Method for determining the safety of an adsorption system and device therefor

Abstract

A method for judging the safety of an adsorption system, the method comprising: conveying sintering flue gas to a primary adsorption tower for desulfurization treatment, discharging the flue gas after the desulfurization treatment from a flue gas outlet of the primary adsorption tower, discharging activated carbon after adsorbing pollutants from an activated carbon outlet of the primary adsorption tower into a desorption tower for heating and regeneration; in a top distribution section of the desorption tower, the activated carbon exchanges heat with hot nitrogen gas, the activated carbon is heated to increase the temperature, and the hot nitrogen gas is cooled to decrease the temperature; according to the heat balance principle, the temperature of the activated carbon when entering the inlet of the desorption tower is calculated by detecting the temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed, and the temperature of the activated carbon when being discharged from the outlet of the primary adsorption tower is converted to obtain, so as to judge the working state of the primary adsorption tower. The present application is based on the heat balance principle, the temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed is detected, the temperature of the activated carbon when being discharged from the outlet of the primary adsorption tower is calculated and converted to obtain, so as to judge the working state of the primary adsorption tower.

Description

TECHNICAL FIELD

[0001] The present application relates to a method and device for judging the safety of an activated carbon desulfurization system, in particular to a method and device for judging the safety of an adsorption system, and belongs to the technical field of activated carbon treatment of flue gas. BACKGROUND

[0002] Activated carbon flue gas purification technology has the characteristics of high efficiency of simultaneous purification of multiple pollutants, stable operation, resource utilization of by-products, and realization of ultra-low emission, and has many advantages in the field of sintering flue gas purification. The activated carbon flue gas purification system mainly includes an adsorption system, a regeneration system, a conveying system, a by-product resource utilization system, etc. The adsorption system is large in volume, has a large amount of activated carbon, and is the main place for adsorbing pollutants in sintering flue gas. In the adsorption system, the functions of desulfurization, dust removal, denitrification, and removal of other pollutants are mainly performed; the desorption system is a place for anaerobic heating of activated carbon that has adsorbed pollutants, and the sulfuric acid or sulfate adsorbed in the activated carbon is decomposed to generate high-concentration SO2; the conveying system is a process of circulating and transporting activated carbon from the adsorption tower to the desorption tower and then back to the adsorption tower.

[0003] As described above, the adsorption system is an environment with high temperature, oxygen, and combustible activated carbon, and the desulfurization reaction performed in the system is a strong exothermic reaction, so the heat effect in the adsorption system is huge. At the same time, it should be noted that a large amount of fine activated carbon powder is generated during the process of activated carbon running from the top to the bottom of the adsorption tower, so there is a risk of high temperature in the adsorption system.

[0004] The structure of the adsorption tower is shown in Figure 3 The tower body is generally divided into three layers, namely front, middle, and rear chambers. Among them, the thickness of the front chamber is the narrowest, the middle chamber is the second, and the rear chamber is the widest. In the process of removing pollutants, by adjusting the discharging frequency of the rollers in the front, middle, and rear chambers of the adsorption tower, efficient removal of pollutants is achieved. Among them, the front and middle chambers perform desulfurization and dust removal, and the rear chamber performs deep desulfurization and dust suppression. Activated carbon converts SO2 in flue gas into H2SO4, which is a strong exothermic reaction. SO2 adsorption is mainly concentrated in the front and middle chambers, and the chemical exothermicity of the front and middle chambers is the most obvious. Therefore, the discharging speed of the front chamber is the fastest, the discharging speed of the middle chamber is the second, and the discharging speed of the rear chamber is the slowest. The adsorption tower is huge in volume, and the temperature is mainly tested by point testing. The temperature measuring points cannot completely cover the adsorption tower, the discharging speed of the front and middle chambers is fast, and the channel is narrow. Therefore, in current industrial applications, the temperature measuring device is mainly placed in the rear chamber.

[0005] Under the normal state of system control and operation, the temperature of the adsorption system remains stable, but when the sintering flue gas temperature fluctuates greatly or the SO2 concentration in the flue gas suddenly rises, etc. Abnormal conditions, high temperature phenomenon will occur in the adsorption tower. The high temperature occurs in the front and middle chambers, and the high temperature point needs to spread to the back chamber to be detected by the thermometer, so it is difficult to detect and feed back in time and accurately, which has a great impact on the safety of the system. To solve this problem, the inventors of the present application proposed a method and system for judging the temperature rise of activated carbon in the desulfurization process in the patent with application number CN 202110008996.0. According to the principle of heat balance in the primary adsorption tower, the temperature of the flue gas entering and leaving the primary adsorption tower is detected in real time, the temperature change of the activated carbon in the primary adsorption tower during the desulfurization process is calculated, and the working state and safety of the primary adsorption tower are judged to prevent the risk of temperature rise abnormality of the system.

[0006] However, in subsequent research, the inventors of the present application found that the technology still has the following problems:

[0007] As mentioned earlier, SO2 adsorption is mainly concentrated in the front and middle chambers of the adsorption tower, so the high temperature occurs in the front and middle chambers. The flue gas inlet and outlet of the adsorption tower are arranged in the middle of the tower body, based on this, when the high temperature phenomenon or the ignition point occurs in the lower position of the front and middle chambers, and the high temperature phenomenon just occurs in the adsorption tower or the high temperature (or ignition) occurs in a small area, at this time, a small amount of high-temperature activated carbon in the lower part of the front and middle chambers basically does not affect the temperature of the flue gas discharged from the middle flue gas outlet, plus the fast discharging speed of the activated carbon in the front and middle chambers, and the flue gas itself has a certain temperature difference, that is, the temperature of the flue gas discharged from the flue gas outlet of the adsorption tower is still within the normal temperature range, so the high-temperature activated carbon cannot be truly fed back by the temperature change of the flue gas at the flue gas outlet, that is, the method of detecting the flue gas temperature to judge the temperature rise of the system in the above-mentioned patent CN 202110008996.0 is not applicable at this time.

[0008] The inventors of the present application also found in specific engineering applications that the flue gas temperature at the flue gas outlet of the adsorption tower is within the normal range, but the activated carbon with high temperature or ignition in the front and middle chambers of the adsorption tower has not been found, and the discharging speed of the activated carbon in the front and middle chambers is fast, the high-temperature activated carbon is not found and discharged from the adsorption tower, and then enters the desorption tower through the conveying device, thereby affecting the safety of the entire system.

[0009] Therefore, how to more accurately and comprehensively judge the safety of the adsorption system in the desulfurization process is a problem that needs to be solved. SUMMARY

[0010] In view of the problem that the high-temperature activated carbon at the lower position of the front and middle chambers of the adsorption tower in the prior art is difficult to detect and find, and the change of the flue gas temperature at the flue gas outlet cannot be detected and fed back to affect the safety of the adsorption system, the present application provides a method for judging the safety of the adsorption system. The method is based on the heat balance calculation of the heat exchange process between the activated carbon discharged from the adsorption tower and entering the desorption tower and the hot nitrogen gas introduced at the top of the desorption tower. The temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed is detected, the temperature of the activated carbon entering the inlet of the desorption tower is calculated, and the temperature of the activated carbon discharged from the outlet of the primary adsorption tower is converted, so as to judge the working state of the primary adsorption tower, guide the subsequent industrial production, and ensure the safety of the operation of the adsorption system.

[0011] Another object of the present application is to provide a device for judging the safety of the adsorption system for the above method. The device is simple in structure and convenient to operate, and can realize real-time monitoring of various parameters through related detection devices, so as to judge the working state and safety of the adsorption system through calculation, accurately guide the industrial production, and further avoid the harm of the activated carbon with abnormal temperature rise to the adsorption tower and even the entire flue gas purification system.

[0012] According to the first embodiment of the present application, a method for judging the safety of the adsorption system is provided.

[0013] A method for judging the safety of the adsorption system, the method comprising: conveying sintering flue gas to a primary adsorption tower, the activated carbon in the primary adsorption tower performing desulfurization treatment on the sintering flue gas, the flue gas after the desulfurization treatment being discharged from the flue gas outlet of the primary adsorption tower, and the activated carbon adsorbing pollutants being discharged from the activated carbon outlet of the primary adsorption tower and then entering a desorption tower for heating and regeneration. In a top distribution section of the desorption tower, the activated carbon entering the desorption tower exchanges heat with hot nitrogen gas introduced at the top of the desorption tower, the activated carbon is heated by the hot nitrogen gas and the temperature of the activated carbon is increased, and the temperature of the hot nitrogen gas is decreased. According to the principle of heat balance, the temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed is detected, the temperature of the activated carbon entering the inlet of the desorption tower is calculated, and the temperature of the activated carbon discharged from the outlet of the primary adsorption tower is converted, so as to judge the working state of the primary adsorption tower.

[0014] In the present application, the judgment of the working state of the primary adsorption tower specifically comprises the following steps:

[0015] 1) According to the activated carbon absorbing heat and the hot nitrogen gas releasing heat in the top distribution section of the desorption tower, the actual temperature of the activated carbon entering the inlet of the desorption tower is calculated.

[0016] 2) According to the temperature drop of the activated carbon during the transportation between the primary adsorption tower and the desorption tower, the actual temperature of the activated carbon entering the inlet of the desorption tower calculated in step 1) is converted to the actual temperature of the activated carbon discharged from the outlet of the primary adsorption tower.

[0017] 3) According to the heat generated in the primary adsorption tower being equal to the heat consumed and discharged by the primary adsorption tower, the theoretical temperature of the activated carbon discharged from the outlet of the primary adsorption tower is calculated.

[0018] 4) The working state of the primary adsorption tower is judged by comparing the actual temperature of the activated carbon discharged from the outlet of the primary adsorption tower with the theoretical temperature.

[0019] In the present application, step 1) is specifically: a first temperature detection device is arranged in the top distribution section of the desorption tower, and the first temperature detection device detects the temperature t3, ℃ of the activated carbon after heat exchange with hot nitrogen gas is completed. According to the heat balance principle, in the heat exchange process, the heat absorbed by the activated carbon is equal to the heat released by the hot nitrogen gas. That is:

[0020] m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1)。

[0021] That is:

[0022]

[0023] In the formula, t1 is the actual temperature of the activated carbon entering the inlet of the desorption tower, ℃. m1 is the amount of activated carbon entering the desorption tower per unit time, kg / h. c p1 is the specific heat capacity of the activated carbon, kJ / (kg·℃). q1 is the flow rate of the hot nitrogen gas introduced into the top of the desorption tower per unit time, Nm 3 / h. ρ1 is the density of nitrogen, kg / Nm 3 . c p2 is the specific heat capacity of nitrogen, kJ / (kg·℃). t2 is the initial temperature of the hot nitrogen gas introduced into the top of the desorption tower, ℃. t3 is the temperature of the activated carbon and nitrogen after heat exchange is completed, ℃. At this time, the temperature of the activated carbon and nitrogen is consistent.

