CN215693008U - System and boats and ships of carbon dioxide in separation flue gas - Google Patents
System and boats and ships of carbon dioxide in separation flue gas Download PDFInfo
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- CN215693008U CN215693008U CN202121976374.9U CN202121976374U CN215693008U CN 215693008 U CN215693008 U CN 215693008U CN 202121976374 U CN202121976374 U CN 202121976374U CN 215693008 U CN215693008 U CN 215693008U
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- flue gas
- carbon dioxide
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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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
Abstract
The utility model provides a system and a ship for desorbing carbon dioxide in flue gas, wherein the system for desorbing the carbon dioxide in the flue gas comprises an absorption device, a desorption device and a flue gas channel, wherein the flue gas channel is used for leading at least part of the flue gas to be firstly introduced into the desorption device to heat a pregnant solution absorbent to a desorption temperature and then to be introduced into the absorption device. According to the utility model, at least part of the flue gas provides energy for desorption from the rich liquid absorbent to the lean liquid absorbent, so that the absorbent can be desorbed without additionally arranging a heating device, the energy consumption is reduced, the structural complexity and the structural size are reduced, the cost is low, and the realization is easy; meanwhile, the temperature of the flue gas introduced into the absorption device can be reduced, and the effect of absorbing carbon dioxide in the flue gas is improved; furthermore, the temperature of the discharged decarbonized flue gas can be reduced, and the device is particularly suitable for ships, is favorable for reducing the heat radiation of the ships, avoids being monitored by radars, and realizes the heat stealth function.
Description
Technical Field
The utility model relates to the technical field of ship tail gas purification, in particular to a system for separating carbon dioxide in flue gas and a ship.
Background
The global warming has become an environmental problem which is widely concerned by the international society at present, and the greenhouse gas CO2Is one of the main factors of global warming, and the combustion of fossil fuels is atmospheric CO2The main source of (1) the various equipments in human production and life, especially the energy conversion equipments such as transportation vehicles such as cars and ships and generators, need to burn a large amount of hydrocarbon fuel every year and emit a large amount of CO to the atmosphere2Gas, causing the global average temperature to rise. Meanwhile, the carbon element is the cornerstone of the earth life, and CO is used by a plurality of plants and microorganisms2As an energy source, CO2Has the important function of maintaining the energy requirement of the earth biological chain. Therefore, if CO could be realized2The recycling and utilization of the waste water have obvious environmental protection significance and economic benefit.
From the current process technology, CO of automobiles2Emission has been promoted with the vigorous spread of new energy vehiclesMild, power plant CO2The emission has also achieved primary results due to the introduction of Carbon dioxide Capture and Storage (CCS) technology, but CCS technology has the disadvantages of high energy consumption, high cost and large occupied space, and thus CO is in limited space, such as in ships2The recycling and utilization of the waste water still have great technical difficulty due to the limitation of space.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects in the prior art, provides a system and a ship for separating carbon dioxide in flue gas, and realizes at least one of the following technical purposes: the desorption of carbon dioxide in the flue gas in a limited space is realized; the cost of carbon dioxide desorption in the flue gas is reduced.
In order to achieve at least one of the above objects, the present invention provides a system for separating carbon dioxide from flue gas, comprising an absorption device, a desorption device and a flue gas channel, wherein the absorption device is used for receiving flue gas and absorbing carbon dioxide in the flue gas through a lean liquid absorbent to form a rich liquid absorbent and a decarbonized flue gas; the desorption device is communicated to the absorption device, the rich liquid absorbent can be input into the desorption device, the desorption device is used for desorbing carbon dioxide in the rich liquid absorbent to form the lean liquid absorbent for the absorption device, and the lean liquid absorbent can be discharged from the desorption device and enter the absorption device; the flue gas channel is communicated to the desorption device and is used for receiving at least part of the flue gas in the flue gas and inputting the at least part of the flue gas into the desorption device; wherein, in the desorption device, the at least part of the flue gas heats the rich liquid absorbent to a desorption temperature by using the rest of heat to form the lean liquid absorbent, and the desorption device can output the lean liquid absorbent to the absorption device and output the at least part of the flue gas to the absorption device.
Optionally, the absorption device is provided with a first inlet for inputting the flue gas and a second inlet for inputting the lean liquid absorbent, and the first inlet is lower than the second inlet, so that the flue gas and the lean liquid absorbent have opposite flow directions.
Optionally, a first heat exchange channel through which at least part of the flue gas flows from bottom to top and a second heat exchange channel through which the rich liquid absorbent flows from top to bottom are arranged in the desorption device, and one of the first heat exchange channel and the second heat exchange channel is located on the circumferential inner side of the other.
