Thio-optimization system for coke oven gas desulfurization process

Abstract

The utility model relates to the technical field of coke oven gas desulfurization processing systems, in particular to a thio optimization system for a coke oven gas desulfurization process, which is characterized in that a thio regulation device is added on the basis of an existing HPF-method coke oven gas desulfurization system, H2S monitoring technology of the thio regulation device is utilized, and real-time ammonia water supplementing and adding technology of an ammonia adding module is matched, so that the thio optimization of the coke oven gas desulfurization process is realized. The molar ratio of NH3 in ammonia water in the desulfurization tower to H2S in the tower is promoted to be greater than 2: 1, so that the reaction is promoted to be carried out in a direction beneficial to generating ammonium sulfide, NH3 in the ammonia water can fully react with H2S in the desulfurization process, the sulfur absorption rate of the system to coke oven gas is further improved, more ammonium sulfide is generated as much as possible, and the coke oven gas desulfurization efficiency is improved. The yield of elemental sulfur after decomposition of ammonium sulfide is increased, the sulfur recovery rate is increased, less ammonium hydrosulfide is generated, the generation of low-value by-salt ammonium thiosulfate is reduced in the regeneration process, the economic benefit is increased, the ammonia loss rate of the system is reduced, the loss is reduced, the cost is saved, and the stability of the system is improved.

Description

TECHNICAL FIELD

[0001] The utility model relates to coke oven gas desulfurization processing system technical field, especially relates to a coke oven gas desulfurization process sulfur replacement optimization system. BACKGROUND

[0002] It is known that coke oven gas contains harmful impurities such as hydrogen sulfide, hydrogen cyanide and organic sulfur. Hydrogen sulfide is a highly toxic gas, which has a strong irritating effect on the human eye and respiratory tract, and high concentration inhalation can cause death. In a humid environment, hydrogen sulfide can form sulfuric acid, accelerate the corrosion of equipment materials, and shorten the service life of equipment. Hydrogen cyanide is also a highly toxic gas, which can quickly inhibit human respiratory enzymes, leading to cell suffocation and threatening life. Hydrogen cyanide aqueous solution can corrode equipment and generate iron salts in the system, causing pipeline blockage. Organic sulfur will produce sulfur dioxide and other sulfides when burning, causing air pollution. When coal gas is used as a chemical raw material, the presence of organic sulfur will also affect the purity and quality of the product. Therefore, coking plants usually configure desulfurization devices to purify coke oven gas, so that the hydrogen sulfide content in coke oven gas is less than 0.02g / m³, so that it will not cause harm to the human body and pollution to the environment when used in industry or civilian.

[0003] The existing coke oven gas desulfurization process is divided into dry desulfurization and wet desulfurization, the desulfurization catalyst used in dry desulfurization is solid, and the desulfurization catalyst used in wet desulfurization is liquid. The present application is aimed at the wet desulfurization process. In the wet desulfurization process, the desulfurization liquid containing catalyst sprayed from the top of the desulfurization tower is in counter-current contact with the gas. Under the catalytic action of the catalyst, hydrogen sulfide, hydrogen cyanide and organic sulfur in the gas are absorbed, so that the hydrogen sulfide content in the gas meets the index requirements and enters the ammonium sulfate section. The desulfurization liquid flows out from the bottom of the desulfurization tower and flows together with the compressed air from the air compressor room to enter the regeneration tower from the bottom. In the regeneration tower, it is regenerated by oxidation reaction. The regenerated ammonia water and the original catalyst flow back to the top of the desulfurization tower through the liquid level regulator and are used again as desulfurization liquid. The elemental sulfur generated after regeneration forms a sulfur foam, which floats on the top of the regeneration tower. The sulfur foam flows into the sulfur foam tank by itself due to the difference in liquid level, and is further resource utilization.

