Preheating and control method, device and equipment for activated carbon in storage bin of adsorption tower

Abstract

The invention relates to the technical field of denitration, and discloses a preheating and control method, device and equipment for activated carbon in an adsorption tower bin. The method comprises the following steps: calculating first heat of activated carbon in a stock bin, second heat brought by flue gas entering the stock bin, third heat released by denitration reaction in an adsorption tower, and fourth heat brought by original flue gas entering a denitration area of the adsorption tower; calculating a first temperature when the active carbon in the stock bin enters the adsorption tower and a second temperature of the active carbon in the denitration area according to the four heat quantities; and the first temperature and the second temperature are judged, and the flow of the smoke entering the stock bin is controlled according to the judgment result. The flue gas preheats the activated carbon in the stock bin through the bypass flue, the purified flue gas is reasonably utilized for preheating, the opening degree of the bypass valve is regulated and controlled according to the first temperature and the second temperature so as to regulate the flow of the flue gas entering the stock bin, the temperature of the activated carbon entering an adsorption area is stabilized in a proper temperature interval of denitration reaction, the denitration effect and efficiency are improved, and the energy consumption is reduced. Meanwhile, the safety of the denitration and desulfurization system is ensured.

Description

Technical Field

[0001] The present invention relates to the technical field of denitration, and in particular to a method, device and equipment for preheating and controlling activated carbon in an adsorption tower silo. Background Art

[0002] Activated carbon desulfurization and denitrification technology includes two steps: adsorption of pollutants and desorption and regeneration of activated carbon. After the activated carbon has completed the adsorption of nitrogen oxides and sulfur dioxide in the adsorption tower, it enters the desorption tower, is regenerated and then circulated back to the activated carbon silo at the top of the adsorption tower. At this time, the temperature of the activated carbon is reduced to 60-70°C, and in the adsorption zone of the activated carbon system, the suitable temperature of the denitrification reaction in the denitrification zone is higher than that in the desulfurization zone. The suitable temperature for the adsorption of NOx by activated carbon is 100-150°C. Therefore, after the activated carbon enters the denitrification zone from the silo, its temperature cannot quickly reach the suitable temperature for the denitrification reaction, thereby affecting the denitrification efficiency. At the same time, due to the denitrification reaction in the denitrification zone, a large amount of chemical reaction heat is released, which can easily cause the temperature of the activated carbon in the tower to rise, and the ignition point temperature of powdered activated carbon is about 160°C. Therefore, during the desulfurization and denitrification process, the temperature in the denitrification zone of the adsorption tower must be kept within a safe range.

[0003] The temperature of activated carbon in the adsorption tower is an important factor that determines the desulfurization and denitrification effects. The flue gas and activated carbon are in countercurrent contact. The original flue gas first enters the desulfurization zone. After desulfurization, the flue gas combines with ammonia water in the ammonia injection zone and enters the denitrification zone. Since the optimal temperature for the denitrification reaction is generally around 130°C, the activated carbon first enters the denitrification zone from the top silo of the adsorption tower after regeneration and circulation. At this time, the activated carbon temperature has not reached the appropriate denitrification reaction temperature, and the NOx removal effect is poor. Summary of the invention

[0004] In view of this, the present invention provides a preheating and control method, device and equipment for activated carbon in an adsorption tower silo to solve the problem of poor denitrification effect caused by low temperature in the existing denitrification zone.

[0005] In a first aspect, the present invention provides a preheating and control method for activated carbon in an adsorption tower silo, wherein the adsorption tower comprises a bypass flue and a bypass valve, wherein the bypass flue is used to allow purified flue gas to enter the silo to heat the activated carbon in the silo, and the bypass valve is used to control the flow rate of the purified flue gas entering the silo;

[0006] Methods include:

[0007] Calculate the first heat of activated carbon in the silo, the second heat brought by the flue gas after purification into the silo, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought by the original flue gas before purification into the denitration zone of the adsorption tower;

[0008] According to the first heat, the second heat, the third heat, and the fourth heat, the first temperature of the activated carbon in the silo when entering the adsorption tower and the second temperature of the activated carbon in the denitration area of ​​the adsorption tower are calculated respectively;

[0009] The first temperature and the second temperature are judged by using a preset judgment model, and the flow rate of the purified flue gas entering the silo is controlled according to the judgment result.

[0010] The preheating and control method of activated carbon in the adsorption tower silo provided by the present invention utilizes the purified flue gas for preheating to heat the activated carbon in the silo through a bypass flue, effectively and reasonably utilizes the purified flue gas for preheating, and regulates the opening of the bypass valve by the activated carbon temperature in the silo and the activated carbon temperature in the denitration zone of the adsorption tower to adjust the flue gas flow entering the silo, so that the temperature of the activated carbon is stabilized in a suitable temperature range for the denitration reaction when entering the adsorption zone, thereby improving the denitration effect and efficiency, and ensuring the safety of the denitration and desulfurization system.

[0011] In an optional embodiment, calculating the first heat of activated carbon in the silo includes:

[0012] Obtain the temperature of activated carbon when it circulates into the silo, the mass of activated carbon in the silo, and the specific heat capacity of activated carbon;

[0013] According to the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat capacity of the activated carbon, the first heat of the activated carbon in the silo is calculated using the heat calculation formula.

[0014] In an optional embodiment, calculating the second heat brought into the silo by the purified flue gas includes:

[0015] Obtain the flow rate and density of the smoke at the smoke inlet of the silo, and determine the mass of the smoke entering the silo per unit time based on the flow rate and density of the smoke at the smoke inlet of the silo;

[0016] Obtain the time the flue gas stays in the adsorption tower, the quality of the flue gas entering the silo per unit time, the temperature of the flue gas at the silo inlet, the temperature of the flue gas at the silo outlet, and the specific heat capacity of the flue gas;

[0017] According to the time the flue gas stays in the adsorption tower, the mass of flue gas entering the silo per unit time, the temperature of the flue gas at the silo flue gas inlet, the temperature of the flue gas at the silo outlet and the specific heat capacity of the flue gas, the second heat brought into the silo by the purified flue gas after entering the silo is calculated using the heat calculation formula.

[0018] The preheating and control method of activated carbon in the adsorption tower silo provided by the present invention detects parameters such as flue gas temperature, flow, density, and mass at relevant positions. The parameter detection is simple and easy to obtain. The first heat of the activated carbon in the silo and the second heat brought into the silo by the purified flue gas after entering the silo are calculated using a heat calculation formula, so as to accurately grasp the heat at different positions and improve the control accuracy of the temperature in the denitrification zone.

[0019] In an optional implementation, the calculation formula of the third heat includes:

[0020] Q 3 =q 2 ×(c 0 -c 1 )×△H(t 3 -t 2 ) / M 0

[0021] Among them, q 2 is the flow rate of the original flue gas at the flue gas inlet of the denitrification zone of the adsorption tower; c 0 is the concentration of nitrogen oxides at the flue gas inlet of the denitrification zone of the adsorption tower; c 1 is the concentration of nitrogen oxides at the flue gas outlet of the denitrification zone of the adsorption tower; △H is the chemical reaction heat of reducing 1 mol of nitrogen monoxide; t 2 is the initial time when the original flue gas enters the denitrification zone of the adsorption tower; t 3 M is the final moment when the original flue gas enters the denitrification zone of the adsorption tower; 0 is the molar mass of nitric oxide.

