CN110763369B - Monitoring method for exhaust gas temperature emission index in colored smoke plume treatment project - Google Patents
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Abstract
The invention discloses a method for monitoring exhaust gas temperature emission indexes in colored smoke plume treatment engineering, which comprises the following steps: assuming that the amount of the precipitated water of the flue gas in the flue is A, calculating a calculated value E of the temperature of the flue gas outlet according to heat balance; according to the saturated steam partial pressure corresponding to the measured temperature of the flue gas inlet and the calculated value E of the flue gas outlet temperature, the absolute humidity of the flue gas inlet and the absolute humidity of the flue gas outlet are calculated, and a calculated value A' of the amount of water separated out from the flue gas is calculated; checking the calculated value A ' of the amount of the precipitated water of the flue gas A and the amount of the precipitated water of the medium flue gas, if A and A ' exceed a certain relative error range, adjusting A and repeating the steps of the invention until the relative error of A and A ' is in the range, and the calculated value E of the temperature of the flue gas outlet is the actual temperature of the flue gas outlet. The invention can accurately calculate the actual temperature of the flue gas outlet and the amount of the flue gas precipitated water, improve the measurement precision, ensure the long-term stable work of the temperature measuring element, accurately realize the continuous monitoring of the emission index and effectively reduce the cost.
Description
Technical Field
The invention relates to the field of environmental protection, in particular to a method for monitoring emission indexes in colored smoke plume treatment engineering.
Background
At present, all large coal-fired power plants in China realize the emission after desulfurization, wherein the use of a limestone-gypsum wet flue gas desulfurization method accounts for more than 90 percent. The content of the humidified steam of the flue gas treated by the wet desulphurization is as high as 12-20 percent and is nearly in a saturated state. In the process of discharging a large amount of condensable particles such as moisture, soluble salt, sulfuric acid mist, organic matters and the like in the saturated wet flue gas into the atmospheric environment from a chimney port, colored smoke plume is easily formed due to condensation caused by temperature reduction, and environmental problems and visual pollution are caused. With further strictness of the state on the ultra-low emission standard and the assessment method, the colored smoke plume treatment becomes a new direction in the atmosphere pollution prevention and control work of the power industry.
In 2016, DB31/963-2016 emission Standard for atmospheric pollutants from coal-fired power plants was first issued in Shanghai to specify that the coal-fired power plants need to control the smoke temperature or take other effective measures to eliminate the colored smoke plume. After the corresponding policy of Shanghai, corresponding policies and standards are issued immediately in Zhejiang, Tianjin, Hebei, Xuzhou of Jiangsu, Shanxi Linfen and the like, and control indexes of the condensed smoke temperature are provided in pertinence, such as the requirements of colored smoke plume treatment of coal-fired power plants in Hebei: the temperature of the condensed smoke in summer (4-10 months) is below 48 ℃; the temperature of the condensed smoke in winter (11 months-3 months in the next year) is below 45 ℃; xu state electric de-whitening requirement: the temperature of the condensed smoke in summer is below 47 ℃; in winter, the temperature of the condensed flue gas is below 45 ℃.
Therefore, accurate monitoring of the flue gas temperature emission index after condensation has important practical significance, but accurate measurement is difficult to realize by the conventional method, wherein:
1. because the flue gas after wet desulphurization treatment is in a saturated steam state, partial moisture can be separated out from the flue gas after the flue gas is further condensed to reduce the temperature according to the treatment requirement of colored smoke plume. Most of the analyzed moisture is collected and led out from the lower part of the flue, but tiny liquid drops inevitably exist in the flue, and along with the flowing of the flue gas, the tiny liquid drops float in the downstream flue, and part of the liquid drops are attached to a primary element arranged at a measuring point for measuring the condensed flue gas temperature, so that the measured value deviates from the actual value. Therefore, the temperature measurement element is simply arranged at the smoke discharge measuring point after condensation to measure the temperature, which is inaccurate.
