CN219072543U - Absorption system for renewable amine desulfurization - Google Patents
Absorption system for renewable amine desulfurization Download PDFInfo
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- CN219072543U CN219072543U CN202320130076.0U CN202320130076U CN219072543U CN 219072543 U CN219072543 U CN 219072543U CN 202320130076 U CN202320130076 U CN 202320130076U CN 219072543 U CN219072543 U CN 219072543U
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Abstract
The utility model relates to the technical field of wet flue gas desulfurization, and particularly discloses an absorption system for a renewable amine method desulfurization so as to absorb sulfur dioxide in sulfur-containing flue gas, wherein the absorption system comprises a primary absorption tower, a secondary absorption tower, a rich liquid storage tank, a lean liquid storage tank and a transfer tank, wherein the primary absorption tower is a spray and filler composite tower, a lower air inlet of the primary absorption tower is used for feeding the sulfur-containing flue gas, a lower liquid outlet of the primary absorption tower is communicated with the rich liquid storage tank, an upper air outlet of the primary absorption tower is communicated with a lower air inlet of the secondary absorption tower, and an upper liquid inlet of the primary absorption tower is communicated with a lower liquid outlet of the secondary absorption tower; the upper gas outlet of the secondary absorption tower discharges flue gas through a demister, and the upper liquid inlet of the secondary absorption tower is communicated with a lean liquid storage tank. The absorption system can effectively improve desulfurization efficiency, increase rich liquor concentration and improve economic benefit.
Description
Technical Field
The utility model relates to the technical field of wet flue gas desulfurization, in particular to an absorption system for renewable amine desulfurization.
Background
The renewable amine desulfurization technology is an emerging flue gas desulfurization technology, has the characteristics of high desulfurization efficiency, recyclable absorbent, no secondary pollution and the like, regenerates and obtains sulfur dioxide gas with higher purity, can further process a series of sulfur products (such as liquid sulfur dioxide), has high production efficiency, is easy to form a certain production scale, and has better economic value.
However, the existing mainstream wet flue gas desulfurization technology has the defect of low desulfurization efficiency, and the application of the existing mainstream wet flue gas desulfurization technology to the renewable amine desulfurization technology can lower the desulfurization efficiency. The conventional method for increasing the operating liquid-gas ratio can improve the desulfurization rate, but the concentration of the produced absorption rich liquid is lower, so that the load of a desorption system is indirectly increased, and the energy consumption of the whole system is increased. As a key link for capturing sulfur dioxide in flue gas, the improvement of the absorption efficiency of the absorption system is important as well as the improvement of the sulfur content of the absorption rich liquid, so that the improvement of the efficiency and the economic benefit of the whole renewable amine desulfurization technology is important how to design the absorption system matched with the renewable amine desulfurization technology on the premise of not increasing the cost and the operation difficulty.
Disclosure of Invention
The utility model aims to provide an absorption system for the renewable amine desulfurization so as to absorb sulfur dioxide in sulfur-containing flue gas, and the absorption system can effectively improve the desulfurization efficiency and the economic benefit.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
the absorption system for the sulfur dioxide in the sulfur-containing flue gas by the renewable amine method comprises a first-stage absorption tower, a second-stage absorption tower, a rich liquid storage tank and a lean liquid storage tank, wherein the first-stage absorption tower is a spraying and filling composite tower, a lower air inlet of the first-stage absorption tower is used for feeding the sulfur-containing flue gas, a lower liquid outlet of the first-stage absorption tower is communicated with the rich liquid storage tank, an upper air outlet of the first-stage absorption tower is communicated with a lower air inlet of the second-stage absorption tower, and an upper liquid inlet of the first-stage absorption tower is communicated with a lower liquid outlet of the second-stage absorption tower; the upper gas outlet of the secondary absorption tower discharges flue gas through a demister, and the upper liquid inlet of the secondary absorption tower is communicated with a lean liquid storage tank.
