CN116510466A - Flue gas carbon capture system and method - Google Patents
Flue gas carbon capture system and method Download PDFInfo
- Publication number
- CN116510466A CN116510466A CN202310449482.8A CN202310449482A CN116510466A CN 116510466 A CN116510466 A CN 116510466A CN 202310449482 A CN202310449482 A CN 202310449482A CN 116510466 A CN116510466 A CN 116510466A
- Authority
- CN
- China
- Prior art keywords
- lean
- rich liquid
- flue gas
- liquid
- outlet
- 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
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 239000003546 flue gas Substances 0.000 title claims abstract description 70
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 213
- 230000008929 regeneration Effects 0.000 claims abstract description 94
- 238000011069 regeneration method Methods 0.000 claims abstract description 94
- 238000010521 absorption reaction Methods 0.000 claims abstract description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000011084 recovery Methods 0.000 claims abstract description 15
- 238000005406 washing Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 44
- 230000002209 hydrophobic effect Effects 0.000 claims description 18
- 238000003795 desorption Methods 0.000 claims description 16
- 238000009792 diffusion process Methods 0.000 claims description 15
- 239000006096 absorbing agent Substances 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 28
- 239000001569 carbon dioxide Substances 0.000 abstract description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000012535 impurity Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- -1 alcohol amine Chemical class 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to the field of carbon capture, and discloses a flue gas carbon capture system and a flue gas carbon capture method. The system comprises a carbon capture unit and a condensate recovery unit; the carbon capture unit comprises a water washing tower, an absorption tower, a lean/rich liquid heat exchanger, a regeneration tower and a reboiler; a flue gas outlet arranged on the water washing tower is connected with the absorption tower; the absorption tower is provided with a first rich liquid outlet which is connected with the lean/rich liquid heat exchanger, and a second rich liquid outlet which is connected with the regeneration tower; the lean/rich liquid heat exchanger is provided with a first outlet connected with the regeneration tower, and a second outlet connected with the absorption tower; the regeneration tower is provided with a first lean solution outlet which is connected with the lean/rich solution heat exchanger, and a second lean solution outlet which is connected with the reboiler; the condensed water recovery unit comprises a drainage expander and an economizer; and conveying the steam subjected to heat exchange in the reboiler to a drainage expander for treatment, and conveying the obtained water to an economizer for utilization. The system has high absorption rate for carbon dioxide and can save energy consumption of the system.
Description
Technical Field
The invention relates to the field of carbon capture, in particular to a flue gas carbon capture system and method.
Background
At present, the combustion of a large amount of fossil fuels such as coal, natural gas and the like leads to a large amount of CO 2 The emission of gas brings serious greenhouse effect, brings wide attention to all human beings, and realizes CO 2 CO reduction by gas capture 2 The discharge of gas is extremely important.
At present, the commonly used carbon trapping technology is a carbon trapping technology by a chemical absorption method, wherein the carbon trapping technology by the chemical absorption method utilizes alcohol amine absorption liquid to absorb CO in flue gas 2 The technology for realizing carbon trapping is the only technology capable of realizing carbon trapping on the scale of hundreds of thousands of tons and above at present. However, the existing carbon trapping system has the problems of low treatment efficiency of flue gas, unsatisfactory carbon trapping effect and the like, and a large amount of steam is needed to be used for absorbing CO in the carbon trapping technology of the chemical absorption method 2 The obtained rich liquid is heated to realize the regeneration of the absorption liquid, but at present, the part of steam is usually directly discharged as waste water or waste gas after being utilized, and water resource waste exists to a great extent.
Disclosure of Invention
The invention aims to solve the problem of serious water resource waste in the carbon trapping process in the prior art, and provides a flue gas carbon trapping system and a flue gas carbon trapping method.
