CN113842752A - Desorption of CO from flue gas2System and ship - Google Patents

Desorption of CO from flue gas2System and ship Download PDF

Info

Publication number
CN113842752A
CN113842752A CN202111283923.9A CN202111283923A CN113842752A CN 113842752 A CN113842752 A CN 113842752A CN 202111283923 A CN202111283923 A CN 202111283923A CN 113842752 A CN113842752 A CN 113842752A
Authority
CN
China
Prior art keywords
branch
desorption
pipeline
flue gas
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN202111283923.9A
Other languages
Chinese (zh)
Inventor
肖凯华
李珂
李晓波
黄昊
苏畅
申博涵
陈秋燕
侯志鹏
俞志鹏
尚铭凯
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shanghai Marine Diesel Engine Research Institute
Original Assignee
Shanghai Marine Diesel Engine Research Institute
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shanghai Marine Diesel Engine Research Institute filed Critical Shanghai Marine Diesel Engine Research Institute
Priority to CN202111283923.9A priority Critical patent/CN113842752A/en
Publication of CN113842752A publication Critical patent/CN113842752A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B17/00—Vessels parts, details, or accessories, not otherwise provided for
    • B63B17/06—Refuse discharge, e.g. for ash
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
    • 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

Abstract

The application provides a desorption CO in flue gas2The system and the ship, the desorption of CO in the flue gas2The system comprises an absorption device, a desorption device, a first branch and a second branch, wherein the rich absorbent formed by the absorption device is divided into a first branch and a second branch, and the first branch is separated from the CO desorbed by the first branch and the desorption device2And the second branch flow exchanges heat with at least one of the lean absorbent and the flue gas through the second branch flow, and the regeneration energy consumption of the rich absorbent is reduced by comprehensively utilizing heat from different sources.

