CN115212710A - Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas - Google Patents
Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas Download PDFInfo
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- CN115212710A CN115212710A CN202210870405.5A CN202210870405A CN115212710A CN 115212710 A CN115212710 A CN 115212710A CN 202210870405 A CN202210870405 A CN 202210870405A CN 115212710 A CN115212710 A CN 115212710A
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- flue gas
- absorption device
- rich liquid
- concentration
- pipeline
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 239000003546 flue gas Substances 0.000 title claims abstract description 50
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 23
- 238000010521 absorption reaction Methods 0.000 claims abstract description 67
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 21
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 20
- 230000002745 absorbent Effects 0.000 claims abstract description 12
- 239000002250 absorbent Substances 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 239000000945 filler Substances 0.000 claims description 6
- 230000001172 regenerating effect Effects 0.000 abstract description 3
- 239000007921 spray Substances 0.000 abstract description 3
- 150000001412 amines Chemical class 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method suitable for ultralow-concentration CO 2 The carbon capture system of flue gas, including one-level absorbing device, the second grade absorbing device, first pipeline, the second pipeline, the cooler, the flue gas gets into second grade absorption unit, the rich liquid is discharged from the bottom export after forming the rich liquid with half rich liquid countercurrent contact, the flue gas is sent into one-level absorbing device's lower part entry, contact back with the absorbent countercurrent and then discharge from the top export, half rich liquid from one-level absorbing device bottom entry exhaust gets into the cooler through the booster pump, cool down the half rich liquid that heaies up because of having absorbed carbon dioxide, half rich liquid after the cooling gets into from second grade absorbing device's upper portion entry, spray the flue gas, form the circulation. The invention is used for ultralow CO 2 The carbon capture of the flue gas with the concentration of 1-10 percent, improves the rich liquid capacity of the absorbent, and can reach over 90 percent of CO for low-concentration flue gas 2 Capture rate while ensuring CO 2 The regenerative load is lowIn 3GJ/tCO 2 。
Description
Technical Field
The invention relates to the technical field of flue gas treatment, in particular to a method for treating ultralow-concentration CO 2 A carbon capture system for flue gas.
Background
Global warming has become the most interesting world problem, CO 2 Is one of the most important greenhouse gases in the atmosphere, and the large amount of emission of the greenhouse gases poses potential threats to the production and the life of human beings. When the concentration of CO2 in the flue gas is more than 10 percent, the existing carbon capture system can meet the requirement of CO simultaneously 2 The trapping rate is more than 90 percent, and CO 2 The regenerative load is less than 3.0GJ/tCO 2 But for CO 2 The low-concentration flue gas with the concentration less than 10 percent has unsatisfactory trapping effect of the traditional carbon trapping system, and can not simultaneously ensure the rich liquid capacity and CO 2 Trapping rate, CO 2 Regeneration load and other parameters. Therefore, a method suitable for low concentration CO has been developed 2 And the carbon capture system of the flue gas promotes the carbon emission reduction process.
In the prior art, there is a low-energy-consumption carbon dioxide capturing method and system with low-concentration carbon dioxide-containing tail gas, publication No. CN111744328A, in which part of amine-rich liquid from the tower bottom of a carbon dioxide absorption tower is cooled by an amine-rich liquid cooler, and then enters the carbon dioxide absorption tower through inlets at the middle part and the upper part of the carbon dioxide absorption tower, although the amount of the amine liquid sprayed by the carbon dioxide absorption tower is increased, and the gas-liquid ratio in the carbon dioxide absorption tower is maintained, the rich liquid capacity of an absorbent still needs to be improved.