[0004] However, in the existing wet desulfurization process, the sulfur replacement is insufficient, and ammonia water will react with hydrogen sulfide to generate more ammonium hydrosulfide and part of ammonium sulfide. Ammonium hydrosulfide is weaker than ammonium sulfide in terms of sulfur absorption rate and ammonia loss rate. During the regeneration process of ammonium hydrosulfide, low-value by-product ammonium thiosulfate is generated, which increases the cost of salt extraction in the resource utilization process and also causes corrosion to the system, damaging the stability of the system. Ammonium sulfide is more easily oxidized to elemental sulfur in the regeneration tower, and the sulfur recovery rate is higher.

[0005] Therefore, there is an urgent need for a coke oven gas desulfurization system that can optimize sulfide and promote the generation of ammonium sulfide from ammonia water and hydrogen sulfide as much as possible. Utility model content

[0006] To solve the above problems, the utility model provides a coke oven gas desulfurization process sulfide optimization system, through increasing sulfide adjusting device on the basis of existing wet coke oven gas desulfurization system, using H2S monitoring technology of sulfide adjusting device, cooperate with real -time ammonia water supplement technology of ammonia module, promote the mole ratio of NH3 in ammonia water and H2S in desulfurization tower is greater than 2:1, so as to promote the reaction to the direction of generating ammonium sulfide, so that NH3 in ammonia water can fully react with H2S in the desulfurization process, and then the sulfur absorption rate of the system to coke oven gas is improved, as much as possible to generate more ammonium sulfide, improve the output of sulfur element after ammonium sulfide decomposition, improve the sulfur recovery rate, less generate ammonium hydrosulfide, reduce the generation of low -value side salt ammonium sulfite in the regeneration process, improve economic benefit, reduce the ammonia loss rate of system, reduce the loss, save the cost, improve the stability of system.

[0007] To achieve the above object, the utility model provides the following technical scheme:

[0008] A coke oven gas desulfurization process sulfide optimization system, comprising:

[0009] Precooling tower, desulfurization tower, regeneration tower, sulfur foam tank and sulfide adjusting device;

[0010] The precooling tower receives coke oven gas and carries out spray cooling treatment;

[0011] The desulfurization tower is communicated with the precooling tower through pipeline and valve, the desulfurization tower receives the precooling treated coke oven gas, and the desulfurization liquid containing catalyst in the desulfurization tower sprays from top to bottom and contacts with the coke oven gas from bottom to top, so that the coke oven gas is desulfurized;

[0012] The top and bottom of the regeneration tower are communicated with the desulfurization tower through pipeline and valve respectively, the regeneration tower receives the desulfurized solution discharged from the desulfurization tower, and after oxidation and regeneration, the regenerated desulfurization liquid is pumped into the desulfurization tower for circulation;

[0013] The sulfur foam tank is communicated with the regeneration tower, the sulfur foam tank receives the sulfur foam discharged from the regeneration tower, and collects the elemental sulfur in the sulfur foam;

[0014] The thiolation regulating device is installed on the desulfurization tower. The thiolation regulating device includes a sensor, a control cabinet, an ammonia addition module, and a catalyst addition module. The sensor is installed at the coke oven gas inlet on the desulfurization tower. The sensor monitors the H2S content in the coke oven gas. The control cabinet is connected to the sensor and the ammonia addition pump in the ammonia addition module and the catalyst addition pump in the catalyst addition module. The control cabinet receives the signal from the sensor and controls the power of the ammonia addition pump and the catalyst addition pump. The ammonia addition module and the catalyst addition module are respectively connected to the top of the desulfurization tower. The ammonia addition module and the catalyst addition module respectively replenish ammonia water and catalyst into the desulfurization tower.

[0015] As an improvement, the ammonia addition module also includes an ammonia tank, an ammonia release pump, and an ammonia tanker truck;

[0016] The ammonia tank is connected to the top of the desulfurization tower via the ammonia injection pump and pipeline;

[0017] The ammonia release pump is installed on the pipeline connecting the ammonia tank and the ammonia tanker truck. The ammonia release pump pumps the ammonia water in the ammonia tanker truck into the ammonia tank.

[0018] As an improvement, the catalyst addition module also includes an additive tank, which is connected to the top of the desulfurization tower via the addition pump and pipeline.

[0019] As an improvement, a spraying mechanism is provided at the top of the desulfurization tower. The spraying mechanism is connected to the regeneration tower, the ammonia addition module and the catalyst addition module respectively. The spraying mechanism includes several sets of spray pipes, which are arranged alternately inside the desulfurization tower.

