CN112705010B - Method and device for obtaining heat exchange coefficient of desorption tower - Google Patents

Method and device for obtaining heat exchange coefficient of desorption tower Download PDF

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CN112705010B
CN112705010B CN201911026224.9A CN201911026224A CN112705010B CN 112705010 B CN112705010 B CN 112705010B CN 201911026224 A CN201911026224 A CN 201911026224A CN 112705010 B CN112705010 B CN 112705010B
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temperature
heating section
activated carbon
hot air
tower
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CN112705010A (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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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling

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Abstract

The application discloses a heat exchange coefficient obtaining method of a desorption tower, which is used for obtaining a heat exchange coefficient of a heating section of the desorption tower, and comprises the following steps: the activated carbon is initially loaded in the desorption tower, and when the activated carbon does not adsorb pollutants: activated carbon starts to flow in the desorption tower; starting a hot blast stove of the desorption tower to heat the activated carbon in the heating section; acquiring the starting point temperature of the heating section, the end point temperature of the heating section, the hot air inlet temperature of the heating section, the hot air outlet temperature of the heating section, the current fan rotating speed of a hot air fan of the analysis tower and the current feeder rotating speed of a feeder of the analysis tower; the heat exchange coefficient is obtained based on the above parameters. The method can effectively and conveniently obtain the heat exchange coefficient of the desorption tower, thereby laying a foundation for the accurate control of the desorption tower. The application also discloses a heat exchange coefficient obtaining device of the desorption tower.

Description

Method and device for obtaining heat exchange coefficient of desorption tower
Technical Field
The application relates to the technical field of sintering flue gas purification, in particular to a method for obtaining a heat exchange coefficient of an analytical tower. In addition, the application also relates to a heat exchange coefficient obtaining device of the desorption 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 obtained.
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 conventional flue gas purification apparatus 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 outside. The activated carbon adsorbing pollutants (main components of the pollutants are SO2) in the flue gas is sent into the desorption tower 1 through a 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 desorbed and activated carbon is cooled to 110-130 ℃ and then discharged out of the desorption tower 1, activated carbon dust is screened out by a vibrating screen 4, and the screened activated carbon particles enter the adsorption tower 2 again through a 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 heat preservation section 103, a retention 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, an SRG gas system and other components.
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 fan F1, the hot air furnace L1 heats air, and the hot air fan 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, the activated carbon in the desorption tower 1 flows in the desorption tower, and enters the heat preservation section 103 after being heated by the heating section 102; the temperature rise of the activated carbon in the desorption tower 1 and the heat source needed for the desorption of pollutants in the activated carbon are both from a hot blast stove system, and the input heat of the hot blast stove L1 and the temperature rise of the activated carbon are related. However, no method for effectively and conveniently obtaining the heat exchange coefficient of the desorption tower exists in the prior art.
Disclosure of Invention
The technical problem to be solved by the application is to provide a method for obtaining the heat exchange coefficient of the analytic tower, and the method can effectively and conveniently obtain the heat exchange coefficient of the analytic tower, so that a foundation is laid for the accurate control of the analytic tower.
In order to solve the above technical problem, a first aspect of the present application provides a heat exchange coefficient obtaining method for a resolving tower, for obtaining a heat exchange coefficient of a heating section of the resolving tower, the heat exchange coefficient obtaining method comprising the following steps:
the activated carbon is initially loaded in the desorption tower, and when the activated carbon does not adsorb pollutants:
the activated carbon starts to flow in the desorption tower;
starting a hot blast stove of the desorption tower to heat the activated carbon in the heating section;
acquiring the starting point temperature of the heating section, the end point temperature of the heating section, the hot air inlet temperature of the heating section, the hot air outlet temperature of the heating section, the current fan rotating speed of a hot air fan of the analysis tower and the current feeder rotating speed of a feeder of the analysis tower;
and obtaining the heat exchange coefficient based on the starting point temperature, the end point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speed.
