CN111947162B - Method for measuring and calculating main control temperature of first flue gas of garbage incinerator - Google Patents
Method for measuring and calculating main control temperature of first flue gas of garbage incinerator Download PDFInfo
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 100
- 239000003546 flue gas Substances 0.000 title claims abstract description 100
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000012544 monitoring process Methods 0.000 claims abstract description 111
- 239000000779 smoke Substances 0.000 claims abstract description 21
- 238000004364 calculation method Methods 0.000 claims abstract description 17
- 230000014759 maintenance of location Effects 0.000 claims abstract description 12
- 238000012937 correction Methods 0.000 claims description 29
- 238000002485 combustion reaction Methods 0.000 claims description 23
- 238000002347 injection Methods 0.000 claims description 10
- 239000007924 injection Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
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- 101150041829 lea1 gene Proteins 0.000 claims description 5
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 3
- 238000005260 corrosion Methods 0.000 claims description 3
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- 238000003780 insertion Methods 0.000 claims description 3
- 230000037431 insertion Effects 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 238000011056 performance test Methods 0.000 claims description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract description 12
- 239000000126 substance Substances 0.000 abstract description 11
- 238000005516 engineering process Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000000185 dioxinlike effect Effects 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000012800 visualization Methods 0.000 description 2
- 150000001491 aromatic compounds Chemical class 0.000 description 1
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- 231100000719 pollutant Toxicity 0.000 description 1
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- 238000013341 scale-up Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/50—Control or safety arrangements
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- G—PHYSICS
- G06—COMPUTING; CALCULATING OR COUNTING
- G06F—ELECTRIC DIGITAL DATA PROCESSING
- G06F17/00—Digital computing or data processing equipment or methods, specially adapted for specific functions
- G06F17/10—Complex mathematical operations
Abstract
The problems that the actual physical structure and the hearth temperature distribution of a typical garbage incinerator are not fully considered in the conventional garbage incineration process, so that the actually calculated retention time is small, the effective control of dioxin substances is difficult to guarantee, and the like are solved. The invention provides a method for measuring and calculating the main control temperature of first flue gas of a garbage incinerator, which comprises the following steps: first, the zero altitude H, which is the starting point of calculation of the master control temperature, is determined 0 The position, the second, appointing each temperature monitoring section and respectively measuring and calculating the temperature of the corresponding furnace section, and the third, measuring and calculating the smoke retention time t when the temperature of the first flue smoke reaches 850 DEG C 850 Fourthly, measuring and calculating the height H of the flue gas when the temperature of the main flue gas of the first flue reaches 850 DEG C 850 Correcting the temperature T by the mean of the respective monitored sections nc Simplifying calculation by utilizing a linear approximation principle and adopting an interpolation method, fifth, measuring and calculating actual flue gas flow and flow velocity, and sixth, measuring and calculating actual height H of the first flue gas after 2 seconds of operation 2s And a master temperature T 2s 。
Description
Technical Field
The invention relates to the technical field of urban domestic garbage incineration, in particular to a method for measuring and calculating the main control temperature of first flue gas of a garbage incinerator.
Background
The Dioxin-like substance is named Dioxin in English, and refers to a general name of a class of planar aromatic compounds with similar molecular structures, physical properties and chemical properties, and the total number of the substances is 210. Dioxin is highly lipophilic and is accumulated in fat after entering a human body. In addition, it also readily forms strong bonds with soil or other particulate matter, is extremely difficult to remove once contaminated, is highly durable and cumulative, and can pose a serious hazard to humans through the scale-up of the food chain.
Dioxin is generally white crystal, has a melting point of 302-305 ℃, starts to decompose at 500 ℃, and completely decomposes within 2s at 800 ℃. Dioxin substances are pollutants mainly monitored in the process of waste incineration power generation, because ways for producing household garbage are different, garbage components are complex, dioxin can be generated in the process of producing some garbage, and documents show that the household garbage contains about 0.03-0.1ngTEQ/kg of dioxin, and the dioxin cannot be thoroughly decomposed in the high-temperature incineration stage and enters rear smoke. The existing online monitoring technology at home and abroad does not realize online monitoring of dioxin substances, and the environment monitoring generally adopts a mode of regular sampling detection.