Description

Desorption of CO from flue gas2System and ship
Technical Field
The application relates to the technical field of flue gas treatment, in particular to a method for desorbing CO in flue gas2The system and the ship.
Background
Global warming has become a widely recognized environmental problem in international society, and according to related estimates, CO in air has been generated after industrial revolution2The concentration of (A) has been kept at a relatively rapid rate of increase, approximately before the industrial revolution of CO2The concentration is 2-3 times, so that the aim of carbon emission reduction is put forward in various countries.
Combustion of fossil fuels being atmospheric CO2The major sources of human production activity, in particular in transportation vehicles, such as cars, ships, etc., burn large amounts of hydrocarbon fuel every year, thus emitting large amounts of CO into the atmosphere2Greenhouse gases cause the global average temperature to rise continuously. However, in fact, carbon is the cornerstone of earth's life, and many plants and microorganisms use CO2As an energy source, the energy requirements of the Earth's biological chain are maintained, so if CO could be achieved2The recycling and utilization of the waste water have obvious environmental protection significance and economic benefit.
From the current process technology, CO of automobiles2The emission is already alleviated along with the vigorous popularization of new energy vehicles, and CO of a power plant2Emissions have also achieved preliminary success due to the introduction of Carbon dioxide Capture and Storage (CCS) technology, but the realization of CO in confined spaces (e.g. in ships)2The recovery and utilization of the oil still have great technical difficulty. Due to the current realization of CO2The recycling technology has the problems of high energy consumption, high cost and large occupied space, so that the recycling technology is difficult to apply to occasions with limited space. In carbonIn the present of rising emission reduction, there is an urgent need to develop a low-energy-consumption and high-efficiency CO suitable for limited space2A trapping technique.
Disclosure of Invention
The application provides a desorption CO in flue gas2The system and the ship to solve the problem of CO desorption in the existing flue gas2The system has high energy consumption and is not suitable for the technical problem of limited space of ships and the like.
The application provides a desorption CO in flue gas2The system comprises an absorption device, a first pipeline, a desorption device, a second pipeline and a third pipeline, wherein the third pipeline comprises a first branch and a second branch. Wherein the absorption device is used for absorbing CO in the flue gas by lean absorbent2And forming a rich absorbent; the first pipeline is connected with the absorption device and is used for supplying the flue gas to the absorption device; the desorption device is used for desorbing CO in the rich absorbent2And forming the lean absorbent; the second line is connected between the absorption device and the desorption device for feeding the lean absorbent from the desorption device to the absorption device; the first branch and the second branch are both connected between the absorption device and the desorption device and are used for supplying the rich absorbent from the absorption device to the desorption device.
The rich absorbent formed by the absorption means is split into a first split stream and a second split stream, the first split stream being CO desorbed from the desorption means via the first branch2And the water vapor in the desorption device exchanges heat, and the second branch flow exchanges heat with at least one of the lean absorbent and the flue gas through the second branch path.
Optionally, the top of the desorption device is connected with the first branch, and CO is arranged at the top of the desorption device2And (7) an outlet.
Optionally, desorbing CO from the flue gas2The system comprises a gas-liquid heat exchanger, a gas side of the gas-liquid heat exchanger is arranged in the first pipeline, and a liquid side of the gas-liquid heat exchanger is arranged in the second branch.
Optionally, desorbing CO from the flue gas2The system of (1) further comprises a first heat exchanger, and two sides of the first heat exchanger are respectively configured in the second pipeline and the second branch.
Optionally, desorbing CO from the flue gas2The system also comprises a first heat exchanger and a gas-liquid heat exchanger, wherein two sides of the first heat exchanger are respectively arranged in the second pipeline and the second branch; a gas side of a gas-liquid heat exchanger is arranged in the first pipeline, and a liquid side of the gas-liquid heat exchanger is arranged in the second branch; and, in the second branch, the first heat exchanger is located upstream of the liquid-gas heat exchanger.
Optionally, a first circulation power mechanism is disposed in the second pipeline, and the first circulation power mechanism is located downstream of the first heat exchanger.
Optionally, a second heat exchanger is further disposed in the second pipeline, and the second heat exchanger is located downstream of the first heat exchanger.
Optionally, the bottom of the absorption device is connected with the first pipeline, and the top of the absorption device is connected with the second pipeline.
Optionally, the top of the desorption device is connected with the first branch and the second branch, the bottom of the desorption device is connected with the second pipeline, a reboiler is arranged in the second pipeline, and a gas outlet of the reboiler is connected to the bottom of the desorption device; the reboiler also comprises a heating pipeline and an overflow plate, wherein the heating pipeline is used for introducing an external heat-conducting medium into the reboiler; the overflow plate divides the interior of the reboiler into a heating cavity and a barren solution temporary storage cavity, the heating cavity is communicated with the desorption device through the second pipeline, and the barren solution temporary storage cavity is communicated with the absorption device through the second pipeline.
Optionally, the rich absorbent outlet of the absorption device is connected to the temporary storage and the second circulation power mechanism and then connected to the first branch and the second branch.
Alternatively, saidDesorption of CO from flue gas2The system according to (1) further comprises a third branch, from which the rich absorbent formed in the absorption device is also branched, the third branch being fed again to the absorption device via the third branch.
Optionally, the third leg connects the bottom of the absorbent device and the top of the absorbent device.
The invention also provides a method for desorbing CO in flue gas2The system comprises an absorption device, a desorption device, a first pipeline, a second pipeline, a third pipeline, a first heat exchanger and a gas-liquid heat exchanger.
Wherein the absorption device has a lean absorbent inlet, a rich absorbent outlet, a flue gas inlet, and a flue gas outlet; the desorption device is provided with a first rich absorbent inlet, a second rich absorbent inlet, a lean absorbent outlet, a heat medium inlet and CO2An outlet; the first pipeline is connected with the flue gas inlet and is used for supplying the flue gas to the absorption device; the second pipeline is connected with the lean absorbent outlet and the lean absorbent inlet, a first circulation power mechanism and a liquid side of a reboiler are arranged in the second pipeline, and a gas side of the reboiler is connected to the heat medium inlet; a second circulating power mechanism is arranged in the third pipeline, the third pipeline comprises a first branch and a second branch, and the first branch is connected with the rich absorbent outlet and the first rich absorbent inlet; the second branch is connected with the rich absorbent outlet and the second rich absorbent inlet; two sides of the first heat exchanger are respectively arranged in the second branch and the second pipeline; a gas side of the gas-liquid heat exchanger is disposed in the first conduit and a liquid side is disposed in the second branch.
