CN114832584A - CO based on two-phase absorbent rich liquid concentrated phase desorption 2 Trapping system and method - Google Patents
CO based on two-phase absorbent rich liquid concentrated phase desorption 2 Trapping system and method Download PDFInfo
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Abstract
本发明涉及一种基于两相吸收剂富液浓相解吸的CO2捕集系统及方法，该系统包括吸收塔、两相吸收剂系统、正渗透装置、再生塔及MVR热泵系统。两相吸收剂系统包括两相吸收剂、相分离器；两相吸收剂系统贫液通过贫液泵与吸收塔顶部连接；吸收塔底部依次通过第一富液泵、贫/富液换热器与两相吸收剂系统连接；贫/富液换热器通过所述贫液泵与吸收塔顶部连接；两相吸收剂系统富液通过第二富液泵与正渗透装置连接，正渗透装置与再生塔连接；再生塔连接有再沸器；MVR热泵系统包括闪蒸罐及压缩机，再生塔贫液出口与闪蒸罐连接，闪蒸罐通过所述压缩机与再生塔的高温高压气体进口连接；闪蒸罐底部贫液出口与贫/富液换热器连接。本发明能够大幅降低烟气CO2捕集工艺的能耗。
The invention relates to a CO2 capture system and method based on the desorption of two-phase absorbent rich liquid and concentrated phase. The system includes an absorption tower, a two-phase absorbent system, a forward osmosis device, a regeneration tower and an MVR heat pump system. The two-phase absorbent system includes a two-phase absorbent and a phase separator; the lean liquid of the two-phase absorbent system is connected to the top of the absorption tower through the lean liquid pump; the bottom of the absorption tower passes through the first rich liquid pump and the lean/rich liquid heat exchanger in turn. Connected with the two-phase absorbent system; the lean/rich liquid heat exchanger is connected to the top of the absorption tower through the lean liquid pump; the rich liquid of the two-phase absorbent system is connected to the forward osmosis device through the second rich liquid pump, and the forward osmosis device is connected to the top of the absorption tower. The regeneration tower is connected; the regeneration tower is connected with a reboiler; the MVR heat pump system includes a flash tank and a compressor, the outlet of the lean liquid of the regeneration tower is connected with the flash tank, and the flash tank passes through the compressor and the high temperature and high pressure gas inlet of the regeneration tower Connection; the lean liquid outlet at the bottom of the flash tank is connected to the lean/rich liquid heat exchanger. The invention can greatly reduce the energy consumption of the flue gas CO 2 capture process.
Description
Technical Field
The invention relates to CO 2 The technical field of trapping, in particular to CO based on rich liquid and concentrated phase desorption of a two-phase absorbent 2 A trapping system and method.
Background
With the continuous development and progress of human society, after entering the industrial civilization, the use of a large amount of fossil fuels (such as coal, petroleum and the like) leads to the use of CO 2 The major greenhouse gas emissions increase dramatically. With the world to the wholeThe climate change of the ball is gradually emphasized, and a series of carbon emission plans such as carbon peak reaching, carbon neutralization and the like gradually fall to the ground.
The Carbon Capture Utilization and Sequestration (CCUS) technology is an important technical means for coping with global climate change and controlling greenhouse gas emission. By treating CO discharged during the production process 2 And (5) carrying out trapping and purification, and then putting the mixture into a new production process for recycling and sealing. At present, research institutions and enterprises at home and abroad capture CO in energy systems 2 The field is subjected to a great deal of research and practice, and CO on a large industrial scale is successfully established 2 Exemplary items are captured.