Domestic and foreign researches show that the sufficient decomposition of dioxin-like substances can be ensured only on the premise that the flow field is sufficiently disturbed when the main control temperature (the flue gas temperature is more than 850 ℃ and the retention time is more than 2s) is met. Most of the existing main control temperature monitoring technologies usually only monitor the temperature when the retention time of the flue gas reaches 2 s. Although the technology provides a research on a calculation method of the actual retention time of the flue gas temperature at 850 ℃, the actual physical structure and the hearth temperature distribution of a typical garbage incinerator are not fully considered, so that the actually calculated retention time is small, even the theoretical retention time is difficult to achieve, and the effective control of dioxin substances is difficult to ensure.
Meanwhile, according to the existing environmental protection policy, the selection of the calculation starting point in the prior art has certain errors, and the flow rate of the flue gas is not calculated through the actual real flue gas volume and the effective volume of the flue, so that the requirements of the existing environmental protection policy are difficult to meet.
Disclosure of Invention
The invention solves the technical problem by adopting the technical scheme that a method for measuring and calculating the main control temperature of the flue gas of a first flue of a garbage incinerator comprises the following steps:
first, the zero altitude H, which is the starting point of calculation of the master control temperature, is determined 0 The position of the mobile phone is determined,
according to environmental regulations, H 0 The position of the last secondary air (the highest layer of secondary air arranged in the incinerator) injection inlet;
secondly, appointing each temperature monitoring section and respectively measuring and calculating the temperature of the corresponding furnace section, further knowing the temperature distribution of the furnace, starting from the last secondary air section of the garbage incinerator, respectively setting the temperature monitoring sections with different elevations from low to high, wherein the elevation is H 0 0 th temperature monitoring section (last secondary air injection port section) with elevation of H Top roof The ceiling temperature monitoring section (the temperature monitoring section located at the uppermost layer) and the elevation are in the range of H 0 And H Top roof A plurality of temperature monitoring sections in between;
thirdly, measuring and calculating the smoke retention time t when the smoke temperature of the first flue reaches 850 DEG C 850 ，
In the formula t 850 The residence time of the first flue gas reaching 850 ℃ is expressed in s (seconds);
H 0 as an elevation origin (starting point, corresponding to the 0 th temperature monitoring section);
H 1 is the outlet elevation of the post combustion chamber (corresponding to the first temperature monitoring section);
H 850 the elevation of the flue gas when the temperature of the flue gas of the first flue reaches 850 ℃ is expressed in m (meter);
Δ H is the calculation starting point H 0 To H 850 In m (meters);
ΔH 0 marking the height H for the starting point 0 To the outlet level H of the post combustion chamber 1 The height difference between them, in m (meters);
ΔH 1 is H 850 To the outlet level H of the post combustion chamber 1 The height difference between them, in m (meters);
t 1 the residence time of the flue gas from the starting point to the outlet of the post-combustion chamber is calculated and is expressed in s (seconds);
t 2 the residence time of the flue gas in the first flue is s (second);
v 1 calculating the average flow speed of the flue gas of a first flue from a starting point to an outlet of a post combustion chamber, wherein the unit is m/s (meter/second);
v 2 is H 850 The average flow speed of the flue gas of the first flue to the outlet of the post combustion chamber is in the unit of m/s (meter/second);
fourthly, the height H of the flue gas when the temperature of the main flue gas of the first flue reaches 850 ℃ is measured and calculated 850 Correcting the temperature T by the mean of the respective monitored sections nc The simplified calculation is carried out by utilizing the principle of linear approximation and adopting an interpolation method,
from the elevation origin H 0 (starting point) starting from the bottom to the top, the corrected average temperature T of each section nc Respectively judging with 850 deg.C, when the average temperature after correcting a certain section is less than 850 deg.C,determining H from the temperature monitoring section and the next temperature monitoring section 850 In a specific position of, wherein, T nc Monitoring the corrected average temperature of the section for a certain temperature, e.g. H for elevation 0 0 th temperature monitoring section corrected average temperature T 0c Elevation is H 1 After the first temperature monitoring section is corrected, the average temperature T 1c … … until the elevation is H Top roof The average temperature T of the first flue ceiling temperature monitoring section after correction Item c (temperature monitoring section of the uppermost layer),
when T is 1c When the temperature is less than or equal to 850 ℃, the method belongs to the low load starting stage of the incinerator:
in the formula T 0c 、T 1c Respectively the average correction temperature of the secondary air injection port and the first monitoring section, and the unit is the temperature T Secondary roof c At a temperature of > 850 ℃, in this case belonging to an incinerator overload stage, wherein T Secondary roof c Is a first flue secondary ceiling temperature monitoring section (the secondary ceiling temperature monitoring section is a first section below the uppermost layer temperature monitoring section),