[0020] As an improvement, the number of spray pipes is N sets, where N is an integer greater than 2, and the included angle between the central axes of adjacent spray pipes is α, where α = 180° / N.

[0021] As an improvement, the spray pipe includes a main pipe, branch pipes, and spray heads;

[0022] The main pipe is suspended radially along the desulfurization tower;

[0023] The branch pipes are symmetrically arranged on both sides of the main pipe along its axial direction, and the branch pipes are connected to the main pipe.

[0024] The nozzles are arranged at equal intervals along the axial direction of the branch pipe, and the nozzles are connected to the branch pipes. The nozzles spray desulfurization catalyst and ammonia water downwards.

[0025] As an improvement, the spraying mechanism is provided in two sets, which are arranged alternately at the top of the desulfurization tower. One set of the spraying mechanism is connected to the regeneration tower, and the other set of the spraying mechanism is connected to the ammonia addition module.

[0026] As an improvement, each spray mechanism is provided with a packing layer below it, which includes a packing mesh, packing material and a packing seat;

[0027] The packing mesh is circular in shape, and several strip grooves are evenly distributed on the packing mesh;

[0028] The packing material is evenly distributed on the packing mesh, and the packing material is fixed on the packing mesh by the packing seat;

[0029] The packing seat is circular and is detachably connected to the packing mesh.

[0030] As an improvement, the packing is arranged in a petal shape, including a core shaft at the center and petals arranged equidistantly around the core shaft. Notches are provided on the sidewalls of both the core shaft and the petals, and inserts protrude outward from the upper and lower ends of the packing.

[0031] As an improvement, the filling seat is provided with insertion holes that correspond to and cooperate with the insertion block.

[0032] The beneficial effects of this utility model are as follows:

[0033] (1) This utility model adds a thiolation adjustment device to the existing wet coke oven gas desulfurization system. By using the H2S monitoring technology of the thiolation adjustment device and the real-time ammonia water replenishment technology of the ammonia addition module, the molar ratio of NH3 in the ammonia water in the desulfurization tower to H2S in the tower is greater than 2:1, thereby promoting the reaction to be more favorable to the generation of ammonium sulfide. During the desulfurization process, NH3 in the ammonia water can fully react with H2S, thereby improving the sulfur absorption rate of the coke oven gas, generating more ammonium sulfide, increasing the output of elemental sulfur after the decomposition of ammonium sulfide, improving the sulfur recovery rate, reducing the generation of ammonium hydrosulfide, reducing the generation of low-value by-product salt ammonium thiosulfate during the regeneration process, improving economic benefits, reducing the ammonia loss rate of the system, reducing losses, saving costs, improving the stability of the system, reducing the disposal cost of desulfurization waste liquid, increasing the salt extraction revenue of desulfurization waste liquid, improving the utilization rate of catalyst, reducing the catalyst usage cost, and increasing the sales revenue of black sulfur, generating considerable economic benefits.

[0034] (2) In designing the desulfurization tower, this utility model improves the spraying mechanism of the desulfurization tower so that a set of spraying mechanisms preferably has three sets of spraying pipes, and the three sets of spraying pipes are staggered with each other, so that the desulfurization catalyst and ammonia water sprayed by the spraying mechanism are more evenly distributed and can be spread on the packing layer, thereby improving the contact rate between the desulfurization catalyst and ammonia water and the coke oven gas, thereby improving the absorption rate of H2S, and at the same time, further promoting the reaction and generation of ammonium sulfide;

[0035] (3) In the design of the packing layer, the present invention preferably adopts the plug-in fixing method, so that the packing is directly fixed to the packing mesh by plugging, thereby ensuring the rapid installation and positioning of the packing, the packing can be quickly replaced, and the packing will not be misaligned during the operation of the desulfurization tower. At the same time, the space of the packing is used as much as possible, the contact reaction area of ​​the desulfurization catalyst and ammonia water with coke oven gas is maximized, and the molar ratio of NH3 to H2S in ammonia water is greater than 2:1, which promotes the conversion rate of ammonium sulfide.