Optionally, a gas-liquid separator is further provided in the desorption device, and the gas-liquid separator is used for separating the lean absorbent and the desorbed carbon dioxide.
Optionally, the flue gas channel comprises a first channel and a second channel, wherein the first channel is communicated to the desorption device for providing the at least part of the flue gas to the desorption device; the second channel is communicated with the desorption device and the absorption device so as to lead at least part of the flue gas discharged by the desorption device to the absorption device.
Optionally, the system for separating carbon dioxide from flue gas further comprises a cooling and impurity removing device, wherein the cooling and impurity removing device is arranged at the upstream of the absorption device and is used for cooling and removing impurities from the flue gas before the flue gas enters the absorption device.
Optionally, the cooling and impurity removing device further comprises a pump structure, and the pump structure is used for pumping seawater used as a cooling and impurity removing agent into the cooling and impurity removing structure.
Optionally, the system for separating carbon dioxide from flue gas further comprises a lean-rich liquid heat exchanger, which is disposed between the absorption device and the desorption device, and is used for exchanging heat between the rich liquid absorbent formed by the absorption device and the lean liquid absorbent formed by the desorption device.
Optionally, the system for separating carbon dioxide from flue gas further comprises a carbon dioxide storage device connected to the desorption device for receiving and storing carbon dioxide desorbed from the rich liquid absorbent.
Optionally, the carbon dioxide storage device comprises a gas-liquid conversion structure and a carbon dioxide storage structure which are connected, and the gas-liquid conversion structure is communicated to the desorption device and is used for converting gaseous carbon dioxide discharged from the desorption device into liquid carbon dioxide, and then conveying the liquid carbon dioxide to the carbon dioxide storage tank for storage.
Optionally, the system for separating carbon dioxide from flue gas further comprises a detection unit and a flue gas flow rate adjustment unit, wherein the detection unit is used for detecting a first flow rate of the rich liquid absorbent to the desorption device; the flue gas flow regulating unit is used for regulating a second flow of at least part of the flue gas to the desorption device according to the first flow.
Optionally, the desorption apparatus comprises a heating arrangement for heating the rich liquid absorbent to a desorption temperature together with the at least part of the flue gas to form the lean liquid absorbent.
The utility model also provides a ship, which comprises the system for separating the carbon dioxide in the flue gas, wherein the system for separating the carbon dioxide in the flue gas is used for desorbing the carbon dioxide in the flue gas generated by the power equipment of the ship.
The utility model has at least the following beneficial effects:
the utility model provides a system, a method and a ship for separating carbon dioxide in flue gas, wherein through the arrangement of a flue gas channel, at least part of flue gas flows to a desorption device firstly, so that a rich liquid absorbent in the desorption device is heated to a desorption temperature through the high-temperature flue gas, carbon dioxide is desorbed, and a lean liquid absorbent is formed, namely, energy is provided for the desorption of the rich liquid absorbent to the lean liquid absorbent through the at least part of flue gas, the energy consumption is reduced, the structural complexity and the structural size are reduced, and the cost is low and the realization is easy; meanwhile, the temperature of the flue gas introduced into the absorption device can be reduced, and the effect of absorbing carbon dioxide in the flue gas is improved; furthermore, the temperature of the discharged decarbonized flue gas can be reduced, and the device is particularly suitable for ships, is favorable for reducing the heat radiation of the ships, avoids being monitored by radars, and realizes the heat stealth function.
Drawings
FIG. 1 illustrates a schematic diagram of a system for separating carbon dioxide from a flue gas.
In the figure: 1. the cooling and impurity removing device 11, the sixth inlet 12, the seventh inlet 13, the sixth outlet 14, the seventh outlet 2, the absorption device 21, the first inlet 22, the second inlet 23, the first outlet 24, the second outlet 3, the first pump structure 4, the second pump structure 5, the desorption device 51, the third inlet 52, the fourth inlet 53, the third outlet 54, the fourth outlet 55, the fifth outlet 6, the carbon dioxide storage device 7, the heat exchange device 8, the flue gas channel 81, the first channel 82 and the second channel.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1, the present embodiment provides a system for separating carbon dioxide from flue gas, including an absorption device 2, a desorption device 5, and a flue gas channel 8, where the flue gas channel 8 is used to enable at least a part of flue gas to be input into the desorption device 5 first and then to be input into the absorption device 2.