As a preferable scheme, a plurality of nozzles are arranged below the first spraying layer from top to bottom in the first-stage absorption tower so as to uniformly spray the liquid entering from the upper liquid inlet of the first-stage absorption tower downwards; the first-stage absorption tower is internally provided with a plurality of spray nozzles from top to bottom, and the upper side and the lower side of the second layer and the lower spray layer are respectively provided with a plurality of spray nozzles so as to spray liquid entering from the upper liquid inlet of the first-stage absorption tower in the upper direction and the lower direction respectively; the peripheral nozzles are obliquely arranged towards the central axis of the primary absorption tower, and the installation inclination angle of the nozzles is smaller than one half of the atomization angle, so that a large amount of fog drops sprayed by the nozzles are not sprayed on the inner wall of the primary absorption tower.
As a preferable scheme, the upper side and the lower side of the spraying layer are respectively provided with a plurality of nozzles so as to spray the liquid entering from the upper liquid inlet of the primary absorption tower in the upper direction and the lower direction respectively.
As a preferred embodiment, the packing absorption section is a structured packing section.
As a preferable scheme, the system further comprises a static mixer, wherein the upper liquid inlet of the primary absorption tower is communicated with the lower liquid outlet of the secondary absorption tower through the static mixer, and the rich liquid storage tank is communicated with the static mixer.
As a preferable scheme, the rich liquid storage tank is communicated with the static mixer through a circulating pump.
As a preferable scheme, the static mixer is communicated with the lower liquid outlet of the secondary absorption tower through a transfer pump.
As a preferable scheme, the transfer pump is communicated with the lower liquid outlet of the secondary absorption tower through a transfer tank.
As a preferable scheme, the secondary absorption tower is communicated with the lean liquid storage tank through a lean liquid delivery pump.
As a preferable scheme, a solid cone nozzle is arranged in the lower air inlet of the primary absorption tower, one end of the solid cone nozzle is connected with a circulating pump outlet pipeline, and the other end of the solid cone nozzle faces into the primary absorption tower to spray atomized liquid drops along the flow direction of sulfur-containing flue gas.
The secondary absorption tower is a packed tower, the diameter of the primary absorption tower is larger than or equal to that of the secondary absorption tower, the packed tower and the primary absorption tower are arranged in series, and both gas phase and liquid phase (flue gas and absorption liquid) are contacted in a countercurrent mode.
As a preferable scheme, the spraying path of the solid conical nozzle is tangential to the lower air inlet of the primary absorption tower, the nozzles on the spraying layer should be prevented from being sprayed to the inner wall of the tower as far as possible, namely, the peripheral nozzles are obliquely arranged towards the central axis of the primary absorption tower, the installation inclination angle of the nozzles is smaller than one half of the atomization angle, and the specific installation angle is based on that the droplets sprayed by the nozzles are not sprayed to the inner wall of the tower in a space with a spraying layer interval.
As a preferable mode, the fresh absorption liquid component is ethylenediamine 0.25-0.35 mol.L -1 And adding a proper amount of phosphoric acid to adjust the pH value of the solution to be between 6.5 and 7.5.
As a preferable scheme, after the absorption system stably operates, the concentration of tetravalent sulfur in the absorption lean solution is 0.1-0.18 mol.L -1 The concentration of tetravalent sulfur in the absorption rich liquid is 0.2-0.3 mol.L -1 Between them.
Compared with the prior art, the utility model has the following beneficial effects:
the utility model comprises a first-stage absorption tower, a second-stage absorption tower, a demister, a lean solution storage tank, a rich solution storage tank, a static mixer and the like, and can be arranged in a flue gas purification system of a coal-fired boiler. The absorption system adopts a chemical absorption method, and adopts a gas-liquid countercurrent contact mode of partial circulation of absorption liquid to dissolve and absorb sulfur dioxide in flue gas into amine-containing solution so as to reduce the emission concentration of sulfur dioxide in flue gas, and rich liquid generated by absorption can be heated and regenerated into lean liquid and returned to the absorption system, thereby realizing the recycling of the absorption liquid.
