CN116492814B - Flue gas carbon dioxide entrapment process systems - Google Patents
Flue gas carbon dioxide entrapment process systemsInfo
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- CN116492814B CN116492814B CN202310591154.1A CN202310591154A CN116492814B CN 116492814 B CN116492814 B CN 116492814B CN 202310591154 A CN202310591154 A CN 202310591154A CN 116492814 B CN116492814 B CN 116492814B
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- carbon dioxide
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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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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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
- B01D53/1425—Regeneration of liquid absorbents
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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
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas carbon dioxide trapping process system, which comprises an absorption tower, a desorption tower and a reboiling tower, wherein a flue gas heat exchange tube is arranged in the reboiling tower, and a flue gas inlet of the flue gas heat exchange tube is communicated with a flue gas pipeline of the system so as to convert part of heat of flue gas into heat required by desorption of rich liquid of the desorption tower to generate carbon dioxide gas; compared with the prior art that steam is used as a heat source of the reboiling tower, the reboiling tower provided by the invention uses the heat carried by the flue gas of the system as the heat source to heat the desorption tower, so that the rich liquid is desorbed to produce carbon dioxide gas, namely, the flue gas waste heat (containing sensible heat and vaporization latent heat) of the system is fully utilized, the full desorption of the carbon dioxide gas in the absorption liquid can be completed without steam, the energy consumption of the system is reduced, the use cost of the system is further reduced, and the reboiling tower is particularly suitable for high-moisture flue gas after low-temperature denitration in the steel industry and the waste incineration industry.
Description
Technical Field
The invention relates to the technical field of carbon dioxide collection, in particular to a flue gas carbon dioxide capturing process system.
Background
In recent years, a CO 2 greenhouse gas emission reduction path and a CO 2 trapping and separating technology from industrial fields such as electric power, metal smelting, cement production, chemical synthesis and the like become a research hot spot at home and abroad. The carbon trapping technology by the organic amine absorption method has the advantages of high trapping efficiency and mature and stable technology, and becomes the CO 2 trapping technology which is most widely researched and applied at present.
The current common carbon dioxide capturing process flow of the organic amine absorption method is shown in fig. 1, and fig. 1 is a schematic diagram of the carbon dioxide capturing process flow of the organic amine absorption method in the prior art. The flue gas from the industrial field after dust removal, desulfurization and denitrification enters an absorption tower 2 'at the temperature of 40 ℃ after being cooled by a pretreatment tower 1', contacts with an absorbent, carbon dioxide in the flue gas is absorbed by the absorbent to form rich liquid to be discharged from the bottom of the absorption tower 2', and decarburized flue gas is discharged from the top of the absorption tower 2'. The rich liquid is heated by the rich liquid pump through the lean-rich liquid heat exchanger 7 'and then is conveyed to the upper end of the filling of the regeneration tower 3'. The rich liquid is regenerated at 120-140 ℃ and about 200kPa to desorb carbon dioxide gas. The regeneration process of the regeneration tower consumes thermal energy and is provided by the reboiling tower 12'. The regenerated gas is cooled by a condenser 10', condensate separated by a reflux tank 11' is conveyed to the regeneration tower 3 'again by a condensate pipeline, and separated carbon dioxide is discharged by a carbon dioxide discharge pipeline on the reflux tank 11'. And discharging the regenerated lean solution from the bottom of the desorption tower 3', cooling, and returning to the absorption tower 2' for cyclic absorption.
The traditional flue gas carbon dioxide capturing process has the defects that ① reboiling towers are used as steam sources and are single in heat source, a large amount of steam sources are needed to be provided for ensuring that CO 2 in absorption liquid is fully desorbed, so that the total energy consumption is high, ② all CO2 is required to be regenerated by means of a single steam source, the load of the absorption towers is large, the design scale of the absorption towers is large, and the investment cost is high.
How to effectively solve at least one of the above defects is a technical problem that needs to be solved by those skilled in the art.