in the formula T Secondary roof c 、T Top c The unit is the average correction temperature of the first flue secondary ceiling and the average correction temperature of the first flue ceiling respectively,
when T is 850 Between T 1c And T Secondary roof c In between, H is determined from the average corrected temperature of adjacent sections using the principles described above 850 ，
Fifthly, measuring and calculating the actual flue gas flow and flow velocity,
sixthly, measuring and calculating the actual height H of the first flue gas after 2 seconds of operation 2s And a master temperature T 2s ，
From H 2s Determining the result of calculating T 2s Two adjacent temperature profiles, Q sj Is the standard condition wet basis flow (wet flue gas flow under standard working condition) and is calculated by utilizing a linear interpolation method,
in the formula T ncL The average correction temperature of the lower section of the temperature area where the main control temperature is located is measured in units of; t is nch The average correction temperature of the upper section of the temperature area where the master control temperature is located is measured in units of; h h And H L The heights of the upper and lower sections of the temperature area where the master control temperature is located are respectively expressed in m.
In the second step, a temperature detecting device is respectively and correspondingly arranged on each temperature monitoring section, specifically, a thermometer is respectively arranged on the left and right side walls and the front wall of the incinerator of each section for temperature monitoring, and T is ni Temperature of monitoring point representing each temperature monitoring section (wherein n represents nth temperature monitoring section, i is 1,2,3), T 01 、T 02 、T 03 Respectively representing the monitoring temperatures of a left side wall, a right side wall and a front wall which are arranged on the 0 th temperature monitoring section; t is 11 、T 12 、T 13 Respectively representing the monitoring temperatures of the left side wall, the right side wall and the front wall which are arranged on the first temperature monitoring section; t is Top 1 、T Top 2 、T Top 3 Respectively representing the monitoring temperatures of the left and right side walls and the front wall of the temperature monitoring section of the first flue ceiling.
In the fourth step, the temperature measuring device is a high-temperature corrosion-resistant wear-resistant K/S type thermocouple, the insertion depth is 500mm, the temperature measured by the thermocouple can only represent the temperature of the side wall near the installation position, the real average temperature of each section needs to be corrected, and T is nc For each cross section after correctionAverage temperature of T 0c Corrected average temperature, T, for the 0 th critical section 1c Corrected average temperature, T, of the first temporary measured section Top c The corrected average temperature of the first flue ceiling temperature monitoring section,
in the formula Q s The actual evaporation capacity of the garbage incinerator is t/h; q N Rated evaporation capacity of the garbage incinerator is t/h; a. b is a dimensionless load correction coefficient, which is checked according to the regular performance test of the incinerator;
the sum of all temperatures of each cross section.
In the preferred scheme of the invention, in the fifth step, the actual flue gas flow of the first flue can be calculated by the total amount of all combustion-supporting air participating in the incineration process of the incinerator:
Q s ＝(Q pri +Q sec +Q pur +Q lea1 )k+Q bur (7)
in the formula Q s Is the total flue gas volume of the first flue, and the unit is Nm 3 H (standard cubic meters per hour); q pri 、Q sec 、Q pur 、Q lea1 、Q bur Respectively represents the total amount of primary air and secondary air of the incinerator, the total amount of various types of blowing air, air leakage of an incineration system and the amount of flue gas generated by combustion of a combustor, and the unit is Nm 3 H; k is a dimensionless smoke coefficient, the influence caused by the air coefficient in the reaction process is generally between 1.1 and 1.192, the total air volume is regularly corrected through performance experiments,
in the preferred embodiment of the present invention, in the fifth step, the actual flue gas flow of the first flue may also be calculated by using a flue gas flow rate measuring device disposed at the rear end of the flue gas flow:
Q s ＝(Q yan -Q lea2 )×c (8)
in the formula Q s Is the total flue gas quantity of the first flue, Nm 3 /h；Q yan 、Q lea2 Respectively representing the total smoke gas quantity at the rear end of the smoke gas flow, the total air leakage quantity at the rear end of the smoke gas flow, Nm 3 H; c is a dimensionless correction coefficient, the relation between the total amount discharged at the rear end of the reaction flue gas flow and the total amount of the flue gas of the first flue is corrected regularly through performance experiments,
starting point to the residence time t of the flue gas in the outlet of the post-combustion chamber 1 ：
Wherein V1 is the starting point H 0 To the outlet H of the afterburner 1 Volume of afterburner in between, in m 3 ；Q sj The standard condition wet basis flow (wet flue gas flow under standard working conditions); d is a dimensionless smoke pressure correction coefficient, generally 1.0028 is taken under automatic control,
the residence time t from the outlet of the post combustion chamber to the temperature of the flue gas of the first flue reaching 850 DEG C 2 ：
In the formula, S is the cross sectional area of the section of the first flue and has the unit of square meter.
