CN112923349A - Dynamic dirt monitoring method and system for low-temperature economizer of coal-fired boiler - Google Patents
Dynamic dirt monitoring method and system for low-temperature economizer of coal-fired boiler Download PDFInfo
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 93
- 239000003546 flue gas Substances 0.000 claims abstract description 93
- 238000012546 transfer Methods 0.000 claims abstract description 74
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
- F28G15/00—Details
- F28G15/003—Control arrangements
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Abstract
A method for dynamically monitoring dirt of a low-temperature economizer of a coal-fired boiler comprises the following steps: acquiring a clean state heat transfer coefficient of each heat exchange module, and acquiring fluid state data and flue gas state data of each heat exchange module in real time; calculating a real-time heat transfer coefficient according to the fluid state data and the smoke state data; and calculating a cleaning factor according to the cleaning state heat transfer coefficient and the real-time heat transfer coefficient. A dynamic dirt monitoring system of a low-temperature economizer of a coal-fired boiler comprises one or more heat exchange modules, wherein data acquisition devices are arranged on the heat exchange modules and are electrically connected with a data processing device; the data acquisition device is used for acquiring fluid state data and flue gas state data of the heat exchange module; the data processing device calculates a real-time heat transfer coefficient according to data collected by the data collecting device, and then calculates a cleaning factor used for expressing the heat transfer influence degree of dirt by combining the heat transfer coefficient in a cleaning state.
Description
Technical Field
The invention relates to the field of heat exchange surface monitoring, in particular to a method and a system for dynamically monitoring dirt of a low-temperature economizer of a coal-fired boiler.
Background
In a coal-fired power plant, heat exchange equipment plays an important role in recycling of flue gas waste heat, but because the application environment is various and the coal quality is uneven, a heat exchange medium on a gas side is often flue gas containing ash, viscous substances and corrosive gas. Meanwhile, along with increasingly strict requirements of energy-saving and emission-reducing policies, in order to meet the requirements of energy saving and emission reduction, the exhaust gas temperature of the boiler gradually decreases, and the wall temperature of the low-temperature heating surface of the reheater is also continuously reduced while the exhaust gas heat loss is reduced. Once the wall temperature is lower than the acid dew point of the flue gas, the flue gas is condensed, so that low-temperature corrosion and ash blockage of a heating surface are caused, the heat exchange performance of equipment is reduced, the resistance of a flue is increased, the power consumption of an induced draft fan is increased, the load of a boiler is influenced, the service life of a heat exchange surface is shortened, explosion and leakage accidents are easy to happen, and potential safety hazards are brought to stable operation of a system.
At present, the corrosion and dust deposition resistance of the surface of the flue gas heat exchanger becomes an important research direction for improving the heat exchange and waste heat utilization efficiency and saving the economic cost for replacing corroded equipment. The current methods for improving the problem mainly comprise the following methods: (1) the regular water cleaning method, namely when the heat exchange efficiency of the heat exchanger is reduced by 15% -20%, the heat exchange surface is washed by high-pressure water to remove the deposited dust and corrosion products, has the advantages of good cleaning effect, the heat exchange efficiency is recovered to more than 99%, and the defect of wasting a large amount of water resources to cause the corrosion of the heat exchange surface; (2) the regular high-pressure air purging method is characterized in that the heat exchange efficiency of the heat exchanger is reduced by 5-15%, and high-pressure air is used for vertically blowing the high-pressure air to the heat exchange surface, so that the method has the advantages of saving a large amount of water resources, recovering the heat exchange efficiency to be more than 95%, and having the defects that the high-pressure air easily causes the deformation of the heat exchange surface and generates a large amount of noise; (3) the material of the heat exchange surface is replaced by 316L stainless steel, 2205 duplex stainless steel, titanium and other materials, the material has the advantages of better corrosion resistance and high price, and the price is one time or even more than several times higher than that of the common carbon steel and ND steel. (4) The surface modification heat exchange method is characterized in that the surface energy of the surface is reduced, the deposition of ash particles is reduced, and the surface corrosion resistance is improved through a surface modification technology. The method has the advantages that the heat exchange efficiency is over 80 percent during the one-year operation of the heat exchanger, the cleaning cost and water resources are saved, the method for evaluating the comprehensive performance of the modified heat exchange surface is complex, the test result is obtained by simulating flue gas in a laboratory, and the result is obtained by testing the actual flue gas working condition.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a method and a system for dynamically monitoring the fouling of a low-temperature economizer of a coal-fired boiler, which are used for carrying out real-time detection and dynamic calculation according to the actual flue gas working condition and providing the operating parameters and the fouling condition of a heat exchange module.