Disclosure of Invention
The invention aims to provide a flue gas carbon dioxide capturing process system with low system energy consumption and low use cost.
The invention provides a flue gas carbon dioxide capturing process system, which comprises the following components;
the absorption tower is provided with a smoke inlet, a smoke outlet and a rich liquid outlet and is used for absorbing part of carbon dioxide in the smoke to form rich liquid;
the rich liquid inlet of the desorption tower is connected with the rich liquid outlet of the absorption tower, and the desorption tower is used for desorbing the rich liquid to generate carbon dioxide gas;
And the reboiling tower is internally provided with a flue gas heat exchange tube, and a flue gas inlet of the flue gas heat exchange tube is communicated with a flue gas pipeline of the system so as to convert part of heat of the flue gas into heat required by desorbing rich liquid of the desorbing tower to generate carbon dioxide gas.
Compared with the prior art that steam is used as a heat source of the reboiling tower, the reboiling tower provided by the invention uses the heat (partial sensible heat and latent heat) carried by the flue gas of the system as the heat source to heat the desorbing tower, so that the rich liquid is desorbed to produce carbon dioxide gas, namely, the flue gas waste heat of the system is fully utilized, the full desorption of the carbon dioxide gas in the absorption liquid can be completed without steam, the energy consumption of the system is reduced, the use cost of the system is further reduced, and the reboiling tower is particularly suitable for high-moisture flue gas after low-temperature denitration in the steel industry and the waste incineration industry.
Optionally, the flue gas outlet of the flue gas heat exchange tube of the reboiling tower can be communicated with the flue gas inlet of the absorption tower, and an adjusting component is further arranged on the communicating pipeline of the flue gas outlet and the flue gas outlet of the flue gas heat exchange tube of the reboiling tower and is used for adjusting the parameter of the flue gas entering the absorption tower to a preset working parameter, wherein the parameter comprises at least one of temperature and pressure.
Optionally, the adjusting component comprises at least one flue gas cooler, and each flue gas cooler is connected in series or parallel or connected in series and parallel on a communication pipeline between a flue gas outlet of the reboiling tower and a flue gas inlet of the absorption tower.
Optionally, a flue gas-rich liquid heat exchanger is arranged on a communicating pipe between the rich liquid outlet of the absorption tower and the rich liquid inlet of the desorption tower, and the flue gas-rich liquid heat exchanger is used for exchanging heat between flue gas flowing through the flue gas-rich liquid heat exchanger and the rich liquid so as to secondarily preheat the rich liquid.
Optionally, at least two stages of absorption filler layers are arranged between the smoke inlet and the smoke outlet of the absorption tower, and each absorption filler layer is arranged at intervals, and the absorption tower further comprises an inter-stage cooler for cooling absorption liquid between the two absorption filler layers.
Optionally, the inter-stage cooler is located outside the absorption tower, an absorption liquid outlet and an inter-stage absorption liquid inlet are arranged between adjacent absorption packing layers of the absorption tower, and two ends of an internal heat exchange runner of the inter-stage cooler are respectively connected with the absorption liquid outlet and the inter-stage absorption liquid inlet.
Optionally, each of the flue gas coolers is connected in series, and each of the flue gas coolers is defined as a first stage flue gas cooler to an Mth stage flue gas cooler along the flue gas flowing direction;
the device also comprises a lean solution cooler for cooling the lean solution flowing out of the desorption tower;
the device also comprises a gas cooler for cooling the carbon dioxide gas flowing out of the desorption tower;
and the cooling medium subjected to heat exchange among the interstage cooler, the Mth stage flue gas cooler, the gas cooler and the lean solution cooler is converged and flows into the first stage flue gas cooler.