[0022] In an optional embodiment, calculating the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification includes:

[0023] Obtain the original flue gas flow rate, original flue gas density, and original flue gas thermometer at the flue gas inlet of the denitrification zone of the adsorption tower, and the flue gas temperature at the flue gas outlet of the denitrification zone of the adsorption tower;

[0024] According to the specific heat capacity of flue gas, the original flue gas flow rate at the flue gas inlet of the adsorption tower denitrification zone, the original flue gas density, and the flue gas temperature at the flue gas outlet of the adsorption tower denitrification zone through the original flue gas thermometer, the fourth heat brought into the denitrification zone of the adsorption tower by the original flue gas before purification is calculated using the heat calculation formula.

[0025] The preheating and control method of activated carbon in the adsorption tower silo provided by the present invention accurately calculates the total heat in the denitration process by calculating the third heat released by the denitration reaction of the adsorption tower and the fourth heat brought into the denitration zone of the original flue gas entering the adsorption tower, which is convenient for accurately calculating and controlling the denitration temperature and improving the denitration efficiency.

[0026] In an optional embodiment, the first temperature of the activated carbon in the silo when entering the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower are calculated according to the first heat, the second heat, the third heat, and the fourth heat, respectively, including:

[0027] Obtain the mass of activated carbon in the silo;

[0028] According to the heat balance principle, the first temperature of the activated carbon in the silo when it enters the adsorption tower is calculated using the first heat, the second heat, and the mass of the activated carbon in the silo;

[0029] Obtain the activated carbon mass in the denitrification zone of the adsorption tower and the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower;

[0030] According to the principle of heat balance, the second temperature of the activated carbon in the denitrification zone of the adsorption tower is calculated using the first heat, the second heat, the third heat, the fourth heat, the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower, and the mass of activated carbon in the denitrification zone of the adsorption tower.

[0031] The preheating and control method of activated carbon in the adsorption tower silo provided by the present invention utilizes the heat at four positions to calculate the temperature of the activated carbon in the adsorption tower and the temperature of the activated carbon in the denitrification zone, thereby avoiding combustion of the activated carbon due to excessive temperature, and at the same time ensuring that the temperature in the denitrification zone is maintained at a suitable temperature for denitrification, thereby improving the denitrification efficiency.

[0032] In an optional implementation, the first temperature and the second temperature are judged by using a preset judgment model, and the flow rate of the purified flue gas entering the silo is controlled according to the judgment result, including:

[0033] If the first temperature is less than the lower limit of the preset temperature range, the increase in the flow rate of the purified flue gas entering the silo is determined according to the difference between the first temperature and the lower limit of the preset temperature range;

[0034] If the second temperature is greater than the upper limit of the preset temperature range, the flow reduction of the purified flue gas entering the silo is determined according to the difference between the second temperature and the upper limit of the preset temperature range;

[0035] The bypass valve opening is controlled according to the increase or decrease in the flow rate of the purified flue gas entering the silo.

[0036] The preheating and control method of activated carbon in the adsorption tower silo provided by the present invention uses a preset judgment model to judge the activated carbon temperature in the silo and the activated carbon temperature in the denitrification zone, and controls the flue gas flow entering the silo according to the judgment result, accurately controlling the two temperatures within a reasonable range, thereby ensuring production safety and improving denitrification efficiency.

[0037] In a second aspect, the present invention provides a preheating and control device for activated carbon in an adsorption tower silo, wherein the adsorption tower comprises a bypass flue and a bypass valve, wherein the bypass flue is used to allow the purified flue gas to enter the silo to heat the activated carbon in the silo, and the bypass valve is used to control the flow rate of the purified flue gas entering the silo; the device comprises:

[0038] The heat calculation module is used to calculate the first heat of the activated carbon in the silo, the second heat brought into the silo by the flue gas after purification, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification;

[0039] A temperature calculation module, used to calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower according to the first heat, the second heat, the third heat, and the fourth heat;

[0040] The flow control module is used to judge the first temperature and the second temperature using a preset judgment model, and control the flow of the purified flue gas entering the silo according to the judgment result.

[0041] In a third aspect, the present invention provides a computer device, comprising: a memory and a processor, the memory and the processor being communicatively connected to each other, the memory storing computer instructions, and the processor executing the method of the first aspect or any corresponding embodiment thereof by executing the computer instructions.

[0042] In a fourth aspect, the present invention provides a computer-readable storage medium having computer instructions stored thereon, the computer instructions being used to cause a computer to execute the method of the first aspect or any corresponding embodiment thereof. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0044] Figure 1 It is a schematic flow chart of a method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention;

[0045] Figure 2 2 is a schematic diagram of the structure of an adsorption tower in a method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention;

[0046] Figure 3 It is a schematic flow chart of another method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention;

[0047] Figure 4 is a structural block diagram of a preheating and control device for activated carbon in an adsorption tower silo according to an embodiment of the present invention;

[0048] Figure 5 It is a schematic diagram of the hardware structure of a computer device according to an embodiment of the present invention. DETAILED DESCRIPTION

[0049] In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative work are within the scope of protection of the present invention.

[0050] An embodiment of the present invention provides a preheating and control method for activated carbon in an adsorption tower silo, which uses purified flue gas preheating through a bypass flue to heat the activated carbon in the silo, and controls the temperature of the activated carbon in the silo and the temperature of the denitrification zone according to the flue gas flow rate, so as to ensure safety while improving the denitrification efficiency.

[0051] During the operation of the activated carbon desulfurization and denitrification system, flue gas purification is mainly achieved through the adsorption of activated carbon, and the operation of the activated carbon in the adsorption tower directly determines the effect of desulfurization and denitrification of the process. The existing countercurrent activated carbon desulfurization and denitrification adsorption tower adopts a vertical structure as a whole. The desulfurization bed and denitrification bed are arranged from bottom to top inside the adsorption tower. The activated carbon enters the adsorption tower from the opening of the activated carbon silo at the top of the adsorption tower and is discharged through the opening at the bottom of the adsorption tower; the flue gas to be treated is introduced through the bottom of the adsorption tower and rises to the top of the adsorption tower in the adsorption tower. The entire system is an integrated desulfurization and denitrification technology. The activated carbon adsorbed with sulfur dioxide and nitrogen oxides enters the regeneration tower through circulation for desorption and regeneration. After the adsorption performance is restored, it enters the adsorption tower through the conveying device. In the adsorption tower, the activated carbon first enters the silo at the top of the tower, and enters the denitrification and desulfurization adsorption modules in turn through the control of the discharge valve. After the activated carbon enters the adsorption module, it is mainly heated by the original flue gas. The heating rate of the activated carbon is slow and the denitrification efficiency is low.