Disclosure of Invention
The invention aims to provide a catalyst suitable for ultralow-concentration CO 2 Carbon capture system for flue gas, overcoming the problems of the prior art, which can be used for ultra low CO 2 The concentration of the carbon capture of the flue gas is 1-10 percent mol, and the CO capture of the flue gas with low concentration can reach more than 90 percent 2 Capture rate while ensuring CO 2 The regenerative load is lower than 3GJ/tCO 2 。
In order to realize the purpose, the invention adopts the technical scheme that: provides a catalyst suitable for ultra-low concentration CO 2 The carbon capture system of the flue gas is characterized by comprising an absorption device, wherein the upper part of the primary absorption device is provided with an absorbent inlet, the top of the primary absorption device is provided with a flue gas outlet,the absorbent is used for absorbing carbon dioxide in the flue gas to generate semi-rich liquid;
the lower part of the secondary absorption device is provided with a flue gas inlet, and the top outlet of the secondary absorption device is connected with the lower inlet of the primary absorption device and used for absorbing carbon dioxide in flue gas by semi-rich liquid to generate rich liquid;
one end of the first pipeline is connected with a bottom outlet of the primary absorption device, and the other end of the first pipeline is connected with an upper inlet of the secondary absorption device;
one end of the second pipeline is connected with the bottom outlet of the secondary absorption device;
and the cooler is arranged on the first pipeline and is used for cooling the semi-rich liquid.
The system also comprises a booster pump and a rich liquid pump, wherein the booster pump is arranged on the first pipeline and between the primary absorption device and the cooler, and the rich liquid pump is arranged on the second pipeline.
The ultra-low concentration of CO 2 The carbon dioxide concentration in the flue gas is 1-10 mol%.
The bottom outlet of the first-stage absorption device is connected with the inlet of the booster pump, the outlet of the booster pump is connected with the inlet of the cooler, and the outlet of the cooler is connected with the inlet at the upper part of the second-stage absorption device.
The first-stage absorption device and the second-stage absorption device are packed towers.
The height of the filler in the first-stage absorption device is 2-8D 1.
And the height of the filler in the secondary absorption device is 2-8D 2.
The diameter of the first-stage absorption device is 0.8-1.2 times of that of the second-stage absorption device.
The height of the first-stage absorption device is 0.2-5 times of that of the second-stage absorption device.
The invention provides a method suitable for ultralow-concentration CO 2 The carbon capture system of flue gas has the beneficial effects that:
for ultra-low CO 2 Carbon capture of flue gas at a concentration of 1% to 10% by mol to improve absorptionThe capacity of the agent rich liquid can reach over 90 percent of CO for low-concentration flue gas 2 Capture rate while ensuring CO 2 The regeneration load is lower than 3GJ/tCO 2 。
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the prior art descriptions will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic view of a carbon capture system of the present invention.
The reference numbers in the figures are as follows: 1. a primary absorption device; 2. a secondary absorption device; 3. a cooler; 4. a booster pump; 5. a rich liquid pump; 6. a first pipeline; 7. a second pipeline.
Detailed Description
In the description of the present invention, it is to be understood that the terms indicating an orientation or positional relationship are based on the orientation or positional relationship shown in the drawings only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device 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 invention.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or may be connected through the use of two elements or the interaction of two elements. The specific meanings of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or the orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only used for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements 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 invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another, and are not to be construed as indicating or implying relative importance.
Referring to FIG. 1, the present invention provides a method for ultra-low CO concentration 2 A carbon capture system for flue gas is illustrated. The system comprises a primary absorption device 1, a secondary absorption device 2, a first pipeline 6, a second pipeline 7 and a cooler 3;
the upper part of the primary absorption device 1 is provided with an absorbent inlet, and the top part of the primary absorption device is provided with a flue gas outlet for absorbing carbon dioxide in flue gas by the absorbent to generate semi-rich liquid; the lower part of the secondary absorption device 2 is provided with a flue gas inlet, and the top outlet is connected with the lower inlet of the primary absorption device 1 and is used for absorbing carbon dioxide in flue gas by semi-rich liquid to generate rich liquid; one end of the first pipeline 6 is connected with the bottom outlet of the primary absorption device 1, and the other end is connected with the upper inlet of the secondary absorption device 2; one end of the second pipeline 7 is connected with the bottom outlet of the secondary absorption device 2; a cooler 3 is provided on the first line 6 for cooling the semi-rich liquid.
The device is characterized by further comprising a booster pump 4 and a rich liquid pump 5, wherein the booster pump 4 is arranged on the first pipeline 6 and is arranged between the first-stage absorption device 1 and the cooler 3, and the rich liquid pump 5 is arranged on the second pipeline 7.
The bottom outlet of the primary absorption device 1 is connected with the inlet of a booster pump 4, the outlet of the booster pump 4 is connected with the inlet of a cooler 3, and the outlet of the cooler 3 is connected with the inlet of the upper part of the secondary absorption device 2.
