CN112990652A - Evaluation method for boiler energy efficiency and economic and technical combination coupled with pollutant emission reduction - Google Patents
Evaluation method for boiler energy efficiency and economic and technical combination coupled with pollutant emission reduction Download PDFInfo
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
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Abstract
The invention discloses an evaluation method for combining boiler energy efficiency and economic and technical performance of coupled pollutant emission reduction, and belongs to the field of boiler energy efficiency. The method comprises the following steps: s100, calculating to obtain the desulfurization cost and the desulfurization unit signature energy consumption; s200, calculating to obtain denitration cost and denitration unit signature energy consumption; s300, calculating to obtain dust removal cost and dust removal unit label folding energy consumption; s400, calculating to obtain the cost of saving the waste heat recovery energy, the profit of saving the energy and the reduced amount of the waste heat recovery net unit; s500, adding the desulfurization cost, the denitration cost, the dedusting cost, the cost of energy saving of waste heat recovery and the profit of energy saving to form final cost or profit; and adding the unit label folding energy consumption and the waste heat recovery net unit label folding saving amount of desulfurization, denitrification and dust removal to form the final unit label folding energy consumption or label folding saving amount.
Description
Technical Field
The invention relates to an evaluation method for combining boiler energy efficiency and economic technology by coupling pollutant emission reduction, and belongs to the technical field of boiler energy efficiency environmental protection treatment.
Background
Since 2013, 9 and 10, and the atmospheric pollution prevention and control action plan was issued by the state department, more and more boilers adopt ultralow emission to control the emission of atmospheric pollutants, particularly in recent years, in order to control haze, the emission control requirements of atmospheric pollutants of boilers are getting tighter and tighter, which also puts forward new requirements on energy conservation and environmental protection, that is to say, under the premise of ensuring the emission control requirements of atmospheric pollutants, energy is saved and cost is reduced as much as possible within the allowable range of technical conditions.
Main control or governing NO for boiler atmospheric pollutant dischargex、SO2And particulate matter. In practical use, SO is treated2Meanwhile, various technical routes can be adopted, for example, in the desulfurization of a circulating fluidized bed boiler, in-furnace desulfurization, combination of in-furnace desulfurization and out-furnace desulfurization, out-furnace desulfurization and the like can be adopted, and the SO can be realized by adopting any desulfurization technical route2The standard requirement of control, but also can save energy or reduce the cost, it is an important technical field; for the discharged smoke (particulate matter), it is currently possible to adoptThe used technologies mainly comprise bag dust removal, electric bag dust removal, wet static electricity, combination of the above and the like, and the adopted method is energy-saving and cost-reducing and is also an important issue for realizing energy conservation and emission reduction; NOxThe ultralow emission is an application model combining the in-furnace control and the out-furnace treatment, after the in-furnace control is performed by adopting low-nitrogen combustion and other modes, the out-furnace treatment cost is obviously reduced, the material resources are saved, the energy is saved, and meanwhile, the reasonable range of the low-nitrogen combustion needs to be considered, namely the influence of the low-nitrogen combustion on the combustion efficiency of the boiler.
Therefore, the development of a technical route which can provide the control and treatment of the emission of the atmospheric pollutants at the beginning of the design and also can provide energy conservation and cost reduction for the reconstruction and operation becomes a problem to be solved by the technical personnel in the field.
Disclosure of Invention
The invention aims to provide an evaluation method for combining energy efficiency and economic and technical performance of a boiler coupled with pollutant emission reduction, so as to solve the problems in the prior art.
An evaluation method for combining energy efficiency and economic and technical performance of a boiler for coupling pollutant emission reduction is an evaluation method based on unit direct or indirect cost, and comprises the following steps:
s100, calculating to obtain the desulfurization cost and the desulfurization unit signature energy consumption;
s200, calculating to obtain denitration cost and denitration unit signature energy consumption;
s300, calculating to obtain dust removal cost and dust removal unit label folding energy consumption;
s400, calculating to obtain the cost of saving the waste heat recovery energy, the profit of saving the energy and the reduced amount of the waste heat recovery net unit;
s500, adding the desulfurization cost, the denitration cost, the dedusting cost, the cost for recovering waste heat and the energy saving cost to form a final cost; and adding the unit label folding energy consumption of desulfurization, denitration and dust removal and the net unit label folding saving amount of waste heat recovery to form final unit label folding energy consumption.
Further, in S100, the evaluation process of the desulfurization economy index includes the following steps:
s110, firstly setting a calcium-sulfur molar ratio, and directly calculating the desulfurization cost in the furnace when the calcium-sulfur molar ratio is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, calculating the desulfurization heat loss, obtaining the increase value of the fuel consumption cost by calculating the desulfurization heat loss, and then calculating the desulfurization cost in the furnace; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the added value of the fuel consumption cost, and calculating the desulfurization cost in the furnace;
s120, respectively calculating SO at inlets of desulfurization facilities under the conditions of different calcium-sulfur molar ratios2Concentration, namely respectively calculating the semi-dry desulfurization cost and the wet desulfurization cost according to the imported concentration, and meanwhile calculating other expenses;
s130, respectively calculating the desulfurization cost in the furnace plus the semi-dry desulfurization cost containing other expenses, and the desulfurization cost in the furnace plus the wet desulfurization cost containing other expenses under the conditions of different calcium-sulfur ratios;
and S140, comparing the total cost difference under different calcium-sulfur molar ratio conditions, selecting the lowest total cost, and forming an optimized design and operation technical route.
Further, the other expenses include depreciation costs, maintenance costs, labor costs, and financial costs.
Further, in S100, the desulfurization energy efficiency index evaluation process includes the following steps:
s150, setting the molar ratio of calcium to sulfur, and directly calculating the unit discount energy consumption of the desulfurization resources in the furnace when the molar ratio of calcium to sulfur is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, calculating the desulfurization heat loss, obtaining the energy consumption increase value of fuel consumption by calculating the desulfurization heat loss, and then calculating the desulfurization energy consumption in the furnace; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the energy consumption increase value of fuel consumption, and calculating the unit signature energy consumption of desulfurization in the furnace;
s160, respectively calculating SO at inlets of desulfurization facilities under the conditions of different calcium-sulfur molar ratios2Concentration, namely respectively calculating unit signature energy consumption of semi-dry desulfurization and unit signature energy consumption of wet desulfurization according to the concentration of the inlet, and simultaneously calculating unit signature energy consumption of other consumptions;
s170, respectively calculating the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of semidry desulfurization, and the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of wet desulfurization under the condition of different calcium-sulfur ratios;
and S180, comparing the unit signature energy consumption under different calcium-sulfur molar ratios, and selecting the lowest unit signature energy consumption to form an optimized design and operation technical route.