The invention prompts that parameters such as temperature of each section of a hearth, total combustion-supporting air quantity and the like are acquired in real time by using a Distributed Control System (DCS), and H is made on a monitoring picture of an incineration hearth by using a dynamic visualization technology 850 And the dynamic display unit is used for displaying the related retention time, is convenient to operate and adjust the incineration working condition in time, and ensures the emission control of dioxin substances.
The furnace temperature dynamic display technology is easy to deploy through a DCS control system, and a good dynamic display effect is obtained. The calculation of the average temperature of the specified temperature section is beneficial to guiding the scientific operation of denitration (SNCR) in the furnace.
The invention has the beneficial effects that: the dynamic display technology for the main control temperature of the flue gas of the first flue of the garbage incinerator can fully combine the physical structure of the incinerator, the real flow rate of the flue gas and the average temperature of the temperature section surface of the hearth, reflect the real residence time and the flue gas height when the temperature of the flue gas of the incinerator reaches 850 ℃ in real time, facilitate the timely adjustment of the incineration by operators, and ensure the full decomposition of dioxin-like substances.
Drawings
Fig. 1, fig. 2 and fig. 3 are schematic structural diagrams of a first embodiment of the present invention. Fig. 1 is a schematic structural diagram of a first flue of the garbage incinerator, fig. 2 is a schematic elevation diagram of each monitoring section of the first flue of the garbage incinerator, and fig. 3 is a layout diagram of a thermometer for monitoring the section of the first flue.
In the drawings
1. A furnace chamber is arranged in the furnace chamber,
2. a first flue, 2A ceiling, 2.0 elevation of H 0 0 th temperature monitoring section (last secondary air injection port section), 2.1 elevation is H 1 2.2 elevation of the first temperature monitoring section (afterburner outlet) of (1) 2 2.3 elevation of H 3 2.4 elevation of H Top roof The ceiling temperature monitoring section (namely the fourth temperature monitoring section at the topmost layer) has the elevation of 2.5H 2 seconds The temperature monitoring section when the flue gas stays for 2 seconds, and the 2.6 elevation is H 850℃ The flue gas reaches the temperature monitoring section of 850 ℃,
3. a secondary air fan,
4. a secondary air pipeline is arranged on the air inlet of the air conditioner,
5.1 left side wall thermometer, 5.2 right side wall thermometer, 5.3 front wall thermometer.
Detailed Description
Fig. 1, fig. 2 and fig. 3 are schematic structural diagrams of a first embodiment of the present invention. Fig. 1 is a schematic view of a first flue structure of a garbage incinerator, fig. 2 is a schematic view of elevation of each monitoring section of the first flue of the garbage incinerator, and fig. 3 is a layout view of a thermometer for monitoring the section of the first flue.
In this example, a method for measuring and calculating the main control temperature of the flue gas in the first flue of a garbage incinerator comprises the following steps:
first, the zero altitude H, which is the starting point of calculation of the master control temperature, is determined 0 ，
According to environmental regulations, H 0 The position of the last secondary air (the highest layer of secondary air arranged in the incinerator) injection inlet is adopted.