[0036] In summary, this invention has advantages such as high sulfur absorption rate, high elemental sulfur recovery rate, high system operation stability, low ammonia loss rate, and high salt extraction benefits from desulfurization waste liquid, and is especially suitable for the technical field of wet desulfurization processing systems for coke oven gas. Attached Figure Description

[0037] Figure 1 This is a schematic diagram of the system structure of this utility model;

[0038] Figure 2 This is a schematic diagram of the top structure of the desulfurization tower of this utility model;

[0039] Figure 3 This is a three-dimensional structural diagram of the spray pipe of this utility model;

[0040] Figure 4 This is a schematic diagram of the spray pipe and filler layer structure of this utility model;

[0041] Figure 5 This is a partial structural diagram of the filler layer of this utility model;

[0042] Figure 6 This is a schematic diagram of the three-dimensional structure of the filler of this utility model;

[0043] Figure 7 This is a schematic diagram of the three-dimensional installation structure of the packing seat of this utility model;

[0044] Figure 8 This is a three-dimensional structural diagram of the packing seat of this utility model.

[0045] Reference numerals: 1. Precooling tower; 2. Desulfurization tower; 21. Spraying mechanism; 21. Spray pipe; 21. Main pipe; 2111. Branch pipe; 2112. Spray head; 2113. Packing layer; 22. Packing mesh; 221. Packing; 222. Mandrel; 2221. Lobe; 2222. Notch; 2223. Insert block; 2224. Packing seat; 223. Insert hole; 2231. Threaded fastener; 2232. Fixing strip; 2233. Regeneration tower; 3. Sulfur foam tank; 4. Sulfurization adjustment device; 5. Sensor; 51. Control cabinet; 52. Ammonia addition module; 53. Ammonia addition pump; 531. Ammonia tank; 532. Ammonia discharge pump; 533. Ammonia tanker; 534. Catalyst addition module; 54. Addition pump; 542. Additive tank. Detailed Implementation

[0046] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0047] In the description of this utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing this utility model and simplifying the description, and are not intended to indicate or imply that the device or component referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model.

[0048] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this utility model, "a plurality of" means two or more, unless otherwise explicitly specified.

[0049] Example 1:

[0050] like Figure 1 As shown, a thiolation optimization system for coke oven gas desulfurization process includes:

[0051] Precooling tower 1, desulfurization tower 2, regeneration tower 3, sulfur foam tank 4, and sulfur substitution regulating device 5;

[0052] The precooling tower 1 receives coke oven gas and sprays it for cooling. A water circulation module is connected to the precooling tower 1. Cooling water is sprayed downwards from the top of the precooling tower 1 to exchange heat with the coke oven gas, thereby cooling the coke oven gas. The cooling water after heat exchange is discharged to the outside through the pipe at the bottom of the precooling tower 1. After cooling, it is circulated back to the top of the precooling tower 1 and discharged. The cooling water after heat exchange still contains some ammonia water. This part of the ammonia water is separated by the gas stripping method and enters the ammonia water clarification tank. The gas stripping method uses steam or air to strip the free ammonia gas (NH3) in the water and recovers the ammonia through gas-liquid separation. Specifically, the ammonia-containing water is heated to 80-95℃ (to increase the volatility of ammonia), and then steam or air is introduced into the stripping tower, and the ammonia gas escapes from the water, thus achieving separation.

[0053] The desulfurization tower 2 is connected to the precooling tower 1 via pipes and valves. The desulfurization tower 2 receives the precooled coke oven gas, and the desulfurization tower 2 sprays catalyst and ammonia water from top to bottom, which come into contact with the coke oven gas from bottom to top to desulfurize the coke oven gas. The desulfurization catalyst can be a PDS catalyst, HPF catalyst, etc., depending on the desulfurization process. This application uses HPF catalyst as an example. HPF catalyst is a composite catalyst composed of hydroquinone, dinuclear cobalt phthalocyanine sulfonation catalyst and ferrous sulfate. The desulfurized coke oven gas is transported to the gas ammonium desulfurization section through the pipe at the top of the desulfurization tower 2.

