An optimized regulation method based on the combination of ammonia method and membrane absorption for desulfurization, and its applications, electronic devices and computer-readable storage media

Abstract

The present application discloses an optimized regulation method based on the combination of ammonia method and membrane absorption for desulfurization, and its application, electronic device, and computer-readable storage medium, belonging to the technical field of flue gas ammonia desulfurization. The method includes the steps of: (1) collecting the system state data within a period of time T before the current moment, where the system state data includes the content of sulfur dioxide in the discharged flue gas, the pH value of the desulfurization liquid in the absorption section, and the pH value of the desulfurization liquid in the concentration and cooling section, and calculating M1 and M2; (2) calculating the ammonia water dosage according to the following formula, the ammonia water dosage = L + △L, where △L is the ammonia water adjustment amount, with the unit of m<supgt;3< / supgt; / h: △L = (M1 - M2) / 0.1 + σ + γ; where σ is the temperature adjustment parameter, with the value range of 0.04 to 0.05, and γ is the ammonia adjustment parameter, with the value range of 0 to 0.5. This method is designed for the desulfurization process combining ammonia method and membrane absorption, optimizes the ammonia water dosage according to the collected sulfur content in the flue gas and the state parameters of the absorption circulating liquid, improves the desulfurization efficiency while reducing ammonia escape, and saves the operation cost of the desulfurization system.

Description

Technical Field

[0001] The present application relates to an optimized regulation method for desulfurization by combining ammonia method and membrane absorption, its application, an electronic device, and a computer-readable storage medium, belonging to the technical field of flue gas ammonia desulfurization. Background Art

[0002] Ammonia desulfurization is a currently commonly used flue gas desulfurization method, which has the advantages of high desulfurization efficiency, wide application range, etc. And ammonium sulfite generated during the desulfurization process undergoes a chemical reaction with oxygen in the introduced air in the oxidation section to generate ammonium sulfate, and then through concentration and crystallization, solid ammonium sulfate by-products are obtained. This by-product can also be used for the preparation of chemical fertilizers, enabling the effective utilization of resources.

[0003] The ammonia desulfurization technology has the disadvantages of large ammonia escape and serious aerosol phenomenon, thus hindering the popularization and use of the ammonia desulfurization technology. At present, the combination of membrane absorption and ammonia desulfurization methods can significantly reduce the consumption of ammonia water, and therefore can also reduce ammonia escape from the source.

[0004] The current ammonia desulfurization can control the ammonia water consumption through parameter settings, but it is only an optimization method for controlling the ammonia water consumption in a single ammonia desulfurization, and is not applicable to the desulfurization system combining membrane absorption and ammonia desulfurization. Therefore, there is an urgent need for an optimized regulation method for desulfurization combining membrane absorption and ammonia. Summary of the Invention

[0005] To solve the above problems, an optimized regulation method for desulfurization by combining ammonia method and membrane absorption is provided. This method is designed for the desulfurization process combining ammonia method and membrane absorption, and can optimize the ammonia water consumption according to the collected state parameters, improve the desulfurization efficiency while reducing ammonia escape, and save the operation cost of the desulfurization system.

[0006] According to one aspect of the present application, an optimized regulation method for desulfurization by combining ammonia method and membrane absorption is provided. The desulfurization system for desulfurization by combining ammonia method and membrane absorption includes a desulfurization tower, a concentration circulation tank, a crystallization tank, an ammonium sulfate product treatment mechanism, and a circulation water tank; the desulfurization tower is divided into a demisting section, a purification section, an absorption section, a concentration and cooling section, and an oxidation section from top to bottom. The concentration and cooling section and the absorption section are separated by a first partition, the absorption section and the purification section are separated by a second partition, and the oxidation section and the concentration and cooling section are separated by a third partition; above the absorption section, a primary demister, a second spraying mechanism, an absorption membrane, and a first packing layer are arranged from top to bottom. The first packing layer is arranged above the riser cap. The absorption membrane is a polypropylene absorption membrane. The second spraying mechanism is arranged above the absorption membrane. The second spraying mechanism is connected to the oxidation section through a circulation pump. The bottom of the absorption section is connected to the oxidation section through a reflux pipeline; specifically includes the following steps:

[0007] (1) Collect the system status data within a period T before the current moment. The system status data includes: the content of sulfur dioxide in the discharged flue gas, the pH value of the desulfurization liquid in the absorption section, and the pH value of the desulfurization liquid in the concentration and cooling section. Calculate M1 and M2. M1 is the change in the pH value of the desulfurization liquid in the absorption section when the flue gas index value changes by 1 mg / Nm³, and M2 is the change in the pH value of the desulfurization liquid in the concentration and cooling section when the flue gas index value changes by 1 mg / Nm³.