Further, in S200, the denitration economic indicator evaluation process includes the following steps:
s210, firstly setting a denitration facility inlet NOxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the SNCR or tail SCR denitration cost in the furnace; when 100 < NOxWhen the concentration of the nitrogen in the gas is less than or equal to 200mg/Nm3, calculating denitration heat loss, obtaining a cost increase value of fuel consumption by calculating the denitration heat loss, and then calculating the SNCR or SCR denitration cost; when NO is presentxWhen the concentration is more than 200mg/Nm3, calculating the denitration heat loss, obtaining the cost increase value of fuel consumption, and calculating the SNCR or SCR denitration cost;
s220, respectively calculating different NO at inlets of denitration facilitiesxThe low-nitrogen combustion plus SNCR denitration cost, the low-nitrogen combustion plus SCR denitration cost;
and S230, comparing the cost under the conditions of different inlet NOx concentrations and the same outlet concentration index, and selecting the lowest cost to form an optimized design and operation technical route.
Further, in S200, the denitration energy efficiency index evaluation process includes the following steps:
s240, firstly setting an inlet NO of a denitration facilityxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the unit signature energy consumption of SNCR or tail SCR denitration in the furnace; when 100 < NOxWhen the concentration of the nitrogen in the gas is less than or equal to 200mg/Nm3, calculating the heat loss of denitration, obtaining the energy consumption increase value of fuel consumption by calculating the heat loss of denitration, and then calculating the unit discount energy consumption of SNCR or SCR denitration; when NO is presentxWhen the concentration is more than 200mg/Nm3, the denitration heat loss needs to be calculated, the unit discount energy consumption increase value of fuel consumption is obtained, and the SNCR or SCR denitration is calculatedMarking energy consumption of saltpeter unit;
s250, respectively calculating different NO at inlets of denitration facilitiesxThen, low-nitrogen combustion plus SNCR denitration unit discount energy consumption, low-nitrogen combustion plus SCR denitration unit discount energy consumption;
s260, comparing different inlet NOxConcentration index, same outlet NOxAnd (4) unit label folding energy consumption under the condition of concentration indexes to form an optimized design or operation technical route.
Further, in S300, the dedusting economy evaluation process specifically includes: and (3) optimizing dust removal technical routes aiming at different furnace types: and (3) selecting a bag dust removal, electrostatic dust removal and wet dust removal combined mode for dust removal for different furnace types respectively, calculating the combined cost of different dust removal modes in the dust removal modes respectively, and selecting the lowest cost to form an optimized design and operation technical route.
Further, in S400, the waste heat recovery evaluation process specifically includes: aiming at the temperature and the quality of the smoke exhaust gas, the cost and the energy saving profit of different recovery modes are respectively calculated according to the proportions of the waste heat recovery of the high-temperature smoke in front of the desulfurizing towers of different furnace types and the waste heat recovery in the desulfurizing process.
Further, the different furnace types include: grate-fired boilers, pulverized coal boilers and circulating fluidized bed boilers.
The main advantages of the invention are: the invention provides an evaluation method for combining energy efficiency and economic and technical performance of a boiler coupled with pollutant emission reduction, which evaluates various technical combination applications by comprehensively considering the treatment synergy of atmospheric pollutants inside and outside the boiler and the low-temperature and high-temperature waste heat recovery synergy. The invention discloses a boiler energy efficiency evaluation method, which is characterized in that the major influence of atmospheric pollutant control in a boiler on the energy consumption of a boiler system is not considered in the traditional boiler energy efficiency evaluation method, the comprehensive energy efficiency after the cooperation of the in-boiler control and the out-of-boiler treatment is comprehensively considered, a cooperative mechanism of high-efficiency and low-nitrogen combustion in the boiler and high-efficiency desulfurization and low-nitrogen combustion is constructed, a technical route which is matched with the tail flue gas treatment and can realize long-period operation in the boiler is provided, a coordination method of exhaust smoke waste heat and desulfurization waste heat recovery is formed, an optimization design and an operation method which comprehensively consider the boiler body efficiency, waste heat recovery and atmospheric pollutant treatment are developed, and the boiler energy efficiency evaluation method has important significance.
Drawings
FIG. 1 is a desulfurization economics evaluation method;
FIG. 2 is a desulfurization energy efficiency evaluation method;
FIG. 3 is a denitration economy evaluation method;
fig. 4 shows a denitration energy efficiency evaluation method.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The boiler economic and technical evaluation comprises the control of the air pollutants in the boiler, the treatment of the air pollutants outside the boiler, the cooperative control of the inside and the outside of the boiler and the cooperation of the waste heat recovery of the high-temperature flue gas and the low-temperature flue gas. The boiler economic technology evaluation adopts two modes, one is an evaluation method based on unit direct or indirect cost, and the other is an evaluation method based on unit energy consumption. The invention evaluates the combined application of various technologies by comprehensively considering the treatment synergy of the atmospheric pollutants inside and outside the furnace and the low-temperature and high-temperature waste heat recovery synergy.
In-furnace atmospheric contamination control including NOx、SO2Control of NOxThe control is generally performed by low-nitrogen combustion technology, SNCR and the like, SO2The control is generally performed by in-furnace limestone desulfurization and the like.
External atmospheric pollutant remediation by NOx、SO2And particulate matter remediation, NOxThe treatment generally adopts SCR technology, ozone method and the like, SO2The treatment is generally wet desulfurization, semidry desulfurization and the like.
The particulate matter treatment outside the furnace generally adopts cloth bag dust removal, electrostatic dust removal, combination of cloth bags and static electricity and the like.
The high-temperature flue gas waste heat recovery generally adopts a dividing wall type heat exchanger, and the low-temperature flue gas waste heat recovery after desulfurization generally adopts a direct contact type heat exchanger.
NOxAnd (4) performing cooperative evaluation of in-furnace control and out-of-furnace treatment. The core idea is to optimize NO inside and outside the furnacexA technical route of control and treatment synergy, coordinates the relationship between high-efficiency combustion and low pollutant emission, and scientifically sets NO according to different furnace typesxInitial emission concentration of NO through furnacexReasonable setting of scientific indexes, and calculating technical economy or energy consumption.
