CN112710160A - Control method and device for hot air fan during cold start of analysis tower - Google Patents

Control method and device for hot air fan during cold start of analysis tower Download PDF

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Publication number
CN112710160A
CN112710160A CN201911025479.3A CN201911025479A CN112710160A CN 112710160 A CN112710160 A CN 112710160A CN 201911025479 A CN201911025479 A CN 201911025479A CN 112710160 A CN112710160 A CN 112710160A
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hot air
temperature
heating section
tower
activated carbon
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CN112710160B (en
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刘雁飞
魏进超
周浩宇
李俊杰
刘昌齐
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Hunan Zhongye Changtian Energy Conservation And Environmental Protection Technology Co ltd
Zhongye Changtian International Engineering Co Ltd
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Hunan Zhongye Changtian Energy Conservation And Environmental Protection Technology Co ltd
Zhongye Changtian International Engineering Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D19/00—Arrangements of controlling devices
    • F27D2019/0028—Regulation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
    • F27M2003/00—Type of treatment of the charge
    • F27M2003/04—Sintering
    • 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
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/70—Efficient control or regulation technologies, e.g. for control of refrigerant flow, motor or heating

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Treating Waste Gases (AREA)

Abstract

The application discloses a control method of a hot air fan during cold starting of an analytic tower, which comprises the following steps: the activated carbon starts flowing in the heating section of the desorption tower; supplying heat to the heating section of the analysis tower through a hot blast stove of the analysis tower and the hot blast fan; acquiring the hot air inlet temperature of the heating section, the hot air outlet temperature of the heating section, the starting point temperature of the heating section and the target control temperature of the terminal point of the heating section, the working heat exchange coefficient of the heating section and the current feeding machine rotating speed of a feeding machine of the analysis tower; and obtaining the target rotating speed of the hot air fan according to the parameters. The method can accurately control the rotating speed of the hot air fan when the analysis tower is started in a cold state, so that the problem of electric energy and fuel waste caused by excessive heat input by the hot air furnace can be effectively solved. In addition, the application also discloses a hot-blast fan control device when the analysis tower is started in a cold state.

Description

Control method and device for hot air fan during cold start of analysis tower
Technical Field
The application relates to the technical field of sintering flue gas purification, in particular to a control method of a hot air fan during cold start of an analytic tower. In addition, the application also relates to a hot air blower control device during cold starting of the analysis tower.
Background
The amount of flue gas generated in the sintering process accounts for about 70% of the total flow of steel, and the main pollutant components in the sintering flue gas comprise dust, SO2 and NOX; in addition, a small amount of VOCs, dioxin, heavy metals and the like are also added; the waste water can be discharged after purification treatment. At present, the technology of treating sintering flue gas by using an activated carbon desulfurization and denitrification device is mature, and the activated carbon desulfurization and denitrification device is popularized and used in China, so that a good effect is achieved.
Referring to fig. 1, fig. 2, fig. 3 and fig. 4, fig. 1 is a schematic structural diagram of a sintering flue gas purification device in the prior art; FIG. 2 is a schematic structural diagram of a desorption tower of the sintering flue gas purification device in FIG. 1; FIG. 3 is a schematic diagram of the heating section of the resolution tower of FIG. 2; fig. 4 is a schematic cross-sectional view of the heating section of fig. 3.
As shown in fig. 1, the sintering flue gas purification apparatus in the prior art includes an adsorption tower 2, a first activated carbon conveyor S1, an activated carbon storage 3, a belt scale C1, a desorption tower 1, a vibrating screen 4, a second activated carbon conveyor S2, and the like. The analysis tower 1 includes a buffer bin 106, an analysis tower feed valve 107, an analysis tower feeder G1, and the like. The adsorption tower 2 includes components such as an adsorption tower feed valve 201 and an adsorption tower feeder G2.
As shown in fig. 1, during operation, raw flue gas (the main component of the pollutant is SO2) generated in the sintering process passes through the activated carbon bed layer of the adsorption tower 2 and becomes clean flue gas to be discharged. The activated carbon adsorbing the pollutants (the main component of the pollutants is SO2) in the flue gas is sent into the desorption tower 1 through the first activated carbon conveyor S1, the activated carbon adsorbing the pollutants in the desorption tower 1 is heated to 400-430 ℃ for desorption and activation, SRG (sulfur-rich) gas released after the desorption and activation is subjected to an acid preparation process, the activated carbon after the desorption and activation is cooled to 110-130 ℃ and then discharged out of the desorption tower 1, the activated carbon dust is screened out by the vibrating screen 4, and the activated carbon particles on the screen reenter the adsorption tower 2 through the second activated carbon conveyor S2, SO that the circulating flow of the activated carbon is realized. The active carbon is lost in the circulating flow, so that the active carbon storage bin 3 is metered by a belt scale C1, and the active carbon is supplemented.
As shown in fig. 2, the desorption tower 1 comprises a buffer bin 106, a desorption tower feed valve 107, a feed section 101, a heating section 102, a holding section 103, a residence section 108, a cooling section 104, a discharge section 105, a desorption tower feeder G1, a hot air system, a cooling air system, a nitrogen system, and an SRG gas system.
