CN113378394B - Intelligent soot blowing algorithm based on Gu Erwei odd heat balance - Google Patents
Intelligent soot blowing algorithm based on Gu Erwei odd heat balance Download PDFInfo
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Abstract
The invention relates to an intelligent soot blowing algorithm based on Gu Erwei odd heat balance, which is a soft measurement technology based on a local heat balance principle, and comprises the steps of calculating to obtain the inlet temperature of flue gas when the checking error of heat absorption and heat release is less than 2% under the condition that the outlet flue gas temperature, the inlet working medium temperature, the outlet working medium temperature and the working medium mass flow by an iterative algorithm, and further calculating to obtain an actual heat transfer coefficient, a theoretical heat transfer coefficient and a cleaning factor. The algorithm solves the problems of incomplete measuring points and the like, and saves the cost. The algorithm can effectively monitor the pollution state of the heating surface of the boiler, determine the optimal soot blowing time, further maintain the cleanliness of the heating surface and improve the operation efficiency of the boiler. Meanwhile, soot blowing media are saved, corrosion and abrasion of the tube wall of the heating surface are reduced, and the service efficiency of each heating surface of the boiler is indirectly prolonged.
Description
Technical Field
The invention relates to an intelligent soot blowing algorithm based on Gu Erwei odd heat balance, and belongs to the field of intelligent algorithms.
Background
Electric energy is one of the most important energy sources in human civilization at present. At present, most of the electric energy production in China is from coal-fired power generation, however, during the combustion process of the coal-fired power generation unit, ash content in the coal-fired power generation unit can cause ash accumulation and slag bonding on the heating surface of the boiler, so that the heat transfer coefficient of the heating surface is reduced, the heat transfer efficiency of the heating surface is influenced, the temperature of main steam and reheated steam is reduced, the temperature of exhaust smoke is increased, the efficiency of the boiler is reduced, energy waste is caused, and even the safe operation of the unit can be damaged in severe cases. Therefore, in order to maximize the utilization of coal combustion energy, the heating surfaces of the boiler tubes must be cleaned and sootblown in time. The most reasonable and scientific soot blowing optimization strategy is formulated, so that the maximization of the heat transfer efficiency of the heating surface within a period of time can be ensured, and the energy conservation and emission reduction and the safe operation of the unit are realized.
At present, soot blowing operation of large power station boilers in China generally adopts a timed and quantitative program control mode. Because the operation mode is carried out under the condition that the actual soot-dirt state of the heating surface is not known, insufficient soot blowing or excessive soot blowing is inevitably generated, the soot blowing time and the soot blowing position are mostly determined by experience, and the soot blowing process has artificial subjectivity, thereby causing more coal consumption. The energy conservation and emission reduction at the present stage provides higher requirements for soot blowing optimization, and the coal-fired power plant can have better economic benefits only by predicting the future state and preparing in advance.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide an intelligent soot blowing algorithm based on Gu Erwei odd heat balance.
In order to achieve the purpose, the invention adopts the technical scheme that:
an intelligent soot blowing algorithm based on Gu Erwei odd heat balance comprises the following steps:
(1) Calculating theoretical Heat transfer coefficient K 0
Wherein:
a 1 ＝a d +a f
in the formula: a is 1 The heat release coefficient of the flue gas to the pipe wall is shown;
a 2 the heat release coefficient of the working medium to the pipe wall;
a d is the surface heat release coefficient;
a f is the radiative heat transfer coefficient;
C z 、C s respectively the correction coefficients of longitudinal and transverse tube rows in the airflow flowing direction;
lambda is the heat conductivity coefficient at the average temperature of the flue gas, W/(m DEG C);
d is the outer diameter of the pipe, m;
re and Pr are respectively the Relo number and the Plantt number of the smoke;
C l a correction coefficient for the relative length of the scoured heating surface;
C t is the fluid temperature and the tube wall temperature T gb The correction coefficient of (1).