The control technique in the grate-fired boiler preferably adopts fuel distribution, combustion atmosphere organization, flue gas recirculation, fly ash recirculation and the like, and NO at the tail or outside the boilerxThe SCR technology is preferably adopted in the treatment technology, and other technologies can also be adopted.
The control in the pulverized coal fired boiler preferentially adopts the low-nitrogen combustion technology, and NO is arranged at the tail part or outside the boilerxThe SCR technology is preferably adopted in the treatment technology, and other technologies can also be adopted.
The control technology of the atmospheric pollutants of the circulating fluidized bed boiler preferably adopts a method of combining a low-nitrogen combustion technology and an SNCR technology, and NO is arranged at the tail part or outside the boilerxThe treatment technology can adopt SCR technology or ozone oxidation technology and the like.
SO2And (4) performing cooperative evaluation on in-furnace control and out-of-furnace treatment. The core idea is that according to a proper principle, whether an in-furnace desulfurization technology is needed or not is selected according to a furnace type, a semi-dry method or a wet method desulfurization technology is preferentially selected for the out-furnace desulfurization, and a technical route is reasonably arranged.
Particle control and treatment technology. The core idea is to arrange different particle removal technical routes according to the emission requirement and optimally configure the removal equipment.
And the recovery of the high-temperature flue gas waste heat and the low-temperature flue gas waste heat is cooperated. The high-temperature flue gas mainly refers to the outlet of a boiler air preheater and the inlet part of a first-stage dust remover; the low-temperature flue gas mainly refers to the waste heat of flue gas in the desulfurizing tower. The core idea of the evaluation is to optimize the combination mode of recovering the waste heat of the high-temperature flue gas and the low-temperature flue gas.
And (4) comprehensive evaluation. The core idea is that boiler combustion efficiency, waste heat recovery and the like are comprehensively considered according to emission requirements, the key point is to evaluate the influence of different atmospheric pollutant control and treatment modes and waste heat recovery modes on boiler energy efficiency, and an optimized design scheme and an optimized operation method for atmospheric pollutant emission reduction and waste heat recovery are provided. Under the condition of meeting the emission target of the atmospheric pollutants, after the technical route is optimized, the comprehensive energy consumption and economic indexes of the boiler and the system thereof are calculated.
The data source is as follows: if the design stage is adopted, the design data can be adopted for evaluation, and the design data mainly comprises boiler thermodynamic calculation, initial emission of atmospheric pollutants, smoke resistance calculation (or fan model selection), hydrodynamic calculation (or water pump model selection), SNCR design data, SCR design data, in-furnace desulfurization design data, out-of-furnace desulfurization design data, dust removal design data and the like. If the operation stage is adopted, actual test data can be adopted for evaluation, and the test data mainly comprises boiler combustion efficiency, boiler thermal efficiency, initial emission of atmospheric pollutants, SNCR (selective non catalytic reduction) denitration reaction resources and energy consumption, SCR (selective catalytic reduction) denitration reaction resources and energy consumption, in-furnace desulfuration reaction resources and energy consumption, out-furnace desulfuration reaction resources and energy consumption, dedusting resources and energy consumption and the like.
Referring to fig. 1, an evaluation method for coupling the energy efficiency and the economic and technical performance of a boiler with pollutant emission reduction is an evaluation method based on unit direct or indirect cost, and comprises the following steps:
s100, calculating to obtain the desulfurization cost and the desulfurization unit signature energy consumption;
s200, calculating to obtain denitration cost and denitration unit signature energy consumption;
s300, calculating to obtain dust removal cost and dust removal unit label folding energy consumption;
s400, calculating to obtain the cost of saving the waste heat recovery energy, the profit of saving the energy and the reduced amount of the waste heat recovery net unit;
s500, adding the desulfurization cost, the denitration cost, the dedusting cost, the cost of energy saving of waste heat recovery and the profit of energy saving to form final cost or profit; and adding the unit label folding energy consumption and the waste heat recovery net unit label folding saving amount of desulfurization, denitrification and dust removal to form the final unit label folding energy consumption or label folding saving amount.
Further, in S100, the evaluation process of the desulfurization economy index includes the following steps:
s110, firstly setting a calcium-sulfur molar ratio, and directly calculating the desulfurization cost in the furnace when the calcium-sulfur molar ratio is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, the calculation of the desulfurization heat loss is recommended, or the direct calculation of the desulfurization cost in the furnace can be selected, the increase value of the fuel consumption cost is obtained by calculating the desulfurization heat loss, and then the desulfurization cost in the furnace is calculated; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the added value of the fuel consumption cost, and calculating the desulfurization cost in the furnace;
s120, respectively calculating SO at inlets of desulfurization facilities under the conditions of different calcium-sulfur molar ratios2Concentration, namely respectively calculating the semi-dry desulfurization cost and the wet desulfurization cost according to the imported concentration, and meanwhile calculating other expenses;
s130, respectively calculating the desulfurization cost in the furnace plus the semi-dry desulfurization cost containing other expenses, and the desulfurization cost in the furnace plus the wet desulfurization cost containing other expenses under the conditions of different calcium-sulfur ratios;
and S140, comparing the total cost difference under different calcium-sulfur molar ratio conditions to form an optimized design or operation technical route.
Further, in S100, the desulfurization energy efficiency index evaluation process includes the following steps:
s150, setting the molar ratio of calcium to sulfur, and directly calculating the unit discount energy consumption of the desulfurization resources in the furnace when the molar ratio of calcium to sulfur is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, the calculation of the desulfurization heat loss is recommended, or the unit energy consumption of desulfurization in the furnace can be directly calculated (the problem is the same as above), the energy consumption increase value of fuel consumption is obtained by calculating the desulfurization heat loss, and then the desulfurization energy consumption in the furnace is calculated; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the energy consumption increase value of fuel consumption, and calculating the unit signature energy consumption of desulfurization in the furnace;
s160, respectively calculating desulfurization facilities under the conditions of different calcium-sulfur molar ratiosOral SO2Concentration, namely respectively calculating unit signature energy consumption of semi-dry desulfurization and unit signature energy consumption of wet desulfurization according to the concentration of the inlet, and simultaneously calculating unit signature energy consumption of other consumptions;
s170, respectively calculating the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of semidry desulfurization, and the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of wet desulfurization under the condition of different calcium-sulfur ratios;
and S180, comparing the unit label reduction energy consumption under different calcium-sulfur molar ratio conditions to form an optimized design or operation technical route.