[0052] According to an embodiment of the present invention, an embodiment of a method for preheating and controlling activated carbon in an adsorption tower silo is provided. It should be noted that the steps shown in the flowchart of the accompanying drawings can be executed in a computer system such as a set of computer executable instructions, and although a logical order is shown in the flowchart, in some cases, the steps shown or described may be executed in an order different from that shown here.

[0053] In this embodiment, a method for preheating and controlling activated carbon in an adsorption tower silo is provided, which can be used in the above-mentioned computer system. Figure 1 It is a structural schematic diagram of an adsorption tower in a method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention. In this embodiment, a bypass flue and a bypass valve are added on the basis of the existing structure of the adsorption tower. The bypass flue is used to allow purified flue gas to enter the silo, and the purified flue gas is used to heat the activated carbon in the silo. The bypass valve is used to control the flow rate of purified flue gas entering the silo.

[0054] Figure 2 is a flow chart of a method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention, such as Figure 2 As shown, the process includes the following steps:

[0055] Step S101, calculate the first heat of the activated carbon in the silo, the second heat brought into the silo by the flue gas after purification, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification.

[0056] Specifically, the factors affecting the temperature of the denitration reaction in the denitration zone of the adsorption tower include: the heat brought in by the activated carbon when it enters the adsorption tower from the silo, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought in by the original flue gas entering the denitration zone of the adsorption tower before purification. These three parts of heat ultimately affect the temperature of the denitration zone when the denitration reaction is carried out. Therefore, it is necessary to calculate these three parts of heat, but because the temperature of the activated carbon directly returned to the silo from the desorption tower is relatively low, a bypass flue is added, and the activated carbon in the silo is preheated in advance with the purified flue gas to increase its temperature. Therefore, the heat brought in by the activated carbon when entering the adsorption tower from the silo includes two parts: one part is the first heat of the activated carbon itself when it returns to the silo from the desorption tower, and the other part is the second heat brought in by the purified flue gas entering the silo. For the convenience of calculation, the first heat and the second heat are calculated separately.

[0057] Step S102, calculating the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower according to the first heat, the second heat, the third heat, and the fourth heat.

[0058] Specifically, since the suitable temperature for activated carbon to adsorb NOx is 100℃-150℃, and the ignition point temperature of powdered activated carbon is around 160℃, in order to ensure that the activated carbon has the best denitration effect when performing denitration reaction in the denitration zone, and the activated carbon will not burn during the whole process, it is necessary to monitor the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower at the same time. The temperature calculation process can be calculated based on the first heat, the second heat, the third heat, and the fourth heat using the heat balance principle.

[0059] Step S103, using a preset judgment model to judge the first temperature and the second temperature, and controlling the flow rate of the purified flue gas entering the silo according to the judgment result.

[0060] Specifically, the preset judgment model is a suitable temperature range of the first temperature and a suitable temperature range of the second temperature determined based on experience. When the adsorption tower is performing denitrification and desulfurization, the first temperature and the second temperature are detected in real time, and the first temperature and the second temperature are judged. The bypass valve is adjusted according to the judgment result to control the flow rate of the purified flue gas entering the silo, change the second heat brought into the silo by the purified flue gas, and then realize the adjustment of the first temperature and the second temperature, so that the first temperature and the second temperature are maintained within the suitable temperature range.

[0061] The present embodiment provides a method for preheating and controlling activated carbon in an adsorption tower silo, which utilizes purified flue gas preheating to heat the activated carbon in the silo through a bypass flue, effectively and reasonably utilizes the purified flue gas preheating, and regulates the opening of the bypass valve by the activated carbon temperature in the silo and the activated carbon temperature in the denitrification zone of the adsorption tower to adjust the flue gas flow entering the silo, so that the temperature of the activated carbon entering the adsorption zone is stabilized in a suitable temperature range for the denitrification reaction, thereby improving the denitrification effect and efficiency, while ensuring the safety of the denitrification and desulfurization system.

[0062] In this embodiment, a preheating and control method for activated carbon in an adsorption tower silo is provided, which can be used in the above-mentioned computer system. The adsorption tower includes: a bypass flue and a bypass valve. The bypass flue is used to allow the purified flue gas to enter the silo to heat the activated carbon in the silo. The bypass valve is used to control the flow rate of the purified flue gas entering the silo. Figure 3 is a flow chart of a method for preheating and controlling activated carbon in an adsorption tower silo according to an embodiment of the present invention, such as Figure 3 As shown, the process includes the following steps:

[0063] Step S201, calculate the first heat of the activated carbon in the silo, the second heat brought into the silo by the flue gas after purification, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification.

[0064] Specifically, the above step S201 includes:

[0065] Step S2011, obtaining the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat of the activated carbon; according to the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat of the activated carbon, the first heat of the activated carbon in the silo is calculated using a heat calculation formula.

[0066] Specifically, a temperature sensor can be installed at an appropriate position at the entrance of the activated carbon into the silo to collect the temperature of the activated carbon when it circulates into the silo. The temperature values ​​in this embodiment can be collected by installing a temperature sensor at an appropriate position, and the mass of the activated carbon in the silo can be collected by installing a mass sensor at an appropriate position in the silo. This is only an example, but not limited to this. The specific heat capacity of activated carbon can be obtained through experiments, using the heat calculation formula: heat = mass × specific heat capacity × temperature. The calculation formula for calculating the first heat of the activated carbon in the silo is:

[0067] Q 1 =1000×C 1 ×M 1 ×T 1 ······ (1)

[0068] Among them, Q 1 Indicates the first heat, the unit is kJ; C 1 Indicates the specific heat capacity of activated carbon, in kJ / (kg·℃); M 1 is the mass of activated carbon in the silo, in t; T 1 It is the initial temperature of the activated carbon recycled from the regeneration tower to the silo, in °C.

[0069] Step S2012, obtain the flow rate and density of the flue gas at the flue gas inlet of the silo, and determine the mass of the flue gas entering the silo per unit time based on the flow rate and density of the flue gas at the flue gas inlet of the silo; obtain the time the flue gas stays in the adsorption tower, the mass of the flue gas entering the silo per unit time, the temperature of the flue gas at the flue gas inlet of the silo, the temperature of the flue gas at the silo outlet and the specific heat of the flue gas; according to the time the flue gas stays in the adsorption tower, the mass of the flue gas entering the silo per unit time, the temperature of the flue gas at the flue gas inlet of the silo, the temperature of the flue gas at the silo outlet and the specific heat of the flue gas, use the heat calculation formula to calculate the second heat brought into the silo by the purified flue gas entering the silo.

