Wet desulphurization device for plasticizer tail gas
By using sodium hydroxide solution to react with sulfur-containing gas in the wet desulfurization device and regenerating it with calcium hydroxide, the problems of high operating costs and equipment blockage in the prior art are solved, and efficient desulfurization effect and cost reduction are achieved. Target.
Patent Information
- Application Number
- CN202323328897.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2023-12-07
- Publication Date
- 2025-01-14
- Estimated Expiration
- 2033-12-07
AI Technical Summary
The existing wet desulfurization device has high operating costs and equipment blockage. Especially when using sodium hydroxide solution as a desulfurization agent, it is difficult to effectively reduce costs and prevent equipment blockage.
A wet desulfurization device for plasticizer exhaust gas was designed. The sodium hydroxide solution reacted with sulfur-containing gas to generate sodium sulfate or sodium sulfite, and regenerated with calcium hydroxide to generate calcium sulfate and sodium hydroxide, which was carried out through a centrifuge. Solid-liquid separation reduces the calcium ion content of the desulfurizer, avoids precipitation and blockage, and achieves continuous supply and regeneration of sodium hydroxide solution through the design of multiple alkaline liquid storage tanks and conveying pipes.
It effectively reduces the operating costs of wet desulfurization, reduces equipment blockage, improves desulfurization efficiency and equipment working efficiency, and has good social and economic benefits.
Smart Images
Figure CN222342472U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the field of desulfurization equipment for plasticizer tail gas, in particular to a wet desulfurization device for plasticizer tail gas. Background Art
[0002] Phthalic anhydride, also known as phthalic anhydride, is a white needle-shaped crystal at room temperature. It is flammable, easy to sublimate below the boiling point, and has a special slight pungent smell. Plasticizers are the largest consumer market for phthalic anhydride, and are also widely used in the processing of synthetic resins such as synthetic rubber, polyurethane, and polystyrene. There are two main methods for the synthesis of phthalic anhydride: the naphthalene method and the ortho-method. The naphthalene method is the earliest method for producing phthalic anhydride and the earliest method for industrial production. Its raw material is tar naphthalene; naphthalene is used as the raw material to produce phthalic anhydride by fixed bed gas phase oxidation. The ortho-method is a method of producing phthalic anhydride by compressing the filtered and purified air in sequence, mixing the preheated air with vaporized o-xylene and entering a fixed bed reactor. Among them, the raw material of the naphthalene method comes from naphthalene, and the process of producing naphthalene mainly comes from the pyrolysis of coal. During the pyrolysis process, coal undergoes a series of physical and chemical changes under high temperature conditions, and finally obtains coal gas, tar and coke products. Sulfur is an important impurity element in coal. During the pyrolysis process of coal, it will undergo complex migration and transformation, and enter the solid-liquid-gas three-phase product. The sulfur element that migrates to tar and coke will cause the quality of tar and coke to decline, affecting downstream utilization. The form of sulfur in coal is divided into inorganic sulfur and organic sulfur. Inorganic sulfur mainly includes sulfide and sulfate and trace elemental sulfur; organic sulfur mainly includes thiophene sulfide, mercaptan sulfide, thioether sulfide, sulfone and disulfide. The tar obtained by pyrolysis will carry some organic sulfur. Tar is distilled to obtain industrial naphthalene, and some organic sulfur will inevitably be mixed into industrial naphthalene.