As shown in fig. 3, a hot air baffle 1021 is arranged inside the heating section 102. The hot air system comprises a hot air furnace L1 and a hot air blower F1, the hot air furnace L1 heats air, and the hot air blower F1 enables the heated air to move rapidly in a circulating mode, so that hot air enters from an air inlet and flows out from a hot air outlet.
As shown in fig. 4, the activated carbon flows downwards in the steel tube of the heating section 102, the hot air passes through the heating section 102, the activated carbon flowing in the steel tube is heated by heating the steel tube, and the activated carbon is hermetically isolated from the hot air; the temperature of the activated carbon at the starting point of the heating section 102 is between 80 and 150 ℃, generally about 100 ℃; the temperature at the end point of the heating section 102 is 400-440 ℃, and the temperature reaches more than 400 ℃, thus meeting the analysis requirement of the activated carbon.
As shown in fig. 3, hot air blower F1 circulates hot air in a closed loop between the pipeline and the desorption tower 1 to heat the activated carbon. At present, the control of a hot air fan F1 is inaccurate, and the situations that the rotating speed of the hot air fan F1 is too high, the input heat of a hot blast stove L1 is too much, and electric energy and fuel are wasted exist. Especially, when the analytical tower 1 is started in a cold state, under the conditions of long starting time and difficult starting state evaluation, how to determine the rotating speed of the hot air fan F1, and further accurately control the hot air fan F1, so as to avoid the waste of electric energy and fuel of the hot air furnace L1 is a problem to be solved urgently in the field.
Disclosure of Invention
The technical problem to be solved by the application is to provide a control method for a hot air fan during cold start of an analytic tower, and the method can accurately control the rotating speed of the hot air fan during cold start of the analytic tower, so that the problem of electric energy and fuel waste caused by excessive heat input of a hot air furnace can be effectively avoided.
In order to solve the technical problem, a first aspect of the present application provides a method for controlling a hot air blower during cold start of an analytic tower, which is used for determining a rotating speed of the hot air blower of the analytic tower during cold start, and the method for controlling the hot air blower includes the following steps:
the activated carbon starts flowing in the heating section of the desorption tower;
supplying heat to the heating section of the analysis tower through a hot blast stove of the analysis tower and the hot blast fan;
obtaining the hot air inlet temperature of the heating section and the hot air outlet temperature of the heating section,
acquiring the starting point temperature of the heating section and the target control temperature of the end point of the heating section,
obtaining the working heat exchange coefficient of the heating section,
acquiring the current rotating speed of the feeder of the analysis tower;
and obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the terminal point target control temperature and the current feeding machine rotating speed.
Alternatively to this, the first and second parts may,
the step of obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeder rotating speed comprises the following steps of:
obtaining the target rotating speed based on the following relational expression:
Figure BDA0002248481490000031
wherein, Ff1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; TK represents the endpoint target control temperature; fG1Representing the current feeder rotational speed.
Alternatively to this, the first and second parts may,
before the step of starting the flow of the activated carbon in the heating section of the desorption tower, the method further comprises the following steps:
and filling the desorption tower with activated carbon until the desorption tower reaches the capacity value of the desorption tower.
Alternatively to this, the first and second parts may,
the step of supplying heat to the heating section of the analysis tower through the hot blast stove of the analysis tower and the hot blast fan comprises the following steps:
so that the hot air blower operates at the maximum rotational speed.
Alternatively to this, the first and second parts may,
monitoring the actual temperature of the end point of the heating section.
Alternatively to this, the first and second parts may,
when the end point actual temperature is greater than or equal to the end point target control temperature,
and obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the terminal point target control temperature and the current feeding machine rotating speed.
Alternatively to this, the first and second parts may,
when the end point actual temperature is less than the end point target control temperature,
and adjusting the current rotating speed of the feeder to enable the current rotating speed of the feeder to be smaller than a preset rotating speed value.
Alternatively to this, the first and second parts may,
the preset rotating speed value is obtained through the following relation:
Figure BDA0002248481490000032
wherein, FG1Representing the predetermined rotational speed value; fF1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; t is1TERepresents the end point temperature.
Alternatively to this, the first and second parts may,
the step of obtaining the operating heat exchange coefficient of the heating section comprises:
the operating heat exchange coefficient is obtained by the following relation:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresenting the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeding machine; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan; cf is the specific heat of hot air and is a constant; when the activated carbon is initially loaded, the activated carbon in the desorption tower does not carry pollutants, and K is 1; when production stops restarting, when the desorption tower is started in a re-cooled state, pollutants in the desorption tower carry activated carbon, and K is 1.2-1.3.
Alternatively to this, the first and second parts may,
the starting temperature is obtained by:
acquiring the temperature of each preset temperature measuring point in the starting point plane of the heating section;
the starting point temperature is obtained based on an arithmetic average of the temperatures at the respective temperature measuring points.