2. Theoretically, the emission temperature of the condensed flue gas can also be calculated according to the heat balance relationship by measuring the water amount separated out from the flue gas in the colored smoke plume treatment process. However, the mainstream colored smoke plume treatment technology is as follows: in the desulfurizing tower thick liquid condensation, install additional heat transfer surface and realize flue gas low temperature condensation techniques such as phase transition condensation, the water yield measurement that the flue gas was appeared also has certain problem:
(1) in the desulfurization tower slurry condensation technique, the amount of water precipitated cannot be measured because the precipitated water is mixed into the slurry.
(2) The phase-change coagulation water extraction technology taking fluoroplastics as a typical technology can trap water, remove smoke pollutants in a synergic manner to cause condensed water containing dust, aerosol and the like, and the separated water amount cannot be accurately measured.
In addition, the scholars at home and abroad concern the application of the membrane separation technology in the treatment of the colored smoke plume, water vapor in the smoke mainly enters the membrane tubes through the selective absorption of the membrane tubes, and a small amount of water vapor is condensed in the process that the smoke passes through the membrane tubes. The magnitude order of the cooling water passing through the membrane system is 10 to the third power, and the magnitude order of the water content of the flue gas passing through the membrane system is 10 to the first power and only accounts for about 1% of the cooling water. The error range of flow measuring devices such as orifice plates and ultrasonic flow meters is 1%, and therefore the amount of precipitated water measured is inaccurate.
Therefore, the accurate measurement of the emission index of the smoke temperature in the colored smoke plume treatment project has a plurality of problems, and the objective evaluation of the emission index of the colored smoke plume treatment is influenced.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a method for monitoring the emission index of the exhaust gas temperature in the colored smoke plume treatment project, so as to solve the problems that the measured value deviates from the actual value and the water precipitation amount cannot be measured in the measurement of the temperature of the exhaust gas outlet.
In order to solve the technical problem, the invention provides a method for monitoring the emission index of the exhaust gas temperature in the colored smoke plume treatment project.
A method for monitoring the discharge index of the exhaust gas temperature in the colored smoke plume treatment project comprises the following steps:
the method comprises the following steps: and (4) assuming that the amount of the precipitated flue gas is A, and calculating a calculated value E of the flue gas outlet temperature according to heat balance.
Step two: and (4) solving the absolute humidity of the flue gas inlet and outlet according to the saturated steam partial pressure corresponding to the measured temperature of the flue gas inlet and the calculated value E of the flue gas outlet temperature, and calculating a calculated value A' of the amount of water separated out from the flue gas.
Step three: checking whether the relative error between the flue gas precipitated water amount A in the step one and the calculated value A' of the flue gas precipitated water amount in the step two is within an error range; if the error range is exceeded, adjusting the step A and performing the steps from the first step to the third step again; and if the temperature is within the error range, outputting the calculated value E of the temperature of the flue gas outlet in the step I, namely the actual temperature of the flue gas outlet.
Further optimizing the technical scheme, the specific process of calculating the calculated value E of the temperature of the flue gas outlet in the step one is as follows:
s1: acquiring basic parameters of each measuring point at the inlet and outlet flue gas side and the cooling water side of the condensing heat exchanger through a DCS (distributed control system), and performing data processing on the acquired parameters to obtain the heat absorption capacity Q of the water side1。
S2: calculating the vaporization latent heat Q of water vapor condensed into water in the flue gas according to the actually measured flue gas inlet temperature and the flue gas precipitation water amount A2。
S3: according to the law of conservation of heat, the heat absorbed by the water side is Q1Latent heat of vaporization Q of water vapor condensed into water2The heat release Q of the dry flue gas can be calculated3。
S4: according to the heat release Q of dry flue gas3And (4) calculating to obtain a calculated value E of the temperature of the flue gas outlet.
Further optimizing the technical scheme, wherein the relative error range in the third step is 0-0.2%.
Further optimizing the technical solution, the basic parameters in S1 include: local atmospheric pressure, flue static pressure mean, flue gas inlet temperature, flue gas inlet actual flow, flue gas outlet temperature, cooling water inlet and outlet temperature and pressure, cooling water flow, condensed water temperature, condensed water pressure and flow.