[0003] Phthalic anhydride produced by the naphthalene process will inevitably introduce some organic sulfur. After the phthalic anhydride is fully reacted as an esterification raw material, most of the organic sulfur will be discharged to the outside along with the tail gas. The mainstream processes for desulfurization in the existing process are divided into two categories: dry desulfurization and wet desulfurization. Dry flue gas desulfurization refers to the use of powdered or granular absorbents, adsorbents or catalysts to remove sulfur-containing gases in flue gas. The sulfur components in sulfur-containing gases mainly exist in the form of sulfur dioxide and sulfur trioxide. Wet desulfurization uses a gas-liquid reaction to react a solution containing a desulfurizer with a sulfur-containing gas to remove the sulfur component in the sulfur-containing gas. It has a fast desulfurization reaction speed, high efficiency, and high desulfurizer utilization rate. The representative process of wet desulfurization is to use calcium hydroxide slurry to spray into the absorption tower, and to contact the sulfur-containing gas entering the absorption tower in countercurrent, so that the sulfur component in the sulfur-containing gas reacts with strong calcium oxide to produce calcium sulfite and calcium sulfate, and the calcium sulfite and calcium sulfate are both solid substances that are insoluble in water, thereby achieving the removal of the sulfur component in the sulfur-containing gas. Of course, sodium hydroxide solution can also be used as a desulfurization agent to achieve the above process. The disadvantage of using calcium hydroxide slurry as a desulfurization agent is that the generated calcium sulfite and calcium sulfate are both solid substances that are insoluble in water, which can easily cause system blockage, especially after a large amount of calcium sulfite and calcium sulfate are enriched in the packing layer in the absorption tower, it is more difficult to clean. The disadvantage of using sodium hydroxide solution as a desulfurization agent is the problem of excessively high operating costs due to the high unit price of sodium hydroxide. Therefore, there is an improvement motivation in the prior art regarding wet desulfurization to reduce operating costs and reduce the situation of equipment blockage to meet market demand. Summary of the invention
[0004] In view of the deficiencies in the prior art, the utility model provides a wet desulfurization device for plasticizer tail gas, which can reduce the operating cost of wet desulfurization and reduce the possibility of equipment clogging, and is used to overcome the defects in the prior art.
[0005] The technical scheme adopted by the utility model is as follows: a wet desulfurization device for plasticizer tail gas comprises a distillation tower, wherein the distillation tower comprises a tower body and a wire mesh coalescer, a nozzle and a packing layer which are sequentially arranged in the tower body from top to bottom, an alkali liquid storage tank is arranged below the tower body, the bottom end of the tower body and the top end of the alkali liquid storage tank are connected through a first absorption liquid delivery pipe, a first regulating valve is arranged on the first absorption liquid delivery pipe, an outlet end of a second absorption liquid delivery pipe is arranged on the inlet end of the nozzle, the inlet end of the second absorption liquid delivery pipe is connected with the bottom end of the alkali liquid storage tank, a second regulating valve and a first booster pump are arranged on the second absorption liquid delivery pipe, an inlet end of a first regeneration liquid delivery pipe is arranged on the bottom end of the alkali liquid storage tank, a top end of a stirring tank is arranged on the outlet end of the first regeneration liquid delivery pipe, a centrifuge is connected to the bottom end of the stirring tank, a stirring shaft is arranged on the stirring tank, a stirring blade is arranged on the stirring shaft in the stirring tank, a stirring motor is transmission-connected on the stirring shaft, and a first pH sensor and a first liquid level sensor are arranged on the alkali liquid storage tank.
[0006] Preferably, the first regeneration liquid delivery pipe is provided with a second booster pump, a liquid flow sensor, a third regulating valve and an outlet end of the circulating liquid delivery pipe in sequence along the direction from the alkali solution storage tank to the stirring tank, the liquid phase outlet end of the centrifuge is connected with a buffer tank, the bottom end of the buffer tank is connected with the inlet end of the circulating liquid delivery pipe, the circulating liquid delivery pipe is provided with a third booster pump, the inlet end of the second regeneration liquid delivery pipe and a first stop valve in sequence along the direction from close to the buffer tank to far away from the buffer tank, the second regeneration liquid delivery pipe is provided with a second stop valve, and the inlet end of the second regeneration liquid delivery pipe is connected with the top end of the alkali solution storage tank.