In addition, in order to solve the above technical problem, a second aspect of the present application further provides a hot air blower control device for a cold start of a desorption tower, for determining a rotation speed of a hot air blower of the desorption tower at the cold start, including the desorption tower, the desorption tower including:
a heating section for heating the activated carbon flowing through the desorption tower;
the hot air fan is used for blowing hot air into the heating section of the desorption tower;
the feeding machine is used for controlling the discharge flow of the activated carbon in the desorption tower;
the desorption tower comprises:
the first temperature measuring element is used for acquiring the hot air inlet temperature of the heating section of the analysis tower;
the second temperature measuring element is used for acquiring the temperature of the hot air outlet of the heating section;
the third temperature measuring element is used for acquiring the starting point temperature of the heating section;
the first calculation unit is used for acquiring the working heat exchange coefficient of the heating section;
and the second calculation unit is used for obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeding machine rotating speed.
Alternatively to this, the first and second parts may,
the second calculation unit obtains the target rotation speed based on the following relational expression:
Figure BDA0002248481490000051
wherein, Ff1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; TK represents the endpoint target control temperature; fG1Representing the current feeder rotational speed.
Alternatively to this, the first and second parts may,
the first calculating unit obtains the working heat exchange coefficient through the following relational expression:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresenting the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeding machine; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan; cf is the specific heat of hot air and is a constant; when the activated carbon is initially loaded, the activated carbon in the desorption tower does not carry pollutants, and K is 1; when production stops restarting, when the desorption tower is started in a re-cooled state, pollutants in the desorption tower carry activated carbon, and K is 1.2-1.3.
Alternatively to this, the first and second parts may,
the third temperature measuring elements are multiple and are uniformly distributed in the starting point plane of the heating section;
and a plurality of thermocouples for measuring temperature are arranged on each third temperature measuring element.
Alternatively to this, the first and second parts may,
the number of the fourth temperature measuring elements is multiple, and the fourth temperature measuring elements are uniformly distributed in the terminal point plane of the heating section;
and a plurality of thermocouples for measuring temperature are arranged on each fourth temperature measuring element.
In the present application, the hot air blower control method includes the steps of:
the activated carbon starts flowing in the heating section of the desorption tower;
supplying heat to the heating section of the analysis tower through a hot blast stove of the analysis tower and the hot blast fan;
obtaining the hot air inlet temperature of the heating section and the hot air outlet temperature of the heating section,
acquiring the starting point temperature of the heating section and the target control temperature of the end point of the heating section,
obtaining the working heat exchange coefficient of the heating section,
acquiring the current rotating speed of the feeder of the analysis tower;
and obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the terminal point target control temperature and the current feeding machine rotating speed.
The method can accurately control the rotating speed of the hot air fan when the analysis tower is started in a cold state, so that the problem of electric energy and fuel waste caused by excessive heat input by the hot air furnace can be effectively solved.
In addition, the technical effect of the warm air blower control device during cold start of the analysis tower provided by the application is the same as that of the above method, and is not repeated herein.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to the drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a sintering flue gas purification device in the prior art;
FIG. 2 is a schematic structural diagram of a desorption tower of the sintering flue gas purification device in FIG. 1;
FIG. 3 is a schematic diagram of the heating section of the resolution tower of FIG. 2;
FIG. 4 is a schematic cross-sectional view of the heating section of FIG. 3;
FIG. 5 is a schematic illustration of a desorber shown in an exemplary embodiment of the present application;
FIG. 6 is a schematic diagram of the distribution of temperature measuring elements of the desorption tower of FIG. 5;
fig. 7 is a logic flow diagram of a method for controlling a hot wind fan during a cold start of a desorption tower according to an exemplary embodiment of the present application.
Wherein, the corresponding relationship between the component names and the reference numbers in fig. 1 to 6 is:
1, a resolving tower; 101 a feeding section; 102 a heating section; 1021 a hot air baffle plate; 103 heat preservation section; 108 a stay section; 104 a cooling section; 105 a discharge section; 106 a buffer bin; 107 a stripper column feed valve;
2, an adsorption tower; 201 adsorption column feed valve;
3, storing the activated carbon in a warehouse;
4, vibrating a screen;
5 protecting the sleeve;
f1 hot air blower;
hot blast stove L1;
g1 resolving tower feeder; g2 adsorption tower feeder;
s1 a first activated carbon conveyor; s2 a second activated carbon conveyor;
c1 belt scale.
Detailed Description
In order to make the technical solutions of the present invention better understood, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention.
In some of the flows described in the present specification and claims and in the above figures, a number of operations are included that occur in a particular order, but it should be clearly understood that these operations may be performed out of order or in parallel as they occur herein, with the order of the operations being indicated as 101, 102, etc. merely to distinguish between the various operations, and the order of the operations by themselves does not represent any order of performance. Additionally, the flows may include more or fewer operations, and the operations may be performed sequentially or in parallel. It should be noted that, the descriptions of "first", "second", etc. in this document are used for distinguishing different messages, devices, modules, etc., and do not represent a sequential order, nor limit the types of "first" and "second" to be different.
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 5 and 6, fig. 5 is a schematic diagram of a desorber shown in an exemplary embodiment of the present application; FIG. 6 is a schematic diagram of the distribution of temperature measuring elements in the desorption tower of FIG. 5.