[0008] (2) Calculate the ammonia water dosage according to the following formula. The ammonia water dosage = L + △L, where △L is the ammonia water adjustment amount, and the unit is m 3 / h:

[0009] △L = (M1 - M2) / 0.1 + σ + γ;

[0010] Where σ is the temperature adjustment parameter, and its value range is 0.04 - 0.05. γ is the ammonia adjustment parameter, and its value range is 0 - 0.5, and the unit is m 3 / h. L is the basic ammonia water dosage, and the calculation formula is:

[0011] L = [C 入口SO2浓度 - C 出口SO2浓度 * V 标 / 64 * 34 / ammonia water concentration / 10000000, where C 入口SO2浓度 and C 出口SO2浓度 are in the unit of mg / Nm 3 , V 标 represents the inlet flue gas volume under standard conditions, and the unit is Nm 3 / h. The unit of ammonia water concentration is %.

[0012] In the above optimization and regulation method, by collecting the content of sulfur dioxide in the discharged flue gas, the pH value of the desulfurization liquid in the absorption section, and the pH value of the desulfurization liquid in the concentration and cooling section, M1 and M2 can be calculated. This application calculates the ammonia water adjustment amount △L with the pH changes of the desulfurization liquid in the concentration and cooling section and the absorption section in the desulfurization tower as the main variables, which can effectively adjust the ammonia water dosage in the desulfurization system, thereby improving the desulfurization efficiency while reducing the ammonia escape in the discharged flue gas. In addition, the above optimized ammonia water dosage can reduce the operation cost of the desulfurization tower and the impact force on the absorption membrane, thereby prolonging the service life of the absorption membrane and ensuring the efficient and stable operation of the desulfurization tower.

[0013] The above temperature adjustment parameter and ammonia adjustment parameter can be adjusted within the above range according to experience, or can be calculated according to the following formula:

[0014] σ = 0.05T1 / T2, where T1 is the outlet temperature of the concentration and cooling section in the desulfurization tower, measured by a temperature sensor, and the unit is °C; T2 is the outlet temperature of the absorption section in the desulfurization tower, measured by a temperature sensor, and the unit is °C.

[0015] The system status data further includes the ammonia content in the flue gas discharged.

[0016] γ = M3×K, M3 = (2M1 + M2) / 2, K is a calculation coefficient, and the real-time ammonia content at the current moment of the flue gas discharged ≥ 0.50 mg / m 3 When the real-time ammonia content at the current moment of the flue gas discharged ≤ 0.50 mg / m 3 and ≥ 0.40 mg / m 3 When the real-time ammonia content at the current moment of the flue gas discharged < 0.40 mg / m 3 K is 0.1.

[0017] During the desulfurization process, the desulfurization liquid in the concentration and cooling section contacts the flue gas to cool the flue gas, and desulfurization is not directly carried out. The outlet temperature of the concentration and cooling section is generally 60 - 63°C; the desulfurization liquid in the absorption section contacts the flue gas for desulfurization, and the outlet temperature of the absorption section is generally 55 - 60°C. In this process, the higher the temperature, the less significant the improvement effect on the desulfurization rate, but the ammonia escape amount will increase significantly. Therefore, using the outlet temperature of the concentration and cooling section and the outlet temperature of the absorption section as the variable of the temperature adjustment parameter can achieve the accurate calculation of the ammonia water dosage to reduce ammonia escape.

[0018] The values of M1 and M2 have great influence on both the desulfurization efficiency and ammonia escape. Therefore, using M1, M2, and K as the variables of the ammonia adjustment parameter can synergistically improve the desulfurization efficiency and reduce ammonia escape. The value of K depends on the value of the ammonia content in the flue gas discharged. When the value ≥ 0.50mg / m 3 It proves that for the desulfurization method combining ammonia method and membrane absorption, at this time the ammonia escape amount is large, and K being 0 can reduce the dosage of ammonia water, thereby reducing the ammonia content in the flue gas discharged. When the value ≤ 0.50mg / m 3 and ≥ 0.40 mg / m 3 At this time, by setting K to 0.05, the desulfurization efficiency can be improved and the ammonia escape amount can be controlled within a lower range; when the value < 0.40mg / m 3 At this time, the ammonia escape amount in the flue gas is small. In order to improve the desulfurization efficiency, the dosage of ammonia water can be appropriately increased, so K is 0.1.

[0019] Optionally, the thickness of the absorption membrane is 60 - 80μm, the average pore diameter is 70 - 75nm, and the porosity is 60 - 70%.

