CN109655487B - Gas calorific value soft measurement method based on air and gas double preheating - Google Patents

Gas calorific value soft measurement method based on air and gas double preheating Download PDF

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CN109655487B
CN109655487B CN201811547915.9A CN201811547915A CN109655487B CN 109655487 B CN109655487 B CN 109655487B CN 201811547915 A CN201811547915 A CN 201811547915A CN 109655487 B CN109655487 B CN 109655487B
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air
temperature
flue gas
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CN109655487A (en
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王宏明
叶亚兰
安翔
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Jiangsu Maritime Institute
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Jiangsu Maritime Institute
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    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N25/00—Investigating or analyzing materials by the use of thermal means
    • G01N25/20—Investigating or analyzing materials by the use of thermal means by investigating the development of heat, i.e. calorimetry, e.g. by measuring specific heat, by measuring thermal conductivity
    • G01N25/22—Investigating or analyzing materials by the use of thermal means by investigating the development of heat, i.e. calorimetry, e.g. by measuring specific heat, by measuring thermal conductivity on combustion or catalytic oxidation, e.g. of components of gas mixtures
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Abstract

The invention relates to a gas heat value soft measurement method based on air and gas double preheating, which comprises the steps of obtaining real-time data of operating parameters of a combustion system; preprocessing the acquired data to obtain effective data for solving the gas heat value; calculating to obtain a coal gas dry basis heat value according to the obtained effective data; the method obtains the dry-based calorific value of the gas through the indirect solution of the relation between the dry air amount and the calorific value of the gas, is suitable for combustion equipment which adopts pure-burning blast furnace gas or pure-burning converter gas and adopts air and gas double preheating technology, can guide the combustion optimization and adjustment of the combustion equipment according to the calculation result, provides basis for the safe and economic operation of the combustion equipment, can solve the inconvenience and difficulty brought to the operation of the combustion equipment by not configuring a gas calorific value online analyzer in most of the gas combustion systems of steel plants at present, and has good engineering practical value.

Description

Gas calorific value soft measurement method based on air and gas double preheating
Technical Field
The invention relates to the technical field of energy conservation of combustion equipment, in particular to a gas heat value soft measurement method based on double preheating of air and gas.
Background
Iron and steel enterprises generate a large amount of by-product metallurgical gas in the production process, including blast furnace gas, converter gas, coke oven gas and the like, wherein the blast furnace gas and the converter gas have high heat value yield but low heat value, so that the high-efficiency utilization of the by-product metallurgical gas is always an important way for reducing cost, improving efficiency and improving market competitiveness of steel mills.
At present, blast furnace gas and converter gas are digested mainly by gas boilers, steel rolling heating furnaces, blast furnace hot blast stoves, ladle roasters and other equipment in steel mills. For these combustion equipments, the calorific value of the fuel is an important basis for adjusting the combustion and is an important input parameter of the thermal efficiency of the equipment, and the change and fluctuation of the calorific value of the fuel can have great influence on the safe and economic operation of the equipment. However, due to the limited conditions, most steel enterprises do not configure the combustion equipment with an online gas calorific value measuring device, and the steel mills basically still use the manual input of the regular laboratory analysis value as the current gas calorific value. In fact, under the influence of factors such as an upstream smelting process and the like, the components and the heat value of the coal gas are difficult to keep stable and are often in a fluctuation state, and the manually input regular test value is likely to greatly deviate from the current true value, so that the operation judgment of operators is disturbed to a great extent, and the optimized operation of the combustion equipment is influenced.
Therefore, a gas heat value soft measurement method based on operation parameters is provided for combustion equipment with double preheating of air and gas, the gas heat value is identified through the operation parameters of the combustion equipment, and the result can be used for guiding combustion optimization and adjustment of the combustion equipment, so that a basis is provided for safe and economic operation of the combustion equipment, and inconvenience and difficulty brought to operation due to the fact that most of the combustion equipment of the steel plant is not provided with a gas heat value online analyzer at present are solved.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a gas heat value soft measurement method based on double preheating of air and gas.