As shown in fig. 5, in the present application, the desorption tower 1 includes a feeding section 101, a heating section 102, a holding section 103, a cooling section 104, and a discharging section 105, and a hot air baffle 1021 is provided in the heating section 102. The activated carbon adsorbed with the pollutants enters from the buffer bin 106, enters through a material inlet valve 107 of the desorption tower, sequentially passes through a material inlet section 101, a heating section 102, a heat preservation section 103, a cooling section 104 and a material outlet section 105, and is finally discharged through a material feeder G1 of the desorption tower. The hot air system of the desorption tower 1 comprises a hot air furnace L1 and a hot air fan F1, the hot air furnace L1 heats air, and the hot air fan F1 enables the heated air to rapidly and circularly move, so that hot air enters from an air inlet and flows out from a hot air outlet.
As shown in fig. 5, a temperature measuring element TF1 is provided at the hot air inlet for measuring the hot air inlet temperature; the hot air outlet is provided with a temperature measuring element TF2 for measuring the temperature of the hot air outlet. A flow rate monitoring element VF1 is arranged at a proper position of the hot air pipeline to measure the flow rate of hot air. A temperature measuring element 1TE is arranged on the plane of the starting point of the heating section 102 of the analysis tower 1 and is used for measuring the temperature of the starting point of the heating section 102; a temperature measuring element 2TE is provided at the location of the end plane of the heating zone 102 of the analytical tower 1 for measuring the end temperature of the heating zone 102.
Specifically, as shown in fig. 6, nine thermocouples (the number of the thermocouples may be not limited to nine, and nine thermocouples are shown in the figure) are arranged in the temperature measuring element 1TE of the analytical tower 1TE11 to 1TE19, and the connection of each thermocouple is led out to the terminal of the temperature measuring element 1TE 1; the temperature measuring element 1TE1 is inserted in the protective sleeve; to protect the temperature measuring element from being washed by the flowing activated carbon. On one temperature measuring plane, a plurality of analytic tower temperature measuring elements (1 TE 1-1 TEN is shown in FIG. 6) are uniformly distributed. As can be seen from the figure, the position of each thermocouple relative to the reference point is fixed, and as long as the detection temperature of a certain temperature measuring element is known, the temperature of the activated carbon at the corresponding position is known. The temperature measurement value of 1TE is the arithmetic mean value of the temperature measurement values of the thermocouples constituting 1TE arranged at the starting point of the heating section.
Similarly, the arrangement of the temperature measuring element 2TE can also be the same as that of the temperature measuring element 1TE, and therefore, the description thereof is omitted. Accordingly, the temperature measurement value of the temperature measurement element 2TE is an arithmetic average of the temperature measurement values of the respective thermocouples constituting 2TE provided at the end of the heating section 102.
First, a technical solution for solving the technical problem of the present application is introduced, and the working principle is utilized:
as shown in fig. 6, the heat of the heating section 102 of the desorption tower 1 comes from the hot blast stove L1, the activated carbon temperature rise consumes the heat, the activated carbon desorption SQ2 consumes the heat, and a part of the heat dissipation is carried out, and the generation and consumption of the heat are balanced, as shown in formula 1:
Qf-Qt + Qj + Qs + Qz equation 1
Wherein:
qf, inputting heat into the hot blast stove in kilojoules;
qt: the temperature rise of the active carbon consumes heat, and the unit is kilojoule;
and (3) Qj: SO desorption by activated carbon2Heat consumption, unit kilojoule;
and Qs: the system dissipates heat, and the unit is kilojoule;
qz, heating the rest components to consume heat in kilojoule;
in formula 1, the proportion of the heat radiation Qs of the system and the heat consumption Qz for heating other components is very small, the influence can be ignored in engineering application, and formula 1 can be replaced by formula 2 in actual use:
Qf-Qt + Qj equation 2
Wherein:
qf, inputting heat into the hot blast stove in kilojoules;
qt: the temperature rise of the active carbon consumes heat, and the unit is kilojoule;
and (3) Qj: SO desorption by activated carbon2Heat consumption, unit kilojoule;
the heat consumed by the activated carbon for resolving the SO2 is related to the quantity of SO2 absorbed by the activated carbon, the activated carbon absorbs SO2 in the adsorption tower, the activated carbon for absorbing the SO2 is heated in the resolving tower 1, the activated carbon for absorbing the SO2 is heated to more than 200 ℃ to start releasing the adsorbed SO2, and the resolving process is an endothermic process. In practical application, the SO2 content in the sintering flue gas content does not fluctuate dramatically, and the relationship between Qt and Qj is shown in formula 3:
Qj-K1-Qt equation 3
Wherein:
qt: the temperature rise of the active carbon consumes heat, and the unit is kilojoule;
and (3) Qj: SO desorption by activated carbon2Heat consumption, unit kilojoule;
k1 is 0.2-0.3, the coefficient is related to the content of pollutants in the flue gas, the coefficient is regarded as a constant, and an empirical value is taken;
from the equations 2 and 3, it can be deduced that the relationship between the hot blast stove input heat and the activated carbon temperature rise consumption heat is shown in equation 4:
qf + K1 Qt (1+ K1) Qt-Qt formula 4
Wherein:
qf, inputting heat into the hot blast stove in kilojoules;
qt: the temperature rise of the active carbon consumes heat, and the unit is kilojoule;
k is 1.2-1.3, the coefficient is related to the content of pollutants in the flue gas, the coefficient is regarded as a constant, and an empirical value is taken;
as shown in fig. 6, the input heat of the hot blast stove can be calculated according to formula 5:
Qf＝(TTF1–TTF2)*VVF1cf equation 5
Wherein:
qf, inputting heat into the hot blast stove in kilojoules;
TTF1,TTF2temperature values measured by temperature measuring elements TF1 and TF2 in unit K;
VVF1the hot air flow value measured by a flow meter VF1 is unit kg/h;
cf is the specific heat of hot air, constant, unit kilojoule/(K x kg/h);
as shown in fig. 5, when the production is stable, the heat consumption of the activated carbon temperature rise is calculated according to equation 6: (definition of production stability: 1. when the activated carbon detected by the activated carbon outlet temperature detection element is heated from the inlet; 2. the flow rate of the activated carbon and the emission of pollutants in the flue gas are not greatly changed in the production process.)