The purpose of the invention is realized by the following technical scheme:
a method for dynamically monitoring dirt of a low-temperature economizer of a coal-fired boiler comprises the following steps:
s1: acquiring a clean state heat transfer coefficient of each heat exchange module, and acquiring fluid state data and flue gas state data of each heat exchange module in real time;
s2: calculating a real-time heat transfer coefficient according to the fluid state data and the smoke state data;
s3: and calculating a cleaning factor for representing the heat transfer influence degree of dirt according to the cleaning state heat transfer coefficient and the real-time heat transfer coefficient.
Further, the fluid status data includes an inlet fluid temperature, an outlet fluid temperature, and a fluid flow rate, and the flue gas status data includes a flue gas inlet temperature and a flue gas outlet temperature.
Further, the real-time heat transfer coefficient in step S2 is calculated as:
wherein k is the real-time heat transfer coefficient, QaIs the heat exchange amount between the flue gas and the working medium, A0Δ T being the total heat exchange areamIs a logarithmic mean temperature difference;
ΔTmis calculated by the formula
ΔTmaxIs the maximum value of the temperature difference between the cold and hot fluids, Delta TmimThe minimum value of the temperature difference of the cold fluid and the hot fluid;
Qathe calculation formula of (2) is as follows:
in the formula, QgIs the heat release of the flue gas, QwIs the fluid heat absorption;
Qgthe calculation formula of (2) is as follows:
Qg＝ρgvgsCp,g(T1-T2)
in the formula, ρgIs the density of the flue gas, vgIs flue gas flow velocity, s is heat exchangeCross-sectional area of heat exchange tubes in module, Cp,gSpecific heat capacity of flue gas, T1Is the flue gas inlet temperature, T2Is the flue gas outlet temperature;
Qwthe calculation formula of (2) is as follows:
Qw＝ρwqwCp,w(t2-t1)
in the formula, ρwIs the density of the fluid, qwIs the volume flow of the fluid, Cp,wIs the specific heat capacity of the fluid, t2、t1The outlet fluid temperature and the inlet fluid temperature, respectively, wherein the volumetric flow of the fluid is obtained from the fluid flow;
the calculation formula of the cleaning factor in step S3 is:
wherein F is a cleaning factor, k is a real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
Further, the method also comprises the following steps:
s4: and calculating the Knudel number according to the fluid state data and the smoke state data.
Further, the step S4 includes the following sub-steps:
s401: reynolds number Re was calculated as follows:
in the formula, omega is the flow velocity of the fluid, the unit m/s, mu is the kinematic viscosity, and the unit m2(ii)/s, D is the fluid diameter in m, and the fluid flow rate is obtained from the fluid flow rate;
qwω · S and
qw- -volumetric flow
Omega- -average fluid flow velocity
S- -pipe cross-sectional area;
s402: the Knoop number was calculated from the Reynolds number Re.
Further, in step S3, a fouling resistance is also calculated, and a calculation formula of the fouling resistance is as follows:
in the formula, RfIs fouling resistance, k is the real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
Further, after the step S3, a plating performance index is calculated based on the cleaning factor according to the following formula:
in the formula (I), the compound is shown in the specification,
as an index of coating performance, FdFor a cleaning factor of the coated pipe, F0Is the original tube cleaning factor.
A dynamic dirt monitoring system of a low-temperature economizer of a coal-fired boiler comprises one or more heat exchange modules, wherein data acquisition devices are arranged on the heat exchange modules and are electrically connected with a data processing device;
the data acquisition device is used for acquiring fluid state data and flue gas state data of the heat exchange module;
the data processing device calculates a real-time heat transfer coefficient according to data collected by the data collecting device, and then calculates a cleaning factor used for expressing the heat transfer influence degree of dirt by combining the heat transfer coefficient in a cleaning state.
Further, the data acquisition device comprises an inlet fluid temperature sensor, an outlet fluid temperature sensor, a fluid flow sensor, a flue gas inlet temperature sensor and a flue gas outlet temperature sensor; the inlet fluid temperature sensor is used for detecting the inlet fluid temperature of the heat exchange module, the outlet fluid temperature sensor is used for detecting the outlet fluid temperature of the heat exchange module, the fluid flow sensor is used for detecting the fluid flow of the heat exchange module, the flue gas inlet temperature sensor is used for detecting the flue gas inlet temperature of the heat exchange module, and the flue gas outlet temperature sensor is used for detecting the flue gas outlet temperature of the heat exchange module.