[0007] Preferably, the number of the alkali liquid storage tanks is several, each alkali liquid storage tank is connected to the first absorption liquid delivery pipe through the third absorption liquid delivery pipe, each alkali liquid storage tank is connected to the second absorption liquid delivery pipe through the fourth absorption liquid delivery pipe, each alkali liquid storage tank is connected to the second regeneration liquid delivery pipe through the third regeneration liquid delivery pipe, each alkali liquid storage tank is connected to the first regeneration liquid delivery pipe through the fourth regeneration liquid delivery pipe, and the third absorption liquid delivery pipe, the fourth absorption liquid delivery pipe, the third regeneration liquid delivery pipe and the fourth regeneration liquid delivery pipe are respectively provided with a fifth stop valve.
[0008] Preferably, the stirring tank and the centrifuge are connected via a suspension delivery pipe, a sixth stop valve is provided on the suspension delivery pipe, and a second liquid level sensor is provided on the buffer tank.
[0009] Preferably, a calcium hydroxide storage tank is arranged above the stirring tank, a powder conveying pipe is arranged between the calcium hydroxide storage tank and the stirring tank, and the powder conveying pipe is sequentially provided with a third stop valve, a first feeder, a weighing tank, a second feeder and a fourth stop valve along the direction from the calcium hydroxide storage tank to the stirring tank, and the first feeder and the second feeder are respectively transmission-connected with a feeder motor.
[0010] Preferably, a third liquid level sensor is provided on the tower body below the packing layer.
[0011] The beneficial effects of the utility model are as follows: first, the sodium hydroxide solution used as a desulfurizing agent in the utility model reacts with sulfur-containing gas to generate sodium sulfate or sodium sulfite, thereby reducing the desulfurization effect. The present solution utilizes a desulfurizing agent containing sodium sulfate or sodium sulfite to react with calcium hydroxide to generate calcium sulfate and sodium hydroxide or calcium sulfite and sodium hydroxide, and then undergoes solid-liquid separation through a centrifuge to achieve the regeneration of the sodium hydroxide used as a desulfurizing agent. It should be noted that the regenerated sodium hydroxide still contains a small amount of sodium sulfate or sodium sulfite, that is, the amount of calcium hydroxide in the regeneration reaction is insufficient, in order to reduce the calcium ion content in the sodium hydroxide solution after regeneration, thereby reducing the phenomenon that the regenerated desulfurizing agent directly generates calcium sulfate or calcium sulfite precipitation after contacting the tail gas, thereby reducing the blockage of the overall equipment, and since the sodium hydroxide solution used as a desulfurizing agent is regenerated using calcium hydroxide during the period, the consumption of sodium hydroxide is reduced, and the operating cost of wet desulfurization is also reduced.
[0012] Secondly, the utility model alkali solution storage tank is provided with a first pH sensor and a first liquid level sensor; installing the first pH sensor is convenient for feeding back corresponding pH parameters, and installing the first liquid level sensor is convenient for feeding back corresponding liquid level parameters.
[0013] Finally, the first regeneration liquid delivery pipe described in the utility model is provided with a second booster pump, a liquid flow sensor, a third regulating valve and an outlet end of the circulating liquid delivery pipe in sequence along the direction from the alkali solution storage tank to the stirring tank. The installation of the liquid flow sensor facilitates the feedback of flow parameters.
[0014] The utility model has the advantages of simple structure, convenient operation, ingenious design, greatly improved working efficiency, good social and economic benefits, and is a product that is easy to promote and use. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 It is a structural schematic diagram of the utility model.