Optionally, the inside of the desorption tower comprises N-level desorption packing layers and at least one-level catalytic packing layer, the desorption packing layers are used for providing sufficient contact surfaces for gas and liquid phases and creating conditions for improving turbulence degree (mainly gas phase) of the desorption packing layers so as to be beneficial to CO2 desorption mass transfer and heat transfer processes and improve desorption efficiency, the catalytic packing layers are used for reducing energy required by CO2 desorption, reducing desorption temperature, promoting desorption efficiency and reducing regeneration energy consumption, the N-level desorption packing layers are arranged at intervals along the height direction of the desorption tower, the catalytic packing layers are positioned below all the desorption packing layers, and air nozzles positioned below the catalytic packing layers are further arranged inside the desorption tower and are communicated with a gas outlet pipeline of the desorption tower.
Optionally, the catalytic filler layer comprises at least two stages, the catalytic filler layers are arranged at intervals along the height direction, and a layer of air jet is arranged below each stage of catalytic filler layer.
Optionally, the desorber includes first connector and second connector, respectively with reboiling tower's feed liquor heat transfer pipe's both ends are connected, first connector is located the lower floor the below of catalysis packing layer, the second connector is located the upper strata the catalysis packing layer with the lower floor between the desorption packing layer.
Optionally, the device further comprises a gas-liquid separator, wherein the gas outlet pipeline is arranged on the desorption tower, and the liquid medium outlet of the gas-liquid separator is communicated with the inner cavity of the absorption tower, wherein the inner cavity is provided with an absorbent.
Optionally, the device further comprises a lean-rich liquid heat exchanger for exchanging heat between the rich liquid flowing out of the absorption tower and the lean liquid flowing out of the desorption tower;
Or/and a rich liquid pump is arranged on the communicating pipe between the rich liquid outlet of the absorption tower and the rich liquid inlet of the desorption tower;
or/and, a lean liquid pump is arranged on the communicating pipe between the lean liquid outlet of the desorption tower and the lean liquid return port of the absorption tower.
Drawings
FIG. 1 is a schematic diagram of a carbon dioxide capturing process flow by an organic amine absorption method in the prior art;
FIG. 2 is a schematic diagram of a flue gas carbon dioxide capture process system according to one embodiment of the present invention.
The one-to-one correspondence of the reference numerals and the component names in fig. 1 to 2 is as follows:
pretreatment column 1', absorption column 2', regeneration column 3', lean-rich liquid heat exchanger 7', reboiling column 12', condenser 10', reflux drum 11';
The device comprises an absorption tower 1, a 1-1 absorption layer, a desorption tower 2, a 2-1 desorption packing layer, a 2-2 catalytic packing layer, a 2-3 spray pipe, a reboiling tower 3, a first-stage flue gas heat exchanger 4, a second-stage flue gas cooler 5, a rich liquid pump 6, a lean-rich liquid heat exchanger 7, a flue gas-rich liquid heat exchanger 8, a lean liquid cooler 9, an interstage cooler 10, a gas cooler 11, a gas-liquid separator 12 and a lean liquid pump 13.
Detailed Description
Aiming at the technical problems of high energy consumption and high use cost of steam energy sources in the background technology, a great deal of research is carried out, and the research discovers that the current flue gas carbon dioxide capturing technology ignores the self conditions of the use environment and only uses steam as the energy source of the reboiling tower, thereby causing high regeneration energy consumption and high running cost.
Based on the research findings, the invention provides a flue gas carbon dioxide capturing process system with low energy consumption.
The terms "first," "second," and the like, herein are merely used for convenience in describing two or more structures or components that are identical or functionally similar, and do not denote any particular limitation of order and/or importance.
Features and exemplary embodiments of various aspects of the present application will be described in detail below, and in order to make the objects, technical solutions and advantages of the present application more apparent, the present application will be described in further detail below with reference to the accompanying drawings and the detailed embodiments.
Referring to fig. 2, fig. 2 is a schematic structural diagram of a flue gas carbon dioxide capturing process system according to an embodiment of the present invention.
The invention provides a flue gas carbon dioxide trapping process system which comprises an absorption tower 1, a desorption tower 2 and a reboiling tower. The process system is particularly suitable for high-moisture flue gas with the flue gas temperature of 130-180 ℃ and the water content of 10-30% and higher latent heat of vaporization, and is particularly suitable for flue gas after medium-low temperature SCR flue gas denitration in the steel industry and the waste incineration industry.