Optionally, the third pipeline further includes a third branch, and the absorption apparatus further includes a third rich absorbent inlet, and the third branch connects the third rich absorbent inlet and the rich absorbent outlet.
The invention also provides a ship which comprises the step of desorbing CO in the flue gas2The system of (1), desorbing CO in the flue gas2The system of (A) is any of the aboveDesorbing CO in flue gas2The system of (1).
The application has at least the following beneficial effects:
the invention provides a method for desorbing CO in flue gas2The system and the ship extract part of the rich absorbent for regeneration, thereby reducing the regeneration energy consumption of the rich absorbent; and the heat from different sources is comprehensively utilized, and the regeneration energy consumption of the rich absorbent is reduced.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 illustrates exemplary desorption of CO from flue gas in accordance with the present invention2Schematic structural diagram of the system of (1).
In the figure, 1-absorption means, 11-flue gas inlet, 12-flue gas outlet, 13-lean absorbent inlet, 14-rich absorbent outlet, 15-third rich absorbent inlet, 2-desorption means, 21-first rich absorbent inlet, 22-second rich absorbent inlet, 23-lean absorbent outlet, 24-heat medium inlet, 25-CO2The heat exchanger comprises an outlet, 3-a first pipeline, 4-a second pipeline, 5-a third pipeline, 51-a first branch, 52-a second branch, 53-a third branch, 6-a first circulation power mechanism, 7-a first heat exchanger, 8-a gas-liquid heat exchanger, 9-a second heat exchanger, 10-a second circulation power mechanism, 20-a temporary storage, 30-a reboiler, 31-a heating pipeline and 32-an overflow plate.
Detailed Description
The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only a part of the embodiments of the present application, 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 application.
Furthermore, it should be understood that the detailed description and specific examples, while indicating exemplary embodiments of the invention, are given by way of illustration and explanation only, and are not intended to limit the scope of the invention. In the present application, unless otherwise specified, the use of directional terms such as "upper", "lower", "left" and "right" generally refer to upper, lower, left and right in the actual use or operation of the device, and specifically to the orientation of the drawing figures.
In the application, the connection between each branch, pipeline and each component may be direct connection or indirect connection; the top, bottom, etc. refer to the area near the top or near the bottom, and not just to the location of the top or bottom ends.
The application provides a desorption CO in flue gas2The system and vessel of (2) are described in detail below. It should be noted that the following description of the embodiments is not intended to limit the preferred order of the embodiments of the present application. In the following embodiments, the descriptions of the respective embodiments have respective emphasis, and reference may be made to related descriptions of other embodiments for parts that are not described in detail in a certain embodiment.
Referring to fig. 1, the embodiment of the present application provides a method for desorbing CO in flue gas2Comprises an absorption device 1, a desorption device 2, a first pipeline 3, a second pipeline 4 and a third pipeline 5.
Wherein the absorption apparatus 1 is used for absorbing CO in flue gas by lean absorbent2And forming a rich absorbent; the first pipeline 3 is connected with the absorption device 1 and is used for supplying the flue gas to the absorption device 1; the desorption device 2 is used for desorbing CO in the rich absorbent2And forming the lean absorbent; the second line 4 is connected between the absorption unit 1 and the desorption unit 2 for feeding the lean absorbent from the desorption unit 2 to the absorption unit 1.
The third pipeline 5 comprises a first branch 51 and a second branch 52, and both the first branch 51 and the second branch 52 are connected between the absorption apparatus 1 and the desorption apparatus 2, and are used for supplying the rich absorbent from the absorption apparatus 1 to the desorption apparatus 2.
Wherein the rich absorbent formed by the absorption unit 1 is split into a first split stream and a second split stream, the first split stream being CO desorbed from the desorption unit 2 via the first branch 512A second bypass 52 for exchanging heat with at least one of the lean absorbent and the flue gas.
The CO in the desorption flue gas is further combined with the attached drawing2The main structures involved in the system of (1) are illustrated.
The first branch 51 is connected between the absorption apparatus 1 and the desorption apparatus 2, and a first partial flow of the rich absorbent leaving the absorption apparatus 1 can be supplied to the desorption apparatus 2 via the absorption apparatus 1. And, the first branch flow is capable of desorbing CO from the desorption apparatus 2 via the first branch 512Heat exchange is carried out to realize the desorption of the released CO2To desorb the released CO subsequently2Storing; at the same time, the temperature of the first split stream is raised, so that the subsequent raising of the temperature of the first split stream to realize CO desorption2The energy consumed; in practical applications, high-temperature water vapor exists in the desorption device 2, and the first branch flow can exchange heat with the water vapor that is not condensed in the desorption device 2 through the first branch 51 and absorb heat in the water vapor that is not condensed, so as to reduce heat loss.
In some embodiments, referring to fig. 1, the top of the desorption device 2 is provided with a first rich absorbent inlet 21 connected with the first branch 51, and the top of the desorption device 2 is provided with a CO inlet 212And an outlet 25. It can be seen that the first partial flow enters the desorption apparatus 2 from the top of the desorption apparatus 2 via the first branch 51, and thus has a flow direction from top to bottom; the top of the desorption device 2 is provided with CO2An outlet 25 for the desorbed CO from the desorption device 22The gas will move from bottom to top to leave the desorption unit 2, the first partial flow and the CO2Gas will generate pairs during movementThe flows are joined and heat exchange can be achieved. Thus, desorption of the liberated CO2Is lowered so as to subsequently desorb the released CO2Storing; at the same time, the temperature of the first split stream is raised, so that the subsequent raising of the temperature of the first split stream to realize CO desorption2The energy consumed.
In other embodiments, a heat exchanger is arranged in the first branch 51, and the CO leaving the desorption device 22Is introduced into the heat exchanger to exchange heat with the first split stream so as to realize the desorption of the released CO2Cooling for the subsequent desorption of the released CO2Storing; at the same time, the temperature of the first split stream is raised, so that the subsequent raising of the temperature of the first split stream to realize CO desorption2The energy consumed.