In the utility model, the absorption liquid from the bottom of the secondary absorption tower and the absorption liquid from the circulating pump are fully mixed by a static mixer, and then enter the top of the primary absorption tower to be used as the absorption liquid. Recycling a part of rich liquid at the bottom of the primary absorption tower back to the top of the primary absorption tower as absorption liquid, and from the aspect of hydrodynamics: the liquid-gas ratio in the first-stage absorption tower is increased, so that the surface area of fog drops and the surface infiltration area of filler are increased, the thickness of a flowing boundary layer can be reduced to a certain extent, and the gas-liquid mass transfer coefficient is indirectly improved. From the mass transfer perspective: although the rich liquid circulation can improve the tetravalent sulfur content in the liquid phase and cause the increase of the sulfur dioxide partial pressure at the gas-liquid interface, the average mass transfer driving force in the absorption tower is still larger because the sulfur dioxide content in the gas phase main body of the flue gas in the first-stage absorption tower is higher, so that the sufficient mass transfer rate can be maintained, and after the flue gas leaves the first-stage absorption tower, the sulfur dioxide concentration in the gas phase main body is greatly reduced, and then enters the second-stage absorption tower, so that the sufficient high mass transfer driving force can be provided by using the lean liquid with low concentration in the second-stage absorption tower; the absorption efficiency of the whole system can be effectively improved by combining the two.
The primary absorption tower is arranged as a spraying and packing composite tower, a plurality of spraying layers are arranged above the inside of the primary absorption tower, and regular packing sections are arranged below the inside of the primary absorption tower, so that the redundancy of a liquid storage unit can be effectively improved, and system fluctuation (such as flue gas concentration change, desorption system processing capacity change and the like) can be more flexibly handled; compared with a pure packed tower, the combination of spraying and packing can reduce the gas flow resistance, adapt to the scene of large flue gas flow, and reduce the power consumption of a fan. In addition, the spraying section has no inner component, and the falling liquid drops directly wash the structured packing, so that the packing can be effectively prevented from being blocked by salt enrichment or solid impurities in the absorption liquid, and the gas-liquid contact dead zone in the packing can be effectively reduced.
In the spray section of the primary absorption tower, the spray layers are uniformly provided with the nozzles up and down, so that liquid can be sprayed upwards and downwards, and the opposite nozzles on the adjacent spray layers are staggered, so that the collision probability of sprayed liquid drops can be increased, on one hand, the surface updating frequency of the liquid drops can be enhanced, and on the basis of the surface updating theory, the mass transfer efficiency can be remarkably improved; on the other hand, the droplets can be broken up by collision, so that the droplets are smaller, the contact surface (mass transfer surface) is larger, and the mass transfer efficiency can be improved. In addition, the arrangement can increase the flow path length of the liquid drop, prolong the residence time of the liquid drop and ensure more sufficient mass transfer absorption.
The top of the spraying section does not need to be provided with a demisting section like a conventional spraying tower, and because mist carried by air flow can be effectively captured by the secondary absorption tower, the secondary absorption tower not only serves as absorption equipment, but also plays a demisting role, the final product is not influenced, and the rationality of the layout of the utility model is embodied.
The packing section of the primary absorption tower is of a regular packing structure, has a certain rectifying effect, and can lead the flue gas to be distributed more uniformly in the spraying section after the flue gas enters the primary absorption tower and passes through the packing; the filler is also a gas-liquid dispersion medium and can provide a part of mass transfer area; under the drive of gravity, the speed of the spray liquid drops falling near the bottom of the tower is high, the mass transfer specific surface area provided by the liquid drops is reduced, the area adopts the filler, the liquid drops impact the surface of the filler and form a liquid film, and the mass transfer area can be effectively improved; the circulation resistance of the structured packing is small, the structured packing is not easy to block, and the risk of scaling and blocking can be further reduced by high-speed scouring of spray liquid drops.
(7) The utility model has large treatment capacity on sulfur-containing flue gas, is favorable for desorption in the process parameter range of absorbing rich liquid, and is a set of renewable amine desulfurization absorption system which is technically feasible, simple, practical, economical and reasonable.
(8) On one hand, the utility model reduces the flow resistance and simultaneously improves the gas-liquid contact area; on the other hand, the concentration of the lean and rich liquid is regulated and controlled to a proper interval to be matched with a subsequent amine liquid regeneration system, so that the aim of reducing the energy consumption of the whole operation is fulfilled.
(9) The utility model can raise tetravalent sulfur content in rich liquid leaving the absorption system (which is helpful for desorption), strengthen mass transfer efficiency per unit filler volume, and further optimize the inner diameter and height of the filler tower to reduce flow resistance of gas-liquid two phases (especially gas phase because of larger gas flow rate in general). Under the same equipment parameters, if a rich liquid circulation loop is omitted, the generated rich liquid flow is high, the tetravalent sulfur concentration in the rich liquid flow is low, and the desorption is definitely unfavorable, so that the absorption system has obvious advantages.