The absorbent enters from an inlet at the upper part of the first-stage absorption device 1, the flue gas containing ultra-low carbon dioxide concentration enters the second-stage absorption device 2 from a flue gas inlet of the second-stage absorption device 2, the flue gas is in countercurrent contact with semi-rich liquid sprayed from the upper part of the second-stage absorption device 2 in the second-stage absorption device 2, and the semi-rich liquid becomes rich liquid after absorbing carbon dioxide in the flue gas and flows out from the bottom of the second-stage absorption device 2 to enter a rich liquid pump 5.
The flue gas is sent into the lower part entry of one-level absorbing device 1 from the top of second grade absorbing device 2 behind second grade absorbing device 2, and the flue gas is discharged from the export in top after the absorbent that sprays down with the upper portion of one-level absorbing device 1 is in the one-level absorbing device 1 adverse current contact, becomes half rich liquid behind the carbon dioxide in the absorbent absorption flue gas and discharges from the entry of one-level absorbing device 1 bottom.
The semi-rich liquid discharged from the bottom inlet of the primary absorption device 1 enters the cooler 3 through the booster pump, the semi-rich liquid heated due to the absorption of carbon dioxide is cooled, and the cooled semi-rich liquid enters from the upper inlet of the secondary absorption device 2 and sprays the flue gas to form circulation.
Wherein one-level absorbing device 1 and second grade absorbing device 2 are the packed tower, and the filler height is 2 ~ 8D1 in one-level absorbing device 1, and the filler height is 2 ~ 8D2 in the second grade absorbing device 2, and 1 diameter of one-level absorbing device is 0.8 ~ 1.2 times of 2 diameters of second grade absorbing device, and 1 height of one-level absorbing device is 0.2 ~ 5 times of 2 heights of second grade absorbing device.
The above embodiments are described in further detail to solve the technical problems, technical solutions and advantages of the present invention, and it should be understood that the above embodiments are only examples of the present invention and are not intended to limit the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. Is suitable for ultralow-concentration CO 2 A carbon capture system for flue gas, comprising:
the device comprises a primary absorption device (1), wherein an absorbent inlet is formed in the upper part of the primary absorption device (1), and a flue gas outlet is formed in the top of the primary absorption device (1) and used for absorbing carbon dioxide in flue gas by using an absorbent to generate semi-rich liquid;
the lower part of the secondary absorption device (2) is provided with a flue gas inlet, and the top outlet of the secondary absorption device (2) is connected with the lower inlet of the primary absorption device (1) and is used for absorbing carbon dioxide in flue gas by semi-rich liquid to generate rich liquid;
one end of the first pipeline (6) is connected with a bottom outlet of the primary absorption device (1), and the other end of the first pipeline (6) is connected with an upper inlet of the secondary absorption device (2);
one end of the second pipeline (7) is connected with a bottom outlet of the secondary absorption device (2);
a cooler (3), the cooler (3) being arranged on the first pipeline (6) for cooling the semi-rich liquid;
the system also comprises a booster pump (4) and a rich liquid pump (5), wherein the booster pump (4) is arranged on the first pipeline (6) and is arranged between the primary absorption device (1) and the cooler (3), and the rich liquid pump (5) is arranged on the second pipeline (7);
the ultra-low concentration of CO 2 The carbon dioxide concentration in the flue gas is 1-10 mol%.
2. The method of claim 1, wherein the CO is used for ultralow concentration of CO 2 The carbon capture system of flue gas, its characterized in that, the bottom export of one-level absorbing device (1) links to each other with booster pump (4) entry, booster pump (4) export links to each other with cooler (3) entry, cooler (3) export links to each other with second grade absorbing device (2) upper portion entry.
3. The method for treating ultralow-concentration CO according to claim 1 2 The carbon capture system for the flue gas is characterized in that the primary absorption device (1) and the secondary absorption device (2) are packed towers.
4. The method of claim 3, wherein the CO concentration is very low 2 The carbon capture system of flue gas, characterized in that, the filler height is 2 ~ 8D1 in one-level absorbing device (1).
5. The method of claim 3, wherein the CO concentration is very low 2 The carbon capture system of flue gas, characterized in that, the filler height is 2-8D 2 in secondary absorption device (2).