The second branch 52 is connected between the absorption unit 1 and the desorption unit 2, and a second partial flow of the rich absorbent leaving the absorption unit 1 can be fed to the desorption unit 2 via the absorption unit 1. And the second split stream exchanges heat with at least one of the lean absorbent and the flue gas via the second branch 52.
Wherein the temperature of the lean absorbent is reduced when the second split stream exchanges heat with the lean absorbent, thereby saving the subsequent cooling of the lean absorbent to enable efficient absorption of CO2The energy consumed by the temperature of (c); at the same time, the temperature of the first split stream can be increased, so that the subsequent process of increasing the first split stream to effectively desorb CO can be saved2The temperature of (a).
When the second partial flow exchanges heat with the flue gas, the temperature of the flue gas is reduced so that the flue gas does not have too high a heat in order to increase the subsequent absorption of CO in the flue gas in the absorption device 12And also contributes to reducing the temperature of the decarbonated flue gases discharged from said absorption apparatus 1; at the same time, the temperature of the first split stream can be increased, so that the subsequent process of increasing the first split stream to effectively desorb CO can be saved2The temperature of (a).
In some embodiments, the desorption of CO from the flue gas2The system of (2) comprises a gas-liquid heat exchanger 8, the first pipeline 3 is provided with a gas side of the gas-liquid heat exchanger 8, and the second branch 52 is provided with a liquid side of the gas-liquid heat exchanger 8. At the gas-liquid heat exchanger 8, the flue gas entering the absorption unit 1 via the first pipeline 3 exchanges heat with the second split stream flowing from the absorption unit 1 to the desorption unit 2 via the second branch 52, the temperature of the flue gas is reduced, and the temperature of the second split stream is increased.
In other embodiments, the desorption of CO from the flue gas2Comprises a first heat exchanger 7, and the second pipeline 4 and the second branch 52 are respectively provided with two sides of the first heat exchanger 7. At the first heat exchanger 7, the lean absorbent flowing from the desorption device 2 via the second line 4 to the absorption device 1 is heat exchanged against the second partial stream flowing from the absorption device 1 via the second branch 52 to the desorption device 2, the temperature of the lean absorbent is lowered and the temperature of the second partial stream is raised.
Here, the two sides of the first heat exchanger 7 refer to a heat medium side and a cold medium side of the first heat exchanger 7, and do not refer to two sides in physical orientation. The heat medium side and the cold medium side may be located on two sides of the first heat exchanger 7 in the physical direction, or may be located in other positions, and this embodiment does not limit the specific structure of the first heat exchanger 7.
In still other embodiments, referring to FIG. 1, the desorption of CO from the flue gas2The system of (a) is provided with both a first heat exchanger 7 and a gas-liquid heat exchanger 8.
Wherein the first conduit 3 is provided with a gas side of the gas-liquid heat exchanger 8, and the second branch 52 is provided with a liquid side of the gas-liquid heat exchanger 8. At the gas-liquid heat exchanger 8, the flue gas entering the absorption unit 1 via the first pipeline 3 exchanges heat with the second split stream flowing from the absorption unit 1 to the desorption unit 2 via the second branch 52, the temperature of the flue gas is reduced, and the temperature of the second split stream is increased.
Both sides of the first heat exchanger 7 are arranged in the second line 4 and the second branch 52, respectively. At the first heat exchanger 7, the lean absorbent flowing from the desorption device 2 via the second line 4 to the absorption device 1 is heat exchanged against the second partial stream flowing from the absorption device 1 via the second branch 52 to the desorption device 2, the temperature of the lean absorbent is lowered and the temperature of the second partial stream is raised.
Here, the two sides of the first heat exchanger 7 refer to a heat medium side and a cold medium side of the first heat exchanger 7, and do not refer to two sides in physical orientation. The heat medium side and the cold medium side may be located on two sides of the first heat exchanger 7 in the physical direction, or may be located in other positions, and this embodiment does not limit the specific structure of the first heat exchanger 7.
In some embodiments, referring to fig. 1, for the second leg 52, the first heat exchanger 7 is located upstream of the liquid-to-gas heat exchanger 8. The second split stream can thus be heat exchanged first with the lean absorbent at the first heat exchanger 7 to ensure efficient cooling of the lean absorbent and to reduce as much as possible the subsequent lowering of the lean absorbent to efficient absorption of CO2The temperature of (a). And then the second split stream exchanges heat with the flue gas at the gas-liquid heat exchanger 8 so as to reduce the temperature of the heat exchanger.
In other embodiments, the liquid-gas heat exchanger 8 may also be located upstream of the first heat exchanger 7 for the second branch 52.
The second line 4 is connected between the absorption unit 1 and the desorption unit 2 for feeding the lean absorbent from the desorption unit 2 to the absorption unit 1. In order to power the supply of lean absorbent, a first circulation power means 6 is arranged in the second line 4.
In some embodiments, CO is in the desorption flue gas2On the basis of the arrangement of the aforementioned first heat exchanger 7 in the system of (1), theThe first circulation power mechanism 6 is arranged in the second pipeline 4 at a position downstream of the first heat exchanger 7. Since the temperature of the lean absorbent flowing through the first circulation power mechanism 6 has been lowered, the first circulation power mechanism 6 does not need to be in contact with the lean absorbent having a higher temperature, and the service life of the first circulation power mechanism 6 is extended. The first circulation power mechanism 6 may be a pump or other driving mechanism, and may be a vane pump, a positive displacement pump, or the like.
In order to be able to cool the lean absorbent in the second line 4 to an optimum absorption of CO2And a second heat exchanger 9 is arranged in the second line 4, which second heat exchanger 9 is capable of cooling the lean absorbent.
In some embodiments, referring to fig. 1, on the basis of the first heat exchanger 7, the second heat exchanger 9 is arranged downstream of the first heat exchanger 7 in the second pipeline 4, the heat medium side of the second heat exchanger 9 is connected in the second pipeline 4, and the cold medium side of the second heat exchanger 9 is connected with cooling liquid, such as cooling water. The lean absorbent exchanges heat with the second split stream of the rich absorbent at the first heat exchanger 7 and is subjected to primary temperature reduction, then exchanges heat at the second heat exchanger 9, and the lean absorbent is cooled through two-stage heat exchange, so that the lean absorbent can be cooled to CO which is most suitable for absorption2Temperature, and also reduces the external energy consumed to lower the temperature of the lean absorbent.