[0020] Optionally, the number of the first packing layers is 1, and the height is 400 - 600mm.

[0021] Optionally, both the first packing layer and the second packing layer are formed by arranging regular corrugated plates in parallel. The thickness of the regular corrugated plate is 1-2 mm, and the spacing is 10-30 mm. The regular corrugated plate is obtained by extrusion molding of polypropylene material.

[0022] Optionally, the distance between the absorption membrane and the first packing layer is 300-350 mm, and the distance between the first packing layer and the riser cap is 2000-3000 mm.

[0023] This distance setting can reserve a retention space for the flue gas between the absorption membrane and the first packing layer and between the riser cap and the first packing layer, playing a buffering role, avoiding damage to the absorption membrane caused by too much flue gas volume, and also being able to stabilize the flue gas volume when the flue gas volume is large or small, thereby improving the treatment efficiency of the flue gas.

[0024] Optionally, in the desulfurization system combining ammonia method and membrane absorption for desulfurization, an air inlet is provided in the oxidation section, a flue gas inlet and a liquid discharge port are provided on the side wall of the concentration and cooling section, a first spraying mechanism is arranged above the concentration and cooling section, the first spraying mechanism is connected to a concentration pump, the liquid discharge port is communicated with a crystallization tank, and the bottom of the crystallization tank is communicated with an ammonium sulfate product treatment mechanism through a crystallization pump;

[0025] In the purification section, a combined demister, a water washing spraying mechanism, and a second packing layer are sequentially arranged from top to bottom. The second packing layer is arranged above the riser cap. The water washing spraying mechanism is communicated with a circulation water tank through a water washing pump, and the water washing liquid in the purification section is returned to the circulation water tank through a water washing return pipe.

[0026] According to the second aspect of the present application, there is provided an application of the optimization and regulation method based on ammonia method and membrane absorption combined desulfurization as described in any one of the above in flue gas desulfurization.

[0027] According to the third aspect of the present application, there is provided an electronic device, including a memory and a processor. The memory stores a computer program, and when the processor executes the computer program, the steps of the optimization and regulation method based on ammonia method and membrane absorption combined desulfurization as described in any one of the above are implemented.

[0028] According to the fourth aspect of the present application, there is provided a computer-readable storage medium, on which a computer program is stored, characterized in that when the computer program is executed by a processor, the optimization and regulation method based on ammonia method and membrane absorption combined desulfurization as described in any one of the above is implemented.

[0029] The beneficial effects of the present application include but are not limited to:

[0030] 1. According to the optimization control method based on ammonia method and membrane absorption combined desulfurization of the present application, it is possible to calculate the ammonia water adjustment amount △L based on the characteristics of ammonia method and membrane absorption combined desulfurization according to the system state data, so as to adjust the dosage of ammonia water in the desulfurization process in real time, which can not only improve the desulfurization efficiency, but also reduce the decomposition of ammonia gas, thereby reducing the ammonia escape amount.

[0031] 2. According to the optimization control method based on ammonia method and membrane absorption combined desulfurization of the present application, the design of the absorption membrane and the first packing layer can increase the contact area between ammonia water and flue gas and extend the residence time of the flue gas, so as to achieve optimal desulfurization under the adjustment of the ammonia water adjustment amount.

[0032] 3. According to the optimization control method based on ammonia method and membrane absorption combined desulfurization of the present application, using the temperature adjustment parameter and ammonia adjustment parameter as the calculation parameters of the ammonia water adjustment amount can further improve the desulfurization rate and reduce ammonia escape, and extend the service life of the absorption membrane, ensuring the efficient and stable operation of the desulfurization tower. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The drawings described herein are used to provide a further understanding of the present application and form a part of the present application. The schematic embodiments of the present application and their descriptions are used to explain the present application and do not constitute an improper limitation of the present application. In the drawings:

[0034] Figure 1 It is a schematic structural diagram of the desulfurization system related to Embodiment 1 of the present application.

[0035] Figure 2 It is a schematic structural diagram of the desulfurization tower related to Embodiment 1 of the present application.

