plant of SNCR mode and Kan Shan power plant dilution water pump all only have " RUN " signal inside the province, therefore, only the dilution air of SCR denitration mode is carried out to the analysis of current data in technical Analysis.
System with the China Telecom Huaiyin (300MW) accessed, south heat, Nanjing (600MW), Nanjing, Huaneng Group (1000MW) three different capacitance grade units are for target of investication and study, intensive investigation and analysis is carried out to dilution air current data in 2011 of target of investication and study, has been classified as follows shown in table according to different load section:
The current of electric of the different load section correspondence of table 3 different capacitance grade unit
Can be found out by above investigational data, above 3 units are when generation load is greater than 50%, and dilution air electric current is at least more than 5A.
Cut down unit oxides of nitrogen denitration operating cost
(1) SCR mode
1. boundary condition: market liquefied ammonia is 4000 yuan/ton to the price at factory, 10,000 kWh produce about 40,000 m
3exhaust gas volumn, liquefied ammonia cost accounts for 25.96% of denitration total cost, and in former flue gas, about 95% volume is NO, and 5% is NO
2, station service power consumption rate is 6%.
The every cost proportion of table 4SCR denitration mode
| Project | Proportion (%) |
| Catalyzer | 23.54 |
| Reductive agent | 25.96 |
| Labour cost | 0.49 |
| Steam takes | 1.35 |
| Water rate | 0.05 |
| The electricity charge | 10.35 |
| Finance charge | 8.93 |
| Premium of insurance | 0.33 |
| Overhaul expense | 5.04 |
| Depreciation cost | 23.96 |
2. Computing Principle
SCR (SCR) technology is under the effect of metallic catalyst, with NH
3as reductive agent, NOx is reduced into N
2, generate H simultaneously
2o.Main chemical reactions formula is as follows:
4NO+4NH
3+O
2→4N
2+6H
2O
2NO
2+4NH
3+O
2→3N
2+6H
2O
Because about 95% volume in former flue gas is NO, 5% is NO
2, so abatement 1 ton of NOx needs the liquefied ammonia amount consumed to be about in theory:
NH
3=(95% × 30 × 17/30/ (95% × 30+5% × 46)+5% × 46 × 17 × 2/46/ (95% × 30+5% × 46)=0.58 ton
Generate electricity at full capacity 1 hour by 600,000 units, produce 2,400,000 m
3exhaust gas volumn, denitration inlet NOx concentration is 400mg/m
3, denitration efficiency 60%, then cut down 240*10000*400*60%/109=0.576 ton NOx, needs to consume liquefied ammonia total expenses M(unit) be:
M=0.576 × 0.58 × 4000=1336 unit
Then cut down the denitration total cost Mtotal(yuan/ton NOx of 1 ton of NOx) be:
M
total=1474/0.576/25.96%=9280 unit
Amount to often spend electricity volume often cut down unit NOx denitration cost (li/(kWh.mg/m
3nOx)) be:
M
tnox=9857 × 10
3/ 10
9× 240 × 10000/ (60 × 10000 × (1-6%)=0.039 li
3. conclusion
As from the foregoing, amount to often degree electricity and often cut down unit NOx emission concentration (with NO
2meter) denitration cost (li/(kWh.mg/m
3nO
2)) be: M
tnox=0.039 × 46/ (95% × 30+5% × 46)=0.059 li
4. check
South, Jiangsu heat
Design load: denitration efficiency 75%, denitration inlet NOx concentration 350mg/m
3, NH
3/ NOx mol ratio 0.765.
#1 unit (600MW) generates electricity 1 hour at full capacity, produces 2,400,000 m
3exhaust gas volumn, then cut down 240*10000*350*75%/109=0.63 ton NOx, then need to consume liquefied ammonia total expenses M(unit) be:
M=240×10000×350/(95%×30+5%×46)/10
9×0.765×17×4000=1418
Namely the denitration total cost Mtotal(yuan/ton NOx of 1 ton of NOx is cut down) be:
M
total=1336/0.63/25%=9008
Amount to often degree online electricity and often cut down unit NOx emission concentration (with NO
2meter) denitration cost (li/(kWh.mg/m
3nO
2)) be:
M
tnox=9008×10
3/10
9×240×10
4/(60×10
4×(1-6%)×46/(95%×30+5%×46)=0.057
Substantially identical with above-mentioned reckoning result 0.059.
Chen Jia port
Design load: denitration efficiency 80%, denitration inlet NOx concentration 400mg/m
3, NH
3/ NOx mol ratio 0.8164.