The research on the CCUS technology in the power industry is mainly focused on coal-fired power plants. CO of coal-fired power plant 2 The trapping and separating method mainly comprises the steps of trapping after combustion, trapping before combustion and oxygen-enriched combustion. Post combustion CO 2 The trapping technology is mainly divided into three categories: absorption, adsorption and membrane processes, of which chemical absorption is one of the most widely used post-combustion capture technologies in power plants. The chemical absorption process is a method for separating the components which are easily dissolved in the absorbent in the gas phase by utilizing the chemical absorbent and through the selectivity of chemical reaction, and is suitable for separating low-concentration CO 2 The method can be carried out under normal pressure, has less modification on the existing equipment of the power plant, has stronger adaptability to load change, mature technology and the like. CO removal by chemical absorption process 2 The essence is to utilize the CO in the alkaline absorbent solution and the flue gas 2 Chemical reaction to form unstable salt, which can be reversely desorbed to release CO under certain conditions (such as heating) 2 Thereby achieving the purpose of introducing CO 2 The purpose of separating and enriching from the flue gas.
CO 2 The capture system process flow is generally as follows: part or all of the desulfurized, denitrated and dedusted flue gas enters the absorption tower from the lower part of the absorption tower through a flue gas cooler and is in countercurrent contact with absorbent barren solution entering the absorption tower from the top of the absorption tower to carry out absorption reaction (the temperature is usually 40-60 ℃), and CO is absorbed 2 Dissolved in the absorbent, and the treated flue gas is discharged from the top of the absorption tower. Absorption of CO 2 The rich liquid is pumped from the bottom of the absorption tower by a rich liquid pump to a lean/rich liquid heat exchanger, and the rich liquid is supplied to the lean/rich liquid heat exchangerThe barren liquor discharged from a barren liquor pump at the bottom of the regeneration tower exchanges heat and is heated, then the barren liquor is sent to the top of the regeneration tower to react with the steam rising in the regeneration tower, and CO is desorbed 2 To obtain reabsorbable CO 2 The lean solution of (4); the regenerated absorbent reaches the bottom of the regeneration tower, is heated by heat provided by a reboiler, is sent to a barren liquor pump, reaches the temperature level of the absorption tower through a barren/rich liquor heat exchanger and a cooler, and enters the absorption tower for continuous absorption.
Currently, the most widely used absorbents in chemical absorption are the alcamines. The alcohol amine method is especially suitable for the low CO with complex components 2 Partial pressure and low CO 2 Decarbonizing the power plant flue gas with concentration. The alcohol amine method is relatively simple in design and operation, high in absorption efficiency and stable in absorption performance, can be used for strengthening the process through various auxiliary solvents or flow optimization, is relatively mature in technology, and is rich in experience in commercial application practice of power plants. But now CO 2 The absorption rich solution mainly adopts a thermal desorption mode to realize the regeneration of the absorbent, the desorption energy consumption is overlarge, and the absorption rich solution occupies the function of capturing CO 2 70-80% of the process. The corresponding equipment corrosion leads to a further increase in the capture costs. Controlling the process to capture CO 2 First, the cost of CO reduction 2 The desorption energy consumption is started, and CO is optimized 2 A trapping absorption-desorption process. Therefore, the development of the method can greatly reduce the CO content in the flue gas 2 The energy consumption of the trapping process has wide application prospect.
Disclosure of Invention
The invention aims to provide CO based on rich liquid concentrated phase desorption of a two-phase absorbent 2 The capture system and the capture method aim at reducing the regeneration energy consumption of the absorbent and improving the regeneration heat efficiency and capture CO in the flue gas by the traditional alcohol amine method 2 The process is optimized, thereby greatly reducing the CO in the flue gas 2 Energy consumption of the trapping process.