[0070] Specifically, the flow rate, density, mass, temperature, time and other parameters can be collected by installing corresponding sensors at appropriate locations. The collection method is a mature technical means and will not be repeated here. The formula for calculating the second heat brought into the silo by the purified flue gas using the heat calculation formula is:

[0071] Q 2 =C 2 ×(t 1 -t 0 )×q 1 ×ρ 1 ×(T 2 -T 3 ) ······ (2)

[0072] Among them, Q 2Indicates the second heat, the unit is kJ; C 2 is the specific heat capacity of flue gas, in kJ / (kg·℃); t 0 is the initial time when the original flue gas enters the activated carbon silo, in h; t 1 It is the final moment when the original flue gas enters the activated carbon silo, in h; q 1 is the flue gas flow rate at the flue gas inlet of the activated carbon silo, in Nm 3 / h;ρ 1 is the density of flue gas at the flue gas inlet of activated carbon silo, in kg / m 3 ; T 2 T is the temperature of the flue gas at the silo flue gas inlet, in °C; 3 It is the temperature of the flue gas at the silo flue gas outlet, in ℃.

[0073] Step S2013, the calculation formula of the third heat includes:

[0074] Q 3 =q 2 ×(c 0 -c 1 )×△H(t 3 -t 2 ) / M 0 ······ (3)

[0075] Among them, Q 3 Indicates the third heat, the unit is kJ; q 2 The original flue gas flow rate at the flue gas inlet of the denitrification zone of the adsorption tower, in Nm 3 / h;c 0 NOx is the concentration of nitrogen oxides at the flue gas inlet of the denitrification zone of the adsorption tower, in mg / Nm 3 ;c 1 NOx is the concentration of nitrogen oxides at the flue gas outlet of the denitrification zone of the adsorption tower, in mg / Nm 3 ; △H is the chemical reaction heat of reducing 1 mol of nitric oxide, in kJ / mol; t 2 is the initial time when the original flue gas enters the denitrification zone of the adsorption tower, in h; t 3 It is the final moment when the original flue gas enters the denitrification zone of the adsorption tower, in h; M 0 is the molar mass of nitric oxide NO, in g / mol.

[0076] Specifically, since more than 90% of the NOx in the sintering flue gas is NO, the chemical reaction heat of the reduction reaction of NO and ammonia is used to represent the denitration reaction heat. The chemical reaction formula of the reaction of NO and ammonia is:

[0077] 4NH 3 +4NO+O 2=4N 2 +6H 2 O. Calculating reaction heat using chemical reaction formula is a mature existing technology and will not be described in detail here.

[0078] Step S2014, obtaining the original flue gas flow rate, original flue gas density, original flue gas thermometer and flue gas temperature at the flue gas outlet of the denitrification zone of the adsorption tower; according to the specific heat capacity of the flue gas, the original flue gas flow rate, original flue gas density and original flue gas thermometer at the flue gas outlet of the denitrification zone of the adsorption tower, the fourth heat brought into the denitrification zone of the adsorption tower before purification by the original flue gas entering the denitrification zone of the adsorption tower is calculated using the heat calculation formula.

[0079] Specifically, the heat calculation formula is used to calculate the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification:

[0080] Q 4 =C 2 ×(t 3 -t 2 )×q 3 ×ρ 2 ×(T 5 -T 4 ) ······ (4)

[0081] Among them, Q 4 Indicates the fourth heat, the unit is kJ; C 2 is the specific heat capacity of flue gas, in kJ / (kg·℃); q 3 The original flue gas flow rate at the flue gas inlet of the denitrification zone of the adsorption tower, in Nm 3 / h;ρ 2 It is the density of flue gas at the flue gas inlet of the denitrification zone of the adsorption tower, in kg / m 3 ; T 4 T is the temperature of the original flue gas entering the denitrification zone of the adsorption tower, in °C; 5 It is the flue gas temperature at the outlet of the denitrification zone of the adsorption tower, in °C.

[0082] The preheating and control method of activated carbon in the adsorption tower silo provided in this embodiment detects the flue gas temperature, flow rate, density, mass and other parameters at relevant positions. The parameter detection is simple and easy to obtain. The heat calculation formula is used to calculate the first heat of the activated carbon in the silo and the second heat brought into the silo by the purified flue gas, accurately grasp the heat at different positions, and improve the control accuracy of the temperature in the denitration zone. By calculating the third heat released by the denitration reaction of the adsorption tower and the fourth heat brought into the denitration zone of the original flue gas entering the adsorption tower, the total heat in the denitration process is accurately calculated, which is convenient for accurately calculating and controlling the denitration temperature and improving the denitration efficiency.

[0083] Step S202, calculating the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower respectively according to the first heat, the second heat, the third heat, and the fourth heat;

[0084] Specifically, the above step S202 includes:

[0085] Step S2021, obtaining the mass of activated carbon in the silo.

[0086] Specifically, the quality of the activated carbon in the silo can be collected by installing a quality sensor at an appropriate position in the silo, which is only an example but not limited to this.

[0087] Step S2022, according to the heat balance principle, using the first heat, the second heat, and the mass of the activated carbon in the silo, calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower.

[0088] Specifically, the temperature of the activated carbon in the silo when it enters the adsorption tower is calculated based on the principle of heat balance. The formula is as follows:

[0089] T 炭0 =(Q 1 +Q 2 ) / (C 1 ×M 1 ) ······ (5)

[0090] Among them, T 炭0 It indicates the temperature of the activated carbon in the silo when it enters the adsorption tower, in °C; Q 1 Indicates the first heat, the unit is kJ; Q 2 Indicates the second heat, the unit is kJ; C 1 Indicates the specific heat capacity of activated carbon, in kJ / (kg·℃); M 1 It indicates the mass of activated carbon in the silo, in t.

[0091] Step S2023, obtaining the mass of activated carbon in the denitration zone of the adsorption tower and the concentration of nitrogen oxides at the flue gas outlet of the denitration zone of the adsorption tower.

[0092] Specifically, the mass of activated carbon in the denitrification zone of the adsorption tower can be indirectly determined by measuring the change in the mass of activated carbon in the adsorption tower silo. The nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower can be collected by installing a concentration sensor at an appropriate position at the outlet. This is only an example, but not limited to this.

[0093] Step S2024, according to the principle of heat balance, uses the first heat, the second heat, the third heat, the fourth heat, the nitrogen oxide concentration at the flue gas outlet of the adsorption tower denitrification zone, and the mass of activated carbon in the adsorption tower denitrification zone to calculate the second temperature of the activated carbon in the adsorption tower denitrification zone.

[0094] Specifically, according to the heat balance principle, the calculation formula for calculating the second temperature of the activated carbon in the denitration zone of the adsorption tower is:

[0095] T 炭1 =(Q 1 +Q 2 +Q 3 +Q 4 ) / (C 1 ×M 2 ) ······ (6)

[0096] Among them, M 2 It is the mass of activated carbon in the denitrification area of ​​the adsorption tower, unit is t.