It is understood that, in the following embodiments, the alkanolamine and the olefin alkanolamine or other substances in a proper ratio can be used as the absorbent for absorbing carbon dioxide, for example, the alkanolamine can be used as the absorbent for absorbing carbon dioxide, specifically, ethanolamine, triethylene diethanolamine, etc. can also be used as the absorbent for absorbing carbon dioxide, while the lean absorbent refers to the absorbent with unsaturated carbon dioxide content which can be used for absorbing carbon dioxide, and the rich absorbent is the absorbent formed after the lean absorbent absorbs carbon dioxide in the absorption device 2.
Wherein the absorption device 2 is used for receiving the flue gas and absorbing carbon dioxide in the flue gas through the lean liquid absorbent to form a rich liquid absorbent and a decarbonized flue gas, and the decarbonized flue gas can be discharged outwards.
In some embodiments, the flue gas has a substantially downward flow path along the absorber 2 and the lean absorbent has a substantially upward flow path along the absorber 2, such that the flue gas and the lean absorbent have opposite flow directions, thereby ensuring that the flue gas and the lean absorbent are in sufficient contact when flowing along the absorber 2.
Further, the absorption device 2 is provided with a first inlet 21 for introducing the flue gas and a second inlet 22 for introducing the lean liquid absorbent, and the first inlet 21 is lower than the second inlet 22, so that after the flue gas is introduced into the absorption device 2, the flue gas moves from bottom to top due to low density, and the lean liquid absorbent moves from top to bottom under the action of gravity, so that the flue gas can fully contact with the lean liquid absorbent, and the lean liquid absorbent can fully absorb carbon dioxide in the flue gas to form the rich liquid absorbent and the decarbonized flue gas.
Specifically, referring to fig. 1, the absorption device 2 is an absorption tower, a first inlet 21 is provided at the bottom of the absorption tower for inputting the flue gas, the at least part of the flue gas and the residual flue gas that does not flow through the desorption device 5 can enter the absorption tower through the first inlet 21, a first outlet 23 is provided at the top of the absorption tower for discharging the decarbonized flue gas, and the flue gas can completely flow through the length of the absorption tower in the vertical direction from bottom to top after entering the absorption tower, so that the flue gas has a longer circulation path in the absorption tower, and thus the carbon dioxide in the flue gas can be more fully absorbed.
Meanwhile, a second inlet 22 for introducing the lean liquid absorbent is arranged on one side of the top of the absorption tower, a second outlet 24 for discharging the rich liquid absorbent is arranged on one side of the bottom of the absorption tower, and the lean liquid absorbent can roughly completely pass through the length of the absorption tower in the vertical direction from top to bottom after entering the absorption tower, so that the lean liquid absorbent has a longer flow path in the absorption tower and can be fully contacted with the flue gas, so as to fully absorb the carbon dioxide in the flue gas and form the rich liquid absorbent and the decarbonized flue gas.
In some embodiments, a first sprayer is disposed in the absorption apparatus 2, and the first sprayer is configured to receive the lean liquid absorbent entering the absorption apparatus 2 and spray the lean liquid absorbent into the absorption apparatus 2, so that the lean liquid absorbent is in a small particle shape, and can better contact with the flue gas to absorb carbon dioxide in the flue gas.
In some embodiments, the desorption device 5 is provided with a first heat exchange channel for allowing the at least part of the flue gas to flow from bottom to top and a second heat exchange channel for allowing the rich liquid absorbent to flow from top to bottom, and one of the first heat exchange channel and the second heat exchange channel is located at the circumferential inner side of the other, so that the at least part of the flue gas and the rich liquid absorbent have opposite flow directions, thereby ensuring sufficient heat exchange between the at least part of the flue gas and the rich liquid absorbent.
Specifically, the desorption device 5 is a desorption tower, the bottom of the desorption tower is provided with a third inlet 51 for inputting the at least part of the flue gas, the top of the desorption tower is provided with a third outlet 53 for discharging the at least part of the flue gas, so that a first heat exchange channel from the third inlet 51 to the third outlet 53 is formed in the desorption tower, and the at least part of the flue gas can completely flow through the length of the desorption tower in the vertical direction from bottom to top due to the lower density after passing through the desorption tower, so that the at least part of the flue gas has a longer circulation path in the desorption tower, and further, the more sufficient heat exchange is realized.
Meanwhile, a fourth inlet 52 for inputting the rich liquid absorbent is arranged on one side of the top of the desorption tower, a fourth outlet 54 for discharging the lean liquid absorbent is arranged on one side of the bottom of the desorption tower, a second heat exchange channel is arranged between the fourth inlet 52 and the fourth outlet 54 in the desorption tower, the second heat exchange channel is positioned on the circumferential inner side of the first heat exchange channel, and the rich liquid absorbent can completely flow through the length of the desorption tower in the vertical direction from top to bottom due to the action of gravity after entering the desorption tower, so that the rich liquid absorbent has a longer circulation path in the desorption tower, and further, heat can be fully obtained from at least part of the flue gas introduced into the desorption tower.
