Optimized regulation and control method based on ammonia process and membrane absorption combined desulfurization, application of optimized regulation and control method, electronic equipment and computer readable storage medium

Abstract

The invention discloses an optimization regulation and control method based on ammonia process and membrane absorption combined desulfurization, application of the optimization regulation and control method, electronic equipment and a computer readable storage medium, and belongs to the technical field of flue gas ammonia process desulfurization. The method comprises the following steps: (1) collecting system state data within a period of time T before the current moment, the system state data comprising the content of sulfur dioxide in discharged flue gas, the pH value of a desulfurization solution in an absorption section and the pH value of a desulfurization solution in a concentration cooling section, and calculating M1 and M2; (2) calculating the amount of ammonia water according to the following formula: ammonia water amount = L + L, L is the ammonia water adjusting amount, and the unit is m < 3 > / h: L = (M1-M2) / 0.1 + sigma + gamma; wherein sigma is a temperature adjusting parameter and ranges from 0.04 to 0.05, and gamma is an ammonia adjusting parameter and ranges from 0 to 0.5. The method is designed for an ammonia process and membrane absorption combined desulfurization process, the ammonia water consumption is optimized according to the collected sulfur content in the flue gas and state parameters of an absorption circulation liquid state, the desulfurization efficiency is improved, meanwhile, ammonia escape is reduced, and the operation cost of a desulfurization system is saved.

Description

Technical Field

[0001] The present application relates to an optimization control method based on ammonia method and membrane absorption combined desulfurization and its application, electronic equipment and computer-readable storage medium, belonging to the technical field of flue gas ammonia method desulfurization. Background Art

[0002] Ammonia desulfurization is currently the most commonly used flue gas desulfurization method. It has the advantages of high desulfurization efficiency and wide application range. In addition, the ammonium sulfite generated in the desulfurization process reacts chemically with the oxygen in the air in the oxidation section to generate ammonium sulfate, which is then concentrated and crystallized into a solid ammonium sulfate by-product. This by-product can also be used to prepare fertilizers, thereby achieving effective utilization of resources.

[0003] Ammonia desulfurization technology has the disadvantages of large ammonia escape and serious aerosol phenomenon, which hinders the promotion and use of ammonia desulfurization technology. At present, the combination of membrane absorption and ammonia desulfurization methods can significantly reduce the use of ammonia water, and thus can also reduce ammonia escape from the source.

[0004] The current ammonia-based desulfurization can control the amount of ammonia water used by parameter setting, but it is only an optimization method for controlling the amount of ammonia water used in a single ammonia-based desulfurization, and is not suitable for a desulfurization system that combines membrane absorption and ammonia-based desulfurization. Therefore, there is an urgent need for an optimization and control method for combined membrane absorption and ammonia-based desulfurization. Summary of the invention

[0005] In order to solve the above problems, an optimization and control method based on desulfurization combined with ammonia method and membrane absorption is provided. The method is designed for the desulfurization process combining ammonia method and membrane absorption, and can optimize the amount of ammonia water according to the collected state parameters, thereby improving the desulfurization efficiency while reducing ammonia escape and saving the operating cost of the desulfurization system.

[0006] According to one aspect of the present application, an optimization control method based on ammonia method and membrane absorption combined desulfurization is provided, and the desulfurization system of ammonia method and membrane absorption combined desulfurization includes a desulfurization tower, a concentration circulation tank, a crystallization tank, an ammonium sulfate product processing mechanism and a circulating water tank; a desulfurization tower, wherein 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 lift 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 %.

[0007] In the above optimization and control method, M1 and M2 can be calculated by collecting 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. This application uses 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 to calculate the ammonia adjustment amount △L, which can achieve effective regulation of the amount of ammonia in the desulfurization system, thereby improving the desulfurization efficiency while reducing the ammonia escape in the exhaust gas. In addition, the above optimized ammonia dosage can reduce the operating cost of the desulfurization tower and reduce the impact on the absorption membrane, thereby extending the service life of the absorption membrane and ensuring the efficient and stable operation of the desulfurization tower.

[0008] The above temperature adjustment parameters and ammonia adjustment parameters can be adjusted within the above range based on experience, or can be calculated according to the following formula: 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.

[0009] 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 ≥0.50 mg / m 3 When K is 0, the real-time ammonia content of the exhaust gas at the current moment is ≤0.50 mg / 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 0.1.