In order to achieve the above object, an aspect of the present invention provides the flue gas carbon capture system, which includes a carbon capture unit and a condensate recovery unit;
the carbon capture unit comprises a water washing tower, an absorption tower, a lean/rich liquid heat exchanger, a regeneration tower and a reboiler;
the water scrubber is provided with a flue gas inlet and a flue gas outlet to be treated, and the flue gas outlet is connected with a gas inlet of the absorber;
the absorption tower is provided with a rich liquid outlet which is respectively connected with a rich liquid inlet of the lean/rich liquid heat exchanger and a first rich liquid inlet of the regeneration tower;
the lean/rich liquid heat exchanger is provided with a first outlet and a second outlet, the first outlet is connected with a second rich liquid inlet of the regeneration tower, and the second outlet is connected with a liquid inlet of the absorption tower;
the bottom of the regeneration tower is provided with a first lean solution outlet and a second lean solution outlet, the first lean solution outlet is connected with a lean solution inlet of the lean/rich solution heat exchanger, and the second lean solution outlet is connected with the reboiler;
part of lean liquid from the regeneration tower is conveyed to the reboiler to exchange heat with high-temperature steam, and the lean liquid returns to the regeneration tower after heat exchange;
the condensed water recovery unit comprises a drainage expander and an economizer;
and conveying the steam subjected to heat exchange in the reboiler to the drainage expander for treatment, and conveying the obtained water to the economizer for utilization.
Preferably, the condensate recovery unit further comprises a cooler for condensing the steam obtained by the drain flash tank.
Preferably, the temperature of the high temperature steam is 110-180 ℃.
Preferably, the carbon capture unit further includes a rich liquid transfer pump for transferring the rich liquid obtained in the absorption tower to the lean/rich liquid heat exchanger and the regeneration tower, respectively.
Preferably, a lean/rich liquid transfer pump is further provided between the lean/rich liquid heat exchanger and the regeneration tower, for transferring lean liquid from the regeneration tower into the lean/rich liquid heat exchanger.
Preferably, a gas outlet is arranged at the top of the absorption tower and is used for discharging the gas after the absorption treatment.
Preferably, the condensed water recovery unit further includes a solution transfer pump for transferring the water obtained in the hydrophobic diffusion tank.
In a second aspect, the present invention provides a method for capturing carbon in flue gas, the method being implemented in the flue gas carbon capturing system, the method comprising:
delivering the flue gas to be treated into the water washing tower for treatment, delivering the treated flue gas into the absorption tower for mixed contact with the absorption liquid to obtain a rich liquid, delivering part of the rich liquid into the regeneration tower for desorption regeneration to obtain a lean liquid, delivering part of the lean liquid into the reboiler for heat exchange with high-temperature steam, and returning the heat exchange to the regeneration tower; the other part of lean liquid is conveyed to the lean/rich liquid heat exchanger to exchange heat with the other part of rich liquid from the absorption tower, and the lean liquid after heat exchange is conveyed to the absorption tower for reuse;
and conveying the steam subjected to heat exchange in the reboiler to the drainage expander for treatment, and conveying the obtained water to the economizer for utilization after the water is tested by the conductivity meter.
Preferably, the conductivity of the water fed to the economizer is less than or equal to 0.15 μS/cm.
The carbon trapping system can absorb carbon dioxide in the flue gas, reduce the emission of the carbon dioxide, has high carbon trapping efficiency, can recycle the steam after heat exchange with lean liquid in the reboiler, conveys the heat exchanged steam to the drainage expander for treatment to obtain water and gas phase, and conveys the obtained water to the economizer for recycling, thereby improving the water inlet temperature in the economizer, recycling the heat of the steam after heat exchange, realizing the purpose of recycling the steam condensate in the carbon trapping process, and further saving water resources and energy consumption.
Drawings
FIG. 1 is a process flow diagram of a flue gas carbon capture system according to the present invention.
Description of the reference numerals
11 a water washing tower; 12 an absorption tower;
13 lean/rich heat exchanger; 14 a regeneration tower;
15 reboiler; a 21 hydrophobic diffusion vessel;
22 conductivity meter; 23 economizers;
24 coolers.
Detailed Description
The following describes specific embodiments of the present invention in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In the description of the present application, the terms "first", "second" are used for descriptive purposes only and are not to be construed as indicating relative importance or implicitly indicating the number of technical features indicated. Thus, unless otherwise indicated, features defining "first", "second" may include one or more such features either explicitly or implicitly; the meaning of "plurality" is two or more. The terms "comprises," "comprising," and any variations thereof, are intended to cover a non-exclusive inclusion, such that one or more other features, integers, steps, operations, elements, components, and/or groups thereof may be present or added.
In addition, terms of orientation or positional relationship indicated by "upper", "lower", "inner", "outer", etc., are described based on the orientation or relative positional relationship shown in the drawings, and are merely for convenience of description of the present application, and do not indicate that the apparatus or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present application.