In a further embodiment, the second heat exchange channel is provided in the desorption device 5 between the fourth inlet 52 and the fourth outlet 54, so as to increase the heat exchange area and the heat exchange time between the rich liquid absorbent in the desorption tower and the at least part of the flue gas, and further to obtain heat from the at least part of the flue gas input to the desorption device 5 more fully.
It can be understood that, in other embodiments, the second heat exchange channel may also be disposed on the circumferential inner side of the first heat exchange channel, and heat exchange between the at least part of the flue gas and the rich liquid absorbent may also be achieved, the principle and effect of which are the same as those in the above embodiments, and details are not repeated in this embodiment. It should be noted that the heat exchange tubes are arranged in a spiral shape in order to increase the heat exchange area and the heat exchange time, and therefore, the heat exchange tubes located at the inner side in the circumferential direction are generally arranged in a spiral shape.
In some embodiments, a gas-liquid separator is further disposed in the desorption device 5 for better achieving separation of the lean liquid absorbent and desorbed carbon dioxide, so as to provide the absorption device 2 with high quality of the lean liquid absorbent, and thus better achieve recycling of the absorbent.
Specifically, the gas-liquid separator, for example, a centrifugal gas-liquid separator, is provided upstream of the fourth outlet 54 of the desorption tower (i.e., the desorption device 5), an inlet of the gas-liquid separator is connected to the heat exchange pipe, a liquid-phase outlet of the gas-liquid separator is communicated to the fourth outlet 54, and a gas-phase outlet of the gas-liquid separator is communicated to the fifth outlet 55 for discharging carbon dioxide. After heat exchange with the at least part of the flue gas, the rich liquid absorbent is heated to a desorption temperature, whereby carbon dioxide is desorbed from the rich liquid absorbent and forms liquid lean liquid absorbent and gaseous carbon dioxide, the liquid lean absorbent being discharged via the fourth outlet 54 and the gaseous carbon dioxide being discharged via the fifth outlet 55.
The flue gas channel 8 is communicated to the desorption device 5, and the flue gas channel 8 is configured to receive at least a portion of the flue gas in the flue gas and input the at least a portion of the flue gas into the desorption device 5, so as to heat the rich liquid absorbent to a desorption temperature by using the at least a portion of the flue gas, and then output the rich liquid absorbent to the absorption device 2.
Further, the flue gas channel 8 comprises a first channel 81 and a second channel 82, wherein the first channel 81 is connected to the desorption device 5 for providing the at least part of the flue gas with high temperature to the desorption device 5 to heat the rich liquid absorbent in the desorption device 5 to a desorption temperature; the second passage 82 is communicated with the desorption device 5 and the absorption device 2, so that at least part of the flue gas discharged by the desorption device 5 is introduced into the absorption device 2 to absorb the carbon dioxide. It should be noted that the communication may be direct communication or indirect communication.
In particular, as shown with reference to fig. 1, the first channel 81 is connected to the third inlet 51 of the desorption device 5 to provide the at least part of the flue gas at high temperature to the desorption device 5; the inlet of the second channel 82 is connected to the third outlet 53 of the desorption device 5 to receive the at least part of the flue gas emitted by the desorption device 5, and the outlet of the second channel 82 is indirectly connected to the first inlet 21 of the absorption device 2 to pass the at least part of the flue gas into the absorption device 2.
Still further, in some embodiments, because the temperature of the at least part of the flue gas is relatively low or other reasons cause the carbon dioxide in the rich liquid absorbent to be unable to be sufficiently desorbed, in order to enable the carbon dioxide absorbed by the rich liquid absorbent to be more sufficiently desorbed, the desorption device 5 further includes a heating structure, which is used for heating the rich liquid absorbent together with the at least part of the flue gas to sufficiently desorb the carbon dioxide in the rich liquid absorbent, so that the formed lean liquid absorbent can achieve a better carbon dioxide absorption effect in the subsequent recycling.
Specifically, high-temperature water vapor is input into a desorption tower (i.e., the desorption device 5) to heat the rich liquid absorbent to the desorption temperature together with the at least part of the flue gas, for example, a reboiler is arranged at the bottom of the desorption tower, and the high-temperature water vapor generated by the reboiler flows through the desorption tower from bottom to top, i.e., has a flow direction opposite to that of the rich liquid absorbent, so that the heating of the rich liquid absorbent is realized, and the carbon dioxide in the rich liquid absorbent can be more sufficiently desorbed.