In order to achieve the purpose, the invention adopts the following technical scheme:
the gas calorific value soft measurement method based on air and gas double preheating is characterized by comprising the following steps: the combustion system is provided with an air preheater and a gas preheater, and the gas calorific value is obtained by obtaining the operating parameters of the combustion system and processing the operating parameters, and the method comprises the following specific steps:
step 1, acquiring real-time data of operating parameters of a combustion system;
step 2, preprocessing the data obtained in the step 1 to obtain effective data for solving the heat value of the coal gas;
and 3, solving the heat value of the coal gas according to the effective data obtained in the step 2, and specifically comprising the following steps:
step 3.1, assuming an initial gas dry basis heating value
Figure BDA00019092031500000219
Step 3.2, passing the assumed dry heat value of the coal gas
Figure BDA0001909203150000021
Calculating the theoretical dry air quantity required by each cubic meter of dry gas combustion
Figure BDA0001909203150000022
And the theoretical amount of dry flue gas generated by the combustion of dry gas per cubic meter
Figure BDA0001909203150000023
Step 3.3, calculating a fuel characteristic factor chi according to the theoretical dry air quantity and the theoretical dry flue gas quantity;
step 3.4, calculating an excess air coefficient alpha through the fuel characteristic factor;
step 3.5, calculating the actual dry flue gas volume V generated by the combustion of dry gas per cubic metergy；
Step 3.6, respectively calculating dry flue gas enthalpy, water vapor enthalpy, air enthalpy and coal gas enthalpy;
step 3.7, calculating the water vapor content in the flue gas generated by burning each cubic meter of dry gas
Figure BDA0001909203150000024
Step 3.8, calculating the dry air flow V flowing through the air preheater corresponding to each cubic meter of dry gasgk；
Step 3.9, calculating the dry heat value Q of the gasd；
Step 3.10, adding QdAnd
Figure BDA0001909203150000025
absolute value of the difference of (2)
Figure BDA0001909203150000026
Comparing with a set error limit epsilon:
when in use
Figure BDA0001909203150000027
When the error is larger than the error limit value epsilon, the gas dry-based heat value is assumed again
Figure BDA0001909203150000028
And performing step 3.2 to step 3.10 again when
Figure BDA0001909203150000029
When the error is less than or equal to the error limit value epsilon, outputting the gas dry-based heat value Qd。
The specific calculation steps of step 3.2 are as follows:
step 3.2.1, calculating the theoretical dry air quantity required by each cubic meter of dry gas combustion
Figure BDA00019092031500000210
The calculation formula is as follows:
Figure BDA00019092031500000211
wherein the content of the first and second substances,
Figure BDA00019092031500000212
the theoretical dry air quantity required for the combustion of each cubic meter of dry gas;
Figure BDA00019092031500000213
is the assumed dry heat value of the coal gas; a is1、b1Calculating a coefficient for the theoretical dry air amount;
step 3.2.2, calculating the theoretical dry flue gas amount generated by burning per cubic meter of dry gas
Figure BDA00019092031500000214
The calculation formula is as follows:
Figure BDA00019092031500000215
wherein the content of the first and second substances,
Figure BDA00019092031500000216
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure BDA00019092031500000217
is the assumed dry heat value of the coal gas; a is2、b2And calculating coefficients for the theoretical dry flue gas amount.
The specific calculation formula of the fuel property factor χ in the step 3.3 is as follows:
Figure BDA00019092031500000218
wherein χ is a fuel property factor;
Figure BDA0001909203150000031
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure BDA0001909203150000032
the theoretical amount of dry air required for the combustion of per cubic meter of dry gas.
The operation parameters collected in the step 1 include the oxygen content of the flue gas, and the calculation step of the excess air coefficient alpha in the step 3.4 is as follows:
Figure BDA0001909203150000033
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) Is the oxygen content of the flue gas;
when the operation parameters collected in the step 1 include the oxygen content of the flue gas and the content of CO in the flue gas, the oxygen content of the flue gas and the content of CO in the flue gas are dry flue gas components at the same measuring point position, and the calculation formula of the excess air coefficient α in the step 3.4 is as follows:
Figure BDA0001909203150000034
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) And phi' (CO) is the oxygen content of the flue gas and the CO content of the flue gas respectively.
The actual dry flue gas volume V generated by the combustion of each cubic meter of dry gas in the step 3.5gyThe calculation formula of (a) is as follows:
Figure BDA0001909203150000035
wherein, VgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure BDA0001909203150000036
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure BDA0001909203150000037
the theoretical dry air quantity required for the combustion of each cubic meter of dry gas; and alpha is the excess air factor.
The combustion system operation parameters collected in the step 1 include an air preheater flue gas side inlet temperature, an air preheater flue gas side outlet temperature, a gas preheater flue gas side inlet temperature, a gas preheater flue gas side outlet temperature, an air preheater air side inlet temperature, an air preheater air side outlet temperature, a gas preheater gas side inlet temperature and a gas preheater gas side outlet temperature, and the calculation methods of the dry flue gas enthalpy, the water vapor enthalpy, the air enthalpy and the gas enthalpy in the step 3.6 are as follows:
(1) respectively calculating the enthalpy values of the dry flue gas at the flue gas side inlet temperature of the air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of the gas preheater and the flue gas side outlet temperature of the gas preheater, wherein the calculation formula is as follows:
when blast furnace gas is taken as fuel, the calculation formula is as follows:
Figure BDA0001909203150000038
Figure BDA0001909203150000039
Figure BDA00019092031500000310
Figure BDA0001909203150000041
when converter gas is taken as fuel, the calculation formula is as follows:
Figure BDA0001909203150000042
Figure BDA0001909203150000043
Figure BDA0001909203150000044
Figure BDA0001909203150000045