Qt＝(T2TE–T1TE)*VTCt equation 6
Wherein:
qt, temperature rise of the active carbon consumes heat in units of kilojoules;
T1TE,T2TEtemperature values measured by temperature measuring elements 1TE and 2TE are in unit K;
Vtthe flow rate of the activated carbon is unit kg/h;
ct is the specific heat of the activated carbon, a constant and a unit of kilojoule/(K kg/h);
it can be derived from equations 4, 5, and 6:
K*(T2TE–T1TE)*VT*Ct＝(TTF1–TTF2)*VVF1cf formula 7
Wherein:
qt, temperature rise of the active carbon consumes heat in units of kilojoules;
T1TE,T2TEtemperature values measured by temperature measuring elements 1TE and 2TE are in unit K;
Vtthe flow rate of the activated carbon is unit kg/h;
ct is the specific heat of the activated carbon, a constant and a unit of kilojoule/(K kg/h);
qf, inputting heat into the hot blast stove in kilojoules;
TTF1,TTF2temperature values measured by temperature measuring elements TF1 and TF2 in unit K;
VVF1the hot air flow value measured by a flow meter VF1 is unit kg/h;
cf is the specific heat of hot air, constant, unit kilojoule/(K x kg/h);
k is 1.2-1.3, and the coefficient is adjusted according to the production condition;
in the formula 7, the specific heat Cf of hot air and the specific heat Ct of activated carbon are constants, all temperature values can be obtained through temperature measuring elements, and the activated carbon in the adsorption tower 2 is finally discharged from the feeding machine G1, so that the working flow of the feeding machine G1 is equal to the flow V of the activated carbon in the heating sectionT(ii) a Flow rate V of activated carbonTProportional to the rotational speed of the stripper feeder G1. As shown in equation 8:
VT＝KG1*FG1equation 8
Wherein:
VTstream of activated carbonAmount, unit kg/h;
KG1constants, determined by the design parameters of feeder G1, in units of kg/(h RPM);
FG1the rotating speed of the feeder and the unit RPM;
it should be noted that the rotation Speed (Rotational Speed or Rev) is the number of turns of the object moving in a circular motion around the center of the circle in unit time, and the unit is RPM, which is an abbreviation of revolution Per minute. Herein, all RPMs represent this meaning.
In the formula 7, the air volume of the hot air blower F1 is in proportional relation with the rotation speed of the hot air blower F1. As shown in equation 9:
VVF1＝KF1*FF1equation 9
Wherein:
VVF1the flow of the hot air fan is unit kg/h;
KF1constants, determined by the design parameters of the fan F1, in units of kg/(h RPM);
FF1the rotating speed of a fan is unit RPM;
substituting the formula 8 and the formula 9 into the formula 7 can deduce the rotating speed F of the hot air fanF1It can be set as follows:
K*(T2TE–T1TE)*KG1*FG1*Ct＝(TTF1–TTF2)*KF1*FF1*Cf
Figure BDA0002248481490000101
wherein:
T1TE,T2TEtemperature values measured by temperature measuring elements 1TE and 2TE are in unit K;
KG1constants, determined by the design parameters of feeder G1, in units of kg/(h RPM);
FG1the rotating speed of the feeding machine and the unit RPM;
ct is the specific heat of the activated carbon, a constant and a unit of kilojoule/(K kg/h);
TTF1,TTF2temperature values measured by temperature measuring elements TF1 and TF2 in unit K;
KF1the constant is determined by the design parameters of a hot air fan F1 and has unit kg/(h RPM);
FF1fan speed, unit RPM;
cf is the specific heat of hot air, constant, unit kilojoule/(K x kg/h);
k is 1.2-1.3, and the coefficient is adjusted according to the production condition;
as shown in equation 10, K, KG1, Ct, KF1, and Cf on the right side are all constants, so equation 10 can be simplified as:
Figure BDA0002248481490000102
wherein: kJIs a coefficient, whose value:
KJ＝(K*KG1*Ct)/(KF1*Cf)
the notation of the symbols in equation 11 is the same as that in equation 10 and will not be described further.
Another derivation of equation 10:
Figure BDA0002248481490000111
wherein: kJIs a coefficient, whose value:
KJ＝(K*KG1*Ct)/(KF1*Cf)
the notation of the symbols in equation 11 is the same as that in equation 10 and will not be described further.