#1 unit (660MW) generates electricity 1 hour at full capacity, produces 2,640,000 m
3exhaust gas volumn, then cut down 264*10000*400*80%/109=0.84 ton NOx, then need to consume liquefied ammonia total expenses M(unit) be:
M=264×10000×400/(95%×30+5%×46)/10
9×0.8164×17×4000=1903
Namely the denitration total cost Mtotal(yuan/ton NOx of 1 ton of NOx is cut down) be:
M
total=1903/0.84/25%=9063
Amount to often degree online electricity and often cut down unit NOx emission concentration (with NO
2meter) denitration cost (li/(kWh.mg/m
3nO
2)) be:
M
tnox=9063×10
3/10
9×264×10
4/(66×10
4×(1-6%))×46/(95%×30+5%×46)=0.058
Substantially identical with above-mentioned reckoning result 0.059.
(2) SNCR mode
1. boundary condition: market urea is 2200 yuan/ton to the price at factory, 10,000 kWh produce about 40,000 m
3exhaust gas volumn,
Urea cost accounts for 19% of denitration total cost, and in former flue gas, about 95% volume is NO, and 5% is NO
2.
Table 5SNCR denitration mode every cost proportion project
| Project | Proportion (%) |
| Boiler efficiency losses | 43.3 |
| Urea | 19.1 |
| Catalyzer | 4.7 |
| Labour cost | 0.7 |
| Project | Proportion (%) |
| Steam takes | 2.7 |
| Water rate | 0.7 |
| The electricity charge | 2.3 |
| Finance charge | 5.3 |
| Value added tax | 8.2 |
| Equipment repair takes | 2.5 |
| Maintenance materials takes | 1.5 |
| Depreciation cost | 9.0 |
2. Computing Principle
SCR (SNCR) technology main chemical reactions formula is as follows:
2CO(NH
2)
2+6NO→5N
2+2CO
2+4H
2O
Cut down the urea amount that 1 ton of NOx needs to consume in theory:
CO (NH
2)
2=1/30 × 1/3 × 60=0.67 ton
Generate electricity at full capacity 1 hour by 600,000 units, 2,400,000 m can be produced
3exhaust gas volumn, estimates abatement x ton NOx.Then consume liquefied ammonia total expenses M(unit) be:
M=x×0.67×2200=1474x
Namely the denitration total cost Mtotal(yuan/ton NOx of 1 ton of NOx is cut down) be:
M
total=1474 × 1/19%=7758 unit
Amount to often degree online electricity often cut down unit NOx denitration cost (li/(kWh.mg/m
3nOx)) be:
M
tnox=7758 × 10
3/ 10
9× 240 × 10
4/ (60 × 10
4× (1-6%))=0.033 li
3. conclusion
As from the foregoing, amount to often degree electricity and often cut down unit NOx emission concentration (with NO
2meter) denitration cost (li/(kWh.mg/m
3/ NO
2)) be:
M
tnox=0.033 × 1.53=0.049 li
Reductive agent flow:
(1) SCR mode
According to above-mentioned reckoning, cutting down 1 ton of NOx needs to consume about 0.58 ton of liquefied ammonia, generates electricity 1 hour, produce 600,000 m by minimum capacity 300,000 unit 50% load possessing denitration facility inside the province
3exhaust gas volumn, denitration inlet NOx concentration is 200mg/m
3, denitration efficiency in 50%, then cuts down 60*10000*200*50%/106=60kg, needs to consume liquefied ammonia total amount M to be: M=60 × 0.58=34kg
Equally with China Telecom Huaiyin (300MW), south heat, Nanjing (600MW), Nanjing, Huaneng Group (1000MW) three different capacitance grade units for target of investication and study, intensive investigation and analysis is carried out to reductive agent datas on flows in 2011 of target of investication and study, has been classified as follows shown in table according to different load section:
The reductive agent flow of the different load section correspondence of table 6 different capacitance grade unit
As can be seen from above investigational data, above 3 units are when generation load is greater than 50%, and reductive agent flow is at least more than 30kg/h.
(2) SNCR mode
According to above-mentioned reckoning, cutting down 1 ton of NOx needs to consume about 0.67 ton of urea, generates electricity 1 hour, produce 600,000 m by 300,000 unit 50% loads
3exhaust gas volumn, denitration inlet NOx concentration is 200mg/m
3, denitration efficiency in 50%, then cuts down 60*10000*200*50%/10
6=60kg, needs to consume liquefied ammonia total amount M and is:
M=60×0.67=40kg
Unit denitration efficiency denitration operating cost
To access 19 135MW of denitrating system and annual data analysis in 2011 of above SCR denitration mode unit, denitration entrance NOx(is with NO
2meter) concentration table data is as follows, and maximum concentration is 400mg/m
3.
The denitration inlet NOx concentration list of a table 719 SCR denitration mode unit
Denitration efficiency standard, by 60%, supposes that denitration entrance NOx(is with NO
2meter) concentration is 400mg/m
3, NOx(is with NO
2meter) concentration of emission is 100mg/m
3.
The denitration cost of per unit denitration efficiency is:
M
tnox=0.037×(400-100*(95%×30+5%×46)/46)/60=0.21
Then as the overproof efficiency 5%(of denitration efficiency that is 65% of genset) time, the denitration cost that electricity power enterprise increases is 1.25 lis/kWh.