σ 0 Boltzmann constant;
ε s the system blackness is obtained;
T gb and T is the tube wall temperature and the system temperature, K, respectively;
(2) Determining the temperature of the flue gas at the inlet of the heat exchanger by using a Gu Erwei odd heat balance intelligent algorithm;
calculating to obtain the heat absorption capacity and the heat release capacity of the working medium through the outlet flue gas temperature, the inlet working medium temperature, the outlet working medium temperature, the working medium mass flow and the assumed inlet flue gas temperature value, wherein each temperature can be converted into a corresponding enthalpy value, and when the checking error of the heat absorption capacity and the heat release capacity is less than 2% through an iterative algorithm based on a local heat balance principle, the assumed inlet flue gas temperature is the finally determined inlet flue gas temperature;
(3) Calculating the actual heat transfer coefficient K sj
Wherein:
Q z ＝D z (h”-h')
in the formula: q z The heat absorption capacity of the working medium is kJ/kg;
D z is the mass flow of inlet working medium, kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
a is the heat transfer area, m 2 ；
Δt max And Δ t min Respectively representing large temperature pressure and small temperature pressure;
wherein, during the counter flow, the temperature and pressure delta t are high max = J' -t "; at downstream, the large temperature and pressure Δ t max ＝J′-t′；
At the time of countercurrent, the small temperature pressure Deltat min = J "-t'; at downstream, the small temperature and pressure Δ t min ＝J″-t″；
J': inlet temperature of flue gas, DEG C; t': working medium outlet temperature, DEG C; j': flue gas exit temperature, deg.C; t': working medium inlet temperature, DEG C;
(4) Calculating the cleaning factor CF
When CF =1, the heated surface is in an ideal clean state, namely the clean factor of a smooth pipe; CF is less than 1, which indicates that the heating surface is polluted by ash, and the smaller the CF is, the more serious the pollution is;
the specific method of the step (2) is as follows:
1) Economizer inlet flue gas temperature algorithm
The economizer is divided into a superheater side and a reheater side through a flue gas baffle;
(1) reheater side economizer
The flue gas temperature and the flue gas enthalpy value are in one-to-one correspondence, the known temperature can obtain the enthalpy value through table lookup, and the known enthalpy value can obtain the temperature; assuming that the temperature of a flue gas inlet of an economizer at the side of a reheater is J';
reheater side economizer working medium heat absorption: q z ＝D z (h”-h')
Reheater-side economizer flue gas heat release: q y ＝m z (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m z the side-burning coal amount of the reheater is kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q is z -Q y If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
(2) superheater side economizer
Assuming that the temperature of a flue gas inlet of a superheater side economizer is J';
heat absorption capacity of working medium of a superheater side economizer: q z ＝D z (h”-h')
Flue gas heat release of a superheater side economizer: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m g the amount of coal is burned on the side of the superheater in kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q z -Q y If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
2) Algorithm for inlet flue gas temperature of horizontal section of low-temperature superheater
The outlet flue gas temperature of the horizontal section of the low-temperature superheater = the inlet flue gas temperature of a coal economizer on the superheater side, and the inlet flue gas temperature of the horizontal section of the low-temperature superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the inlet working medium of the low-temperature superheater is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m g the amount of coal fired on the superheater side is kg/s;
h 'and H' are respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.02Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
3) Algorithm for temperature of flue gas at vertical section inlet of low-temperature superheater
The temperature of a flue gas outlet of the vertical section of the low-temperature superheater = the temperature of a flue gas inlet of the horizontal section of the low-temperature superheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : the mass flow of the working medium at the inlet of the low-temperature superheater is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h ', H': respectively the enthalpy value of the flue gas inlet and the enthalpy value of the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj To add convective heat absorption, Q, to the heated surface fj ＝0.05Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
4) Algorithm for inlet flue gas temperature of horizontal section of low-temperature reheater
The temperature of a flue gas outlet of the horizontal section of the low-temperature reheater = the temperature of a flue gas inlet of an economizer on the side of the reheater, and the temperature of the flue gas inlet of the horizontal section of the low-temperature reheater is assumed to be J';
heat absorption capacity of working medium: q z ＝D z (h”-h')
Heat release of flue gas: q y ＝m z (H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m z : the side-burning coal amount of the reheater is kg/s;
h ', H': respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.015Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