Further, the data processing device calculates the Knudel number according to the fluid state data and the flue gas state data, the data processing device calculates the fouling resistance according to the real-time heat transfer coefficient and the clean state heat transfer coefficient, and the data processing device calculates the performance index of the coating according to the cleaning factor.
The invention has the beneficial effects that:
real-time detection and dynamic calculation can be performed according to the actual flue gas working condition, and the operation parameters and the scaling condition of the heat exchange module are provided; the method is scientific and reasonable, has strong applicability, and provides reliable and accurate performance detection data of the heat exchange module.
Drawings
FIG. 1 is an electrical schematic diagram of a dynamic fouling monitoring system for a low-temperature economizer of a coal-fired boiler;
FIG. 2 is a schematic structural diagram of a system for dynamically monitoring fouling of a low-temperature economizer of a coal-fired boiler;
FIG. 3 is a schematic view of a first configuration of a heat exchange module;
FIG. 4 is a schematic view of a second construction of a heat exchange module;
FIG. 5 is a cross-sectional view taken along A-A of FIG. 4;
FIG. 6 is a display interface diagram of an online monitoring system.
In the figure, 1 a first heat exchange module, 2 a second heat exchange module, 3 a third heat exchange module, 4 a fourth heat exchange module, 5 a fifth heat exchange module, 6 a first water inlet stop valve, 7 a first water outlet stop valve, 8 a second water inlet stop valve, 9 a second water outlet stop valve, 10 a third water inlet stop valve, 11 a third water outlet stop valve, 12 a fourth water inlet stop valve, 13 a fourth water outlet stop valve, 14 a fifth water inlet stop valve, 15 a fifth water outlet stop valve, 16 a first water inlet temperature sensor, 17 a first water outlet temperature sensor, 18 a second water inlet temperature sensor, 19 a second water outlet temperature sensor, 20 a third water inlet temperature sensor, 21 a third water outlet temperature sensor, 22 a fourth water inlet temperature sensor, 23 a fourth water outlet temperature sensor, 24 a fifth water inlet temperature sensor, 25 a fifth water outlet temperature sensor, 26 a first flowmeter, 27 a second flowmeter, 28 third flow meter, 29 fourth flow meter, 30 fifth flow meter, 31 first flue gas temperature sensor, 32 second flue gas temperature sensor, 33 third flue gas temperature sensor, 34 fourth flue gas temperature sensor, 35 inlet pipe main valve, 36 outlet pipe main valve, 37 data processing device, 38 data transmission equipment, 39 inlet water main pipe, 40 outlet water main pipe, 41 flue cross section, 42 outlet water header, 43 heat exchange pipe, 44 inlet water header, 45 outlet water header connecting pipe, 46 air vent, 47 inlet water header connecting pipe, 48 water vent, 49 orifice plate.
Detailed Description
The embodiments of the present invention are described below with reference to specific embodiments, and other advantages and effects of the present invention will be easily understood by those skilled in the art from the disclosure of the present specification. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention. It is to be noted that the features in the following embodiments and examples may be combined with each other without conflict.
It should be noted that the drawings provided in the following embodiments are only for illustrating the basic idea of the present invention, and the components related to the present invention are only shown in the drawings rather than drawn according to the number, shape and size of the components in actual implementation, and the type, quantity and proportion of the components in actual implementation may be changed freely, and the layout of the components may be more complicated.
The first embodiment is as follows:
as shown in fig. 1 to 6, a method for dynamically monitoring fouling of a low-temperature economizer of a coal-fired boiler comprises the following steps:
s1: acquiring a clean state heat transfer coefficient of each heat exchange module, and acquiring fluid state data and flue gas state data of each heat exchange module in real time;
s2: calculating a real-time heat transfer coefficient according to the fluid state data and the smoke state data;
s3: and calculating a cleaning factor for representing the heat transfer influence degree of dirt according to the cleaning state heat transfer coefficient and the real-time heat transfer coefficient.
Preferably, the fluid status data comprises an inlet fluid temperature, an outlet fluid temperature and a fluid flow rate, and the flue gas status data comprises a flue gas inlet temperature and a flue gas outlet temperature.
Preferably, the real-time heat transfer coefficient calculation formula in step S2 is:
wherein k is the real-time heat transfer coefficient, QaIs the heat exchange amount between the flue gas and the working medium, A0Δ T being the total heat exchange areamIs a logarithmic mean temperature difference;
ΔTmis calculated by the formula
ΔTmaxIs the maximum value of the temperature difference between the cold and hot fluids, Delta TmimThe minimum value of the temperature difference of the cold fluid and the hot fluid;
the clean state heat transfer coefficient is calculated by using the temperature and flow values of the device in the initial operation according to the formula (1).