[0010] During the desulfurization process, the desulfurization liquid in the concentration and cooling section contacts the flue gas to cool the flue gas, but does not directly desulfurize. The outlet temperature of the concentration and cooling section is generally 60~63℃; 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℃. The higher the temperature in this process, the less significant the effect on the desulfurization rate, but the ammonia escape will increase significantly. Therefore, the outlet temperature of the concentration and cooling section and the outlet temperature of the absorption section are used as variables of the temperature adjustment parameters to achieve accurate calculation of the amount of ammonia water used to reduce ammonia escape.

[0011] The values ​​of M1 and M2 have a great impact on the desulfurization efficiency and ammonia slip. Therefore, using M1, M2 and K as variables of ammonia adjustment parameters can synergistically improve the desulfurization efficiency and reduce ammonia slip. The value of K depends on the value of ammonia content in the exhaust gas. When the value is ≥0.50mg / m 3 It is proved that for the desulfurization method combining ammonia method and membrane absorption, the ammonia escape is large at this time, and K is 0, which can reduce the amount of ammonia water, thereby reducing the ammonia content in the exhaust gas. When the value is ≤0.50mg / m 3 and ≥0.40 mg / m 3 When K is set to 0.05, the desulfurization efficiency can be improved and the ammonia escape can be controlled within a lower range; when the value is less than 0.40 mg / m 3 At this time, the amount of ammonia escape in the flue gas is small. In order to improve the desulfurization efficiency, the amount of ammonia water can be appropriately increased, so K is 0.1.

[0012] Optionally, the absorption film has a thickness of 60-80 μm, an average pore size of 70-75 nm, and a porosity of 60-70%.

[0013] Optionally, the number of the first packing layer is one and the height is 400-600 mm.

[0014] Optionally, the first filler layer and the second filler layer are both formed by regular corrugated plates arranged in parallel, the regular corrugated plates have a thickness of 1-2 mm and a spacing of 10-30 mm, and the regular corrugated plates are obtained by extrusion molding of polypropylene materials.

[0015] Optionally, 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.

[0016] This spacing setting can reserve retention space for smoke between the absorption membrane and the first filler layer and between the air lift cap and the first filler layer, which plays a buffering role and prevents damage to the absorption membrane caused by excessive smoke volume. It can also stabilize the smoke volume when the smoke volume fluctuates, thereby improving the smoke treatment efficiency.

[0017] Optionally, 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; The purification section is provided with a combined demister, a water washing spray mechanism, and a second packing layer in sequence from top to bottom. 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.

[0018] According to a second aspect of the present application, there is provided an application of the optimization control method based on ammonia method and membrane absorption combined desulfurization as described in any one of the above items in flue gas desulfurization.

[0019] According to a third aspect of the present application, an electronic device is provided, comprising a memory and a processor, wherein the memory stores a computer program, and the processor implements the steps of any of the above-mentioned optimization and control methods based on ammonia method and membrane absorption combined with desulfurization when executing the computer program.

[0020] According to a fourth aspect of the present application, a computer-readable storage medium is provided, on which a computer program is stored, 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 as described in any one of the above items is implemented.

[0021] The beneficial effects of this application include but are not limited to: 1. According to the optimization control method based on the combined desulfurization of ammonia method and membrane absorption of the present application, based on the characteristics of the combined desulfurization of ammonia method and membrane absorption, the ammonia water adjustment amount △L can be calculated according to the system state data to adjust the amount 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.

[0022] 2. According to the optimized control method based on ammonia method and membrane absorption combined desulfurization of the present application, the design of the absorption membrane and the first filler layer can increase the contact area between ammonia water and flue gas and prolong the residence time of flue gas, thereby achieving optimized desulfurization under the adjustment of ammonia water regulation amount.

[0023] 3. According to the optimized control method based on ammonia method and membrane absorption combined desulfurization of the present application, the temperature adjustment parameter and the ammonia adjustment parameter are used as the calculation parameters of the ammonia water adjustment amount, which can further improve the desulfurization rate and reduce ammonia escape, and extend the service life of the absorption membrane, thereby ensuring the efficient and stable operation of the desulfurization tower. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The drawings described herein are used to provide a further understanding of the present application and constitute a part of the present application. The illustrative embodiments of the present application and their descriptions are used to explain the present application and do not constitute an improper limitation on the present application. In the drawings: Figure 1 This is a schematic diagram of the structure of the desulfurization system involved in Example 1 of the present application.

[0025] Figure 2 This is a schematic diagram of the structure of the desulfurization tower involved in Example 1 of the present application.

