WO2025035352A1 - Système d'absorption et de désorption de so2 et procédé d'absorption et de désorption - Google Patents

Système d'absorption et de désorption de so2 et procédé d'absorption et de désorption Download PDF

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Publication number
WO2025035352A1
WO2025035352A1 PCT/CN2023/112872 CN2023112872W WO2025035352A1 WO 2025035352 A1 WO2025035352 A1 WO 2025035352A1 CN 2023112872 W CN2023112872 W CN 2023112872W WO 2025035352 A1 WO2025035352 A1 WO 2025035352A1
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Prior art keywords
tower
absorption
water
liquid
outlet
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Chinese (zh)
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黄锐
齐俊岭
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Keyon Process Co Ltd
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Keyon Process Co Ltd
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Priority to PCT/CN2023/112872 priority Critical patent/WO2025035352A1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact

Definitions

  • the invention relates to an SO2 absorption and desorption system and an absorption and desorption method.
  • Industrial waste gas usually contains pollutants such as SO2 , which directly affects the ecological environment on which we depend for survival. There are related measures to control SO2 emissions, but the results are limited.
  • SO2 is an acidic gas that not only destroys ecosystems such as land, forests, and rivers, but also causes irreparable harm to human buildings, industrial facilities, cultural relics, and other historical sites. In addition, it also has a very large impact on human health. Therefore, how to effectively control the emission of SO2 gas is imminent. At present, there are more than 200 flue gas desulfurization technologies developed by countries around the world, but there are very few actual commercial applications.
  • the mainstream processes for treating the flue gas include ammonia absorption and limestone slurry absorption.
  • the ammonia absorption method is referred to as ammonia desulfurization. Its raw material is ammonia, which is a raw material for fertilizer. The source is precious and the cost is high. It causes certain production losses to synthetic ammonia enterprises. In addition, ammonia is easy to volatilize, which can easily cause white smoke from the top and produce secondary aerosol pollution.
  • the limestone slurry absorption method is referred to as wet lime absorption method. Limestone absorption is convenient in source and low in production cost, but the gypsum produced is a kind of solid waste with low economic value, and the device consumes a lot of water. Therefore, it is necessary to develop a green and recyclable flue gas desulfurization process.
  • ionic liquid refers to a substance that is liquid at room temperature or low temperature and is completely composed of ions. It is also called room temperature ionic liquid (Room Temperature Ionic Liquid), room temperature molten salt (Room Temperature Molten Salt) or organic ionic liquid; its biggest feature is that it has almost no vapor pressure and has good chemical stability and thermal stability. In addition, ionic liquids have good solubility for a variety of organic or inorganic gases, and the differences are large, which shows that ionic liquids, as an environmentally friendly green solvent, have great application prospects in gas separation. Using ionic liquids as absorbents to absorb SO2 has become a new research direction. Towards.
  • the technical problem to be solved by the present invention is to overcome the defects of low desulfurization efficiency and high sulfur dioxide content in outlet gas in the prior art, and to provide a SO 2 absorption and desorption system and absorption and desorption method.
  • the system and method of the present application can not only reduce the sulfur dioxide content in the outlet gas and further improve the desulfurization efficiency, but also realize the recycling of sulfur dioxide, thereby meeting the requirements of energy conservation and environmental protection and improving the absorption effect.
  • the present invention provides a SO2 absorption and desorption system, which includes a water washing tower, an absorption tower, a regeneration tower, a rich liquid pipeline and a lean liquid pipeline; wherein:
  • the water washing tower comprises a first feed inlet and a first tower top outlet, wherein the first feed inlet is respectively connected to an exhaust gas feed pipeline and a supplementary water pipeline;
  • the absorption tower comprises a second feed inlet, a first tower top inlet and a second tower bottom outlet; the first tower top outlet is connected to the second feed inlet;
  • the regeneration tower comprises a third feed inlet, a fourth feed inlet, a second tower top inlet, a third tower bottom outlet and a third tower top outlet; the third feed inlet is located above the fourth feed inlet; the rich liquid pipeline passes through the cold fluid channel of the heat exchanger from the second tower bottom outlet and is connected to the third feed inlet; the lean liquid pipeline passes through the hot fluid channel of the heat exchanger and the lean liquid cooler from the third tower bottom outlet and is connected to the first tower top inlet and the fourth feed inlet respectively;
  • the third tower top outlet is connected to the second tower top inlet via a water cooler to form a tower top circulation loop.