Furthermore, unless explicitly specified and limited otherwise, the terms "connected," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; either directly or indirectly through intermediaries, or in communication with each other. The specific meaning of the terms in this application will be understood by those of ordinary skill in the art as the case may be.
Here, the rich liquid is a liquid obtained by absorbing carbon dioxide in the flue gas by the absorbing liquid in the absorbing tower 12, and the lean liquid is a liquid obtained by transferring the rich liquid to the regenerating tower 14 and desorbing the rich liquid by heating.
Referring to fig. 1 in combination, the flue gas carbon capture system provided by the invention comprises a carbon capture unit and a condensate recovery unit;
the carbon capture unit includes a water wash column 11, an absorber column 12, a lean/rich heat exchanger 13, a regenerator column 14, and a reboiler 15.
In the system of the present invention, the water scrubber 11 is used for removing dust, NOx, SOx and other impurities in the flue gas to be treated, and the treated flue gas is sent to the absorber 12 for treatment.
In a specific embodiment, the water washing tower 11 uses water washing liquid to remove impurities in the flue gas to be treated, and the water washing liquid can be water or sodium hydroxide water solution.
In the system of the invention, the water scrubber 11 is provided with a flue gas inlet to be treated and a flue gas outlet, the flue gas inlet to be treated is used for inputting flue gas to be treated, the flue gas outlet is used for conveying the flue gas after impurity removal, and the flue gas outlet is connected with the gas inlet of the absorber 12; the flue gas to be treated is subjected to impurity removal and then is conveyed to the absorption tower 12.
In the system of the present invention, the absorption tower 12 is used for absorbing carbon dioxide in the flue gas after impurity removal, so as to realize the capturing process of carbon dioxide in the flue gas, and the absorbed gas can be directly discharged to the atmosphere.
In a specific embodiment, a gas outlet is disposed at the top of the absorption tower 12, and is used for discharging the gas after the absorption treatment, where the absorption treatment refers to the gas obtained by using an absorbent to absorb the carbon dioxide in the gas.
In a specific embodiment, the absorption tower 12 absorbs the carbon dioxide gas in the flue gas by using an absorption liquid, and a rich liquid is obtained after the treatment is completed. The absorption liquid may be an absorption liquid commonly used in the art for absorbing carbon dioxide gas, and may be an alcohol amine absorption liquid, for example.
In the system of the present invention, a rich liquid outlet is provided on the absorption tower 12, and the rich liquid outlet is connected to a rich liquid inlet of the lean/rich liquid heat exchanger 13 and a first rich liquid inlet of the regeneration tower 14, respectively; specifically, the rich liquid obtained in the absorption tower 12 is output through the rich liquid outlet and then divided into two branches, one branch is sent to the lean/rich liquid heat exchanger 13 for heat exchange, and the other branch is sent to the regeneration tower 14 for desorption regeneration.
In a specific embodiment, the rich liquid outlet is provided at the bottom of the absorption column 12.
In a specific embodiment, a rich liquid delivery pump is disposed at a rich liquid outlet of the absorption tower 12, and is used for delivering the rich liquid obtained in the absorption tower 12 to the lean/rich liquid heat exchanger 13 for heat exchange and the regeneration tower 14 for desorption regeneration.
In a specific embodiment, the rich liquid transfer pump may be a solution transfer pump common in the art, such as a centrifugal pump.
In a specific embodiment, the carbon capture unit further includes an inter-stage cooler for cooling the rich liquid obtained in the absorption tower 12, so as to ensure stable operation of the absorption tower 12. The refrigerant of the inter-stage cooler may be a medium commonly used in the art for heat exchange with a solution, for example, cooling water.
In the system of the present invention, the regeneration tower 14 is used for heating, desorbing and regenerating the rich liquid, and the regenerated absorption liquid can be returned to the absorption tower 12 for reuse.
In a specific embodiment, the desorption mode of the rich liquid in the regeneration tower 14 is thermal desorption, that is, the rich liquid sent into the regeneration tower 14 is heated, so that the absorbed liquid is desorbed to obtain lean liquid, and the regeneration of the absorption liquid is realized.