6. The method for treating ultralow-concentration CO according to claim 1 2 The carbon capture system of the flue gas is characterized in that the diameter of the primary absorption device (1) is 0.8-1.2 times of that of the secondary absorption device (2).
7. The method of claim 1, wherein the CO is used for ultralow concentration of CO 2 The carbon capture system for the flue gas is characterized in that the height of the primary absorption device (1) is 0.2-5 times of that of the secondary absorption device (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210870405.5A CN115212710A (en) | 2022-07-22 | 2022-07-22 | Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210870405.5A CN115212710A (en) | 2022-07-22 | 2022-07-22 | Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas |
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| Publication Number | Publication Date |
|---|---|
| CN115212710A true CN115212710A (en) | 2022-10-21 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210870405.5A Pending CN115212710A (en) | 2022-07-22 | 2022-07-22 | Is suitable for ultralow-concentration CO 2 Carbon capture system of flue gas |
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| Country | Link |
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| CN (1) | CN115212710A (en) |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05146625A (en) * | 1991-11-28 | 1993-06-15 | Hitachi Ltd | Removal of acidic gas from combustion exhaust gas |
| CN1235931A (en) * | 1998-02-27 | 1999-11-24 | 味之素株式会社 | Process for recovering carbon dioxide in glutamic acid fermentation |
| CN101157462A (en) * | 2007-09-14 | 2008-04-09 | 中国成达工程公司 | Cleaning process for outer cooling shift gas alkali preparation |
| CN101229475A (en) * | 2007-10-31 | 2008-07-30 | 武汉凯迪电力环保有限公司 | Method of using ammonia process to remove carbon dioxide from generating plant smoke gas and system thereof |
| US20140338394A1 (en) * | 2013-05-20 | 2014-11-20 | Kabushiki Kaisha Toshiba | Carbon dioxide separating and capturing apparatus and method of operating same |
| CN204865483U (en) * | 2015-07-31 | 2015-12-16 | 辽宁中电投电站燃烧工程技术研究中心有限公司 | Desorption device is united to multiple pollutant of coal -fired power plant boiler flue gas |
| US20190030481A1 (en) * | 2017-07-27 | 2019-01-31 | National Tsing Hua University | System and method for capturing carbon dioxide |
| CN111201199A (en) * | 2017-08-29 | 2020-05-26 | 赛德环境公司 | Method for value-added utilization of gaseous effluent produced by alcoholic fermentation |
| CN113491927A (en) * | 2020-04-01 | 2021-10-12 | 南京工业大学 | Method and device for removing carbon dioxide through multi-section membrane absorption |
-
2022
- 2022-07-22 CN CN202210870405.5A patent/CN115212710A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05146625A (en) * | 1991-11-28 | 1993-06-15 | Hitachi Ltd | Removal of acidic gas from combustion exhaust gas |
| CN1235931A (en) * | 1998-02-27 | 1999-11-24 | 味之素株式会社 | Process for recovering carbon dioxide in glutamic acid fermentation |
| CN101157462A (en) * | 2007-09-14 | 2008-04-09 | 中国成达工程公司 | Cleaning process for outer cooling shift gas alkali preparation |
| CN101229475A (en) * | 2007-10-31 | 2008-07-30 | 武汉凯迪电力环保有限公司 | Method of using ammonia process to remove carbon dioxide from generating plant smoke gas and system thereof |
| US20140338394A1 (en) * | 2013-05-20 | 2014-11-20 | Kabushiki Kaisha Toshiba | Carbon dioxide separating and capturing apparatus and method of operating same |
| CN204865483U (en) * | 2015-07-31 | 2015-12-16 | 辽宁中电投电站燃烧工程技术研究中心有限公司 | Desorption device is united to multiple pollutant of coal -fired power plant boiler flue gas |
| US20190030481A1 (en) * | 2017-07-27 | 2019-01-31 | National Tsing Hua University | System and method for capturing carbon dioxide |
| CN111201199A (en) * | 2017-08-29 | 2020-05-26 | 赛德环境公司 | Method for value-added utilization of gaseous effluent produced by alcoholic fermentation |
| CN113491927A (en) * | 2020-04-01 | 2021-10-12 | 南京工业大学 | Method and device for removing carbon dioxide through multi-section membrane absorption |
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Application publication date: 20221021 |