[0054] The desulfurization reaction process is as follows:

[0055] NH3 + H2O → NH3·H2O;

[0056] NH3·H2O + H2S → NH4HS + H2O;

[0057] 2NH3·H2O+H2S→(NH4)2S +2H2O;

[0058] NH3·H2O + HCN → NH4CN + H2O;

[0059] NH3·H2O+ NH4HS+(x-1)S (NH4)2S X +H2O;

[0060] NH4CN+(NH4)2S X NH4CNS+(NH4)2S (x-1) ;

[0061] The top and bottom of the regeneration tower 3 are connected to the desulfurization tower 2 through pipes and valves, respectively. The regeneration tower 3 receives the desulfurized solution discharged from the desulfurization tower 2, and after oxidation regeneration, the regenerated desulfurized liquid is pumped back into the desulfurization tower 2.

[0062] The regeneration reaction process is as follows:

[0063] NH4S+1 / 2O2 NH4OH + S;

[0064] (NH4)2S + 1 / 2O2 + H2O 2NH4OH + S;

[0065] (NH4)2Sx + 1 / 2O2 + H2O 2NH4OH + S;

[0066] NH4HS+2O2→(NH4)2S2O3+ H2O;

[0067] (NH4)2S2O3+O2→2(NH4)2SO4+S;

[0068] NH4CN + S → NH4SCN.

[0069] The sulfur foam tank 4 is connected to the regeneration tower 3. The sulfur foam tank 4 receives the sulfur foam discharged from the regeneration tower 3 and collects the elemental sulfur in the sulfur foam. Specifically, the sulfur foam tank separates the elemental sulfur in the sulfur-containing foam from the desulfurization liquid by gravity settling, bubble flotation or mechanical stirring, so as to achieve the enrichment and recovery of sulfur.

[0070] The thiolation regulating device 5 is installed on the desulfurization tower 2. The thiolation regulating device 5 includes a sensor 51, a control cabinet 52, an ammonia addition module 53, and a catalyst addition module 54. The sensor 51 is installed at the coke oven gas inlet of the desulfurization tower 2 and monitors the H2S content in the coke oven gas. The control cabinet 52 is connected to the sensor 51 and the ammonia addition pump 531 in the ammonia addition module 53 and the addition pump 541 in the catalyst addition module 54. The control cabinet 52 receives the signal from the sensor 51 and controls the power of the ammonia addition pump 531 and the addition pump 541. The ammonia addition module 53 and the catalyst addition module 54 are respectively connected to the top of the desulfurization tower 2 and respectively replenish ammonia water and catalyst into the desulfurization tower 2.

[0071] The ammonia addition module 53 also includes an ammonia tank 532, an ammonia release pump 533, and an ammonia tanker truck 534;

[0072] The ammonia tank 532 and the desulfurization catalyst inlet of the desulfurization tower 2 are connected through the ammonia addition pump 531 and pipeline;

[0073] The ammonia release pump 533 is installed on the pipeline connecting the ammonia tank 532 and the ammonia tanker truck 534. The ammonia release pump 533 pumps the ammonia water in the ammonia tanker truck 534 into the ammonia tank 532.

[0074] The catalyst addition module 54 also includes an additive tank 542, which is connected to the top of the desulfurization tower 2 via the addition pump 541 and a pipeline. Since the system will cause some catalyst poisoning and the discharged desulfurization waste liquid contains some catalyst during the desulfurization process, it is inevitable that the catalyst will flow out, resulting in a gradual decrease in the catalyst content. The catalyst addition module 54 can replenish the catalyst in a timely manner to ensure sufficient catalyst content in the system. The addition of catalyst is based on the following: Specifically, the catalyst addition module 54 adds catalyst synchronously with each addition of ammonia water by the ammonia addition module 53, and the amount of catalyst added is preset according to the previous catalyst usage.

[0075] It should be noted that the precooling tower, desulfurization tower, regeneration tower and sulfur foam tank 4 in this application are all conventional equipment used in the coke oven gas desulfurization process. This application only describes the differences between the above equipment and existing equipment. Other parts with the same structure will not be described in detail. You can refer to the structure of existing equipment.