In order to ensure that the flue gas and the lean absorbent can be more fully contacted and heat exchanged to absorb CO in the flue gas2In some embodiments, referring to fig. 1, the bottom of the absorption device 1 is provided with a flue gas inlet 11 for connecting the first pipeline 3, and the flue gas enters the absorption device 1 from the bottom of the absorption device 1 and moves upwards due to the lower density; the top of the absorption device 1 is provided with a lean absorbent inlet 13 for connecting the second pipeline 4, the lean absorbent enters the absorption device 1 from the top of the absorption device 1 and is sprayedDriven and/or gravitationally moved downward. The flue gas and the lean absorbent have opposite flow directions in the absorption device 1, and can be sufficiently intersected and contacted, so that the lean absorbent can effectively treat CO in the flue gas2Absorption of (2). In other embodiments, the absorption device 1 may be configured in other structures, and the connection positions of the first pipeline 3 and the second pipeline 4 to the absorption device 1 may be different.
The desorption device 2 is used for desorbing CO in the rich absorbent2And forming the lean absorbent in order to make the CO in the rich absorbent at the desorption unit 22Can be sufficiently desorbed, a reboiler 30 is provided at the desorption apparatus 2, the reboiler 30 is used for heating the absorbent at the desorption apparatus 2, and the reboiler 30 includes: a heating line 31, wherein the heating line 31 is used for introducing an external heat transfer medium into the reboiler, and CO is enriched in the regeneration tower (i.e. the desorption device 2)2The absorption liquid enters the reboiler 30 through the second pipeline 4, and generates CO after exchanging heat with the heat medium in the heating pipeline 31 in the reboiler 302Gas and water vapor, so that CO in the absorbent2Can be desorbed more sufficiently and form a lean absorbent having a better absorption effect. Reboiler 30 is inside to be provided with overflow plate 32, overflow plate 32 separates reboiler inside liquid and becomes heating chamber and barren liquor chamber of keeping in, with desorption apparatus 2 passes through the cavity that second pipeline 4 links to each other is the heating chamber, with absorption apparatus 1 passes through the cavity that second pipeline 4 links to each other is barren liquor chamber of keeping in, CO2In the rising process, the absorption liquid exchanges heat with the heat-conducting medium in the heating pipeline 31, rises to the height of the overflow plate 32, overflows into the barren solution temporary storage cavity, and flows to the absorption device 1 through the second pipeline 4.
In some embodiments, referring to fig. 1, the reboiler 30 is disposed in the second pipeline 4, a gas outlet of the reboiler 30 is connected to the heat medium inlet 24 at the bottom of the desorption device 2, and the heat medium inlet 24 is higher than that for connecting the second pipeline 4Lean absorbent outlet 23. CO discharged from the gas outlet of the reboiler 302The gas and the water vapor flow from bottom to top in the desorption device 2; the top of the desorption device 2 is connected with the first branch 51 and the second branch 52, the bottom of the desorption device 2 is connected with the second pipeline 4, and the rich absorbent entering the desorption device 2 from the first branch 51 and the second branch 52 moves from top to bottom. At this time, the CO2Gas and water vapor can meet and sufficiently contact the rich absorbent convection so that the CO is2The temperature of the gas and the water vapor is reduced, the water vapor is condensed and reacts with the CO2Separating gas phase; the temperature of the rich absorbent is raised, and part of CO in the rich absorbent2Is desorbed and forms a semi-lean absorbent. The semi-lean absorbent enters the reboiler 30 through the second pipeline 4, exchanges heat with the heating pipe 31 in the process of rising inside the reboiler, and finally overflows the upper edge of the overflow plate 32 to enter a lean absorbent temporary storage cavity.
In order to provide motive force for the rich absorbent to flow in the first branch 51 and the second branch 52, in some embodiments, the rich absorbent outlet 14 of the absorption device 1 is connected to the first branch 51 and the second branch 52 after being connected to the second circulation motive device 10. The second power cycle mechanism 10 is capable of simultaneously powering the rich absorbent in the first branch 51 and the second branch 52. The second circulation power mechanism 10 may be a pump or the like. In other embodiments, the first branch 51 and the second branch 52 may be respectively provided with a circulating power mechanism.
In order to store the rich absorbent leaving the absorption unit 1 for feeding to the desorption unit 2 as required. In some embodiments, the rich absorbent outlet 14 of the absorption device 1 is connected to the temporary storage 20 and then connected to the first branch 51 and the second branch 52.
In some embodiments, referring to fig. 1, the rich absorbent outlet 14 of the absorption device 1 is connected to the temporary storage 20 and the second power cycle mechanism 10, and then connected to the first branch 51 and the second branch 52. In this embodiment, the connection order between the temporary storage device 20 and the second power cycle mechanism 10 is not limited. For example, the temporary storage device 20 may be connected first and then the second power cycle mechanism 10 may be connected. The temporary storage 20 may be a temporary storage tank, a temporary storage bucket, etc. In other embodiments, the rich absorbent outlet 14 of the absorption device 1 is connected to the temporary storage 20 and then connected to the first branch 51 and the second branch 52, and the first branch 51 and the second branch 52 may be respectively provided with a circulating power mechanism.
In the foregoing embodiment, the ratio of the first split flow to the second split flow may be specifically adjusted according to the actual use requirement. In some embodiments, the ratio of the first split stream to the second split stream is from 5:95 to 20: 80.
The applicant has also found that the rich absorbent leaving the absorption unit 1 absorbs a certain amount of CO despite the absorption of CO2However, normally the rich absorbent has not yet reached a state of complete absorption saturation, i.e. the rich absorbent can still be used for absorbing CO in the flue gas2. Thus, in some embodiments, the desorption of CO from the flue gas2The system of (2) further comprises a third branch 53, from which the rich absorbent formed by the absorption unit 1 is further branched, and which is fed again to the absorption unit 1 via the third branch 53, in order to reuse the third branch and reduce the energy consumed for regenerating the rich absorbent. The specific proportion of the third partial flow in the rich absorbent formed in the absorption unit 1 can be adjusted according to the actual use requirements.
In some embodiments, the third branch 53 connects the bottom of the absorption apparatus 1 and the top of the absorption apparatus 1, and the rich absorbent leaving the absorption apparatus 1 leaves the absorption apparatus 1 from the bottom and enters the absorption apparatus 1 from the top again to absorb the CO contained in the flue gas in the absorption apparatus 12. In other embodiments, the connection position of the third branch 53 and the absorption apparatus 1 may be determined according to different structures of the absorption apparatus 1 or other requirements such as site restrictionsThe position may be other positions, and this embodiment is not limited.