[0036] List of components and reference numerals:

[0037] 10. Desulfurization tower; 11. Purification section; 111. Combined demister; 112. Water washing spray mechanism; 113. Second packing layer; 114. Water washing pump; 12. Absorption section; 121. First packing layer; 122. Second spray mechanism; 123. Primary demister; 124. Return pipeline; 125. Second partition; 126. Circulation pump; 127. Absorption membrane; 13. Concentration and cooling section; 131. Flue gas inlet; 132. First spray mechanism; 133. Concentration pump; 134. First partition; 14. Oxidation section; 141. Air inlet; 142. Third partition; 20. Crystallization tank; 21. Crystallization pump; 30. Circulation water tank; 40. Ammonium sulfide product treatment mechanism; 50. Gas lift cap; 60. Three-layer spiral cone nozzle; 61. Volute nozzle; 70. Concentration circulation tank; 80. Feed liquid tank; 81. Feed liquid pump; 90. Water replenishment mechanism; 91. Ammonia replenishment mechanism. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0038] The present application will be described in detail below in conjunction with embodiments, but the present application is not limited to these embodiments.

[0039] Unless otherwise specified, the raw materials in the embodiments of the present application are all purchased through commercial channels.

[0040] Unless otherwise specified, the methods adopted in the embodiments of the present application are conventional methods in the prior art.

[0041] Embodiment 1

[0042] Reference Figure 1-2 , this embodiment relates to an ammonia desulfurization system and an ammonia desulfurization method. The ammonia desulfurization system includes a desulfurization tower 10, a crystallization tank 20, a circulating water tank 30, and an ammonium sulfide product treatment mechanism 40. The desulfurization tower 10 is divided into a demisting section, a purification section 11, an absorption section 12, a concentration and cooling section 13, and an oxidation section 14 from top to bottom:

[0043] The oxidation section 14 is provided with an air inlet 141, and air oxidizes the liquid in the oxidation section 14. The oxidized liquid is supplied to the absorption section 12 for spraying. When the ammonium sulfate content in the oxidation section 14 reaches the second threshold, a part of the liquid is sent into the concentration circulation tank 70;

[0044] The side wall of the concentration and cooling section 13 is provided with a flue gas inlet 131 and a liquid discharge port. A first spraying mechanism 132 is arranged above the concentration and cooling section 13. The first spraying mechanism 132 is connected to a concentration pump 133. The concentration pump 133 is used to transport the concentrated liquid in the concentration circulation tank 70 to the first spraying mechanism 132. The liquid after spraying flows back into the crystallization tank 20 through the liquid discharge port for crystallization. The upper-layer concentrated liquid in the crystallization tank 20 overflows into the concentration circulation tank 70. When the solid content in the crystallization tank 20 is greater than the first threshold, the substance at the bottom of the crystallization tank 20 is transported to the ammonium sulfate product treatment mechanism through a crystallization pump 21; The oxidation section and the concentration and cooling section are separated by a third partition 142. The form of the third partition 142 has two types: an inclined partition and a roof partition. The roof is divided into a positive roof and an inverted roof. The form of the third partition 142 is determined according to actual needs.

[0045] The oxidation section 14, the concentration and cooling section 13, the absorption section 12, and the purification section 11 of the desulfurization tower are separated into 4 independent systems by the third partition 142, the first partition 134, and the second partition 125: an oxidation system, a concentration and cooling system, an absorption system, and a purification system.

[0046] The concentration and cooling section 13 and the absorption section 12 are separated by a first partition plate 134. A plurality of uniformly distributed gas-lifting caps 50 are arranged on the first partition plate 134. Above the absorption section 12, a primary demister 123, a second spraying mechanism 122, an absorption film 127 and a first packing layer 121 are arranged from top to bottom. The first packing layer 121 is arranged above the gas-lifting caps 50. The absorption film is a polypropylene absorption film. The circulating pump 126 transports the liquid in the oxidation section 14 to the second spraying mechanism 122 for flue gas absorption. The liquid at the bottom of the absorption section 12 re-enters the oxidation section 14 through the reflux pipeline 124;

[0047] The absorption section 12 and the purification section 11 are separated by a second partition plate 125. A plurality of uniformly distributed gas-lifting caps 50 are also arranged on the second partition plate 125. In the purification section 11, a combined demister 111, a water washing spraying mechanism 112 and a second packing layer 113 are arranged in sequence from top to bottom. The water washing pump 114 transports the water in the circulating water tank 30 to the water washing spraying mechanism 112 for flue gas water washing. The water washing liquid in the purification section 11 is then refluxed into the circulating water tank 30.