[0026] List of parts and reference numerals: 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. First-stage demister; 124. Reflux pipe; 125. Second partition; 126. Circulation pump; 127. Absorption membrane; 13. Concentration and cooling section; 131. Flue gas inlet; 132. A spray mechanism; 133, a concentration pump; 134, a first partition; 14, an oxidation section; 141, an air inlet; 142, a third partition; 20, a crystallization tank; 21, a crystallization pump; 30, a circulating water tank; 40, an ammonium sulfide product processing mechanism; 50, an air lift cap; 60, a three-layer spiral cone nozzle; 61, a volute nozzle; 70, a concentration circulation tank; 80, a liquid tank; 81, a liquid pump; 90, a water replenishment mechanism; 91, an ammonia replenishment mechanism. DETAILED DESCRIPTION

[0027] The present application is described in detail below with reference to embodiments, but the present application is not limited to these embodiments.

[0028] Unless otherwise specified, the raw materials in the examples of this application were purchased through commercial channels.

[0029] Unless otherwise specified, the methods used in the embodiments of the present application are conventional methods in the prior art.

[0030] Example 1 refer to Figure 1-2 This embodiment relates to an ammonia desulfurization system and an ammonia desulfurization method, the ammonia desulfurization system comprises a desulfurization tower 10, a crystallization tank 20, a circulating water tank 30 and an ammonium sulfide product processing 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: The oxidation section 14 is provided with an air inlet 141, and the air oxidizes the liquid in the oxidation section 14, and the oxidized liquid is sprayed by the absorption section 12. When the ammonium sulfate content in the oxidation section 14 reaches a second threshold value, a portion of the liquid is sent to the concentration circulation tank 70; A flue gas inlet 131 and a liquid discharge port are provided on the side wall of the concentration and cooling section 13. A first spray mechanism 132 is provided above the concentration and cooling section 13. The first spray 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 spray mechanism 132. The liquid after spraying flows back to the crystallization tank 20 through the liquid discharge port for crystallization. The upper concentrated liquid in the crystallization tank 20 overflows to the concentration circulation tank 70. When the solid content in the crystallization tank 20 is greater than the first threshold value, the material at the bottom of the crystallization tank 20 is transported to the ammonium sulfate product processing mechanism through the crystallization pump 21. The oxidation section and the concentration and cooling section are separated by a third partition 142. The third partition 142 has two types: an inclined partition and a ridge partition. The ridge is further divided into a positive ridge and an inverted ridge. The type of the third partition 142 is determined according to actual needs.

[0031] 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 four 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.

[0032] The concentration and cooling section 13 and the absorption section 12 are separated by a first partition 134, and a plurality of evenly distributed gas lift caps 50 are arranged on the first partition 134. A primary demister 123, a second spray mechanism 122, an absorption film 127 and a first packing layer 121 are arranged from top to bottom above the absorption section 12. The first packing layer 121 is arranged above the gas lift cap 50. The absorption film is a polypropylene absorption film. The circulation pump 126 transports the liquid in the oxidation section 14 to the second spray 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 pipe 124. The absorption section 12 and the purification section 11 are separated by a second partition 125, and a plurality of evenly distributed air lifting caps 50 are also provided on the second partition 125. A combined demister 111, a water washing spray mechanism 112, and a second packing layer 113 are sequentially provided in the purification section 11 from top to bottom. The water washing pump 114 transports the water in the circulating water tank 30 to the water washing spray mechanism 112 for flue gas water washing, and the water washing liquid in the purification section 11 flows back to the circulating water tank 30.

[0033] The method of using the desulfurization system is: (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 by the first spray mechanism 132. The concentrated liquid in the concentration section enters the crystallization tank 20 through the drain port. The upper concentrated liquid in the crystallization tank 20 overflows to the concentration circulation tank 70. The concentration pump 133 then sends the liquid in the concentration circulation tank into the concentration section for spraying. When the solid content in the crystallization tank 20 reaches a first threshold value (for example, more than 20%), the material at the bottom of the crystallization tank 20 is transported to the ammonium sulfate product processing mechanism; (2) The flue gas then rises to the absorption section 12, passes through the first packing layer 121, the second spray mechanism 122 and the primary demister 123 for defog, and then enters the purification section 11. The liquid in the absorption section 12 re-enters the oxidation section 14 through the reflux pipe 124; (3) The flue gas passes through the second packing layer 113 and water washing in the purification section 11 to capture ammonium sulfate and excess ammonia. After that, the flue gas is defogged by the combined defogger 111 in the demisting section and then discharged from the desulfurization tower 10 into the chimney. The water washing liquid in the purification section 11 is then returned to the circulating water tank 30. (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 a second threshold value (for example, above 95%), a portion of the liquid is sent to the concentration circulation tank 70.

