CN113457381A - Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas - Google Patents
Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas Download PDFInfo
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- CN113457381A CN113457381A CN202110740127.7A CN202110740127A CN113457381A CN 113457381 A CN113457381 A CN 113457381A CN 202110740127 A CN202110740127 A CN 202110740127A CN 113457381 A CN113457381 A CN 113457381A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- 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
- B01D53/1418—Recovery of products
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention discloses an energy-saving process for capturing and recovering carbon dioxide from chimney exhaust, which is implemented by an energy-saving recovery device, wherein the energy-saving recovery device comprises an absorption tower for cooling high-temperature flue gas and recovering carbon dioxide, a washing liquid storage tank arranged on one side of the absorption tower, a washing liquid pump for pumping washing liquid, a washing liquid heat exchanger and an underground tank. In the process of capturing and recycling the carbon dioxide, the energy consumption can be reduced by recycling the multistage heat, the content of the regenerated gas is effectively reduced by recycling the regenerated gas through reboiling, so that the emission is reduced, the efficiency of recycling the carbon dioxide is improved, the carbon dioxide in the exhaust gas of the chimney is effectively recycled, the recycling of the carbon dioxide is realized, the large-scale emission reduction of the carbon dioxide in the exhaust gas of the chimney is realized, and the environment protection is facilitated.
Description
Technical Field
The invention relates to the technical field of waste gas treatment and recovery, in particular to an energy-saving process for capturing and recovering carbon dioxide from chimney exhaust.
Background
China will adopt more powerful policies and measures, the emission of carbon dioxide strives to reach the peak value 2030 years ago, and strives to realize carbon neutralization 2060 years ago.
At present, the carbon dioxide in the exhaust gas of the chimney is mainly recovered by pressure swing adsorption and chemical absorption methods in China. The main disadvantages of pressure swing adsorption: large investment, high consumption and low recovery efficiency.
The main disadvantages of the chemical absorption method are:
(1) the heat required for regeneration is large;
(2) the corrosion to equipment such as heat exchange equipment, an absorption tower, a washing tower and the like is serious;
(3) is not suitable for recovering CO2 from tail gas with higher oxygen content;
(4) the consumption of the absorbent is huge;
at present, the cost for capturing carbon dioxide from flue gas at home and abroad mainly depends on low-pressure saturated steam of 0.4-0.6 MPa.g, 2.2t steam (even higher) is needed for capturing 1 ton of carbon dioxide from flue gas, and the regeneration energy consumption is particularly high.
Disclosure of Invention
Based on the technical problems in the background art, the invention provides an energy-saving process for capturing and recovering carbon dioxide from chimney exhaust.
The invention provides an energy-saving process for capturing and recovering carbon dioxide by using chimney exhaust gas, which is implemented by an energy-saving recovery device, wherein the energy-saving recovery device comprises an absorption tower for cooling high-temperature flue gas and recovering carbon dioxide, a washing liquid storage tank arranged on one side of the absorption tower, a washing liquid pump for pumping washing liquid, a washing liquid heat exchanger, an underground tank, a barren liquid pump, a liquid-rich pump, a carbon dioxide separator, a carbon dioxide water cooler, a regenerated gas condenser, a heat recovery heater, a gas-liquid separator, a rich liquid reheater, a compressor, a regeneration tower and a steam reboiler;
the energy-saving process for capturing and recovering carbon dioxide by using the chimney exhaust gas comprises the following steps:
s1: the method comprises the following steps of (1) flue gas pretreatment, namely introducing high-temperature flue gas into an absorption tower from the lower part of the absorption tower, and washing and cooling the high-temperature flue gas to 40-50 ℃ by cooling water atomized and sprayed from the inside of the tower top of the absorption tower;
s2: absorbing carbon dioxide, namely introducing the pretreated flue gas into the absorption tower again, absorbing the carbon dioxide in the flue gas by using an absorption tower atomized and sprayed carbon dioxide absorption liquid to form a rich liquid, pumping the rich liquid out of the bottom of the absorption tower by using a rich liquid pump, pressurizing the rich liquid, and then introducing the pressurized rich liquid into a regenerated gas condenser 17 to exchange heat with the gas coming out of the top of a regeneration tower 19 so as to carry out primary heat recovery;
s3: exchanging lean and rich liquid, heating the rich liquid, then feeding the heated rich liquid into a heat recovery heater, spraying the heated rich liquid into a regeneration tower through a spray head at the top of the regeneration tower, decomposing a solution in the regeneration tower to release carbon dioxide, allowing the carbon dioxide to flow out of the top of the regeneration tower along with a large amount of steam, feeding the carbon dioxide into a regeneration gas condenser to exchange heat with the solution pumped by the rich liquid, and performing secondary heat recovery;
s4: recovering carbon dioxide, wherein most of water vapor in the gas discharged from the regenerated gas condenser is condensed, condensate and the gas enter a carbon dioxide water cooler 16 together to exchange heat with circulating water, the regenerated gas is cooled to be less than or equal to 40 ℃, then a carbon dioxide separator is arranged, the condensate carried by the gas is separated in the carbon dioxide separator, the separated carbon dioxide is sent to the next procedure for use after being specially defoamed and metered at the upper part of the carbon dioxide separator, and condensate in the carbon dioxide separator returns to an inlet of a barren liquid pump after entering an underground tank;
s5: reducing the content of the regenerated gas, pressurizing the regenerated gas at the tower top to over 180KPa.g from 20KPa.g by a special compressor, raising the temperature from 98 ℃ to over 160 ℃, heating the pressurized and heated gas by rich liquid or installing a process gas reboiler at the tower bottom of a regeneration tower, and continuing the condensation separation process in S4 after reboiling to reduce the regenerated steam again.