Alternatively to this, the first and second parts may,
the process of obtaining the heat exchange coefficient based on the starting point temperature, the ending point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speed comprises the following steps:
the heat exchange coefficient is obtained based on the following relation:
KH＝FF1*(TTF1-TTF2)/(T2TE-T1TE)*FG1
wherein, T1TERepresents the starting point temperature; t is2TERepresents the end point temperature; t isTF1The hot air inlet temperature; t isTF2The hot air outlet temperature; fF1Representing the current fan speed; fG1Representing the current feeder speed.
Alternatively to this, the first and second parts may,
before the step of starting the flow of the activated carbon in the desorption tower, the method also 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 method comprises the following steps of starting a hot blast stove of the desorption tower to heat activated carbon in the heating section, wherein the steps comprise:
and heating the activated carbon in the heating section for a preset working time.
Alternatively to this, the first and second parts may,
the preset working time satisfies the following relational expression:
t>k*L/v1
wherein t represents the predetermined operating time period, L represents the length of the heating section, and v1 represents the flow rate of activated carbon.
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.
Alternatively to this, the first and second parts may,
the end temperature is obtained by:
acquiring the temperature of each preset temperature measuring point in the terminal plane of the heating section;
the end point temperature is obtained based on an arithmetic average of the temperatures at the respective temperature measurement points.
In addition, in order to solve the above technical problem, the present application further provides a heat exchange coefficient obtaining apparatus for a desorption tower, configured to obtain a heat exchange coefficient of a heating section of the desorption tower, wherein the desorption tower includes:
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 fourth temperature measuring element is used for acquiring the end point temperature of the heating section;
and the calculating unit is used for obtaining the heat exchange coefficient based on the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point temperature, the current fan rotating speed of the hot air fan and the current feeder rotating speed of the feeder.
Alternatively to this, the first and second parts may,
the calculation unit obtains the heat exchange coefficient based on the following relational expression:
KH＝FF1*(TTF1-TTF2)/(T2TE-T1TE)*FG1
wherein, T1TERepresents the starting point temperature; t is a unit of2TERepresents the end point temperature; t isTF1The hot air inlet temperature; t isTF2The hot air outlet temperature; fF1Representing the current fan speed; fG1Representing the current feeder speed.
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,
and a protective sleeve is arranged outside the 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 alternative,
and a protective sleeve is arranged outside the fourth temperature measuring element.
In the present application, the heat exchange coefficient obtaining method includes the steps of:
the activated carbon is initially loaded in the desorption tower, and when the activated carbon does not adsorb pollutants:
activated carbon starts to flow in the desorption tower;
starting a hot blast stove of the desorption tower to heat the activated carbon in the heating section;
acquiring the starting point temperature of the heating section, the end point temperature of the heating section, the hot air inlet temperature of the heating section, the hot air outlet temperature of the heating section, the current fan rotating speed of a hot air fan of the analysis tower and the current feeder rotating speed of a feeder of the analysis tower;
and obtaining the heat exchange coefficient based on the starting point temperature, the end point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speed.
The method can effectively and conveniently obtain the heat exchange coefficient of the desorption tower, thereby laying a foundation for the accurate control of the desorption tower.
In addition, the heat exchange coefficient obtaining device of the desorption tower provided by the application has the same technical effects as the above, 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 of obtaining heat exchange coefficients for a desorber shown in 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, an analysis 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 surge 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 flows described in the present specification and claims and 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 given as 101, 102, etc. merely to distinguish between various operations, and the order of the operations itself 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 1TE11 to 1TE19 (the number of the thermocouples may be not limited to nine, and nine thermocouples are shown in the figure) are provided in the temperature measuring element 1TE of the analytical tower, 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 amount of SO2 absorbed by the activated carbon, the activated carbon absorbs SO2 in the adsorption tower 2, the activated carbon for absorbing SO2 is heated in the resolving tower 1, the activated carbon for absorbing 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 is consumed, 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 temperature of the feeding machine G1 is constantThe flow rate is equal to the flow rate V of the activated carbon in the heating sectionT(ii) a Flow rate V of activated carbonTProportional to the speed of feed G1. As shown in equation 8:
VT＝KG1*FG1equation 8
Wherein:
VTthe flow rate of the activated carbon is unit kg/h;
KG1constants, determined by the design parameters of feeder G1, in units of kg/(h RPM);
FG1feeding machine rotation speed, 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 rate of a hot air fan is in unit kg/h;
KF1constants, determined by the design parameters of the fan F1, in units of kg/(h RPM);
FF1the rotating speed of the hot air 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 BDA0002248682940000091
wherein:
T1TE,T2TEtemperature measured by temperature measuring elements 1TE,2TEValue, in units of 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);
FF1the rotating speed of the hot air fan is 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;
k, K on its right side as shown in equation 10G1、Ct、KF1Cf are constants, so equation 10 can be simplified as:
Figure BDA0002248682940000092
wherein: kHFor the heat exchange coefficient of the analytical column, the value:
KH＝(KG1*Ct)/(KF1cf) formula 12
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 deduce:
KH＝FF1*(TTF1-TTF2)/K*(T2TE-T1TE)*FG1equation 13
It should be noted that, in the following description,
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 heat exchange coefficient obtaining method of a desorption tower shown in an exemplary embodiment of the present application.