And secondly, appointing each temperature monitoring section, respectively measuring and calculating the temperature of the corresponding furnace section, and further knowing the temperature distribution of the furnace. FIG. 2 shows that in this example, five temperature monitoring sections with different elevations are set from low to high, including the elevation H, starting with the last secondary air section of the garbage incinerator 0 (zero elevation) 0 th temperature monitoring section 2.0 (last secondary air injection port section) with elevation H 1 First temperature monitoring section 2.1 (afterburner outlet) at level H 2 A second temperature monitoring section 2.2 with an elevation of H 3 The third temperature monitoring section 2.3 and the elevation are H Top roof 2.4 (i.e., the fourth temperature monitoring section located at the topmost layer).
In this example, a temperature detection device is correspondingly arranged on each temperature monitoring section; as shown in FIG. 3, a thermometer is respectively arranged on the left and right side walls and the front wall of the incinerator at each section for temperature monitoring, T ni Represents the monitoring point temperature of each monitoring section, wherein n is 0, 1,2,3, 4 (representing the 0 th temperature monitoring section to the fourth temperature monitoring section), i is 1,2,3 (representing the monitoring temperature of the left and right side walls and the front wall respectively), and T is 01 、T 02 、T 03 Respectively representing the monitoring temperatures of the left side wall, the right side wall and the front wall which are arranged on the 0 th temperature monitoring section; t is 11 、T 12 、T 13 Respectively representing the monitoring temperatures of the left side wall, the right side wall and the front wall which are arranged on the first temperature monitoring section; t is 41 、T 42 、T 43 Respectively representing the monitoring temperatures of the left and right side walls and the front wall of the temperature monitoring section of the first flue ceiling.
Thirdly, measuring and calculating the smoke retention time t when the smoke temperature of the first flue reaches 850 DEG C 850 ，
In the formula t 850 The residence time of the first flue gas to reach 850 ℃ is expressed in s (seconds);
H 0 the initial point of the elevation is the zero elevation (starting point, corresponding to the 0 th temperature monitoring section);
H 1 is the outlet elevation of the post combustion chamber (corresponding to the first temperature monitoring section);
H 850 the elevation of the flue gas when the temperature of the flue gas of the first flue reaches 850 ℃ is expressed in m (meter);
Δ H is the calculation starting point H 0 To H 850 In m (meters);
ΔH 0 marking the height H for the starting point 0 To the outlet level H of the post combustion chamber 1 The height difference between them, in m (meters);
ΔH 1 is H 850 To the outlet level H of the post combustion chamber 1 The height difference between them, in m (meters);
t 1 the residence time of the flue gas from the starting point to the outlet of the post-combustion chamber is calculated and is expressed in s (seconds);
t 2 the residence time of the flue gas in the first flue is s (seconds);
v 1 the average flow speed of the flue gas of a first flue from a starting point to an outlet of a post combustion chamber is calculated, and the unit is m/s (meter/second);
v 2 is H 850 The average flow speed of the flue gas of the first flue to the outlet of the post combustion chamber is in the unit of m/s (meter/second);
fourthly, the height H of the flue gas when the temperature of the main flue gas of the first flue reaches 850 ℃ is measured and calculated 850 Correcting the temperature T by the mean of the respective monitored sections nc The simplified calculation is carried out by interpolation method based on the principle of linear approximation.
In this example, from the origin of elevation H 0 Starting from the starting point, the total five temperature monitoring sections from bottom to top are arranged, namely a 0 th temperature monitoring section to a fourth temperature monitoring section, wherein the fourth temperature monitoring section is a first flue ceiling temperature monitoring section (the elevation is H) 4 ). Corrected average temperature T of each cross section nc Respectively judging with 850 deg.C, and determining H from the temperature section and the next layer of temperature section when the average temperature of one section after correction is less than 850 deg.C 850 The specific location of (a). Wherein, T nc Corrected average temperature for a monitored cross-section, i.e. elevation H 0 0 th monitoring section average correction temperature T 0c Elevation is H 1 First monitored cross-section average correction temperature T 1c … … until the elevation is H 4 First flue ceiling temperature monitoring section average correction temperature T 4c In this example, the temperature measuring device is a high-temperature corrosion-resistant wear-resistant K/S type thermocouple, the insertion depth is 500mm, considering that the temperature measured by the thermocouple can only represent the temperature of the side wall near the installation position, the real average temperature of each section needs to be corrected, and T is nc For the corrected average temperature, T, of each cross-section 0c Corrected average temperature, T, for the 0 th temporary section 1c Corrected average temperature, T, for the first temporary measured section Top c The corrected average temperature of the first flue ceiling temperature monitoring section,
in the formula Q s The actual evaporation capacity of the garbage incinerator is t/h; q N Rated evaporation capacity of the garbage incinerator is t/h; a. b is a dimensionless load correction coefficient, which is checked according to the regular performance test of the incinerator;
the sum of all temperatures of each cross section.