The absorption tower 1 is provided with at least a smoke inlet, a smoke outlet and a rich liquid outlet, the smoke inlet is usually positioned at the lower part of the absorption tower 1, the smoke outlet is positioned at the top of the absorption tower 1, at least two stages of absorption filler layers 1-1 are arranged between the smoke inlet and the smoke outlet of the absorption tower 1, and the absorption filler layers 1-1 are arranged at intervals. The absorption tower 1 is used for absorbing part of carbon dioxide in the flue gas to form a rich liquid, specifically, in the process that the flue gas flows from the flue gas inlet to the flue gas outlet, the flue gas can be contacted with the absorbent in the absorption filler layer and absorbed by the absorbent to form the rich liquid, the rich liquid can flow out from the rich liquid outlet arranged at the bottom of the absorption tower 1, and the flue gas after decarbonization flows out from the flue gas outlet at the top of the absorption tower 1.
The desorption column 2 in the present invention has a rich liquid inlet, a lean liquid outlet, a first connection port, a second connection port, and a gas outlet. The rich liquid inlet of the desorption tower 2 is connected with the rich liquid outlet of the absorption tower 1, and the rich liquid can be desorbed in the desorption tower 2 to generate carbon dioxide gas. Specifically, the inside of the desorption tower 2 is provided with desorption filler, and the main function of the desorption filler is to provide sufficient contact surfaces for gas and liquid phases and create conditions for improving the turbulence degree (mainly gas phase) of the gas and liquid phases, so as to be beneficial to the desorption mass transfer and heat transfer process of CO 2 and improve the desorption efficiency. The rich liquid inlet and the gas outlet are usually positioned at the top of the desorption tower 2, the lean liquid outlet is positioned at the bottom of the desorption tower 2, and the first connecting port and the second connecting port are positioned below the bottom desorption filler and are respectively communicated with a heat exchange pipeline of the reboiling tower. The rich liquid flowing into the desorption tower 2 from the rich liquid inlet is desorbed with carbon dioxide gas, the desorbed lean liquid flows to the bottom position of the desorption tower 2, and part of lean liquid can return to the inside of the absorption tower 1 from the lean liquid outlet.
The reboiling tower is internally provided with a flue gas heat exchange tube, and a flue gas inlet of the flue gas heat exchange tube is communicated with a flue gas pipeline of the system so as to convert part of sensible heat and a large amount of latent heat of flue gas into heat required by desorption of rich liquid in the desorption tower 2 to generate carbon dioxide gas. In a specific example, the reboiling tower is internally provided with a flue gas heat exchange tube, and part of sensible heat and a great amount of latent heat of external flue gas are indirectly transferred to the inside of the desorption tower 2 through heat exchange with the absorption liquid in the process of flowing through the flue gas heat exchange tube.
Compared with the prior art that steam is used as a heat source of the reboiling tower, the reboiling tower provided by the invention uses the latent heat and sensible heat carried by the flue gas of the system as the heat source to heat the desorption tower 2, so that rich liquid desorption is realized to produce carbon dioxide gas, namely, the flue gas waste heat of the system is fully utilized, the full desorption of the carbon dioxide gas in the absorption liquid can be completed without steam, the energy consumption of the system is reduced, the use cost of the system is further reduced, and the reboiling tower is particularly suitable for flue gas which has high vaporization latent heat and high moisture content after low-temperature denitration in the steel industry and the waste incineration industry.
In a specific example, the flue gas outlet of the flue gas heat exchange tube of the reboiling tower can be communicated with the flue gas inlet of the absorption tower 1, and the communicating pipe of the flue gas outlet and the reboiling tower is also provided with an adjusting component for adjusting parameters of flue gas entering the absorption tower 1 to preset working parameters, wherein the parameters comprise at least one of temperature and pressure. The adjusting member may be a temperature adjusting member, or may be a pressure adjusting member, or may be a member capable of adjusting both temperature and pressure.