Equation 11 can derive:
KH＝FF1*(TTF1-TTF2)/K*(T2TE-T1TE)*FG1equation 13
The technical scheme for solving the technical problems is the working principle utilized by the application.
Let us now present in detail an embodiment of the solution of the present application.
Referring to fig. 7, fig. 7 is a logic flow diagram of a method for controlling a hot wind fan during a cold start of a desorption tower according to an exemplary embodiment of the present application.
In an embodiment, the control method of the hot air fan F1 during cold start of the desorption tower 1 provided by the present application is used for determining the rotation speed of the hot air fan F1 of the desorption tower 1 during cold start, and the control method of the hot air fan F1 includes the following steps:
step S101: the activated carbon starts flowing within the heating section 102 of the desorption tower 1;
step S102: heat is supplied to the heating section 102 of the analysis tower 1 through a hot blast stove L1 and a hot blast fan F1 of the analysis tower 1;
step S103: acquiring a hot air inlet temperature of the heating section 102, a hot air outlet temperature of the heating section 102, a starting point temperature of the heating section 102, a target control temperature of a terminal point of the heating section 102, a working heat exchange coefficient of the heating section 102, and a current feeder rotating speed of a feeder of the analysis tower 1;
step S104: and obtaining the target rotating speed of the hot air fan F1 based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeding machine rotating speed.
The method can accurately control the rotating speed of the hot air fan F1 when the analysis tower 1 is started in a cold state, so that the problem of electric energy and fuel waste caused by excessive heat input by the hot air furnace L1 can be effectively solved.
In the above-described embodiment, the manner of the target rotation speed may be specifically designed.
For example, the step of obtaining the target rotating speed of the hot air fan F1 based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeder rotating speed includes:
obtaining the target rotating speed based on the following relational expression:
Figure BDA0002248481490000112
wherein, Ff1Representing a target rotational speed; kJRepresents the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Represents the hot air outlet temperature; t is1TERepresents the starting point temperature; TK represents the end point target control temperature; fG1Representing the current feeder speed.
According to the formula, on the premise of obtaining the working heat exchange coefficient, the rotating speed of the hot air fan F1 can be controlled accurately very easily based on the end point target control temperature, and therefore energy-saving operation is achieved.
Further, before step S101, the following steps are further included:
the desorption tower 1 was charged with activated carbon until the desorption tower 1 reached its own capacity value.
Further, in step S102, the hot air blower F1 is caused to operate at the maximum rotation speed.
In addition, the control method of the hot air fan F1 further comprises the following steps:
the end point actual temperature of the heating section 102 is monitored.
And, when the end point actual temperature is less than the end point target control temperature,
and adjusting the current rotating speed of the feeder to enable the current rotating speed of the feeder to be smaller than a preset rotating speed value.
The predetermined speed value is obtained by the following relation:
Figure BDA0002248481490000121
wherein, FG1Indicating a predetermined value of the rotational speed; fF1Representing a target rotational speed; kJRepresents the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Represents the hot air outlet temperature; t is1TERepresents the starting point temperature; t is1TEThe end point temperature is indicated.
The step of obtaining an operating heat exchange coefficient for the heating section 102 includes:
the operating heat exchange coefficient is obtained by the following relation:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresents the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeder; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan F1; cf is the specific heat of hot air and is a constant.
K is a coefficient related to the amount of adsorption of activated carbon contaminants, and can be considered as a constant because the sintering conditions are relatively stable over time. When the activated carbon is initially loaded, the activated carbon in the desorption tower does not carry pollutants, and K is 1; when production stops restarting, when the desorption tower is started in a re-cooled state, pollutants in the desorption tower carry activated carbon, and K is 1.2-1.3.
In any of the above embodiments, we can also make specific designs for the obtaining methods of the respective temperatures. For example, the end point temperature is obtained by:
acquiring the temperature of each preset temperature measuring point in the terminal plane of the heating section 102;
the end point temperature is obtained based on the arithmetic mean of the temperatures at the respective temperature measurement points.
For example, the starting temperature is obtained by:
acquiring the temperature of each preset temperature measuring point in the starting point plane of the heating section 102;
the starting point temperature is obtained based on the arithmetic mean of the temperatures at the respective temperature measurement points.
Obviously, the starting and ending temperatures obtained by this method will be more accurate.
In addition, as shown in fig. 5, when events such as initial installation of activated carbon, shutdown of sintering, overhaul and the like occur, the activated carbon in the desorption tower 1 is all in a cold state, when the flue gas purification system is started, a cycle between the adsorption tower 2 and the desorption tower 1 is established first, and the cycle speed of the activated carbon is set according to a design working condition; then the hot blast stove L1 is started again, the hot blast fan is started, and hot blast is blown in to heat the cold activated carbon.
As shown in fig. 5, after the activated carbon cycle is established, the flow rate of the activated carbon in the heating section 102 of the desorption tower 1 is v1, and the length of the activated carbon heating section 102 is L; it can be known that the maximum heating time of the activated carbon in the heating section 102 is L/v1, that is, the hot air furnace L1 starts to work, after the hot air is blown, the activated carbon at the inlet of the heating section 102 enters the heating section 102 to start heating, and when the activated carbon leaves the heating section 102, the activated carbon passes through L/v1 time, and the heating time of the activated carbon is shorter as the activated carbon is closer to the outlet of the heating section 102.