Illustratively, referring to FIG. 1, the desorption of CO from flue gas2The system of (1) comprises the third branch 53, the temporary storage 20 and the second circulating power mechanism 10, and the rich absorbent outlet 14 of the absorption device 1 is connected with the temporary storage 20 and the second circulating power mechanism 10 and then connected with the first branch 51, the second branch 52 and the third branch 53. The second circulation power mechanism 10 simultaneously provides power for the movement of the fat absorbent in the first branch 51, the second branch 52 and the third branch 53.
Application example 1
In the present application example, the desorption of CO in the flue gas2The system comprises an absorption device 1, a desorption device 2, a first pipeline 3, a second pipeline 4, a third pipeline 5, a first heat exchanger 7 and a gas-liquid heat exchanger 8.
Wherein the absorption device 1 has a flue gas inlet 11, a flue gas outlet 12, a lean absorbent inlet 13 and a rich absorbent outlet 14; the desorption device 2 has a first rich absorbent inlet 21, a second rich absorbent inlet 22, a lean absorbent outlet 23, a heat medium inlet 24 and CO2And an outlet 25.
Said first pipe 3 is connected to said flue gas inlet 11 for supplying said flue gas to said absorption unit 1; the second pipeline 4 connects the lean absorbent outlet 23 and the lean absorbent inlet 13, and the second pipeline 4 is provided with a first circulation power mechanism 6 and a liquid side of a reboiler 30, and a gas side of the reboiler 30 is connected to the heat medium inlet 24; a second circulating power mechanism 10 is arranged in the third pipeline 5, the third pipeline 5 comprises a first branch 51 and a second branch 52, and the first branch 51 is connected with the rich absorbent outlet 14 and the first rich absorbent inlet 21; the second branch 52 connects the rich absorbent outlet 14 and the second rich absorbent inlet 22; both sides of the first heat exchanger 7 are respectively arranged in the second branch 52 and in the second pipeline 4; the gas side of the gas-liquid heat exchanger 8 is disposed in the first conduit 3, and the liquid side is disposed in the second branch 52.
When in use, the carbon-containing flue gas firstly flows through the gas-liquid heat exchanger 8 to exchange heat with the second sub-stream, and the cooled flue gas enters CO2Absorption column (i.e. the absorption apparatus 1) in CO2In the absorption tower, the flue gas and the lean absorbent are subjected to convective mass transfer and are subjected to CO removal2Can be discharged outwards, while the lean absorbent absorbs CO2The latter becomes the rich absorbent, which is CO2Has a low absorption capacity and can be reused after regeneration.
In order to reduce the energy consumption for regeneration of the rich absorbent, in this example a part of the rich absorbent is tapped off as the first split stream, and the first split stream is fed via the first branch 51 to the CO2The remaining part of the rich absorbent becomes the second split stream, and the second split stream is sent to the CO after passing through the first heat exchanger 7 and the gas-liquid heat exchanger 8 via the second branch 522A regeneration column into which said CO is introduced2The rich absorbent of the regenerator column is mixed with high temperature steam and CO from the reboiler 302The gas exchanges heat, and CO in the rich absorbent2Is desorbed and becomes the lean absorbent.
It is known that part of the rich absorbent (i.e. the second split stream) exchanges heat with the flue gas and the lean absorbent before regeneration, and the rich absorbent is preheated, which helps to reduce the energy consumption required for regeneration; at the same time, the temperature of the flue gas and the lean absorbent is reduced, contributing to improving CO2The absorption effect reduces the energy consumption required for cooling the lean absorbent, and the temperature of the discharged decarbonized flue gas is reduced.
The lean absorbent is fed via the second line 4 into the heating chamber of the reboiler 30 and further heated to desorb CO2And water vapor, then flows through the first heat exchanger 7 to be cooled and then can be sent into the CO again2The absorption tower and the second heat exchanger 9 can be configured in the second pipeline 4 to further cool the lean absorbent to a temperature more suitable for absorbing CO2The temperature of (2). The above-mentionedHigh temperature CO exiting reboiler 302And steam re-entering the CO2The regeneration tower exchanges heat with the rich absorbent to desorb the sucked CO2And steam temperature is high, and the temperature of the steam entering the first branch is low due to no heat exchange, so that the CO can be treated2Exchanging heat with steam to reduce temperature, and reducing temperature of CO2More convenient for subsequent storage and utilization, in the application example, the CO is2Introducing CO2And storing in a storage tank.
It is known that part of the rich absorbent (i.e. the first split stream) is associated with high temperature CO2Exchanging heat with steam to make CO2Is separated from the water vapor phase, and CO2The temperature of the liquid is reduced, so that the subsequent storage and utilization are facilitated; at the same time, the temperature of the first split stream is increased, contributing to CO in the first split stream2Is desorbed and can reduce the energy consumption required to heat the first substream.
Application example two
Concrete structure of the application example and desorption of CO in flue gas2And the process of regenerating the absorbent is substantially the same as in the first application example, except that in this application example, the third pipeline 5 further comprises a third branch 53, and the CO is regenerated by the third branch 532The absorption column, i.e. the absorption unit 1, further has a third rich absorbent inlet 15, and the third branch 53 connects the third rich absorbent inlet 15 and the rich absorbent outlet 14. The rich absorbent is also split out of the third split, which separates the CO2Enters the CO again through the third branch 53 after the absorption tower2An absorption tower.
It is known that part of the rich absorbent (i.e. the third split stream) is directly reused for CO in flue gas without regeneration2The energy consumption required for regeneration of the rich absorbent is reduced.
The embodiment of this application still provides a boats and ships, boats and ships are including aforesaid CO in desorption flue gas2The system of (1), desorbing CO in the flue gas2For subjecting the exhaust gas of said vessel to CO2And (5) absorption treatment.
It will be appreciated that the vessel includes the aforementioned desorption of CO from flue gas2In the system of the present invention, the structures shown in the foregoing embodiments can be correspondingly applied to the ship, so that the ship can also have corresponding technical effects, and details are not described in this embodiment.
The above provides the present application with respect to desorbing CO from flue gas2The system and the ship are introduced in detail, and the principle and the implementation mode of the application are explained by applying specific examples, and the description of the above examples is only used for helping to understand the method and the core idea of the application; meanwhile, for a person skilled in the art, according to the idea of the present application, there may be variations in the specific embodiments and the application scope, and in summary, the content of the present specification should not be construed as a limitation to the present application.