  • an electric demisting device is provided in the top of the water washing tower for removing acid mist and fine particles in the flue gas.
  • the water washing tower also includes a first tower kettle outlet and a water-cooling circulation pipeline, and the water-cooling circulation pipeline is respectively connected to the make-up water pipeline and the top inlet of the water washing tower after passing through a water-cooling tower circulation cooler from the first tower kettle outlet; more preferably, a water-cooling tower bottom circulation pump is provided on the water-cooling circulation pipeline; more preferably, an external liquid outlet is provided on the water-cooling circulation pipeline.
  • the water washing tower comprises a plate tower or a packed tower, more preferably a packed tower, and further preferably a two-stage packed tower.
  • the first feed inlet is provided with a gas distributor for allowing the gas to enter the water cooling tower evenly to provide sufficient contact area for gas-liquid mass transfer.
  • the first feed inlet is arranged at the lower part of the water washing tower.
  • the absorption tower further comprises a second tower top outlet, and the second tower top outlet is used to discharge tail gas.
  • the absorption tower is a packed tower, more preferably a two-stage packed tower.
  • the second feed inlet is arranged at the lower part of the absorption tower.
  • a rich liquid pump is provided on the pipeline between the second tower bottom outlet and the heat exchanger.
  • a lean liquid pump is provided on the pipeline between the heat exchanger and the lean liquid cooler.
  • a pre-filtration cooler and a filter are sequentially provided on the pipeline between the lean liquid cooler and the fourth feed port.
  • the regeneration tower is a packed tower, more preferably a three-stage packed tower.
  • the third feed port is arranged above the packing layer of the regeneration tower, and the third feed port is used to transport the rich liquid to the regeneration tower for regeneration; the fourth feed port is used to transport the lean liquid as the regenerated solvent to the kettle of the regeneration tower.
  • the fourth feed inlet is arranged at the lower part of the regeneration tower.
  • a regeneration tower top reflux pump is provided on the tower top circulation loop.
  • a regeneration tower top reflux tank is provided on the tower top circulation loop, the inlet of the regeneration tower top reflux tank is connected to the outlet of the water cooler, the liquid phase outlet of the regeneration tower top reflux tank is connected to the second tower top inlet, and the gas phase outlet of the regeneration tower top reflux tank is connected to the sulfur dioxide collection device.
  • the kettle of the regeneration tower is provided with a reboiling circuit, and the reboiling circuit A reboiler is provided; the heat exchange medium of the reboiler is low-pressure steam, and the low-pressure steam forms steam condensate after heat exchange.
  • the present invention also provides a SO2 absorption and desorption method, which adopts the SO2 absorption and desorption system as described above and comprises the following steps:
  • the SO2 rich liquid is passed from the rich liquid pipeline through the heat exchanger to the regeneration tower for SO2 desorption, and a mixed gas and a SO2 lean liquid are obtained at the top and bottom of the regeneration tower respectively;
  • the mixed gas passes through the top circulation loop to obtain SO2 gas;
  • the SO2 lean liquid passes through the lean liquid pipeline through the heat exchanger and is passed into the absorption tower and the regeneration tower from the first tower top inlet and the fourth feed inlet respectively.
  • Nm 3 is a unit of standard gas cubic meter conventionally used in the art.
  • step S1 those skilled in the art should know that the purpose of the water washing is to cool down and remove dust from the flue gas.
  • the content of SO 2 in the flue gas is not particularly limited, and is preferably 5000-12000 mg/Nm 3 , such as 10000 mg/Nm 3 .
  • step S1 preferably, before entering the water scrubber, the flue gas is also subjected to a pressure-boosting treatment; the pressure-boosting treatment is achieved by a booster fan.
  • the water washing tower is a two-stage packed tower, and the two-stage packed tower is divided into a first packing section and a second packing section from bottom to top; more preferably, the gas temperature in the first packing section is 35-45°C, and the gas temperature in the second packing section is 30-40°C; further preferably, the temperature of the gas in the second packing section changes from bottom to top from 40°C to 30°C.
  • step S1 preferably, the washing water flowing out from the first tower kettle outlet of the water washing tower is passed through The water-cooling circulation pipeline of the water washing tower flows back to the top inlet of the water washing tower for recycling. More preferably, the washing water is pressurized by the water-cooling tower bottom circulation pump on the water-cooling circulation pipeline.