5) Algorithm for inlet flue gas temperature of vertical section of low-temperature reheater
The temperature of a flue gas outlet of the vertical section of the low-temperature reheater = the temperature of a flue gas inlet of the horizontal section of the low-temperature reheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature reheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h ', H': respectively the enthalpy value of the flue gas inlet and the enthalpy value of the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.04Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
6) Algorithm for inlet flue gas temperature of high-temperature reheater
The high-temperature reheater flue gas outlet temperature = the low-temperature reheater vertical section flue gas inlet temperature, and the high-temperature reheater flue gas inlet temperature is assumed to be J';
heat absorption capacity of working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein: d z : reheater steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.06Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed temperature of the flue gas inlet is the finally determined inlet flue gas temperature, otherwise, the temperature of the flue gas inlet is assumed again for calculation until the calculation error is met;
7) Algorithm for inlet flue gas temperature of high-temperature superheater
The high-temperature superheater flue gas outlet temperature = the high-temperature reheater flue gas inlet temperature, and the high-temperature superheater flue gas inlet temperature is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : main steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj To add convective heat absorption, Q, to the heated surface fj ＝0.06Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
8) Algorithm for inlet flue gas temperature of platen superheater
The temperature of a flue gas outlet of the platen superheater = the temperature of a flue gas inlet of the high-temperature superheater, and the temperature of the flue gas inlet of the platen superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Total heat absorbed by the screen: q p ＝Q d p +Q f p
Convective heat absorption of the heated surface: q d p ＝Q y -Q d fj ，
Convection heat absorption of additional heating surface: q d fj ＝0.15Q z
Radiant heat absorbed by the screen: q f p ＝Q f -Q f fj
Direct radiation inside the furnace absorbed by the screen: q f ＝Q f ′-Q f ″
Direct radiation in the furnace obtained by the additional heating surface:
direct radiation in the furnace falling into the screen area:
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direct in-furnace radiation through the screen zone:
furnace outlet heat flow falling into the screen area:
heat absorption capacity of the hearth:
in the formula D z : steam entering platen superheaterFlow rate, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
f': the area of a smoke window at the outlet of the hearth and the square meter;
a: the blackness of the smoke;
x' p is the angular coefficient of the outlet cross section;
A ch the area of a smoke window at the outlet of the screen and the square meter;
T pj : average temperature of flue gas, K;
B j : total coal combustion amount, kg/s;
beta: the heat exchange coefficient between the hearth and the screen is increased;
eta: a coefficient of non-uniformity along the height of the hearth;
H 1 : the effective radiation heating area of the hearth and the square meter;
Q 1 : low calorific value, kJ/kg;
I 1 ", the smoke enthalpy at the outlet of the hearth, kJ/kg;
A fj : adding a heated area and a square meter;
s: the total heating area and the square meter;
calculating a checking error: q p -Q z
If Q is p -Q z If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met.
The invention has the beneficial effects that:
the cleaning Factor CF (Cleanliness Factor) can represent the pollution state of the convection heating surface, is a mark of the cleaning degree of the heating surface and is defined as the ratio of the actual heat transfer coefficient to the theoretical heat transfer coefficient. The dust deposition condition of each heating surface is usually monitored by calculating a cleaning factor, however, the calculation of the cleaning factor requires knowing the temperature of a flue gas inlet and outlet of each heating surface, and many power plants have no measuring point, so that the calculation of the cleaning factor is limited.
The invention utilizes Gu Erwei odd heat balance intelligent soot blowing algorithm, soft measurement technology based on local heat balance principle, and iterative algorithm, under the condition of known outlet flue gas temperature, inlet working medium temperature, outlet working medium temperature and working medium mass flow, when the checking error of heat absorption and heat release is less than 2%, the flue gas inlet temperature is calculated, and then the actual heat transfer coefficient, theoretical heat transfer coefficient and cleaning factor are calculated. The algorithm solves the problems of incomplete measuring points and the like, and saves the cost.
The intelligent soot blowing algorithm based on Gu Erwei odd heat balance can effectively monitor the pollution state of the heating surface of the boiler, determine the optimal soot blowing time, further maintain the cleanliness of the heating surface and improve the operation efficiency of the boiler. Meanwhile, soot blowing media are saved, corrosion and abrasion of the tube wall of the heating surface are reduced, and the service efficiency of each heating surface of the boiler is indirectly prolonged.