More than show and describe ultimate principle of the present invention, principal character and advantage.The technician of the industry should understand, and above-described embodiment does not limit the present invention in any form, the technical scheme that the mode that all employings are equal to replacement or equivalent transformation obtains, and all drops in protection scope of the present invention.
Claims (3)
1. a Thermal generation unit denitration electricity price method for supervising, is characterized in that, comprise the following steps:
1) denitrification apparatus operational percentage is calculated: denitrification apparatus operational percentage is within the scope of assessment period, denitrating flue gas facility puts into operation the number percent of time divided by the assessment period time, described assessment period is exert oneself after genset starts to reach 50% of nominal output and start to drop to exerting oneself before unit trip time period 50% of nominal output, the denitrating flue gas facility time of putting into operation is the difference of denitrating system start-up time and idle time
The criterion of denitrating system start-up time is:
11) for SCR mode:
During using liquefied ammonia as reductive agent, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the 100mg/m of concentration
3;
Little hourly value >=the lower threshold of arbitrary dilution air electric current; Little hourly value >=the lower threshold of arbitrary side spray ammonia flow;
Little hourly value >=50% of unit denitration efficiency;
During urea pyrolysis technique, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the 100mg/m of concentration
3;
40% of the little hourly value >=ratings of urea pyrolysis electric heater running current;
Little hourly value >=the lower threshold of urea cycle pump motor current;
Little hourly value >=50% of unit denitration efficiency;
12) for SNCR mode, meet following condition simultaneously:
Chimney entrance NO
xlittle hourly value≤the design load of concentration;
Arbitrary dilution water pump operation signal=1;
Arbitrary region urea flow hour average >=lower threshold;
13) for Circulating Fluidized Bed Boiler, meet following condition simultaneously:
Install equipment for denitrifying flue gas additional;
Little hourly value≤the 200mg/m of chimney inlet NOx concentration
3;
Denitrating system stoppage in transit signal criterion is:
For SCR mode:
When liquefied ammonia is as reductive agent, meet one of following condition:
Chimney entrance NO
xconcentration little hourly value > 100mg/m
3;
All dilution air electric currents little hourly value < lower threshold;
Two side spray ammonia flows little hourly value < lower threshold;
The little hourly value < 50% of unit denitration efficiency;
Urea pyrolysis technique, meets one of following condition:
Chimney entrance NO
xconcentration little hourly value > 100mg/m
3;
Urea pyrolysis electric heater running current little hourly value < specified 40%;
Urea cycle pump motor current little hourly value < lower threshold;
The little hourly value < 50% of unit denitration efficiency;
During in SNCR mode, meet one of following condition:
Chimney entrance NO
xconcentration little hourly value > design load;
All dilution water pump operation signal=0;
All regions urea flow hour average < lower threshold;
For Circulating Fluidized Bed Boiler: install equipment for denitrifying flue gas additional and chimney entrance NO
xconcentration little hourly value > 200mg/m
3;
2) denitration electricity price is calculated: M=T × P
e× (1-e) × a
Wherein: M is subsidy electricity price;
T is denitrification apparatus operational percentage;
P
efor checking energy;
E is station service power consumption rate;
A is that unit electricity allowance is used.
2. Thermal generation unit denitration electricity price method for supervising according to claim 1, is characterized in that, the step calculating denitration efficiency comprises:
For SCR mode: get the NO after denitrification apparatus import and exiting flue gas analytic system measurement conversion
xconcentration,
wherein NOx is for conversion is to 6%O
2under concentration, NOx
actual measurement, O
2 actual measurementsbe respectively actual measurement NOx concentration, O
2concentration;
Then denitration efficiency is:
wherein NOx
import, NOx
outletthe NOx being respectively denitrification apparatus import and export converts concentration;
For SNCR mode, do not examine denitration efficiency.
3. Thermal generation unit denitration electricity price method for supervising according to claim 1, is characterized in that: all to convert to when all flue gas flow rates make weighted mean mark state under flow velocity,
Wherein: V is actual measurement flue gas flow rate, V
0for flow velocity under mark state; P is actual measurement flue gas static pressure; T is actual measurement flue-gas temperature; X is actual measurement smoke moisture.
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| CN105214494B (en) * | 2014-06-27 | 2018-08-17 | 广东电网公司电力科学研究院 | The adjustment method of fired power generating unit SCR denitration system |
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| CN104793050A (en) * | 2015-04-23 | 2015-07-22 | 西安西热电站信息技术有限公司 | Method for calculating denitration on-grid electric quantity of thermal power plant |
| CN107202857A (en) * | 2017-04-28 | 2017-09-26 | 国网天津市电力公司 | A kind of laboratory's denitrating catalyst denitration efficiency computational methods |
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| CN101279261A (en) * | 2008-05-23 | 2008-10-08 | 清华大学 | Preparation of iron-based selective catalytic reduction denitration catalyst |
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