  • the washing water contacts the flue gas in countercurrent and is used again to wash and cool the flue gas.
  • step S1 preferably, the gas velocity of the water scrubber is 1-2 m/s.
  • the liquid-gas ratio of the water washing refers to the volume ratio of water to flue gas.
  • step S2 preferably, the temperature of the SO 2 absorption is 10-100°C, more preferably 40-90°C.
  • the pressure of the SO2 absorption is 0.01-0.2 MPa, more preferably 0.05-0.2 MPa.
  • the liquid-gas ratio of the SO 2 absorption is 0.1-3 L/Nm 3 , more preferably 0.35-1.3 L/Nm 3 ; those skilled in the art should know that the liquid-gas ratio of the SO 2 absorption refers to the volume ratio of the SO 2 absorbent to the flue gas after water washing.
  • the gas velocity of the absorption tower is 0.5-5 m/s, more preferably 1.5-2.5 m/s.
  • the absorption tower is a two-stage packed tower
  • the liquid holding capacity of the packing layer of the two-stage packed tower is 3-10m3 liquid/ m3 packing, more preferably 4-8m3 liquid/ m3 packing, so as to provide sufficient contact area for gas-liquid mass transfer.
  • the SO2 absorbent comprises: 30wt%-70wt% ionic liquid, 0.1wt%-4.0wt% activator, 0.1wt%-0.5wt% antioxidant, 0.1wt%-0.5wt% corrosion inhibitor, and water; wt% refers to the ratio of the mass of the above component to the total mass of the SO2 absorbent.
  • the water content is preferably 35wt%-65wt%.
  • the content of the ionic liquid is preferably 35wt%-55wt%.
  • the ionic liquid comprises cations and anions; the cations comprise Nitrogen organic substances, the anions include organic acids.
  • the cations of the ionic liquid are selected from one or more of guanidine salts, alcohol amines, imidazoles, pyridines, tetrazoles, quaternary ammonium salts, thiazoles, and dicyandiamide substances; the anions are selected from one or more of lactic acid, tartaric acid, citric acid, methanesulfonic acid, malic acid, oxalic acid, and acetic acid.
  • the ionic liquid can absorb SO 2 with high selectivity, and almost does not absorb other acidic gases, such as CO 2 .
  • the activator in the SO2 absorbent, includes an organic alcohol substance; preferably, the activator includes one or two of n-butanol, n-hexanol and n-octanol.
  • the antioxidant includes phenolic or quinone substances with weak reducing properties; preferably, the antioxidant includes one or more of hydroquinone, butylated hydroxytoluene, tert-butylhydroquinone, naphthoquinone, anthraquinone and their derivatives.
  • the corrosion inhibitor includes an inorganic salt substance; preferably, the corrosion inhibitor is selected from one or more of basic copper carbonate, potassium metavanadate, arsenic trioxide and antimony trichloride.
  • the composition of the SO 2 absorbent is: 45 wt% of tetramethylguanidine tartrate, 0.3 wt% of n-butanol, 0.15 wt% of hydroquinone, 0.2 wt% of basic copper carbonate, and the rest is water.
  • the composition of the SO 2 absorbent is: 30 wt % of metformin lactate, 0.3 wt % of n-butanol, 0.15 wt % of hydroquinone, 0.2 wt % of basic copper carbonate, and the rest is water.
  • the composition of the SO 2 absorbent is: 70wt% of ethanolamine tartrate, 0.3wt% of n-butanol, 0.15wt% of hydroquinone, 0.2wt% of basic copper carbonate, and the rest is water.
  • step S2 preferably, after the SO2 absorption is completed, tail gas is obtained at the top of the absorption tower, and the tail gas is discharged from the second top outlet of the absorption tower.
  • the temperature of SO2 desorption is 100-150°C, more preferably 110-140°C.
  • the pressure of SO2 desorption is 0.01-0.2MPa, more preferably 0.05-0.2MPa.
  • step S3 preferably, the gas velocity of the regeneration tower is 0.2-1.5 m/s, more preferably 0.6-0.8 m/s.
  • the regeneration tower is a three-stage packed tower, and the liquid holding capacity of the packing layer of the three-stage packed tower is 1-8m3 liquid/ m3 packing, more preferably 1.5-5m3 liquid/ m3 packing, so as to provide sufficient contact area for gas-liquid mass transfer.