[0048] The usage method of this desulfurization system is as follows:

[0049] (1) The flue gas after dust removal enters the concentration and cooling section 13 from the flue gas inlet 131, and is sprayed and cooled to below 60°C through the first spraying mechanism 132. The concentrated liquid in the concentration section enters the crystallization tank 20 through the liquid discharge port. The upper-layer concentrated liquid in the crystallization tank 20 overflows into the concentrated circulation tank 70. The concentrated pump 133 then sends the liquid in the concentrated circulation tank into the concentration section for spraying. When the solid content in the crystallization tank 20 reaches the first threshold (for example, more than 20%), the substance at the bottom of the crystallization tank 20 is transported to the ammonium sulfate product treatment mechanism;

[0050] (2) Then the flue gas rises to the absorption section 12, passes through the first packing layer 121, the second spraying mechanism 122 and the primary demister 123 for demisting, and then enters the purification section 11. The liquid in the absorption section 12 re-enters the oxidation section 14 through the reflux pipeline 124;

[0051] (3) The flue gas passes through the second packing layer 113 in the purification section 11, washes and captures ammonium sulfate and excess ammonia with water. Then, after demisting through the combined demister 111 in the demisting section, it enters the chimney for emission from the desulfurization tower 10. The water washing liquid in the purification section 11 is then refluxed into the circulating water tank 30;

[0052] (4) Compressed air enters the oxidation section 14 to oxidize the absorption liquid refluxed from the absorption section 12. The liquid formed after sufficient oxidation is then sent to the absorption section 12 for spraying. When the content of ammonium sulfate in the oxidation section 14 reaches the second threshold (for example, more than 95%), a part of the liquid is sent into the concentrated circulation tank 70.

[0053] Specifically, the uniform distribution of the riser caps 50 on the first partition plate 134 and the second partition plate 125 includes both longitudinal and transverse uniform distributions. Those skilled in the art can set them into appropriate arrangement shapes according to the needs of installation or production. For example, they can be arranged in a square pattern, a polygon pattern, etc. The above arrangement methods do not constitute a limitation to this application, as long as the flue gas can be evenly distributed so that the flue gas can evenly contact the absorption liquid or the water washing liquid.

[0054] As an implementation manner, it further includes a concentration circulation tank 70 and a liquid material tank 80. The concentration circulation tank 70 is connected to the crystallization tank 20. The liquid material tank 80 is connected to the ammonium sulfide product treatment mechanism 40 and is connected to the crystallization tank 20 through a liquid material pump 81.

[0055] The upper-layer concentrated liquid in the crystallization tank 20 first enters the concentration circulation tank 70, and then the liquid in the concentration circulation tank 70 is sent into the concentration section for spraying through a concentration pump 133. The liquid processed by the ammonium sulfide product treatment mechanism 40 through a hydrocyclone enters the liquid material tank 80, and the liquid in the liquid material tank 80 is then transported to the crystallization tank 20 through the liquid material pump 81 to participate in the cycle and crystallization.

[0056] The setting of the concentration circulation tank 70 can improve the component stability of the spraying liquid in the concentration and cooling section 13. The settings of the liquid material tank 80 and the liquid material pump 81 can improve the utilization rate of ammonia in the overall desulfurization system and reduce the flue gas treatment cost.

[0057] As an implementation manner, it further includes a water replenishing mechanism 90 and an ammonia replenishing mechanism 91. The inlet of the water replenishing mechanism 90 is arranged above the desulfurization tower 10, and the ammonia water inlet of the ammonia replenishing mechanism 91 is arranged on the pipeline for transporting the absorption liquid from the oxidation section 14 to the absorption section 12.

[0058] As an implementation manner, both the first spraying mechanism 132 and the second spraying mechanism 122 include a plurality of circular brackets. A plurality of three-layer spiral cone nozzles 60 are arranged on each circular bracket of the second spraying mechanism 122. The three-layer spiral cone nozzles 60 are evenly distributed longitudinally and transversely. A plurality of volute nozzles 61 are arranged on each circular bracket of the first spraying mechanism 132. The volute nozzles 61 are also evenly distributed longitudinally and transversely.

[0059] The uniform distribution of the three-layer spiral cone nozzles 60 along with the circular brackets can achieve the uniform spraying of the liquid in the concentration and cooling section 13 and the absorption section 12, thereby increasing the contact area between the flue gas and the liquid in the two sections and improving the absorption efficiency. Using the three-layer spiral cone nozzles 60 can spray out three liquid films, and the single-layer spraying coverage rate reaches 150 - 200%. When the flue gas passes through the three liquid films, it can make the gas-liquid fully contact and undergo an absorption reaction, greatly improving the absorption efficiency of sulfur dioxide, and can re-absorb some decomposed ammonia, further preventing the escape of ammonia.

[0060] As an implementation manner, the distances between the three-layer spiral cone nozzles 60 and volute nozzles 61 on the outermost circular bracket and the wall of the desulfurization tower 10 are both 700 - 1200 mm. This setting can improve the spray coverage rate. Firstly, it is convenient for operators to install and maintain the three-layer spiral cone nozzles 60 and volute nozzles 61. Secondly, it reduces the contact area between the spray liquid and the wall of the desulfurization tower 10, reduces the corrosion of the wall of the desulfurization tower 10, and improves the service life and use safety of the desulfurization system.