[0034] Specifically, the uniform distribution of the rising air caps 50 on the first partition 134 and the second partition 125 includes both longitudinal uniform distribution and lateral uniform distribution. Those skilled in the art can set them to a suitable arrangement shape according to the needs of installation or production, such as a square arrangement, a polygonal arrangement, etc. The above arrangement does not constitute a limitation to the present application, as long as the flue gas can be evenly distributed so that the flue gas can be evenly contacted with the absorption liquid or the washing liquid.

[0035] As an embodiment, it also includes a concentration circulation tank 70 and a feed liquid tank 80, the concentration circulation tank 70 is connected to the crystallization tank 20, the feed liquid tank 80 is connected to the ammonium sulfide product processing mechanism 40 and is connected to the crystallization tank 20 through a feed liquid pump 81.

[0036] The upper concentrated liquid of the crystallization tank 20 first enters the concentration circulation tank 70, and then the liquid in the concentration circulation tank 70 is sent to the concentration section for spraying through the concentration pump 133. The liquid treated by the cyclone in the ammonium sulfide product processing mechanism 40 enters the feed liquid tank 80, and the liquid in the feed liquid tank 80 is then transported to the crystallization tank 20 through the feed liquid pump 81 to participate in circulation and crystallization.

[0037] The provision of the concentration circulation tank 70 can improve the component stability of the spray liquid in the concentration cooling section 13, and the provision of the liquid tank 80 and the liquid pump 81 can improve the utilization rate of ammonia in the overall desulfurization system and reduce the flue gas treatment cost.

[0038] As an embodiment, it also includes a water replenishment mechanism 90 and an ammonia replenishment mechanism 91. The inlet of the water replenishment mechanism 90 is arranged above the desulfurization tower 10, and the ammonia water inlet of the ammonia replenishment mechanism 91 is arranged on the pipeline that transports the absorption liquid from the oxidation section 14 to the absorption section 12.

[0039] As an embodiment, the first spray mechanism 132 and the second spray mechanism 122 both include a plurality of circular brackets, each circular bracket of the second spray mechanism 122 is provided with a plurality of three-layer spiral cone nozzles 60, and the three-layer spiral cone nozzles 60 are evenly distributed in the longitudinal and transverse directions, and each circular bracket of the first spray mechanism 132 is provided with a plurality of volute nozzles 61, and the volute nozzles 61 are also evenly distributed in the longitudinal and transverse directions.

[0040] The three-layer spiral cone nozzle 60 is evenly distributed with the circular bracket to achieve 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. The three-layer spiral cone nozzle 60 can spray three layers of liquid film, and the single-layer spray coverage rate reaches 150-200%. The flue gas passes through the three layers of liquid film, which can make the gas and liquid fully contact and cause absorption reaction, greatly improving the absorption efficiency of sulfur dioxide, and can reabsorb part of the decomposed ammonia, further preventing the escape of ammonia.

[0041] As an implementation mode, the distance between the three-layer spiral cone nozzle 60 and the volute nozzle 61 on the outermost circular bracket and the wall of the desulfurization tower 10 is 700-1200 mm. This setting can improve the spray coverage rate, and at the same time, it is convenient for operators to install and repair the three-layer spiral cone nozzle 60 and the volute nozzle 61, and 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 safety of the desulfurization system.

[0042] As an implementation manner, the number of the first packing layer 121 is one, and the height of the first packing layer 121 is 400-600 mm; the number of the second packing layer 113 is one, and the height of the first packing layer 121 is 400-450 mm.

[0043] As an implementation mode, the first packing layer 121 and the second packing layer 113 are both formed by regular corrugated plates arranged in parallel, the regular corrugated plates have a thickness of 1-2 mm, a spacing of 10-30 mm, and are obtained by extrusion molding of polypropylene.

[0044] The arrangement of the regular corrugated plates can improve the uniformity of the redistribution of the flue gas, thereby achieving the best contact effect between the flue gas and the absorption liquid or the washing liquid.

[0045] As an embodiment, the absorption film 127 has a thickness of 60-80 μm, an average pore size of 70-75 nm, and a porosity of 60-70%. The absorption film is obtained by melt spinning polypropylene particles to obtain primary fibers, which are stretched to form pores and then treated at 100-110° C. for 200 seconds.

[0046] As an implementation method, the distance between the absorption film 127 and the first filler layer 121 is 300-350 mm. This distance setting can reserve a retention space for smoke between the absorption film 127 and the first filler layer 121, play a buffering role, avoid damage to the absorption film caused by too much smoke, and can also stabilize the smoke volume when the smoke volume fluctuates, thereby improving the smoke treatment efficiency.