[0097] Substituting formula (1)-formula (4) into formula (6) we can get T 炭1 The final expression of is:

[0098]

[0099] The preheating and control method of activated carbon in the adsorption tower silo provided in this embodiment uses the heat at four positions to calculate the temperature of the activated carbon in the adsorption tower and the temperature of the activated carbon in the denitrification zone, thereby avoiding combustion of the activated carbon due to excessive temperature, while ensuring that the temperature in the denitrification zone is maintained at a suitable temperature for denitrification, thereby improving the denitrification efficiency.

[0100] Step S203, using a preset judgment model to judge the first temperature and the second temperature, and controlling the flow rate of the purified flue gas entering the silo according to the judgment result.

[0101] Specifically, the above step S203 includes:

[0102] Step S2031, if the first temperature is less than the lower limit of the preset temperature range, the increase in the flow rate of the purified flue gas entering the silo is determined according to the difference between the first temperature and the lower limit of the preset temperature range.

[0103] Specifically, the preset temperature range may be a suitable temperature (100-150°C) for activated carbon to adsorb NOx. If the first temperature of the activated carbon in the silo when entering the adsorption tower is less than the lower limit of the preset temperature range (T 炭0<100℃), it means that the temperature of the activated carbon in the silo is too low. At this time, it is necessary to increase the opening of the bypass valve of the bypass flue and increase the flow rate of the purified flue gas entering the silo to increase the preheating temperature of the flue gas on the activated carbon. The opening adjustment amount of the bypass valve directly affects the increase in the flow rate of the flue gas entering the silo, so it can be determined how much the temperature of the activated carbon in the silo needs to be increased based on the difference between the first temperature and the lower limit of the preset temperature range. The increase in the flow rate of the flue gas is determined based on the correspondence between the temperature of the activated carbon in the silo and the flow rate of the flue gas entering the silo, and then the opening of the bypass valve is controlled based on the increase in flow rate. The correspondence between the temperature of the activated carbon in the silo and the flow rate of the flue gas entering the silo can be determined based on historical experience, as an example only, but not limited to this.

[0104] Step S2032: If the second temperature is greater than the upper limit of the preset temperature range, the flow reduction of the purified flue gas entering the silo is determined according to the difference between the second temperature and the upper limit of the preset temperature range.

[0105] Specifically, if the second temperature of the activated carbon in the denitration zone of the adsorption tower is greater than the upper limit of the preset temperature range (T 炭1 >150℃), indicating that the temperature rise of activated carbon in the adsorption tower is abnormal, which may cause the activated carbon to burn in the adsorption tower. It is necessary to reduce the opening of the bypass valve to reduce the flow of flue gas entering the silo, reduce the preheating of the flue gas on the activated carbon in the silo, and reduce the temperature of the activated carbon in the silo. According to the operating status of the adsorption tower, it may be necessary to adjust the operating conditions of the adsorption tower to ensure safe and stable operation.

[0106] It should be noted that the bypass valve opening is the main factor affecting the flow rate of flue gas entering the silo, and the flow rate of flue gas entering the silo is the main factor affecting the degree of preheating of the activated carbon in the silo by the flue gas, so the first temperature of the activated carbon in the silo when entering the adsorption tower can be indirectly adjusted by controlling the bypass valve opening. In practical applications, the reduction in the flow rate of the flue gas entering the silo after purification can be determined based on the difference between the second temperature and the upper limit of the preset temperature range, combined with the corresponding relationship between the temperature of the activated carbon in the silo and the flow rate of the flue gas entering the silo, and then the opening adjustment amount of the bypass valve can be determined based on the reduction in the flow rate of the flue gas entering the silo.

[0107] If the first temperature of the activated carbon in the silo when entering the adsorption tower is greater than the lower limit of the preset temperature range (T 炭0 >100℃), the second temperature of the activated carbon in the denitration zone of the adsorption tower is further judged. If the second temperature is less than the upper limit of the preset temperature range (T 炭1 <150℃), it means that the activated carbon temperature in the denitrification area is within the normal range, which not only meets the efficient denitrification reaction, but also does not have the safety hazard of activated carbon combustion. The adsorption tower can continue to desulfurize and denitrify normally without adjusting the bypass valve.

[0108] Step S2033, controlling the opening of the bypass valve according to the increase or decrease in the flow rate of the purified flue gas entering the silo.

[0109] Specifically, the flow rate of the flue gas entering the silo after purification is proportional to the opening of the bypass valve. The larger the opening of the bypass valve, the greater the flow rate of the flue gas entering the silo. Therefore, the opening of the bypass valve can be controlled according to the increase or decrease in the flow rate of the flue gas entering the silo after purification.

[0110] The preheating and control method of activated carbon in the adsorption tower silo provided in this embodiment uses a preset judgment model to judge the activated carbon temperature in the silo and the activated carbon temperature in the denitrification zone, and controls the flue gas flow entering the silo according to the judgment result, accurately controlling the two temperatures within a reasonable range, thereby ensuring production safety and improving denitrification efficiency.

[0111] In a specific embodiment, the specific heat capacity C of the activated carbon is 1 is 0.84 kJ / (kg·℃); the mass of activated carbon in the silo is M 1 is 1000t; the initial temperature of the activated carbon recycled from the regeneration tower to the silo is T 1 The temperature is 60℃. According to formula (1), the heat Q contained in the activated carbon in the silo is calculated. 1 =50400000kJ.

[0112] Specific heat capacity of flue gas C 2 is 0.97 kJ / (kg·℃); the initial time t when the original flue gas enters the first-stage adsorption tower 0 is 0h; the final time when the original flue gas enters the first-stage adsorption tower is t 1 is 1h; the flue gas flow rate q at the flue gas inlet of the activated carbon silo 1 1 million Nm 3 / h; density of flue gas at the flue gas inlet of activated carbon silo ρ 1 2.23kg / m 3 ; Temperature of flue gas at the silo flue gas inlet T 2 is 110℃; the temperature of the flue gas at the silo flue gas outlet is T 3 The temperature is 95℃. According to formula (2), the heat Q brought into the activated carbon silo by the flue gas after purification is calculated as 2 =32446500kJ.

[0113] The original flue gas flow rate q at the flue gas inlet of the adsorption tower denitrification zone 2 2 million Nm 3 / h; NOx concentration at the flue gas inlet of the denitrification zone of the adsorption tower c 0 300mg / Nm 3 ; NOx concentration at the flue gas outlet of the adsorption tower denitrification zone c 1 30mg / Nm3 ; The chemical reaction heat △H of reducing 1 mol NO is 317.25 kJ / mol. The initial time t when the original flue gas enters the denitrification zone of the adsorption tower 2 0h; the final time when the original flue gas enters the denitrification zone of the adsorption tower is t 3 is 1h; the molar mass of NO is M 0 is 30 g / mol, and the heat Q released by the denitration reaction in the adsorption tower is calculated according to formula (3): 3 =5710500kJ.