[0076] Among them, the sensor 51 is preferably an infrared spectral sensor. The infrared spectral sensor utilizes the absorption characteristics of H2S molecules to infrared light of a specific wavelength (such as the 3.8-4.0 μm band) to calculate the concentration by light intensity attenuation.

[0077] When the infrared spectral sensor detects a significant increase in the H2S content in the coke oven gas input to desulfurization tower 2, the infrared spectral sensor will send a signal to the control cabinet. The processor in the control cabinet will calculate the H2S concentration through the calculation module, and then transmit the signal to the frequency converter in the ammonia addition pump 531 through the signal transmission module. The frequency converter will change the frequency of the ammonia addition pump 531 to output more ammonia water to match the H2S, ensuring that the molar ratio of NH3 in the ammonia water to H2S in the desulfurization tower 2 is greater than 2:1.

[0078] Due to the setting of the thioregulation device 5, the desulfurization tower 2 can be replenished with ammonia water in real time. The ammonia water and the desulfurization catalyst are sprayed through the corresponding spraying mechanism, which, together with the corresponding packing layer, allows H2S to react and generate ammonium sulfide as much as possible.

[0079] It is important to emphasize that, in order to ensure the stability of the desulfurization system, the control cabinet classifies the H2S concentration monitored by sensor 51 into different levels. Only when the H2S concentration fluctuates by more than 5% will the control cabinet control the ammonia pump 531 to add ammonia. For fluctuations within 5%, the desulfurization system has preset parameters to ensure that the ammonia water input to the thiolation regulating device 5 meets the H2S concentration fluctuation within 5%, thereby avoiding frequent adjustments to the ammonia water supply by the thiolation regulating device 5.

[0080] Furthermore, it should be emphasized that the thiomodification adjustment device 5 of this application is not limited to the HPF method in wet desulfurization technology. All wet desulfurization technologies that meet the application scenarios of the thiomodification adjustment device 5 of this application are within the scope of protection of this application.

[0081] Example 2:

[0082] Referring to Example 1, the difference between Example 2 and Example 1 lies in the following:

[0083] like Figure 2 , Figure 3 As shown, a spraying mechanism 21 is provided on the top of the desulfurization tower 2. The spraying mechanism 21 is connected to the regeneration tower 3, the ammonia addition module 53 and the catalyst addition module 54 respectively. The spraying mechanism 21 includes several sets of spray pipes 211, which are arranged alternately inside the desulfurization tower 2.

[0084] The number of spray pipes 211 is N sets, where N is an integer greater than 2, and the included angle between the central axes of adjacent spray pipes 211 is α, where α = 180° / N.

[0085] Furthermore, the specific spray pipe 211 includes a main pipe 2111, a branch pipe 2112, and a spray head 2113;

[0086] The main pipe 2111 is suspended along the radial direction of the desulfurization tower 2;

[0087] The branch pipe 2112 is symmetrically arranged on both sides of the main pipe 2111 along the axial direction, and the branch pipe 2112 is connected to the main pipe 2111.

[0088] The nozzles 2113 are arranged at equal intervals along the axial direction of the branch pipe 2112. The nozzles 2113 are connected to the branch pipe 2112, and the nozzles 2113 spray desulfurization catalyst and ammonia water downward.

[0089] The spraying mechanism 21 is provided in two sets, and the two sets of spraying mechanisms 21 are arranged alternately at the top of the desulfurization tower 2. One set of spraying mechanisms 21 is connected to the regeneration tower 3, and the other set of spraying mechanisms 21 is connected to the ammonia addition module 53. The ammonia water spraying area is separate from the HPF catalyst spraying area, and preferably the HPF catalyst spraying area is located above the ammonia water spraying area.

[0090] It should be noted that, unlike existing spraying mechanisms, this application adopts a multi-set spraying mode, preferably three sets of spraying pipes, which are staggered together. This allows the desulfurization catalyst and ammonia water sprayed by a single set of spraying mechanisms to cover the cross-section of the desulfurization tower, ensuring sufficient contact between the coke oven gas and the desulfurization catalyst and ammonia water, resulting in a more complete reaction.