In an embodiment of the present application, the heat exchange coefficient obtaining method of the desorption tower 1 is used for obtaining the heat exchange coefficient of the heating section 102 of the desorption tower 1, and comprises the following steps:
step S101: the activated carbon is initially installed in the desorption tower 1, and when the activated carbon does not adsorb pollutants: the activated carbon starts to flow in the desorption tower 1;
step S102: starting a hot blast stove L1 of the desorption tower 1 to heat the activated carbon in the heating section 102;
step S103: acquiring the starting point temperature of the heating section 102, the end point temperature of the heating section 102, the hot air inlet temperature of the heating section 102, the hot air outlet temperature of the heating section 102, the current fan rotating speed of a hot air fan F1F1 of the analysis tower 1 and the current feeder rotating speed of a feeder of the analysis tower 1;
step S104: and obtaining a heat exchange coefficient based on the starting point temperature, the end point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speed.
The method can effectively and conveniently obtain the heat exchange coefficient of the desorption tower 1, thereby laying a foundation for the accurate control of the desorption tower 1.
In the above embodiment, further design may be made for a specific obtaining method of the heat exchange coefficient. For example,
based on the starting point temperature, the end point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speed, the process of obtaining the heat exchange coefficient comprises the following steps:
the heat exchange coefficient is obtained based on the following relation:
KH＝FF1*(TTF1-TTF2)/K*(T2TE-T1TE)*FG1
wherein, T1TERepresents the starting point temperature; t is2TERepresents the end point temperature; t isTF1Hot air inlet temperature; t isTF2Hot air outlet temperature; fF1Representing the current fan speed; fG1Indicates the currentThe rotating speed of the feeding machine.
Knowing the heat exchange coefficient KHRelated to a series of parameters such as design parameters of a feeder, design parameters of a fan, a coefficient K, specific heat of activated carbon, specific heat of hot air and the like; however, in actual production, it is often difficult to obtain these parameters. However, in the above formula, four temperature values and two rotation speeds can be obtained relatively easily, and thus the heat exchange coefficient can be obtained very easily.
In addition, in the above formula, T on the right sideTF1、TTF2、T1TE、T2TE、FG1、FG2Can be read directly from a computer control system; when the desorption tower 1 is stably produced, when the activated carbon is initially loaded, the flue gas is not introduced into the adsorption tower, namely the activated carbon flowing through the desorption tower 1 does not contain pollutants, and when the activated carbon of the desorption tower 1 is heated by the hot blast stove L1, the consumed heat Qj of the activated carbon desorption SO2 is 0 corresponding to the formula 1; k1 is 0 corresponding to formula 3, and K is 1 corresponding to formulas 4 to 11, so that the heat exchange coefficient K of the analytical tower 1 can be obtained through formula 13 at the initial stage of activated carbon loadingH。
In the above-described embodiment, further improvements can be made. Specifically, before step S101, the method further includes the following steps:
the desorption tower 1 was charged with activated carbon until the desorption tower 1 reached its own capacity value.
Further, in step S102, the activated carbon in the heating section 102 is heated for a predetermined operation time.