[0114] Specific heat capacity of flue gas C 2 is 0.97 kJ / (kg·℃); the original flue gas flow rate q at the flue gas inlet of the denitrification zone of the adsorption tower 3 2 million Nm 3 / h; density of flue gas at the flue gas inlet of the denitrification zone of the adsorption tower ρ 2 2.23kg / m 3 ; The temperature of the original flue gas entering the denitrification zone of the adsorption tower T 4 is 120℃; the flue gas temperature at the outlet of the denitrification zone of the adsorption tower is T 5 The temperature is 110℃. According to formula (4), the heat Q brought into the denitrification zone of the adsorption tower by the original flue gas is calculated as 4 =43262000kJ.

[0115] According to formula (5), the temperature T of the activated carbon in the silo when it enters the adsorption tower is calculated. 炭0 =98.63℃, T is obtained by the preset judgment model 炭0 <100℃, then the flow rate q of the flue gas at the flue gas inlet of the activated carbon silo is increased by increasing the opening of the bypass valve 1 , increase the preheating temperature of the activated carbon in the silo.

[0116] In another specific embodiment, based on the previous specific embodiment, the flow rate q of the flue gas at the flue gas inlet of the activated carbon silo is 1 1.2 million Nm 3 / h, calculate the temperature T of the activated carbon in the silo when it enters the adsorption tower 炭0 =106.35℃, T is obtained by the preset judgment model 炭0 >100℃, so it is necessary to further calculate the temperature T of the activated carbon in the denitrification zone of the adsorption tower according to formula (6): 炭1 =137.21℃, T is obtained by the preset judgment model 炭1 <150℃, indicating that the temperature of activated carbon in the denitrification zone of the adsorption tower is normal. The flow rate of flue gas at the flue gas inlet of the activated carbon silo is determined. The system operates normally and there is no need to adjust the opening of the bypass valve.

[0117] In another specific embodiment, based on the first specific embodiment, the flow rate q of the flue gas at the flue gas inlet of the activated carbon silo is 1 1.6 million Nm 3 / h, calculate the temperature T of the activated carbon in the silo when it enters the adsorption tower 炭0 =121.80℃, T is obtained by the preset judgment model 炭0 >100℃, so the temperature T of the activated carbon in the denitrification zone of the adsorption tower is calculated according to formula (6): 炭1 =150.09℃, T is obtained by the preset judgment model 炭1 >150℃, indicating that the temperature rise of activated carbon in the adsorption tower is abnormal. At this time, reduce the opening of the bypass flue valve and reduce the preheated flue gas volume q 1 , and at the same time adjust the operating conditions of the adsorption tower to ensure safe and stable operation of the system.

[0118] In yet another specific embodiment, the specific heat capacity C of the activated carbon 1 is 0.84 kJ / (kg·℃); the mass of activated carbon in the silo is M 1 is 1000t; the initial temperature of the activated carbon recycled from the regeneration tower to the silo is T 1 The temperature is 60℃. According to formula (1), the heat Q contained in the activated carbon in the silo is calculated. 1 =50400000kJ.

[0119] Specific heat capacity of flue gas C 2 is 0.97 kJ / (kg·℃); the initial time t when the original flue gas enters the first-stage adsorption tower 0 is 0h; the final time when the original flue gas enters the first-stage adsorption tower is t 1 is 1h; the flue gas flow rate q at the flue gas inlet of the activated carbon silo 1 1.5 million Nm 3 / h; density of flue gas at the flue gas inlet of activated carbon silo ρ 1 2.23kg / m 3 ; Temperature of flue gas at the silo flue gas inlet T 2 is 110℃; the temperature of the flue gas at the silo flue gas outlet is T 3 The temperature is 100℃. According to formula (2), the heat Q brought into the activated carbon silo by the flue gas after purification is calculated as 2 =48669750kJ.

[0120] The original flue gas flow rate q at the flue gas inlet of the adsorption tower denitrification zone 2 2 million Nm 3 / h; NOx concentration at the flue gas inlet of the denitrification zone of the adsorption tower c 0 300mg / Nm 3 ; NOx concentration at the flue gas outlet of the adsorption tower denitrification zone c 130mg / Nm 3 ; The chemical reaction heat △H of reducing 1 mol NO is 317.25 kJ / mol. The initial time t when the original flue gas enters the denitrification zone of the adsorption tower 2 0h; the final time when the original flue gas enters the denitrification zone of the adsorption tower is t 3 is 1h; the molar mass of NO is M 0 is 30 g / mol, and the heat Q released by the denitration reaction in the adsorption tower is calculated according to formula (3): 3 =5710500kJ.

[0121] Specific heat capacity of flue gas C 2 is 0.97 kJ / (kg·℃); the original flue gas flow rate q at the flue gas inlet of the denitrification zone of the adsorption tower 3 2 million Nm 3 / h; density of flue gas at the flue gas inlet of the denitrification zone of the adsorption tower ρ 2 2.23kg / m 3 ; The temperature of the original flue gas entering the denitrification zone of the adsorption tower T 4 is 120℃; the flue gas temperature at the outlet of the denitrification zone of the adsorption tower is T 5 The temperature is 110℃. According to formula (4), the heat Q brought into the denitrification zone of the adsorption tower by the original flue gas is calculated as 4 =43262000kJ.

[0122] According to formula (5), the temperature T of the activated carbon in the silo when it enters the adsorption tower is calculated. 炭0 =117.94℃, T is obtained by the preset judgment model 炭0 >100℃, so the temperature T of the activated carbon in the denitrification zone of the adsorption tower is calculated according to formula (6): 炭1 =146.87℃, T is obtained by the preset judgment model 炭1 <150℃, indicating that the temperature of activated carbon in the denitrification zone of the adsorption tower is normal. The flow rate of flue gas at the flue gas inlet of the activated carbon silo is determined. The system operates normally and there is no need to adjust the opening of the bypass valve.

[0123] In this embodiment, a preheating and control device for activated carbon in an adsorption tower silo is also provided, which is used to implement the above-mentioned embodiments and preferred embodiments, and will not be repeated hereafter. As used below, the term "module" can implement a combination of software and / or hardware for a predetermined function. Although the devices described in the following embodiments are preferably implemented in software, the implementation of hardware, or a combination of software and hardware, is also possible and conceivable.

[0124] This embodiment provides a preheating and control device for activated carbon in an adsorption tower silo. The adsorption tower includes a bypass flue and a bypass valve. The bypass flue is used to allow the purified flue gas to enter the silo to heat the activated carbon in the silo. The bypass valve is used to control the flow rate of the purified flue gas entering the silo. Figure 4 As shown, including:

[0125] The heat calculation module 401 is used to calculate the first heat of the activated carbon in the silo, the second heat brought into the silo by the flue gas after purification, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification.

[0126] The temperature calculation module 402 is used to calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower according to the first heat, the second heat, the third heat and the fourth heat.

[0127] The flow control module 403 is used to judge the first temperature and the second temperature by using a preset judgment model, and control the flow of the purified flue gas entering the silo according to the judgment result.

[0128] In some optional implementations, the heat calculation module 401 includes:

[0129] The first heat calculation unit is used to obtain the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat capacity of the activated carbon; according to the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat capacity of the activated carbon, the first heat of the activated carbon in the silo is calculated using a heat calculation formula.