The invention provides CO based on rich liquid concentrated phase desorption of a two-phase absorbent 2 The trapping system comprises an absorption tower, a two-phase absorbent system, a forward osmosis device, a regeneration tower and an MVR heat pump system;
a flue gas cooler is arranged at the flue gas inlet of the absorption tower;
two are describedThe phase absorbent system comprises a two-phase absorbent (A + B) composed of two CO of different types and ratios and a phase separator 2 Absorbent A and absorbent B; in which CO is absorbed 2 After then, CO 2 One phase with large load capacity mainly consists of an absorbent B and is called pregnant solution; CO 2 2 The phase with the smaller load is mainly composed of an absorbent A and is called barren liquor;
the barren solution of the two-phase absorbent system is connected with the top of the absorption tower through a barren solution pump;
the bottom of the absorption tower is connected with the two-phase absorbent system sequentially through a first rich liquid pump and a lean/rich liquid heat exchanger; the lean/rich liquid heat exchanger is connected with the top of the absorption tower through the lean liquid pump;
the two-phase absorbent system rich solution is connected with the forward osmosis device through a second rich solution pump, and the forward osmosis device is connected with the regeneration tower; the regeneration tower is connected with a reboiler;
the MVR heat pump system comprises a flash tank and a compressor, wherein a barren solution outlet of the regeneration tower is connected with the flash tank, and the flash tank is connected with a high-temperature high-pressure gas inlet of the regeneration tower through the compressor; and a lean solution outlet at the bottom of the flash tank is connected with the lean/rich solution heat exchanger.
The invention also provides a method for applying the CO 2 Capture system for capturing CO 2 The method of (1), comprising:
cooling the flue gas to 40-60 ℃ after the flue gas passes through environmental protection equipment of a power plant and a flue gas cooler, allowing the flue gas to enter from the bottom of an absorption tower and to be in countercurrent contact with an absorbent (A + B) barren solution to realize CO 2 The decarbonized flue gas is discharged from the top of the absorption tower;
absorption of CO 2 Exchanging heat between the rich liquid of the absorbent (A + B) and the desorbed lean liquid B in a lean/rich liquid heat exchanger, and then entering a phase separator;
the absorbent (A + B) is phase-separated in a phase separator, CO 2 The lean solution A with low load and the lean solution B after desorption and heat exchange are mixed into (A + B) lean solution which directly returns to the absorption tower;
CO after phase separation 2 Load(s)B rich liquid with high amount enters a forward osmosis device through a second rich liquid pump, is further dehydrated and concentrated, and is sent to the top of a regeneration tower for thermal desorption;
the desorbed B lean solution enters a flash tank for flash evaporation to generate a large amount of secondary steam, the secondary steam is pressurized by a compressor and then is changed into high-temperature and high-pressure gas, the high-temperature and high-pressure gas enters a regeneration tower, and then the B rich solution is heated and desorbed to reduce the load of a reboiler;
and the gasified lean solution B flows out from the bottom of the flash tank, exchanges heat with the lean solution A through the lean/rich solution heat exchanger, and then is mixed with the lean solution A.
Further, the absorbent A and the absorbent B are DEEA + BDA, DEEA + MAPA, DEEA + MEA, or DMAC + DETA.
Further, the forward osmosis device adopts an ammonium bicarbonate system to draw liquid.
By means of the scheme, CO desorbed by a rich liquid and a concentrated phase based on a two-phase absorbent 2 The trapping system has the following technical effects:
1) by using a two-phase absorbent and additionally arranging a forward osmosis device in front of the regeneration tower, part of solvent is removed in advance through forward osmosis before the rich solution enters a thermal desorption process, so that the rich solution is further concentrated. The water content of the solvent is reduced after concentration, and CO is 2 The equilibrium partial pressure is improved, and the driving force of mass transfer of rich liquor regeneration is strengthened, so that the latent heat of vaporization and the sensible heat of evaporation of the solvent water in the regeneration process are reduced. Meanwhile, after the rich liquid is further concentrated, the flow of the rich liquid entering the regeneration tower is correspondingly reduced, the temperature of the rich liquid at the inlet of the regeneration tower can be increased, and the waste heat recovery is enhanced.
2) The MVR heat pump is additionally arranged behind the regeneration tower, the low-quality barren solution is changed into high-quality steam through a flash evaporation compression process, heat is provided for a desorption process, and the insufficient part is provided by the reboiler. The system has obvious energy-saving advantages on the premise of solving the problems of corrosion, degradation and the like of the high-concentration absorbent.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to implement them in accordance with the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.
Drawings
FIG. 1 shows CO desorption of a two-phase absorbent rich liquid phase according to the invention 2 The structure of the trapping system is shown schematically.