(10) The utility model also arranges a solid cone nozzle on the air inlet of the first-stage absorption tower, which can be fixed on the inner wall of the air inlet through a hollow circular ring, the installation position of the solid cone nozzle should be proper that the fog conical surface is just tangential with the inner wall of the tower, the diameter of fog drops sprayed by the solid cone nozzle is between 50 and 500 microns, the flow rate of the nozzle is small, the nozzle is easy to be entrained by flue gas, and the nozzle can flow along with sulfur-containing flue gas at the inlet of the flue gas and fully contact with the flue gas, thus realizing the rapid absorption reaction with the flue gas.
Drawings
FIG. 1 is a schematic diagram of the structure of the present utility model;
FIG. 2 is a schematic view of the installation angle of the spray nozzles on the spray level of the present utility model;
FIG. 3 is a schematic view of the installation angle of the solid cone nozzle of the present utility model.
Wherein, the names corresponding to the reference numerals are:
the device comprises a 1-primary absorption tower, a 2-secondary absorption tower, a 3-rich liquid storage tank, a 4-lean liquid storage tank, a 5-demister, a 6-static mixer, a 7-circulating pump, an 8-transfer pump, a 9-transfer tank, a 10-lean liquid delivery pump, a 11-spray layer, a 12-nozzle and a 13-solid cone nozzle.
Description of the embodiments
The utility model will be further illustrated by the following description and examples, which include but are not limited to the following examples.
As shown in fig. 1, the present embodiment provides an absorption system for renewable amine desulfurization to absorb sulfur dioxide in sulfur-containing flue gas. The absorption system comprises a lean liquid storage tank 4, a lean liquid delivery pump 10, a secondary absorption tower 2, a transfer tank 9, a transfer pump 8, a static mixer 6, a primary absorption tower 1 and a rich liquid storage tank 3 which are sequentially connected in series, wherein the path is also a main flow channel of the lean liquid. Meanwhile, the primary absorption tower 1, the secondary absorption tower 2 and the demister 5 are connected in series to form a channel of sulfur-containing flue gas. In the two path channels, sulfur-containing flue gas and lean liquid are countercurrent absorbed in the first-stage absorption tower 1 and the second-stage absorption tower 2.
In addition, the rich liquid storage tank 3 is also communicated with the static mixer 6 through a circulating pump 7, namely, a part of rich liquid at the bottom of the primary absorption tower is recycled back to the top of the primary absorption tower as absorption liquid, and from the aspect of hydrodynamics: the liquid-gas ratio in the first-stage absorption tower is increased, which is favorable for increasing the infiltration area of the surface of the filler, and can reduce the thickness of the flowing boundary layer to a certain extent and indirectly increase the gas-liquid mass transfer coefficient. From the mass transfer perspective: although the rich liquid circulation can improve the tetravalent sulfur content in the liquid phase and cause the increase of the sulfur dioxide partial pressure at the gas-liquid interface, the average mass transfer driving force in the absorption tower is still larger because the sulfur dioxide content in the gas phase main body of the flue gas in the primary absorption tower is higher, the sufficient mass transfer rate can be maintained, and after the flue gas leaves the primary absorption tower, the sulfur dioxide concentration in the gas phase main body is greatly reduced, and then the flue gas enters the secondary absorption tower, so that the sufficient high mass transfer driving force can be provided by the lean liquid with low concentration in the secondary absorption tower. The construction mode can improve the tetravalent sulfur content in the rich liquid leaving the absorption system, strengthen the mass transfer efficiency of unit packing volume, and further optimize the inner diameter and the height of the packing tower so as to reduce the flow resistance of gas-liquid two phases.