Further optimizing the technical scheme that the water side heat absorption quantity Q in S1 and S31Is the sum of the cooling water heat absorption and the condensed water heat absorption.
Further optimizing the technical scheme that the heat absorption capacity Q of the water side1The value of (A) requires the addition of heat to a small amount of condensed water generated in the flue when the membrane separation technique is employedAmount of the compound (A).
Further optimizing the technical scheme that in the S4, the heat release quantity Q of the dry flue gas3The formula is as follows: heat release Q of dry flue gas3The flue gas flow is dry basis dry flue gas constant pressure specific heat capacity is inlet and outlet temperature difference.
Due to the adoption of the technical scheme, the technical progress of the invention is as follows.
1) According to the scheme, the problem of interference of temperature measurement of the flue gas outlet can be solved, the actual temperature of the flue gas outlet and the amount of water separated out from the flue gas can be calculated, the continuous monitoring of emission indexes is further realized, the measurement precision is improved, and the long-term stable work of a temperature measuring element is guaranteed.
2) The whole set of method is completely based on actual detection equipment, can accurately realize continuous monitoring of exhaust gas temperature emission indexes in wet smoke plume treatment engineering, and effectively reduces upgrading and modification cost of a continuous monitoring system for smoke emission of a coal-fired power plant.
Drawings
FIG. 1 is a schematic flow chart of the present invention;
Detailed Description
The invention will be described in further detail below with reference to the figures and specific examples.
A monitoring method for exhaust gas temperature emission indexes in colored smoke plume treatment engineering specifically comprises the following steps:
the method comprises the following steps: assuming that the precipitated water amount of the flue gas is A, calculating a calculated value E of the temperature of the flue gas outlet according to heat balance, wherein the calculation process is as follows:
s1: detecting basic parameters of each measuring point through DCS (distributed control system), acquiring local atmospheric pressure, flue static pressure mean value, flue gas inlet temperature, flue gas inlet actual flow, flue gas outlet temperature, cooling water inlet and outlet temperature and pressure, cooling water flow, condensate water temperature, condensate water pressure and flow, processing data of the acquired parameters, calculating the value of cooling water heat absorption capacity and the value of condensate water heat absorption capacity, and adding the values to obtain water side heat absorption capacity Q1。
If the membrane separation technology is adopted, a small amount of condensed water exists in the flue, and Q is calculated1When it is neededThe heat of this condensed water is taken into account.
S2: obtaining a saturated water ratio enthalpy value and a saturated steam ratio enthalpy value according to the actually measured flue gas inlet temperature, and multiplying the difference between the saturated water ratio enthalpy value and the saturated steam ratio enthalpy value by the assumed flue gas water precipitation A to obtain the vaporization latent heat Q of the water vapor condensed into water in the flue gas2。
S3: according to the law of conservation of heat, the heat absorbed by the water side is Q1Latent heat of vaporization Q of water vapor condensed into water2Calculating the difference to obtain the heat release Q of the dry flue gas3。
S4: according to the heat release Q of dry flue gas3The calculation formula of (2): heat release Q of dry flue gas3And (4) calculating to obtain a calculated value E of the temperature at the flue gas outlet based on the dry flue gas flow and the constant pressure specific heat capacity of the dry flue gas.
Step two: and (4) solving absolute humidity of the inlet and the outlet of the flue gas according to the saturated steam partial pressure corresponding to the calculated value E of the temperature of the outlet of the flue gas, and calculating a calculated value A' of the amount of water separated out from the flue gas.
Step three: checking the flue gas precipitated water amount A in the step one and the calculated flue gas precipitated water amount A ' in the step two, if the relative error of A and A ' exceeds 0.2%, adjusting A, then, repeating the steps one to three until the relative error of A and A ' is in the range of 0-0.2%, and outputting the calculated flue gas outlet temperature value E corresponding to the step one, namely the actual flue gas outlet temperature.