[0091] Furthermore, each spray pipe adopts a tree-branch design, with branch pipes set on both sides of the main pipe and spray nozzles installed on the branch pipes. The branch pipes between the three sets of spray pipes are further intertwined, so that the spray nozzles on the three sets of spray pipes cooperate with each other, thereby achieving the purpose of covering the cross section of the desulfurization tower.

[0092] Example 3:

[0093] Referring to Examples 1 and 2, the difference between Example 3 and Examples 1 and 2 is that:

[0094] like Figure 4-8 As shown, each spraying mechanism 21 has a set of packing layer 22 below it, which includes a packing mesh 221, packing 222 and packing seat 223.

[0095] The packing mesh 221 is circular in shape, and a number of strip grooves 2211 are evenly distributed on the packing mesh 221;

[0096] The packing material 222 is evenly distributed on the packing mesh 221, and the packing material 222 is fixed on the packing mesh 221 by the packing seat 223;

[0097] The packing seat 223 is circular and is detachably connected to the packing mesh 221.

[0098] Furthermore, the filler 222 is arranged in a petal shape. The filler 222 includes a core shaft 2221 at the center and petals 2222 arranged equidistantly around the core shaft 2221. Notches 2223 are provided on the sidewalls of the core shaft 2221 and the petals 2222. Inserts 2224 protrude outward from the upper and lower ends of the filler 222.

[0099] Furthermore, the packing seat 223 has an insertion hole 2231 that corresponds to and cooperates with the insertion block 2224, and the packing seat 223 is installed on the packing mesh 221 by threaded fasteners 2232 and fixing strips 2233.

[0100] It should be noted that, compared with ordinary packing layers, the packing in this application adopts a petal-shaped design, which makes the contact area between the packing and the gas and liquid larger, more complete and more uniform. Furthermore, the fixing method of the packing on the packing mesh has been improved, and the packing can be quickly installed through the packing seat. During maintenance, it can be quickly replaced and maintained.

[0101] Specifically, the petal-shaped packing has blades that are distributed radially or in a stepped pattern, forming a large number of micropores and channels, which significantly increases the gas-liquid contact area (20%-40% higher than traditional Raschig rings). The gaps between the petals are evenly distributed, which reduces gas flow resistance (pressure drop) and promotes uniform liquid distribution. Furthermore, when gas passes through the tortuous path of the petal-shaped packing, the local resistance is small, and the overall pressure drop is reduced by 30%-50% compared to traditional packing (such as Raschig rings), which can reduce the energy consumption of the fan.

[0102] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.

Claims

1. A sulfurization optimization system for coke oven gas desulfurization process, characterized in that, include: Precooling tower (1), desulfurization tower (2), regeneration tower (3), sulfur foam tank (4) and sulfur regulation device (5); The precooling tower (1) receives coke oven gas for spray cooling treatment; The desulfurization tower (2) and the precooling tower (1) are connected by pipes and valves. The desulfurization tower (2) receives the coke oven gas after precooling treatment, and the catalyst-containing desulfurization liquid sprayed from the top to the bottom of the desulfurization tower (2) comes into contact with the coke oven gas from the bottom to the top to desulfurize the coke oven gas. The top and bottom of the regeneration tower (3) are connected to the desulfurization tower (2) through pipes and valves respectively. The regeneration tower (3) receives the desulfurized solution discharged from the desulfurization tower (2). After regeneration, the regenerated desulfurized liquid is pumped into the desulfurization tower (2) for recycling. The sulfur foam tank (4) is connected to the regeneration tower (3). The sulfur foam tank (4) receives the sulfur foam discharged from the regeneration tower (3) and collects the elemental sulfur in the sulfur foam. The thiolation regulating device (5) is installed on the desulfurization tower (2). The thiolation regulating device (5) includes a sensor (51), a control cabinet (52), an ammonia addition module (53), and a catalyst addition module (54). The sensor (51) is installed at the coke oven gas inlet of the desulfurization tower (2). The sensor (51) monitors the H2S content in the coke oven gas. The control cabinet (52) is connected to the sensor (51) and the ammonia addition pump (53) in the ammonia addition module (53). 1) The addition pump (541) in the catalyst addition module (54) is connected to the control cabinet (52) to receive the signal from the sensor (51) and control the power of the ammonia addition pump (531) and the addition pump (541). The ammonia addition module (53) and the catalyst addition module (54) are respectively connected to the top of the desulfurization tower (2). The ammonia addition module (53) and the catalyst addition module (54) respectively supplement ammonia water and catalyst into the desulfurization tower (2).

