CN111477284B - Interactive cement production simulation method - Google Patents

Interactive cement production simulation method Download PDF

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CN111477284B
CN111477284B CN202010254672.0A CN202010254672A CN111477284B CN 111477284 B CN111477284 B CN 111477284B CN 202010254672 A CN202010254672 A CN 202010254672A CN 111477284 B CN111477284 B CN 111477284B
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张勤芳
诸华军
候海军
候贵华
蔡树元
罗驹华
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Abstract

The invention relates to an interactive cement production simulation method, and belongs to the field of computer simulation modeling. The interactive cement production simulation method comprises the steps of utilizing a computer modeling platform to model a combustion reaction process of a cement plant, utilizing an energy conservation law to model a heat transfer process of smoke and materials of the cement plant, and calculating heat of various components of the smoke and the materials in an enthalpy form; simulating the flow characteristics of the working medium in the cement plant, and calculating the flow and the flow speed of the working medium in the pipeline; the computer modeling platform is fed back and displayed on a process flow interface in an OPC communication mode to form a visual simulation interactive interface, and input cement production parameters are revised through the interactive interface so as to simulate the current cement production state. The invention further draws a process flow interface of the whole cement plant through the multidisciplinary simulation platform, and displays the modeling calculation result on the process flow interface through an OPC communication mode, thereby forming a visual interactive interface.

Description

Interactive cement production simulation method
Technical Field
The invention relates to an interactive cement production simulation method, and belongs to the field of computer simulation modeling.
Background
With the rapid development of economic society in China and the large-scale development of national infrastructure (freeways, bridges, airports and the like) and real estate, cement products become the most common building materials used to the maximum extent. The cement is an important building material in the construction of large-scale projects such as buildings, roads, bridges and the like, and the cement production system is a complex system which is restricted by a plurality of links such as material preparation, grinding, firing, control and the like. At present, the training of production personnel of a cement production line can only be a mode that a master has a brother, the master needs to learn the content, the brother can only listen to explanation and watch operation, actual operation cannot be carried out, the learning efficiency is poor, the learning time is long, and important phenomena and production parameters are often difficult to understand. The method is especially suitable for students in related professions of institutions, and the students can only study on books, so that the actual production parameter calculation process and method are difficult to understand.
Disclosure of Invention
The invention provides an interactive cement production simulation method aiming at the problems.
The invention adopts the following technical scheme:
the interactive cement production simulation method specifically comprises the following steps:
step (1), a computer modeling platform is utilized to model the combustion reaction process of a cement plant,
the computer modeling platform utilizes a Mendeleev calorific value formula to calculate and obtain the application base high-order calorific value of the coal powder;
calculating the latent heat of vaporization and heat absorption of the water vapor by using an average density method, and calculating the mass content of each component in the generated flue gas, wherein the mass content comprises the pulverized coal amount, the air amount, the moisture and the heat brought in; calculating the amount of pulverized coal, air quantity, moisture and heat brought in by the law of conservation of energy; carrying out function calculation on the obtained pulverized coal quantity, air quantity, moisture, introduced heat and output parameters of combustion products;
modeling the heat transfer process of the flue gas and the materials of the cement plant by utilizing an energy conservation law, and calculating the heat of various components of the flue gas and the materials in an enthalpy form;
simulating the flow characteristics of the working medium in the cement plant, and calculating the flow and the flow speed of the working medium in the pipeline;
and (4) the computer modeling platform feeds back and displays the calculation results obtained in the step (1), the step (2) and the step (3) on a process flow interface in an OPC communication mode to form a visual simulation interactive interface, and input cement production parameters are revised through the interactive interface so as to simulate the current cement production state.