In the above embodiment, the flue gas after heat exchange in the reboiling tower is adjusted to the flue gas meeting the parameters of the absorption tower 1 by the adjusting component, so as to decarbonize the flue gas.
In the invention, the regulating component comprises at least one flue gas cooler, at least one flue gas cooler is connected in series or in parallel or in series-parallel connection on a communication pipeline between a flue gas outlet of the reboiling tower and a flue gas inlet of the absorption tower 1, each flue gas cooler is used for cooling flue gas flowing through the flue gas cooler, fig. 2 shows that each flue gas cooler is connected in series with the communication pipeline between the flue gas outlet of the reboiling tower and the flue gas inlet of the absorption tower 1, and each flue gas cooler is respectively defined as a first-stage flue gas cooler 4 to an Mth-stage flue gas cooler along the flue gas flowing direction.
Of course, the connection mode of each flue gas cooler is not limited to that shown in fig. 2, and the flue gas coolers can be arranged in parallel or in series-parallel.
In this embodiment, the cooling medium may cool down the flue gas flowing through the flue gas cooler when passing through the flue gas cooler, so as to adjust the temperature and pressure of the flue gas. The number of the flue gas coolers and the temperature of the introduced cooling medium can be reasonably selected according to the practical application environment. The flue gas cooler is arranged to adjust the temperature of the flue gas, so that the cooling effect can be fully exerted, and the flue gas parameter adjustment is simple and quick.
In a specific embodiment, a rich liquor pump 6, a rich liquor-lean liquor heat exchanger and a flue gas-rich liquor heat exchanger 8 are arranged on the communicating pipes of the rich liquor outlet of the absorption tower 1 and the rich liquor inlet of the desorption tower 2, the rich liquor pump 6 mainly provides flow power of the rich liquor, and the rich liquor-lean liquor heat exchanger is mainly used for carrying out heat exchange on the rich liquor flowing out of the absorption tower 1 and the lean liquor flowing out of the desorption tower 2, and in the process, the release heat temperature of the high-temperature lean liquor is reduced, and the absorption heat temperature of the rich liquor is increased. The flue gas-rich liquid heat exchanger 8 is used for exchanging heat between the flue gas flowing through the flue gas-rich liquid heat exchanger and the rich liquid so as to perform secondary preheating on the rich liquid. The rich liquid-lean liquid heat exchanger is located upstream of the flue gas-rich liquid heat exchanger 8, that is, the flue gas-rich liquid heat exchanger 8 is closer to the desorption tower 2, that is, the rich liquid flowing out of the absorption tower 1 absorbs heat of lean liquid and then is continuously heated by flue gas.
In the embodiment, the raw flue gas with the flue gas temperature of 130-180 ℃ and the moisture content of 10-30% can be introduced into the flue gas-rich liquid heat exchanger 8 to serve as a heat source required by system regeneration, and the high-temperature high-humidity raw flue gas and the rich liquid with relatively low temperature in the flue gas-rich liquid heat exchanger 8 are subjected to full heat exchange, so that partial sensible heat of the flue gas and a large amount of latent heat of water vapor in the flue gas are fully utilized to replace steam with high cost, and the running cost of the system is greatly reduced. And, set up flue gas-rich liquid heat exchanger 8 in the anterior segment of desorber 2 can promote the rich liquid temperature that gets into desorber 2 effectively, realize the desorption in advance of rich liquid to reduce the load of catalytic desorber 2 to a certain extent, reach energy-conserving effect.
In addition, the heat of the lean solution can be recycled through the rich solution-lean solution heat exchanger, and the running cost of the system is further reduced.