The predetermined operating time satisfies the following relation:
t>k*L/v1
wherein t represents the preset working time, L represents the length of the heating section 102, v1 represents the flow rate of the activated carbon, and k is a coefficient and takes a value of 1.5-3.
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, it should be noted that, in practical applications, the adsorption tower 2 may be formed by connecting a plurality of adsorption towers 2 in parallel, and the desorption tower 1 may be formed by connecting a plurality of desorption towers 1 in parallel; the scale of the sintered activated carbon flue gas purification device is large, for example, the filling amount of activated carbon of the sintered activated carbon flue gas purification device is about 1ten thousand tons in Bao steel 700m2, and the empty tower filling time of the adsorption tower 2 and the desorption tower 1 is about 1 month; the time for completing one cycle of the active carbon in the desorption tower 1 and the adsorption tower 2 is about 10 days; after two cycles of the activated carbon in the activated carbon flue gas purification device, the adsorption tower 2 can be used for introducing sintering flue gas (see fig. 1 in the prior art).
After the activated carbon flue gas purification device is built, activated carbon is not filled in the adsorption tower 2 and the desorption tower 1, and at the moment, the activated carbon is filled in the activated carbon flue gas purification device through the activated carbon storage 3.
When the activated carbon is filled, the new activated carbon sequentially passes through the activated carbon storage bin 3, the first activated carbon conveyor S1, the buffer bin 106, the analysis tower feed valve 107, the analysis tower 1, the analysis tower feeder G1, the vibrating screen 4, the second activated carbon conveyor S2, the adsorption tower feed valve 201, the adsorption tower 2, the adsorption tower feeder G2 and the first activated carbon conveyor S1, and finally an activated carbon cycle in the adsorption tower of the analysis tower 1 is formed.
After the desorption tower 1 starts to be filled with the activated carbon, the hot blast stove L1 can be started, and the activated carbon enters the adsorption tower after being desorbed and activated by the heating section 102.
Under normal conditions, only one time of initial installation of the activated carbon is needed in the whole life cycle of the activated carbon flue gas purification device; the lost active carbon in the future production is supplemented by an active carbon storage bin (see figure 1); during the period of the large repair and production stop of the sintering machine, the activated carbon flue gas purification device stops circulating, and the hot blast stove L1 stops; after the sintering production is recovered, the activated carbon flue gas purification device can be put into production immediately.
As shown in fig. 5, the hot air circulation system can be opened when the desorption tower 1 starts to be filled with activated carbon in the conventional activated carbon filling method, in which case the flow of activated carbon flowing through the heating section 102 of the desorption tower 1 is unstable, which causes distortion of detection data, and the hot air circulation system is opened only after the desorption tower 1 is filled.
As shown in fig. 5, when the activated carbon is initially loaded, the activated carbon in the desorption tower 1 is all in a cold state, when the flue gas purification system is started, the circulation between the adsorption tower and the desorption tower 1 is established first, and the circulation speed of the activated carbon is set according to the designed working condition; then the hot blast stove L1 is started, the hot blast fan F1 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 closer the activated carbon is to the outlet of the heating section 102, the shorter the heating time is.
In addition, the present application also provides an apparatus invention, a heat exchange coefficient obtaining apparatus of a desorption tower 1, for obtaining a heat exchange coefficient of a heating section 102 of the desorption tower 1, wherein 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;
the fourth temperature measuring element is used for acquiring the end 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 measurement file is the temperature measurement element TF1 used for measuring the hot air inlet temperature in FIG. 5, and the second temperature measurement file is the temperature measurement element TF2 used for measuring the hot air outlet temperature in FIG. 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.
And the calculating unit is used for obtaining the heat exchange coefficient based on the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point temperature, the current fan rotating speed of the hot air fan F1 and the current feeder rotating speed of the feeder.
The method can effectively and conveniently obtain the heat exchange coefficient of the analytic tower 1, thereby laying a foundation for the accurate control of the analytic tower 1.
In the above-described apparatus embodiment, further improvements can be made. For example, the calculating unit obtains the heat exchange coefficient based on the following relation:
KH＝FF1*(TTF1-TTF2)/K*(T2TE-T1TE)*FG1
wherein, T1TERepresents the starting point temperature; t is2TERepresents the end point temperature; t isTF1Hot air inlet temperature; t isTF2Hot air outlet temperature; fF1Representing the current fan speed; fG1Representing the current feeder speed.