The interactive cement production simulation method disclosed by the invention has the following specific steps of modeling the combustion reaction process of a cement plant in the step (1):
step (1a), carrying out component analysis on the coal powder according to an application base:
Car+Har+Oar+Nar+Sar+Mar+Aar＝1
wherein, Car is the content of carbon element, Har is the content of hydrogen element, Oar is the content of oxygen element, Nar is the content of nitrogen element, Sar is the content of sulfur element, Mar is the content of moisture, Aar is the content of ash;
step (1b), obtaining a coal powder combustion heat productivity formula according to the Mendeleev heat productivity formula:
Qar＝K·100.0·(339.0·Car+1030.0·Har-109.0·(Oar-Sar)-25.0·Mar)
wherein Qar is the calorific value of coal powder, and the unit kJ/kg; k is a high calorific value coefficient;
step (1c), calculating a pulverized coal combustion efficiency formula according to the excess air coefficient:
η＝(Har/4.0+Sar/32.0+Car/12.0-Oar/32.0)*32.0
wherein eta is the combustion efficiency of the pulverized coal;
step (1d), calculating the mass flow of each component of the combusted smoke according to an average density method:
MNO＝VNO30.0, wherein MNOMass flow of NO in kg/s; vNOIs the molar volume flow of NO;
MN2＝VN228.0, wherein MN2Is N2Mass flow of (2), unit kg/s; vN2Is N2Molar volume flow of (c);
MCO2＝VCO244.0, wherein MCO2Is CO2Mass flow of (2), unit kg/s; vCO2Is CO2Molar volume flow of (c);
MCO＝VCO28.0, wherein MCOIs COMass flow of (2), unit kg/s; vCOIs the molar volume flow of CO;
MSO2＝VSO264.0, wherein MSO2Is SO2Mass flow of (2), unit kg/s; vSO2Is SO2Molar volume flow of (c);
MO2＝VO232.0, wherein MO2Is O2Mass flow of (2), unit kg/s; vO2Is O2Molar volume flow of (c);
Mh＝Vh18.0, wherein MhThe mass flow of the water vapor is unit kg/s; vhIs the molar volume flow of water vapor;
step (1e), calculating the flue gas temperature after pulverized coal combustion by a mass flow method:
Figure BDA0002436823420000021
Figure BDA0002436823420000022
wherein HfIs the enthalpy value of the flue gas, MairFor the mass flow of the incoming cold air HairFor the enthalpy of the incoming cold air, MmMass flow of pulverized coal injected before combustion, HmEnthalpy value, T, of coal dust injected before combustionfIs the flue gas temperature, P is the current gas pressure, CpThe specific heat capacity of the flue gas is;
the interactive cement production simulation method provided by the invention has the advantages that the modeling of the heat transfer process of the flue gas and the materials of the cement plant in the step (2) specifically comprises the following steps:
step (2a), calculating the convective heat transfer coefficient:
Figure BDA0002436823420000031
wherein, Kf1For heat convectionCoefficient, FmIs the mass flow of the material, FarIs the mass flow of the flue gas;
step (2b), calculating the heat conduction and heat exchange coefficient:
Kf2＝0.000698+Fm*0.00064，
wherein, Kf2Is the heat conduction and heat exchange coefficient;
and (2c) calculating coefficients of two heat exchange modes of convection and heat conduction as a total heat exchange coefficient:
Kf＝1/Kf1+1/Kf2；
step (2d), calculating the heat transfer rate:
Figure BDA0002436823420000032
step (2e), calculating the heat exchange quantity:
Qf＝Kf·Far·Sf·(Tar-Tm)
in the formula, TarIs the temperature of the flue gas, TmIs the temperature of the material.
The interactive cement production simulation method comprises the following steps of (3) calculating the flow and the flow speed of the working medium in the pipeline:
step (3a), determining a resistance loss calculation formula:
Figure BDA0002436823420000033
Figure BDA0002436823420000034
wherein h isfThe length loss of the liquid column caused by resistance is unit m; Δ P is fluid pressure loss due to resistance, in Pa; λ is the drag loss coefficient; l is the length of the pipeline in m; rho is the valve inlet steam density in kg/m3(ii) a d is the pipe diameter in m; v is the fluid flowSpeed, unit m/s; q is fluid mass flow rate, unit kg/s; g is the acceleration of gravity;
step (3b), defining the pipeline circulation capacity adm, and deducing an adm calculation formula:
Figure BDA0002436823420000041
wherein Q is liquid mass flow rate, unit kg/s; rho is the valve inlet steam density in kg/m3(ii) a dP is the pressure difference between the inlet and the outlet of the valve, and the unit is MPa;
step (3c), obtaining the linear relation between the flow and the circulation capacity by inputting the pressure difference between an inlet and an outlet of a pipeline or a valve and the density of the working medium; and obtaining the circulation capacity according to the pipeline size data, and further calculating the flow and the flow speed in the pipeline.