In the system of the present invention, the regeneration tower 14 is provided with a first lean solution outlet and a second lean solution outlet, the first lean solution outlet is connected with a lean solution inlet of the lean/rich solution heat exchanger 13, and the second lean solution outlet is connected with the reboiler 15; specifically, a part of the lean liquid obtained in the regeneration tower 14 is sent to the lean/rich liquid heat exchanger 13 through the first lean liquid outlet, and the other part of the lean liquid is sent to the reboiler 15 through the second lean liquid outlet to exchange heat with the high-temperature steam in the reboiler 15, so that the lean liquid is gasified into lean liquid steam through heat exchange, and then the lean liquid steam is sent to the regeneration tower 14 to supply energy for desorption regeneration of the rich liquid.
In a specific embodiment, the lean liquid steam sent to the regeneration tower 14 is subjected to mixed heat exchange with the rich liquid, then condensed into lean liquid, a part of lean liquid steam is sent to the lean/rich liquid heat exchanger 13 to exchange heat with the rich liquid, and a part of lean liquid steam is sent to the reboiler 15 to exchange heat with high-temperature steam to become lean liquid steam, and the lean liquid steam is returned to the regeneration tower 14.
In a more specific embodiment, the first lean liquid outlet and the second lean liquid outlet are disposed in parallel at the bottom of the regeneration tower 14.
In a specific embodiment, the top of the regeneration column 14A regeneration gas outlet is arranged at the position for discharging the regeneration gas obtained by desorption regeneration of the rich liquid, and the main component of the regeneration gas is CO 2 . How much form the use of the regeneration gas exists, for example, the regeneration gas can be used for the preparation of chemicals and the like.
In the system according to the present invention, the lean/rich liquid heat exchanger 13 is used to exchange heat the lean liquid obtained in the regeneration tower 14 with the rich liquid obtained in the absorption tower 12. Because the temperature of the lean solution obtained by thermal desorption regeneration in the regeneration tower 14 is higher, the obtained lean solution can be conveyed into the lean/rich solution heat exchanger 13 to heat the rich solution, the heat of the lean solution is recovered, the recycling of heat energy is realized, and the heat energy of the flue gas carbon capture system disclosed by the invention is saved.
In a specific embodiment, the lean/rich liquid heat exchanger 13 is a shell-and-tube heat exchanger, and is composed of a shell and a heat exchange tube bundle arranged in the shell. The inner area of the heat exchange tube bundle is a tube side, and the outer area of the heat exchange tube bundle is a shell side. In the present invention, the types of the medium transported in the tube side and the shell side are not limited, that is, lean liquid or rich liquid may be transported in the tube side, and when lean liquid is transported in the tube side, rich liquid is transported in the tube side; and when the rich liquid is conveyed in the tube pass, the lean liquid is conveyed in the tube pass.
In the system of the present invention, the lean/rich heat exchanger 13 is provided with a first outlet connected to the second rich liquid inlet of the regeneration tower 14 and a second outlet connected to the liquid inlet of the absorption tower 12.
In a specific embodiment, part of the rich liquid from the absorption tower 12 is conveyed to the tube side of the lean/rich liquid heat exchanger 13 through the rich liquid inlet of the lean/rich liquid heat exchanger 13, part of the lean liquid from the regeneration tower 14 is conveyed to the shell side of the lean/rich liquid heat exchanger 13 through the lean liquid inlet of the lean/rich liquid heat exchanger 13, the lean liquid and the rich liquid exchange heat in the lean/rich liquid heat exchanger 13, the rich liquid after heat exchange and temperature increase is conveyed to the regeneration tower 14 for regeneration, and the lean liquid after heat exchange and temperature reduction is conveyed to the absorption tower 12 for absorbing carbon dioxide in the flue gas.
In the system of the present invention, a lean/rich liquid transfer pump is further disposed between the lean/rich liquid heat exchanger 13 and the regeneration tower 14, and is configured to transfer part of the lean liquid from the regeneration tower 14 to the lean/rich liquid heat exchanger 13 to exchange heat with part of the rich liquid from the absorption tower 12.
In a specific embodiment, the lean solution transfer pump may be a solution transfer pump common in the art, such as a centrifugal pump.