Further, in S200, the denitration economic indicator evaluation process includes the following steps:
s210, firstly setting a denitration facility inlet NOxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the SNCR or tail SCR denitration cost in the furnace; when 100 < NOxWhen the concentration of the nitrogen in the gas is less than or equal to 200mg/Nm3, the denitration heat loss calculation is recommended, or the SNCR or SCR denitration cost can be directly calculated, the cost increase value of fuel consumption is obtained by calculating the denitration heat loss, and then the SNCR or SCR denitration cost is calculated; when NO is presentxWhen the concentration is more than 200mg/Nm3, calculating the denitration heat loss, obtaining the cost increase value of fuel consumption, and calculating the SNCR or SCR denitration cost;
s220, respectively calculating different NO at inlets of denitration facilitiesxThe low-nitrogen combustion plus SNCR denitration cost, the low-nitrogen combustion plus SCR denitration cost;
and S230, comparing the cost under the conditions of different inlet NOx concentrations and the same outlet concentration index to form an optimized design or operation technical route.
Further, in S200, the denitration energy efficiency index evaluation process includes the following steps:
s240, firstly setting an inlet NO of a denitration facilityxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the unit signature energy consumption of SNCR or tail SCR denitration in the furnace; when 100 < NOxWhen the concentration is less than or equal to 200mg/Nm3, the calculation of denitration heat loss is recommended, or the direct calculation of SNCR or SCR denitration unit discount can be selectedStandard energy consumption, namely calculating the denitration heat loss to obtain an energy consumption increase value of fuel consumption, and then calculating the unit standard discount energy consumption of SNCR or SCR denitration; when NO is presentxWhen the concentration is more than 200mg/Nm3, calculating the denitration heat loss, obtaining the unit discount energy consumption increase value of fuel consumption, and calculating the unit discount energy consumption of SNCR or SCR denitration;
s250, respectively calculating different NO at inlets of denitration facilitiesxThen, low-nitrogen combustion plus SNCR denitration unit discount energy consumption, low-nitrogen combustion plus SCR denitration unit discount energy consumption;
s260, comparing different inlet NOxConcentration index, same outlet NOxAnd (4) unit label folding energy consumption under the condition of concentration indexes to form an optimized design or operation technical route.
Further, in S300, the dedusting economy evaluation process specifically includes: and (3) optimizing dust removal technical routes aiming at different furnace types: and (3) selecting a bag dust removal, electrostatic dust removal and wet dust removal combined mode for dust removal respectively for different furnace types, and calculating the cost of different dust removal mode combinations in the dust removal modes respectively to form an optimized design or operation technical route.
Further, in S400, the waste heat recovery evaluation process specifically includes: aiming at the temperature and the quality of the smoke exhaust gas, the cost and the energy saving profit of different recovery modes are respectively calculated according to the proportions of the waste heat recovery of the high-temperature smoke in front of the desulfurizing towers of different furnace types and the waste heat recovery in the desulfurizing process.
Further, the different furnace types include: grate-fired boilers, pulverized coal boilers and circulating fluidized bed boilers.
The following are the calculation methods of various data involved in the present evaluation method:
evaluation of in-furnace desulfurization economy:
limestone consumption: during design, the limestone consumption can be calculated by adopting the formula (1), and the formula (1) can be also used in the case of an operation stage, or the measured limestone consumption data can be directly used.
In the formula:
w-limestone consumption, t;
a-limestone purity, either assay data or 0.9;
SO generated after combustion of sulfur in K-solid fuel2Can be measured for SO2Post calculation, 0.9 can be taken;
Bj-boiler fuel consumption, measured or statistical data, t/h;
Sar-fuel received basal sulfur, assay data,%;
Kglb-a probabilistic molar ratio, measured or set data;
h-boiler annual run time, measured or expected data.
Cost of limestone:
in the formula:
V1-operating costs (limestone), ten thousand dollars;
u1-limestone unit price, yuan/ton;
the operating power consumption cost is as follows:
there are two cases, one is the direct purchase of limestone powder and the other is the presence of a limestone preparation plant.
V2Operating costs (limestone milling), ten thousand yuan;
Pt-total rated power of the motor, kW;
wCa-limestone yield, t/h;
Pc-air compressor rated power, kW;
the beta-compressed air coefficient is generally 1.92;
wCaproduction of compressed air，m3/min；
BS-consumption of limestone in the furnace, t/h;
u2electricity prices (internet), W/kWh.
If the limestone powder is directly purchased, the running electricity consumption cost of the part is zero.
Evaluation of in-furnace desulfurization energy efficiency:
and (3) operation power consumption: and performing label folding from the energy consumption perspective.
In the formula:
E2-preparing limestone milling operation signature energy consumption, t standard coal;
Heat loss by desulfurization in the furnace:
and respectively calculating the heat loss change of the boiler caused by adding the desulfurizer, respectively calculating the desulfurization heat loss under different calcium-sulfur molar ratio conditions in the boiler, and further calculating the change of the fuel consumption.
In the formula:
FI-energy consumption for desulfurization heat loss, t;
BA-adding a calculated or measured fuel quantity, t/h, after limestone desulfurization;
BB-adding a calculated or measured fuel quantity, t/h, after limestone desulfurization;
h-hours of boiler operation, H.
The operation cost is as follows: the transportation cost of the limestone is calculated into the unit price of the limestone and is not calculated independently.
Evaluation of economy of wet desulfurization:
cost of limestone:
and (4) calculating the limestone consumption outside the wet desulphurization furnace, and determining the desulphurization efficiency in the furnace according to the molar ratio of calcium to sulfur in the furnace. According to SO2Emission limit, calculating the desulfurization efficiency to be achieved outside the furnace, if the operation condition is the condition, combining the test data of a power plant to obtain the molar ratio of calcium and sulfur outside the furnace, namely calculating SO at the wet desulfurization inlet2The total amount is obtained to the consumption of limestone.
The external desulfurization efficiency of the wet desulfurization furnace is as follows:
in the formula:
CSO2wet desulfurization inlet (or in-furnace desulfurization outlet) SO2Concentration, mg/Nm 3;
c-emission Limit, mg/Nm3；
ηtlIn-furnace desulfurization efficiency,%.
The cost of the limestone outside the wet desulphurization furnace is as follows:
in the formula:
K′glbthe molar ratio of calcium to sulfur outside the wet desulphurization furnace is;
u′1the limestone is the unit price of limestone, yuan/ton.