[0024] In the present application, step 2) is specifically: the temperature drop of the activated carbon during transportation between the primary adsorption tower and the desorption tower is Δt, ℃. Therefore, the actual temperature of the activated carbon discharged from the outlet of the primary adsorption tower is:

[0025] t4=t1+Δt…(3)。

[0026] In the formula, t4 is the actual temperature of the activated carbon discharged from the outlet of the primary adsorption tower, ℃.

[0027] In the present application, in step 3), the heat generated in the primary adsorption tower being equal to the heat consumed and discharged by the primary adsorption tower is specifically:

[0028] 301) Calculate the heat generated in the primary adsorption tower: the heat Q入 The heat Q1 brought in by the sintering flue gas into the primary adsorption tower, the heat Q2 released by the desulfurization reaction, the heat Q f That is:

[0029] Q 入 = Q1 + Q2 + Q f …(4).

[0030] 302) Calculate the heat consumed and discharged by the primary adsorption tower: the heat Q 出 The heat Q3 brought out by the flue gas after desulfurization out of the primary adsorption tower, the heat Qc brought out by the activated carbon out of the primary adsorption tower, and the heat loss Q5. That is:

[0031] Q 出 = Q3 + Qc + Q5.

[0032] Since the heat Qc brought out by the activated carbon out of the primary adsorption tower is the sum of the heat Q f Brought in by the activated carbon into the primary adsorption tower and the heat Q4 absorbed by the activated carbon in the primary adsorption tower. That is:

[0033] Qc = Q f + Q4.

[0034] That is:

[0035] Q 出 = Q3 + Q4 + Q f + Q5…(5).

[0036] 303) According to the principle of heat balance, the heat generated in the primary adsorption tower is equal to the heat consumed and discharged by the primary adsorption tower. That is:

[0037] Q1 + Q2 + Q f = Q3 + Q4 + Q f + Q5…(6).

[0038] Equation (6) can be simplified as: Q1 + Q2 = Q3 + Q4 + Q5…(7).

[0039] In the heat consumed and discharged by the primary adsorption tower, the heat loss Q5 ≈ 0, thus, equation (7) can be simplified as:

[0040] Q1 + Q2 = Q3 + Q4…(8).

[0041] In the present application, in step 3), according to equation (8), the theoretical temperature of the activated carbon out of the primary adsorption tower outlet is calculated, specifically:

[0042] Calculate the heat Q1 brought in by the sintering flue gas into the primary adsorption tower:

[0043]

[0044] Q1 = q2·c p3 wherein Q1 is the heat brought by the sintering flue gas into the primary adsorption tower, kJ. q2 is the flow rate of the sintering flue gas at the flue gas inlet of the primary adsorption tower, L / h. c m is the specific heat capacity of the flue gas, kJ / (mol·℃). v p3 is the standard molar volume, L / mol. t5 is the temperature of the sintering flue gas at the flue gas inlet of the primary adsorption tower, ℃. t0 is the temperature reference value, generally 25 ℃. T0 is the initial time when the sintering flue gas enters the primary adsorption tower, h. T1 is the end time when the sintering flue gas enters the primary adsorption tower, h.

[0045] The heat Q2 released by the desulfurization reaction is calculated as follows:

[0046]

[0047] Q2 = q2·(C0 - C1)·M·H

[0048] The heat Q3 brought out by the flue gas after desulfurization when it is discharged from the primary adsorption tower is calculated as follows:

[0049]

[0050] Q3 = q2·c

[0051] Q3 = q2·c m wherein Q3 is the heat brought out by the flue gas after desulfurization when it is discharged from the primary adsorption tower, kJ. q2 is the flue gas flow rate at the flue gas outlet of the primary adsorption tower, L / h. c p3 is the specific heat capacity of the flue gas, kJ / (mol·℃). v m is the standard molar volume, L / mol. t6 is the temperature of the flue gas after desulfurization at the flue gas outlet of the primary adsorption tower, ℃. t0 is the temperature reference value, ℃. T0 + δT is the initial time when the flue gas after desulfurization is discharged from the primary adsorption tower, h. T1 + δT is the end time when the flue gas after desulfurization is discharged from the primary adsorption tower, h.

[0052] The heat Q4 absorbed by the activated carbon in the primary adsorption tower is calculated as follows:

[0053] Q4 = m2·c p1(t'4-t7)…(13).

[0054] wherein: Q4 is the heat absorbed by the activated carbon in the primary adsorption tower, kJ.m2 is the mass of the activated carbon loaded in the primary adsorption tower, kg. c is the specific heat capacity of the activated carbon, kJ / (kg·℃). t7 is the temperature of the activated carbon entering the inlet of the primary adsorption tower, ℃. t'4 is the theoretical temperature of the activated carbon exiting the outlet of the primary adsorption tower, ℃. p1

[0055] According to formula (8), the theoretical temperature t'4 of the activated carbon exiting the outlet of the primary adsorption tower is calculated, i.e.:

[0056]

[0057] wherein the flow rate q2 of the sintering flue gas at the inlet of the primary adsorption tower is consistent with the flow rate q3 of the desulfurized flue gas at the outlet of the primary adsorption tower, q2≈q3=q. That is:

[0058]

[0059] In the present application, step 4) is specifically: calculating the deviation Z of the actual temperature t4 of the activated carbon exiting the outlet of the primary adsorption tower and the theoretical temperature t'4. That is:

[0060]

[0061] When Z is less than or equal to 10%, preferably less than or equal to 8%, more preferably less than or equal to 5%, it indicates that the temperature of the activated carbon discharged by the primary adsorption tower after the adsorption desulfurization treatment is within the normal temperature range, and the adsorption system is running normally.

[0062] On the contrary, it indicates that the temperature of the activated carbon discharged by the primary adsorption tower at this time exceeds the fluctuation range of the normal temperature, i.e. the working state of the primary adsorption tower is abnormal, at this time the operating conditions of the primary adsorption tower are adjusted or the system is shut down for inspection, to ensure the safety and stability of the system.

[0063] According to the second embodiment of the present application, a device for judging the safety of an adsorption system is provided.

[0064] ​A device for judging the safety of an adsorption system or a device for judging the safety of an adsorption system in the method of the first embodiment, which comprises a primary adsorption tower, a desorption tower, a sintering flue gas pipeline and a desulfurized flue gas pipeline. The sintering flue gas pipeline is connected to the flue gas inlet of the primary adsorption tower. The desulfurized flue gas pipeline is connected to the flue gas outlet of the primary adsorption tower. The activated carbon outlet of the primary adsorption tower is connected to the activated carbon inlet of the desorption tower through a conveying device. A hot nitrogen gas pipeline is connected to the top distribution section of the desorption tower. It is characterized in that: a first temperature detection device is arranged in the top distribution section of the desorption tower. A first flow detection device is arranged at the activated carbon inlet position of the desorption tower. A second flow detection device and a second temperature detection device are arranged on the hot nitrogen gas pipeline. A third flow detection device, a third temperature detection device and a first SO2 concentration detection device are arranged on the sintering flue gas pipeline and close to the flue gas inlet of the primary adsorption tower. A fourth temperature detection device and a second SO2 concentration detection device are arranged on the desulfurized flue gas pipeline and close to the flue gas outlet of the primary adsorption tower. A first mass detection device and a fifth temperature detection device are arranged at the activated carbon inlet position of the primary adsorption tower. The device further comprises a timing element. The timing element is used to record the time when the flue gas enters and exits the primary adsorption tower.

[0065] As a preference, the device further comprises a fourth flow detection device arranged on the desulfurized flue gas pipeline and close to the flue gas outlet of the primary adsorption tower.

[0066] As a preference, the device further comprises a second mass detection device arranged at the activated carbon outlet position of the primary adsorption tower.

[0067] In the invention, the device further comprises a control system. The control system is connected with the first temperature detection device, the second temperature detection device, the third temperature detection device, the fourth temperature detection device, the fifth temperature detection device, the first flow detection device, the second flow detection device, the third flow detection device, the fourth flow detection device, the first SO2 concentration detection device, the second SO2 concentration detection device, the first mass detection device and the second mass detection device, and calculates the deviation degree of the actual temperature of the activated carbon when it exits the outlet of the primary adsorption tower from the theoretical temperature in real time according to formulas (2), (3), (15) and (16), so as to judge the working state of the primary adsorption tower.

[0068] The activated carbon converts SO2 in flue gas into H2SO4, which is a strong exothermic reaction, and the adsorption of SO2 is mainly concentrated in the front chamber and the middle chamber of the adsorption tower. The chemical exothermicity of the front chamber and the middle chamber is most obvious, so the high temperature often occurs in the front chamber and the middle chamber. The flue gas inlet and outlet of the adsorption tower are arranged in the middle of the tower body, so when the high temperature phenomenon or the ignition point occurs below the front chamber and the middle chamber, and the high temperature phenomenon or the ignition point just occurs in the adsorption tower or a small area and a small range, the small amount of high-temperature activated carbon below the front chamber and the middle chamber basically does not affect the temperature of the flue gas discharged from the middle flue gas outlet. In addition, the activated carbon in the front chamber and the middle chamber is discharged at a high speed, and the flue gas itself has a certain temperature difference, that is, the temperature of the flue gas discharged from the flue gas outlet of the adsorption tower is still within the normal temperature range. Therefore, the high-temperature activated carbon cannot be truly fed back through the change of the flue gas temperature at the flue gas outlet, and the high-temperature activated carbon is not found. The high-temperature activated carbon discharged from the adsorption tower enters the desorption tower, thereby affecting the safety of the entire system.