In the system of the present invention, the reboiler 15 is used to heat the lean liquid from the regeneration tower 14 into lean liquid steam, and then to convey the lean liquid steam into the regeneration tower 14 to supply energy for desorption regeneration of the rich liquid. The reboiler 15 is internally provided with a shell-and-tube heat exchange structure, high-temperature steam is conveyed in the tube side, and lean liquid is conveyed in the shell side. Specifically, a part of the lean liquid from the regeneration tower 14 in the shell side is heated to lean liquid steam after heat exchange with the high temperature steam in the tube side, and then the lean liquid steam is sent to the regeneration tower 14.
In the system of the present invention, the reboiler 15 is provided with a lean solution steam outlet, the lean solution steam outlet is communicated with a lean solution steam inlet provided on the regeneration tower 14, and the lean solution steam delivered into the regeneration tower 14 can supply energy for desorption and regeneration of the rich solution in the regeneration tower 14.
In a specific embodiment, the high temperature steam in the reboiler 15 has a temperature of 110-180 ℃, and may be from a turbine set in a generator set.
In the system according to the invention, the condensate recovery unit comprises a connected hydrophobic diffuser 21 and an economizer 23.
In a specific embodiment, the steam after heat exchange in the reboiler 15 is sent to the hydrophobic diffusion tank 21 for treatment, and the obtained water is sent to the economizer 23 for use.
In the system of the present invention, the hydrophobic diffusion vessel 21 is used for treating the steam heat-exchanged in the reboiler 15 to obtain water and gas phase. The structure of the hydrophobic diffusion vessel 21 is a hydrophobic diffusion vessel common in the art, and only water and gas phase are required to be separated. In a specific embodiment, the gas phase is water vapor.
In the system of the invention, the steam after heat exchange in the reboiler 15 is conveyed into the drainage expander 21, so that the steam can be recovered without reducing the temperature of the steam, and the recovered water can be conveyed into the economizer 23 for increasing the water inlet temperature of the economizer 23, thereby saving the energy consumption of the economizer 23.
In the system of the present invention, the condensate recovery unit further comprises a conductivity meter 22, the conductivity meter 22 being arranged between the hydrophobic diffuser 21 and the economizer 23 for detecting water fed into the economizer 23.
In a specific embodiment, before the water obtained in the drainage expander 21 is conveyed to the economizer 23, the conductivity of the water needs to be tested by adopting the conductivity meter 22, so as to judge the quality of the water body, and avoid polluting the water quality in the economizer 23, thereby causing more serious water resource waste.
In a specific embodiment, the condensate recovery unit further includes a cooler 24, where the cooler 24 is configured to condense the steam obtained by the drain flash tank 21, and the liquid obtained after condensation may enter a water circulation system of the generator set for use, so as to further realize reuse of water resources. More specifically, the liquid obtained in the cooler 24 may be transported to the deaerator for use.
In the system of the present invention, a solution transfer pump is disposed between the hydrophobic diffusion vessel 21 and the conductivity meter 22, and the water obtained by the hydrophobic diffusion vessel 21 is transferred to the conductivity meter 22 for detection and then transferred to the economizer 23 for use by the solution transfer pump. The solution delivery pump may be a pump for delivering a liquid as is common in the art.
In the system according to the invention, the hydrophobic diffusion vessel 21 is provided with a liquid outlet connected to the solution delivery pump and a gas outlet connected to the cooler 24; the solution delivery pump, the conductivity meter 22 and the economizer 23 are in communication in sequence.
The operation mode of the system of the invention is as follows: the flue gas to be treated is conveyed to the water scrubber 11 to remove impurities such as dust, SOx, NOx and the like, after the treatment is finished, the flue gas is conveyed to the absorber 12 to be mixed with absorption liquid for carbon capture, the gas after the absorption is finished is discharged from a gas outlet at the top of the absorber 12, and a part of rich liquid obtained after absorption in the absorber 12 is conveyed to the regenerator 14 to be desorbed and regenerated to obtain lean liquid;
a part of the lean liquid obtained in the regeneration tower 14 is conveyed to the reboiler 15 to be converted into lean liquid steam through heat exchange with high-temperature steam, the lean liquid is returned to the regeneration tower 14 to be mixed and heat exchanged with rich liquid, and the rest of the lean liquid is conveyed to the lean/rich liquid heat exchanger 13 to be heat exchanged with the rich liquid from the rest of the absorption tower 12; the rich liquid after heat exchange is conveyed to the regeneration tower 14 for desorption regeneration, and the lean liquid after heat exchange is conveyed to the absorption tower 12 for absorbing carbon dioxide in the flue gas;
the regenerated gas obtained by desorption and regeneration of the rich liquid in the regeneration tower 14 is discharged from a regenerated gas outlet at the top of the regeneration tower 14;
and the steam subjected to heat exchange in the reboiler 15 is conveyed to the drainage expander 21 for treatment to obtain water and gas phase, the conductivity of the obtained water is tested by adopting the conductivity meter 22 and then conveyed to the economizer 23 for use, and the obtained gas phase is conveyed to the cooler 24 for cooling and then conveyed to the deaerator.