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 simplicity 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 (11)

1. A heat exchange coefficient obtaining method of a desorption tower for obtaining a heat exchange coefficient of a heating section of the desorption tower, which is characterized by comprising the following steps:
the activated carbon is initially loaded in the desorption tower, and when the activated carbon does not adsorb pollutants:
activated carbon starts to flow in the desorption tower;
starting a hot blast stove of the desorption tower to heat the activated carbon in the heating section;
acquiring the starting point temperature of the heating section, the end point temperature of the heating section, the hot air inlet temperature of the heating section, the hot air outlet temperature of the heating section, the current fan rotating speed of a hot air fan of the analysis tower and the current feeder rotating speed of a feeder of the analysis tower;
obtaining the heat exchange coefficient K based on the starting point temperature, the end point temperature, the hot air inlet temperature, the hot air outlet temperature, the current fan rotating speed and the current feeder rotating speedH；
KH＝FF1*(TTF1-TTF2)/(T2TE-T1TE)*FG1
Wherein, T1TERepresents the starting point temperature; t is2TERepresents the end point temperature; t is a unit ofTF1The hot air inlet temperature; t isTF2The hot air outlet temperature; fF1Representing the current fan speed; fG1Representing the current feeder speed.
2. The method for obtaining a heat exchange coefficient of a stripping column according to claim 1,
before the step of starting the flow of the activated carbon in the desorption tower, the method also comprises the following steps:
and filling the desorption tower with activated carbon until the desorption tower reaches the capacity value of the desorption tower.
3. The method for obtaining a heat exchange coefficient of a stripping column according to claim 1,
the method comprises the following steps of starting a hot blast stove of the desorption tower and heating the activated carbon in the heating section, wherein the steps comprise:
and heating the activated carbon in the heating section for a preset working time.
4. The method for obtaining a heat exchange coefficient of a stripping tower as set forth in claim 3,
the preset working time satisfies the following relational expression:
t>k*L/v1
wherein t represents the predetermined operating time period, L represents the length of the heating section, and v1 represents the flow rate of activated carbon.
5. The method for obtaining the heat exchange coefficient of a stripping column according to any of claims 1 to 4,
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.
6. The method for obtaining a heat exchange coefficient of a stripping column according to claim 1,
the end temperature is obtained by:
acquiring the temperature of each preset temperature measuring point in the terminal plane of the heating section;
the end point temperature is obtained based on an arithmetic average of the temperatures at the respective temperature measurement points.
7. A heat exchange coefficient obtaining apparatus of a resolving tower for obtaining a heat exchange coefficient of a heating section of the resolving tower, comprising:
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;
characterized in that the analytical 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 fourth temperature measuring element is used for acquiring the end point temperature of the heating section;
a calculation unit for obtaining the heat exchange coefficient K based on the hot air inlet temperature, the hot air outlet temperature, the starting point temperature, the end point temperature, the current fan rotating speed of the hot air fan and the current feeder rotating speed of the feederH；
KH＝FF1*(TTF1-TTF2)/(T2TE-T1TE)*FG1
Wherein, T1TERepresents the starting point temperature; t is2TERepresents the end point temperature; t isTF1The hot air inlet temperature; t isTF2The hot air outlet temperature; fF1Representing the current fan speed; fG1Representing the current feeder speed.
8. The heat exchange coefficient obtaining apparatus of a stripping tower as claimed in claim 7,
the third temperature measuring elements 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.
9. The heat exchange coefficient obtaining apparatus of a stripping tower as claimed in claim 7,
and a protective sleeve is arranged outside the third temperature measuring element.
10. The heat exchange coefficient obtaining apparatus of a stripping tower as claimed in claim 7,
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.
11. The heat exchange coefficient obtaining apparatus of a stripping tower as claimed in claim 10,
and a protective sleeve is arranged outside the fourth temperature measuring element.
CN201911026224.9A 2019-10-25 2019-10-25 Method and device for obtaining heat exchange coefficient of desorption tower Active CN112705010B (en)

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