Advantageous effects
The interactive cement production simulation method provided by the invention carries out modeling calculation on three key problems of combustion, heat transfer and working medium flow related in a cement plant, forms high-precision cement production state numerical simulation, and further expresses the production state of the cement plant at the present stage; and drawing a process flow interface of the whole cement plant by using a multidisciplinary simulation platform, and displaying a modeling calculation result on the process flow interface in an OPC communication mode to form a visual interactive interface.
Drawings
FIG. 1 is a schematic diagram of a simulation method framework of the present invention;
FIG. 2 is a diagram of a simulation setup produced using the simulation method of the present invention;
FIG. 3 is a schematic diagram of the operation architecture of the simulation method of the present invention;
FIG. 4 is a schematic diagram of the series control of incompressible fluid valves according to the simulation method of the present invention;
FIG. 5 is a schematic diagram of the parallel control of incompressible fluid valves according to the simulation method of the present invention;
FIG. 6 is a schematic diagram of a compressible fluid valve tandem control of the simulation method of the present invention;
FIG. 7 is a schematic diagram of a compressible fluid valve parallel control of the simulation method of the present invention.
Detailed Description
In order to make the purpose and technical solution of the embodiments of the present invention clearer, the technical solution of the embodiments of the present invention will be clearly and completely described below with reference to the drawings of the embodiments of the present invention. It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the described embodiments of the invention without any inventive step, are within the scope of protection of the invention.
As shown in fig. 1: an interactive simulation method for cement production features that the mathematical model-building calculation is performed on the three core links of combustion, heat transfer and working medium flow in cement plant. And converting the mathematical algorithm into a computer algorithm by using PowerBuilder software, and generating a computer executable program and a database. And (3) applying Gview software, and communicating the calculation result to an operation interface of cement production through a database to form an interactive operation simulation mode.
The method comprises the following steps that (1) the computer modeling platform utilizes a Mendeleev calorific value formula to calculate and obtain the application base high-order calorific value of the coal powder; calculating the latent heat of vaporization and heat absorption of the water vapor by using an average density method, and calculating the mass content of each component in the generated flue gas, wherein the mass content comprises the pulverized coal amount, the air amount, the moisture and the heat brought in; calculating the amount of pulverized coal, air quantity, moisture and heat brought in by the law of conservation of energy; carrying out function calculation on the obtained pulverized coal quantity, air quantity, moisture, introduced heat and output parameters of combustion products;
step (1a), carrying out component analysis on the coal powder according to an application base:
Car+Har+Oar+Nar+Sar+Mar+Aar＝1
wherein, Car is the content of carbon element, Har is the content of hydrogen element, Oar is the content of oxygen element, Nar is the content of nitrogen element, Sar is the content of sulfur element, Mar is the content of moisture, Aar is the content of ash;
step (1b), obtaining a coal powder combustion heat productivity formula according to the Mendeleev heat productivity formula:
Qar＝K·100.0·(339.0·Car+1030.0·Har-109.0·(Oar-Sar)-25.0·Mar)
wherein Qar is the calorific value of coal powder, and the unit kJ/kg; k is a high calorific value coefficient;
step (1c), calculating a pulverized coal combustion efficiency formula according to the excess air coefficient:
η＝(Har/4.0+Sar/32.0+Car/12.0-Oar/32.0)*32.0
wherein eta is the combustion efficiency of the pulverized coal;
step (1d), calculating the mass flow of each component of the combusted smoke according to an average density method:
MNO＝VNO30.0, wherein MNOMass flow of NO in kg/s; vNOIs the molar volume flow of NO;
MN2＝VN228.0, wherein MN2Is N2Mass flow of (2), unit kg/s; vN2Is N2Molar volume flow of (c);
MCO2＝VCO244.0, wherein MCO2Is CO2Mass flow of (2), unit kg/s; vCO2Is CO2Molar volume flow of (c);
MCO＝VCO28.0, wherein MCOMass flow of CO in kg/s; vCOIs the molar volume flow of CO;
MSO2＝VSO264.0, wherein MSO2Is SO2Mass flow of (2), unit kg/s; vSO2Is SO2Molar volume flow of (c);
MO2＝VO232.0, wherein MO2Is O2Mass flow of (2), unit kg/s; vO2Is O2Molar volume flow of (c);
Mh＝Vh18.0, wherein MhThe mass flow of the water vapor is unit kg/s; vhIs the molar volume flow of water vapor;
step (1e), calculating the flue gas temperature after pulverized coal combustion by a mass flow method:
Figure BDA0002436823420000061
Figure BDA0002436823420000062
wherein HfIs the enthalpy value of the flue gas, MairFor the mass flow of the incoming cold air HairFor the enthalpy of the incoming cold air, MmMass flow of pulverized coal injected before combustion, HmEnthalpy value, T, of coal dust injected before combustionfIs the flue gas temperature, P is the current gas pressure, CpIs the specific heat capacity of the flue gas.