The invention further provides a method for capturing carbon in flue gas, which is implemented in the system for capturing carbon in flue gas, and comprises the following steps:
delivering the flue gas to be treated into the water washing tower 11 for treatment, delivering the treated flue gas into the absorption tower 12 for mixed contact with absorption liquid to obtain rich liquid, delivering part of the rich liquid into the regeneration tower 14 for desorption regeneration to obtain lean liquid, delivering part of the lean liquid into the reboiler 15 for heat exchange with high-temperature steam, and returning the heat exchange to the regeneration tower 14; the other part of lean liquid is conveyed to the lean/rich liquid heat exchanger 13 to exchange heat with the other part of rich liquid from the absorption tower 12, and the lean liquid after heat exchange is conveyed to the absorption tower 12 for reuse;
and the steam subjected to heat exchange in the reboiler 15 is conveyed to the drainage expander 21 for treatment, and the obtained water is conveyed to the economizer 23 for utilization after being tested by the conductivity meter 22.
In a preferred embodiment, the conductivity of the water fed to the economizer 23 is controlled to be less than or equal to 0.15. Mu.S/cm, preferably 0.05 to 0.1. Mu.S/cm, in order to ensure that the water fed to the economizer 23 does not adversely affect the original water quality in the generator set.
The present invention will be described in detail by way of examples, but the scope of the present invention is not limited thereto.
The following embodiments are implemented with a flue gas carbon capture system including a carbon capture unit and a condensate recovery unit, referring in conjunction to FIG. 1;
the carbon capture unit comprises a water washing tower 11, an absorption tower 12, a lean/rich liquid heat exchanger 13, a regeneration tower 14, a reboiler 15, a rich liquid delivery pump and a lean liquid delivery pump;
the water scrubber 11 is provided with a flue gas inlet and a flue gas outlet to be treated, and the flue gas outlet is connected with a gas inlet of the absorber 12;
the absorption tower 12 is provided with a rich liquid outlet which is respectively connected with a rich liquid inlet of the lean/rich liquid heat exchanger 13 and a first rich liquid inlet of the regeneration tower 14;
the lean/rich liquid heat exchanger 13 is provided with a first outlet and a second outlet, the first outlet is connected with a second rich liquid inlet of the regeneration tower 14, and the second outlet is connected with a liquid inlet of the absorption tower 12;
the regeneration tower 14 is provided with a first lean solution outlet and a second lean solution outlet, the first lean solution outlet is connected with a lean solution inlet of the lean/rich solution heat exchanger 13, and the second lean solution outlet is connected with the reboiler 15;
a lean solution steam outlet is arranged on the reboiler 15 and is communicated with a lean solution steam inlet arranged on the regeneration tower 14;
a rich liquid delivery pump is arranged at the rich liquid outlet;
the lean liquid transfer pump is located between the lean/rich liquid heat exchanger 13 and the regeneration tower 14;
the condensed water recovery unit comprises a hydrophobic diffusion vessel 21, a conductivity meter 22, an economizer 23, a cooler 24 and a solution delivery pump;
the drainage expander 21 is provided with a liquid outlet and a gas outlet, the liquid outlet is connected with the solution delivery pump, and the gas outlet is connected with the cooler 24; the solution delivery pump, the conductivity meter 22 and the economizer 23 are connected in sequence.