[0130] The second heat calculation unit is used to obtain the flow rate and density of the smoke at the smoke inlet of the silo, and determine the mass of the smoke entering the silo per unit time according to the flow rate and density of the smoke at the smoke inlet of the silo; obtain the time the smoke stays in the adsorption tower, the mass of the smoke entering the silo per unit time, the temperature of the smoke at the smoke inlet of the silo, the temperature of the smoke at the silo outlet and the specific heat of the smoke; according to the time the smoke stays in the adsorption tower, the mass of the smoke entering the silo per unit time, the temperature of the smoke at the smoke inlet of the silo, the temperature of the smoke at the silo outlet and the specific heat of the smoke, use the heat calculation formula to calculate the second heat brought into the silo by the purified smoke entering the silo.

[0131] The third heat calculation unit, the calculation formula for the third heat includes:

[0132] Q 3 =q 2 ×(c 0 -c 1 )×△H(t 3 -t 2 ) / M 0 ······ (3)

[0133] Among them, Q 3 Indicates the third heat, the unit is kJ; q 2The original flue gas flow rate at the flue gas inlet of the denitrification zone of the adsorption tower, in Nm 3 / h;c 0 NOx is the concentration of nitrogen oxides at the flue gas inlet of the denitrification zone of the adsorption tower, in mg / Nm 3 ;c 1 NOx is the concentration of nitrogen oxides at the flue gas outlet of the denitrification zone of the adsorption tower, in mg / Nm 3 ; △H is the chemical reaction heat of reducing 1 mol of nitric oxide, in kJ / mol; t 2 is the initial time when the original flue gas enters the denitrification zone of the adsorption tower, in h; t 3 It is the final moment when the original flue gas enters the denitrification zone of the adsorption tower, in h; M 0 is the molar mass of nitric oxide NO, in g / mol.

[0134] The fourth heat calculation unit is used to obtain the original flue gas flow rate at the flue gas inlet of the adsorption tower denitrification zone, the original flue gas density, the original flue gas thermometer and the flue gas temperature at the flue gas outlet of the adsorption tower denitrification zone; according to the specific heat capacity of the flue gas, the original flue gas flow rate at the flue gas inlet of the adsorption tower denitrification zone, the original flue gas density, and the original flue gas thermometer and the flue gas temperature at the flue gas outlet of the adsorption tower denitrification zone, the fourth heat brought into the denitrification zone of the adsorption tower before purification is calculated using the heat calculation formula.

[0135] In some optional implementations, the temperature calculation module 402 includes:

[0136] The first parameter acquisition unit is used to obtain the mass of activated carbon in the silo and the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower.

[0137] The first temperature calculation unit is used to calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower according to the heat balance principle by using the first heat, the second heat, the mass of the activated carbon in the silo, and the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower.

[0138] The second parameter acquisition unit is used to obtain the mass of activated carbon in the denitration zone of the adsorption tower.

[0139] The second temperature calculation unit is used to calculate the second temperature of the activated carbon in the denitrification zone of the adsorption tower according to the principle of heat balance by using the first heat, the second heat, the third heat, the fourth heat, the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower, and the mass of activated carbon in the denitrification zone of the adsorption tower.

[0140] In some optional implementations, the flow control module 403 includes:

[0141] The flow increasing unit is used to determine the flow increase of the purified flue gas entering the silo according to the difference between the first temperature and the lower limit of the preset temperature range if the first temperature is lower than the lower limit of the preset temperature range.

[0142] The flow reduction unit is used to determine the flow reduction amount of the purified flue gas entering the silo according to the difference between the second temperature and the upper limit of the preset temperature range if the second temperature is greater than the upper limit of the preset temperature range.

[0143] The opening adjustment unit is used to control the opening of the bypass valve according to the increase or decrease in the flow rate of the purified flue gas entering the silo.

[0144] The further functional description of each of the above modules and units is the same as that of the above corresponding embodiments and will not be repeated here.

[0145] The preheating and control device for activated carbon in the adsorption tower silo in this embodiment is presented in the form of a functional unit, where the unit refers to an ASIC (Application Specific Integrated Circuit) circuit, a processor and memory that executes one or more software or fixed programs, and / or other devices that can provide the above functions.

[0146] The embodiment of the present invention also provides a computer device having the above Figure 4 The preheating and control device of activated carbon in the adsorption tower silo is shown.

[0147] See also Figure 5 , Figure 5 is a schematic diagram of the structure of a computer device provided by an optional embodiment of the present invention, such as Figure 5 As shown, the computer device includes: one or more processors 10, a memory 20, and interfaces for connecting various components, including high-speed interfaces and low-speed interfaces. Various components are connected to each other using different buses for communication, and can be installed on a common mainboard or installed in other ways as needed. The processor can process the instructions executed in the computer device, including instructions stored in or on the memory to display the graphical information of the GUI on an external input / output device (such as, a display device coupled to the interface). In some optional embodiments, if necessary, multiple processors and / or multiple buses can be used together with multiple memories and multiple memories. Similarly, multiple computer devices can be connected, and each device provides some necessary operations (for example, as a server array, a group of blade servers, or a multi-processor system). Figure 5 A processor 10 is taken as an example.

[0148] The processor 10 may be a central processing unit, a network processor or a combination thereof. The processor 10 may further include a hardware chip. The hardware chip may be a dedicated integrated circuit, a programmable logic device or a combination thereof. The programmable logic device may be a complex programmable logic device, a field programmable gate array, a general purpose array logic or any combination thereof.

[0149] The memory 20 stores instructions executable by at least one processor 10, so that the at least one processor 10 executes the method shown in the above embodiment.

[0150] The memory 20 may include a program storage area and a data storage area, wherein the program storage area may store an operating system, an application required for at least one function; the data storage area may store data created according to the use of the computer device, etc. In addition, the memory 20 may include a high-speed random access memory, and may also include a non-transient memory, such as at least one disk storage device, a flash memory device, or other non-transient solid-state storage device. In some optional embodiments, the memory 20 may optionally include a memory remotely arranged relative to the processor 10, and these remote memories may be connected to the computer device via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.

[0151] The memory 20 may include a volatile memory, such as a random access memory; the memory may also include a non-volatile memory, such as a flash memory, a hard disk or a solid state drive; the memory 20 may also include a combination of the above types of memory.

[0152] The computer device further comprises a communication interface 30 for the computer device to communicate with other devices or a communication network.

[0153] The embodiment of the present invention also provides a computer-readable storage medium. The method according to the embodiment of the present invention can be implemented in hardware, firmware, or can be implemented as a computer code that can be recorded in a storage medium, or can be implemented as a computer code that is originally stored in a remote storage medium or a non-temporary machine-readable storage medium and will be stored in a local storage medium through a network download, so that the method described herein can be stored in such software processing on a storage medium using a general-purpose computer, a dedicated processor, or programmable or dedicated hardware. Among them, the storage medium can be a magnetic disk, an optical disk, a read-only storage memory, a random access memory, a flash memory, a hard disk or a solid-state hard disk, etc.; further, the storage medium can also include a combination of the above types of memories. It can be understood that a computer, a processor, a microprocessor controller, or programmable hardware includes a storage component that can store or receive software or computer code. When the software or computer code is accessed and executed by a computer, a processor, or hardware, the method shown in the above embodiment is implemented.