Therefore, according to the utility model, through the arrangement of the flue gas channel 8, at least part of the flue gas flows to the desorption device 5 first, so that the rich liquid absorbent in the desorption device 5 is heated to the desorption temperature by the high-temperature at least part of the flue gas, carbon dioxide is desorbed, and a lean liquid absorbent is formed, that is, the at least part of the flue gas provides energy for desorption of the rich liquid absorbent to the lean liquid absorbent, so that the energy consumption is reduced, the structural complexity and the structural size are reduced, and the cost is low and the implementation is easy; meanwhile, the temperature of the flue gas entering the absorption device 2 can be reduced, and the effect of absorbing carbon dioxide in the flue gas is improved; furthermore, the temperature of the discharged decarbonized flue gas can be reduced, the temperature of components in the system is low, the heat radiation is reduced, and particularly when the system is applied to a ship, the heat radiation of the ship is reduced, the monitoring by a radar is avoided, and the heat stealth function is realized.
In addition, because the existing absorbent has high carbon dioxide absorption efficiency when the temperature is close to the normal temperature, the temperature of at least part of the flue gas is reduced in the process of heating and warming the rich liquor absorbent, and the power consumption of the flue gas in the overall cooling process is also reduced.
In some embodiments, the system for separating carbon dioxide from flue gas further comprises a cooling and impurity removing device 1, wherein the cooling and impurity removing device 1 is arranged upstream of the absorption device 2, and is used for cooling the flue gas to an absorption temperature suitable for absorbing carbon dioxide by the lean liquid absorbent before the flue gas enters the absorption device 2, and removing impurities in the flue gas.
Furthermore, a cooling impurity removing agent used for cooling and removing impurities from the flue gas is introduced into the cooling impurity removing device 1, the flue gas has a flow path from bottom to top, and the cooling impurity removing agent has a flow path from top to bottom, so that the flue gas and the cooling impurity removing agent have opposite flow directions, and the flue gas and the cooling impurity removing agent can be fully contacted, and cooling and impurity removing of the flue gas are realized.
Still further, a sixth inlet 11 for inputting the flue gas and a seventh inlet 12 for inputting the cooling impurity-removing agent are arranged in the cooling impurity-removing device 1, the sixth inlet 11 is lower than the seventh inlet 12, so that after the flue gas enters the cooling impurity-removing device 1, the flue gas moves from bottom to top due to lower density, the cooling impurity-removing agent moves from top to bottom under the action of gravity, the flue gas can fully contact with the cooling impurity-removing agent, the cooling impurity-removing agent can fully absorb heat in the flue gas so as to reduce the temperature of the flue gas suitable for being absorbed by the barren solution absorbent, and impurities in the flue gas are removed.
Specifically, referring to fig. 1, the cooling and impurity removing device 1 is a cooling and impurity removing tower, a sixth inlet 11 for inputting the flue gas is arranged at the bottom of the cooling and impurity removing tower, a sixth outlet 13 for discharging the flue gas after cooling and impurity removing is arranged at the top of the cooling and impurity removing tower, the second channel 82 is communicated to the sixth inlet 11 to be indirectly connected to the absorption device 2, and the sixth outlet 13 is connected to the first inlet 21 of the absorption device 2. After the at least part of flue gas and the residual flue gas which does not flow through the desorption device 5 are mixed, the flue gas can roughly completely flow through the length of the cooling impurity removing tower in the vertical direction from bottom to top after being introduced into the cooling impurity removing tower, so that the flue gas has a longer circulation path in the cooling impurity removing tower, and the flue gas can be cooled and purified more fully.
Meanwhile, a seventh inlet 12 for inputting the cooling impurity removing agent is formed in the top of the cooling impurity removing tower, a seventh outlet 14 for discharging the cooling impurity removing agent is formed in the bottom of the cooling impurity removing tower, the cooling impurity removing agent enters the cooling impurity removing tower and then can roughly and completely pass through the length of the cooling impurity removing tower in the vertical direction from top to bottom, so that the cooling impurity removing agent has a longer circulation path in the cooling impurity removing tower and can be fully contacted with the flue gas, the heat of the flue gas is fully absorbed, and impurities of the flue gas are removed.
In a further embodiment, a second sprayer is arranged in the cooling impurity removing device 1, and the second sprayer is used for receiving a cooling impurity removing agent entering the cooling impurity removing device 1 through the seventh inlet 12 and spraying the cooling impurity removing agent into the cooling impurity removing device 1, so that the cooling impurity removing agent is in a small particle shape, and can be better contacted with the flue gas to realize cooling and impurity removing of the flue gas.