wherein, theta1The temperature of the flue gas side inlet of the air preheater; theta2The temperature of the flue gas side outlet of the air preheater; theta3The temperature of the flue gas side inlet of the gas preheater is the temperature of the flue gas side inlet of the gas preheater; theta4The temperature of the flue gas side outlet of the gas preheater is set; hgy，1For dry flue gas at theta1Enthalpy at temperature; hgy，2For dry flue gas at theta2Enthalpy at temperature; hgy，3For dry flue gas at theta3Enthalpy at temperature; hgy，4For dry flue gas at theta4Enthalpy at temperature;
(2) respectively calculating the enthalpy values of the dry flue gas at the flue gas side inlet temperature of the air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of the gas preheater and the flue gas side outlet temperature of the gas preheater, wherein the calculation formula is as follows:
Figure BDA0001909203150000046
Figure BDA0001909203150000047
Figure BDA0001909203150000048
Figure BDA0001909203150000049
wherein, theta1The temperature of the flue gas side inlet of the air preheater; theta2The temperature of the flue gas side outlet of the air preheater; theta3The temperature of the flue gas side inlet of the gas preheater is the temperature of the flue gas side inlet of the gas preheater; theta4The temperature of the flue gas side outlet of the gas preheater is set;
Figure BDA00019092031500000412
is water vapor at theta1Enthalpy at temperature;
Figure BDA00019092031500000414
is water vapor at theta2Enthalpy at temperature;
Figure BDA00019092031500000415
is water vapor at theta3Enthalpy at temperature;
Figure BDA00019092031500000413
is water vapor at theta4Enthalpy at temperature;
(3) respectively calculating the enthalpy values of wet air corresponding to each cubic meter of dry air at the air side inlet temperature of the air preheater and the air side outlet temperature of the air preheater, wherein the calculation formula is as follows:
Figure BDA00019092031500000410
Figure BDA00019092031500000411
wherein, tk1Is the air preheater air side inlet temperature; t is tk2Is the air preheater air side outlet temperature; hk，1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature; hk，2Wet air at t for each cubic meter of dry airk2Enthalpy at temperature;
(4) respectively calculating the enthalpy values of wet coal gas corresponding to each cubic meter of dry coal gas at the coal gas side inlet temperature of the coal gas preheater and the coal gas side outlet temperature of the coal gas preheater, wherein the calculation formula is as follows:
for blast furnace gas, the calculation formula is:
Figure BDA0001909203150000051
Figure BDA0001909203150000052
for converter gas, the calculation formula is as follows:
Figure BDA0001909203150000053
Figure BDA0001909203150000054
wherein, tm1The gas side inlet temperature of the gas preheater is adopted; t is tm2The temperature of the coal gas side outlet of the coal gas preheater is set; hm，1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature; hm，2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature.
The combustion system operating parameters collected in the step 1 include local atmospheric pressure, atmospheric relative humidity, ambient temperature, gas pressure and gas temperature, and the calculation method for the absolute humidity of the air and the moisture content of the gas in the step 3.6 is as follows:
the absolute humidity d of the airkThe calculation formula of (2) is as follows:
Figure BDA0001909203150000055
wherein d iskIs the absolute humidity of the air; p is a radical ofaIs the local atmospheric pressure; phi is the atmospheric relative humidity; p is a radical ofsIs the ambient temperature t0Lower water vapor saturation pressure;
the moisture content d of the coal gasgThe calculation formula of (2) is as follows:
Figure BDA0001909203150000056
wherein d isgThe moisture content of the coal gas; p is a radical ofaIs the local atmospheric pressure; p is a radical ofgGas pressure (gauge pressure); p is a radical ofsIs the gas temperature tgLower saturated partial vapor pressure.
The amount of water vapor contained in the flue gas generated by the combustion of each cubic meter of dry gas in the step 3.7
Figure BDA0001909203150000057
The calculation formula of (a) is as follows:
Figure BDA0001909203150000061
wherein the content of the first and second substances,
Figure BDA0001909203150000062
the water vapor content in the flue gas generated by burning per cubic meter of dry gas; vgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas; hgy，3For dry flue gas at theta3Enthalpy at temperature; hgy，4For dry flue gas at theta4Enthalpy at temperature;
Figure BDA0001909203150000063
is water vapor at theta3Enthalpy at temperature;
Figure BDA0001909203150000064
is water vapor at theta4Enthalpy at temperature; hm，1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature; hm，2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature.
The dry air flow V flowing through the air preheater corresponding to each cubic meter of dry gas in the step 3.8gkThe calculation steps are as follows:
Figure BDA0001909203150000065
wherein, VgkThe dry air flow rate of the dry gas flowing through the air preheater is corresponding to each cubic meter of the dry gas; vgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure BDA0001909203150000066
the water vapor content in the flue gas generated by burning per cubic meter of dry gas; hgy，1For dry flue gas at theta1Enthalpy at temperature; hgy，2For dry flue gas at theta2Enthalpy at temperature;
Figure BDA0001909203150000067
is water vapor at theta1Enthalpy at temperature;
Figure BDA0001909203150000068
is water vapor at theta2Enthalpy at temperature; hk，1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature; hk，2Wet air at t for each cubic meter of dry airk2Temperature ofLower enthalpy value.
The dry basis heat value Q of the gas in the step 3.9dThe calculation formula of (a) is as follows:
Figure BDA0001909203150000069
wherein Q isdCalculating the dry heat value of the coal gas; vgkDry air flow through the air preheater for each cubic meter of dry gas); alpha is the excess air factor; delta alpha is an air leakage coefficient which is the air leakage coefficient after the air leakage of an upstream flue of a comprehensive hearth air leakage and flue gas oxygen content measuring point; k is a conversion coefficient.
The gas calorific value soft measurement method based on air and gas double preheating has the beneficial effects that:
firstly, the invention is suitable for the combustion equipment which is used for pure combustion of blast furnace gas or pure combustion of converter gas and adopts the air and gas double preheating technology, the soft measurement result of the gas heat value can be used for guiding the combustion optimization adjustment of the combustion equipment, a basis is provided for the safe and economic operation of the combustion equipment, the inconvenience and difficulty brought to the operation of the combustion equipment by not configuring a gas heat value online analyzer in most steel mill enterprises at present are solved, and the invention has good engineering practical value.