Reference numbers in the figures:
1-a flue gas cooler; 2-an absorption column; 3-a barren liquor pump; 4-a first rich liquid pump; 5-lean/rich liquor heat exchanger; 6-two-phase absorbent system; 7-a second rich liquid pump; 8-a forward osmosis unit; 9-a regeneration tower; 10-a flash tank; 11-a compressor; 12-reboiler.
Detailed Description
The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
Referring to FIG. 1, this example provides a two-phase absorbent rich liquid concentrated desorption based CO 2 The trapping system comprises an absorption tower 2, a two-phase absorbent system 6, a regeneration tower 9, a forward osmosis device 8 and an MVR heat pump system;
a flue gas cooler 1 is arranged at a flue gas inlet of the absorption tower 2;
the two-phase absorbent system 6 comprises a two-phase absorbent composed of two CO of different types and proportions and a phase separator 2 Absorbent A and absorbent B; in which CO is absorbed 2 After then, CO 2 One phase with large load capacity mainly consists of an absorbent B and is called pregnant solution; CO 2 2 The phase with the smaller load is mainly composed of an absorbent A and is called barren liquor;
the two-phase absorbent system 6 is connected with the top of the absorption tower 2 through a barren liquor pump 3;
the bottom of the absorption tower 2 is connected with the two-phase absorbent system 2 through a first rich liquid pump 4 and a lean/rich liquid heat exchanger 5 in sequence; the lean/rich liquid heat exchanger 5 is connected with the top of the absorption tower 2 through a lean liquid pump 3;
the two-phase absorbent system 2 is connected with a forward osmosis device 8 through a second rich liquid pump 7, and the forward osmosis device 8 is connected with a regeneration tower 9; the regeneration tower 9 is connected with a reboiler 12;
the MVR heat pump system comprises a flash tank 10 and a compressor 11, a barren liquor outlet of the regeneration tower 9 is connected with the flash tank 10, and the flash tank 10 is connected with a high-temperature high-pressure gas inlet of the regeneration tower 9 through the compressor 11; the lean liquid outlet at the bottom of the flash tank 10 is connected with the lean/rich liquid heat exchanger 5.
After passing through environmental protection equipment of a power plant and a flue gas cooler 1, cooling the flue gas to 40-60 ℃, entering from the bottom of an absorption tower 2, and realizing countercurrent contact with an absorbent (A + B) barren solution to realize CO 2 The decarbonized flue gas is discharged from the top of the absorption tower 2;
absorption of CO 2 Exchanging heat between the rich liquid of the absorbent (A + B) and the desorbed lean liquid B in a lean/rich liquid heat exchanger 5, and then entering a phase separator;
the absorbent (A + B) is phase-separated in a phase separator, CO 2 The lean solution A with low load and the desorbed lean solution B after heat exchange are mixed into (A + B) lean solution and directly return to the absorption tower 2;
CO after phase separation 2 B rich liquid with high load enters a forward osmosis device 8 through a second rich liquid pump 7, is further dehydrated and concentrated, and is sent to the top of a regeneration tower 9 for thermal desorption;
the desorbed B lean solution enters a flash tank 10 for flash evaporation to generate a large amount of secondary steam, the secondary steam is pressurized by a compressor 11 and then is changed into high-temperature and high-pressure gas, the high-temperature and high-pressure gas enters a regeneration tower 9, the B rich solution is heated and desorbed, and the load of a reboiler 12 is reduced;
the gasified lean solution B flows out from the bottom of the flash tank 10, and is mixed with the lean solution A after heat exchange of the lean/rich solution heat exchanger 5.
Two-phase absorbent system absorbent in this example absorbs CO 2 Post-generation liquid-liquid phase separation, upper and lower two-phase CO 2 The load amounts differ greatly. CO 2 2 One phase with large loading capacity is called rich liquid, CO 2 The phase with the smaller loading is called lean solution. The absorbent is subjected to phase separation in a phase separator, the barren solution is directly returned to the absorption tower, and only the rich solution is subjected to a subsequent regeneration process. Compared with the traditional MEA system, the two-phase absorbent system can reduce the energy consumption by 30 to 50 percent.