In a further embodiment, the cooling and impurity-removing device 1 further comprises a pump structure, and the pump structure is used for pumping seawater used as a cooling and impurity-removing agent into the cooling and impurity-removing structure. The system is particularly suitable for the system for separating carbon dioxide from flue gas on a ship so as to reduce the cost of cooling and impurity removal of the flue gas.
Therefore, the arrangement of the cooling and impurity removing device 1 is beneficial to reducing the temperature of the flue gas input into the absorption device 2, so that the effect of absorbing carbon dioxide in the flue gas is improved; furthermore, the temperature of the discharged decarbonized flue gas can be reduced, the heat radiation of ships can be reduced, the monitoring by a radar is avoided, and the heat stealth function is realized. Meanwhile, at least part of the flue gas is subjected to heat exchange in the desorption device 5, so that the temperature of at least part of the flue gas is reduced, and the power consumption of cooling the flue gas by the cooling impurity removal device 1 can be further reduced.
In some embodiments, the system for separating carbon dioxide from flue gas further comprises a heat exchanging device 7, wherein the heat exchanging device 7 is disposed between the absorption device 2 and the desorption device 5, and is used for realizing heat exchange between the rich liquid absorbent formed by the absorption device 2 and the lean liquid absorbent formed by the desorption device 5.
Further, the rich liquid absorbent discharged from the absorption device 2 is first fed into a lean rich liquid heat exchanger serving as the heat exchange device 7 and then fed into the desorption device 5, the lean liquid absorbent discharged from the desorption device 5 is first fed into the heat exchange device 7 and then fed into the absorption device 2, and in the heat exchange device 7, the lean liquid absorbent having a higher temperature transfers heat to the rich liquid absorbent, so that the temperature of the lean liquid absorbent is lowered to absorb carbon dioxide, and the temperature of the rich liquid absorbent is raised to be subsequently heated to desorb carbon dioxide.
Specifically, referring to fig. 1, the second outlet 24 of the absorption device 2 for discharging the rich liquid absorbent is connected to the heat exchange device 7 and then connected to the fourth inlet 52 of the desorption device 5 for inputting the rich liquid absorbent, the fourth outlet 54 of the desorption device 5 for discharging the lean liquid absorbent is connected to the heat exchange device 7 and then connected to the second inlet 22 of the absorption device 2 for inputting the lean liquid absorbent, and the lean liquid absorbent and the rich liquid absorbent can exchange heat in the heat exchange device 7.
More specifically, a first pump structure 3 is connected to the second outlet 24 of the absorption device 2 for discharging the rich absorbent so as to pump the rich absorbent into the heat exchange device 7 and the desorption device 5, and a second pump structure 4 is connected to the fourth outlet 54 of the desorption device 5 for discharging the lean absorbent so as to pump the lean absorbent into the heat exchange device 7 and the absorption device 2.
Therefore, according to the utility model, the heat exchange device 7 is arranged between the absorption device 2 and the desorption device 5, so that heat exchange between the lean liquid absorbent and the rich liquid absorbent is realized, the temperature of the lean liquid absorbent is reduced so as to absorb carbon dioxide, the temperature of the rich liquid absorbent is increased so as to desorb carbon dioxide, and further, the effect of realizing energy transfer and rebalancing in a closed-loop system is achieved, and the reduction of the energy consumption of the whole system is facilitated.
In some embodiments, the system for separating carbon dioxide from flue gas further comprises a carbon dioxide storage device 6, and the carbon dioxide storage device 6 is connected to the desorption device 5 for receiving and storing carbon dioxide desorbed from the rich liquid absorbent.
Specifically, referring to fig. 1, the carbon dioxide storage device 6 includes a carbon dioxide storage tank connected to a fifth outlet 55 of the desorption device 5 for discharging desorbed carbon dioxide, and gaseous carbon dioxide discharged from the desorption device 5 is input to the carbon dioxide storage tank and stored.
In other embodiments, the carbon dioxide storage device 6 includes a gas-liquid conversion structure and a carbon dioxide storage tank, the gas-liquid conversion structure is connected to the fifth outlet 55 of the desorption device 5 for discharging desorbed carbon dioxide, and gaseous carbon dioxide discharged from the desorption device 5 is cooled and/or pressurized by the gas-liquid conversion structure to convert gaseous carbon dioxide into liquid carbon dioxide, and then is conveyed to the carbon dioxide storage tank for storage.
In some embodiments, the system for separating carbon dioxide from flue gas further comprises a detection unit and a flue gas flow regulation unit. Wherein the detection unit is used for detecting the first flow rate of the rich liquid absorbent to the desorption device 5, for example, a flow rate sensor arranged between the downstream of the second outlet 24 and the upstream of the fourth inlet 52 can be adopted; the flue gas flow regulating unit is adapted to regulate a second flow of the at least part of the flue gas to the desorption device 5 in dependence of the first flow, for example by controlling the power of a fan for driving the at least part of the flue gas into the first channel 81.