According to the heat balance principle, the heat exchange quantity of the heat exchange module is equal to the heat absorption quantity and the smoke heat release quantity of the fluid in the heat exchange module. From the thermal equilibrium equation:
Qa＝Qw＝Qg
(3)
thus, QaThe calculation formula of (2) is as follows:
in the formula, QgIs the heat release of the flue gas, QwIs the fluid heat absorption;
Qgthe calculation formula of (2) is as follows:
Qg＝ρgvgsCp,g(T1-T2) (5)
in the formula, ρgIs the density of the flue gas, vgIs the flow velocity of flue gas, s is the cross-sectional area of the heat exchange tube in the heat exchange module, Cp,gSpecific heat capacity of flue gas, T1Is the flue gas inlet temperature, T2Is the flue gas outlet temperature;
Qwthe calculation formula of (2) is as follows:
Qw＝ρwqwCp,w(t2-t1)
(6)
in the formula, ρwIs the density of the fluid, qwIs the volume flow of the fluid, Cp,wIs the specific heat capacity of the fluid, t2、t1The outlet fluid temperature and the inlet fluid temperature, respectively, wherein the volumetric flow of the fluid is obtained from the fluid flow;
the calculation formula of the cleaning factor in step S3 is:
wherein F is a cleaning factor, k is a real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
Preferably, the fouling resistance is also calculated in step S3,
heat transfer coefficient k of heat exchange tube in clean state0Can be represented by the following formula:
wherein the content of the first and second substances,
the ratio of the internal surface area to the internal surface area of the heat exchange tube can also be simplified to the ratio of the external diameter to the internal diameter if the tube is not finned.
In the formula:
is smoke side thermal resistance, where α1The heat release coefficient of the flue gas to the outer wall of the pipe,
is the working medium side thermal resistance, wherein alpha2Is the convective heat release coefficient, delta, from the tube wall to the working mediumwIs the thickness of the pipe wall, and lambda is the heat conductivity coefficient of the pipe wall material. Generally the thermal resistance inside the tube is negligible.
The heat transfer coefficient k of the heat exchange tube after scaling can be represented by the following formula:
in the formula, deltafIs the thickness of the fouling layer, λfIs the thermal conductivity of the fouling layer.
Therefore, the calculation formula of the fouling resistance is as follows:
in the formula, RfIs fouling resistance, k is the real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
Dirt thermal resistance is generally selected as a dirt characteristic parameter in heat exchange calculation, but the influence degree of dust deposition and corrosion on heat transfer of a heated surface cannot be visually expressed by a single dirt thermal resistance value, so that the dust degree is reflected by a cleaning factor through the change of a heat transfer coefficient, and the ratio of a real-time heat transfer coefficient to a clean-state heat transfer coefficient (an ideal value) is used as the dust characteristic parameter of the heated surface.
And 4, the comprehensive performance evaluation is carried out on the heating surface under the actual flue gas working condition by comprehensively considering the fouling thermal resistance and the cleaning factor, so that the evaluation is more accurate.
Preferably, the method further comprises the following steps:
s4: and calculating the Knoop number for representing the heat transfer characteristics of the heat exchange tube according to the fluid state data and the smoke state data.
The Knudsen number is also considered when the comprehensive performance of the heating surface under the actual flue gas working condition is evaluated, and the evaluation is more comprehensive.
Preferably, the step S4 includes the following sub-steps:
s401: reynolds number Re was calculated as follows:
in the formula, omega is the flow velocity of the fluid, the unit m/s, mu is the kinematic viscosity, and the unit m2(ii)/s, D is the fluid diameter in m, and the fluid flow rate is obtained from the fluid flow rate;
qwω · S and
qw- -volumetric flow
Omega- -average fluid flow velocity
S- -pipe cross-sectional area;
s402: the Knoop number was calculated from the Reynolds number Re.
The physical meaning of the Knoop number is a standard number representing the intensity of convective heat transfer, and also represents the ratio of the heat conduction resistance and the convective heat transfer resistance of the fluid laminar flow bottom layer.
The calculated relationship for the nussel number is:
l-is the geometrical characteristic length of the heat transfer surface, the dimension perpendicular to the direction of the heat transfer surface, and the unit is m; such as the diameter of the heat pipe, the thickness of the heat transfer layer, etc.
h-is the surface convective heat transfer coefficient of the fluid, and the unit is W/(m)2·K)；
λ -is the thermal conductivity of the fluid, in W/(m.K);
the Knoop number is a function of the convective heat transfer coefficient and is therefore used to characterize the heat transfer characteristics of a heat exchange tube.