[0069] In view of the problem that the high-temperature activated carbon below the front chamber and the middle chamber of the adsorption tower is difficult to detect and find, and cannot be detected and fed back through the change of the flue gas temperature at the flue gas outlet to affect the safety of the adsorption system, the present application provides a method for judging the safety of the adsorption system and a device thereof. The present application does not need to detect the temperature of the activated carbon at the outlet of the primary adsorption tower, and does not need to rely on the change of the flue gas temperature at the flue gas outlet of the primary adsorption tower to judge the safety of the adsorption system. Instead, according to the heat balance principle, in the top distribution section of the desorption tower, based on the heat balance of the heat exchange process between the activated carbon discharged from the adsorption tower and entering the desorption tower and the hot nitrogen gas introduced at the top of the desorption tower, the temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed is detected in real time, the temperature of the activated carbon when entering the inlet of the desorption tower is calculated, and the temperature of the activated carbon when discharged from the outlet of the primary adsorption tower is converted, so as to judge the real-time working state of the primary adsorption tower, guide the subsequent industrial production, and thereby avoid the system safety hidden danger caused by the high-temperature activated carbon not being found in the prior art, and provide protection for the safety of the operation of the adsorption tower and the entire flue gas purification system.

[0070] In the existing activated carbon flue gas purification system, the desorption tower is a place for heating and regeneration of activated carbon adsorbed with pollutants, which mainly includes a top distribution section, a heating section, a transition section, a cooling section and a bottom distribution section. Among them, the top distribution section is to initially distribute the activated carbon discharged from the adsorption tower into the shorter pipe, and a temperature measuring point is arranged in the top distribution section to detect the temperature of the activated carbon discharged from the adsorption tower. In order to prevent the phenomenon of condensation corrosion of the pipe wall in the top distribution section, hot nitrogen gas needs to be added at the top of the tower, and the temperature of the nitrogen gas is generally higher than 100℃; at the same time, the added nitrogen gas can also be used as a carrier gas for the desorbed SRG gas. The heating section is a place for heating and regeneration of activated carbon adsorbed with pollutants, and the temperature is generally controlled at 430℃. The transition section is a position for discharging the desorbed SRG gas. The cooling section is a place for cooling the activated carbon after heating and regeneration, and the outlet temperature of the cooling section is generally controlled within 100℃. The bottom distribution section is a place for re-distribution of the activated carbon discharged from the cooling section to prevent the discharge port of the desorption tower from being blocked.

[0071] Specifically, the method for judging the safety of the adsorption system comprises the following steps:

[0072] 1) In the top distribution section of the desorption tower, according to the heat balance principle, the heat absorbed by the activated carbon is equal to the heat released by the hot nitrogen gas, and the actual temperature of the activated carbon entering the inlet of the desorption tower is calculated.

[0073] Generally, the filling amount of activated carbon in the adsorption tower is very large, compared with the difficulty of detecting or finding a small amount of high-temperature activated carbon in the adsorption tower, the exchange heat of high-temperature activated carbon with hot nitrogen gas is more sufficient when the high-temperature activated carbon enters the desorption tower from the activated carbon inlet of the desorption tower, so that the actual temperature of the activated carbon entering the inlet of the desorption tower can be calculated relatively accurately through the temperature change of nitrogen gas before and after heat exchange.

[0074] 2) According to the temperature drop of the activated carbon during transportation between the primary adsorption tower and the desorption tower, the actual temperature of the activated carbon entering the inlet of the desorption tower calculated in the above step 1) is converted into the actual temperature of the activated carbon discharged from the outlet of the primary adsorption tower.

[0075] An activated carbon conveying system (such as a conveyor) is arranged between the activated carbon outlet of the primary adsorption tower and the activated carbon inlet of the desorption tower. At present, the activated carbon conveying system will be heat-insulated, so that the heat dissipation temperature of the activated carbon remains basically unchanged (for example, Δt=60℃) during the conveying process. In addition, the present application is aimed at the case that high-temperature phenomenon occurs at the lower position of the front and middle chambers of the adsorption tower or small area and small range of high temperature, and a small amount of high-temperature activated carbon is mixed in a large amount of normal-temperature activated carbon during the conveying process, so that the small amount of high-temperature activated carbon basically does not affect the normal temperature drop caused by heat dissipation in the conventional conveying process.

[0076] It should be noted that the normal temperature drop corresponding to the conveying system of different activated carbon flue gas purification equipment of each steel plant is not necessarily the same, and the actual application equipment and working condition is specific. For example, the conveying temperature drop of activated carbon between the first-stage adsorption tower and the desorption tower corresponding to a set of equipment of a steel plant is Δt = 60°C, the conveying temperature drop of activated carbon between the first-stage adsorption tower and the desorption tower corresponding to another set of equipment of the steel plant is Δt = 52°C; and the conveying temperature drop of activated carbon between the first-stage adsorption tower and the desorption tower corresponding to a set of equipment of another steel plant is Δt = 71°C.

[0077] 3) In the first-stage adsorption tower, according to the heat balance principle, the heat generated in the first-stage adsorption tower is equal to the heat consumed and discharged by the first-stage adsorption tower, and the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower is calculated.

[0078] As described above, the present application is aimed at the case that high temperature phenomenon occurs at the lower position of the front and middle chambers of the adsorption tower or small area and small range high temperature occurs, at this time, the small amount of high temperature activated carbon located at the lower position of the front and middle chambers basically does not affect the temperature of the flue gas discharged from the middle flue gas outlet, that is, the temperature of the flue gas discharged from the flue gas outlet of the adsorption tower is still within the normal temperature range. Based on this, the heat balance of the first-stage adsorption tower can be calculated, and the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower (i.e. the temperature of the activated carbon discharged from the first-stage adsorption tower under normal working condition) is calculated by detecting the flue gas temperature at the inlet and outlet of the first-stage adsorption tower.

[0079] 4) Compare the actual temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower with the theoretical temperature to determine the working condition of the first-stage adsorption tower.

[0080] By calculating the deviation degree of the actual temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower and the theoretical temperature, it is determined whether the temperature of the activated carbon discharged from the first-stage adsorption tower is within the controllable fluctuation range of the normal temperature, so as to determine the real-time working condition of the first-stage adsorption tower, that is, the safety of the adsorption system; and then accurately guide the industrial production, timely adjust the activated carbon temperature rise in the adsorption system during the desulfurization process, prevent the risk of abnormal temperature rise of the system, and ensure the safe and stable operation of the entire flue gas purification system.

[0081] Specifically, when the actual temperature of the activated carbon discharged from the outlet of the first adsorption tower is within the normal fluctuation range of the theoretical temperature, it indicates that the adsorption system is running normally at this time, and the system can continue to run. When the actual temperature of the activated carbon discharged from the outlet of the first adsorption tower exceeds the controllable fluctuation range of the theoretical temperature, it indicates that the working state of the first adsorption tower is abnormal at this time, and the running condition of the first adsorption tower is adjusted (for example, the activated carbon is discharged quickly to remove the high-temperature activated carbon, or nitrogen is introduced into the front and middle chambers of the first adsorption tower) or the system is stopped for inspection according to the temperature fluctuation degree, so as to ensure the safety and stability of the system.

[0082] In the present application, the heat generated in the first adsorption tower includes the heat brought in by the sintering flue gas entering the first adsorption tower, the heat released by the desulfurization reaction, and the heat brought in by the activated carbon entering the first adsorption tower, i.e. Q 入 = Q 1+ Q 2+ Q f …(4). The heat consumed and discharged by the first adsorption tower includes the heat brought out by the flue gas after desulfurization discharged from the first adsorption tower, the heat brought out by the activated carbon discharged from the first adsorption tower, and the heat loss, i.e. Q 出 = Q 3+ Qc + Q5. Since the heat brought out by the activated carbon discharged from the first adsorption tower is the sum of the heat brought in by the activated carbon entering the first adsorption tower and the heat absorbed by the activated carbon in the first adsorption tower, i.e. Qc = Q 4+ Q f , we have Q 出 = Q 3+ Q 4+ Q f+ Q5…(5). The heat generated in the first adsorption tower is equal to the heat consumed and discharged by the first adsorption tower, i.e. Q 1+ Q 2+ Q f = Q 3+ Q 4+ Q f+ Q5…(6), which can be simplified as Q 1+ Q2 = Q 3+ Q 4+ Q5…(7). In the present application, since the proportion of heat loss consumed heat is very small, far less than the heat brought out by the flue gas after desulfurization discharged from the first adsorption tower and the heat absorbed by the activated carbon in the first adsorption tower, the influence of heat loss can be ignored in engineering application, i.e. Q5 ≈ 0, thus formula (7) can be simplified as Q 1+ Q2 = Q 3+ Q4…(8).

[0083] In the present application, the sintering flue gas purification system is continuously operated for a long time. In the equilibrium state reached by long-term operation, the flow rate q2 of the sintering flue gas at the inlet of the primary adsorption tower is substantially consistent with the flow rate q3 of the desulfurized flue gas at the outlet of the primary adsorption tower, i.e., q2≈q3=q. According to formula (8), the theoretical temperature t'4 of the activated carbon discharged from the outlet of the primary adsorption tower can be obtained:

[0084]

[0085] In the formula, q is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower or the flow rate of the desulfurized flue gas at the outlet of the primary adsorption tower, which can be detected by the third flow rate detection device arranged at the inlet position of the primary adsorption tower or the fourth flow rate detection device arranged at the outlet position of the primary adsorption tower. C0 is the SO2 concentration at the inlet of the primary adsorption tower, which can be detected by the first SO2 concentration detection device arranged at the inlet position of the primary adsorption tower. C1 is the SO2 concentration at the outlet of the primary adsorption tower, which can be detected by the second SO2 concentration detection device arranged at the outlet position of the primary adsorption tower. t5 is the temperature of the sintering flue gas at the inlet of the primary adsorption tower, which can be detected by the third temperature detection device arranged at the inlet position of the primary adsorption tower. t6 is the temperature of the desulfurized flue gas at the outlet of the primary adsorption tower, which can be detected by the fourth temperature detection device arranged at the outlet position of the primary adsorption tower. m2 is the loading mass of the activated carbon in the primary adsorption tower. Generally, the corresponding loading mass is known after the selected adsorption tower is determined. In addition, m2 can also be detected by the first mass detection device arranged at the activated carbon inlet position of the primary adsorption tower or the second mass detection device arranged at the activated carbon outlet position of the primary adsorption tower. t7 is the temperature of the activated carbon entering the inlet of the primary adsorption tower, which can be detected by the fifth temperature detection device arranged at the activated carbon inlet position of the primary adsorption tower. TO is the initial time when the sintering flue gas enters the primary adsorption tower, and T1 is the end time when the sintering flue gas enters the primary adsorption tower. TO and T1 can be measured by a timing element.