Drawings
FIG. 1 is a block diagram of an economizer (reheater side) inlet flue gas temperature algorithm;
FIG. 2 is a block diagram of an economizer (superheater side) inlet flue gas temperature algorithm;
FIG. 3 is a block diagram of an algorithm for inlet flue gas temperature of a horizontal section of a low-temperature superheater;
FIG. 4 is a block diagram of a low-temperature superheater vertical section inlet flue gas temperature algorithm;
FIG. 5 is a block diagram of a low temperature reheater horizontal section inlet flue gas temperature algorithm;
FIG. 6 is a block diagram of a low temperature reheater vertical section inlet flue gas temperature algorithm;
FIG. 7 is a block diagram of a high temperature reheater inlet flue gas temperature algorithm;
FIG. 8 is a block diagram of a high temperature superheater inlet flue gas temperature algorithm;
FIG. 9 is a block diagram of a platen superheater inlet flue gas temperature algorithm;
FIG. 10 is a flow chart of the Gu Erwei odd heat balance intelligent algorithm of the present invention.
Detailed Description
The following examples further illustrate the embodiments of the present invention in detail.
The units of heat and enthalpy values related in the formula of the invention are kJ/kg.
Examples
An intelligent soot blowing algorithm based on Gu Erwei odd heat balance comprises the following steps:
(1) Calculating theoretical heat transfer coefficient K 0
Wherein:
a 1 ＝a d +a f
in the formula: a is 1 The heat release coefficient of the flue gas to the pipe wall is shown;
a 2 the heat release coefficient of the working medium to the pipe wall;
a d is the surface heat release coefficient;
a f is the radiative heat transfer coefficient;
C z 、C s respectively the correction coefficients of the longitudinal and transverse tube rows in the airflow flowing direction;
lambda is the heat conductivity coefficient at the average temperature of the flue gas, W/(m DEG C);
d is the outer diameter of the pipe, m;
re and Pr are respectively the Relo number and the Plantt number of the smoke;
C l a correction coefficient for the relative length of the scoured heating surface;
C t is the fluid temperature and the tube wall temperature T gb And (5) correcting the coefficient.
σ 0 Boltzmann constant;
ε s the system blackness is obtained;
T gb and T is the tube wall temperature and the system temperature, K, respectively;
(2) Determining the temperature of the flue gas at the inlet of the heat exchanger by using a Gu Erwei odd heat balance intelligent algorithm;
calculating to obtain the heat absorption capacity and the heat release capacity of the working medium through the outlet flue gas temperature, the inlet working medium temperature, the outlet working medium temperature, the working medium mass flow and the assumed inlet flue gas temperature value, wherein each temperature can be converted into a corresponding enthalpy value, and when the checking error of the heat absorption capacity and the heat release capacity is less than 2% through an iterative algorithm based on a local heat balance principle, the assumed inlet flue gas temperature is the finally determined inlet flue gas temperature;
(3) Calculating the actual heat transfer coefficient K sj
Wherein:
Q z ＝D z (h”-h')
in the formula: q z kJ/kg is the heat absorption capacity of the working medium;
D z the mass flow of inlet working medium is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
a is the heat transfer area, m 2 ；
Δt max And Δ t min Respectively represent large temperature and pressure and small temperaturePressing;
wherein, during the counter flow, the temperature and pressure delta t are high max = J' -t "; at downstream, the large temperature and pressure Δ t max ＝J′-t′；
At the time of countercurrent, the small temperature pressure Deltat min = J "-t'; at downstream, the small temperature and pressure Δ t min ＝J″-t″；
J' is the temperature of the flue gas inlet, DEG C;
t': working medium outlet temperature, DEG C;
j' is the temperature of the smoke outlet at DEG C;
t': working medium inlet temperature, DEG C;
(4) Calculating the cleaning factor CF
When CF =1, the heated surface is in an ideal clean state, i.e., the cleaning factor of a smooth tube; a CF of less than 1 indicates that the heated surface is contaminated with soot, and the smaller the CF, the more serious the contamination.
The specific method for determining the temperature of the inlet flue gas of the heat exchanger through the Gu Erwei odd heat balance intelligent algorithm in the step (2) is as follows:
1) Economizer inlet flue gas temperature algorithm
The economizer is divided into a superheater side and a reheater side by a flue gas baffle.