This embodiment employs a forward osmosis technique, and utilizes osmotic pressure between the draw solution and the feed solution to cause water to automatically diffuse from the feed side with high electrochemical potential to the draw solution side with low electrochemical potential through the permselective membrane. The forward osmosis technology is operated at low pressure or no pressure, and has low energy consumption, good separation effect and low membrane pollution. The forward osmosis is utilized to achieve the purposes of removing part of the solvent and further concentrating the rich solution. A forward osmosis device is additionally arranged at a rich solution outlet behind the phase separator, and a part of solvent is removed in advance before the rich solution enters a thermal desorption process, so that the concentration of the rich solution is improved, the mass transfer condition of desorption reaction in a regeneration tower is improved, and the energy consumption caused by solvent evaporation in the regeneration process is reduced. On the premise of solving the problems of corrosion, degradation and the like of the high-concentration absorbent, the energy-saving absorbent has the obvious energy-saving advantage.
The heat pump is a heating device for transferring heat energy from a low-temperature heat source to a high-temperature heat source, can convert the low-temperature heat energy into the high-temperature heat energy, improves the effective utilization rate of the energy, and can realize the recovery of low-temperature waste heat. In the embodiment, a mechanical vapor recompression heat pump technology (MVR heat pump technology) is adopted, and a low-quality barren solution is changed into high-quality steam through a flash evaporation compression process to provide heat for a desorption process, and the insufficient part is provided by a reboiler.
The two-phase absorbent (A + B) used in this example consists of two CO species of different type and ratio 2 Absorbent A and absorbent B. Assuming absorption of CO 2 After then, CO 2 One phase with large load capacity mainly consists of an absorbent B and is called pregnant solution; CO 2 2 The phase with the smaller loading is composed mainly of absorbent a and is called barren liquor. As shown in FIG. 1, in CO 2 In the trapping process, flue gas of a thermal power plant passes through environmental protection equipment of a power plant and then passes through a flue gas cooler, the temperature of the flue gas is cooled to 40-60 ℃, and then the flue gas enters an absorption tower from the bottom and is in countercurrent contact with an absorbent (A + B) barren solution entering from the top of the absorption tower. The pressure in the absorption tower is normal pressure, and the initial temperature of the absorbent is 40 ℃. CO 2 2 Dissolved in the absorbent, and the decarbonized flue gas is discharged from the top of the absorption tower. Absorption of CO 2 And pumping the rich liquid of the absorbent (A + B) from the bottom of the absorption tower by a high-pressure pump, and introducing the rich liquid of the absorbent (A + B) and the desorbed lean liquid of the absorbent (B) into a phase separator after heat exchange in a lean-rich liquid heat exchanger. The end difference of the lean-rich liquid heat exchanger is 5-15 ℃, and the temperature of the (A + B) rich liquid after passing through the heat exchanger is about 95 ℃. The rich solution of the absorbent (A + B) is subjected to phase separation in a phase separator, CO 2 The lean solution A with small load capacity is mixed with the lean solution B after desorption and heat exchange, and the mixture is directly returned to the absorption tower, and only CO is used 2 And carrying out subsequent regeneration process on the B rich solution with large loading capacity.