The electricity consumption cost of wet desulphurization operation is as follows:
the main energy consumption equipment in the wet desulphurization process is a slurry circulating pump and an oxidation fan, and accounts for about 60-70% of the total energy consumption of the total desulphurization system. In the energy consumption of the induced draft fan, the contribution rate of the resistance of the desulfurizing tower is about 20 percent. In actual operation, aiming at different desulfurizationSystem inlet SO2Concentration, the different power circulation pumps are combined to achieve the lowest energy consumption, and the calculation ignores the influence. In addition, no flue gas reheater (GGH) is provided. The electricity consumption cost for the operation outside the wet desulphurization furnace is as follows:
V′2＝P1u'2H×10-4 (8)
in the formula:
P1the total power consumption of the wet desulphurization system is kW;
u′2is the electricity price, yuan/kWh.
The operation water consumption cost is as follows:
the water consumption point of the desulfurization system mainly comprises 4 parts of water vapor carried away by flue gas, liquid water carried away by the flue gas, water quantity carried away by gypsum and discharged wastewater. The water cost is as follows:
in the formula:
BH2Owater consumption of the external desulfurization system is t;
u′3the unit price of water is yuan/ton.
Gypsum yield from wet desulfurization:
the industrial by-product of the external desulfurization is gypsum, the main component is crystalline calcium sulfate, and the water content is generally 10-20%. The yield of the desulfurized gypsum outside the furnace is as follows:
in the formula:
u′4selling price for gypsum, yuan/ton.
The cost of wastewater treatment by wet desulphurization:
V′5＝Bflu'5H×10-4 (10)
in the formula:
Bflis the desulfurization wastewater treatment capacity, t;
u′5is the cost of wastewater treatment, yuan/ton.
Evaluation of Wet desulfurization energy consumption
Operation power consumption signature
The main energy consumption equipment in the wet desulphurization process is a slurry circulating pump and an oxidation fan, and accounts for about 60-70% of the total energy consumption of the total desulphurization system. In the energy consumption of the induced draft fan, the contribution rate of the resistance of the desulfurizing tower is about 20 percent. In actual operation, different power circulating pumps are used for combination to achieve the lowest energy consumption for different concentrations of SO2 at the inlet of the desulfurization system, and the influence is ignored in calculation. In addition, no flue gas reheater (GGH) is provided. The energy consumption for the operation outside the wet desulphurization furnace is as follows:
in the formula:
P1-Total Power consumption of the Wet desulfurization System, kW.
Operation water consumption signature:
the water consumption point of the desulfurization system mainly comprises 4 parts of water vapor carried away by flue gas, liquid water carried away by the flue gas, water quantity carried away by gypsum and discharged wastewater. The water cost is as follows:
in the formula:
BH2Owater consumption of the external desulfurization system is t;
Evaluation of semi-dry desulfurization economy:
the cost of the limestone outside the semidry method furnace is as follows:
in the formula:
a' is the purity of the quicklime-;
K″glbthe molar ratio of calcium to sulfur outside the semi-dry desulfurization furnace is shown;
u″1the quicklime is produced in unit price of yuan/ton.
The semidry method has the following operating power consumption cost:
compared with a wet desulphurization process, the semi-dry desulphurization process needs to be additionally provided with a high-efficiency bag-type dust remover, so that the contribution rate of the resistance of the semi-dry desulphurization system and the resistance of the bag-type dust remover to the power consumption of the induced draft fan needs to be considered. The existing design data show that the sum of the resistance of the semi-dry desulfurization system and the resistance of the bag-type dust collector is about twice of the resistance of the wet desulfurization system, so that the power consumption of the semi-dry desulfurization system and the bag-type dust collector is approximately twice of the power consumption of an induced draft fan caused by the wet desulfurization resistance. The electricity consumption cost for the operation outside the semidry method desulfurization furnace is as follows:
V″2＝P′1u″2H×10-4 (15)
in the formula:
P′1the total power consumption of the semi-dry desulphurization system is kW;
u″2is the electricity price, yuan/kWh.
The semidry method consumes water for operation:
in the formula:
u″3the unit price of water is yuan/ton.
Evaluation of semi-dry desulfurization energy consumption:
and (3) running power consumption indexes of the semidry method:
in the formula:
P′1-total power consumption of the semi-dry desulfurization system, kW;
And (3) performing semidry method operation water consumption signature:
in the formula:
Other expenses, reported depreciation costs, maintenance costs, labor costs, and financial costs.
Depreciation cost:
the depreciation age limit of the desulfurization device is 15 years, the fixed asset formation rate is 95%, and the depreciation cost is as follows:
in the formula:
f is the static total investment cost of the desulphurization device, ten thousand yuan;
and n is the service life of the equipment, namely year.
Maintenance cost:
the maintenance cost is calculated according to 3% of the static investment, and then the maintenance cost is as follows:
Vmaintenance＝F×3％ (20)
Labor cost:
suppose that each unit increases n operators, each operator has a wage of y ten thousand yuan per year, and the labor cost is as follows:
Vartificial operation＝n·y (21)
Financial cost:
the financial cost is calculated as 5% of the static investment, then the financial cost is:
Vfinance affairs＝F×5％ (22)
Evaluation of in-furnace denitration economy:
SNCR denitrifier (urea) cost:
the denitration efficiency has a direct relation with the ammonia nitrogen molar ratio, and the critical denitration efficiency which enables the NOx emission value to be less than 50mg/Nm3 can be obtained according to the value of the inlet flue gas volume, so that the required ammonia nitrogen molar ratio is reversely deduced.
Ammonia nitrogen molar ratio:
the urea consumption is:
in the formula:
ηtxthe denitration efficiency in the furnace is percent;
bns is the urea consumption, t/h;
gamma is ammonia nitrogen molar ratio;
CNOxin terms of SNCR inlet NOx content, mg/Nm3(calculated as 95% NO and 5% NO 2);
vy is SNCR inlet flue gas volume, Nm3/h。
The cost of urea is as follows:
W1＝Bnsv1H×10-4 (25)
in the formula:
v1is the unit price of urea, yuan/ton.
Cost of SNCR water use:
before using, the urea needs to be diluted into urea solution with certain concentration by water. The water cost is as follows:
in the formula:
b is the concentration of urea solution;
v2the cost is water, yuan/ton.