(1) Economizer (reheater side)
The flue gas temperature and the flue gas enthalpy value are in one-to-one correspondence, the known temperature can obtain the enthalpy value through table lookup, and the known enthalpy value can obtain the temperature. Assume that the economizer (reheater side) flue gas inlet temperature is J'.
Economizer (reheater side) working medium heat absorption: q z ＝D z (h”-h')
Economizer (reheater side) flue gas heat release: q y ＝m z (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h 'and h' are respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m z the side-burning coal amount of the reheater is kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q z -Q y If the calculated temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met (as shown in fig. 1).
(2) Economizer (superheater side)
Assume that the economizer (superheater side) flue gas inlet temperature is J'.
Heat absorption capacity of working medium on the economizer (superheater side): q z ＝D z (h”-h')
Economizer (superheater side) flue gas heat release: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h 'and h' are respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m g the amount of coal is burned on the side of the superheater in kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q is z -Q y If the calculated temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met (as shown in fig. 2). 2) Algorithm for inlet flue gas temperature of horizontal section of low-temperature superheater
The outlet flue gas temperature of the horizontal section of the low-temperature superheater = the inlet flue gas temperature of the economizer (superheater side), and the inlet flue gas temperature of the horizontal section of the low-temperature superheater is assumed to be J'.
Heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the low-temperature superheater is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m g the amount of coal fired on the superheater side is kg/s;
h 'and H' are respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.02Q z
If Q is y -Q z -Q fj If the calculated smoke temperature is less than 2%, the assumed smoke inlet temperature is the finally determined inlet smoke temperature, otherwise, the smoke inlet temperature is assumed again for calculation until the calculation error is met (as shown in FIG. 3). 3) Algorithm for temperature of flue gas at vertical section inlet of low-temperature superheater
The temperature of the flue gas outlet of the vertical section of the low-temperature superheater = the temperature of the flue gas inlet of the horizontal section of the low-temperature superheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature superheater is assumed to be J'.
Heat absorption capacity of working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : the mass flow of the working medium at the inlet of the low-temperature superheater is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj To add convective heat absorption, Q, to the heated surface fj ＝0.05Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed temperature of the flue gas inlet is the finally determined temperature of the inlet flue gasOtherwise, the calculation is carried out again assuming the temperature of the smoke inlet until the calculation error is met (as shown in FIG. 4). 4) Algorithm for inlet flue gas temperature of horizontal section of low-temperature reheater
The outlet temperature of the flue gas at the horizontal section of the low-temperature reheater = the inlet temperature of the flue gas at the economizer (on the reheater side), and the inlet temperature of the flue gas at the horizontal section of the low-temperature reheater is assumed to be J'.
Heat absorption capacity of the working medium: q z ＝D z (h”-h')
Heat release of flue gas: q y ＝m z (H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m z : the side-burning coal amount of the reheater is kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q fj For additional heat transfer surface convection heat absorption, Q fj ＝0.015Q z
If Q y -Q z -Q fj If the calculated smoke temperature is less than 2%, the assumed smoke inlet temperature is the finally determined inlet smoke temperature, otherwise, the smoke inlet temperature is assumed again for calculation until the calculation error is met (as shown in FIG. 5). 5) Algorithm for inlet flue gas temperature of vertical section of low-temperature reheater
The temperature of the flue gas outlet of the vertical section of the low-temperature reheater = the temperature of the flue gas inlet of the horizontal section of the low-temperature reheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature reheater is assumed to be J'.
Heat absorption capacity of working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.04Q z
If Q is y -Q z -Q fj If the calculated smoke temperature is less than 2%, the assumed smoke inlet temperature is the finally determined inlet smoke temperature, otherwise, the smoke inlet temperature is assumed again for calculation until the calculation error is met (as shown in FIG. 6). 6) Algorithm for inlet flue gas temperature of high-temperature reheater
The high-temperature reheater flue gas outlet temperature = the low-temperature reheater vertical section flue gas inlet temperature, and the high-temperature reheater flue gas inlet temperature is assumed to be J'.
Heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein: d z : reheater steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.06Q z
If Q is y -Q z -Q fj If the calculated smoke temperature is less than 2%, the assumed smoke inlet temperature is the finally determined inlet smoke temperature, otherwise, the smoke inlet temperature is assumed again for calculation until the calculation error is met (as shown in FIG. 7). 7) Algorithm for inlet flue gas temperature of high-temperature superheater
The high-temperature superheater flue gas outlet temperature = the high-temperature reheater flue gas inlet temperature, and the high-temperature superheater flue gas inlet temperature is assumed to be J'.
Heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : main steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.06Q z
If Q y -Q z -Q fj If the calculated smoke temperature is less than 2%, the assumed smoke inlet temperature is the finally determined inlet smoke temperature, otherwise, the smoke inlet temperature is assumed again for calculation until the calculation error is met (as shown in FIG. 8). 8) Algorithm for inlet flue gas temperature of platen superheater
And (3) the flue gas outlet temperature of the platen superheater = the flue gas inlet temperature of the high-temperature superheater, and the flue gas inlet temperature of the platen superheater is assumed to be J'.
Heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Total heat absorbed by the screen: q p ＝Q d p +Q f p
Convective heat absorption of the heated surface: q d p ＝Q y -Q d fj ，
Convection heat absorption of additional heating surface: q d fj ＝0.15Q z
Radiant heat absorbed by the screen: q f p ＝Q f -Q f fj
Direct radiation inside the furnace absorbed by the screen: q f ＝Q f ′-Q f ″
Direct radiation in the furnace obtained by the additional heating surface:
direct radiation in the furnace falling into the screen area:
direct radiation in the furnace penetrating the screen area:
furnace outlet heat flow falling into the screen area:
/>
heat absorption capacity of the hearth:
in the formula D z : the steam flow entering the platen superheater is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h ', H': enthalpy values of a flue gas inlet and a flue gas outlet are kJ/kg;
f': the area of a smoke window at the outlet of the hearth and the square meter;
a: the blackness of the smoke;
x' p is the angular coefficient of the outlet cross section;
A ch the area of a smoke window at the outlet of the screen is square meter;
T pj : average temperature of flue gas, K;
B j : total coal combustion amount, kg/s;
beta: the heat exchange coefficient between the hearth and the screen is increased;
η: a coefficient of non-uniformity along the hearth height;
H 1 : the effective radiation heating area of the hearth and the square meter;
Q 1 : low calorific value, kJ/kg;
I 1 ", the enthalpy of the smoke at the outlet of the hearth is kJ/kg;
A fj : adding a heated area and a square meter;
s: the total heating area is square meter;
calculating a checking error: q p -Q z
If Q is p -Q z If the calculated temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met (as shown in fig. 9).
Claims (1)
1. An intelligent soot blowing algorithm based on Gu Erwei odd heat balance is characterized by comprising the following steps of: (1) Calculating theoretical heat transfer coefficient K 0
Wherein:
a 1 ＝a d +a f
in the formula: a is 1 For flue gas to pipeThe heat release coefficient of the wall;
a 2 the heat release coefficient of the working medium to the pipe wall is shown;
a d is the surface heat release coefficient;
a f is the radiative heat transfer coefficient;
C z 、C s respectively the correction coefficients of the longitudinal and transverse tube rows in the airflow flowing direction;
lambda is the heat conductivity coefficient at the average temperature of the flue gas, W/(m DEG C);
d is the outer diameter of the pipe, m;
re and Pr are respectively the Relode number and the Plantt number of the smoke;
C l a correction coefficient for the relative length of the scoured heating surface;
C t is the fluid temperature and the tube wall temperature T gb The correction coefficient of (1).