The flue gas carbon dioxide capture process system of the present invention further includes an inter-stage cooler 10 for cooling all absorption liquid flowing through both absorption filler layers. As shown in fig. 2, three stages of absorption filler layers are arranged in the absorption tower 1, namely a first absorption filler layer, a second absorption filler layer and a third absorption filler layer from bottom to top, wherein a space between the first absorption filler layer and the second absorption filler layer and the inter-stage cooler 10 form a circulation loop. After passing through the first absorption filler layer, the absorption liquid is cooled by the inter-stage cooler 10 and then returns to the second absorption filler layer to absorb the filler layer, so that the solubility of CO2 in the absorption liquid can be improved through the cooling effect, and the capture efficiency of the absorption liquid on other carbon dioxide in the flue gas can be greatly improved.
Of course, the number and placement of the inter-stage coolers 10 are not limited to that described herein, e.g., the inter-stage coolers 10 may also form a recirculation loop with the space between the second and third absorption packing layers.
Specifically, the inter-stage cooler 10 may be located outside the absorber tower 1, so that improvement of the existing absorber tower 1 can be achieved without affecting the internal structure of the existing absorber tower 1 as much as possible, and the inter-stage cooler 10 is located outside the absorber tower 1 with relatively high arrangement flexibility. An interstage absorption liquid outlet and an interstage absorption liquid inlet are arranged between adjacent absorption filler layers of the absorption tower 1, and two ends of an internal heat exchange flow channel of the interstage cooler 10 are respectively connected with the absorption liquid outlet and the interstage absorption liquid inlet.
In the above embodiments, the system further comprises a lean solution cooler 9 for cooling the lean solution flowing out of the desorption tower 2, wherein the outlets of the cooling medium of the interstage cooler 10 and the lean solution cooler 9 are both communicated with the cooling medium inlet of the first stage flue gas cooler 4. The gas outlet of the desorption tower 2 is also provided with a gas cooler 11 for cooling the gaseous medium flowing out of the desorption tower 2. The inter-stage cooler 10, the 2 nd to M-stage coolers, the gas cooler 11 and the lean liquor cooler 9 can be connected in parallel to a cooling medium pipeline, and the cooling medium subjected to heat exchange of the three can be gathered and flows into the first-stage flue gas cooler 4 to cool the flue gas.
Through the multistage utilization of the cooling water, the cooling potential of the cooling water is fully exerted, and meanwhile, through the multistage cooling effect on the flue gas, the consumption of the cooling water can be reduced to the greatest extent, the energy consumption of power equipment is reduced, and the energy conservation and consumption reduction of the system are realized.
In a specific example, the inside of the desorption tower 2 comprises N-level desorption packing layers 2-1 and at least one-level catalysis packing layer 2-2, the desorption packing layers 2-1 are used for providing sufficient contact surfaces for gas and liquid phases and creating conditions for improving turbulence degree (mainly gas phase) of the gas and liquid phases so as to be beneficial to CO2 desorption mass transfer and heat transfer processes, improve desorption efficiency, the catalysis packing layers 2-2 are used for reducing energy required by CO2 desorption reaction, reducing desorption temperature, promoting desorption reaction rate, improving desorption efficiency and reducing regeneration energy consumption, the N-level desorption packing layers 2-1 are arranged at intervals along the height direction of the desorption tower 2, the catalysis packing layers 2-2 are positioned below all the desorption packing layers 2-1, and gas nozzles positioned below the catalysis packing layers 2-2 are also arranged inside the desorption tower 2 and are communicated with a gas outlet pipeline of the desorption tower 2.
Specifically, the air jet can be arranged on the spray pipe, and the spray pipe can be provided with a plurality of spray pipe layers which are formed on the same plane. A spray pipe layer is arranged below each catalytic packing layer 2-2.
The integrated coupling catalysis, desorption and blowing and stripping effects with finished gas in the desorption tower 2 can fully play the inherent catalytic desorption effect of the catalyst and the blowing and stripping effect of CO 2 to reduce gas-liquid mass transfer resistance, can ensure continuous updating of the contact surface of the catalyst and the absorption liquid through the scouring vibration effect of the CO 2 blowing bubbles on the catalyst, promote the full contact of active sites and the absorption liquid, effectively improve the catalytic desorption effect of the catalyst and realize the effect of 1+1> 2.