SNCR running electricity consumption cost:
and determining denitration power consumption P2 according to the actual denitration data of the boiler. The approximate relationship between the electricity consumption and the urea consumption can be found with reference to the running data statistics as follows:
P2＝20Bns (27)
the operating power consumption cost is as follows:
W3＝P2v3H×10-4 (28)
in the formula:
v3is the electricity price, yuan/kWh.
In-furnace SNCR denitration (using urea) energy consumption evaluation:
water consumption in operation
In the formula:
Bns-water consumption of the denitration system outside the furnace, t;
Consumption of operating power
In the formula:
Denitration heat loss in the furnace:
when the SNCR system uses urea as a reducing agent, the urea solution needs to be diluted and then directly sprayed into a reaction area. Obviously, the effect on boiler efficiency is greater when entering the furnace in solution. Therefore, the influence of the SNCR denitration process on the boiler efficiency was analyzed with urea as the reducing agent.
After the SNCR reducing agent is sprayed into the hearth, the SNCR reducing agent sequentially undergoes the main processes of reducing agent solution evaporation, denitration reaction, emission along with flue gas and the like. From the above main process, it can be summarized that the influence of SNCR technology on boiler efficiency is mainly in the following three aspects: the reducing agent solution absorbs heat by evaporation, the denitration reaction releases heat, the enthalpy of the smoke discharged by the boiler is increased, and the like.
The reducing agent solution evaporates endothermically:
after the reducing agent solution is sprayed into the hearth, the three main processes of solution heat absorption, liquid evaporation, gas temperature rise after evaporation to the flue gas temperature and the like are carried out in sequence.
The mass flow calculation formula of the reducing agent solution is as follows:
the endothermic heat calculation for heating the reducing agent solution from injection temperature (20 ℃) to evaporation temperature (100 ℃) is as follows:
the reducing agent solution then enters the evaporation process and the heat absorption for evaporation is calculated as follows:
after the reducing agent solution is evaporated, the steam of the reducing agent solution continuously absorbs heat, and finally reaches the temperature same as the temperature of the exhaust smoke. The endothermic amount calculation formula in the process is as follows:
in summary, the calculation formula of the total endothermic heat quantity of the whole process of the reducing agent solution evaporation endothermic heat is as follows:
q1＝qa+qb+qc (35)
the denitration reaction releases heat:
the reaction of urea with NOx in SNCR systems is as follows:
HNO、HNO2respectively corresponding to two reactionsThe heat of reaction. Both reactions are exothermic, and the denitration reaction exotherm is calculated by the following formula:
change of enthalpy of boiler exhaust smoke:
after the reducing agent solution is sprayed into the hearth, the volume of the flue gas can be increased by the water vapor, CO2 and N2 brought in and generated by the reaction, the enthalpy of the flue gas exhausted by the boiler is increased, the loss of the flue gas is increased, and the overall efficiency of the boiler is reduced. Studies have shown that changes in boiler smoke exhaust enthalpy have very little, if any, effect on boiler efficiency.
The denitration heat loss can also be calculated approximately according to the following rules:
when the concentration of inlet NOx is less than or equal to 00mg/m3 and the denitration efficiency is more than 40%, the total heat loss of denitration is calculated according to 0.1%, the fuel quantity is increased according to 0.11% Bj, and the total heat loss is 0.11B after the denotationj0.7413; when the concentration of NOx is more than 100 at the inlet and less than or equal to 300mg/m3 and the denitration efficiency is more than 40%, the total heat loss of denitration is calculated according to 0.4%, the fuel quantity is increased according to 0.44% Bj, and the denitration rate is 0.44Bj0.7413; when the concentration of inlet NOx is more than 300mg/m3 and the denitration efficiency is more than 40%, the total heat loss of denitration is calculated according to 1%, the fuel quantity is increased according to 1.11% Bj, and the total heat loss is 1.11B after the denotationj·0.7413。
SCR denitration (using liquid ammonia) economy evaluation:
SCR denitration (use of liquid ammonia) reductant cost:
when the SCR uses liquid ammonia, the denitration efficiency can reach 90 percent when the ammonia nitrogen molar ratio is 0.9. Therefore, the ammonia nitrogen molar ratio is 0.9, and the emission requirement can be met.
The liquid ammonia consumption is:
in the formula:
gamma' is ammonia nitrogen molar ratio.
The cost of liquid ammonia is as follows:
in the formula (I), the compound is shown in the specification,
v'1the liquid ammonia is monovalent, yuan/ton.
Power consumption cost for SCR denitration (using liquid ammonia) operation:
the SCR liquid ammonia denitration technology mainly comprises a liquid ammonia unloading compressor, a liquid ammonia pump, a dilution fan and a waste water pump. The standard separately treats the shaft power of the fixed continuous operation equipment and the change of the power consumption of other equipment along with the liquid ammonia. Determining denitration power consumption P 'according to boiler operation data'2Then, the power consumption is:
the operating power consumption cost is as follows:
W'2＝P'2v'2H×10-4 (40)
in the formula:
v′2is the electricity price, yuan/kWh.
SCR denitration (using liquid ammonia) steam consumption cost
Soot blowing and heating of the reducing agent consumes steam. The steam consumption cost is as follows:
W′3＝sv'3H×10-4 (40)
in the formula:
s is steam consumption per hour, t/h;
v′3for steam prices, yuan/ton (180 yuan/ton can be taken here).
SCR denitration (using liquid ammonia) catalyst cost
The operating cost of the SCR denitration (using liquid ammonia) catalyst is as follows:
in the formula (I), the compound is shown in the specification,
v is the annual catalyst change volume, m 3;
h is the service cycle of the catalyst, h;
v′4for catalyst price, Yuan/m 3.
SCR denitration (using liquid ammonia) for other costs
SCR denitration (using liquid ammonia) depreciation cost
The depreciation age limit of the denitration device is 15 years, the fixed asset formation rate is 95%, and the depreciation cost is as follows:
in the formula:
f is the static total investment cost of the denitration device, ten thousand yuan;
and n is the service life of the equipment, namely year.
SCR denitration (using liquid ammonia) cost of maintenance:
the maintenance cost is calculated according to 3% of the static investment, and then the maintenance cost is as follows:
Vmaintenance＝F×3％ (43)
SCR denitration (using liquid ammonia) labor cost
Suppose that each unit increases n operators, each operator has a wage of y ten thousand yuan per year, and the labor cost is as follows:
Vartificial operation＝n·y (44)
SCR denitration (using liquid ammonia) financial cost
The financial cost is calculated as 5% of the static investment, then the financial cost is:
Vfinance affairs＝F×5％ (45)
SCR denitration (using liquid ammonia) energy consumption evaluation
SCR denitration (using liquid ammonia) operation power consumption label-marking energy consumption
The SCR liquid ammonia denitration technology mainly comprises a liquid ammonia unloading compressor, a liquid ammonia pump, a dilution fan and a waste water pump. The standard separately treats the shaft power of the fixed continuous operation equipment and the change of the power consumption of other equipment along with the liquid ammonia. Determining denitration power consumption P 'according to boiler operation data'2Then, the power consumption is:
in the formula:
P′gfixed continuously operating plant shaft power, kwh.