[0047] Example 2 This embodiment relates to an optimization control method using the desulfurization system of embodiment 1, which specifically includes 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 %.

[0048] Specifically, the method for calculating M1 and M2 is: 1) Based on the collected data on the sulfur dioxide content in the flue gas emitted within a period of time T before the current moment, the average sulfur dioxide content A in the flue gas emitted every hour within a period of time T before the current moment is obtained by averaging 1，2……n , n is the number of hours in time T; 2) Based on the collected pH data of the desulfurization liquid in the absorption section within a period of time T before the current moment, the average pH value of the desulfurization liquid per hour within a period of time T before the current moment is obtained by averaging B 1，2……n , n is the number of hours in time T; according to the collected pH data of the desulfurization liquid in the concentrated cooling section in a period of time T before the current moment, the average pH value C of the desulfurization liquid in each hour in the period of time T before the current moment is obtained by averaging 1，2……n , n is the number of hours in time T 3) The change in sulfur dioxide content in the flue gas emitted in two consecutive hours is calculated by subtracting the average sulfur dioxide content in the flue gas emitted in the previous hour from the average sulfur dioxide content in the flue gas emitted in the next hour, An=An-An-1; 4) The average pH value of the desulfurization liquid in the next hour is subtracted from the average pH value of the desulfurization liquid in the previous hour to calculate the pH value change of the desulfurization liquid in the absorption section for two consecutive hours ΔBn=Bn-Bn-1; the average pH value of the desulfurization liquid in the next hour is subtracted from the average pH value of the desulfurization liquid in the previous hour to calculate the pH value change of the desulfurization liquid in the concentration and cooling section for two consecutive hours ΔCn=Cn-Cn-1; 5) The calculated change in sulfur dioxide content in the flue gas in two consecutive hours ΔAn is averaged to obtain the average change A1 of sulfur dioxide content in the flue gas in a period of time T before the current moment; 6) The calculated changes in pH value of the desulfurization liquid in the absorption section for two consecutive hours ΔBn are averaged to obtain the average change in pH value of the desulfurization liquid in a period of time T before the current moment B1; the calculated changes in pH value of the desulfurization liquid in the concentration and cooling section for two consecutive hours ΔCn are averaged to obtain the average change in pH value of the desulfurization liquid in a period of time T before the current moment C1; 7) Calculate M1 by dividing the average change B1 of the pH value of the desulfurization liquid in the absorption section within a period of time T before the current moment by the average change A1 of the sulfur dioxide content in the flue gas emitted within a period of time T before the current moment, that is, M1=B1 / A1; calculate M1 by dividing the average change C1 of the pH value of the desulfurization liquid in the concentration and cooling section within a period of time T before the current moment by the average change A1 of the sulfur dioxide content in the flue gas emitted within a period of time T before the current moment, that is, M1=C1 / A1.

[0049] As an implementation method, σ=0.05T1 / T2, wherein T1 is the outlet temperature of the concentration and cooling section in the desulfurization tower, measured by a temperature sensor, and the unit is ℃; T2 is the outlet temperature of the absorption section in the desulfurization tower, measured by a temperature sensor, and the unit is ℃.

[0050] As an implementation method, 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 0.1.

[0051] The simulation adjustment by the method of this embodiment can ensure that the desulfurization efficiency is greater than 99% and the ammonia escape is less than 0.90 mg / m 3 , it can be applied in the enterprise, and it can operate sustainably and efficiently, achieving the same operating effect as the simulation, and the sulfur dioxide content in the exhaust gas is 10~30mg / m 3 Fluctuates within the range of 0.30~0.90mg / m 3 The fluctuation range is small, so the components in the exhaust gas do not fluctuate much, which proves that the optimization control method can help the desulfurization system combining ammonia method and membrane absorption to maintain a stable and environmentally friendly operation state for a long time.

[0052] Example 3 This embodiment relates to an electronic device, which includes a memory and a processor. The memory stores a computer program. When the processor executes the computer program, the steps of the optimization control method based on ammonia method and membrane absorption combined with desulfurization described in Example 1 are implemented.

[0053] Example 4 This embodiment relates to a computer-readable storage medium having a computer program stored thereon. When the computer program is executed by a processor, the optimization and control method based on ammonia method and membrane absorption combined desulfurization described in Example 1 is implemented.

[0054] The above is only the embodiment of the present application, and the protection scope of the present application is not limited by these specific embodiments, but is determined by the claims of the present application. For those skilled in the art, the present application can have various changes and variations. Any modification, equivalent replacement, improvement, etc. made within the technical ideas and principles of the present application should be included in the protection scope of the present 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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