[0086] It should be noted that the present application is directed to the adsorption and purification treatment of sintering flue gas. The oxygen content of the sintering flue gas is generally 14-18%, with an average of about 16%. The water content is generally 8-12%, with an average of about 10%. The fluctuation range of the SO2 content in the sintering flue gas is approximately 400-2000 mg / Nm 3The concentration of oxygen and water in the sintering flue gas is far greater than the concentration of sulfur dioxide, and the active carbon desulfurization principle is 2SO2+O2+2H2O=2H2SO4, obviously, the oxygen content and water content in the sintering flue gas can meet the demand of the reaction formula 2SO2+O2+2H2O=2H2SO4, that is, the oxygen content and water content in the sintering flue gas can meet the condition that all SO2 in the flue gas is converted into H2SO4. That is to say, the SO2 adsorbed in the primary adsorption tower in the application is basically converted into H2SO4, so the heat released by the desulfurization reaction calculated by the SO2 concentration change amount obtained by C0-C1 in the above formula (15) is basically consistent.

[0087] Compared with the prior art, the application has the following beneficial technical effects:

[0088] 1. The application is aimed at the small range of high temperature phenomenon appearing below the front and middle rooms of the adsorption tower, the heat balance of the heat exchange process of the active carbon entering the desorption tower and the hot nitrogen gas introduced into the top of the desorption tower is calculated, the temperature of the active carbon entering the desorption tower inlet is calculated, and the temperature of the active carbon discharged from the primary adsorption tower outlet is converted, so as to judge the working state of the primary adsorption tower, guide the subsequent industrial production, and ensure the safety of the adsorption system operation.

[0089] 2. The application does not need to detect the temperature of the active carbon at the outlet position of the primary adsorption tower, and does not need to rely on the change of the flue gas temperature at the flue gas outlet position of the primary adsorption tower to judge the safety of the adsorption system, but according to the heat balance principle, based on the heat balance in the top distribution section of the desorption tower, the actual temperature of the active carbon discharged from the primary adsorption tower outlet is calculated and converted, and based on the heat balance in the primary adsorption tower, the theoretical temperature of the active carbon discharged from the primary adsorption tower outlet is calculated, and the working state of the primary adsorption tower is judged by the deviation between the two, so as to avoid the system safety hidden danger caused by the high temperature active carbon below the front and middle rooms in the prior art, and provide protection for the safety of the adsorption tower and the whole flue gas purification system operation.

[0090] 3. The device of the application has simple structure and convenient operation, can more accurately and comprehensively judge the safety of the adsorption system in the desulfurization process, and is not affected by the number distribution, damage and the like of the temperature measuring device in the adsorption tower. BRIEF DESCRIPTION OF DRAWINGS

[0091] Figure 1 The principle diagram of the method for judging the safety of the adsorption system of the application;

[0092] Figure 2 The flow chart of the method for judging the safety of the adsorption system of the application;

[0093] Figure 3 Fig. 1 is a structural schematic diagram of a primary adsorption tower in the present application;

[0094] Figure 4 Fig. 2 is a structural schematic diagram of a device for judging the safety of an adsorption system in the present application;

[0095] Figure 5 Fig. 3 is a schematic diagram of a control system in the present application.

[0096] Fig. 1 is a structural schematic diagram of a primary adsorption tower in the present application;

[0097] L1: sintering flue gas pipeline; L2: flue gas pipeline after desulfurization; L3: hot nitrogen gas pipeline. DETAILED DESCRIPTION

[0098] The technical solutions of the present application are illustrated below, and the scope of protection requested by the present application includes but is not limited to the following embodiments.

[0099] According to a first embodiment of the present application, a method for judging the safety of an adsorption system is provided.

[0100] A method for judging the safety of an adsorption system, the method comprising: conveying sintering flue gas to a primary adsorption tower 1, the activated carbon in the primary adsorption tower 1 performing desulfurization treatment on the sintering flue gas, the flue gas after desulfurization treatment being discharged from a flue gas outlet of the primary adsorption tower 1, and the activated carbon adsorbing pollutants being discharged from an activated carbon outlet of the primary adsorption tower 1 and then entering a desorption tower 2 for heating and regeneration. In a top distribution section 201 of the desorption tower 2, the activated carbon entering the desorption tower 2 exchanges heat with hot nitrogen gas introduced into the top of the desorption tower 2, the activated carbon is heated by the hot nitrogen gas and its temperature rises, and the temperature of the hot nitrogen gas decreases. According to the principle of heat balance, by detecting the temperature of the hot nitrogen gas and the activated carbon after heat exchange is completed, the temperature of the activated carbon when it enters the inlet of the desorption tower 2 is calculated, and the temperature of the activated carbon when it is discharged from the outlet of the primary adsorption tower 1 is converted to obtain, so as to judge the working state of the primary adsorption tower 1.

[0101] In the present application, the judging of the working state of the primary adsorption tower 1 specifically comprises the following steps:

[0102] 1) According to the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas being equal in the top distribution section 201 of the desorption tower 2, the actual temperature of the activated carbon entering the inlet of the desorption tower 2 is calculated.

[0103] 2) According to the temperature drop of the activated carbon during transportation between the primary adsorption tower 1 and the desorption tower 2, the actual temperature of the activated carbon entering the inlet of the desorption tower 2 calculated in step 1) is converted into the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1.

[0104] 3) According to the heat generated in the primary adsorption tower 1 and the heat consumed and discharged by the primary adsorption tower 1 being equal, the theoretical temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 is calculated.

[0105] 4) The working state of the primary adsorption tower 1 is judged by comparing the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 with the theoretical temperature.

[0106] In the present application, step 1) is specifically: a first temperature detection device 301 is arranged in the top distribution section 201 of the desorption tower 2, and the first temperature detection device 301 detects the temperature t3, ℃ of the activated carbon after heat exchange with the hot nitrogen gas is completed. According to the heat balance principle, the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas are equal during the heat exchange process. That is:

[0107] m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1)。

[0108] That is:

[0109]

[0110] In the formula: t1 is the actual temperature of the activated carbon entering the inlet of the desorption tower, ℃. m1 is the amount of activated carbon entering the desorption tower per unit time, kg / h. c p1 is the specific heat capacity of the activated carbon, kJ / (kg·℃). q1 is the flow rate of the hot nitrogen gas introduced into the top of the desorption tower per unit time, Nm 3 / h. ρ1 is the density of nitrogen, kg / Nm 3 . c p2 is the specific heat capacity of nitrogen, kJ / (kg·℃). t2 is the initial temperature of the hot nitrogen gas introduced into the top of the desorption tower, ℃. t3 is the temperature of the activated carbon and nitrogen after the heat exchange is completed, ℃.

[0111] In the present application, step 2) is specifically: the temperature drop of the activated carbon during transportation between the primary adsorption tower 1 and the desorption tower 2 is Δt, ℃. Therefore, the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 is:

[0112] t4=t1+Δt…(3).

[0113] In the formula, t4 is the actual temperature of the activated carbon at the outlet of the first-stage adsorption tower, in ℃.

[0114] In the present application, in step 3), the heat generated in the first-stage adsorption tower 1 is equal to the heat consumed and discharged by the first-stage adsorption tower 1, specifically:

[0115] 301) Calculate the heat generated in the first-stage adsorption tower 1: the heat generated in the first-stage adsorption tower 1 Q 入 including the heat Q1 brought in by the sintering flue gas entering the first-stage adsorption tower 1, the heat Q2 released by the desulfurization reaction, and the heat Q f That is:

[0116] Q 入 = Q1 + Q2 + Q f …(4).

[0117] 302) Calculate the heat consumed and discharged by the first-stage adsorption tower 1: the heat consumed and discharged by the first-stage adsorption tower 1 Q 出 including the heat Q3 brought out by the flue gas after desulfurization discharging the first-stage adsorption tower 1, the heat Qc brought out by the activated carbon discharging the first-stage adsorption tower 1, and the heat loss Q5. That is:

[0118] Q 出 = Q3 + Qc + Q5.

[0119] Since the heat Qc brought out by the activated carbon discharging the first-stage adsorption tower 1 is the sum of the heat Q f brought in by the activated carbon entering the first-stage adsorption tower 1 and the heat Q4 absorbed by the activated carbon in the first-stage adsorption tower 1. That is:

[0120] Qc = Q f + Q4.

[0121] That is:

[0122] Q 出 = Q3 + Q4 + Q f+ Q5…(5).

[0123] 303) According to the principle of heat balance, the heat generated in the first-stage adsorption tower 1 is equal to the heat consumed and discharged by the first-stage adsorption tower 1. That is:

[0124] Q 1+ Q 2+ Q f = Q 3+ Q 4+ Q f+ Q5…(6).

[0125] Formula (6) can be simplified as: Q1+ Q2=Q 3+ Q 4+ Q5…(7)。

[0126] In the heat consumed and discharged by the primary adsorption tower 1, the heat loss Q5≈0, and thus, formula (7) can be simplified as:

[0127] Q 1+ Q2=Q 3+ Q4…(8)。

[0128] In the present application, in step 3), the theoretical temperature of the activated carbon discharged from the outlet of the primary adsorption tower 1 is calculated according to formula (8), specifically:

[0129] The heat Q1 brought in by the sintering flue gas into the primary adsorption tower 1 is calculated as follows:

[0130]

[0131] wherein Q1 is the heat brought in by the sintering flue gas into the primary adsorption tower, kJ. q2 is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower, L / h. c p3 is the specific heat capacity of the flue gas, kJ / (mol·℃). v m is the standard molar volume, L / mol. t5 is the temperature of the sintering flue gas at the inlet of the primary adsorption tower, ℃. t0 is the temperature reference value, generally 25℃. T0 is the initial time when the sintering flue gas enters the primary adsorption tower, h. T1 is the end time when the sintering flue gas enters the primary adsorption tower, h.