[0061] As an implementation manner, there is 1 first packing layer 121, and the height of the first packing layer 121 is 400 - 600 mm; there is 1 second packing layer 113, and the height is 400 - 450 mm.

[0062] As an implementation manner, both the first packing layer 121 and the second packing layer 113 are formed by arranging regular corrugated plates in parallel. The thickness of the regular corrugated plate is 1 - 2 mm, the spacing is 10 - 30 mm, and the regular corrugated plate is obtained by extrusion molding of polypropylene.

[0063] The above setting of the regular corrugated plate can improve the redistribution uniformity of the flue gas, making the contact effect between the flue gas and the absorption liquid or washing liquid the best.

[0064] As an implementation manner, the thickness of the absorption membrane 127 is 60 - 80 μm, the average pore diameter is 70 - 75 nm, and the porosity is 60 - 70%. The absorption membrane is obtained by melt spinning polypropylene particles to obtain primary fibers, and the primary fibers are stretched to form pores and then treated at 100 - 110 °C for 200 s.

[0065] As an implementation manner, the distance between the absorption membrane 127 and the first packing layer 121 is 300 - 350 mm. This distance setting can reserve a retention space for the flue gas between the absorption membrane 127 and the first packing layer 121, playing a buffering role, avoiding damage to the absorption membrane caused by too large a flue gas volume, and also being able to stabilize the flue gas volume when the flue gas volume changes suddenly, thereby improving the treatment efficiency of the flue gas.

[0066] Example 2

[0067] This example relates to an optimization control method using the desulfurization system of Example 1, specifically including the following steps:

[0068] (1) Collect the system status data within a period of time T before the current moment. The system status data includes: the content of sulfur dioxide in the discharged flue gas, the pH value of the desulfurization liquid in the absorption section, and the pH value of the desulfurization liquid in the concentration and cooling section. Calculate M1 and M2. M1 is the change in the pH value of the desulfurization liquid in the absorption section when the flue gas index value changes by 1 mg / Nm³, and M2 is the change in the pH value of the desulfurization liquid in the concentration and cooling section when the flue gas index value changes by 1 mg / Nm³.

[0069] (2) Calculate the ammonia water dosage according to the following formula. The ammonia water dosage = L + △L, where △L is the ammonia water adjustment amount, and the unit is m 3 / h:

[0070] △L = (M1 - M2) / 0.1 + σ + γ;

[0071] where σ is the temperature adjustment parameter, and its value range is 0.04 - 0.05. γ is the ammonia adjustment parameter, and its value range is 0 - 0.5, and the unit is m 3 / h. L is the basic ammonia water dosage, and its calculation formula is:

[0072] L = [C 入口SO2浓度 - C 出口SO2浓度 ] * V 标 / 64 * 34 / ammonia water concentration / 10000000, where C 入口SO2浓度 and C 出口SO2浓度 are in the unit of mg / Nm 3 , V 标 represents the inlet flue gas volume under standard conditions, and the unit is Nm 3 / h. The unit of ammonia water concentration is %.

[0073] Specifically, the methods for calculating M1 and M2 are as follows:

[0074] 1) According to the collected sulfur dioxide content data in the discharged flue gas within a period of time T before the current moment, obtain the average content A of sulfur dioxide in the discharged flue gas per hour within a period of time T before the current moment by taking the average. 1，2……n , where n is the number of hours within time T;

[0075] 2) According to the collected pH data of the desulfurization liquid in the absorption section within a period of time T before the current moment, obtain the average value B of the pH of the desulfurization liquid per hour within a period of time T before the current moment by taking the average. 1，2……n , where n is the number of hours within time T; According to the collected pH data of the desulfurization liquid in the concentration and cooling section within a period of time T before the current moment, obtain the average value C of the pH of the desulfurization liquid per hour within a period of time T before the current moment by taking the average. 1，2……n , where n is the number of hours within time T

[0076] 3) Calculate the change in sulfur dioxide content in the flue gas emissions between two adjacent hours, ΔAn = An - An-1, by subtracting the average sulfur dioxide content in the flue gas emissions in the previous adjacent hour from the average sulfur dioxide content in the flue gas emissions in the next hour.