The following three calculation formulas 13, 14, and 15 of the knossel number have the same effect as the previous calculation relational expression 12 of the knossel number, are empirical formulas of the knossel number, and have Re (reynolds number) and Pr (prandtl number, which can be found from the physical property parameter table) as main parameters. These parameters change with the temperature of the fluid and can be found from the physical property parameter table according to the average temperature.
If Re > 10000, the calculation formula of the Nussel number is as follows:
Nu＝0.02Re0.8Pr0.3 (13)
if Re is less than 2300, laminar flow is obtained, and the calculation formula of the Knudel number is as follows:
if 2300 < Re < 10000, the transition flow is obtained, and the calculation formula of the Knudel number is as follows:
the physical property parameter corresponding to the average water temperature is checked through the physical property parameter table, and the physical property parameter table comprises the following steps: dynamic viscosity vfThermal conductivity lambdafKinematic viscosity μfAnd PrfAnd kinematic viscosity mu corresponding to wall temperatureW。
Preferably, after the step S3, a plating performance index is calculated based on the cleaning factor according to the following formula:
in the formula (I), the compound is shown in the specification,
as an index of coating performance, FdFor a cleaning factor of the coated pipe, F0Is the original tube cleaning factor.
The evaluation indexes are verified from multiple aspects, multiple angles and mutually through the dirt thermal resistance, the cleaning factor and the Nossel number, the reliability is improved, and the consistency of data trends is observed after results are obtained.
By quantifying the index of the coating properties
The method can represent the surface dust deposition and corrosion states of different heat exchange surfaces or coated pipes, and is used for heat exchange surface evaluation to achieve the target of optimizing the heat exchange surface material.
When evaluating the heat exchange surface, firstly, the heat exchange tube is used as the original tube to be detected to obtain the cleaning factor of the original tube, then the heat exchange tube in the heat exchange module is replaced by the required evaluation tube or the coating tube is formed on the heat exchange tube by coating to be detected to obtain the cleaning factor of the coating tube, and then the quantitative index of the coating performance can be obtained by calculating
The preference of the heat exchanging surface material is hereby performed.
By researching the comprehensive performances of corrosion resistance, dust deposition resistance and the like of different heat exchange surface materials under the actual flue gas working condition, a reliable basis is provided for the improvement of the flue gas waste heat recovery efficiency and the economic operation of the generator set.
The system for dynamically monitoring the dirt of the low-temperature economizer of the coal-fired boiler comprises one or more heat exchange modules, wherein the heat exchange modules are respectively provided with a data acquisition device, and the data acquisition devices are electrically connected with a data processing device;
the data acquisition device is used for acquiring fluid state data and flue gas state data of the heat exchange module;
the data processing device calculates a real-time heat transfer coefficient according to data collected by the data collecting device, and then calculates a cleaning factor used for expressing the heat transfer influence degree of dirt by combining the heat transfer coefficient in a cleaning state.
Preferably, the data acquisition device comprises an inlet fluid temperature sensor, an outlet fluid temperature sensor, a fluid flow sensor, a flue gas inlet temperature sensor and a flue gas outlet temperature sensor; the inlet fluid temperature sensor is used for detecting the inlet fluid temperature of the heat exchange module, the outlet fluid temperature sensor is used for detecting the outlet fluid temperature of the heat exchange module, the fluid flow sensor is used for detecting the fluid flow of the heat exchange module, the flue gas inlet temperature sensor is used for detecting the flue gas inlet temperature of the heat exchange module, and the flue gas outlet temperature sensor is used for detecting the flue gas outlet temperature of the heat exchange module.
Preferably, the data processing device calculates the Knudel number used for representing the heat transfer characteristic of the heat exchange tube according to the fluid state data and the flue gas state data, the data processing device calculates the fouling resistance according to the real-time heat transfer coefficient and the clean state heat transfer coefficient, and the data processing device calculates the performance index of the coating according to the cleaning factor.
The data acquisition device adopts a direct measurement mode, wherein the inlet fluid temperature sensor, the outlet fluid temperature sensor, the flue gas inlet temperature sensor and the flue gas outlet temperature sensor adopt high-precision thermal resistance sensors, and the fluid flow sensor adopts an electromagnetic flowmeter.
The thermal resistance sensor is directly connected with the data recorder; the electromagnetic flowmeter is connected with a 485 field bus, RS-485 communication is adopted, then the electromagnetic flowmeter is connected with a computer through an RS-485-USB interface, and the data recorder converts analog signals collected by the sensor into digital signals and sends the digital signals to an upper computer (namely the computer).