More importantly, the primary absorption tower of the embodiment is a spray and filler composite tower, the inner diameter 100 1600 of the outer shell of the primary absorption tower is a spray absorption section (1400 mm) at the upper part and a filler absorption section (200 mm) at the lower part; the spraying absorption sectionThe spray layer 11 is communicated with the upper liquid inlet of the primary absorption tower, and a plurality of nozzles 12 are arranged on each spray layer. A plurality of nozzles are arranged below the first spraying layer from top to bottom in the first-stage absorption tower 1 so as to evenly spray the liquid entering from the upper liquid inlet of the first-stage absorption tower 1 downwards; the first-stage absorption tower 1 is internally provided with a plurality of nozzles from top to bottom, and the upper side and the lower side of the second layer and the lower spraying layer 11 are respectively provided with a plurality of nozzles so as to spray the liquid entering from the upper liquid inlet of the first-stage absorption tower 1 in the upper direction and the lower direction respectively. The spray nozzles on the spray layer should avoid spraying to the inner wall of the tower as far as possible, so in the angle setting of the spray nozzles, the spray layers should be installed obliquely from the circle center to the circumferential direction, and the installation angle should be based on that the droplets sprayed by the spray nozzles are not sprayed to the inner wall of the tower in a large amount in the space between the spray layers. In the present embodiment, as shown in fig. 2, the atomization angle is smaller than one-half (θ 1 ＜0.5θ 2 ) And then properly adjusting the interval between the spraying layers to ensure that the fog drops sprayed by the nozzles are not sprayed on the inner wall of the primary absorption tower in a large quantity.
This arrangement retains the advantages of a spray tower, such as low gas flow resistance, since the flue gas flow is generally large, if a packed or secondary packed tower is used in its entirety, the flow resistance will be large and the fan power consumption will be greatly increased, while in combination with a spray tower these drawbacks can be avoided. And the mass transfer areas exposed by the spray liquid drops are effective mass transfer areas, and unlike a pure packing tower, gas-liquid contact dead areas can be formed, the spray heads on the top layer of the spray tower are downwards distributed, and the spray heads on each layer of spray layer below the spray tower are vertically staggered, so that the liquid drops frequently collide in a spray section, the surface updating frequency of the liquid drops is obviously improved due to the collision, and the mass transfer efficiency is obviously improved based on the surface updating theory. In addition, this structure need not to set up the defogging section like conventional spray column at spray section top, because the secondary absorption tower has taken into account the effect of defogging, has embodied the rationality of this structural layout.
Meanwhile, the packing section of the primary absorption tower of the embodiment adopts regular packing; on one hand, the rectification can be realized, and after the flue gas enters the absorption tower, the flue gas can be distributed more uniformly in the spraying section through the filler; on the other hand, the mass transfer area can be effectively increased, the filler can also serve as a gas-liquid dispersion medium, a part of mass transfer area can be provided, the speed of the spray liquid drops falling near the bottom of the tower is high, the mass transfer area can be continuously reduced, after the filler is adopted, the liquid drops quickly impact the filler to indicate and form a liquid film, and the mass transfer area can be effectively increased. The structured packing has small flow resistance, is not easy to block, can effectively reduce the risk of scaling and blocking by high-speed scouring of spray liquid drops, has relatively high liquid concentration of the absorption tower at the stage, is free from dust in flue gas, and is easy to deposit and scale by salt/particles.
The second-stage absorption tower of the embodiment is a packed tower, the inner diameter of the second-stage absorption tower is 35 mm, the height of the packed section is 300 mm, and the theta-ring packing with the specification of 4 mm is adopted.
In terms of materials, the ethylenediamine concentration in the fresh absorption solution was such that an appropriate amount of phosphoric acid was added to adjust the pH of the solution to 7. Regarding the control conditions, the sulfur dioxide content in the flue gas is simulated: 6, the flue gas flow is 1.5. 1.5 m·hThe volume flow of the lean solution entering the system and the volume flow of the rich solution leaving the system are both 50, and the ratio of the flow of the circulating pump to the flow of the lean solution delivery pump is 80:1, the sulfur content of the lean solution is 0.170 mol.L。
In this embodiment, a solid cone nozzle is disposed in the lower air inlet of the primary absorption tower, one end of the solid cone nozzle is connected with the circulating pump outlet pipe, and the other end of the solid cone nozzle faces the primary absorption tower to spray atomized liquid drops along the flow direction of sulfur-containing flue gas. Wherein, as shown in fig. 3, the spray path of the solid conical nozzle is tangential to the lower air inlet of the primary absorption tower. The solid cone nozzle is fixed on the inner wall of the air inlet through the hollow circular ring, the diameter of the sprayed fog drops is between 50 and 500 microns, the flow of the nozzle is small, the nozzle is easy to be entrained by flue gas, and the nozzle can flow along with sulfur-containing flue gas at the flue gas inlet and fully contact with the sulfur-containing flue gas to realize rapid absorption reaction with the flue gas.