Claims (15)

1. Desorbing CO in flue gas2The system of (a), characterized by comprising,
an absorption apparatus for absorbing CO in flue gas by lean absorbent2And forming a rich absorbent;
the first pipeline is connected with the absorption device and is used for supplying the flue gas to the absorption device;
desorption means for desorbing CO from said rich absorbent2And forming the lean absorbent;
a second line connected between the absorption device and the desorption device for supplying the lean absorbent from the desorption device to the absorption device; and
a third pipeline comprising a first branch and a second branch, wherein the first branch and the second branch are connected between the absorption device and the desorption device, and are used for supplying the rich absorbent from the absorption device to the desorption device;
wherein the rich absorbent formed by the absorption device is split into a first split stream and a second split stream, the first split stream being the CO desorbed from the desorption device via the first branch2And the solutionAnd the water vapor in the suction device exchanges heat, and the second branch flow exchanges heat with at least one of the lean absorbent and the flue gas through the second branch circuit.
2. The desorption of CO in flue gas as claimed in claim 12The system is characterized in that the top of the desorption device is connected with the first branch, and CO is arranged at the top of the desorption device2And (7) an outlet.
3. The desorption of CO in flue gas as claimed in claim 12The system of (1) further comprises a gas-liquid heat exchanger, the first pipeline is provided with a gas side of the gas-liquid heat exchanger, and the second branch is provided with a liquid side of the gas-liquid heat exchanger.
4. The desorption of CO in flue gas as claimed in claim 12The system of (2), characterized by also including first heat exchanger, dispose the both sides of first heat exchanger in second pipeline and the second branch road respectively.
5. The desorption of CO in flue gas as claimed in claim 12The system is characterized by also comprising a first heat exchanger and a gas-liquid heat exchanger, wherein,
two sides of the first heat exchanger are respectively arranged in the second pipeline and the second branch;
a gas side of a gas-liquid heat exchanger is arranged in the first pipeline, and a liquid side of the gas-liquid heat exchanger is arranged in the second branch;
and, in the second branch, the first heat exchanger is located upstream of the liquid-gas heat exchanger.
6. The desorption of CO in flue gas as claimed in claim 52The system of (2) is characterized in that a first circulation power mechanism is arranged in the second pipeline, and the first circulation power mechanism is positioned at the downstream of the first heat exchanger.
7. The desorption of CO in flue gas as claimed in claim 62The system of (a), wherein a second heat exchanger is also disposed in the second conduit, the second heat exchanger being downstream of the first heat exchanger.
8. The desorption of CO in flue gas as claimed in claim 12The system is characterized in that the bottom of the absorption device is connected with the first pipeline, and the top of the absorption device is connected with the second pipeline.
9. The desorption of CO in flue gas as claimed in claim 12The system is characterized in that the top of the desorption device is connected with the first branch and the second branch, the bottom of the desorption device is connected with the second pipeline, a reboiler is arranged in the second pipeline, and a gas outlet of the reboiler is connected to the bottom of the desorption device;
the reboiler also comprises a heating pipeline and an overflow plate, wherein the heating pipeline is used for introducing an external heat-conducting medium into the reboiler; the overflow plate divides the interior of the reboiler into a heating cavity and a barren solution temporary storage cavity, the heating cavity is communicated with the desorption device through the second pipeline, and the barren solution temporary storage cavity is communicated with the absorption device through the second pipeline.
10. The desorption of CO in flue gas as claimed in claim 12The system is characterized in that a rich absorbent outlet of the absorption device is connected with the temporary storage device and the second circulation power mechanism and then is connected with the first branch and the second branch.
11. The desorption of CO in flue gas as claimed in claim 12The system according to (1), characterized in that it further comprises a third branch, from which said fat absorbent formed by said absorption means is also branched, said third branch being fed again to said absorption means via said third branch.
12. The desorption of CO in flue gas of claim 112Wherein the third leg connects the bottom of the absorbent device and the top of the absorbent device.
13. Desorbing CO in flue gas2The system of (a), characterized by comprising,
an absorption unit having a lean absorbent inlet, a rich absorbent outlet, a flue gas inlet, and a flue gas outlet;
a desorption unit having a first rich absorbent inlet, a second rich absorbent inlet, a lean absorbent outlet, a heat medium inlet and CO2An outlet;
the first pipeline is connected with the flue gas inlet and is used for supplying the flue gas to the absorption device;
a second pipeline connecting the lean absorbent outlet and the lean absorbent inlet, wherein a first circulation power mechanism and a liquid side of a reboiler are arranged in the second pipeline, and a gas side of the reboiler is connected to the heat medium inlet;
the third pipeline is provided with a second circulating power mechanism and comprises a first branch and a second branch, and the first branch is connected with the rich absorbent outlet and the first rich absorbent inlet; the second branch is connected with the rich absorbent outlet and the second rich absorbent inlet;
the two sides of the first heat exchanger are respectively arranged in the second branch and the second pipeline; and
a gas side of the gas-liquid heat exchanger is disposed in the first conduit and a liquid side is disposed in the second branch.
14. The desorption of CO in flue gas of claim 132The system according to (1), characterized in that said third pipeline further comprises a third branch, said absorption unit further comprises a third rich absorbent inlet, said third branch connecting said third rich absorbent inlet and said rich absorbent outlet.
15. A ship comprising a desorption flue gas CO according to any one of claims 1 to 142The system of (1).
CN202111283923.9A 2021-11-01 2021-11-01 Desorption of CO from flue gas2System and ship Pending CN113842752A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111283923.9A CN113842752A (en) 2021-11-01 2021-11-01 Desorption of CO from flue gas2System and ship