Second, the thermal value soft measurement result of the present invention has high accuracy and reliability.
Thirdly, the invention has small investment, low cost, can be realized without adding expensive thermal instruments and has good feasibility of implementation.
Drawings
FIG. 1 is a working flow chart of the gas calorific value soft measurement method based on air and gas double preheating.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings.
As shown in fig. 1, in the present embodiment, the gas combustion device has the following characteristics: pure blast furnace gas or pure converter gas is adopted and air and gas double preheating technology is adopted.
In the embodiment, the gas calorific value soft measurement method based on air and gas double preheating comprises the following specific implementation steps:
step 1, acquiring real-time data of operating parameters of a combustion system; the combustion system operating parameters obtained include, but are not limited to: flue gas oxygen content, local atmospheric pressure, atmospheric relative humidity, ambient temperature, gas pressure, gas temperature, air preheater flue gas side inlet temperature, air preheater flue gas side outlet temperature, gas preheater flue gas side inlet temperature, gas preheater flue gas side outlet temperature, air preheater air side inlet temperature, air preheater air side outlet temperature, gas preheater gas side inlet temperature, and gas preheater gas side outlet temperature.
Preferably, the measuring point position of the oxygen content of the flue gas is positioned in the flue between the flue gas side outlet of the air preheater and the flue gas side inlet of the gas preheater. Furthermore, if the flue gas side inlet of the gas preheater is close to the flue gas side outlet of the air preheater, only one of the temperature of the flue gas side outlet of the air preheater and the temperature of the flue gas side inlet of the gas preheater can be measured.
And 2, preprocessing the data obtained in the step 1 in a mode including but not limited to dead point processing and data smoothing processing to obtain effective data for solving the gas heat value.
And 3, solving the heat value of the coal gas according to the effective data obtained in the step 2, and specifically comprising the following steps:
step 3.1, assuming an initial gas dry basis low calorific value
Figure BDA0001909203150000071
Step 3.2, calculating the theoretical dry air quantity required by the combustion of each cubic meter of dry gas
Figure BDA0001909203150000072
And the theoretical amount of dry flue gas generated by the combustion of dry gas per cubic meter
Figure BDA0001909203150000073
The method comprises the following specific steps:
step 3.2.1, calculating the theoretical dry air quantity required by each cubic meter of dry gas combustion
Figure BDA0001909203150000074
The calculation formula is as follows:
Figure BDA0001909203150000075
wherein the content of the first and second substances,
Figure BDA0001909203150000076
theoretical amount of dry air, Nm, required for each cubic meter of dry gas combustion3/Nm3(dry gas);
Figure BDA0001909203150000077
is an assumed dry-based low calorific value of gas, kJ/Nm3；
For blast furnace gas, a1＝1.955×10-4，b10; for converter gas, a1＝1.858×10-4，b1＝0；
Step 3.2.2, calculating the theoretical dry flue gas amount generated by the combustion of dry gas per cubic meter, wherein the calculation formula is as follows:
Figure BDA0001909203150000081
wherein the content of the first and second substances,
Figure BDA0001909203150000082
theoretical amount of dry flue gas, Nm, produced per cubic meter of dry gas combustion3/Nm3(dry gas); qd，netIs the low calorific value of dry gas, kJ/Nm3；
For blast furnace gas, a2＝1.470×10-4，b21 is ═ 1; for converter gas, a2＝1.449×10-4，b2＝1。
And 3.3, calculating a fuel property factor chi, wherein the calculation formula is as follows:
Figure BDA0001909203150000083
wherein χ is a fuel characteristic factor χ;
Figure BDA0001909203150000084
theoretical amount of dry flue gas, Nm, produced per cubic meter of dry gas combustion3/Nm3(dry gas);
Figure BDA0001909203150000085
theoretical amount of dry air, Nm, required for each cubic meter of dry gas combustion3/Nm3(dry gas).
Step 3.4, calculating the excess air coefficient, wherein the calculation formula is as follows:
Figure BDA0001909203150000086
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) Is the oxygen content of the flue gas,%;
further preferably, when the operation parameters acquired in step 1 further include the CO content in the flue gas, at this time, the fourth calculation formula is changed to:
Figure BDA0001909203150000087
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) Phi' (CO) is the oxygen content of the flue gas and the CO content of the flue gas respectively;
the oxygen content of the smoke and the CO content in the smoke are dry smoke components at the same measuring point position.
Step 3.5, calculating the actual dry flue gas volume generated by the combustion of dry gas per cubic meter, wherein the calculation formula is as follows:
Figure BDA0001909203150000088
wherein, VgyThe actual dry flue gas quantity, Nm, generated by the combustion of dry gas per cubic meter3/Nm3(dry gas);
Figure BDA0001909203150000089
theoretical amount of dry flue gas, Nm, produced per cubic meter of dry gas combustion3/Nm3(dry gas);
Figure BDA00019092031500000810
theoretical amount of dry air, Nm, required for each cubic meter of dry gas combustion3/Nm3(dry gas); and alpha is the excess air factor.