An L1 system of the activated carbon hot blast stove is designed with enough margin, when the activated carbon hot blast stove is normally started in a cold state, the temperature of the activated carbon can be heated to a control temperature within the time of L/v1, after the heating temperature of the activated carbon reaches the control temperature, the rotating speed of a hot blast fan F1 can be adjusted according to a formula 11, and the cold start of the analytical tower 1 is completed; in abnormal conditions, if the temperature of the activated carbon does not reach the set temperature within the time of L/v1, the flow rate of the activated carbon is too high, and the heating time is insufficient, the rotating speed of the circular roller feeder at the outlet of the analysis tower 1 can be adjusted to be lower than the calculated value of the formula 12.
In addition, referring to fig. 5 and fig. 6, the present application also provides an apparatus invention, which is a control apparatus of a hot air blower F1 when a desorption tower 1 is cold-started, and is used for determining a rotation speed of a hot air blower F1 of the desorption tower 1 when the desorption tower 1 is cold-started, including the desorption tower 1, in which the desorption tower 1 includes:
a heating section 102 for heating the activated carbon flowing through the desorption tower 1;
a hot air blower F1 for blowing hot air into the heating zone 102 of the analytical tower 1;
the feeding machine is used for controlling the discharge flow of the activated carbon in the desorption tower 1;
the stripping column 1 comprises:
the first temperature measuring element is used for acquiring the hot air inlet temperature of the heating section 102 of the analysis tower 1;
the second temperature measuring element is used for acquiring the temperature of the hot air outlet of the heating section 102;
the third temperature measuring element is used for acquiring the starting point temperature of the heating section 102;
it should be noted that, for the sake of convenience, the numbering of the temperature measuring elements is merely required for expression and is not inconsistent with the foregoing. The first temperature measuring file is the temperature measuring element TF1 used for measuring the temperature of the hot air inlet in the figure 5, and the second temperature measuring file is the temperature measuring element TF2 used for measuring the temperature of the hot air outlet in the figure 5; the third temperature measurement file is the temperature measurement element 1TE of FIG. 5 for measuring the temperature at the beginning of the heating section 102, and the fourth temperature measurement file is the temperature measurement element 2TE of FIG. 5 for measuring the temperature at the end of the heating section 102.
A first calculation unit for obtaining the operating heat exchange coefficient of the heating section 102;
and the second calculation unit is used for obtaining the target rotating speed of the hot air fan F1 based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current rotating speed of the feeder.
In the above-described embodiments, further improvements can be made. For example, the second calculation unit obtains the target rotation speed based on the following relational expression:
Figure BDA0002248481490000141
wherein, Ff1Representing a target rotational speed; kJRepresents the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Represents the hot air outlet temperature; t is1TERepresents the starting point temperature; TK represents the end point target control temperature; fG1Representing the current feeder speed.
The first calculation unit obtains the working heat exchange coefficient through the following relation:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresents the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeder; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan F1; cf is the specific heat of hot air and is a constant.
In addition, in the above embodiments, the layout of the temperature measuring element can be specifically designed. For example, as shown in FIG. 6, the number of the third temperature measuring elements is plural and is uniformly distributed in the starting plane of the heating section 102; and a plurality of thermocouples for measuring temperature are arranged on each third temperature measuring element. And a protective sleeve 5 is arranged outside the third temperature measuring element.
For example, as shown in FIG. 6, the number of the fourth temperature measuring elements is multiple and is uniformly distributed in the terminal plane of the heating section 102; and a plurality of thermocouples for measuring temperature are arranged on each fourth temperature measuring element. And a protective sleeve 5 is arranged outside the fourth temperature measuring element.
It can be clearly understood by those skilled in the art that, for convenience and brevity of description, the specific working processes and corresponding technical effects of the above-described systems, apparatuses and units may refer to the corresponding processes in the foregoing method embodiments, and are not described herein again.
The above-described embodiments of the apparatus are merely illustrative, and the units described as separate parts may or may not be physically separate, and the parts displayed as units may or may not be physical units, may be located in one place, or may be distributed on a plurality of network units. Some or all of the modules may be selected according to actual needs to achieve the purpose of the solution of the present embodiment. One of ordinary skill in the art can understand and implement it without inventive effort.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.

Claims (14)

1. A control method of a hot air fan during cold starting of an analytic tower is used for determining the rotating speed of the hot air fan of the analytic tower during cold starting, and is characterized by comprising the following steps:
the activated carbon starts flowing in the heating section of the desorption tower;
supplying heat to the heating section of the analysis tower through a hot blast stove of the analysis tower and the hot blast fan;
obtaining the hot air inlet temperature of the heating section and the hot air outlet temperature of the heating section,
acquiring the starting point temperature of the heating section and the target control temperature of the end point of the heating section,
obtaining the working heat exchange coefficient of the heating section,
acquiring the current rotating speed of the feeder of the analysis tower;
and obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the terminal point target control temperature and the current feeding machine rotating speed.