The computer stores data in the memory card, and the online monitoring system installed on the computer monitors the data of the heat exchange module, so that the following functions are realized: data acquisition, data storage, real-time display, data processing, remote monitoring and the like. The on-line monitoring system is developed in a C # mode, and the main working mode is that after the transmitted data are received, the data enter an operation module firstly to calculate dirt thermal resistance, cleaning factors, Nussel number, plating layer performance quantization indexes and the like, then the data are stored, and all the data are displayed on a display interface.
After the upper computer is used as a data processing device for calculation, the temperature and flow information and various data obtained after calculation are stored in the upper computer, and the connection with a remote server is realized through a data transmission device 38 through a commercial data network (such as a wireless network). The remote server realizes data reading and storage of the upper computer through a remote control program. The user equipment is connected with the server in a butt joint mode, and the online monitoring system is also installed on the user equipment, so that the running condition of the heat exchange system is displayed in real time.
The models of the instruments are as follows:
1. thermal resistance sensor: WZP-291 thermal resistor, reference number PT100
2. An electromagnetic flow meter: l-mag electromagnetic flowmeter produced by Henan Pufeit instruments and meters Limited, the electromagnetic flowmeter measuring volume flow qw；
3. A data recorder: THTZ1608R paperless recorder produced by Temp control instrument factory of Yuyao City;
4. developing a plate: LatteBanda Win 104G/64G;
5. a touch screen: DFRobot7 inch LCD capacitive touch screen (1024 × 600 HDMI).
The development board and the touch screen are used for on-site debugging, remote startup and shutdown by using sunflower remote control software, data storage, debugging and the like.
The embodiment can perform real-time detection and dynamic calculation according to the actual flue gas working condition, and provides the operation parameters and the scaling condition of the heat exchange module; the method is scientific and reasonable, has strong applicability, and provides reliable and accurate performance detection data of the heat exchange module.
The monitoring device is portable, simple in structure, convenient to replace, independent of factory operation equipment, and free of influence on device operation during disassembly.
The monitoring system is low in manufacturing cost, and can test multiple heat exchange materials in the same actual operation working condition, so that the testing efficiency is high.
The heat exchange performance of the heat exchange material can be monitored on line, the dust deposition corrosion condition of the heat exchange modules can be judged by inquiring the change rule of the heat transfer coefficient of each heat exchange module, and the corrosion resistance and dust deposition resistance of the heat exchange surface can be evaluated.
The monitoring system collects necessary data and transmits the data to the on-site upper computer through the RS-485 bus for storage, calculation and display. The field upper computer is connected with the remote server through the cloud end, field operation data can be checked and collected in real time through the remote server, remote modification, downloading and execution can be achieved through the server in the testing method and the testing process, and maintenance amount of field personnel is reduced. Data are backed up simultaneously by the upper computer and the server, so that the influence caused by communication abnormity is reduced. The data use is facilitated.
Example two:
as shown in fig. 1 to 6, the second embodiment has all the technical features of the first embodiment, and the differences are as follows:
the heat exchange modules are connected in parallel, a water inlet of each heat exchange module is connected with a water inlet main pipe through a water inlet sub-pipe, and a water outlet of each heat exchange module is connected with a water outlet main pipe through a water outlet sub-pipe. And cooling water is adopted as fluid in the heat exchange module to exchange heat.
Each heat exchange module runs independently and is not interfered with each other, and the temperature and the flow are monitored respectively for calculating the performance parameters of each heat exchange module.
The heat exchange module is horizontally arranged in the flue, and the main body consists of three rows of nine carbon steel heat exchange tubes in staggered arrangement.
The two ends of the heat exchange tube are respectively connected with a tube plate and a semi-cylindrical header, and the headers at the left end and the right end are respectively provided with a horizontal hole which is a water inlet and a water outlet.
The inlet fluid temperature sensor and the fluid flow sensor are arranged near the water inlet stop valve, and the outlet fluid temperature sensor is arranged near the water outlet stop valve.
The flow is measured in order to calculate the amount of heat exchange, using only the inlet fluid flow calculation, and is therefore arranged near the water inlet shutoff valve.
The heat medium water of each heat exchange module is led out to the water inlet of the heat exchange module by the heat medium water main pipe, and the heat medium water flows in from the water inlet of the heat exchange module and then converges into the main pipe from the water outlet after exchanging heat with the low-temperature flue gas, so that a circulating water system is formed.
The number of the heat exchange modules is 5, the heat exchange modules are respectively a first heat exchange module 1, a second heat exchange module 2, a third heat exchange module 3, a fourth heat exchange module 4 and a fifth heat exchange module 5 which are subjected to surface modification and have different heat exchange surfaces, and the heat exchange modules are connected in parallel to ensure that each heat exchange module is in the same working condition in the flue 41.