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111283923.9A CN113842752A (en) 2021-11-01 2021-11-01 Desorption of CO from flue gas2System and ship

Publications (1)

Publication Number Publication Date
CN113842752A true CN113842752A (en) 2021-12-28

Family

ID=78983841

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111283923.9A Pending CN113842752A (en) 2021-11-01 2021-11-01 Desorption of CO from flue gas2System and ship

Country Status (1)

Country Link
CN (1) CN113842752A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115475488A (en) * 2022-09-22 2022-12-16 上海船舶研究设计院 Carbon dioxide treatment system for ship, treatment method thereof and ship

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100062926A1 (en) * 2006-11-24 2010-03-11 Simon Woodhouse Absorbent regeneration with flashed lean solution and heat integration
CN103977683A (en) * 2014-04-30 2014-08-13 天津大学 Method and device for reducing regeneration energy consumption of decarburization absorption liquid
CN108744893A (en) * 2018-07-12 2018-11-06 华中农业大学 CO based on heat pipe intensified recuperation of heat2Chemical absorbing System and method for
CN112387071A (en) * 2019-08-16 2021-02-23 国家能源投资集团有限责任公司 CO2Trapping method and apparatus
CN113230832A (en) * 2021-05-27 2021-08-10 浙江浙能技术研究院有限公司 CO with low volatile organic pollutant emission2Trapping system and method
CN113332831A (en) * 2021-05-06 2021-09-03 中太海事技术(上海)有限公司 Ship tail gas dedusting, desulfurizing and decarbonizing integrated device and ship
CN216092974U (en) * 2021-11-01 2022-03-22 中国船舶重工集团公司第七一一研究所 Desorption of CO from flue gas2System and ship

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100062926A1 (en) * 2006-11-24 2010-03-11 Simon Woodhouse Absorbent regeneration with flashed lean solution and heat integration
CN103977683A (en) * 2014-04-30 2014-08-13 天津大学 Method and device for reducing regeneration energy consumption of decarburization absorption liquid
CN108744893A (en) * 2018-07-12 2018-11-06 华中农业大学 CO based on heat pipe intensified recuperation of heat2Chemical absorbing System and method for
CN112387071A (en) * 2019-08-16 2021-02-23 国家能源投资集团有限责任公司 CO2Trapping method and apparatus
CN113332831A (en) * 2021-05-06 2021-09-03 中太海事技术(上海)有限公司 Ship tail gas dedusting, desulfurizing and decarbonizing integrated device and ship
CN113230832A (en) * 2021-05-27 2021-08-10 浙江浙能技术研究院有限公司 CO with low volatile organic pollutant emission2Trapping system and method
CN216092974U (en) * 2021-11-01 2022-03-22 中国船舶重工集团公司第七一一研究所 Desorption of CO from flue gas2System and ship

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115475488A (en) * 2022-09-22 2022-12-16 上海船舶研究设计院 Carbon dioxide treatment system for ship, treatment method thereof and ship

Similar Documents

Publication Publication Date Title
CN103303920B (en) Carbon dioxide recovering apparatus and process for carbon dioxide recovery
CN108187455B (en) Flue gas carbon dioxide capture system based on two-phase absorbent
KR20120098929A (en) Water wash method and system for a carbon dioxide capture process
CN103561848A (en) Combustion exhaust gas treatment system and combustion exhaust gas treatment method
CN212166984U (en) CO2Trapping system
JP2008307520A (en) Co2 or h2s removal system, co2 or h2s removal method
CN103189124B (en) System and method for recovering gas containing c02 and h2s
CN216092974U (en) Desorption of CO from flue gas2System and ship
CN104936677A (en) System and method for recovering gas containing CO2 and H2S
KR101961609B1 (en) High efficiency system and method for acidic gas absorption
CN113842752A (en) Desorption of CO from flue gas2System and ship
CN114832584A (en) CO based on two-phase absorbent rich liquid concentrated phase desorption 2 Trapping system and method
CN114191942A (en) Flue gas CO2Hypergravity regeneration energy-saving process for trapping system
JP5591083B2 (en) CO2 recovery system
KR20120007417A (en) Apparatus for separating acid gas from mixed gas
CN216799295U (en) Trapping device of post-combustion CO2
KR20170114802A (en) Apparatus and method for carbon dioxide capturing by reusing the stripper`s overhead vapor thermal energy
CN217092863U (en) Ammonia process decarbonization tower and desulfurization decarbonization device
KR102533169B1 (en) Carbon dioxide capture device with improved energy efficiency
CN217795387U (en) Low-energy-consumption carbon trapping device
CN116878286B (en) System and method for enriching and utilizing carbon dioxide in tail gas of pure oxygen combustion kiln
CN218077173U (en) Coke oven flue gas carbon dioxide capture system
CN220418200U (en) Carbon dioxide capturing and recycling modularized device for ground oil-gas engineering
CN220558898U (en) Heat pipe energy-saving ionic solution carbon trapping device
CN217431317U (en) Low-energy consumption device for flue gas CO2 trapping process

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
RJ01 Rejection of invention patent application after publication

Application publication date: 20211228

RJ01 Rejection of invention patent application after publication