In the above embodiments, the system includes at least two stages of catalytic filler layers 2-2, each catalytic filler layer 2-2 is arranged at intervals along the height direction, and a layer of air jet is arranged below each stage of catalytic filler layer 2-2, so as to further improve the scouring effect of carbon dioxide on the catalytic filler layer 2-2.
Specifically, the desorption tower 2 comprises a first connecting port and a second connecting port, which are respectively connected with two ends of a liquid inlet heat exchange tube of the reboiling tower, wherein the first connecting port is positioned below the lowest catalytic packing layer 2-2, and the second connecting port is positioned between the uppermost catalytic packing layer 2-2 and the lowest desorption packing layer 2-1.
Further, the system also comprises a gas-liquid separator 12, a gas outlet pipeline is arranged on the desorption tower 2, and a liquid medium outlet of the gas-liquid separator 12 is communicated with an inner cavity of the absorption tower, wherein absorption liquid is arranged in the inner cavity.
The communicating pipe of the lean liquid outlet of the desorption tower 2 and the lean liquid return port of the absorption tower 1 is also provided with a lean liquid pump 13 to provide lean liquid flowing power.
The specific working principle of the system provided by the figure 2 is that the flue gas temperature is 130-180 ℃, high-moisture original flue gas with the water content of 10-30% enters a reboiling tower 3 and a flue gas-rich liquid heat exchanger 8 respectively, then sequentially passes through a first stage flue gas cooler 4 and a second stage flue gas cooler 5, the flue gas temperature is reduced to the optimal CO 2 absorption temperature (about 40 ℃) through multiple cooling actions, then enters an absorption tower 1, is reversely contacted with absorption liquid from a lean liquid cooler 9 and an interstage cooler 10, CO 2 is efficiently trapped by the absorbent, the flue gas is discharged through a washing section and a demister of the absorption tower 1, the rich liquid absorbed by CO 2 is conveyed through a rich liquid pump 6, firstly enters a lean liquid heat exchanger 7 and is heated to be more than 90 ℃ through heat exchange with the lean liquid, then enters the flue gas-rich liquid heat exchanger 8, then enters a desorption tower 2 after further heating, a part of CO 2 is discharged through a packing section and a bottom catalytic desorption section to realize efficient desorption, CO 2 discharged from the top of the catalytic desorption tower 2 enters a absorption tower 2, enters a catalytic desorption tower 2, a part of the CO 2 is discharged through the top of the catalytic desorption tower 2, and then enters a catalytic desorption tower 2, and a catalytic desorption system is cooled, and a part of the CO 2 is discharged through the catalytic desorption tower 2 after the CO is discharged through the catalytic desorption tower 2, the absorption section is cooled, and the CO is partially enters a catalytic desorption tower 2 after the catalytic desorption tower 2 is subjected to a part to be subjected to a cooling system to a subsequent to a cooling system to a cooling effect to a part to a cooling effect to a cooling system. The heat of the desorption tower 2 is provided by heat exchange between the lean liquid at the bottom and the raw flue gas of the reboiling tower 3 and heat exchange between the rich liquid at the top and the flue gas-rich liquid heat exchanger 8, the regenerated lean liquid is conveyed to the lean-rich liquid heat exchanger 7 from the bottom of the desorption tower 2 through the lean liquid pump 13, and enters the lean liquid cooler 9 to be further cooled to about 40 ℃ and then enters the absorption tower 1, so that the circulation of the absorption liquid is realized. Cooling water from outlets of the second-stage flue gas cooler 5, the interstage cooler 10, the lean solution cooler 9 and the gas cooler 11 is converged and then enters into a cold water intake inlet end of the first-stage flue gas heat exchanger to exchange heat with flue gas, so that the flue gas is cooled again.