  • step S3 the SO 2 gas can be sent to the next stage to synthesize H 2 SO 4 .
  • the concentration of SO 2 in the SO 2 gas can reach more than 95%, and the concentration of SO 2 refers to the volume percentage of SO 2 in the SO 2 gas. If SO 2 is mixed with water vapor, it can be directly introduced into the next stage to synthesize a high-concentration H 2 SO 4 byproduct.
  • the SO 2 content in the SO 2 outlet gas when the SO 2 content reaches 10000 mg/Nm 3 , the SO 2 content in the SO 2 outlet gas will be less than or equal to 70 mg/Nm 3 , and the desulfurization efficiency is as high as 99.3% and above.
  • the ionic liquid-based absorbent provided by the present invention has good absorption and desorption capabilities for SO2 gas.
  • the desulfurization mechanism is shown in formulas (1) and (2):
  • R represents the absorbent
  • the overall reaction is a reversible reaction. At low temperatures, the reaction proceeds from left to right; at high temperatures, the reaction proceeds from right to left.
  • This process uses this principle to absorb sulfur dioxide at low temperatures and desorb sulfur dioxide from the absorbent at high temperatures. This achieves the purpose of removing and recovering sulfur dioxide from flue gas.
  • the system and method of the present application have the following advantages: stable performance, extremely low vapor pressure, The sulfur dioxide absorption capacity is strong, the energy consumption is low, the desulfurization efficiency is high, and it is easy to desorb and regenerate.
  • This application can not only reduce the sulfur dioxide content in the tail gas and further improve the desulfurization efficiency, but also realize the recycling of sulfur dioxide, thereby meeting the requirements of energy conservation and environmental protection and improving the absorption effect.
  • FIG1 is a schematic structural diagram of a SO 2 absorption and desorption system according to Example 1 of the present invention.
  • Water washing tower 1 The first feed port 101 First tower top outlet 102 Electric demisting device 103 First tower kettle outlet 104 Water cooling tower circulating cooler 105 Water cooling tower bottom circulation pump 106 External liquid outlet 107 Absorption tower 2 Second feed port 201 First Tower Top Entrance 202 Second tower kettle outlet 203 Second tower top outlet 204 Regeneration Tower 3 The third feed port 301 Fourth feed port 302 Second top entrance 303 The third tower kettle outlet 304 The third tower top outlet 305 Water cooler 306 Regeneration tower top reflux tank 307 Reboiler 308 Low pressure steam 309 Steam condensate 310 Regeneration tower top reflux pump 311 Heat exchanger 401 Rich liquid pump 402 Lean liquid pump 403 Lean liquid cooler 404 Pre-filter cooler 405 Filter 406 Sulfur dioxide collection device 5 Exhaust gas feed line 1001 Make-up water pipeline 1002 Rich liquid pipeline 1003 Lean liquid pipeline 1004 Water cooling circulation pipeline 1005 Tower top circulation loop 1006 Reboiling loop 1007.
  • the system includes a water washing tower 1, an absorption tower 2, a regeneration tower 3, a rich liquid pipeline 1003 and a lean liquid pipeline 1004; wherein the water washing tower 1 includes a first feed inlet 101 and a first tower top outlet 102, the first feed The inlet 101 is connected to the exhaust gas feed pipeline 1001 and the make-up water pipeline 1002 respectively; the absorption tower 2 includes a second feed inlet 201, a first tower top inlet 202 and a second tower bottom outlet 203; the first tower top outlet 102 is connected to the second feed inlet 201; the regeneration tower 3 includes a third feed inlet 301, a fourth feed inlet 302, a second tower top inlet 303, a third tower bottom outlet 304 and a third tower top outlet 305; the third feed inlet 301 is located at the fourth feed inlet 302 Above; the rich liquid pipeline 1003 is connected to the third feed port 301 after passing through the cold fluid channel of the heat exchanger 401 from the second tower bottom outlet 203; the lean liquid pipeline 100
  • An electric demisting device 103 is provided in the top of the water washing tower 1;
  • the water washing tower 1 also includes a first tower kettle outlet 104 and a water cooling circulation pipeline 1005.