The specific operation flow is as follows:
firstly, the absorption system is assembled according to the figure 1, a lean solution delivery pump is started, and the set flow is 50 mL min -1 Absorbing liquid (sulfur content of lean liquid is 0.170 mol.L) in the lean liquid storage tank -1 ) Conveying the liquid to the top of a secondary absorption tower, flowing the liquid into a transfer tank from top to bottom by gravity, starting a transfer pump after the liquid level rises to a certain height, enabling the liquid to enter the top of the primary absorption tower, spraying the liquid into a spraying section, enabling the liquid to enter a filling section from top to bottom by gravity, flowing into a rich liquid storage tank, and starting a circulating pump (flow 4000 mL.min) after the liquid level rises to a certain height -1 ) And the circulating pump conveys part of the rich liquid to the static mixer to be mixed with the absorption liquid conveyed by the transfer pump, and the mixed liquid is conveyed to the top of the primary absorption tower. And then continuously extracting the absorbed rich liquid in the rich liquid storage tank (sending the absorbed rich liquid to a desorption system), wherein the extraction flow is consistent with the lean liquid flow so as to maintain the conservation of the material in the system. After the absorption liquid flow rate reached a steady state, the simulated flue gas (1.5. 1.5 m 3 ·h -1 ，6000 mg·m -3 ) And introducing the flue gas into an absorption system, sequentially flowing through a primary absorption tower, a secondary absorption tower and a demister, and discharging the flue gas out of the absorption system. And when the temperature, pressure, flow and concentration of each flow of the system reach stability, the system is considered to be stable.
The concentration of the absorption rich liquid measured at this time was 0.217 mol.L -1 Through concentration analysis of sulfur dioxide in inlet and outlet flue gas, the desulfurization rate of the absorption system is 99%, and the expected effect is achieved.
In summary, the utility model provides an absorption system for desulfurizing by a renewable amine method, which adopts a chemical absorption method to dissolve and absorb sulfur dioxide in flue gas into an amine-containing solution in a gas-liquid countercurrent contact mode of partial circulation of absorption liquid so as to reduce the emission concentration of sulfur dioxide in the flue gas, and the rich liquid generated by absorption can be regenerated into lean liquid and returned to the absorption system to realize the recycling of the absorption liquid; the sulfur-containing flue gas treatment capacity is large, the process parameter range of the rich liquid absorption is favorable for desorption, and the system is a renewable amine desulfurization absorption system which is feasible in technology, simple, practical, economical and reasonable; the gas-liquid contact area is increased while the flow resistance is reduced; on the other hand, the concentration of the lean and rich liquid is regulated and controlled to a proper interval to be matched with a subsequent amine liquid regeneration system, so that the aim of reducing the energy consumption of the whole operation is fulfilled; can lift offThe tetravalent sulfur content in the rich liquid of the absorption system (which is helpful for desorption) is opened, the mass transfer efficiency of the unit packing volume is enhanced, and the inner diameter and the height of the packing tower can be further optimally designed to reduce the flow resistance of gas-liquid two phases (especially gas phase because of large gas flow rate in general). If the rich liquid circulation loop is omitted under the same equipment parameters, the generated rich liquid flow is high, the tetravalent sulfur concentration in the rich liquid flow is low, and the desorption is definitely unfavorable. In addition, the whole process of the embodiment can easily cope with the fluctuation of working conditions, such as SO in the flue gas 2 The content suddenly rises, can ensure that the exhaust emission reaches the standard through the mode of increasing the absorption liquid-gas ratio, and utilizes the buffer capacity of storage tank, improves suitable buffering for the back-end analytic system, can guarantee the long-term steady operation of system. Therefore, the absorption system of the embodiment can be matched with the renewable amine desulfurization technology on the premise of not increasing the cost and the operation difficulty, so that the efficiency and the economic benefit of the whole renewable amine desulfurization technology are improved.