Therefore, the outlet flue gas temperature can be calculated by the formula as long as the application base analysis of the pulverized coal, the inlet air flow and the inlet pulverized coal parameters are input.
The heat transfer process of the flue gas and the materials in the cement plant calculates the heat of various components of the flue gas and the materials in an enthalpy mode by utilizing the law of energy conservation. Taking any section, taking an inlet and an outlet as calculation intercept points, and establishing an energy equation before and after heat transfer of each component because the inlet and the outlet are in energy conservation. A physical library of heat transfer coefficients of smoke and components of materials is established, when the components of the materials or the components of the smoke change, the current heat transfer coefficients can be rapidly calculated, endothermic and exothermic reactions of the components in the materials are fully considered, and the temperature of the materials and the smoke after heat transfer is finally obtained.
Modeling the heat transfer process of the flue gas and the materials of the cement plant by utilizing an energy conservation law, and calculating the heat of various components of the flue gas and the materials in an enthalpy form;
step (2a), calculating the convective heat transfer coefficient:
Figure BDA0002436823420000063
wherein, Kf1To convective heat transfer coefficient, FmIs the mass flow of the material, FarIs the mass flow of the flue gas;
step (2b), calculating the heat conduction and heat exchange coefficient:
Kf2＝0.000698+Fm*0.00064，
wherein, Kf2Is the heat conduction and heat exchange coefficient;
and (2c) calculating coefficients of two heat exchange modes of convection and heat conduction as a total heat exchange coefficient:
Kf＝1/Kf1+1/Kf2；
step (2d), calculating the heat transfer rate:
Figure BDA0002436823420000064
calculating the heat exchange amount:
Qf＝Kf·Far·Sf·(Tar-Tm)
in the formula, TarIs the temperature of the flue gas, TmIs the temperature of the material.
The simulation of the flow characteristic of the working medium in the cement plant is mainly the flow characteristic of the flue gas in the pipeline. The fluid mechanics formula is simplified, the local resistance loss and the on-way resistance loss are uniformly converted into the circulation capacity of the pipeline, and the flow speed of the working medium in the pipeline can be calculated only by inputting the pressure values and the circulation capacity values of the inlet and the outlet of the pipeline. The calculation process is simple and efficient.
Simulating the flow characteristics of the working medium in the cement plant, and calculating the flow and the flow speed of the working medium in the pipeline;
determining a resistance loss calculation formula in the step (3 a):
Figure BDA0002436823420000071
Figure BDA0002436823420000072
wherein h isfThe length loss of the liquid column caused by resistance is unit m; Δ P is fluid pressure loss due to resistance, in Pa; λ is the drag loss coefficient; l is the length of the pipeline in m; rho is the valve inlet steam density in kg/m3(ii) a d is the pipe diameter in m; v is the flow velocity of the fluid in m/s; q is fluid mass flow rate, unit kg/s;
step (3b), defining the pipeline circulation capacity adm, and deducing an adm calculation formula:
Figure BDA0002436823420000073
wherein Q is liquid mass flow rate, unit kg/s; rho is the valve inlet steam density in kg/m3(ii) a And dP is the pressure difference between the inlet and the outlet of the valve and is unit MPa.