The heat medium water is led out from the water inlet main pipe 39 and is connected with the water inlet header connecting pipe 47 of the heat exchange module through the water inlet sub-pipe, the heat medium water flows out from the water outlet header 42 after entering the water inlet header 44 and exchanging heat with the cold flue gas through the heat exchange pipe 43, the water outlet header connecting pipe 45 is connected with the water outlet main pipe 40 again, and the water after exchanging heat is sent out. The inlet and outlet positions of each module are provided with a data acquisition device, a first water inlet stop valve 6 is distributed above an inlet sub-pipe (a water inlet header connecting pipe 47) of the first heat exchange module 1, in order to ensure the accuracy of measurement of a flowmeter, more than 10D straight pipe sections need to be reserved at the inlet of the flowmeter, more than 5D straight pipe sections need to be reserved at the outlet of the flowmeter, a first flowmeter 26 is distributed 500mm below the first water inlet stop valve 6, a first water inlet temperature sensor 16 is placed at the position, close to the water inlet header connecting pipe 47, below the first flowmeter 26 as far as possible, a first water outlet stop valve 7 is distributed above a water outlet header connecting pipe 45, and a first water outlet temperature sensor 17 is placed at the position, close to the water outlet header connecting pipe 45, below the first. The installation positions and the operation modes of the data acquisition devices and the valves of the second heat exchange module 2, the third heat exchange module 3, the fourth heat exchange module 4 and the fifth heat exchange module 5 are the same as those of the first heat exchange module 1.
In the data acquisition device, the inlet fluid temperature sensors of each heat exchange module are respectively a first inlet water temperature sensor 16, a second inlet water temperature sensor 18, a third inlet water temperature sensor 20, a fourth inlet water temperature sensor 22 and a fifth inlet water temperature sensor 24; the outlet fluid temperature sensors of each heat exchange module are respectively a first outlet water temperature sensor 17, a second outlet water temperature sensor 19, a third outlet water temperature sensor 21, a fourth outlet water temperature sensor 23 and a fifth outlet water temperature sensor 25; the fluid flow sensors of each heat exchange module are respectively a first flow meter 26, a second flow meter 27, a third flow meter 28, a fourth flow meter 29 and a fifth flow meter 30;
because heat exchange module is very little for the flue of power plant, and the heat transfer volume is limited, and the flue gas skips the temperature variation behind the heat exchanger minimum, so think that the flue gas is imported and exported the temperature and is similar, merge into a flue gas temperature sensor with flue gas inlet temperature sensor and flue gas outlet temperature sensor, set up four flue gas temperature sensor's purpose and be: the heat exchanger is horizontally arranged, and temperature change can be generated in the transverse direction, so that the temperature change can be monitored. The flue gas temperature sensors are respectively a first flue gas temperature sensor 31, a second flue gas temperature sensor 32, a third flue gas temperature sensor 33 and a fourth flue gas temperature sensor 34. The data acquisition device is connected with a data processing device 37 through a data transmission line, and the data processing device 37 is connected with a data transmission device 38.
Each heat exchange module comprises a water outlet header 42, a heat exchange pipe 43, a water inlet header 44, a water outlet header connecting pipe 45, an exhaust port 46, a water inlet header connecting pipe 47, a water outlet 48 and a pore plate 49. The tube array mode that the orifice plate 49 hole adopted is the staggered arrangement circular tube, for simulating real low temperature economizer, adopt that the horizontal pitch is 46mm, the longitudinal pitch is 80mm, the heat exchange tube 43 both sides are connected with orifice plate 49, and then with the collection case 44 of intaking and the collection case 42 of play water are connected, the collection case 44 of intaking and the collection case 42 of play water are connected with water collection case takeover 47, play water collection case takeover 45 respectively. In actual use, the air outlet 46 and the water outlet 48 are sealed according to actual requirements.
The above-mentioned embodiments only express the specific embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention.
Claims (10)
1. A method for dynamically monitoring dirt of a low-temperature economizer of a coal-fired boiler is characterized by comprising the following steps: the method comprises the following steps:
s1: acquiring a clean state heat transfer coefficient of each heat exchange module, and acquiring fluid state data and flue gas state data of each heat exchange module in real time;
s2: calculating a real-time heat transfer coefficient according to the fluid state data and the smoke state data;
s3: and calculating a cleaning factor for representing the heat transfer influence degree of dirt according to the cleaning state heat transfer coefficient and the real-time heat transfer coefficient.
2. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 1, wherein the method comprises the following steps: the fluid status data includes an inlet fluid temperature, an outlet fluid temperature, and a fluid flow rate, and the flue gas status data includes a flue gas inlet temperature and a flue gas outlet temperature.
3. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 2, characterized in that: the calculation formula of the real-time heat transfer coefficient in the step S2 is as follows:
wherein k is the real-time heat transfer coefficient, QaIs the heat exchange amount between the flue gas and the working medium, A0Δ T being the total heat exchange areamIs a logarithmic mean temperature difference;
ΔTmis calculated by the formula
ΔTmaxIs the maximum value of the temperature difference between the cold and hot fluids, Delta TmimThe minimum value of the temperature difference of the cold fluid and the hot fluid;
Qathe calculation formula of (2) is as follows:
in the formula, QgIs the heat release of the flue gas, QwIs the fluid heat absorption;
Qgthe calculation formula of (2) is as follows:
Qg＝ρgvgsCp,g(T1-T2)
in the formula, ρgIs the density of the flue gas, vgIs the flow velocity of flue gas, s is the cross-sectional area of the heat exchange tube in the heat exchange module, Cp,gSpecific heat capacity of flue gas, T1Is the flue gas inlet temperature, T2Is the flue gas outlet temperature;
Qwthe calculation formula of (2) is as follows:
Qw＝ρwqwCp,w(t2-t1)
in the formula, ρwIs the density of the fluid, qwIs the volume flow of the fluid, Cp,wIs the specific heat capacity of the fluid, t2、t1The outlet fluid temperature and the inlet fluid temperature, respectively, wherein the volumetric flow of the fluid is obtained from the fluid flow;
the calculation formula of the cleaning factor in step S3 is:
wherein F is a cleaning factor, k is a real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
4. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 1, wherein the method comprises the following steps:
further comprising the steps of:
s4: and calculating the Knudel number according to the fluid state data and the smoke state data.
5. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 4, wherein the method comprises the following steps:
the step S4 includes the following sub-steps:
s401: reynolds number Re was calculated as follows:
in the formula, omega is the flow velocity of the fluid, the unit m/s, mu is the kinematic viscosity, and the unit m2And/s, D is the fluid diameter, in m,
the fluid flow rate is obtained according to the fluid flow;
s402: the Knoop number was calculated from the Reynolds number Re.
6. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 1, wherein the method comprises the following steps: in step S3, a fouling resistance is also calculated, and the calculation formula of the fouling resistance is:
in the formula, RfIs fouling resistance, k is the real-time heat transfer coefficient, k0The heat transfer coefficient is in a clean state.
7. The method for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to any one of the preceding claims, characterized in that:
after the step S3, a plating performance index is calculated based on the cleaning factor according to the following formula:
in the formula (I), the compound is shown in the specification,
as an index of coating performance, FdFor a cleaning factor of the coated pipe, F0Is the original tube cleaning factor.
8. A dirt dynamic monitoring system of a coal-fired boiler low-temperature economizer is characterized in that: the heat exchanger comprises one or more heat exchange modules, wherein the heat exchange modules are respectively provided with a data acquisition device, and the data acquisition devices are electrically connected with a data processing device;
the data acquisition device is used for acquiring fluid state data and flue gas state data of the heat exchange module;
the data processing device calculates a real-time heat transfer coefficient according to data collected by the data collecting device, and then calculates a cleaning factor used for expressing the heat transfer influence degree of dirt by combining the heat transfer coefficient in a cleaning state.
9. The system for dynamically monitoring the fouling of the low-temperature economizer of the coal-fired boiler according to claim 8, wherein: the data acquisition device comprises an inlet fluid temperature sensor, an outlet fluid temperature sensor, a fluid flow sensor, a flue gas inlet temperature sensor and a flue gas outlet temperature sensor; the inlet fluid temperature sensor is used for detecting the inlet fluid temperature of the heat exchange module, the outlet fluid temperature sensor is used for detecting the outlet fluid temperature of the heat exchange module, the fluid flow sensor is used for detecting the fluid flow of the heat exchange module, the flue gas inlet temperature sensor is used for detecting the flue gas inlet temperature of the heat exchange module, and the flue gas outlet temperature sensor is used for detecting the flue gas outlet temperature of the heat exchange module.
10. The system for dynamically monitoring fouling of a low-temperature economizer of a coal-fired boiler according to claim 8 or 9, characterized in that: the data processing device calculates the Knudel number according to the fluid state data and the flue gas state data, the data processing device calculates the fouling resistance according to the real-time heat transfer coefficient and the clean state heat transfer coefficient, and the data processing device calculates the performance index of the coating according to the cleaning factor.
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