Step 3.6, respectively calculating dry flue gas enthalpy, water vapor enthalpy, air enthalpy and coal gas enthalpy:
(1) respectively calculating enthalpy values of dry flue gas at the flue gas side inlet temperature of an air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of a coal gas preheater and the flue gas side outlet temperature of the coal gas preheater, wherein the calculation steps are as follows:
when blast furnace gas is used as fuel, the calculation formula is as follows:
Figure BDA0001909203150000091
Figure BDA0001909203150000092
Figure BDA0001909203150000093
Figure BDA0001909203150000094
when converter gas is used as fuel, the calculation formula is as follows:
Figure BDA0001909203150000095
Figure BDA0001909203150000096
Figure BDA0001909203150000097
Figure BDA0001909203150000098
wherein, theta1The temperature of the inlet at the flue gas side of the air preheater is DEG C; theta2The temperature of the flue gas side outlet of the air preheater is at the temperature of DEG C; theta3The temperature of the inlet at the flue gas side of the gas preheater is DEG C; theta4The temperature of the flue gas side outlet of the gas preheater is at the temperature of DEG C; hgy，1For dry flue gas at theta1Enthalpy at temperature, kJ/Nm3；Hgy，2For dry flue gas at theta2Enthalpy at temperature, kJ/Nm3；Hgy，3For dry flue gas at theta3Enthalpy at temperature, kJ/Nm3；Hgy，4For dry flue gas at theta4Enthalpy at temperature, kJ/Nm3；
(2) Respectively calculating enthalpy values of dry flue gas at the flue gas side inlet temperature of an air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of a coal gas preheater and the flue gas side outlet temperature of the coal gas preheater, wherein the calculation steps are as follows:
Figure BDA0001909203150000099
Figure BDA00019092031500000910
Figure BDA00019092031500000911
Figure BDA00019092031500000912
wherein, theta1The temperature of the inlet at the flue gas side of the air preheater is DEG C; theta2The temperature of the flue gas side outlet of the air preheater is at the temperature of DEG C; theta3The temperature of the inlet at the flue gas side of the gas preheater is DEG C; theta4The temperature of the flue gas side outlet of the gas preheater is at the temperature of DEG C;
Figure BDA00019092031500000913
is water vapor at theta1Enthalpy at temperature, kJ/Nm3；
Figure BDA00019092031500000914
Is water vapor at theta2Enthalpy at temperature, kJ/Nm3；
Figure BDA00019092031500000915
Is water vapor at theta3Enthalpy at temperature, kJ/Nm3；
Figure BDA00019092031500000916
Is water vapor at theta4Enthalpy at temperature, kJ/Nm3；
(3) Respectively calculating the enthalpy values of wet air corresponding to each cubic meter of dry air at the air side inlet temperature of the air preheater and the air side outlet temperature of the air preheater, wherein the calculation steps are as follows:
Figure BDA0001909203150000101
Figure BDA0001909203150000102
wherein, tk1Air side inlet temperature, deg.C, of the air preheater; t is tk2The air side outlet temperature of the air preheater is at DEG C; hk，1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature, kJ/Nm3；Hk，2Wet air at t for each cubic meter of dry airk2Enthalpy at temperature, kJ/Nm3；
(4) Respectively calculating the enthalpy values of wet coal gas corresponding to each cubic meter of dry coal gas at the coal gas side inlet temperature of the coal gas preheater and the coal gas side outlet temperature of the coal gas preheater, wherein the calculation steps are as follows:
for blast furnace gas, the calculation formula is as follows:
Figure BDA0001909203150000103
Figure BDA0001909203150000104
for converter gas, the calculation formula is as follows:
Figure BDA0001909203150000105
Figure BDA0001909203150000106
wherein, tm1The gas side inlet temperature of the gas preheater is DEG C; t is tm2The gas side outlet temperature of the gas preheater is DEG C; hm，1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature, kJ/Nm3；Hm，2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature, kJ/Nm3。
In this embodiment, the absolute air humidity and the gas moisture content required for calculation in step 3.6 may both be set values that are simplified, or may also be accurate values obtained by calculation, and when the absolute air humidity and the gas moisture content are obtained by calculation, the specific calculation steps are as follows:
calculating the absolute humidity d of the airkThe calculation formula is as follows:
Figure BDA0001909203150000107
wherein d iskAir absolute humidity, kg/kg (dry air); p is a radical ofaIs local atmospheric pressure, Pa; phi is atmospheric relative humidity,%; p is a radical ofsIs the ambient temperature t0Lower water vapor saturation pressure, Pa, passing ambient temperature t0Solving to obtain;
calculating the moisture content d of the gasgThe calculation formula is as follows:
Figure BDA0001909203150000108
wherein d isgIs the moisture content of the coal gas, kg/Nm3(dry gas); p is a radical ofaIs local atmospheric pressure, Pa; p is a radical ofgIs the gas pressure (gauge pressure), Pa; p is a radical ofsIs the gas temperature tgLower saturated water vapor partial pressure, Pa, passing gas temperature tgAnd (6) solving to obtain.