Claims (10)
1. The absorption system for the desulfurization of the renewable amine method is used for absorbing sulfur dioxide in sulfur-containing flue gas and is characterized by comprising a first-stage absorption tower (1), a second-stage absorption tower (2), a rich liquid storage tank (3) and a lean liquid storage tank (4), wherein the first-stage absorption tower (1) is a spraying and filler composite tower, and a spraying absorption section is arranged above the inside of the first-stage absorption tower and a filler absorption section is arranged below the inside of the first-stage absorption tower; the spray absorption section comprises a plurality of spray layers (11) which are sequentially arranged from top to bottom and are communicated with an upper liquid inlet of the primary absorption tower, and each spray layer is provided with a plurality of nozzles (12); the lower air inlet of the primary absorption tower (1) is used for feeding sulfur-containing flue gas, the lower liquid outlet of the primary absorption tower is communicated with the rich liquid storage tank (3), the upper air outlet of the primary absorption tower is communicated with the lower air inlet of the secondary absorption tower (2), and the upper liquid inlet of the primary absorption tower is communicated with the lower liquid outlet of the secondary absorption tower; the upper air outlet of the secondary absorption tower (2) discharges flue gas through a demister (5), and the upper liquid inlet of the secondary absorption tower is communicated with a lean liquid storage tank (4).
2. The absorption system for the desulfurization by the renewable amine method according to claim 1, wherein a plurality of nozzles are arranged below the first spraying layer from top to bottom in the primary absorption tower (1) so as to evenly spray down the liquid entering from the upper liquid inlet of the primary absorption tower (1); the first-stage absorption tower (1) is internally provided with a plurality of nozzles from top to bottom, and the upper side and the lower side of the second layer and the lower spraying layer (11) are respectively provided with a plurality of nozzles so as to spray liquid entering from the upper liquid inlet of the first-stage absorption tower (1) in the upper direction and the lower direction respectively; the peripheral nozzles are obliquely arranged towards the central axis of the primary absorption tower, and the installation inclination angle of the nozzles is smaller than one half of the atomization angle, so that a large amount of fog drops sprayed by the nozzles are not sprayed on the inner wall of the primary absorption tower.
3. An absorption system for use in the desulfurization of regenerable amines as claimed in claim 2, wherein said packing absorption section is a structured packing section.
4. An absorption system for desulfurization by a renewable amine method according to any one of claims 1 to 3, further comprising a static mixer (6), wherein the upper liquid inlet of the primary absorption tower (1) is communicated with the lower liquid outlet of the secondary absorption tower (2) through the static mixer, and the rich liquid storage tank (3) is communicated with the static mixer.
5. An absorption system for the desulfurization of regenerable amines according to claim 4, characterized in that said rich liquid storage tank (3) is in communication with a static mixer (6) via a circulation pump (7).
6. The absorption system for the desulfurization by the renewable amine method according to claim 5, wherein a solid cone nozzle (13) is arranged in a lower air inlet of the primary absorption tower (1), one end of the solid cone nozzle is connected with an outlet pipeline of the circulating pump (7), and the other end of the solid cone nozzle faces into the primary absorption tower (1) to spray atomized liquid drops along the flow direction of sulfur-containing flue gas.
7. An absorption system for the desulfurization by the renewable amine method according to claim 5 or 6, characterized in that the static mixer (6) is communicated with the lower liquid outlet of the secondary absorption tower (2) through a transfer pump (8).
8. An absorption system for the desulfurization by the renewable amine method according to claim 7, wherein the transfer pump (8) is communicated with the lower liquid outlet of the secondary absorption tower (2) through a transfer tank (9).
9. An absorption system for the desulfurization by the regenerable amine method according to claim 1, wherein said secondary absorption tower (2) is in communication with a lean liquid reservoir (4) through a lean liquid transfer pump (10).
10. The absorption system for the desulfurization by a renewable amine method according to claim 1, wherein the secondary absorption tower (2) is a packed tower, and the diameter of the primary absorption tower is equal to or larger than the diameter of the secondary absorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320130076.0U CN219072543U (en) | 2023-01-18 | 2023-01-18 | Absorption system for renewable amine desulfurization |
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| CN202320130076.0U CN219072543U (en) | 2023-01-18 | 2023-01-18 | Absorption system for renewable amine desulfurization |
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2023
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