According to different compositions of the absorbent, the water content of the B rich solution after phase separation is 20% -50%, and the B rich solution enters a forward osmosis device through a rich solution pump for further dehydration and concentration. The forward osmosis device adopts an ammonium bicarbonate system to draw liquid (NH) 4 HCO 3 -NH 4 OH mixed solution) with a concentration ratio of 1.5-2.0 to the absorbent. And the B rich solution is further concentrated by a forward osmosis device and then sent to the top of a regeneration tower for thermal desorption. The operating pressure of the regeneration tower is 1.2 bar-2 bar, the gas phase temperature of the outlet at the top of the tower is 100 ℃, the liquid phase at the outlet at the bottom of the tower is 115 ℃, and the lean liquid CO is desorbed 2 The load was 0.25mol CO 2 Per mol of amine. As the rich solution is further concentrated, the water content of the solvent is reduced, and CO is generated 2 The equilibrium partial pressure is improved, and the driving force of mass transfer of rich liquor regeneration is strengthened, so that the latent heat of vaporization and the sensible heat of evaporation of the solvent water in the regeneration process are reduced. Meanwhile, after the rich liquid is further concentrated, the flow of the rich liquid entering the regeneration tower is correspondingly reduced, the temperature of the rich liquid at the inlet of the regeneration tower can be increased, and the waste heat recovery is enhanced.
And enabling the desorbed B barren solution to enter a flash tank of the MVR heat pump system for flash evaporation, wherein the flash evaporation temperature is 90 ℃. Because the pressure in the flash tower is reduced, a large amount of liquid is instantaneously gasified, a large amount of steam (secondary steam) is generated, and the latent heat of vaporization of the liquid is converted into the sensible heat of the gas to be extracted. The gasified liquid flows out from the bottom of the flash tank under the action of self gravity, passes through the lean-rich liquid heat exchanger and then is mixed with the lean liquid A to return to the absorption tower. And the secondary steam generated in the flash tank is pressurized by the compressor to be changed into gas with the temperature of 120-130 ℃, and the gas enters the desorption tower to heat and desorb the B-enriched liquid, so that the load of a reboiler is reduced.
The (a + B) absorbent may be DEEA + BDA, DEEA + MAPA, DEEA + MEA, DMAC + DETA, or the like.
The invention has the following technical effects:
1) by using a two-phase absorbent and additionally arranging a forward osmosis device in front of the regeneration tower, part of solvent is removed in advance through forward osmosis before the rich solution enters a thermal desorption process, so that the rich solution is further concentrated. The water content of the solvent is reduced after concentration, and CO is 2 The equilibrium partial pressure is increased and,the driving force of mass transfer of rich liquor regeneration is strengthened, so that the latent heat of vaporization and the sensible heat of evaporation of the solvent water in the regeneration process are reduced. Meanwhile, after the rich liquid is further concentrated, the flow of the rich liquid entering the regeneration tower is correspondingly reduced, the temperature of the rich liquid at the inlet of the regeneration tower can be increased, and the waste heat recovery is enhanced.
2) The MVR heat pump is additionally arranged behind the regeneration tower, the low-quality barren solution is changed into high-quality steam through a flash evaporation compression process, heat is provided for a desorption process, and the insufficient part is provided by the reboiler. The system has obvious energy-saving advantages on the premise of solving the problems of corrosion, degradation and the like of the high-concentration absorbent.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, it should be noted that, for those skilled in the art, many modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the protection scope of the present invention.
Claims (4)
1. CO based on two-phase absorbent rich liquid concentrated phase desorption 2 The trapping system is characterized by comprising an absorption tower, a two-phase absorbent system, a forward osmosis device, a regeneration tower and an MVR heat pump system;
a flue gas cooler is arranged at the flue gas inlet of the absorption tower;
the two-phase absorbent system comprises a two-phase absorbent and a phase separator, wherein the two-phase absorbent (A + B) consists of two CO with different types and proportions 2 Absorbent A and absorbent B; in which CO is absorbed 2 After then, CO 2 One phase with large load capacity mainly consists of an absorbent B and is called pregnant solution; CO 2 2 The phase with the smaller load is mainly composed of an absorbent A and is called barren liquor;
the barren solution of the two-phase absorbent system is connected with the top of the absorption tower through a barren solution pump;
the bottom of the absorption tower is connected with the two-phase absorbent system sequentially through a first rich liquid pump and a lean/rich liquid heat exchanger; the lean/rich liquid heat exchanger is connected with the top of the absorption tower through the lean liquid pump;
the two-phase absorbent system rich solution is connected with the forward osmosis device through a second rich solution pump, and the forward osmosis device is connected with the regeneration tower; the regeneration tower is connected with a reboiler;
the MVR heat pump system comprises a flash tank and a compressor, wherein a barren solution outlet of the regeneration tower is connected with the flash tank, and the flash tank is connected with a high-temperature high-pressure gas inlet of the regeneration tower through the compressor; and a lean solution outlet at the bottom of the flash tank is connected with the lean/rich solution heat exchanger.