And (4) the computer modeling platform feeds back and displays the calculation results obtained in the step (1), the step (2) and the step (3) on a process flow interface in an OPC communication mode to form a visual simulation interactive interface, and input cement production parameters are revised through the interactive interface so as to simulate the current cement production state.
Simulating the pressure difference of an inlet and an outlet of an input pipeline or a valve and the density of a working medium in the current cement production state to obtain the linear relation between the flow and the flow capacity; and obtaining the circulation capacity according to the pipeline size data, and further calculating the flow and the flow speed in the pipeline. The linear relation between the flow and the flow capacity can be obtained only by inputting the pressure difference between the inlet and the outlet of the pipeline or the valve and the density of the working medium. The flow capacity can be obtained by the size data of the pipeline, and the flow rate and the flow velocity in the pipeline are further calculated.
From the definition of the flow-through capability adm, it can be seen that:
Figure BDA0002436823420000081
wherein: q-liquid mass flow kg/s;
rho-valve inlet steam density kg/m3；
dp-pressure difference MPa between inlet and outlet of valve.
Liquid adm conversion:
Figure BDA0002436823420000082
the unit conversion is performed on the formula (2-2):
Figure BDA0002436823420000083
wherein: q. q.sm-liquid mass flow kg/h;
rho-valve inlet steam density kg/m3；
dp-pressure difference MPa between inlet and outlet of valve.
Figure BDA0002436823420000084
Wherein: q-liquid mass flow kg/s.
Then, as can be deduced from equation (2-4):
Figure BDA0002436823420000085
obtainable from the formulae (2-1) (2-5):
Figure BDA0002436823420000086
steam adm conversion:
from equation (2-3):
Figure BDA0002436823420000091
wherein: q. q.smQuality of the liquidThe flow is kg/h;
rho-valve inlet steam density kg/m3；
Delta p is the pressure difference KPa between the inlet and the outlet of the valve.
For non-choked flow, the steam flow coefficient K 'was calculated by the coefficient of expansion method'VThe formula of (1) is:
Figure BDA0002436823420000092
wherein: gS-liquid mass flow kg/h;
y-coefficient of expansion.
The results from equations (2-7) (2-8) are:
KV＝K′V*y (2-9)
then from equations (2-6) (2-9):
Figure BDA0002436823420000093
for choked flow, K is calculated using the expansion coefficient methodVThe formula for the value is:
Figure BDA0002436823420000094
wherein: xT-critical pressure difference ratio coefficient.
The results from equations (2-7) (2-11) are:
Figure BDA0002436823420000095
wherein: x-the pressure difference ratio of the mixture,
Figure BDA0002436823420000096
then, from equations (2-6) (2-12):
Figure BDA0002436823420000101
as shown in fig. 5: the valve is equivalent to a serial and parallel adm: calculating formula according to Kv value of valve
Figure BDA0002436823420000102
The pipelines are connected in series, and the flow through the valves is equal; and the fluid density can be considered constant due to the incompressible fluid.
For valve 1 there are:
Figure BDA0002436823420000103
then
Figure BDA0002436823420000104
For valve 2 there are:
Figure BDA0002436823420000105
then
Figure BDA0002436823420000106
If the valves 1, 2 are equivalent to one valve, then there are:
Figure BDA0002436823420000107
then
Figure BDA0002436823420000108
Substituting formula (3-1) (3-2) into (3-3):
Figure BDA0002436823420000109
is finished to obtain
Figure BDA00024368234200001010
Can be pushed out by the formula (3-4)
Figure BDA00024368234200001011
As shown in fig. 5: when the valves are connected in parallel, adm is equivalent: parallel pipelines, the pressure drop through the valves is equal; q. q.sV＝qV1+qV2. And the fluid density can be considered constant due to the incompressible fluid.