  • the water cooling circulation pipeline 1005 is connected to the make-up water pipeline 1002 and the top inlet of the water washing tower 1 respectively after passing through the water cooling tower circulation cooler 105 from the first tower kettle outlet 104; a water cooling tower bottom circulation pump 106 is provided on the water cooling circulation pipeline 1005; and an external liquid discharge outlet 107 is provided on the water cooling circulation pipeline 1005.
  • the water washing tower 1 is a two-stage packed tower; the first feed inlet 101 is provided with a gas distributor; the first feed inlet 101 is arranged at the lower part of the water washing tower 1.
  • the absorption tower 2 further includes a second tower top outlet 204; the absorption tower 2 is a two-stage packed tower; the second feed inlet 201 is provided at the lower part of the absorption tower 2; a rich liquid pump 402 is provided on the pipeline between the second tower bottom outlet 203 and the heat exchanger 401;
  • a lean liquid pump 403 is provided on the pipeline between the heat exchanger 401 and the lean liquid cooler 404 ; a pre-filtration cooler 405 and a filter 406 are provided in sequence on the pipeline between the lean liquid cooler 404 and the fourth feed port 302 .
  • the regeneration tower 3 is a three-stage packed tower; the fourth feed inlet 302 is arranged at the lower part of the regeneration tower 3; a regeneration tower top reflux pump 311 is arranged on the tower top circulation loop 1006; a regeneration tower top reflux tank 307 is arranged on the tower top circulation loop 1006, the inlet of the regeneration tower top reflux tank 307 is connected to the outlet of the water cooler 306, the liquid phase outlet of the regeneration tower top reflux tank 307 is connected to the second tower top inlet 303, and the regeneration tower top reflux tank The gas phase outlet of 307 is connected to the sulfur dioxide collecting device 5.
  • the bottom of the regeneration tower 3 is provided with a reboiler circuit, and a reboiler 308 is provided on the reboiler circuit; the heat exchange medium of the reboiler 308 is low-pressure steam 309, and the low-pressure steam 309 forms steam condensate 310 after heat exchange.
  • Flue gas with a temperature of 140°C and containing 10000mg/Nm 3 SO 2 is passed from the waste gas feed pipeline 1001 into the water washing tower 1 for water washing, and the washed flue gas is obtained at the top of the water washing tower 1.
  • the liquid-gas ratio of the water washing is 5L/Nm 3 ; the temperature of the washed flue gas is 40°C; wherein, the gas velocity of the water washing tower 1 is 1.5m/s;
  • the flue gas Before entering the water scrubber 1, the flue gas is also subjected to a pressure-boosting treatment; the pressure-boosting treatment is achieved by a booster fan;
  • the water washing tower 1 is a two-stage packed tower, which is divided into a first packed section and a second packed section from bottom to top; the gas temperature in the first packed section is 35-45°C, and the gas temperature in the second packed section is 40-30°C;
  • the washing water flowing out from the first tower kettle outlet 104 of the water washing tower 1 is refluxed to the tower top inlet of the water washing tower 1 through the water cooling circulation pipeline 1005 of the water washing tower 1, and is circulated and reused, and is in countercurrent contact with the flue gas; the washing water is pressurized by the water cooling tower bottom circulation pump 106 on the water cooling circulation pipeline 1005;
  • the temperature of SO 2 absorption is 60-70°C; the pressure of SO 2 absorption is 0.1MPa; the liquid-gas ratio of SO 2 absorption is 0.7L/Nm 3 ; the gas velocity of absorption tower 2 is 2m/s;
  • Absorption tower 2 is a two-stage packed tower, and the liquid holding capacity of the packing layer of the two-stage packed tower is 7m3 liquid/ m3 packing;
  • the SO2 absorbent comprises: 45% methylguanidine tartrate, 0.3% n-butanol, 0.15% hydroquinone, 0.2% basic copper carbonate, and the rest is water;
  • tail gas is obtained at the top of absorption tower 2.
  • the tail gas is discharged from the second The tower top outlet 204 is discharged.