[0132] The heat Q2 released by the desulfurization reaction is calculated as follows:

[0133]

[0134] wherein Q2 is the heat released by the desulfurization reaction, kJ. q2 is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower, L / h. C0 is the SO2 concentration at the inlet of the primary adsorption tower, g / L. C1 is the SO2 concentration at the outlet of the primary adsorption tower, g / L. M is the molar mass of SO2, g / mol. H is the heat released by the generation of 1 mol of sulfuric acid, kJ / mol. T0 is the initial time when the sintering flue gas enters the primary adsorption tower, h. T1 is the end time when the sintering flue gas enters the primary adsorption tower, h.

[0135] The heat Q3 brought out by the flue gas discharged from the primary adsorption tower 1 after desulfurization is calculated as follows:

[0136]

[0137] i.e.:

[0138] Q3 = q2·c p3 c is the specific heat capacity of the flue gas, kJ / (mol·℃). m t6 is the temperature of the desulfurized flue gas at the outlet of the first-stage adsorption tower, ℃. t0 is the temperature reference value, ℃. T0+δT is the initial time when the desulfurized flue gas is discharged from the first-stage adsorption tower, h. T1+δT is the end time when the desulfurized flue gas is discharged from the first-stage adsorption tower, h.

[0139] The heat Q4 absorbed by the activated carbon in the first-stage adsorption tower 1 is calculated as follows:

[0140] Q4 = m2·c pi ·(t′4-t7)...(13).

[0141] Q4 = m2·c p1 c is the specific heat capacity of the activated carbon, kJ / (kg·℃). t7 is the temperature of the activated carbon entering the inlet of the first-stage adsorption tower, ℃. t′4 is the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower 1, ℃.

[0142] According to formula (8), the theoretical temperature t′4 of the activated carbon discharged from the outlet of the first-stage adsorption tower 1 is calculated, that is,

[0143]

[0144] wherein the flow rate q2 of the sintering flue gas at the inlet of the first-stage adsorption tower 1 is consistent with the flow rate q3 of the desulfurized flue gas at the outlet of the first-stage adsorption tower 1, q2≈q3=q. That is,

[0145]

[0146] In the present application, step 4) is specifically: calculating the deviation Z of the actual temperature t4 of the activated carbon discharged from the outlet of the first-stage adsorption tower 1 and the theoretical temperature t′4. That is,

[0147]

[0148] When Z is less than or equal to 10%, preferably less than or equal to 8%, more preferably less than or equal to 5%, it indicates that the temperature of the activated carbon discharged from the first-stage adsorption tower 1 after the adsorption desulfurization treatment is within the normal temperature range, and the adsorption system is running normally.

[0149] Conversely, it indicates that the temperature of the activated carbon discharged from the primary adsorption tower 1 exceeds the fluctuation range of the normal temperature, i.e. the working state of the primary adsorption tower 1 is abnormal, and the running condition of the primary adsorption tower 1 is adjusted or the primary adsorption tower 1 is stopped for inspection to ensure the safety and stability of the system.

[0150] According to the second embodiment of the present application, a device for judging the safety of an adsorption system is provided.

[0151] A device for judging the safety of an adsorption system or a device for judging the safety of an adsorption system according to the method of the first embodiment, the device comprising a primary adsorption tower 1, a desorption tower 2, a sintering flue gas pipeline L1 and a flue gas pipeline L2 after desulfurization. The sintering flue gas pipeline L1 is connected to the flue gas inlet of the primary adsorption tower 1. The flue gas pipeline L2 after desulfurization is connected to the flue gas outlet of the primary adsorption tower 1. The activated carbon outlet of the primary adsorption tower 1 is connected to the activated carbon inlet of the desorption tower 2 through a conveying device. A hot nitrogen gas pipeline L3 is connected to the top distribution section 201 of the desorption tower 2. The device is characterized in that: a first temperature detection device 301 is arranged in the top distribution section 201 of the desorption tower 2. A first flow detection device 401 is arranged at the activated carbon inlet position of the desorption tower 2. A second flow detection device 402 and a second temperature detection device 302 are arranged on the hot nitrogen gas pipeline L3. A third flow detection device 403, a third temperature detection device 303 and a first SO2 concentration detection device 501 are arranged on the sintering flue gas pipeline L1 and close to the flue gas inlet position of the primary adsorption tower 1. A fourth temperature detection device 304 and a second SO2 concentration detection device 502 are arranged on the flue gas pipeline L2 after desulfurization and close to the flue gas outlet position of the primary adsorption tower 1. A first mass detection device 601 and a fifth temperature detection device 305 are arranged at the activated carbon inlet position of the primary adsorption tower 1. The device further comprises a timing element. The timing element is used to record the time when the flue gas enters and exits the primary adsorption tower 1.

[0152] As a preferred embodiment, the device further comprises a fourth flow detection device 404 arranged on the flue gas pipeline L2 after desulfurization and close to the flue gas outlet position of the primary adsorption tower 1.

[0153] As a preferred embodiment, the device further comprises a second mass detection device 602 arranged at the activated carbon outlet position of the primary adsorption tower 2.

[0154] In the invention, the device further comprises a control system 7. The control system 7 is connected with the first temperature detecting device 301, the second temperature detecting device 302, the third temperature detecting device 303, the fourth temperature detecting device 304, the fifth temperature detecting device 305, the first flow detecting device 401, the second flow detecting device 402, the third flow detecting device 403, the fourth flow detecting device 404, the first SO2 concentration detecting device 501, the second SO2 concentration detecting device 502, the first mass detecting device 601, the second mass detecting device 602, and calculates the deviation of the actual temperature from the theoretical temperature of the activated carbon discharged from the outlet of the first adsorption tower 1 in real time according to the formulas (2), (3), (15), (16), so as to determine the working state of the first adsorption tower 1.

[0155] Example 1

[0156] As shown in Figure 3 and 4 , a device for determining the safety of an adsorption system, the device comprising a first adsorption tower 1, a desorption tower 2, a sintering flue gas pipeline L1 and a flue gas pipeline L2 after desulfurization. The sintering flue gas pipeline L1 is connected to the flue gas inlet of the first adsorption tower 1. The flue gas pipeline L2 after desulfurization is connected to the flue gas outlet of the first adsorption tower 1. The activated carbon outlet of the first adsorption tower 1 is connected to the activated carbon inlet of the desorption tower 2 through a conveying device. A hot nitrogen gas pipeline L3 is connected to the top distribution section 201 of the desorption tower 2. The device is characterized in that: a first temperature detecting device 301 is arranged in the top distribution section 201 of the desorption tower 2. A first flow detecting device 401 is arranged at the activated carbon inlet position of the desorption tower 2. A second flow detecting device 402 and a second temperature detecting device 302 are arranged on the hot nitrogen gas pipeline L3. A third flow detecting device 403, a third temperature detecting device 303 and a first SO2 concentration detecting device 501 are arranged on the sintering flue gas pipeline L1 and close to the flue gas inlet of the first adsorption tower 1. A fourth temperature detecting device 304 and a second SO2 concentration detecting device 502 are arranged on the flue gas pipeline L2 after desulfurization and close to the flue gas outlet of the first adsorption tower 1. A first mass detecting device 601 and a fifth temperature detecting device 305 are arranged at the activated carbon inlet position of the first adsorption tower 1. The device further comprises a timing element. The timing element is used to record the time when the flue gas enters and exits the first adsorption tower 1.

[0157] Example 2

[0158] Example 1 is repeated, except that the device further comprises a fourth flow detecting device 404 arranged on the flue gas pipeline L2 after desulfurization and close to the flue gas outlet of the first adsorption tower 1.

[0159] Example 3

[0160] Example 2 is repeated, except that the device further comprises a second mass detection device 602 arranged at the activated carbon outlet position of the first adsorption tower 2.

[0161] Example 4

[0162] As shown in Figure 5 Example 3 is repeated, except that the device further comprises a control system 7. The control system 7 is connected with the first temperature detection device 301, the second temperature detection device 302, the third temperature detection device 303, the fourth temperature detection device 304, the fifth temperature detection device 305, the first flow detection device 401, the second flow detection device 402, the third flow detection device 403, the fourth flow detection device 404, the first SO2 concentration detection device 501, the second SO2 concentration detection device 502, the first mass detection device 601, and the second mass detection device 602, and calculates the deviation degree of the actual temperature and the theoretical temperature of the activated carbon when it is discharged from the outlet of the first adsorption tower 1 in real time according to formulas (2), (3), (15), and (16), so as to judge the working state of the first adsorption tower 1.

[0163]

[0164] t4 = t1 + Δt… (3) ;

[0165]

[0166]

[0167] Example 5

[0168] As shown in Figure 1 A method for judging the safety of an adsorption system, the method comprising: conveying sintering flue gas to a first adsorption tower 1, activated carbon in the first adsorption tower 1 performing desulfurization treatment on the sintering flue gas, flue gas after the desulfurization treatment being discharged from a flue gas outlet of the first adsorption tower 1, and activated carbon after absorbing pollutants being discharged from an activated carbon outlet of the first adsorption tower 1 and then entering a stripping tower 2 for heating and regeneration. In a top distribution section 201 of the stripping tower 2, activated carbon entering the stripping tower 2 exchanges heat with hot nitrogen gas introduced into the top of the stripping tower 2, the activated carbon is heated by the hot nitrogen gas and its temperature rises, and the temperature of the hot nitrogen gas decreases. According to the principle of heat balance, the temperature of the activated carbon when it enters the stripping tower 2 is calculated by detecting the temperature of the hot nitrogen gas and the activated carbon after the heat exchange is completed, and the temperature of the activated carbon when it is discharged from the outlet of the first adsorption tower 1 is converted, so as to judge the working state of the first adsorption tower 1.

[0169] Example 6

[0170] As shown in Figure 2 Example 1 is repeated, except that judging the working state of the first adsorption tower 1 specifically comprises the following steps:

[0171] 1) According to the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas being equal in the top distribution section 201 of the desorption tower 2, the actual temperature of the activated carbon entering the inlet of the desorption tower 2 is calculated.

[0172] 2) According to the temperature drop of the activated carbon during the transportation between the primary adsorption tower 1 and the desorption tower 2, the actual temperature of the activated carbon entering the inlet of the desorption tower 2 calculated in step 1) is converted into the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1.

[0173] 3) According to the heat generated in the primary adsorption tower 1 and the heat consumed and discharged by the primary adsorption tower 1 being equal, the theoretical temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 is calculated.

[0174] 4) The working state of the primary adsorption tower 1 is judged by comparing the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 with the theoretical temperature.