Therefore, the detection unit and the flue gas flow adjusting unit are arranged, so that the flow of at least part of the flue gas for heating the rich liquid absorbent can be adjusted according to the flow of the rich liquid absorbent, the heating effect can be fully ensured, and the high system automation degree is realized.
The embodiment also provides a method for desorbing carbon dioxide in flue gas, which comprises a carbon dioxide absorption step and a rich liquid absorbent desorption step.
Wherein the carbon dioxide absorption step is specifically as follows: absorbing carbon dioxide in the flue gas by using a lean liquid absorbent to form a rich liquid absorbent and decarbonized flue gas;
the rich liquid absorbent desorption step specifically comprises the following steps: heating the rich liquid absorbent by using the residual heat of at least part of the flue gas in the flue gas to desorb the carbon dioxide in the rich liquid absorbent and form the lean liquid absorbent, wherein the carbon dioxide absorption step is performed on the at least part of the flue gas after the rich liquid absorbent is heated.
In some embodiments, the method for desorbing carbon dioxide from flue gas further comprises the step of: heat exchange is performed on the rich liquid absorbent and the lean liquid absorbent to lower the temperature of the lean liquid absorbent and to raise the temperature of the rich liquid absorbent.
In some embodiments, the method of desorbing carbon dioxide from a flue gas adjusts the second flow rate of the at least part of the flue gas in dependence on the first flow rate of the rich liquid absorbent formed in the carbon dioxide absorption step.
In some embodiments, the flue gas cannot directly heat the rich liquid absorbent to a temperature sufficient for desorption and regeneration due to a low temperature of the flue gas or other reasons, and therefore, in the rich liquid absorbent desorption step, the rich liquid absorbent is also heated by the heating structure, that is, the rich liquid absorbent is heated by the heating of the heating structure and the residual heat of at least part of the flue gas together to a desorption temperature at which carbon dioxide can be more sufficiently desorbed from the rich liquid absorbent.
Specifically, high-temperature steam is input into the desorption device, the high-temperature steam and the rich liquid absorbent have opposite flow directions, for example, the high-temperature steam moves from bottom to top, the rich liquid absorbent moves from top to bottom, and desorption and regeneration of the rich liquid absorbent are finally realized through heat exchange between the high-temperature steam and the rich liquid absorbent on the basis of primary heating of the rich liquid absorbent by the at least part of flue gas. And, because the at least part of the flue gas is input to heat the rich liquid absorbent, the temperature of the rich liquid absorbent is increased, and the usage amount of the high-temperature steam can be correspondingly reduced, i.e. the power consumption for increasing the temperature of the rich liquid absorbent is less.
Therefore, according to the method for desorbing carbon dioxide in flue gas provided by the utility model, the rich liquid absorbent is heated to the desorption temperature through the high-temperature at least part of flue gas, carbon dioxide is desorbed, and a lean liquid absorbent is formed, namely, energy is provided for desorption of the rich liquid absorbent to the lean liquid absorbent through the at least part of flue gas, so that desorption of the absorbent can be realized without additionally arranging a heating device, energy consumption is reduced, the structural complexity and the structural size are reduced, and the method is low in cost and easy to realize; meanwhile, the temperature of at least part of the flue gas can be reduced, and the subsequent carbon dioxide absorption effect can be improved; furthermore, the temperature of the discharged decarbonized flue gas can be reduced, the heat radiation of ships can be reduced, the monitoring by a radar is avoided, and the heat stealth function is realized.
The embodiment also provides a ship, which comprises the system for separating the carbon dioxide in the flue gas, and the system is used for desorbing the carbon dioxide in the tail gas generated by the power equipment of the ship.
It can be understood that, when the system for separating carbon dioxide from flue gas is loaded on the ship, the specific structure of the system for separating carbon dioxide from flue gas can be applied, so the specific technical effects are the same, and the details are not repeated in this embodiment.
Further, the system of carbon dioxide in the separation flue gas is particularly useful for narrow and small spaces such as boats and ships because compact structure, just the system of carbon dioxide in the separation flue gas is applied to in the boats and ships, because the temperature of exhaust decarbonization flue gas is lower, is close the normal temperature, still is favorable to reducing the heat radiation of boats and ships, avoids being monitored by the radar, has the function of realizing the hot stealthy of boats and ships.