  • the SO2 rich liquid is passed from the rich liquid pipeline 1003 to the regeneration tower 3 after heat exchange in the heat exchanger 401 for SO2 desorption, and a mixed gas and a SO2 lean liquid are obtained at the top and bottom of the regeneration tower 3 respectively;
  • the mixed gas passes through the top circulation loop 1006 to obtain SO2 gas;
  • the SO2 lean liquid passes through the lean liquid pipeline 1004 and the heat exchanger 401 and then passes into the absorption tower 2 and the regeneration tower 3 from the first tower top inlet 202 and the fourth feed inlet 302 respectively;
  • the temperature of SO 2 desorption is 120°C; the pressure of SO 2 desorption is 0.1MPa; the gas velocity of regeneration tower 3 is controlled within the range of 0.6-0.8m/s;
  • the regeneration tower 3 is a three-stage packed tower, and the liquid holding capacity of the packing layer of the three-stage packed tower is 4m3 liquid/ m3 packing.
  • the concentration of SO 2 desorbed from the regeneration tower 3 can reach more than 95%.
  • the SO 2 is cooled by the condenser 8 and then enters the gas-liquid separator 9.
  • the separated and purified SO 2 is sent to the subsequent process, such as the sulfuric acid device to produce sulfuric acid, or it can be pressurized and cooled to produce liquid SO 2 products.
  • the concentration of SO 2 in the purified gas is reduced to 48mg/Nm 3 , and the desulfurization efficiency is 99.5%.
  • the process operation results show that the system and method of the present application can effectively absorb SO 2 in flue gas with high absorption efficiency and good selectivity, and the system can operate stably for a long time.
  • step S2 of this embodiment the composition of the SO 2 absorbent is (the proportions of each component are in mass fraction): 30 wt% of metformin lactate, 0.3 wt% of n-butanol, 0.15 wt% of hydroquinone, 0.2 wt% of basic copper carbonate, and the rest is water.
  • the remaining steps are the same as those in embodiment 2.
  • the concentration of SO 2 in the purified gas is reduced to 50 mg/Nm 3 , and the desulfurization efficiency is 99.5%.
  • step S2 of this embodiment the composition of the SO 2 absorbent is (the proportions of each component are in mass fraction): 70wt% of ethanolamine tartrate, 0.3wt% of n-butanol, 0.15wt% of hydroquinone, 0.2wt% of basic copper carbonate, and the rest is water.
  • the remaining steps are the same as those in Example 2.
  • the concentration of SO 2 in the purified gas is reduced to 70 mg/Nm 3 , and the desulfurization efficiency is 99.3%.

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  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

L'invention concerne un système d'absorption et de désorption de SO2 et un procédé d'absorption et de désorption. Le système d'absorption et de désorption de SO2 comprend une tour de lavage à l'eau (1), une tour d'absorption (2), une tour de régénération (3), une conduite de liquide riche (1003) et une conduite de liquide pauvre (1004) ; la tour de lavage à l'eau (1) comprend un premier orifice d'alimentation (101) et une première sortie supérieure de tour (102), et le premier orifice d'alimentation (101) est raccordé à une conduite d'alimentation en gaz résiduaire (1001) et à une conduite d'eau supplémentaire (1002) séparément ; la tour d'absorption (2) comprend un second orifice d'alimentation (201), une première entrée supérieure de tour (202) et une seconde sortie inférieure de tour (203) ; la première sortie supérieure de tour (102) est raccordée au second orifice d'alimentation (201) ; la tour de régénération (3) comprend un troisième orifice d'alimentation (301), un quatrième orifice d'alimentation (302), une seconde entrée supérieure de tour (303), une troisième sortie inférieure de tour (304) et une troisième sortie supérieure de tour (305) ; le troisième orifice d'alimentation (301) est situé au-dessus du quatrième orifice d'alimentation (302) ; et la troisième sortie supérieure de tour (305) est raccordée à la seconde entrée supérieure de tour (303) au moyen d'un refroidisseur d'eau (306) pour former une boucle de circulation supérieure de tour (1006). Selon le système et le procédé, la teneur en dioxyde de soufre dans un gaz de sortie peut être réduite, l'efficacité de désulfuration peut être davantage améliorée, et le dioxyde de soufre peut être davantage recyclé, ce qui permet de satisfaire aux exigences de conservation de l'énergie et de protection de l'environnement, et d'améliorer l'effet d'absorption.
PCT/CN2023/112872 2023-08-14 2023-08-14 Système d'absorption et de désorption de so2 et procédé d'absorption et de désorption Pending WO2025035352A1 (fr)

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Cited By (1)

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CN120420818A (zh) * 2025-07-08 2025-08-05 中核核电运行管理有限公司 一种14c同位素分离的连续生产装置

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