[0175] Example 7

[0176] Example 2 is repeated, except that step 1) is specifically: a first temperature detection device 301 is arranged in the top distribution section 201 of the desorption tower 2, and the first temperature detection device 301 detects the temperature t3, ℃ of the activated carbon after the heat exchange with the hot nitrogen gas is completed. According to the heat balance principle, the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas are equal during the heat exchange. That is:

[0177] m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1)。

[0178] That is:

[0179]

[0180] In the formula: t1 is the actual temperature of the activated carbon entering the inlet of the desorption tower, ℃. m1 is the amount of the activated carbon entering the desorption tower per unit time, kg / h. c p1 is the specific heat capacity of the activated carbon, kJ / (kg·℃). q1 is the flow of the hot nitrogen gas introduced into the top of the desorption tower per unit time, Nm 3 / h. ρ1 is the density of nitrogen, kg / Nm 3 . c p2 is the specific heat capacity of nitrogen, kJ / (kg·℃). t2 is the initial temperature of the hot nitrogen gas introduced into the top of the desorption tower, ℃. t3 is the temperature of the activated carbon and the nitrogen gas after the heat exchange is completed, ℃.

[0181] Step 2) is specifically: the temperature drop of the activated carbon during the transportation between the primary adsorption tower 1 and the desorption tower 2 is Δt, ℃. Therefore, the actual temperature of the activated carbon discharging from the outlet of the primary adsorption tower 1 is:

[0182] t4 = t1 + At … (3).

[0183] Wherein: t4 is the actual temperature of the activated carbon at the outlet of the primary adsorption tower, ℃.

[0184] In step 3), the heat generated in the primary adsorption tower 1 is equal to the heat consumed and discharged by the primary adsorption tower 1, specifically:

[0185] 301) Calculate the heat generated in the primary adsorption tower 1: the heat generated in the primary adsorption tower 1 Q 入 Including the heat Q1 brought in by the sintering flue gas into the primary adsorption tower 1, the heat Q2 released by the desulfurization reaction, the heat Q f That is:

[0186] Q 入 = Q 1+ Q 2+ Q f … (4).

[0187] 302) Calculate the heat consumed and discharged by the primary adsorption tower 1: the heat consumed and discharged by the primary adsorption tower 1 Q 出 Including the heat Q3 taken out by the flue gas after desulfurization discharging from the primary adsorption tower 1, the heat Qc taken out by the activated carbon discharging from the primary adsorption tower 1, the heat loss Q5. That is:

[0188] Q 出 = Q3 + Qc + Q5.

[0189] Since the heat Qc taken out by the activated carbon discharging from the primary adsorption tower 1 is the sum of the heat Q f And the heat Q4 absorbed by the activated carbon in the primary adsorption tower 1. That is:

[0190] Qc = Q f + Q4.

[0191] That is:

[0192] Q 出 = Q 3+ Q 4+ Q f+ Q5… (5).

[0193] 303) According to the principle of heat balance, the heat generated in the primary adsorption tower 1 is equal to the heat consumed and discharged by the primary adsorption tower 1. That is:

[0194] Q 1+ Q 2+ Q f = Q3+ Q 4+ Q f+ Q5…(6)。

[0195] Formula (6) can be simplified as: Q 1+ Q2=Q 3+ Q 4+ Q5…(7)。

[0196] In the heat consumed and discharged by the primary adsorption tower 1, the heat loss Q5≈0, and thus formula (7) can be simplified as:

[0197] Q 1+ Q2=Q 3+ Q4…(8)。

[0198] In step 3), according to formula (8), the theoretical temperature of the activated carbon discharged from the outlet of the primary adsorption tower 1 is calculated, specifically:

[0199] The heat Q1 brought in by the sintering flue gas entering the primary adsorption tower 1 is calculated:

[0200]

[0201] In the formula: Q1 is the heat brought in by the sintering flue gas entering the primary adsorption tower, kJ. q2 is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower, L / h. c p3 is the specific heat capacity of the flue gas, kJ / (mol·℃). v m is the standard molar volume, L / mol. t5 is the temperature of the sintering flue gas at the inlet of the primary adsorption tower, ℃. t0 is the temperature reference value, generally taken as 25℃. T0 is the initial time when the sintering flue gas enters the primary adsorption tower, h. T1 is the end time when the sintering flue gas enters the primary adsorption tower, h.

[0202] The heat Q2 released by the desulfurization reaction is calculated:

[0203]

[0204] In the formula: Q2 is the heat released by the desulfurization reaction, kJ. q2 is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower, L / h. C0 is the SO2 concentration at the inlet of the primary adsorption tower, g / L. C1 is the SO2 concentration at the outlet of the primary adsorption tower, g / L. M is the molar mass of SO2, g / mol. H is the heat released by the generation of 1 mol of sulfuric acid, kJ / mol. T0 is the initial time when the sintering flue gas enters the primary adsorption tower, h. T1 is the end time when the sintering flue gas enters the primary adsorption tower, h.

[0205] The heat Q3 brought out by the desulfurized flue gas discharged from the primary adsorption tower 1 is calculated:

[0206]

[0207] Q3 = q2 · c · (t6 - t0) … (7).

[0208] wherein: Q3 is the heat taken out by the desulfurized flue gas when it is discharged from the first-stage adsorption tower, kJ. q2 is the flue gas flow rate at the outlet of the first-stage adsorption tower, L / h. c p3 is the specific heat capacity of the flue gas, kJ / (mol·℃). v m is the standard molar volume, L / mol. t6 is the temperature of the desulfurized flue gas at the outlet of the first-stage adsorption tower, ℃. t0 is the temperature reference value, ℃. T0 + δT is the initial time when the desulfurized flue gas is discharged from the first-stage adsorption tower, h. T1 + δT is the end time when the desulfurized flue gas is discharged from the first-stage adsorption tower, h.

[0209] The heat Q4 absorbed by the activated carbon in the first-stage adsorption tower 1 is calculated as follows:

[0210] Q4 = m2 · c p1 · (t'4 - t7) … (13).

[0211] wherein: Q4 is the heat absorbed by the activated carbon in the first-stage adsorption tower, kJ. m2 is the loading mass of the activated carbon in the first-stage adsorption tower, kg. c p1 is the specific heat capacity of the activated carbon, kJ / (kg·℃). t7 is the temperature of the activated carbon when it enters the inlet of the first-stage adsorption tower, ℃. t'4 is the theoretical temperature of the activated carbon when it is discharged from the outlet of the first-stage adsorption tower 1, ℃.

[0212] According to formula (8), the theoretical temperature t'4 of the activated carbon when it is discharged from the outlet of the first-stage adsorption tower 1 is calculated, i.e.:

[0213]

[0214] wherein, the flow rate q2 of the sintering flue gas at the inlet of the first-stage adsorption tower 1 is consistent with the flow rate q3 of the desulfurized flue gas at the outlet of the first-stage adsorption tower 1, q2 ≈ q3 = q. Thus, we have:

[0215]

[0216] Step 4) is specifically: calculating the deviation Z of the actual temperature t4 of the activated carbon when it is discharged from the outlet of the first-stage adsorption tower 1 and the theoretical temperature t'4. Thus, we have:

[0217]

[0218] When Z is less than or equal to 10%, it indicates that the temperature of the activated carbon discharged from the first-stage adsorption tower 1 is within the normal temperature range after the adsorption desulfurization treatment, and the adsorption system is running normally.

[0219] On the contrary, it indicates that the temperature of the activated carbon discharged from the first adsorption tower 1 exceeds the fluctuation range of the normal temperature, i.e., the working state of the first adsorption tower 1 is abnormal, at this time, the system is stopped to check to ensure the safety and stability of the system.

[0220] Example 8

[0221] Example 7 is repeated, except that when Z is less than or equal to 8%, it indicates that after the adsorption desulfurization treatment, the temperature of the activated carbon discharged from the first adsorption tower 1 is within the normal temperature range, and the adsorption system is running normally.

[0222] On the contrary, it indicates that the temperature of the activated carbon discharged from the first adsorption tower 1 exceeds the fluctuation range of the normal temperature, i.e., the working state of the first adsorption tower 1 is abnormal, at this time, the system is stopped to check to ensure the safety and stability of the system.

[0223] Example 9

[0224] Example 7 is repeated, except that when Z is less than or equal to 5%, it indicates that after the adsorption desulfurization treatment, the temperature of the activated carbon discharged from the first adsorption tower 1 is within the normal temperature range, and the adsorption system is running normally.

[0225] On the contrary, it indicates that the temperature of the activated carbon discharged from the first adsorption tower 1 exceeds the fluctuation range of the normal temperature, i.e., the working state of the first adsorption tower 1 is abnormal, at this time, the system is stopped to check to ensure the safety and stability of the system.

[0226] Application Example 1

[0227] The method described in Example 7 is applied to a certain steel plant, and the safety of the adsorption system is judged, which specifically includes the following steps:

[0228] 1) According to the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas in the top distribution section 201 of the desorption tower 2, the actual temperature of the activated carbon entering the inlet of the desorption tower 2 is calculated.

[0229] A first temperature detection device 301 is arranged in the top distribution section 201 of the desorption tower 2, and the first temperature detection device 301 detects the temperature t3=90℃ of the activated carbon after heat exchange with the hot nitrogen gas. According to the heat balance principle, the heat absorbed by the activated carbon is equal to the heat released by the hot nitrogen gas during the heat exchange. That is:

[0230] m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1)。

[0231] That is:

[0232]

[0233] wherein: t1 is the actual temperature of the activated carbon entering the desorption tower inlet, ℃. m1 is the amount of activated carbon entering the desorption tower per unit time, m1 = 3000 kg / h. c p1 is the specific heat capacity of the activated carbon, c p1 = 0.95 kJ / (kg·℃). q1 is the flow rate of the hot nitrogen gas introduced at the top of the desorption tower per unit time, q1 = 380 Nm 3 / h. ρ1 is the density of nitrogen gas, ρ1 = 1.25 kg / Nm 3 . c p2 is the specific heat capacity of nitrogen gas, c p2 = 1.039 kJ / (kg·℃). t2 is the initial temperature of the hot nitrogen gas introduced at the top of the desorption tower, t2 = 120 ℃. t3 is the temperature of the activated carbon and nitrogen gas after heat exchange is completed, ℃.