[0016] Figure 2 for Figure 1 A partial enlarged schematic diagram of detail A. DETAILED DESCRIPTION
[0017] like Figure 1 and Figure 2 As shown, a wet desulfurization device for plasticizer tail gas includes a distillation tower, wherein the distillation tower includes a tower body 1 and a wire mesh coalescer 2, a nozzle 3 and a packing layer 4 arranged in sequence from top to bottom in the tower body 1, an alkali liquid storage tank 5 is arranged below the tower body 1, the bottom end of the tower body 1 and the top end of the alkali liquid storage tank 5 are connected through a first absorption liquid delivery pipe 6, a first regulating valve 7 and a second pH sensor 45 are arranged on the first absorption liquid delivery pipe 6, an outlet end of a second absorption liquid delivery pipe 8 is arranged on the inlet end of the nozzle 3, and the inlet end of the second absorption liquid delivery pipe 8 and the inlet end of the alkali liquid storage tank 5 are connected. The bottom ends are connected, a second regulating valve 9 and a first booster pump 10 are arranged on the second absorption liquid delivery pipe 8, an inlet end of a first regeneration liquid delivery pipe 11 is arranged on the bottom end of the alkali solution storage tank 5, a top end of a stirring tank 12 is arranged on the outlet end of the first regeneration liquid delivery pipe 11, a centrifuge 13 is connected to the bottom end of the stirring tank 12, a stirring shaft 14 is arranged on the stirring tank 12, a stirring blade 15 is arranged on the stirring shaft 14 in the stirring tank 12, a stirring motor 16 is transmission-connected to the stirring shaft 14, and a first pH sensor 17 and a first liquid level sensor 18 are arranged on the alkali solution storage tank 5.
[0018] The first regeneration liquid delivery pipe 11 is provided with a second booster pump 19, a liquid flow sensor 20, a third regulating valve 21 and the outlet end of the circulating liquid delivery pipe 22 in sequence along the direction from the alkali solution storage tank 5 to the stirring tank 12. The liquid phase outlet end of the centrifuge 13 is connected with a buffer tank 23, and the bottom end of the buffer tank 23 is connected with the inlet end of the circulating liquid delivery pipe 22. The circulating liquid delivery pipe 22 is provided with a third booster pump 24, the inlet end of the second regeneration liquid delivery pipe 25 and a first stop valve 26 in sequence along the direction from close to the buffer tank 23 to far away from the buffer tank 23. The second regeneration liquid delivery pipe 25 is provided with a second stop valve 27, and the inlet end of the second regeneration liquid delivery pipe 25 is connected with the top of the alkali solution storage tank 5.
[0019] In order to improve the continuity of the supply of sodium hydroxide solution, the number of alkali liquid storage tanks 5 described in this product is several, each alkali liquid storage tank 5 and the first absorption liquid delivery pipe 6 are connected through the third absorption liquid delivery pipe 28, each alkali liquid storage tank 5 and the second absorption liquid delivery pipe 8 are connected through the fourth absorption liquid delivery pipe 29, each alkali liquid storage tank 5 and the second regeneration liquid delivery pipe 25 are connected through the third regeneration liquid delivery pipe 30, each alkali liquid storage tank 5 and the first regeneration liquid delivery pipe 11 are connected through the fourth regeneration liquid delivery pipe 31, and the third absorption liquid delivery pipe 28, the fourth absorption liquid delivery pipe 29, the third regeneration liquid delivery pipe 30 and the fourth regeneration liquid delivery pipe 31 are respectively provided with a fifth stop valve 32. The stirring tank 12 and the centrifuge 13 are connected through the suspension delivery pipe 33, the suspension delivery pipe 33 is provided with a sixth stop valve 34, and the buffer tank 23 is provided with a second liquid level sensor 35.
[0020] A calcium hydroxide storage tank 36 is arranged above the stirring tank 12, a powder delivery pipe 37 is arranged between the calcium hydroxide storage tank 36 and the stirring tank 12, and the powder delivery pipe 37 is sequentially provided with a third stop valve 38, a first feeder 39, a weighing tank 40, a second feeder 41 and a fourth stop valve 42 along the direction from the calcium hydroxide storage tank 36 to the stirring tank 12, and the first feeder 39 and the second feeder 41 are respectively connected to a feeder motor 43. A third liquid level sensor 44 is arranged on the tower body 1 below the packing layer 4.