The operating power consumption is labeled as:
in the formula:
SCR denitration (using liquid ammonia) steam consumption signature
Soot blowing and heating of the reducing agent consumes steam. The steam consumption cost is as follows:
in the formula:
s is steam consumption per hour, t/h;
Economic and energy efficiency evaluation of coupled dust removal process
Evaluation of economical efficiency of bag-type dust collector
And if the design stage is adopted, respectively calculating the power increased by the induced draft fan, the power consumption increased by the compressed air system and the power consumption of the dust remover in operation according to the design data. If the operation stage is the operation stage, the power increased by the induced draft fan, the power consumption increased by the compressed air system and the power consumption of the dust remover operation caused by the resistance can be respectively calculated according to the operation data.
Drag causes increased power consumption costs for induced draft fans
Wbdc1＝ΔpQvbdc1H×10-4/0.85 (49)
In the formula:
Wbdc1-operating costs, ten thousand dollars;
delta p-the pressure difference between the inlet and the outlet of the dust remover, Pa;
q-inlet air volume of the dust remover, m 3/s;
vbdc1-electricity prices, yuan/kWh.
Increased power consumption cost of compressed air systems
Wbdc2＝0.746Padc2Hvadc2[Radc2+R′adc2]×10-4/0.9 (50)
In the formula:
Wbdc2-operating costs, ten thousand dollars;
Padc2-motor full horsepower, hp;
vbdc2-electricity price, dollars/kWh;
Radc2-ratio of time on full load,%;
R′adc2-ratio of idle running time,%.
Evaluation of energy consumption of bag-type dust collector
Power consumption signature for resistance induced draught fan increase
In the formula:
Increased power consumption signature for compressed air systems
In the formula:
Evaluation of economical efficiency of electric bag dust collector
The power consumption of the electric-bag composite dust removal is the sum of the power consumption of electric dust removal and the power consumption of cloth-bag dust removal.
Power consumption cost of induced draft fan
The power consumption cost of the induced draft fan is calculated according to the formula (49).
Increased power consumption cost of compressed air systems
The incremental power consumption cost of the compressed air system is calculated as equation (50).
Cost of energy consumption of the body equipment
The energy consumption of the electric bag dust remover body equipment comprises all electric equipment of a dust removing facility, such as a primary rectifier transformer, a secondary rectifier transformer, frequency conversion equipment, a heating device and the like.
Evaluation of energy consumption of electric bag dust collector
Power consumption and energy consumption label of induced draft fan
The power consumption of the induced draft fan is calculated according to the formula (51).
Increased power consumption cost of compressed air systems
The increased power consumption of the compressed air system is calculated according to the energy consumption signature (52).
Cost of energy consumption of the body equipment
The energy consumption of the electric bag dust remover body equipment comprises all electric equipment of a dust removing facility, such as a primary rectifier transformer, a secondary rectifier transformer, frequency conversion equipment, a heating device and the like.
Evaluation of Wet electric dust collector economy
Resistance power consumption cost of dust remover
The electricity consumption cost of the dust collector resistance is calculated according to the formula (49).
Other electricity consumption cost of dust remover
And (5) calculating the electricity consumption of high-voltage power supply equipment, low-voltage electric equipment and the like of the electric dust collector according to (49).
Wet electric dust collector energy consumption evaluation
Energy consumption signature of dust remover resistance power consumption
The power consumption cost of the dust collector resistance is calculated according to the formula (50).
Energy consumption signature of other power consumptions of dust remover
And (5) calculating the electricity consumption of high-voltage power supply equipment, low-voltage electric equipment and the like of the electric dust collector according to (49).
Other costs
Depreciation cost of bag-type dust collector
The depreciation age limit of the denitration device is 15 years, the fixed asset formation rate is 95%, and the depreciation cost is as follows:
in the formula:
f is the static total investment cost of the dust removal device, ten thousand yuan;
and n is the service life of the equipment, namely year.
Maintenance cost of bag-type dust collector
The maintenance cost is calculated according to 3% of the static investment, and then the maintenance cost is as follows:
Vmaintenance＝F×3％ (54)
Labor cost of bag-type dust collector
Suppose that each unit increases n operators, each operator has a wage of y ten thousand yuan per year, and the labor cost is as follows:
Vartificial operation＝n·y (55)
Evaluation of desulfurization waste heat utilization economy
The required input amount for the progressive evaluation of the desulfurization waste heat utilization is shown in a table 1, the calculation part is shown in a table 2,
TABLE 1 evaluation of the economics of desulfurization waste heat utilization
Calculating part
TABLE 2 desulfurization residual heat utilization energy resource consumption calculation
Energy resource consumption calculation
TABLE 3 evaluation calculation of desulfurization waste heat utilization economics
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. An evaluation method for combining boiler energy efficiency and economic and technical performance by coupling pollutant emission reduction is characterized in that the evaluation method is an evaluation method based on unit direct or indirect cost, and comprises the following steps:
s100, calculating to obtain the desulfurization cost and the desulfurization unit signature energy consumption;
s200, calculating to obtain denitration cost and denitration unit signature energy consumption;
s300, calculating to obtain dust removal cost and dust removal unit label folding energy consumption;
s400, calculating to obtain the cost of saving the waste heat recovery energy, the profit of saving the energy and the reduced amount of the waste heat recovery net unit;
s500, adding the desulfurization cost, the denitration cost, the dedusting cost, the cost for recovering waste heat and the energy saving cost to form a final cost; and adding the unit label folding energy consumption of desulfurization, denitration and dust removal and the net unit label folding saving amount of waste heat recovery to form final unit label folding energy consumption.