[0077] 4) Calculate the change in pH value of the desulfurization liquid in the absorption section between two adjacent hours, ΔBn = Bn - Bn-1, by subtracting the average pH value of the desulfurization liquid in the previous adjacent hour from the average pH value of the desulfurization liquid in the next hour; calculate the change in pH value of the desulfurization liquid in the concentration and cooling section between two adjacent hours, ΔCn = Cn - Cn-1, by subtracting the average pH value of the desulfurization liquid in the previous adjacent hour from the average pH value of the desulfurization liquid in the next hour.

[0078] 5) Average the calculated change in sulfur dioxide content in the flue gas emissions between two adjacent hours, ΔAn, to obtain the average change in sulfur dioxide content in the flue gas emissions, A1, over a period of time T before the current moment.

[0079] 6) Average the calculated change in pH value of the desulfurization liquid in the absorption section between two adjacent hours, ΔBn, to obtain the average change in pH value of the desulfurization liquid, B1, over a period of time T before the current moment; average the calculated change in pH value of the desulfurization liquid in the concentration and cooling section between two adjacent hours, ΔCn, to obtain the average change in pH value of the desulfurization liquid, C1, over a period of time T before the current moment.

[0080] 7) Calculate M1 by dividing the average change in pH value of the desulfurization liquid in the absorption section, B1, over a period of time T before the current moment by the average change in sulfur dioxide content in the flue gas emissions, A1, over a period of time T before the current moment, i.e., M1 = B1 / A1; calculate M1 by dividing the average change in pH value of the desulfurization liquid in the concentration and cooling section, C1, over a period of time T before the current moment by the average change in sulfur dioxide content in the flue gas emissions, A1, over a period of time T before the current moment, i.e., M1 = C1 / A1.

[0081] As an implementation manner, σ = 0.05T1 / T2, where T1 is the outlet temperature of the concentration and cooling section in the desulfurization tower, measured by a temperature sensor, with the unit of °C; T2 is the outlet temperature of the absorption section in the desulfurization tower, measured by a temperature sensor, with the unit of °C.

[0082] As an implementation manner, the system status data further includes the ammonia content in the flue gas emissions.

[0083] γ = M3×K, M3 = (2M1 + M2) / 2, K is a calculation coefficient, and when the real-time ammonia content at the current moment of the flue gas emissions ≥ 0.50 mg / m 3 , K is 0, and when the real-time ammonia content at the current moment of the flue gas emissions ≤ 0.50 mg / m3 and ≥ 0.40 mg / m 3 When it is, K is 0.05, and the real-time ammonia content at the current moment of the discharged flue gas < 0.40 mg / m 3 When it is, K is 0.1.

[0084] By using the method of this embodiment for simulation regulation, it can ensure that the desulfurization efficiency is greater than 99% and the ammonia escape amount is lower than 0.90 mg / m 3 , and applying it in enterprises on-site, it can operate sustainably and efficiently, achieving the same operation effect as the simulation. The sulfur dioxide content in the discharged flue gas fluctuates within the range of 10 - 30 mg / m 3 range, and the ammonia content fluctuates within the range of 0.30 - 0.90 mg / m 3 range. Therefore, the composition fluctuation in the discharged flue gas is not significant, proving that this optimized regulation method can help the desulfurization system combining ammonia method and membrane absorption to be in a stable and environmentally friendly operation state for a long time.

[0085] Embodiment 3

[0086] This embodiment relates to an electronic device, which includes a memory and a processor. The memory stores a computer program, and when the processor executes the computer program, it realizes the steps of the optimized regulation method for desulfurization combining ammonia method and membrane absorption described in Embodiment 1.

[0087] Embodiment 4

[0088] This embodiment relates to a computer-readable storage medium, on which a computer program is stored. When the computer program is executed by a processor, it realizes the optimized regulation method for desulfurization combining ammonia method and membrane absorption described in Embodiment 1.

[0089] As mentioned above, only the embodiments of this application are described. The protection scope of this application is not limited by these specific embodiments, but is determined by the claims of this application. For those skilled in the art, various changes and modifications can be made to this application. Any modifications, equivalent replacements, improvements, etc. made within the technical idea and principle of this application should be included in the protection scope of this application.