The flue gas carbon dioxide trapping process system provided by the invention is described in detail. The principles and embodiments of the present invention have been described herein with reference to specific examples, the description of which is intended only to facilitate an understanding of the method of the present invention and its core ideas. It should be noted that it will be apparent to those skilled in the art that various modifications and adaptations of the invention can be made without departing from the principles of the invention and these modifications and adaptations are intended to be within the scope of the invention as defined in the following claims.
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310591154.1A CN116492814B (en) | 2023-05-24 | 2023-05-24 | Flue gas carbon dioxide entrapment process systems |
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| CN119345857B (en) * | 2024-12-25 | 2025-04-04 | 中国华能集团清洁能源技术研究院有限公司 | Flue gas cleaning and CO2Trapping coupling system and carbon trapping method |
| CN119926124A (en) * | 2025-03-06 | 2025-05-06 | 中冶南方都市环保工程技术股份有限公司 | A low energy consumption carbon capture and desorption system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214973031U (en) * | 2021-06-29 | 2021-12-03 | 华润电力（海丰）有限公司 | A carbon dioxide capture system |
| CN114082294A (en) * | 2021-12-21 | 2022-02-25 | 华能营口热电有限责任公司 | Device and method for cascade utilization of flue gas waste heat with carbon dioxide capture |
| CN114699883A (en) * | 2022-04-22 | 2022-07-05 | 浙江大学 | Catalyst-synergistic external field-enhanced carbon dioxide low-energy-consumption desorption system and method |
| CN216935390U (en) * | 2022-03-16 | 2022-07-12 | 陕西科技大学 | A high temperature hot-blast furnace flue gas carbon dioxide entrapment system for waste heat recovery |
| CN115463516A (en) * | 2022-07-22 | 2022-12-13 | 国家能源集团新能源技术研究院有限公司 | System and method for using flue gas waste heat for carbon capture regeneration |
| CN218637003U (en) * | 2022-10-31 | 2023-03-17 | 福建龙净环保股份有限公司 | Flue gas carbon dioxide capture system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2015097982A (en) * | 2013-11-18 | 2015-05-28 | 三菱日立パワーシステムズ株式会社 | Reclaiming method |
| GB2541339B (en) * | 2014-06-04 | 2021-03-31 | Toshiba Kk | Carbon dioxide recovery apparatus and method for treating exhaust gas |
| JP2018515327A (en) * | 2015-04-02 | 2018-06-14 | シーメンス アクティエンゲゼルシャフト | Apparatus and method for separating carbon dioxide from a gas stream |
| CN206823509U (en) * | 2017-04-12 | 2018-01-02 | 浙江奇彩环境科技股份有限公司 | A kind of processing system of the organic exhaust gas containing cyanogen |
| CN115254142B (en) * | 2022-05-13 | 2024-01-26 | 清华大学 | Catalytic analytical functional filler and preparation method thereof |
-
2023
- 2023-05-24 CN CN202310591154.1A patent/CN116492814B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214973031U (en) * | 2021-06-29 | 2021-12-03 | 华润电力（海丰）有限公司 | A carbon dioxide capture system |
| CN114082294A (en) * | 2021-12-21 | 2022-02-25 | 华能营口热电有限责任公司 | Device and method for cascade utilization of flue gas waste heat with carbon dioxide capture |
| CN216935390U (en) * | 2022-03-16 | 2022-07-12 | 陕西科技大学 | A high temperature hot-blast furnace flue gas carbon dioxide entrapment system for waste heat recovery |
| CN114699883A (en) * | 2022-04-22 | 2022-07-05 | 浙江大学 | Catalyst-synergistic external field-enhanced carbon dioxide low-energy-consumption desorption system and method |
| CN115463516A (en) * | 2022-07-22 | 2022-12-13 | 国家能源集团新能源技术研究院有限公司 | System and method for using flue gas waste heat for carbon capture regeneration |
| CN218637003U (en) * | 2022-10-31 | 2023-03-17 | 福建龙净环保股份有限公司 | Flue gas carbon dioxide capture system |
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