When T is 1c When the temperature is less than or equal to 850 ℃, the method belongs to the low load starting stage of the incinerator:
in the formula T 0c 、T 1c Respectively average calibration of secondary air injection port and first monitoring sectionPositive temperature in ° c when T 3c At a temperature of > 850 ℃, in this case belonging to an incinerator overload stage, wherein T 3c Monitoring the cross-sectional average corrected temperature for a third temperature,
in the formula T 3c 、T 4c The average correction temperature of the third monitoring section and the first flue ceiling is respectively in the unit of ℃.
When T is 850 Between T 1c And T 3c In between, H is determined from the average corrected temperature of adjacent sections using the principles described above 850 ，
And fifthly, measuring and calculating the actual flue gas flow and flow velocity. In this example, the actual flue gas flow of the first flue can be calculated by the total amount of all combustion-supporting air participating in the incineration process of the incinerator:
Q s ＝(Q pri +Q sec +Q pur +Q lea1 )k+Q bur
in the formula Q s Is the total flue gas volume of the first flue, and the unit is Nm 3 Per hour (standard cubic meters per hour); q pri 、Q sec 、Q pur 、Q lea1 、Q bur Respectively represents the total amount of primary air and secondary air of the incinerator, the total amount of various types of blowing air, air leakage of an incineration system and the amount of flue gas generated by combustion of a combustor, and the unit is Nm 3 H; k is a dimensionless smoke coefficient, the influence caused by the air coefficient in the reaction process is generally 1.1-1.192, and the total air volume is regularly corrected through performance experiments.
Sixthly, measuring and calculating the actual height H of the first flue gas after 2 seconds of operation 2s And a master temperature T 2s ，
From H 2s Determining the result of calculating T 2s Two adjacent temperature profiles and using linear interpolationAnd calculating by a value method.
The present invention suggests that, unlike the first embodiment, in other embodiments, in the fifth step, the actual flue gas flow of the first flue may also be calculated by using a flue gas volume measuring device arranged at the rear end of the flue gas flow:
Q s ＝(Q yan -Q lea2 )×c
in the formula Q s Is the total flue gas quantity of the first flue, Nm 3 /h；Q yan 、Q lea2 Respectively representing the total smoke gas quantity at the rear end of the smoke gas flow, the total air leakage quantity at the rear end of the smoke gas flow, Nm 3 H; c is a dimensionless correction coefficient, the relation between the total amount discharged at the rear end of the reaction flue gas flow and the total amount of the flue gas of the first flue is corrected regularly through performance experiments,
starting point to the residence time t of the flue gas in the outlet of the post-combustion chamber 1 ：
Wherein V1 is the starting point H 0 To the outlet H of the afterburner 1 Volume of afterburner in between, in m 3 ；Q sj The standard condition wet basis flow (wet flue gas flow under standard working conditions); d is a dimensionless smoke pressure correction coefficient, generally 1.0028 is taken under automatic control,
the residence time t from the outlet of the post combustion chamber to the temperature of the flue gas of the first flue reaching 850 DEG C 2 ：
In the formula, S is the cross sectional area of the section of the first flue and has the unit of square meter.
The invention prompts that parameters such as temperature of each section of a hearth, total combustion-supporting air quantity and the like are acquired in real time by using a Distributed Control System (DCS), and H is made on a monitoring picture of an incineration hearth by using a dynamic visualization technology 850 And the dynamic display unit is used for displaying the related retention time, is convenient to operate and adjust the incineration working condition in time, and ensures the emission control of dioxin substances.
The furnace temperature dynamic display technology is easy to deploy through a DCS control system, and a good dynamic display effect is obtained. The calculation of the average temperature of the specified temperature section is beneficial to guiding the scientific operation of denitration (SNCR) in the furnace.