[0021] The use of this product is as follows: Figure 1 and Figure 2 As shown, the sodium hydroxide solution of the configured concentration is transported to one of the alkali liquid storage tanks 5. When the first liquid level sensor 18 on the alkali liquid storage tank 5 reaches the preset height, the sodium hydroxide solution is stopped from being transported to the alkali liquid storage tank 5; then the sodium hydroxide solution of the configured concentration is added to another alkali liquid storage tank 5 until the first liquid level sensor 18 on the alkali liquid storage tank 5 reaches the preset height; the above operation is fully performed until all the alkali liquid storage tanks 5 are loaded with sodium hydroxide solution of the preset liquid level. Then the preset weight of powdered calcium hydroxide is placed in the calcium hydroxide storage tank 36. When the above operation is completed, the preparation work of this product is completed, and the formal operation of this product can be carried out. The specific steps are as follows:
[0022] S1, one of the alkali liquid storage tanks 5 is in working state, and the remaining alkali liquid storage tanks 5 are in standby state; after turning on the first booster pump 10, the alkali liquid storage tank 5 in working state transports the sodium hydroxide solution atomized by the nozzle 3 to the inner cavity of the tower body 1 through the second absorption liquid delivery pipe 8; the sodium hydroxide solution moves downward along the inner cavity of the tower body 1 under the action of its own gravity to form a descending liquid flow, and at the same time, the tower body 1 below the packing layer 4 receives the sulfur-containing gas transported from the upstream, and the sulfur-containing gas and the sodium hydroxide solution are fully contacted in countercurrent under the resistance of the packing layer 4, and the sulfur component in the sulfur-containing gas reacts with the sodium hydroxide solution to produce sodium sulfate solution or sodium sulfite solution and flows to the bottom of the tower body 1 along with the descending liquid flow and is sent back to the alkali liquid storage tank 5 in working state through the first absorption liquid delivery pipe 6 to form a circulation, during which parameters are fed back through the second pH sensor 45 and the first pH sensor 17.
[0023] S2. When the parameters fed back by the second pH sensor 45 and / or the parameters fed back by the first pH sensor 17 deviate from the preset range, the product needs to be switched. By operating the fifth stop valve 32 on the corresponding third absorption liquid delivery pipe 28 and the fifth stop valve 32 on the corresponding fourth absorption liquid delivery pipe 29, one of the alkali liquid storage tanks 5 that was originally in the standby state is connected to the second absorption liquid delivery pipe 8 and the inner cavity of the tower body 1. The alkali liquid storage tank 5 that was originally in the standby state is now in the working state; the alkali liquid storage tank 5 that was originally in the working state is now in the alkali liquid storage tank 5 to be regenerated; the alkali liquid storage tank 5 that is now in the working state continues to execute step S1, and keeps supplying sodium hydroxide solution to the inner cavity of the tower body 1 to meet the demand of upstream gas desulfurization.
[0024] S3, according to the liquid level height fed back by the first liquid level sensor 18 on the alkali liquid storage tank 5 in the state of waiting for regeneration, a part of the solution medium to be regenerated in the alkali liquid storage tank 5 in the state of waiting for regeneration is transported to the stirring tank 12 through the first regeneration liquid delivery pipe 11, when the cumulative flow fed back by the liquid flow sensor 20 reaches the preset value; stop continuing to transport the solution medium to be regenerated to the stirring tank 12; turn on the stirring motor 16, at the same time, the calcium hydroxide storage tank 36 continuously transports powdered calcium hydroxide to the weighing tank 40 until the weighing tank 40 reaches a preset weight, and after the weighing tank 40 is weighed, the weighing tank 40 continuously transports the weighed calcium hydroxide to the stirring tank 12, and when the powdered calcium hydroxide enters the stirring tank, the The sodium sulfate solution or sodium sulfite in the regenerated solution medium reacts with the calcium hydroxide dissolved in the solution medium to produce calcium sulfate or calcium sulfite precipitate and suspends it in the solution medium in the stirring tank 12 to form a suspension. When all the calcium hydroxide is added and stirring is maintained for a preset time, the seventh stop valve 47 is opened, and the suspension is transported to the centrifuge 13. The solid phase of the suspension is a large amount of calcium sulfate or calcium sulfite precipitate, and the liquid phase of the suspension is a sodium hydroxide solution containing dissolved calcium hydroxide. The solid phase of the suspension is discharged through the solid phase outlet of the centrifuge 13, and the liquid phase of the suspension is discharged into the buffer tank 23 through the liquid phase outlet of the centrifuge 13.