2. Use of the CO of claim 1 2 Capture system for capturing CO 2 The method of (2), comprising:
the flue gas passes through environmental protection equipment of a power plant and a flue gas cooler, the temperature of the flue gas is cooled to 40-60 ℃, the flue gas enters from the bottom of an absorption tower and is in countercurrent contact with barren solution of an absorbent (A + B) to realize CO 2 The decarbonized flue gas is discharged from the top of the absorption tower;
absorption of CO 2 Exchanging heat between the rich liquid of the absorbent (A + B) and the desorbed lean liquid B in a lean/rich liquid heat exchanger, and then entering a phase separator;
the absorbent (A + B) is phase-separated in a phase separator, CO 2 The lean solution A with low load and the desorbed lean solution B after heat exchange are mixed into (A + B) lean solution and directly return to the absorption tower;
CO after phase separation 2 B rich liquid with high load enters a forward osmosis device through a second rich liquid pump, is further dehydrated and concentrated, and is sent to the top of a regeneration tower for thermal desorption;
the desorbed B lean solution enters a flash tank for flash evaporation to generate a large amount of secondary steam, the secondary steam is pressurized by a compressor and then is changed into high-temperature and high-pressure gas, the high-temperature and high-pressure gas enters a regeneration tower, and then the B rich solution is heated and desorbed to reduce the load of a reboiler;
and the gasified lean solution B flows out from the bottom of the flash tank, exchanges heat with the lean solution A through the lean/rich solution heat exchanger, and then is mixed with the lean solution A.
3. The process according to claim 2, characterized in that the absorbent (a + B) is DEEA + BDA, DEEA + MAPA, DEEA + MEA, or DMAC + DETA.
4. The method as claimed in claim 2, wherein the forward osmosis apparatus employs a draw solution of ammonium bicarbonate system.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116036838A (en) * | 2023-01-06 | 2023-05-02 | 江苏科技大学 | A carbon dioxide capture system and capture method |
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| CN116850751A (en) * | 2023-07-13 | 2023-10-10 | 陕西科技大学 | A system and method for capturing carbon dioxide in blast furnace gas based on two-phase absorbent |
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| CN116036838A (en) * | 2023-01-06 | 2023-05-02 | 江苏科技大学 | A carbon dioxide capture system and capture method |
| CN116492816A (en) * | 2023-03-23 | 2023-07-28 | 中国能源建设集团广东省电力设计研究院有限公司 | High CO 2 Loaded absorbent carbon capture desorption system and method |
| CN116492816B (en) * | 2023-03-23 | 2024-03-12 | 中国能源建设集团广东省电力设计研究院有限公司 | High CO 2 Loaded absorbent carbon capture desorption system and method |
| CN116850751A (en) * | 2023-07-13 | 2023-10-10 | 陕西科技大学 | A system and method for capturing carbon dioxide in blast furnace gas based on two-phase absorbent |
| WO2025218346A1 (en) * | 2024-04-18 | 2025-10-23 | 中国华能集团清洁能源技术研究院有限公司 | Compact composite absorption tower suitable for carbon capture in peaking coal-fired power plant |
| CN118499987A (en) * | 2024-07-17 | 2024-08-16 | 江苏乐科节能科技股份有限公司 | Second-class absorption heat pump system based on liquid-liquid phase separation and waste heat recovery device |
| CN118751025A (en) * | 2024-07-24 | 2024-10-11 | 天府永兴实验室 | A low energy consumption heat pump assisted carbon dioxide capture system and capture process |
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