For valve 1 there are:
Figure BDA0002436823420000111
then
Figure BDA0002436823420000112
For valve 2 there are:
Figure BDA0002436823420000113
then
Figure BDA0002436823420000114
If the valves 1, 2 are equivalent to one valve, then there are:
Figure BDA0002436823420000115
then
Figure BDA0002436823420000116
Substituting the formula (3-6), (3-7) and (3-8) into qV＝qV1+qV2：
Figure BDA0002436823420000117
Is finished to obtain
Kv＝Kv1+Kv2 (3-9)
As shown in fig. 6: compressible fluid valve series connection according to valve Kv value calculation formula (2-8)
Figure BDA0002436823420000118
The pipelines are connected in series, and the flow through the valves is equal; the system pressure drop is equal to Δ p1 +/Δ p 2.
For valve 1 there are:
Figure BDA0002436823420000119
then
Figure BDA00024368234200001110
For valve 2 there are:
Figure BDA0002436823420000121
then
Figure BDA0002436823420000122
If the valves 1, 2 are equivalent to one valve, then there are:
Figure BDA0002436823420000123
substituting formula (3-10) (3-11) into (3-12):
Figure BDA0002436823420000124
can be pushed out by the formula (16)
Figure BDA0002436823420000125
As shown in fig. 7: parallel pipelines, the pressure drop through the valves is equal; q. q.sV＝qV1+qV2。
For valve 1 there are:
Figure BDA0002436823420000126
then
Figure BDA0002436823420000127
For valve 2 there are:
Figure BDA0002436823420000128
then
Figure BDA0002436823420000129
If the valves 1, 2 are equivalent to one valve, then there are:
Figure BDA00024368234200001210
then
Figure BDA00024368234200001211
Substituting the formula (3-15), (3-16) and (3-17) into qV＝qV1+qV2：
Figure BDA0002436823420000131
Is finished to obtain
Kv＝Kv1+Kv2 (3-18)
Through the three modeling modes, the temperature, pressure and flow information of the smoke and materials of any working section of the cement plant can be clearly calculated, and the production state of the cement plant at the current stage is further expressed. The technological process interface of the whole cement plant is drawn through a multidisciplinary simulation platform, the modeling calculation result is displayed on the technological process interface in an OPC communication mode, a visual interactive interface is formed, cement production parameters can be directly input on the interactive interface, and then the current cement production state is calculated.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.

Claims (3)

1. An interactive cement production simulation method is characterized by specifically comprising the following steps:
step (1), a computer modeling platform is utilized to model the combustion reaction process of a cement plant,
the computer modeling platform utilizes a Mendeleev calorific value formula to calculate and obtain the application base high-order calorific value of the coal powder;
calculating each component of the generated flue gas by using an average density method to obtain the mass content of each component, wherein the mass content comprises the coal powder amount, the air amount and the moisture; then calculating the quantity of pulverized coal, the air quantity and the heat brought by each component of water through an energy conservation law; performing function calculation on the obtained pulverized coal quantity, air quantity, moisture, introduced heat and output parameters of combustion products;
the modeling aiming at the combustion reaction process of the cement plant specifically comprises the following steps:
step (1a), carrying out component analysis on the coal powder according to an application base:
Car+Har+Oar+Nar+Sar+Mar+Aar＝1
wherein, Car is the content of carbon element, Har is the content of hydrogen element, Oar is the content of oxygen element, Nar is the content of nitrogen element, Sar is the content of sulfur element, Mar is the content of moisture, Aar is the content of ash;
step (1b), obtaining a coal powder combustion heat productivity formula according to the Mendeleev heat productivity formula:
Qar＝K·100.0·(339.0·Car+1030.0·Har-109.0·(Oar-Sar)-25.0·Mar)
wherein Qar is the calorific value of coal powder, and the unit kJ/kg; k is a high calorific value coefficient;
step (1c), calculating a pulverized coal combustion efficiency formula according to the excess air coefficient:
η＝(Har/4.0+Sar/32.0+Car/12.0-Oar/32.0)*32.0
wherein eta is the combustion efficiency of the pulverized coal;
step (1d), calculating the mass flow of each component of the combusted smoke according to an average density method:
MNO＝VNO30.0, wherein MNOMass flow of NO in kg/s; vNOIs the molar volume flow of NO;
MN2＝VN228.0, wherein MN2Is N2Mass flow of (2), unit kg/s; vN2Is N2Molar volume flow of (c);
MCO2＝VCO244.0, wherein MCO2Is CO2Mass flow of (2), unit kg/s; vCO2Is CO2Molar volume flow of (c);
MCO＝VCO28.0, wherein MCOMass flow of CO in kg/s; vCOIs the molar volume flow of CO;
MSO2＝VSO264.0, wherein MSO2Is SO2Mass flow of (2), unit kg/s; vSO2Is SO2Molar volume flow of (c);
MO2＝VO232.0, wherein MO2Is O2Mass flow of (2), unit kg/s; vO2Is O2Molar volume flow of (c);
Mh＝Vh18.0, wherein MhThe mass flow of the water vapor is unit kg/s; vhIs a molar volume flow of water vapourAn amount;
step (1e), calculating the flue gas temperature after pulverized coal combustion by a mass flow method:
Figure FDA0002770022440000021
Figure FDA0002770022440000022
wherein HfIs the enthalpy value of the flue gas, MairFor the mass flow of the incoming cold air HairFor the enthalpy of the incoming cold air, MmMass flow of pulverized coal injected before combustion, HmEnthalpy value, T, of coal dust injected before combustionfIs the flue gas temperature, P is the current gas pressure, CpThe specific heat capacity of the flue gas is;
modeling the heat transfer process of the flue gas and the materials of the cement plant by utilizing an energy conservation law, and calculating the heat of various components of the flue gas and the materials in an enthalpy form;
simulating the flow characteristics of the working medium in the cement plant, and calculating the flow and the flow speed of the working medium in the pipeline;
and (4) the computer modeling platform feeds back and displays the calculation results obtained in the step (1), the step (2) and the step (3) on a process flow interface in an OPC communication mode to form a visual simulation interactive interface, and input cement production parameters are revised through the interactive interface so as to simulate the current cement production state.
2. The interactive cement production simulation method of claim 1, wherein the modeling of the heat transfer process between the flue gas and the material of the cement plant in the step (2) specifically comprises the following steps:
step (2a), calculating the convective heat transfer coefficient:
Figure FDA0002770022440000023
wherein, Kf1To convective heat transfer coefficient, FmIs the mass flow of the material, FarIs the mass flow of the flue gas;
step (2b), calculating the heat conduction and heat exchange coefficient:
Kf2＝0.000698+Fm*0.00064，
wherein, Kf2Is the heat conduction and heat exchange coefficient;
and (2c) calculating coefficients of two heat exchange modes of convection and heat conduction as a total heat exchange coefficient:
Kf＝1/Kf1+1/Kf2；
step (2d), calculating the heat transfer rate:
Figure FDA0002770022440000024
step (2e), calculating the heat exchange quantity:
Qf＝Kf·Far·Sf·(Tar-Tm)
in the formula, TarIs the temperature of the flue gas, TmIs the temperature of the material.
3. The interactive cement production simulation method of claim 1, wherein the step (3) of calculating the flow and the flow rate of the working medium in the pipeline specifically comprises the following steps:
step (3a), determining a resistance loss calculation formula:
Figure FDA0002770022440000031
Figure FDA0002770022440000032
wherein h isfThe length loss of the liquid column caused by resistance is unit m; Δ P is fluid pressure loss due to resistance, in Pa; λ is the drag loss coefficient; l is the length of the pipeline in m; rho is the valve inlet steam density in kg/m3(ii) a d is the pipe diameter in m; v is the flow velocity of the fluid in m/s; q is fluid mass flow rate, unit kg/s; g is the acceleration of gravity;
step (3b), defining the pipeline circulation capacity adm, and deducing an adm calculation formula:
Figure FDA0002770022440000033
wherein Q is liquid mass flow rate, unit kg/s; rho is the valve inlet steam density in kg/m3(ii) a dP is the pressure difference between the inlet and the outlet of the valve, and the unit is MPa;
step (3c), obtaining the linear relation between the flow and the circulation capacity by inputting the pressure difference between an inlet and an outlet of a pipeline or a valve and the density of the working medium; and obtaining the circulation capacity according to the pipeline size data, and further calculating the flow and the flow speed in the pipeline.
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