[0154] Although the embodiments of the present invention have been described in conjunction with the accompanying drawings, those skilled in the art may make various modifications and variations without departing from the spirit and scope of the present invention, and such modifications and variations are all within the scope defined by the appended claims.

Claims

1. A method for preheating and controlling activated carbon in an adsorption tower silo, characterized in that: The adsorption tower includes a bypass flue and a bypass valve, wherein the bypass flue is used to allow the purified flue gas to enter the silo to heat the activated carbon in the silo, and the bypass valve is used to control the flow rate of the purified flue gas entering the silo; The method comprises: Calculate the first heat of activated carbon in the silo, the second heat brought by the flue gas after purification into the silo, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought by the original flue gas before purification into the denitration zone of the adsorption tower; According to the first heat, the second heat, the third heat, and the fourth heat, respectively calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower; The first temperature and the second temperature are judged using a preset judgment model, and the flow rate of the purified flue gas entering the silo is controlled according to the judgment result.

2. The method according to claim 1, characterized in that The calculating the first heat quantity of the activated carbon in the silo comprises: Obtain the temperature of activated carbon when it circulates into the silo, the mass of activated carbon in the silo, and the specific heat capacity of activated carbon; The first heat of the activated carbon in the silo is calculated using a heat calculation formula according to the temperature of the activated carbon when it circulates into the silo, the mass of the activated carbon in the silo, and the specific heat capacity of the activated carbon.

3. The method according to claim 2, characterized in that Calculate the second heat brought into the silo by the purified flue gas, including: Obtain the flow rate and density of the smoke at the smoke inlet of the silo, and determine the mass of the smoke entering the silo per unit time based on the flow rate and density of the smoke at the smoke inlet of the silo; Obtain the time the flue gas stays in the adsorption tower, the quality of the flue gas entering the silo per unit time, the temperature of the flue gas at the silo inlet, the temperature of the flue gas at the silo outlet, and the specific heat capacity of the flue gas; According to the time the flue gas stays in the adsorption tower, the mass of flue gas entering the silo per unit time, the temperature of the flue gas at the silo flue gas inlet, the temperature of the flue gas at the silo outlet and the specific heat capacity of the flue gas, the second heat brought into the silo by the purified flue gas after entering the silo is calculated using the heat calculation formula.

4. The method according to claim 3, characterized in that The third heat calculation formula include: Q3=q2×(c0-c1)×△H(t3-t2) / M0 Among them, q2 is the flow rate of the original flue gas at the flue gas inlet of the adsorption tower denitrification zone; c0 is the nitrogen oxide concentration at the flue gas inlet of the adsorption tower denitrification zone; c1 is the nitrogen oxide concentration at the flue gas outlet of the adsorption tower denitrification zone; △H is the chemical reaction heat of reducing 1 mol of nitric oxide; t2 is the initial moment when the original flue gas enters the denitrification zone of the adsorption tower; t3 is the final moment when the original flue gas enters the denitrification zone of the adsorption tower; M0 is the molar mass of nitric oxide.

5. The method according to claim 4, characterized in that Calculate the fourth heat brought into the denitrification zone of the adsorption tower by the original flue gas before purification, including: Obtain the original flue gas flow rate, original flue gas density, and original flue gas thermometer at the flue gas inlet of the denitrification zone of the adsorption tower, and the flue gas temperature at the flue gas outlet of the denitrification zone of the adsorption tower; According to the specific heat capacity of flue gas, the original flue gas flow rate at the flue gas inlet of the denitrification zone of the adsorption tower, the original flue gas density, and the flue gas temperature at the flue gas outlet of the denitrification zone of the adsorption tower measured by the original flue gas thermometer, the fourth heat brought into the denitrification zone of the adsorption tower by the original flue gas before purification is calculated using the heat calculation formula.

6. The method according to claim 5, characterized in that According to the first heat, the second heat, the third heat, and the fourth heat, the first temperature of the activated carbon in the silo when entering the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower are calculated respectively, including: Obtain the mass of activated carbon in the silo; According to the heat balance principle, the first temperature of the activated carbon in the silo when it enters the adsorption tower is calculated using the first heat, the second heat, and the mass of the activated carbon in the silo; Obtain the activated carbon mass in the denitrification zone of the adsorption tower and the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower; According to the principle of heat balance, the second temperature of the activated carbon in the denitrification zone of the adsorption tower is calculated using the first heat, the second heat, the third heat, the fourth heat, the nitrogen oxide concentration at the flue gas outlet of the denitrification zone of the adsorption tower, and the mass of activated carbon in the denitrification zone of the adsorption tower.

7. The method according to claim 1 or 6, characterized in that: The first temperature and the second temperature are judged by using a preset judgment model, and the flow rate of the purified flue gas entering the silo is controlled according to the judgment result, including: If the first temperature is less than the lower limit of the preset temperature range, the increase in the flow rate of the purified flue gas entering the silo is determined according to the difference between the first temperature and the lower limit of the preset temperature range; If the second temperature is greater than the upper limit of the preset temperature range, the flow reduction of the purified flue gas entering the silo is determined according to the difference between the second temperature and the upper limit of the preset temperature range; The opening of the bypass valve is controlled according to the increase or decrease in the flow rate of the purified flue gas entering the silo.

8. A preheating and control device for activated carbon in an adsorption tower silo, characterized in that: The adsorption tower includes a bypass flue and a bypass valve, wherein the bypass flue is used to allow the purified flue gas to enter the silo to heat the activated carbon in the silo, and the bypass valve is used to control the flow rate of the purified flue gas entering the silo; The device comprises: The heat calculation module is used to calculate the first heat of the activated carbon in the silo, the second heat brought into the silo by the flue gas after purification, the third heat released by the denitration reaction in the adsorption tower, and the fourth heat brought into the denitration zone of the adsorption tower by the original flue gas before purification; A temperature calculation module, used to calculate the first temperature of the activated carbon in the silo when it enters the adsorption tower and the second temperature of the activated carbon in the denitration zone of the adsorption tower according to the first heat, the second heat, the third heat, and the fourth heat; The flow control module is used to judge the first temperature and the second temperature by using a preset judgment model, and control the flow of the purified flue gas entering the silo according to the judgment result.

9. A computer device, characterized in that: include: A memory and a processor, wherein the memory and the processor are communicatively connected to each other, the memory stores computer instructions, and the processor executes the method according to any one of claims 1 to 7 by executing the computer instructions.

10. A computer-readable storage medium, characterized in that: The computer-readable storage medium stores computer instructions, and the computer instructions are used to enable a computer to execute the method according to any one of claims 1 to 7.

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