[0025] S4, the buffer tank 23 receives the solution delivered through the liquid phase outlet of the centrifuge 13 for the first time. When the buffer tank 23 receives all the solutions, the third booster pump 24 is turned on to send the received solution back to the stirring tank 12. When the stirring tank 12 receives all the solutions from the buffer tank 23, the stirring motor 16 is turned on to continuously stir the solution in the stirring tank 12 with the stirring blade 15. Then the alkali liquid storage tank 5 in the state to be regenerated delivers the remaining solution medium to be regenerated to the stirring tank 12. The remaining solution medium to be regenerated reacts with the continuously stirred sodium hydroxide solution with dissolved calcium hydroxide to form calcium sulfate or calcium sulfite precipitation again and form a suspension. At this time, the suspension still contains a small amount of sodium sulfate or sodium sulfite, but most of the suspension has been converted into sodium hydroxide. Finally, the suspension is transported to the centrifuge 13, and the solid phase of the suspension is still discharged from the solid phase outlet of the centrifuge 13, while the liquid phase of the suspension is still discharged from the liquid phase outlet to the buffer tank 23.
[0026] S5, the buffer tank 23 receives the solution delivered through the liquid phase outlet of the centrifuge 13 for the first time. After the buffer tank 23 receives all the solution, the third booster pump 24 is turned on to send the received solution back to the alkali solution storage tank 5 in the state to be regenerated. When the alkali solution storage tank 5 in the state to be regenerated receives all the solution, the alkali solution storage tank 5 originally in the state to be regenerated is converted into the alkali solution storage tank 5 in the standby state.
[0027] S6. Repeat steps S1 to S6. During this period, the consumption of the powdered calcium hydroxide in the calcium hydroxide storage tank 36 needs to be recorded according to the information fed back by the weighing tank 40, and the corresponding weight of powdered calcium hydroxide is added to the calcium hydroxide storage tank 36 in time.
[0028] According to this embodiment, the sodium hydroxide solution as a desulfurizing agent reacts with the sulfur-containing gas to generate sodium sulfate or sodium sulfite, which leads to a decrease in the desulfurization effect. In this scheme, the desulfurizing agent containing sodium sulfate or sodium sulfite reacts with calcium hydroxide to generate calcium sulfate and sodium hydroxide or calcium sulfite and sodium hydroxide, and then undergoes solid-liquid separation through a centrifuge 13 to achieve the regeneration of the sodium hydroxide as a desulfurizing agent. It should be noted that the regenerated sodium hydroxide still contains a small amount of sodium sulfate or sodium sulfite, that is, the amount of calcium hydroxide in the regeneration reaction is insufficient, which is to reduce the calcium ion content in the sodium hydroxide solution after regeneration, thereby reducing the phenomenon that the regenerated desulfurizing agent directly generates calcium sulfate or calcium sulfite precipitation after contacting the tail gas, thereby reducing the blockage of the overall equipment and because the sodium hydroxide solution as a desulfurizing agent is regenerated using calcium hydroxide during the period, the consumption of sodium hydroxide is reduced and the operating cost of wet desulfurization is also reduced.
[0029] The embodiments described above are only preferred embodiments of the present invention and are not intended to limit the scope of implementation of the present invention. Therefore, any equivalent changes or modifications made based on the structures, features and principles described in the patent scope of the present invention should be included in the patent application scope of the present invention.