Claims

1. An optimization and control method based on ammonia process and membrane absorption combined desulfurization, characterized in that: The desulfurization system of ammonia method and membrane absorption combined desulfurization comprises a desulfurization tower, a concentration circulation tank, a crystallization tank, an ammonium sulfate product processing mechanism and a circulation water tank; the desulfurization tower is divided into a demisting section, a purification section, an absorption section, a concentration cooling section and an oxidation section from top to bottom, the concentration cooling section and the absorption section are separated by a first partition, the absorption section and the purification section are separated by a second partition, and the oxidation section and the concentration cooling section are separated by a third partition; a primary demister, a second spray mechanism, an absorption membrane and a first packing layer are arranged from top to bottom above the absorption section, the first packing layer is arranged above the air lifting cap, the absorption membrane is a polypropylene absorption membrane, the second spray mechanism is arranged above the absorption membrane, the second spray mechanism is connected to the oxidation section through a circulation pump, and the bottom of the absorption section is connected to the oxidation section through a reflux pipe; specifically comprising the following steps: (1) Collect system status data for a period of time T before the current moment, including the content of sulfur dioxide in the exhaust gas, the pH value of the desulfurization liquid in the absorption section, and the pH value of the desulfurization liquid in the concentration and cooling section, and calculate M1 and M2, where M1 is the change in the pH value of the desulfurization liquid in the absorption section when the flue gas index value changes by 1 mg / Nm³, and M2 is the change in the pH value of the desulfurization liquid in the concentration and cooling section when the flue gas index value changes by 1 mg / Nm³; (2) Calculate the amount of ammonia water according to the following formula: Ammonia water amount = L + △L, △L is the amount of ammonia water adjustment, unit is m 3 / h: △L=(M1-M2) / 0.1+σ+γ; Where σ is the temperature adjustment parameter, the value range is 0.04~0.05, γ is the ammonia adjustment parameter, the value range is 0~0.5, the unit is m 3 / h, L is the basic amount of ammonia water, and the calculation formula is: L=[C 入口SO2浓度 -C 出口SO2浓度 ]* V 标 / 64*34 / ammonia concentration / 10000000, where C 入口SO2浓度 and C 出口SO2浓度 The unit is mg / Nm 3 , V 标 Represents the smoke intake under standard conditions, in Nm 3 / h, the unit of ammonia concentration is %.

2. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to claim 1, characterized in that: σ=0.05T1 / T2, where T1 is the outlet temperature of the concentration and cooling section in the desulfurization tower, measured by a temperature sensor, in degrees Celsius; T2 is the outlet temperature of the absorption section in the desulfurization tower, measured by a temperature sensor, in degrees Celsius.

3. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to claim 1 is characterized in that: The system status data also includes ammonia content in the exhaust gas; γ=M3×K, M3=(2M1+M2) / 2, K is the calculation coefficient, the real-time ammonia content of the exhaust gas at the current moment is ≥0.50mg / m 3 When K is 0, the real-time ammonia content of the exhaust gas at the current moment is ≤0.50mg / m 3 and ≥0.40 mg / m 3 When K is 0.05, the real-time ammonia content of the exhaust gas at the current moment is less than 0.40 mg / m 3 When , K is 0.

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4. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to claim 1, characterized in that: The absorption film has a thickness of 60-80 μm, an average pore diameter of 70-75 nm, and a porosity of 60-70%.

5. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to claim 1, characterized in that: The number of the first packing layer is one and the height is 400-600 mm.

6. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to claim 5, characterized in that: The distance between the absorption film and the first filler layer is 300-350 mm, and the distance between the first filler layer and the air lifting cap is 2000-3000 mm.

7. The optimization and control method based on ammonia process and membrane absorption combined desulfurization according to any one of claims 1 to 6, characterized in that: In the desulfurization system combining ammonia method and membrane absorption desulfurization, the oxidation section is provided with an air inlet, the side wall of the concentration and cooling section is provided with a flue gas inlet and a liquid discharge port, a first spray mechanism is provided above the concentration and cooling section, the first spray mechanism is connected to a concentration pump, the liquid discharge port is connected to a crystallization tank, and the bottom of the crystallization tank is connected to an ammonium sulfate product processing mechanism through a crystallization pump; A water washing spray mechanism and a second packing layer are arranged in sequence from top to bottom in the purification section. The second packing layer is arranged above the air lifting cap. The water washing spray mechanism is connected to the circulating water tank through a water washing pump. The water washing liquid in the purification section is then returned to the circulating water tank through a water washing reflux pipe.

8. Application of the optimization control method based on ammonia method and membrane absorption combined desulfurization as described in any one of claims 1 to 7 in flue gas desulfurization.

9. An electronic device, characterized in that: The method comprises a memory and a processor, wherein the memory stores a computer program, and the processor implements the steps of the optimization control method based on ammonia method and membrane absorption combined with desulfurization as described in any one of claims 1 to 7 when executing the computer program.

10. A computer-readable storage medium having a computer program stored thereon, characterized in that: When the computer program is executed by a processor, the optimization and control method based on ammonia method and membrane absorption combined desulfurization according to any one of claims 1 to 7 is implemented.

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