2. The method for controlling a hot air blower at cold start-up of a stripper according to claim 1,
the step of obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeder rotating speed comprises the following steps of:
obtaining the target rotating speed based on the following relational expression:
Figure FDA0002248481480000011
wherein, Ff1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; TK represents the endpoint target control temperature; fG1Representing the current feeder rotational speed.
3. The method for controlling a hot air blower at cold start-up of a stripper according to claim 1,
before the step of starting the flow of the activated carbon in the heating section of the desorption tower, the method further comprises the following steps:
and filling the desorption tower with activated carbon until the desorption tower reaches the capacity value of the desorption tower.
4. The method for controlling a hot air blower at cold start-up of a stripper according to claim 1,
the step of supplying heat to the heating section of the analysis tower through the hot blast stove of the analysis tower and the hot blast fan comprises the following steps:
so that the hot air blower operates at the maximum rotational speed.
5. The method for controlling a hot air blower at cold start-up of a stripper as claimed in claim 4,
monitoring the actual temperature of the end point of the heating section.
6. The method for controlling a hot air blower at cold start-up of a stripper as claimed in claim 5,
when the end point actual temperature is greater than or equal to the end point target control temperature,
and obtaining the target rotating speed of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the terminal point target control temperature and the current feeding machine rotating speed.
7. The method for controlling a hot air blower at cold start-up of a stripper as claimed in claim 5,
when the end point actual temperature is less than the end point target control temperature,
and adjusting the current rotating speed of the feeder to enable the current rotating speed of the feeder to be smaller than a preset rotating speed value.
8. The method for controlling a hot air blower at cold start-up of a stripper according to claim 7,
the preset rotating speed value is obtained through the following relation:
Figure FDA0002248481480000021
wherein, FG1Representing the predetermined rotational speed value; fF1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; t is1TERepresents the end point temperature.
9. The method for controlling a hot-air blower at the cold start-up of a stripper according to any of claims 1-8,
the step of obtaining the operating heat exchange coefficient of the heating section comprises:
the operating heat exchange coefficient is obtained by the following relation:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresenting the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeding machine; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan; cf is the specific heat of hot air and is a constant; when the activated carbon is initially loaded, the activated carbon in the desorption tower does not carry pollutants, and K is 1; when production stops restarting, when the desorption tower is started in a re-cooled state, pollutants in the desorption tower carry activated carbon, and K is 1.2-1.3.
10. A hot air blower control device for a cold start of a desorption tower is used for determining the output frequency of a hot air blower of the desorption tower during the cold start, and comprises the desorption tower, wherein the desorption tower comprises:
a heating section for heating the activated carbon flowing through the desorption tower;
the hot air fan is used for blowing hot air into the heating section of the desorption tower;
the feeding machine is used for controlling the discharge flow of the activated carbon in the desorption tower; it is characterized in that the preparation method is characterized in that,
the desorption tower comprises:
the first temperature measuring element is used for acquiring the hot air inlet temperature of the heating section of the analysis tower;
the second temperature measuring element is used for acquiring the temperature of the hot air outlet of the heating section;
the third temperature measuring element is used for acquiring the starting point temperature of the heating section;
the first calculation unit is used for acquiring the working heat exchange coefficient of the heating section;
and the second calculation unit is used for obtaining the target output frequency of the hot air fan based on the working heat exchange coefficient, the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point target control temperature and the current feeding output frequency.
11. The control device of the hot air blower at the cold start of the desorption tower as set forth in claim 10,
the second calculation unit obtains the target rotation speed based on the following relational expression:
Figure FDA0002248481480000031
wherein, Ff1Representing the target rotational speed; kJRepresenting the operating heat exchange coefficient; t isTF1Represents the hot air inlet temperature; t isTF2Representing the hot blast outlet temperature; t is1TERepresents the starting point temperature; TK represents the endpoint target control temperature; fG1Representing the current feeder rotational speed.
12. The control device of the hot air blower at the cold start of the desorption tower as set forth in claim 10,
the first calculating unit obtains the working heat exchange coefficient through the following relational expression:
KJ＝(K*KG1*Ct)/(KF1*Cf)
wherein, KJRepresenting the operating heat exchange coefficient; kG1Is a constant and is determined by the design parameters of the feeding machine; ct is the specific heat of the activated carbon and is a constant; kF1Is a constant and is determined by the design parameters of the hot air fan; cf is the specific heat of hot air and is a constant; when the activated carbon is initially loaded, the activated carbon in the desorption tower does not carry pollutants, and K is 1; when production stops restarting, when the desorption tower is started in a re-cooled state, pollutants in the desorption tower carry activated carbon, and K is 1.2-1.3.
13. The control device of the hot fan at the cold start-up of the desorption tower according to any one of claims 10 to 12,
the third temperature measuring elements are multiple and are uniformly distributed in the starting point plane of the heating section;
and a plurality of thermocouples for measuring temperature are arranged on each third temperature measuring element.
14. The control device of the hot fan at the cold start-up of the desorption tower according to any one of claims 10 to 12,
the number of the fourth temperature measuring elements is multiple, and the fourth temperature measuring elements are uniformly distributed in the terminal point plane of the heating section;
and a plurality of thermocouples for measuring temperature are arranged on each fourth temperature measuring element.
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