When the method is used for calculating the emission index of the exhaust gas temperature in the colored smoke plume treatment project, the steps are as follows:
the method comprises the following steps: assuming that the amount A of the precipitated water of the flue gas in the flue is 28kg/h, the basic parameters of the measurement points at the flue gas side and the cooling water side of the inlet and the outlet of the condensing heat exchanger are acquired by DCS, and the specific numerical values are shown in Table 1.
TABLE 1 basic parameters and values taken from DCS
| Name (R) | Unit of | Numerical value | Name (R) | Unit of | Numerical value |
| Local atmospheric pressure | kPa | 100.50 | Inlet temperature of flue gas | ℃ | 52.40 |
| Mean value of flue static pressure | kPa | -0.10 | Actual flow of flue gas inlet | m3/h | 9547.80 |
| Flue gas outlet temperature | ℃ | 51.51 | Inlet temperature of cooling water | ℃ | 31.05 |
| Inlet pressure of cooling water | kPa | 100.00 | Outlet temperature of cooling water | ℃ | 32.99 |
| Outlet pressure of cooling water | kPa | 63.36 | Flow rate of cooling water | t/h | 9.03 |
| Temperature of condensed water | ℃ | 47.40 | Pressure of condensed water | kPa | 100.00 |
| Flow rate of condensed water: | kg/h | 6.00 |
the specific enthalpy values of the inlet and the outlet of the cooling water are 130.24kJ/kg and 138.32kJ/kg respectively, and the difference of the specific enthalpy values is multiplied by the flow rate to obtain the heat absorption quantity delta Q of the cooling waterCooling waterNamely:
ΔQcooling water＝9.03t/h*103*(138.32kJ/kg-130.24kJ/kg)＝72962.4kJ/h
The enthalpy value of the condensed water is 198.53kJ/kg, and the heat absorption quantity delta Q of the condensed water is obtained by multiplying the enthalpy value by the flowCondensed waterNamely:
ΔQcondensed water＝6kg/h*198.53kJ/kg＝1191.18kJ/h
Adding the heat absorption capacity of the cooling water and the heat absorption capacity of the condensed water to obtain the heat absorption capacity Q of the water side1Namely:
Q1＝ΔQcondensed water+ΔQCondensed water＝72962.4kJ/h+1191.18kJ/h＝74153.58kJ/h
S1: according to the actually measured flue gas inlet temperature, the enthalpy values of saturated water and saturated steam are respectively 213.58kJ/kg and 2594.65kJ/kg, the specific enthalpy values of the saturated water and the saturated steam are subjected to difference, and then the difference is multiplied by the assumed flue gas separated water amount A to obtain the latent heat of vaporization Q of the water steam condensed into water2Namely:
Q2＝28kg/h*(2594.65kJ/kg-213.58kJ/kg)＝66669.96kJ/h
s2: according to the law of conservation of heat, the heat absorbed by the water side is Q1Latent heat of vaporization Q of water vapor condensed into water2Calculating the difference to obtain the heat release Q of the dry flue gas3Namely:
Q3＝Q1-Q2＝74153.58kJ/h-66669.96kJ/h＝7483.62kJ/h
s3: according to the heat release Q of dry flue gas3The calculation formula of (2):
heat release Q of dry flue gas3Dry flue gas flow dry basis dry flue gas constant pressure specific heat capacity inlet and outlet temperature difference
And calculating to obtain the temperature difference of the flue gas inlet and the flue gas outlet, and further calculating to obtain a calculated value E of the temperature of the flue gas outlet.
Wherein: the flue gas dry basis flow rate is the actual flow rate of the flue gas inlet (1-corresponding saturated humidity/100% at inlet temperature), and the saturated humidity corresponding to 52.40 ℃ is 13.8414% by checking a temperature and humidity table, namely the flue gas dry basis flow rate is 8226.2m3/h。
The clean smoke (dry basis) components only comprise carbon dioxide, nitrogen and oxygen, and the concentration of other gas components is extremely low and can be ignored. Constant pressure specific heat capacity of dry flue gas
Wherein
Respectively as dioxide in flue gasThe volume fractions of carbon, nitrogen and oxygen respectively have the following values: 12%, 82% and 6%.