[0234] 2) According to the temperature drop of the activated carbon during transportation between the primary adsorption tower 1 and the desorption tower 2, the actual temperature of the activated carbon entering the desorption tower 2 inlet calculated in step 1) is converted into the actual temperature of the activated carbon exiting the primary adsorption tower 1 outlet.

[0235] The temperature drop of the activated carbon during transportation between the primary adsorption tower 1 and the desorption tower 2 is Δt = 55 ℃. Thus, the actual temperature of the activated carbon exiting the primary adsorption tower 1 outlet is:

[0236] t4 = t1 + Δt = 139.81 ℃ … (3).

[0237] wherein: t4 is the actual temperature of the activated carbon exiting the primary adsorption tower outlet, ℃.

[0238] 3) According to the heat generated in the primary adsorption tower 1 being equal to the heat consumed and discharged by the primary adsorption tower 1, the theoretical temperature of the activated carbon exiting the primary adsorption tower 1 outlet is calculated.

[0239] According to the heat balance principle, the theoretical temperature of the activated carbon exiting the primary adsorption tower 1 outlet derived in Example 7 is:

[0240]

[0241] wherein: t'4 is the theoretical temperature of the activated carbon at the outlet of the first adsorption tower, ℃. q is the flow rate of the sintering flue gas at the inlet of the first adsorption tower, q = 1600000000 L / h. C0 is the SO2 concentration at the inlet of the first adsorption tower, C0 = 0.0006 g / L. C1 is the SO2 concentration at the outlet of the first adsorption tower, C1 = 0.00001 g / L. t5 is the temperature of the sintering flue gas at the inlet of the first adsorption tower, t5 = 141 ℃. t6 is the temperature of the flue gas after desulfurization at the outlet of the first adsorption tower, t6 = 140 ℃. m2 is the loading mass of the activated carbon in the first adsorption tower, m2 = 1200000 kg. t7 is the temperature of the activated carbon at the inlet of the first adsorption tower, t7 = 130 ℃. T0 is the initial time when the sintering flue gas enters the first adsorption tower, T0 is 0 h. T1 is the end time when the sintering flue gas enters the first adsorption tower, T1 is 1 h. p1 c is the specific heat capacity of the activated carbon, c p1 = 0.95 kJ / (kg·℃). p3 c is the specific heat capacity of the flue gas, c p3 = 0.03254 kJ / (mol·℃). H is the heat released for generating 1 mol of sulfuric acid, H = 275.3 kJ / mol. m v is the standard molar volume, v m = 22.4 L / mol. M is the molar mass of SO2, M = 64 g / mol.

[0242] 4) Comparing the actual temperature of the activated carbon at the outlet of the first adsorption tower 1 with the theoretical temperature, the working state of the first adsorption tower 1 is judged.

[0243] The deviation Z of the actual temperature t4 of the activated carbon at the outlet of the first adsorption tower 1 from the theoretical temperature t'4 is calculated. That is:

[0244]

[0245] Obviously, the deviation Z < 10%, which indicates that the temperature of the activated carbon discharged from the first adsorption tower 1 at this time is within the normal temperature range after the adsorption desulfurization treatment, and the adsorption system is running normally.

[0246] Application Example 2

[0247] The method described in Example 7 is applied to another steel plant, and the safety of the adsorption system is judged, specifically comprising the following steps:

[0248] 1) According to the fact that the heat absorbed by the activated carbon and the heat released by the hot nitrogen gas are equal in the top distribution section 201 of the stripping tower 2, the actual temperature of the activated carbon at the inlet of the stripping tower 2 is calculated.

[0249] A first temperature detecting device 301 is arranged in the top distribution section 201 of the desorption tower 2, and detects the temperature t3 of the activated carbon after heat exchange with the hot nitrogen gas, which is 108℃. According to the heat balance principle, the heat absorbed by the activated carbon is equal to the heat released by the hot nitrogen gas during the heat exchange. That is,

[0250] m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1)。

[0251] That is,

[0252]

[0253] In the formula, t1 is the actual temperature of the activated carbon entering the desorption tower, ℃. m1 is the amount of the activated carbon entering the desorption tower per unit time, m1 = 3000 kg / h. c p1 is the specific heat capacity of the activated carbon, c p1 = 0.95 kJ / (kg·℃). q1 is the flow of the hot nitrogen gas introduced into the top of the desorption tower per unit time, q1 = 380 Nm 3 / h. ρ1 is the density of the nitrogen gas, ρ1 = 1.25 kg / Nm 3 . c p2 is the specific heat capacity of the nitrogen gas, c p2 = 1.039 kJ / (kg·℃). t2 is the initial temperature of the hot nitrogen gas introduced into the top of the desorption tower, t2 = 120℃. t3 is the temperature of the activated carbon after the heat exchange, ℃.

[0254] 2) According to the temperature drop of the activated carbon during the transportation between the primary adsorption tower 1 and the desorption tower 2, the actual temperature of the activated carbon entering the desorption tower 2 calculated in step 1) is converted into the actual temperature of the activated carbon discharged from the primary adsorption tower 1.

[0255] The temperature drop of the activated carbon during the transportation between the primary adsorption tower 1 and the desorption tower 2 is Δt = 62℃. Therefore, the actual temperature of the activated carbon discharged from the primary adsorption tower 1 is:

[0256] t4 = t1 + Δt = 167.92℃…(3).

[0257] In the formula, t4 is the actual temperature of the activated carbon discharged from the primary adsorption tower 1, ℃.

[0258] 3) According to the heat generated in the primary adsorption tower 1 and the heat consumed and discharged by the primary adsorption tower 1, the theoretical temperature of the activated carbon discharged from the primary adsorption tower 1 is calculated.

[0259] According to the heat balance principle, the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower 1 is derived from Example 7 as follows:

[0260]

[0261] In the formula, t'4 is the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower, in ℃. q is the flow rate of the sintering flue gas at the inlet of the first-stage adsorption tower, q = 1000000000 L / h. C0 is the SO2 concentration at the inlet of the first-stage adsorption tower, C0 = 0.0006 g / L. C1 is the SO2 concentration at the outlet of the first-stage adsorption tower, C1 = 0.00001 g / L. t5 is the temperature of the sintering flue gas at the inlet of the first-stage adsorption tower, t5 = 141 ℃. t6 is the temperature of the flue gas after desulfurization at the outlet of the first-stage adsorption tower, t6 = 140 ℃. m2 is the loading mass of the activated carbon in the first-stage adsorption tower, m2 = 800000 kg. t7 is the temperature of the activated carbon entering the inlet of the first-stage adsorption tower, t7 = 136 ℃. T0 is the initial time when the sintering flue gas enters the first-stage adsorption tower, T0 is 0 h. T1 is the end time when the sintering flue gas enters the first-stage adsorption tower, T1 is 1 h.c p1 c is the specific heat capacity of the activated carbon, c p1 = 0.95 kJ / (kg·℃).c p3 c is the specific heat capacity of the flue gas, c p3 = 0.03254 kJ / (mol·℃). H is the heat released for generating 1 mol of sulfuric acid, H = 275.3 kJ / mol.v m v is the standard molar volume, v m = 22.4 L / mol. M is the molar mass of SO2, M = 64 g / mol.

[0262] 4) Comparing the actual temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower 1 with the theoretical temperature, the working state of the first-stage adsorption tower 1 is determined.

[0263] The deviation Z of the actual temperature t4 of the activated carbon discharged from the outlet of the first-stage adsorption tower 1 from the theoretical temperature t'4 is calculated. That is,

[0264]

[0265] Since the deviation Z > 10%, it is indicated that the temperature of the activated carbon discharged from the first-stage adsorption tower 1 exceeds the fluctuation range of the normal temperature, that is, the working state of the first-stage adsorption tower 1 is abnormal, and at this time, the system is stopped for inspection to ensure the safety and stability of the system.

Claims

1. A method for determining the safety of an adsorption system, the method comprising: The sintering flue gas is transported to the primary adsorption tower (1). The activated carbon in the primary adsorption tower (1) desulfurizes the sintering flue gas. The desulfurized flue gas is discharged from the flue gas outlet of the primary adsorption tower (1). The activated carbon that has adsorbed pollutants is discharged from the activated carbon outlet of the primary adsorption tower (1) and then enters the desorption tower (2) for heating and regeneration. The feature is that: in the top distribution section (201) of the desorption tower (2), the activated carbon entering the desorption tower (2) exchanges heat with the hot nitrogen gas introduced at the top of the desorption tower (2). The activated carbon is heated by the hot nitrogen gas and its temperature rises, while the temperature of the hot nitrogen gas decreases. Based on the principle of heat balance, the temperature of the activated carbon entering the desorption tower (2) is calculated by detecting the temperature after the hot nitrogen gas and the activated carbon have exchanged heat. The temperature of the activated carbon when it exits the primary adsorption tower (1) is then calculated, thereby determining the working state of the primary adsorption tower (1). The determination of the working state of the primary adsorption tower (1) specifically includes the following steps: 1) Based on the fact that the heat absorbed by the activated carbon and the heat released by the hot nitrogen are equal in the top distribution section (201) of the desorption tower (2), calculate the actual temperature of the activated carbon when it enters the inlet of the desorption tower (2). 2) Based on the temperature drop of activated carbon during transport between the primary adsorption tower (1) and the desorption tower (2), the actual temperature of activated carbon entering the inlet of the desorption tower (2) calculated in step 1) is converted into the actual temperature of activated carbon exiting the outlet of the primary adsorption tower (1). 3) Calculate the theoretical temperature at which activated carbon is discharged from the outlet of the first-stage adsorption tower (1) based on the fact that the heat generated in the first-stage adsorption tower (1) is equal to the heat consumed and discharged by the first-stage adsorption tower (1). 4) Compare the actual temperature of activated carbon discharged from the outlet of the primary adsorption tower (1) with the theoretical temperature to determine the working status of the primary adsorption tower (1).