Example 1
The flue gas to be treated is conveyed to the water scrubber 11 to remove impurities such as dust, SOx, NOx and the like, after the treatment is finished, the flue gas is conveyed to the absorber 12 to be mixed with absorption liquid for carbon capture, the gas after the absorption is finished is discharged from a gas outlet at the top of the absorber 12, and a part of rich liquid obtained after absorption in the absorber 12 is conveyed to the regenerator 14 to be desorbed and regenerated to obtain lean liquid;
a part of the lean liquid obtained in the regeneration tower 14 is conveyed to the reboiler 15 to exchange heat with high-temperature steam (temperature 130 ℃) to be changed into lean liquid steam, the lean liquid steam is returned to the regeneration tower 14 to exchange heat with rich liquid in a mixing way, and the rest lean liquid is conveyed to the lean/rich liquid heat exchanger 13 to exchange heat with the rich liquid from the rest in the absorption tower 12; the rich liquid after heat exchange is conveyed to the regeneration tower 14 for desorption regeneration, and the lean liquid after heat exchange is conveyed to the absorption tower 12 for absorbing carbon dioxide in the flue gas;
the regenerated gas obtained by desorption and regeneration of the rich liquid in the regeneration tower 14 is discharged from a regenerated gas outlet at the top of the regeneration tower 14;
and the steam subjected to heat exchange in the reboiler 15 is conveyed to the hydrophobic diffusion vessel 21 for treatment to obtain water and gas phase, the conductivity of the obtained water is tested to be 0.1 mu S/cm by adopting the conductivity meter 22 and then conveyed to the economizer 23 for use, and the obtained gas phase is conveyed to the cooler 24 for cooling and then conveyed to the deaerator.
The system can quickly absorb carbon dioxide in the flue gas and reduce the emission of the carbon dioxide, and can recycle the steam used for heating the lean solution in the reboiler, thereby saving the water resource of the flue gas carbon capture system and reducing the energy consumption of the system.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (10)
1. The flue gas carbon capture system is characterized by comprising a carbon capture unit and a condensate recovery unit;
the carbon capture unit comprises a water washing tower (11), an absorption tower (12), a lean/rich liquid heat exchanger (13), a regeneration tower (14) and a reboiler (15);
the water scrubber (11) is provided with a flue gas inlet and a flue gas outlet to be treated, and the flue gas outlet is connected with a gas inlet of the absorber (12);
a rich liquid outlet is arranged on the absorption tower (12), and the rich liquid outlet is respectively connected with a rich liquid inlet of the lean/rich liquid heat exchanger (13) and a first rich liquid inlet of the regeneration tower (14);
the lean/rich liquid heat exchanger (13) is provided with a first outlet and a second outlet, the first outlet is connected with a second rich liquid inlet of the regeneration tower (14), and the second outlet is connected with a liquid inlet of the absorption tower (12);
a first lean solution outlet and a second lean solution outlet are arranged on the regeneration tower (14), the first lean solution outlet is connected with a lean solution inlet of the lean/rich solution heat exchanger (13), and the second lean solution outlet is connected with the reboiler (15);
part of lean liquid from the regeneration tower (14) is conveyed to the reboiler (15) to exchange heat with high-temperature steam, and the lean liquid returns to the regeneration tower (14) after heat exchange;
the condensed water recovery unit comprises a hydrophobic diffusion tank (21) and an economizer (23);
and conveying the steam subjected to heat exchange in the reboiler (15) to the drainage expander (21) for treatment to obtain gas phase and water, and conveying the obtained water to the economizer (23) for utilization.
2. The flue gas carbon capture system according to claim 1, wherein a conductivity meter (22) is arranged between the hydrophobic diffuser (21) and the economizer (23) for detecting the conductivity of water fed to the economizer (23).
3. The flue gas carbon capture system according to claim 1, wherein the condensate recovery unit further comprises a cooler (24), the cooler (24) being adapted to condense the gas phase obtained by the hydrophobic diffusion vessel (21).
4. The flue gas carbon capture system of claim 1, wherein the temperature of the high temperature steam is 110-180 ℃.
5. The flue gas carbon capturing system according to claim 1, wherein a rich liquid delivery pump is provided on a rich liquid outlet of the absorption tower (12) for delivering the rich liquid obtained in the absorption tower (12) to the lean/rich liquid heat exchanger (13) and the regeneration tower (14), respectively.
6. The flue gas carbon capturing system according to claim 1, wherein a lean/rich liquid transfer pump is further provided between the lean/rich liquid heat exchanger (13) and the regeneration tower (14) for transferring lean liquid from the regeneration tower (14) into the lean/rich liquid heat exchanger (13).