Step 3.7, calculating the water vapor content in the flue gas generated by burning each cubic meter of dry gas
Figure BDA0001909203150000111
The calculation formula is as follows:
Figure BDA0001909203150000112
wherein the content of the first and second substances,
Figure BDA0001909203150000113
the amount of water vapor, Nm, contained in the flue gas generated by the combustion of dry gas per cubic meter3/Nm3(dry gas); vgyThe actual dry flue gas quantity, Nm, generated by the combustion of dry gas per cubic meter3/Nm3(dry gas); hgy，3For dry flue gas at theta3Enthalpy at temperature, kJ/Nm3；Hgy，4For dry flue gas at theta4Enthalpy at temperature, kJ/Nm3；
Figure BDA0001909203150000114
Is water vapor at theta3Enthalpy at temperature, kJ/Nm3；
Figure BDA0001909203150000115
Is water vapor at theta4Enthalpy at temperature, kJ/Nm3；Hm，1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature, kJ/Nm3；Hm，2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature, kJ/Nm3。
Step 3.8, calculating the dry air flow V flowing through the air preheater corresponding to each cubic meter of dry gasgkThe calculation formula is as follows:
Figure BDA0001909203150000116
wherein, VgkDry air flow through the air preheater, Nm, for each cubic meter of dry gas3/Nm3；VgyThe actual dry flue gas quantity, Nm, generated by the combustion of dry gas per cubic meter3/Nm3(dry gas);
Figure BDA0001909203150000117
the amount of water vapor, Nm, contained in the flue gas generated by the combustion of dry gas per cubic meter3/Nm3(dry gas); hgy，1For dry flue gas at theta1Enthalpy at temperature, kJ/Nm3；Hgy，2Is driedFlue gas at theta2Enthalpy at temperature, kJ/Nm3；
Figure BDA0001909203150000119
Is water vapor at theta1Enthalpy at temperature, kJ/Nm3；
Figure BDA00019092031500001110
Is water vapor at theta2Enthalpy at temperature, kJ/Nm3；Hk，1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature, kJ/Nm3；Hk，2Wet air at t for each cubic meter of dry airk2Enthalpy at temperature, kJ/Nm3。
Step 3.9, calculating the dry-based low calorific value Q of the gasd，netThe calculation formula is as follows:
Figure BDA0001909203150000118
wherein Q isd，netCalculated value of low calorific value of coal gas dry basis, kJ/Nm3；VgkDry air flow through the air preheater, Nm, for each cubic meter of dry gas3/Nm3(dry gas); alpha is the excess air factor; delta alpha is an air leakage coefficient which is the air leakage coefficient after the air leakage of the upstream flue of the integrated hearth air leakage and flue gas oxygen content measuring point, the value of combustion equipment which runs at positive pressure for the hearth and the flue is 0, and the set value can be adopted for the combustion equipment which runs at negative pressure for the hearth and the flue; k is a conversion coefficient, and for blast furnace gas, k is 5122; for converter gas, k is 5381.
Step 3.10, adding Qd，netAnd
Figure BDA0001909203150000121
absolute value of the difference of (2)
Figure BDA0001909203150000122
Comparing with a set error limit epsilon:
when in use
Figure BDA0001909203150000123
When the error is larger than the set error limit value epsilon, the coal gas dry-based low calorific value is assumed again
Figure BDA0001909203150000124
And performing step 3.2 to step 3.10 again when
Figure BDA0001909203150000125
When the heat value is less than or equal to the set value epsilon, outputting the dry-based low-grade heat value Q of the gasd，net。
Further, when
Figure BDA0001909203150000126
If the error is larger than the set error limit value epsilon, the error will be
Figure BDA0001909203150000127
Assigning a value to said assumed dry basis lower heating value of the gas
Figure BDA0001909203150000128
Step 3.2 to step 3.10 are performed again until
Figure BDA0001909203150000129
Less than or equal to the set error limit epsilon.
In the embodiment, the gas heat value is solved by adopting a gas dry-based low-level heat value. In the specific implementation process, the gas calorific value can also be solved by adopting a gas dry-based high-level calorific value, and only the correlation coefficients of all the formulas are correspondingly adjusted.
The above is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above-mentioned embodiments, and all technical solutions belonging to the idea of the present invention belong to the protection scope of the present invention. It should be noted that modifications and embellishments within the scope of the invention may be made by those skilled in the art without departing from the principle of the invention.