Claims (6)
1. A method for measuring and calculating the main control temperature of first flue gas of a garbage incinerator comprises the following steps:
first, a calculation start position H for calculating the master temperature is determined 0 Selecting the position of the last secondary air nozzle as the position H of the calculation starting point 0
Secondly, appointing each temperature monitoring section and respectively measuring and calculating the temperature of the corresponding furnace section, further knowing the temperature distribution of the furnace, respectively setting temperature monitoring sections with different elevations from low to high from the last secondary air section of the garbage incinerator, wherein the 0 th temperature monitoring section passes through the position H of the calculation starting point 0 Ceiling temperature monitoring section H Top roof And elevation is at H 0 And H Top roof A plurality of temperature monitoring sections in between;
thirdly, measuring and calculating the smoke retention time t when the temperature of the first flue smoke reaches 850 DEG C 850 ，
t 850 =
In the formula t 850 The residence time of the first flue gas to reach 850 ℃ is s(seconds);
H 1 the elevation of the outlet of the afterburner chamber is corresponding to a first temperature monitoring section;
H 850 the elevation of the flue gas when the temperature of the flue gas of the first flue reaches 850 ℃ is expressed in m (meter);
Δ H is the calculated starting position H 0 To H 850 In m (meters);
∆H 0 to calculate the starting point position H 0 To H 1 The height difference between them, in m (meters);
∆H 1 is H 850 To H 1 The height difference therebetween in m (meters);
t 1 the residence time of the flue gas from the starting point to the outlet of the post-combustion chamber is calculated and is expressed in s (seconds);
t 2 the residence time of the flue gas in the first flue is s (seconds);
v1 is the average flow velocity of the flue gas of the first flue from the starting point to the outlet of the post combustor, and the unit is m/s (meter/second);
v 2 is H 850 The average flow speed of the flue gas of the first flue to the outlet of the post combustion chamber is in the unit of m/s (meter/second);
fourthly, measuring and calculating the height H of the flue gas when the temperature of the flue gas of the first flue reaches 850 DEG C 850 Correcting the temperature T by the mean of the respective monitored sections nc The simplified calculation is carried out by utilizing the principle of linear approximation and adopting an interpolation method,
from the calculation of the starting position H 0 Starting from the bottom to the top, the corrected average temperature T of each section nc Respectively judging with 850 deg.C, and determining H from the temperature monitoring section and the next temperature monitoring section when the average temperature of one section after correction is less than 850 deg.C 850 In a specific position of, wherein, T nc Monitoring the corrected average temperature of the section for a certain temperature, e.g. calculating the starting point position H 0 0 th temperature monitoring section corrected average temperature T 0c ， H 1 After the first temperature monitoring section is corrected, the average temperature T 1c … … until the elevation is H Top roof First flue ceiling temperature monitorAverage temperature T after cross section correction Item c Namely the temperature monitoring section of the uppermost layer,
when T is 1c When the temperature is less than or equal to 850 ℃, the method belongs to the low load starting stage of the incinerator:
H 850 =
in the formula T 0c 、T 1c Respectively the average correction temperature of the secondary air injection port and the first monitoring section, the unit is,
when T is Secondary roof c When the temperature is higher than 850 ℃, the process belongs to the overload stage of the incinerator,
H 850 =
in the formula:
H top roof The elevation of the temperature monitoring section of the first flue ceiling is obtained;
H secondary roof The elevation of a first section from the uppermost layer of temperature monitoring section to the lower part, namely the elevation of the temperature monitoring section of the first flue secondary ceiling;
T top C The average correction temperature of the temperature monitoring section of the first flue ceiling is calculated in unit;
T sub top C The average correction temperature of the temperature monitoring section of the secondary ceiling of the first flue is obtained; when T is 850 Between T 1c And T Secondary roof c In between, H is determined from the average corrected temperature of adjacent sections using the principles described above 850 ，
Fifthly, measuring and calculating the actual flue gas flow and flow velocity,
sixthly, measuring and calculating the actual height H of the first flue gas after 2 seconds of operation 2s And a master temperature T 2s ，
H 2s =
From H 2s Determining the result of calculating T 2s Two adjacent temperature sections of (C), Q sj Is the standard condition wet basis flow and is calculated by utilizing a linear interpolation method,
T 2s =
in the formula T ncL The average correction temperature of the lower section of the temperature area where the main control temperature is located is measured in units of; t is nch The average correction temperature of the upper section of the temperature area where the main control temperature is located is measured in units of; h h And H L The heights of the upper and lower sections of the temperature area where the master control temperature is located are respectively expressed in m.