The temperature difference between the flue gas inlet and the flue gas outlet is 7483.62kJ/h/(8226.2 m)3/h*1.359961kJ/(m3*℃))＝0.6673℃
The calculated value E of the temperature of the flue gas outlet is the temperature difference between the temperature of the flue gas inlet and the temperature of the flue gas outlet (52.4-0.6673 ℃) 51.732751.7287 DEG C
Step two: and (4) solving the absolute humidity of the flue gas inlet and outlet according to the saturated steam partial pressure corresponding to the measured temperature of the flue gas inlet and the calculated value E of the outlet temperature, and further calculating to obtain a calculated value A' of the water yield of the flue gas analysis.
Because the relative humidity of the flue gas at the outlet of the desulfurizing tower is 100%, the saturated steam pressure corresponding to the temperature of the flue gas is equal to the partial pressure of the moisture. The moisture pressure can be found by looking up a steam pressure versus saturated steam temperature table. I.e. a water pressure of 13.897 kPa.
According to the Kerbelon equation:
1m3the mole number of water in the flue gas is 1m, since the water pressure volume/(constant R temperature) 1000L 13.897kPa/(8.31441 (273.15K +52.40 ℃)) 5.134mol3The mass of the moisture in the smoke is 5.134 mol/18 g/mol 92.415g
1m3The volume of dry smoke in the smoke (1-saturated humidity at corresponding temperature/100%) is 1-13.814%/100%/0.8616 m3
1m3The volume of the dry standard state in the flue gas is 1m3Volume of dry flue gas in flue gas (273.15K/(273.15K + inlet flue gas temperature)) (local atmospheric pressure + flue static pressure)/101.325 kPa) ═ 0.8616m3*(273.15K/(273.15K+52.40℃))*((100.5kPa-0.1kPa)/101.325kPa)＝0.7163Nm3
Inlet absolute humidity of 1m3Mass of water in flue gas/1 m3The volume of the dry standard state in the smoke is 92.415g/0.7163Nm3＝129.015g/Nm3
Similarly, the absolute humidity of the opening can be determined to be 123.078g/Nm3。
The flue gas dry basis standard flow rate is (273.15K/(273.15K + inlet and outlet average smoke temperature)) (local atmospheric pressure + flue static pressure)/101.325 kPa) ═ 8226.2m3/h*(273.15K/(273.15K+52.40℃))*((100.5kPa-0.1kPa)/101.325kPa)＝6849.8Nm3/h
The water content of the separated flue gas is 6849.8Nm (inlet absolute humidity-outlet absolute humidity) of the flue gas dry basis standard state flow3/h*(129.015g/Nm3-123.078g/Nm3)＝40.665kg/h
Step three: and (4) checking the relative error of the calculated value A 'of the amount A' of the separated water of the flue gas in the flue and the calculated amount of the separated water of the flue gas in the step two. The error is calculated to be 12.665kg/h, and the relative error is > 0.2%, so the value of the smoke precipitated water A is adjusted, and the smoke precipitated water A is assumed to be 29.19 kg/h.
The correlation calculation formula is shown in step two, and the correlation calculation result is as follows:
the temperature difference between the inlet and the outlet of the smoke is 0.4279 DEG C
The calculated value E of the smoke outlet temperature is 51.9681 ℃ (52.4 ℃ -0.4279 ℃), and
the water content of the smoke gas is 29.162kg/h
And checking the relative error between the flue gas precipitated water amount A in the step one and the calculated flue gas precipitated water amount A' in the step two after adjustment. Through calculation, the error is 0.037kg/h, and the relative error is 0.126% < 0.2%, so the calculated value is output as the actual temperature of the flue gas outlet, namely 51.9681 ℃, and the actual value is 51.51 ℃ which has larger deviation than the actual value.