Claims (9)

1. The gas calorific value soft measurement method based on air and gas double preheating is characterized by comprising the following steps: the combustion system is provided with an air preheater and a gas preheater, and the gas calorific value is obtained by obtaining the operating parameters of the combustion system and processing the operating parameters, and the method comprises the following specific steps:
step 1, acquiring real-time data of operating parameters of a combustion system;
step 2, preprocessing the data obtained in the step 1 to obtain effective data for solving the heat value of the coal gas;
and 3, solving the heat value of the coal gas according to the effective data obtained in the step 2, and specifically comprising the following steps:
step 3.1, assuming an initial gas dry basis heating value
Figure FDA0003060856170000011
Step 3.2, passing the assumed dry heat value of the coal gas
Figure FDA0003060856170000012
Calculating the theoretical dry air quantity required by each cubic meter of dry gas combustion
Figure FDA0003060856170000013
And the theoretical amount of dry flue gas generated by the combustion of dry gas per cubic meter
Figure FDA0003060856170000014
Step 3.3, calculating a fuel characteristic factor chi according to the theoretical dry air quantity and the theoretical dry flue gas quantity;
step 3.4, calculating an excess air coefficient alpha through the fuel characteristic factor;
step 3.5, calculating the actual dry flue gas volume V generated by the combustion of dry gas per cubic metergy；
Step 3.6, respectively calculating dry flue gas enthalpy, water vapor enthalpy, air enthalpy and coal gas enthalpy;
step 3.7, calculating the dry coal per cubic meterThe amount of water vapor contained in the flue gas generated by gas combustion
Figure FDA0003060856170000015
Step 3.8, calculating the dry air flow V flowing through the air preheater corresponding to each cubic meter of dry gasgk；
Step 3.9, calculating the dry heat value Q of the gasd；
Gas dry basis heating value QdThe calculation formula of (a) is as follows:
Figure FDA0003060856170000016
wherein Q isdCalculating the dry heat value of the coal gas; vgkThe dry air flow rate of the dry gas flowing through the air preheater is corresponding to each cubic meter of the dry gas; alpha is the excess air factor; delta alpha is an air leakage coefficient which is the air leakage coefficient after the air leakage of an upstream flue of a comprehensive hearth air leakage and flue gas oxygen content measuring point; k is a conversion coefficient;
step 3.10, adding QdAnd
Figure FDA0003060856170000017
absolute value of the difference of (2)
Figure FDA0003060856170000018
Comparing with a set error limit epsilon:
when in use
Figure FDA0003060856170000019
When the error is larger than the error limit value epsilon, the gas dry-based heat value is assumed again
Figure FDA00030608561700000110
And performing step 3.2 to step 3.10 again when
Figure FDA00030608561700000111
Less than or equal to errorWhen the difference value is epsilon, the dry heat value Q of the output gasd。
2. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 1, wherein: the specific calculation steps of step 3.2 are as follows:
step 3.2.1, calculating the theoretical dry air quantity required by each cubic meter of dry gas combustion
Figure FDA0003060856170000021
The calculation formula is as follows:
Figure FDA0003060856170000022
wherein the content of the first and second substances,
Figure FDA0003060856170000023
the theoretical dry air quantity required for the combustion of each cubic meter of dry gas;
Figure FDA0003060856170000024
is the assumed dry heat value of the coal gas; a is1、b1Calculating a coefficient for the theoretical dry air amount;
step 3.2.2, calculating the theoretical dry flue gas amount generated by burning per cubic meter of dry gas
Figure FDA0003060856170000025
The calculation formula is as follows:
Figure FDA0003060856170000026
wherein the content of the first and second substances,
Figure FDA0003060856170000027
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure FDA0003060856170000028
is the assumed dry heat value of the coal gas; a is2、b2And calculating coefficients for the theoretical dry flue gas amount.
3. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 2, wherein: the specific calculation formula of the fuel property factor χ in the step 3.3 is as follows:
Figure FDA0003060856170000029
wherein χ is a fuel property factor;
Figure FDA00030608561700000210
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure FDA00030608561700000211
the theoretical amount of dry air required for the combustion of per cubic meter of dry gas.
4. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 3, wherein: the operation parameters collected in the step 1 include the oxygen content of the flue gas, and the calculation formula of the excess air coefficient alpha in the step 3.4 is as follows:
Figure FDA00030608561700000212
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) Is the oxygen content of the flue gas;
when the operation parameters collected in the step 1 include the oxygen content of the flue gas and the content of CO in the flue gas, the oxygen content of the flue gas and the content of CO in the flue gas are dry flue gas components at the same measuring point position, and the calculation formula of the excess air coefficient α in the step 3.4 is as follows:
Figure FDA00030608561700000213
wherein, alpha is the excess air coefficient; χ is a fuel property factor; phi' (O)2) And phi' (CO) is the oxygen content of the flue gas and the CO content of the flue gas respectively.
5. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 4, wherein: the actual dry flue gas volume V generated by the combustion of each cubic meter of dry gas in the step 3.5gyThe calculation formula of (a) is as follows:
Figure FDA0003060856170000031
wherein, VgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure FDA0003060856170000032
the theoretical dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure FDA0003060856170000033
the theoretical dry air quantity required for the combustion of each cubic meter of dry gas; and alpha is the excess air factor.
6. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 5, wherein: the combustion system operation parameters collected in the step 1 include an air preheater flue gas side inlet temperature, an air preheater flue gas side outlet temperature, a gas preheater flue gas side inlet temperature, a gas preheater flue gas side outlet temperature, an air preheater air side inlet temperature, an air preheater air side outlet temperature, a gas preheater gas side inlet temperature and a gas preheater gas side outlet temperature, and the calculation methods of the dry flue gas enthalpy, the water vapor enthalpy, the air enthalpy and the gas enthalpy in the step 3.6 are as follows:
(1) respectively calculating the enthalpy values of the dry flue gas at the flue gas side inlet temperature of the air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of the gas preheater and the flue gas side outlet temperature of the gas preheater, wherein the calculation formula is as follows:
when blast furnace gas is taken as fuel, the calculation formula is as follows:
Figure FDA0003060856170000034
Figure FDA0003060856170000035
Figure FDA0003060856170000036
Figure FDA0003060856170000037
when converter gas is taken as fuel, the calculation formula is as follows:
Figure FDA0003060856170000038
Figure FDA0003060856170000039
Figure FDA00030608561700000310
Figure FDA00030608561700000311
wherein, theta1The temperature of the flue gas side inlet of the air preheater; theta2The temperature of the flue gas side outlet of the air preheater; theta3The temperature of the flue gas side inlet of the gas preheater is the temperature of the flue gas side inlet of the gas preheater; theta4The temperature of the flue gas side outlet of the gas preheater is set; hgy,1For dry flue gas at theta1Enthalpy at temperature; hgy,2For dry flue gas at theta2Enthalpy at temperature; hgy,3For dry flue gas at theta3Enthalpy at temperature; hgy,4For dry flue gas at theta4Enthalpy at temperature;
(2) respectively calculating the enthalpy values of the dry flue gas at the flue gas side inlet temperature of the air preheater, the flue gas side outlet temperature of the air preheater, the flue gas side inlet temperature of the gas preheater and the flue gas side outlet temperature of the gas preheater, wherein the calculation formula is as follows:
Figure FDA0003060856170000041
Figure FDA0003060856170000042
Figure FDA0003060856170000043
Figure FDA0003060856170000044
wherein, theta1The temperature of the flue gas side inlet of the air preheater; theta2The temperature of the flue gas side outlet of the air preheater; theta3The temperature of the flue gas side inlet of the gas preheater is the temperature of the flue gas side inlet of the gas preheater; theta4The temperature of the flue gas side outlet of the gas preheater is set;
Figure FDA0003060856170000045
is water vapor at theta1Enthalpy at temperature;
Figure FDA0003060856170000046
is water vapor at theta2Enthalpy at temperature;
Figure FDA0003060856170000047
is water vapor at theta3Enthalpy at temperature;
Figure FDA0003060856170000048
is water vapor at theta4Enthalpy at temperature;
(3) respectively calculating the enthalpy values of wet air corresponding to each cubic meter of dry air at the air side inlet temperature of the air preheater and the air side outlet temperature of the air preheater, wherein the calculation formula is as follows:
Figure FDA0003060856170000049
Figure FDA00030608561700000410
wherein, tk1Is the air preheater air side inlet temperature; t is tk2Is the air preheater air side outlet temperature; hk,1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature; hk,2Wet air at t for each cubic meter of dry airk2Enthalpy at temperature; dkIs the absolute humidity of the air;
(4) respectively calculating the enthalpy values of wet coal gas corresponding to each cubic meter of dry coal gas at the coal gas side inlet temperature of the coal gas preheater and the coal gas side outlet temperature of the coal gas preheater, wherein the calculation formula is as follows:
for blast furnace gas, the calculation formula is:
Figure FDA00030608561700000411
Figure FDA00030608561700000412
for converter gas, the calculation formula is as follows:
Figure FDA00030608561700000413
Figure FDA00030608561700000414
wherein, tm1The gas side inlet temperature of the gas preheater is adopted; t is tm2The temperature of the coal gas side outlet of the coal gas preheater is set; hm,1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature; hm,2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature; dgThe moisture content of the gas.
7. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 6, wherein: the operation parameters of the combustion system collected in the step 1 comprise local atmospheric pressure, atmospheric relative humidity, ambient temperature, gas pressure and gas temperature, and the calculation method of the absolute humidity of the air and the moisture content of the gas comprises the following steps:
the absolute humidity d of the airkThe calculation formula of (2) is as follows:
Figure FDA0003060856170000051
wherein d iskIs the absolute humidity of the air; p is a radical ofaIs the local atmospheric pressure(ii) a Phi is the atmospheric relative humidity; p is a radical ofsIs the ambient temperature t0Lower water vapor saturation pressure;
the moisture content d of the coal gasgThe calculation formula of (2) is as follows:
Figure FDA0003060856170000052
wherein d isgThe moisture content of the coal gas; p is a radical ofaIs the local atmospheric pressure; p is a radical ofgThe gas pressure is adopted; p is a radical ofsIs the gas temperature tgLower saturated partial vapor pressure.
8. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 6, wherein: the amount of water vapor contained in the flue gas generated by the combustion of each cubic meter of dry gas in the step 3.7
Figure FDA0003060856170000053
The calculation formula of (a) is as follows:
Figure FDA0003060856170000054
wherein the content of the first and second substances,
Figure FDA0003060856170000055
the water vapor content in the flue gas generated by burning per cubic meter of dry gas; vgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas; hgy,3For dry flue gas at theta3Enthalpy at temperature; hgy,4For dry flue gas at theta4Enthalpy at temperature;
Figure FDA0003060856170000056
is water vapor at theta3Enthalpy at temperature;
Figure FDA0003060856170000057
is water vapor at theta4Enthalpy at temperature; hm,1Wet gas at t for each cubic meter of dry gasm1Enthalpy at temperature; hm,2Wet gas at t for each cubic meter of dry gasm2Enthalpy at temperature.
9. The gas calorific value soft measurement method based on air and gas double preheating as claimed in claim 8, wherein: the dry air flow V flowing through the air preheater corresponding to each cubic meter of dry gas in the step 3.8gkThe calculation steps are as follows:
Figure FDA0003060856170000058
wherein, VgkThe dry air flow rate of the dry gas flowing through the air preheater is corresponding to each cubic meter of the dry gas; vgyThe actual dry flue gas amount generated by the combustion of each cubic meter of dry gas;
Figure FDA0003060856170000061
the water vapor content in the flue gas generated by burning per cubic meter of dry gas; hgy,1For dry flue gas at theta1Enthalpy at temperature; hgy,2For dry flue gas at theta2Enthalpy at temperature;
Figure FDA0003060856170000062
is water vapor at theta1Enthalpy at temperature;
Figure FDA0003060856170000063
is water vapor at theta2Enthalpy at temperature; hk,1Wet air at t for each cubic meter of dry airk1Enthalpy at temperature; hk,2Wet air at t for each cubic meter of dry airk2Enthalpy at temperature.
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