σ 0 Boltzmann constant;
ε s the system blackness is obtained;
T gb and T is the tube wall temperature and the system temperature, K, respectively;
(2) Determining the temperature of the inlet flue gas of the heat exchanger through a Gu Erwei odd heat balance intelligent algorithm;
calculating to obtain the heat absorption capacity and the heat release capacity of the working medium through the outlet flue gas temperature, the inlet working medium temperature, the outlet working medium temperature, the working medium mass flow and the assumed inlet flue gas temperature value, wherein each temperature can be converted into a corresponding enthalpy value, and when the checking error of the heat absorption capacity and the heat release capacity is less than 2% through an iterative algorithm based on a local heat balance principle, the assumed inlet flue gas temperature is the finally determined inlet flue gas temperature;
(3) Calculating the actual heat transfer coefficient K sj
Wherein:
Q z ＝D z (h”-h')
in the formula: q z The heat absorption capacity of the working medium is kJ/kg;
D z the mass flow of inlet working medium is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
a is the heat transfer area, m 2 ；
Δt max And Δ t min Respectively representing large temperature pressure and small temperature pressure;
wherein, during the counter flow, the temperature and pressure delta t are high max = J' -t "; at downstream, the large temperature and pressure Δ t max ＝J′-t′；
At the time of countercurrent, the small temperature pressure Deltat min = J "-t'; at downstream, the small temperature and pressure Δ t min ＝J″-t″；
J': flue gas inlet temperature, deg.C; t': working medium outlet temperature, DEG C; j': flue gas exit temperature, deg.C; t': working medium inlet temperature, DEG C;
(4) Calculating the cleaning factor CF
When CF =1, the heated surface is in an ideal clean state, i.e., the cleaning factor of a smooth tube; CF is less than 1, which indicates that the heating surface is polluted by ash, and the smaller the CF is, the more serious the pollution is;
the specific method of the step (2) is as follows:
1) Economizer inlet flue gas temperature algorithm
The economizer is divided into a superheater side and a reheater side through a flue gas baffle;
(1) reheater side economizer
The flue gas temperature and the flue gas enthalpy value are in one-to-one correspondence, the known temperature can obtain the enthalpy value through table lookup, and the known enthalpy value can obtain the temperature; assuming that the temperature of a flue gas inlet of a reheater-side economizer is J';
reheater side economizer working medium heat absorption: q z ＝D z (h”-h')
Heat release of flue gas of a reheater-side economizer: q y ＝m z (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m z the side-burning coal amount of the reheater is kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q is z -Q y If the temperature is less than 2%, the assumed temperature of the flue gas inlet is the finally determined inlet flue gas temperature, otherwise, the temperature of the flue gas inlet is assumed again for calculation until the calculation error is met;
(2) superheater side economizer
Assuming that the temperature of a flue gas inlet of an economizer on the superheater side is J';
heat absorption capacity of working medium of a superheater side economizer: q z ＝D z (h”-h')
Flue gas heat release of a superheater side economizer: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the economizer is kg/s;
h and h' are enthalpy values of the working medium outlet and the working medium inlet respectively, and kJ/kg;
m g the amount of coal is burned on the side of the superheater in kg/s;
h 'and H' are respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q z -Q y
If Q is z -Q y If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
2) Algorithm for inlet flue gas temperature of horizontal section of low-temperature superheater
The outlet flue gas temperature of the horizontal section of the low-temperature superheater = the inlet flue gas temperature of a coal economizer on the superheater side, and the inlet flue gas temperature of the horizontal section of the low-temperature superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m g (H'-H”)
Wherein: d z The mass flow of the working medium at the inlet of the low-temperature superheater is kg/s;
h 'and h' are respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m g the amount of coal fired on the superheater side is kg/s;
h 'and H' are respectively the enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.02Q z
If Q y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
3) Algorithm for temperature of flue gas at vertical section inlet of low-temperature superheater
The temperature of a flue gas outlet of the vertical section of the low-temperature superheater = the temperature of a flue gas inlet of the horizontal section of the low-temperature superheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : the mass flow of the working medium at the inlet of the low-temperature superheater is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj ，
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.05Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed temperature of the flue gas inlet is the finally determined inlet flue gas temperature, otherwise, the temperature of the flue gas inlet is assumed again for calculation until the calculation error is met;
4) Algorithm for inlet flue gas temperature of horizontal section of low-temperature reheater