Claims
1. A wet desulfurization device for plasticizer tail gas, comprising a distillation tower, wherein the distillation tower comprises a tower body (1) and a wire mesh coalescer (2), a nozzle (3) and a packing layer (4) arranged in sequence from top to bottom in the tower body (1), characterized in that: An alkali liquid storage tank (5) is arranged below the tower body (1), the bottom end of the tower body (1) and the top end of the alkali liquid storage tank (5) are connected via a first absorption liquid delivery pipe (6), a first regulating valve (7) is arranged on the first absorption liquid delivery pipe (6), an outlet end of a second absorption liquid delivery pipe (8) is arranged on the inlet end of the nozzle (3), the inlet end of the second absorption liquid delivery pipe (8) is connected to the bottom end of the alkali liquid storage tank (5), a second regulating valve (9) and a first booster pump (10) are arranged on the second absorption liquid delivery pipe (8), and the alkali liquid storage tank (5) is connected to the bottom end of the alkali liquid storage tank (5). ) is provided at the bottom end of the regeneration liquid delivery pipe (11), the top end of the stirring tank (12) is provided at the outlet end of the first regeneration liquid delivery pipe (11), the bottom end of the stirring tank (12) is connected to a centrifuge (13), a stirring shaft (14) is provided on the stirring tank (12), a stirring blade (15) is provided on the stirring shaft (14) in the stirring tank (12), a stirring motor (16) is transmission-connected to the stirring shaft (14), and a first pH sensor (17) and a first liquid level sensor (18) are provided on the alkali solution storage tank (5).
2. The wet desulfurization device for plasticizer tail gas according to claim 1, characterized in that: The first regeneration liquid delivery pipe (11) is provided with a second booster pump (19), a liquid flow sensor (20), a third regulating valve (21) and an outlet end of a circulating liquid delivery pipe (22) in sequence along the direction from the alkali liquid storage tank (5) to the stirring tank (12); the liquid phase outlet end of the centrifuge (13) is connected to a buffer tank (23); the bottom end of the buffer tank (23) is connected to the inlet end of the circulating liquid delivery pipe (22); the circulating liquid delivery pipe (22) is provided with a third booster pump (24), an inlet end of a second regeneration liquid delivery pipe (25) and a first stop valve (26) in sequence along the direction from close to the buffer tank (23) to far away from the buffer tank (23); the second regeneration liquid delivery pipe (25) is provided with a second stop valve (27); and the inlet end of the second regeneration liquid delivery pipe (25) is connected to the top end of the alkali liquid storage tank (5).
3. The wet desulfurization device for plasticizer tail gas according to claim 2, characterized in that: The number of the alkali liquid storage tanks (5) is several, each alkali liquid storage tank (5) is connected to the first absorption liquid delivery pipe (6) via a third absorption liquid delivery pipe (28), each alkali liquid storage tank (5) is connected to the second absorption liquid delivery pipe (8) via a fourth absorption liquid delivery pipe (29), each alkali liquid storage tank (5) is connected to the second regeneration liquid delivery pipe (25) via a third regeneration liquid delivery pipe (30), each alkali liquid storage tank (5) is connected to the first regeneration liquid delivery pipe (11) via a fourth regeneration liquid delivery pipe (31), and the third absorption liquid delivery pipe (28), the fourth absorption liquid delivery pipe (29), the third regeneration liquid delivery pipe (30), and the fourth regeneration liquid delivery pipe (31) are each provided with a fifth stop valve (32).
4. The wet desulfurization device for plasticizer tail gas according to claim 2, characterized in that: The stirring tank (12) and the centrifuge (13) are connected via a suspension delivery pipe (33), a sixth stop valve (34) is provided on the suspension delivery pipe (33), and a second liquid level sensor (35) is provided on the buffer tank (23).
5. The wet desulfurization device for plasticizer tail gas according to claim 1, characterized in that: A calcium hydroxide storage tank (36) is arranged above the stirring tank (12); a powder delivery pipe (37) is arranged between the calcium hydroxide storage tank (36) and the stirring tank (12); a third stop valve (38), a first feeder (39), a weighing tank (40), a second feeder (41) and a fourth stop valve (42) are arranged in sequence on the powder delivery pipe (37) in a direction from the calcium hydroxide storage tank (36) to the stirring tank (12); and a feeder motor (43) is respectively connected to the first feeder (39) and the second feeder (41).
6. The wet desulfurization device for plasticizer tail gas according to claim 1, characterized in that: A third liquid level sensor (44) is provided on the tower body (1) below the packing layer (4).