Claims (12)
1. A system for separating carbon dioxide from flue gas, comprising:
an absorption device for receiving flue gas and absorbing carbon dioxide in the flue gas by a lean liquid absorbent to form a rich liquid absorbent and a decarbonized flue gas;
a desorption device communicated to the absorption device, the rich liquid absorbent being capable of being input into the desorption device, the desorption device being used for desorbing carbon dioxide in the rich liquid absorbent to form the lean liquid absorbent for the absorption device, the lean liquid absorbent being capable of being discharged from the desorption device and entering the absorption device; and
the flue gas channel is communicated to the desorption device and used for receiving at least part of the flue gas in the flue gas and inputting the at least part of the flue gas into the desorption device;
wherein, in the desorption device, the at least part of the flue gas heats the rich liquid absorbent to a desorption temperature with the remaining heat to form the lean liquid absorbent, and the desorption device is capable of outputting the lean liquid absorbent to the absorption device and outputting the at least part of the flue gas to the absorption device.
2. The system for separating carbon dioxide from flue gas according to claim 1, wherein a first inlet for feeding the flue gas and a second inlet for feeding the lean absorbent are provided in the absorption unit, and the first inlet is lower than the second inlet, so that the flue gas and the lean absorbent have opposite flow directions.
3. The system for separating carbon dioxide from flue gas according to claim 1 or 2, wherein the desorption device is provided with a first heat exchange channel for allowing at least part of the flue gas to flow from bottom to top and a second heat exchange channel for allowing the rich liquid absorbent to flow from top to bottom, and one of the first heat exchange channel and the second heat exchange channel is located on the circumferential inner side of the other.
4. The system for separating carbon dioxide from flue gas according to claim 1, wherein a gas-liquid separator is further provided in the desorption device, and the gas-liquid separator is used for separating the lean liquid absorbent and desorbing the carbon dioxide.
5. The system for separating carbon dioxide from a flue gas of claim 1, wherein the flue gas channel comprises:
a first channel communicating to the desorption device for providing the at least part of the flue gas to the desorption device; and
and the second channel is communicated with the desorption device and the absorption device so as to lead at least part of the flue gas discharged by the desorption device to the absorption device.
6. A system for separating carbon dioxide from flue gas according to claim 1 or 5, further comprising a cooling and impurity removing device disposed upstream of the absorption device for cooling and removing impurities from the flue gas before the flue gas enters the absorption device.
7. The system for separating carbon dioxide from flue gas according to claim 6, wherein the cooling and impurity removing device further comprises a pump structure, and the pump structure is used for pumping seawater used as a cooling and impurity removing agent into the cooling and impurity removing structure.
8. The system for separating carbon dioxide from flue gas according to claim 1, further comprising a lean-rich liquid heat exchanger disposed between the absorption device and the desorption device for exchanging heat between the rich liquid absorbent formed by the absorption device and the lean liquid absorbent formed by the desorption device.
9. The system for separating carbon dioxide from flue gas as claimed in claim 1, further comprising a carbon dioxide storage device connected to said desorption device for receiving and storing carbon dioxide desorbed from said rich liquid absorbent.
10. The system for separating carbon dioxide from flue gas according to claim 9, wherein the carbon dioxide storage device comprises a gas-liquid conversion structure and a carbon dioxide storage structure which are connected, and the gas-liquid conversion structure is communicated to the desorption device and is used for converting gaseous carbon dioxide discharged from the desorption device into liquid carbon dioxide, and then conveying the liquid carbon dioxide to the carbon dioxide storage tank for storage.
11. The system for separating carbon dioxide from flue gas as claimed in claim 1, further comprising:
a detection unit for detecting a first flow rate of the rich liquid absorbent to the desorption device; and
a flue gas flow regulating unit for regulating a second flow of the at least part of the flue gas to the desorption device in dependence of the first flow.
12. A marine vessel, comprising:
a system for separating carbon dioxide from flue gas according to any one of claims 1 to 11 for desorbing carbon dioxide from flue gas generated by a power plant of said vessel.
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| CN202121976374.9U CN215693008U (en) | 2021-08-20 | 2021-08-20 | System and boats and ships of carbon dioxide in separation flue gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113750744A (en) * | 2021-08-20 | 2021-12-07 | 中国船舶重工集团公司第七一一研究所 | System and method for separating carbon dioxide in flue gas and ship |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113750744A (en) * | 2021-08-20 | 2021-12-07 | 中国船舶重工集团公司第七一一研究所 | System and method for separating carbon dioxide in flue gas and ship |
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Address after: 201108 Shanghai city Minhang District Huaning Road No. 3111 Patentee after: The 711 Research Institute of China Shipbuilding Corp. Address before: 201108 Shanghai city Minhang District Huaning Road No. 3111 Patentee before: Shanghai Marine Diesel Engine Research Institute |