2. The sulfation optimization system for coke oven gas desulfurization process according to claim 1, characterized in that: The ammonia addition module (53) also includes an ammonia tank (532), an ammonia release pump (533), and an ammonia tanker (534); The ammonia tank (532) is connected to the top of the desulfurization tower (2) via the ammonia pump (531) and pipeline; The ammonia release pump (533) is installed on the pipeline connecting the ammonia tank (532) and the ammonia tanker (534). The ammonia release pump (533) pumps the ammonia water in the ammonia tanker (534) into the ammonia tank (532).

3. The sulfation optimization system for coke oven gas desulfurization process according to claim 1, characterized in that: The catalyst addition module (54) also includes an additive tank (542), which is connected to the top of the desulfurization tower (2) via the addition pump (541) and a pipeline.

4. The sulfation optimization system for coke oven gas desulfurization process according to claim 1, characterized in that: The top of the desulfurization tower (2) is provided with a spraying mechanism (21), which is connected to the regeneration tower (3), the ammonia addition module (53) and the catalyst addition module (54) respectively. The spraying mechanism (21) includes several sets of spray pipes (211), which are staggered in the desulfurization tower (2).

5. The sulfation optimization system for coke oven gas desulfurization process according to claim 4, characterized in that: The number of spray pipes (211) is N sets, where N is an integer greater than 2, and the included angle between the central axes of adjacent spray pipes (211) is α, where α = 180° / N.

6. The sulfation optimization system for coke oven gas desulfurization process according to claim 4, characterized in that: The spray pipe (211) includes a main pipe (2111), a branch pipe (2112), and a nozzle (2113). The main pipe (2111) is suspended radially along the desulfurization tower (2); The branch pipe (2112) is symmetrically arranged on both sides of the main pipe (2111) along the axial direction, and the branch pipe (2112) is connected to the main pipe (2111). The nozzles (2113) are arranged at equal intervals along the axial direction of the branch pipe (2112). The nozzles (2113) are connected to the branch pipe (2112), and the nozzles (2113) spray desulfurization catalyst and ammonia water downward.

7. The sulfation optimization system for coke oven gas desulfurization process according to claim 4, characterized in that: The spray mechanism (21) is provided in two sets. The two sets of spray mechanisms (21) are arranged alternately on the top of the desulfurization tower (2). One set of spray mechanisms (21) is connected to the regeneration tower (3), and the other set of spray mechanisms (21) is connected to the ammonia addition module (53).

8. The sulfation optimization system for coke oven gas desulfurization process according to claim 4, characterized in that: Each spray mechanism (21) of each group is provided with a packing layer (22) below it, which includes a packing mesh (221), packing (222) and a packing seat (223). The packing mesh (221) is circular, and several strip grooves (2211) are evenly distributed on the packing mesh (221). The packing material (222) is evenly distributed on the packing mesh (221), and the packing material (222) is fixed on the packing mesh (221) by the packing seat (223); The packing seat (223) is circular and is detachably connected to the packing mesh (221).

9. A sulfation optimization system for coke oven gas desulfurization process according to claim 8, characterized in that: The packing material (222) is arranged in a petal shape. The packing material (222) includes a core shaft (2221) at the center and petals (2222) arranged equidistantly around the core shaft (2221). Notches (2223) are provided on the side walls of the core shaft (2221) and the petals (2222). Inserts (2224) protrude outward from the upper and lower ends of the packing material (222).

10. A sulfation optimization system for coke oven gas desulfurization process according to claim 9, characterized in that: The filling seat (223) has a corresponding insertion hole (2231) that matches the insertion block (2224).

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