Claims (4)
1. A method for monitoring the discharge index of the exhaust gas temperature in the colored smoke plume treatment project is characterized by comprising the following steps:
the method comprises the following steps: assuming that the amount of the precipitated water of the flue gas is A, calculating a calculated value E of the temperature of the flue gas outlet according to heat balance;
the specific process of calculating the calculated value E of the temperature of the flue gas outlet is as follows:
s1: acquiring basic parameters of each measuring point at the inlet and outlet flue gas side and the cooling water side of the condensing heat exchanger through a DCS (distributed control system), and performing data processing on the acquired parameters to obtain the heat absorption capacity Q of the water side1(ii) a The basic parameters include: local atmospheric pressure, flue static pressure mean value, flue gas inlet temperature, actual flue gas inlet flow, flue gas outlet temperature, cooling water inlet and outlet temperature and pressure, cooling water flow, condensed water temperature, condensed water pressure and flow;
s2: calculating the vaporization latent heat Q of water vapor condensed into water in the flue gas according to the actually measured flue gas inlet temperature and the flue gas precipitation water amount A2；
S3: according to the law of conservation of heat, the heat absorbed by the water side is Q1Latent heat of vaporization Q of water vapor condensed into water2Calculating to obtain the heat release Q of the dry flue gas3；
S4: according to the heat release Q of dry flue gas3Calculating to obtain a calculated value E of the temperature of the flue gas outlet; the heat release Q of the dry flue gas3The formula is as follows: heat release Q of dry flue gas3The flow rate of the flue gas is dry basis, the constant pressure specific heat capacity of the dry flue gas is the temperature difference of an inlet and an outlet;
step two: according to the saturated steam partial pressure corresponding to the measured temperature of the flue gas inlet and the calculated value E of the flue gas outlet temperature, the absolute humidity of the flue gas inlet and the absolute humidity of the flue gas outlet are calculated, and a calculated value A' of the amount of water separated out from the flue gas is calculated;
step three: checking whether the relative error between the flue gas precipitated water amount A in the step one and the calculated value A' of the flue gas precipitated water amount in the step two is within an error range; if the error range is exceeded, adjusting the step A and performing the steps from the first step to the third step again; and if the temperature is within the error range, outputting the calculated value E of the temperature of the flue gas outlet in the step I, namely the actual temperature of the flue gas outlet.
2. The method for monitoring the emission temperature index of the discharged smoke in the colored smoke plume governing project according to claim 1, which is characterized in that: the relative error range in the third step is 0-0.2%.
3. The method for monitoring the emission temperature index of the discharged smoke in the colored smoke plume governing project according to claim 2, which is characterized in that: water side heat absorption Q in S1 and S31Is the sum of the cooling water heat absorption and the condensed water heat absorption.
4. The method for monitoring the emission temperature index of the discharged smoke in the colored smoke plume governing project according to claim 3, wherein the method comprises the following steps: the water side heat absorption capacity Q1The value of (b) requires the addition of heat from a small amount of condensed water produced in the flue when membrane separation technology is employed.
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| CN102901113A (en) * | 2011-07-25 | 2013-01-30 | 邵勇 | Technology and device for recovering heat energy of discharging chimney |
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| CN110285439A (en) * | 2019-07-25 | 2019-09-27 | 李爱华 | Flue gas processing method and its device |
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| US20030126869A1 (en) * | 2002-01-09 | 2003-07-10 | Wen-Jie Liu | Window air conditioner with a fire alarm and smoke exhausting device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102901113A (en) * | 2011-07-25 | 2013-01-30 | 邵勇 | Technology and device for recovering heat energy of discharging chimney |
| CN107983077A (en) * | 2017-12-02 | 2018-05-04 | 北京清新环境技术股份有限公司 | A kind of system and method for administering desulfurization fume white plume |
| CN109012068A (en) * | 2018-10-17 | 2018-12-18 | 上海外高桥第二发电有限责任公司 | It is a kind of for administering the Emission Optimization method of white plume |
| CN110285439A (en) * | 2019-07-25 | 2019-09-27 | 李爱华 | Flue gas processing method and its device |
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