2. The method for evaluating the combination of the energy efficiency and the economic and technical performance of the boiler coupled with the pollutant emission reduction according to claim 1, wherein in S100, the desulfurization economic index evaluation process comprises the following steps:
s110, firstly setting a calcium-sulfur molar ratio, and directly calculating the desulfurization cost in the furnace when the calcium-sulfur molar ratio is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, calculating the desulfurization heat loss, obtaining the increase value of the fuel consumption cost by calculating the desulfurization heat loss, and then calculating the desulfurization cost in the furnace; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the added value of the fuel consumption cost, and calculating the desulfurization cost in the furnace;
s120, respectively calculating differentDesulfurizing facility inlet SO under condition of calcium-sulfur molar ratio2Concentration, namely respectively calculating the semi-dry desulfurization cost and the wet desulfurization cost according to the imported concentration, and meanwhile calculating other expenses;
s130, respectively calculating the desulfurization cost in the furnace plus the semi-dry desulfurization cost containing other expenses, and the desulfurization cost in the furnace plus the wet desulfurization cost containing other expenses under the conditions of different calcium-sulfur ratios;
and S140, comparing the total cost difference under different calcium-sulfur molar ratio conditions, selecting the lowest total cost, and forming an optimized design and operation technical route.
3. The method of claim 2, wherein the other expenses comprise depreciation cost, maintenance cost, labor cost and financial cost.
4. The method for evaluating the combination of the boiler energy efficiency and the economic and technical performance for coupling the pollutant emission reduction according to claim 1, wherein in S100, the process for evaluating the desulfurization energy efficiency index comprises the following steps:
s150, setting the molar ratio of calcium to sulfur, and directly calculating the unit discount energy consumption of the desulfurization resources in the furnace when the molar ratio of calcium to sulfur is less than or equal to 2.0; when the molar ratio of calcium to sulfur is more than 2.0 and less than or equal to 2.5, calculating the desulfurization heat loss, obtaining the energy consumption increase value of fuel consumption by calculating the desulfurization heat loss, and then calculating the desulfurization energy consumption in the furnace; when the molar ratio of calcium to sulfur is more than or equal to 2.5, calculating the desulfurization heat loss, obtaining the energy consumption increase value of fuel consumption, and calculating the unit signature energy consumption of desulfurization in the furnace;
s160, respectively calculating SO at inlets of desulfurization facilities under the conditions of different calcium-sulfur molar ratios2Concentration, namely respectively calculating unit signature energy consumption of semi-dry desulfurization and unit signature energy consumption of wet desulfurization according to the concentration of the inlet, and simultaneously calculating unit signature energy consumption of other consumptions;
s170, respectively calculating the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of semidry desulfurization, and the unit signature energy consumption of desulfurization in the furnace plus the unit signature energy consumption of wet desulfurization under the condition of different calcium-sulfur ratios;
and S180, comparing the unit signature energy consumption under different calcium-sulfur molar ratios, and selecting the lowest unit signature energy consumption to form an optimized design and operation technical route.
5. The method for evaluating the combination of the energy efficiency and the economic and technical performance of the boiler coupled with the pollutant emission reduction according to claim 1, wherein in S200, the denitration economic indicator evaluation process comprises the following steps:
s210, firstly setting a denitration facility inlet NOxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the SNCR or tail SCR denitration cost in the furnace; when 100 < NOxWhen the concentration of the nitrogen in the gas is less than or equal to 200mg/Nm3, calculating denitration heat loss, obtaining a cost increase value of fuel consumption by calculating the denitration heat loss, and then calculating the SNCR or SCR denitration cost; when NO is presentxWhen the concentration is more than 200mg/Nm3, calculating the denitration heat loss, obtaining the cost increase value of fuel consumption, and calculating the SNCR or SCR denitration cost;
s220, respectively calculating different NO at inlets of denitration facilitiesxThe low-nitrogen combustion plus SNCR denitration cost, the low-nitrogen combustion plus SCR denitration cost;
and S230, comparing the cost under the conditions of different inlet NOx concentrations and the same outlet concentration index, and selecting the lowest cost to form an optimized design and operation technical route.
6. The method for evaluating the combination of the boiler energy efficiency and the economic and technical performance in coupling with the pollutant emission reduction according to claim 1, wherein in S200, the denitration energy efficiency index evaluation process comprises the following steps:
s240, firstly setting an inlet NO of a denitration facilityxConcentration index, NO when using low nitrogen combustion technologyxWhen the concentration is less than or equal to 100mg/Nm3, directly calculating the unit signature energy consumption of SNCR or tail SCR denitration in the furnace; when 100 < NOxWhen the concentration is less than or equal to 200mg/Nm3, calculating the heat loss of denitration, obtaining the energy consumption increase value of fuel consumption by calculating the heat loss of denitration, and calculating the unit energy of SNCR or SCR denitrationConsumption; when NO is presentxWhen the concentration is more than 200mg/Nm3, calculating the denitration heat loss, obtaining the unit discount energy consumption increase value of fuel consumption, and calculating the unit discount energy consumption of SNCR or SCR denitration;
s250, respectively calculating different NO at inlets of denitration facilitiesxThen, low-nitrogen combustion plus SNCR denitration unit discount energy consumption, low-nitrogen combustion plus SCR denitration unit discount energy consumption;
s260, comparing different inlet NOxConcentration index, same outlet NOxAnd (4) unit label folding energy consumption under the condition of concentration indexes to form an optimized design or operation technical route.
7. The method for evaluating the combination of the energy efficiency and the economic and technical performance of the boiler coupled with the pollutant emission reduction according to claim 1, wherein in S300, a dedusting economic performance evaluation process specifically comprises the following steps: and (3) optimizing dust removal technical routes aiming at different furnace types: and (3) selecting a bag dust removal, electrostatic dust removal and wet dust removal combined mode for dust removal for different furnace types respectively, calculating the combined cost of different dust removal modes in the dust removal modes respectively, and selecting the lowest cost to form an optimized design and operation technical route.
8. The method for evaluating the combination of the energy efficiency and the economic and technical performance of the boiler coupled with the pollutant emission reduction according to claim 1, wherein in S400, a waste heat recovery evaluation process specifically comprises the following steps: aiming at the temperature and the quality of the smoke exhaust gas, the cost and the energy saving profit of different recovery modes are respectively calculated according to the proportions of the waste heat recovery of the high-temperature smoke in front of the desulfurizing towers of different furnace types and the waste heat recovery in the desulfurizing process.
9. The method for evaluating the combination of energy efficiency and economic efficiency and technical efficiency of the boiler coupled with pollutant reduction according to claim 7 or 8, wherein the different types of the boiler comprise: grate-fired boilers, pulverized coal boilers and circulating fluidized bed boilers.
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