2. The method for measuring and calculating the flue gas main control temperature of the first flue of the garbage incinerator according to claim 1, wherein in the first step, the last secondary air injection position is the highest layer secondary air injection position of the incinerator.
3. The method for measuring and calculating the flue gas main control temperature of the first flue of the garbage incinerator according to claim 1, wherein in the second step, temperature detecting devices are correspondingly arranged on the temperature monitoring sections, specifically, a thermometer is arranged on each of the left and right side walls and the front wall of the incinerator on each section for temperature monitoring, and T is the temperature of the flue gas main control temperature of the first flue of the garbage incinerator ni Represents the monitoring point temperature of each temperature monitoring section, wherein n represents the nth temperature monitoring section, and i =1,2, 3; t is 01 、T 02 、T 03 Respectively representing the monitoring temperatures of the left side wall, the right side wall and the front wall which are arranged on the 0 th temperature monitoring section; t is 11 、T 12 、T 13 Respectively representing the monitoring temperatures of the left side wall, the right side wall and the front wall which are arranged on the first temperature monitoring section; t is a unit of Top 1 、T Top 2 、T Top 3 Respectively representing the monitoring temperatures of the left and right side walls and the front wall of the temperature monitoring section of the first flue ceiling.
4. A method as claimed in claim 1In the fourth step, the temperature measuring device is a high-temperature corrosion-resistant wear-resistant K/S type thermocouple, the insertion depth is 500mm, the temperature measured by the thermocouple can only represent the temperature of the side wall near the installation position, the real average temperature of each section needs to be corrected, and T is the temperature measured by the thermocouple nc For the corrected average temperature, T, of each cross-section 0c Corrected average temperature, T, for the 0 th temporary section 1c Corrected average temperature, T, for the first temporary measured section Top c The corrected average temperature of the first flue ceiling temperature monitoring section,
T nc = 
in the formula Q s The actual evaporation capacity of the garbage incinerator is t/h; q N Rated evaporation capacity of the garbage incinerator is t/h; a. b is a dimensionless load correction coefficient, which is checked according to the regular performance test of the incinerator;
the sum of all temperatures of each cross section.
5. The method for measuring and calculating the main control temperature of the flue gas in the first flue of the garbage incinerator according to claim 1, wherein in the fifth step, the actual flue gas flow of the first flue can be calculated by the total amount of all combustion-supporting air participating in the incineration process of the incinerator:
Q s =
in the formula Q s The unit is Nm/h (standard cubic meters per hour) for the total flue gas quantity of the first flue; q pri 、Q sec 、Q pur 、Q lea1 、Q bur Respectively representing the total amount of primary air, the total amount of secondary air, the total amount of various types of blowing air, air leakage of an incineration system and the amount of flue gas generated by combustion of a combustor in Nm/h;k is a dimensionless smoke coefficient, the influence caused by the air coefficient in the reaction process is generally 1.1-1.192, and the total air volume is regularly corrected through performance experiments.
6. The method for measuring and calculating the main control temperature of the flue gas in the first flue of the garbage incinerator according to claim 1, wherein in the fifth step, the actual flue gas flow of the first flue can also be calculated by a flue gas flow measuring device arranged at the rear end of the flue gas flow:
Q s =
in the formula Q s Carrying out Nm/h for the total flue gas volume of the first flue; q yan 、Q lea2 Respectively representing the total flue gas quantity at the rear end of the flue gas flow, the total air leakage quantity at the rear end of the flue gas flow, Nm/h; c is a dimensionless correction coefficient, the relation between the total amount discharged at the rear end of the reaction flue gas flow and the total amount of the flue gas of the first flue is corrected regularly through performance experiments,
starting point to the residence time t of the flue gas in the outlet of the post-combustion chamber 1 ：
t 1 =
Wherein V1 is the calculated starting position H 0 To the outlet H of the afterburner 1 In m, for the volume of the afterburner between; q sj The standard wet base flow and the standard wet flue gas flow are obtained; d is a dimensionless smoke pressure correction coefficient, generally 1.0028 is taken under automatic control,
the residence time t from the outlet of the post combustion chamber to the temperature of the flue gas of the first flue reaching 850 DEG C 2 ：
t 2 =
In the formula, S is the cross sectional area of the section of the first flue and has the unit of square meter.
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