7. The flue gas carbon capture system according to claim 1, wherein a gas outlet is provided at the top of the absorption tower (12) for discharging the gas after the absorption treatment.
8. The flue gas carbon capture system according to claim 2, wherein a solution transfer pump is provided between the hydrophobic diffusion vessel (21) and the conductivity meter (22) for transferring water obtained in the hydrophobic diffusion vessel (21).
9. A method of carbon capture of flue gas, characterized in that the method is implemented in a carbon capture system of flue gas according to any one of claims 1 to 8, said method comprising:
delivering the flue gas to be treated into the water washing tower (11) for treatment, delivering the treated flue gas into the absorption tower (12) for mixed contact with the absorption liquid to obtain a rich liquid, delivering part of the rich liquid into the regeneration tower (14) for desorption regeneration to obtain a lean liquid, delivering part of the lean liquid into the reboiler (15) for heat exchange with high-temperature steam, and returning the heat exchange to the regeneration tower (14); the rest part of lean liquid is conveyed to the lean/rich liquid heat exchanger (13) to exchange heat with the rest part of rich liquid from the absorption tower (12), and the lean liquid after heat exchange is conveyed to the absorption tower (12) for reuse;
and the steam subjected to heat exchange in the reboiler (15) is conveyed to the drainage expander (21) for treatment, and the obtained water is conveyed to the economizer (23) for utilization after being tested by adopting the conductivity meter (22).
10. The method of carbon capture of flue gas according to claim 9, wherein the conductivity of water fed to the economizer (23) is less than or equal to 0.15 μs/cm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310449482.8A CN116510466A (en) | 2023-04-24 | 2023-04-24 | Flue gas carbon capture system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310449482.8A CN116510466A (en) | 2023-04-24 | 2023-04-24 | Flue gas carbon capture system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116510466A true CN116510466A (en) | 2023-08-01 |
Family
ID=87393438
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310449482.8A Pending CN116510466A (en) | 2023-04-24 | 2023-04-24 | Flue gas carbon capture system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116510466A (en) |
-
2023
- 2023-04-24 CN CN202310449482.8A patent/CN116510466A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2578290B1 (en) | CO2 recovery system and method | |
| CN110115910A (en) | A kind of energy-saving carbon dioxide capture system and method | |
| CN114768488B (en) | Coal-fired unit flue gas carbon dioxide entrapment system | |
| CN103561848A (en) | Combustion exhaust gas treatment system and combustion exhaust gas treatment method | |
| CN112387071A (en) | CO2Trapping method and apparatus | |
| CN212166984U (en) | CO2Trapping system | |
| CN101708414A (en) | System and method for desulphurizing waste gas by cyclic absorption and application thereof | |
| CN102980198B (en) | Washing condensing smoke triple recovery device | |
| CN105536484A (en) | Pollutant pretreating tower condensing based on flue gas | |
| CN219815797U (en) | Ship CO capable of being flexibly arranged 2 Trapping system | |
| MX2011009370A (en) | Flue gas treatment system and the method using amonia solution. | |
| KR20220086287A (en) | Equipment for wet type carbon dioxide capturing | |
| CN202942807U (en) | Water-washing condensing-type smoke triple-recovery device | |
| CN113374552A (en) | Device system and method for capturing carbon dioxide by amine method and utilizing energy of analytical tower | |
| CN108744932A (en) | One kind removing from industrial smoke or tail gas and recycle SO2Device and technique | |
| CN115212709A (en) | Chemical method flue gas carbon dioxide capture system and capture method thereof | |
| CN101920158B (en) | Flue gas desulfurization device utilizing ammonia water and humate solution and desulfurization method | |
| CN113101786A (en) | Flue gas carbon dioxide capture system and method based on organic solvent absorption-extraction regeneration cycle | |
| CN117205720A (en) | Process for coupling waste heat utilization of boiler tail gas with carbon dioxide capturing system | |
| JP2016112482A (en) | Carbon dioxide collection method and device | |
| CN111054187A (en) | Recovery system and gas recovery method | |
| CN217410281U (en) | Flue gas alcohol amine method decarbonization device system | |
| CN217829546U (en) | Chemical method flue gas carbon dioxide entrapment system | |
| CN215486191U (en) | Device system for capturing energy of carbon dioxide analysis tower by amine method | |
| CN116510466A (en) | Flue gas carbon capture system and method |
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 |