The temperature of a flue gas outlet of the horizontal section of the low-temperature reheater = the temperature of a flue gas inlet of an economizer on the side of the reheater, and the temperature of the flue gas inlet of the horizontal section of the low-temperature reheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Heat release of flue gas: q y ＝m z (H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m z : the side-burning coal amount of the reheater is kg/s;
h', H ": respectively the enthalpy value of the flue gas inlet and the enthalpy value of the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj To add convective heat absorption, Q, to the heated surface fj ＝0.015Q z
If Q y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
5) Algorithm for inlet flue gas temperature of vertical section of low-temperature reheater
The temperature of a flue gas outlet of a vertical section of the low-temperature reheater is = the temperature of a flue gas inlet of a horizontal section of the low-temperature reheater, and the temperature of the flue gas inlet of the vertical section of the low-temperature reheater is assumed to be J';
heat absorption capacity of working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : mass flow of the low-temperature reheater inlet working medium is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h ', H': respectively the enthalpy value of the flue gas inlet and the enthalpy value of the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.04Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
6) Algorithm for inlet flue gas temperature of high-temperature reheater
The high-temperature reheater flue gas outlet temperature = the low-temperature reheater vertical section flue gas inlet temperature, and the high-temperature reheater flue gas inlet temperature is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein: d z : reheater steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": enthalpy values of a flue gas inlet and a flue gas outlet are kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.06Q z
If Q is y -Q z -Q fj Less than 2%, the assumed flue gas inlet temperature is the highest at this timeFinally determining the inlet flue gas temperature, otherwise, assuming the flue gas inlet temperature again for calculation until the calculation error is met;
7) Algorithm for inlet flue gas temperature of high-temperature superheater
The high-temperature superheater flue gas outlet temperature = the high-temperature reheater flue gas inlet temperature, and the high-temperature superheater flue gas inlet temperature is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Wherein D is z : main steam flow, kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": respectively the enthalpy values of the flue gas inlet and the flue gas outlet, kJ/kg;
calculating a checking error: q y -Q z -Q fj
Wherein Q is fj For additional heat transfer surface convection heat absorption, Q fj ＝0.06Q z
If Q is y -Q z -Q fj If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met;
8) Algorithm for inlet flue gas temperature of platen superheater
The temperature of a flue gas outlet of the platen superheater = the temperature of a flue gas inlet of the high-temperature superheater, and the temperature of the flue gas inlet of the platen superheater is assumed to be J';
heat absorption capacity of the working medium: q z ＝D z (h”-h')
Flue gas heat release: q y ＝m(H'-H”)
Total heat absorbed by the screen: q p ＝Q d p +Q f p
Convective heat absorption of the heated surface: q d p ＝Q y -Q d fj ，
Convection heat absorption of additional heating surface:Q d fj ＝0.15Q z
radiant heat absorbed by the screen: q f p ＝Q f -Q f fj
Direct radiation inside the furnace absorbed by the screen: q f ＝Q f ′-Q f ″
Direct in-furnace radiation obtained by additional heating surfaces:
direct radiation in the furnace falling into the screen area:
direct radiation in the furnace penetrating the screen area:
furnace outlet heat flow falling into the screen area:
heat absorption capacity of the hearth:
in the formula, D z : the steam flow entering the platen superheater is kg/s;
h ', h': respectively the enthalpy values of the working medium outlet and the working medium inlet, kJ/kg;
m: total coal combustion amount, kg/s;
h', H ": enthalpy values of a flue gas inlet and a flue gas outlet, kJ/kg;
f': the area of a smoke window at the outlet of the hearth and the square meter;
a: the blackness of the smoke;
x' p is the angular coefficient of the outlet cross section;
A ch the area of a smoke window at the outlet of the screen and the square meter;
T pj : levelling of flue gasesTemperature equalization, K;
B j : total coal combustion amount, kg/s;
beta: the heat exchange coefficient between the hearth and the screen is increased;
eta: a coefficient of non-uniformity along the height of the hearth;
H 1 : the effective radiation heating area of the hearth and the square meter;
Q 1 : low calorific value, kJ/kg;
I 1 ", the smoke enthalpy at the outlet of the hearth, kJ/kg;
A fj : adding a heated area and a square meter;
s: the total heating area and the square meter;
calculating a checking error: q p -Q z
If Q p -Q z If the temperature is less than 2%, the assumed flue gas inlet temperature is the finally determined inlet flue gas temperature, otherwise, the flue gas inlet temperature is assumed again for calculation until the calculation error is met.
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| CN104896457A (en) * | 2015-06-03 | 2015-09-09 | 华北电力科学研究院有限责任公司 | All-level boiler heating surface flue-gas temperature determination method and device |
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| JPH05264005A (en) * | 1992-01-21 | 1993-10-12 | Babcock Hitachi Kk | Computing device for boiler apparatus |
| CN105276563A (en) * | 2015-11-11 | 2016-01-27 | 东南大学 | Method for soft measurement of smoke temperature of outlet of hearth based on real-time slagging condition of hearth |
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