2. The method according to claim 1, characterized in that: Step 1) Specifically: A first temperature detection device (301) is installed in the top distribution section (201) of the analytical tower (2). The first temperature detection device (301) detects the temperature t3, °C, after the heat exchange between the activated carbon and the hot nitrogen is completed. According to the principle of heat balance, during the heat exchange process, the heat absorbed by the activated carbon is equal to the heat released by the hot nitrogen. That is: m1*c p1 *(t3-t1)=q1*ρ1*c p2 *(t2-t3)…(1); That is, we get: In the formula: t1 is the actual temperature of the activated carbon when it enters the inlet of the stripping tower, in °C; m1 is the amount of activated carbon entering the stripping tower per unit time, in kg / h; c p1 q1 is the specific heat capacity of activated carbon, kJ / (kg·℃); q1 is the flow rate of hot nitrogen gas introduced into the top of the desorption tower per unit time, Nm³. 3 / h; ρ1 is the density of nitrogen gas, kg / Nm³ 3 ;c p2 t1 is the specific heat capacity of nitrogen, kJ / (kg·℃); t2 is the initial temperature of the hot nitrogen introduced at the top of the desorption tower, ℃; t3 is the temperature of the activated carbon and nitrogen after heat exchange, ℃.

3. The method according to claim 2, characterized in that: Step 2) specifically involves: the temperature drop during the transport of activated carbon between the primary adsorption tower (1) and the desorption tower (2) is Δt, °C; therefore, the actual temperature at which the activated carbon exits the primary adsorption tower (1) is: t4=t1+Δt…(3); In the formula: t4 is the actual temperature at which the activated carbon is discharged from the outlet of the primary adsorption tower, in °C.

4. The method according to claim 3, characterized in that: In step 3), the heat generated in the primary adsorption tower (1) is equal to the heat consumed and discharged by the primary adsorption tower (1), specifically: 301) Calculate the heat generated in the first-stage adsorption tower (1): The heat Q generated in the first-stage adsorption tower (1) 入 This includes the heat Q1 brought in by the sintering flue gas entering the primary adsorption tower (1), the heat Q2 released by the desulfurization reaction, and the heat Q brought in by the activated carbon entering the primary adsorption tower (1). f That is: Q 入 =Q1+Q2+Q f …(4); 302) Calculate the heat consumed and discharged by the first-stage adsorption tower (1): The heat consumed and discharged by the first-stage adsorption tower (1) Q 出 This includes the heat Q3 carried out by the flue gas after desulfurization exiting the primary adsorption tower (1), the heat Qc carried out by the activated carbon exiting the primary adsorption tower (1), and the heat loss Q5; that is: Q 出 =Q 3+ Qc + Q5; The heat Qc carried out by the activated carbon exiting the primary adsorption tower (1) is equal to the heat Q carried in by the activated carbon entering the primary adsorption tower (1). f The sum of the heat Q4 absorbed by the activated carbon in the primary adsorption tower (1); That is: Qc=Q f +Q4; That is, we get: Q 出 =Q3+Q4+Q f+ Q5…(5); 303) According to the principle of heat balance, the heat generated in the first-stage adsorption tower (1) is equal to the heat consumed and discharged by the first-stage adsorption tower (1); that is: Q 1+ Q 2+ Q f =Q 3+ Q 4+ Q f+ Q5…(6); Formula (6) can be simplified to: Q 1+ Q2 = Q 3+ Q 4+ Q5…(7); Of the heat consumed and discharged by the first-stage adsorption tower (1), the heat loss Q5≈0. Therefore, formula (7) can be simplified to: Q 1+ Q2=Q 3+ Q4…(8)。 5. The method according to claim 4, characterized in that: In step 3), the theoretical temperature at which activated carbon exits the primary adsorption tower (1) is calculated according to formula (8), specifically: Calculate the heat Q1 carried by the sintering flue gas entering the primary adsorption tower (1): Where: Q1 is the heat carried by the sintering flue gas into the primary adsorption tower, kJ; q2 is the flow rate of the sintering flue gas at the inlet of the primary adsorption tower, L / h; c p3 V represents the specific heat capacity of the flue gas, in kJ / (mol·℃); v m t5 is the standard molar volume, L / mol; t5 is the temperature of the sintering flue gas at the inlet of the first-stage adsorption tower, °C; t0 is the temperature reference value, °C; T0 is the initial time when the sintering flue gas enters the first-stage adsorption tower, h; T1 is the final time when the sintering flue gas enters the first-stage adsorption tower, h. Calculate the heat Q2 released by the desulfurization reaction: In the formula: Q2 is the heat released by the desulfurization reaction, kJ; q2 is the flow rate of the sintering flue gas at the inlet of the first-stage adsorption tower, L / h; C0 is the SO2 concentration at the inlet of the first-stage adsorption tower, g / L; C1 is the SO2 concentration at the outlet of the first-stage adsorption tower, g / L; M is the molar mass of SO2, g / mol; H is the heat released by generating 1 mol of sulfuric acid, kJ / mol; T0 is the initial time when the sintering flue gas enters the first-stage adsorption tower, h; T1 is the final time when the sintering flue gas enters the first-stage adsorption tower, h. Calculate the heat Q3 carried out by the flue gas after desulfurization from the primary adsorption tower (1): That is, we get: Where: Q3 is the heat carried out by the flue gas after desulfurization at the first-stage adsorption tower, kJ; q2 is the flue gas flow rate at the outlet of the first-stage adsorption tower, L / h; c p3 V represents the specific heat capacity of the flue gas, in kJ / (mol·℃); v m t6 is the standard molar volume, L / mol; t6 is the temperature of the desulfurized flue gas at the outlet of the first-stage adsorption tower, °C; t0 is the temperature reference value, °C; T0+δT is the initial time when the desulfurized flue gas exits the first-stage adsorption tower, h; T1+δT is the final time when the desulfurized flue gas exits the first-stage adsorption tower, h. Calculate the heat Q4 absorbed by the activated carbon in the primary adsorption tower (1): Q4=m2·c p1 ·(t’4-t7)…(13); In the formula: Q4 is the heat absorbed by the activated carbon in the primary adsorption tower, kJ; m2 is the mass of activated carbon packed in the primary adsorption tower, kg; c p1 t7 is the specific heat capacity of activated carbon, kJ / (kg·℃); t7 is the temperature of activated carbon entering the inlet of the primary adsorption tower, ℃; t′4 is the theoretical temperature of activated carbon exiting the outlet of the primary adsorption tower (1), ℃. According to formula (8), the theoretical temperature t′4 at the outlet of the primary adsorption tower (1) when the activated carbon is discharged is calculated, that is: Among them, the flow rate q2 of the sintering flue gas at the flue gas inlet of the first-stage adsorption tower (1) is the same as the flow rate q3 of the desulfurized flue gas at the flue gas outlet of the first-stage adsorption tower (1), q2≈q3=q; that is:

6. The method according to claim 5, characterized in that: Step 4) specifically involves calculating the deviation Z between the actual temperature t4 and the theoretical temperature t′4 when the activated carbon is discharged from the outlet of the primary adsorption tower (1); that is: When Z is less than or equal to 10%, it means that after the adsorption desulfurization treatment, the temperature of the activated carbon discharged from the first-stage adsorption tower (1) is within the normal temperature range, and the adsorption system is operating normally. Conversely, if the temperature of the activated carbon discharged from the primary adsorption tower (1) exceeds the normal temperature fluctuation range, it means that the working state of the primary adsorption tower (1) is abnormal. At this time, the operating conditions of the primary adsorption tower (1) should be adjusted or the tower should be shut down for inspection to ensure the safety and stability of the system.

7. The method according to claim 6, characterized in that: When Z is less than or equal to 8%, it means that after the adsorption desulfurization treatment, the temperature of the activated carbon discharged from the first-stage adsorption tower (1) is within the normal temperature range, and the adsorption system is operating normally; otherwise, it means that the temperature of the activated carbon discharged from the first-stage adsorption tower (1) exceeds the normal temperature fluctuation range.

8. The method according to claim 7, characterized in that: When Z is less than or equal to 5%, it means that after the adsorption desulfurization treatment, the temperature of the activated carbon discharged from the first-stage adsorption tower (1) is within the normal temperature range, and the adsorption system is operating normally; otherwise, it means that the temperature of the activated carbon discharged from the first-stage adsorption tower (1) exceeds the normal temperature fluctuation range.

9. An apparatus for determining the safety of an adsorption system using the method described in any one of claims 1-8, the apparatus comprising a primary adsorption tower (1), a desorption tower (2), a sintering flue gas duct (L1), and a desulfurized flue gas duct (L2); the sintering flue gas duct (L1) is connected to the flue gas inlet of the primary adsorption tower (1); the desulfurized flue gas duct (L2) is connected to the flue gas outlet of the primary adsorption tower (1); the activated carbon outlet of the primary adsorption tower (1) is connected to the activated carbon inlet of the desorption tower (2) via a conveying device; a hot nitrogen duct (L3) is connected to the top distribution section (201) of the desorption tower (2); characterized in that: A first temperature detection device (301) is provided in the top distribution section (201) of the desorption tower (2); a first flow detection device (401) is provided at the activated carbon inlet of the desorption tower (2); a second flow detection device (402) and a second temperature detection device (302) are provided on the hot nitrogen pipeline (L3); a third flow detection device (403), a third temperature detection device (303), and a first SO2 concentration detection device (501) are provided on the sintering flue gas pipeline (L1) near the flue gas inlet of the first-stage adsorption tower (1); a fourth temperature detection device (304) and a second SO2 concentration detection device (502) are provided on the desulfurized flue gas pipeline (L2) near the flue gas outlet of the first-stage adsorption tower (1); a first mass detection device (601) and a fifth temperature detection device (305) are provided at the activated carbon inlet of the first-stage adsorption tower (1); the device also includes a timing element; the timing element is used to record the time when the flue gas enters and exits the first-stage adsorption tower (1).

10. The apparatus according to claim 9, characterized in that: The device also includes a fourth flow detection device (404) installed on the flue gas duct (L2) after desulfurization and near the flue gas outlet of the primary adsorption tower (1); and / or The device also includes a second quality detection device (602) located at the activated carbon outlet of the primary adsorption tower (1).

11. The apparatus according to claim 9 or 10, characterized in that: The device also includes a control system (7); the control system (7) is connected to the first temperature detection device (301), the second temperature detection device (302), the third temperature detection device (303), the fourth temperature detection device (304), the fifth temperature detection device (305), the first flow detection device (401), the second flow detection device (402), the third flow detection device (403), the fourth flow detection device (404), the first SO2 concentration detection device (501), the second SO2 concentration detection device (502), the first mass detection device (601), and the second mass detection device (602), and calculates the deviation between the actual temperature and the theoretical temperature of the activated carbon discharged from the outlet of the first-stage adsorption tower (1) in real time according to formulas (2), (3), (15), and (16), thereby determining the working status of the first-stage adsorption tower (1).

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