Preferably, the rich liquid pump is connected with a regeneration gas condenser through a control valve, and the lower part of the regeneration gas condenser is connected with a heat recovery heater.
Preferably, one side of the heat recovery heater is connected with a barren liquor pump through a conduit, the top of the barren liquor pump is connected with a carbon dioxide water cooler through a control valve, and the upper end of the carbon dioxide water cooler is connected to the upper part inside the absorption tower.
Preferably, the lower end of the heat recovery heater is connected to the upper part of the regeneration tower, the bottom of the regeneration tower is connected with the heat recovery heater through a pipeline, the steam reboiler is fixedly installed on the outer wall of one side of the bottom of the regeneration tower, and the top of the regeneration tower is communicated with the regenerated gas condenser.
Preferably, the lower part of the regeneration gas condenser is fixedly connected with a carbon dioxide water cooler through a connecting pipe, the lower part of the carbon dioxide water cooler is communicated with the inside of the carbon dioxide separator, and the bottom of the carbon dioxide separator is communicated with the barren liquid pump through a control valve.
The invention has the beneficial effects that:
according to the energy-saving process for capturing and recovering the carbon dioxide from the chimney exhaust gas, disclosed by the invention, in the process of capturing and recovering the carbon dioxide, the energy consumption can be reduced by recycling the multistage heat, the content of the regenerated gas is effectively reduced by reboiling and recovering the regenerated gas, so that the emission is reduced, the efficiency of recovering the carbon dioxide is improved, the carbon dioxide in the chimney exhaust gas is effectively recovered, the reutilization of the carbon dioxide is realized, the large-scale emission reduction of the carbon dioxide in the chimney exhaust gas is realized, and the environmental protection is facilitated.
Drawings
FIG. 1 is a schematic view of a first flow structure of a process for capturing and recovering carbon dioxide from an energy-saving stack exhaust gas according to the present invention;
FIG. 2 is a schematic diagram of a second flow structure of the energy-saving process for capturing and recovering carbon dioxide from stack exhaust gas according to the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Example 1, referring to fig. 1 to 2, an energy-saving process for capturing and recovering carbon dioxide from stack exhaust gas is implemented by an energy-saving recovery apparatus including an absorption tower for cooling high-temperature flue gas and recovering carbon dioxide, a washing liquid storage tank installed at one side of the absorption tower, a washing liquid pump for pumping washing liquid, a washing liquid heat exchanger, an underground tank, a lean liquid pump, a rich liquid pump, a carbon dioxide separator, a carbon dioxide water cooler, a regeneration gas condenser, a heat recovery heater, a gas-liquid separator, a rich liquid reheater, a compressor, a regeneration tower and a steam reboiler, wherein the rich liquid pump is connected to the regeneration gas condenser through a control valve, the regeneration gas condenser is connected to the heat recovery heater below the regeneration gas condenser, one side of the heat recovery heater is connected to the lean liquid pump through a conduit, and the top of the lean liquid pump is connected to the carbon dioxide water cooler through a control valve, the upper end of a carbon dioxide water cooler is connected to the upper part of the inside of an absorption tower, the lower end of a heat recovery heater is connected to the upper part of a regeneration tower, the bottom of the regeneration tower is connected with the heat recovery heater through a pipeline, a steam reboiler is fixedly arranged on the outer wall of one side of the bottom of the regeneration tower, the top of the regeneration tower is communicated with a regeneration gas condenser, the lower part of the regeneration gas condenser is fixedly connected with the carbon dioxide water cooler through a connecting pipe, the lower part of the carbon dioxide water cooler is communicated with the inside of a carbon dioxide separator, and the bottom of the carbon dioxide separator is communicated with a barren liquid pump through a control valve;
the energy-saving process for capturing and recovering carbon dioxide by using the chimney exhaust gas comprises the following steps:
s1: the method comprises the following steps of (1) flue gas pretreatment, namely introducing high-temperature flue gas into an absorption tower from the lower part of the absorption tower, and washing and cooling the high-temperature flue gas to 40-50 ℃ by cooling water atomized and sprayed from the inside of the tower top of the absorption tower;
s2: absorbing carbon dioxide, namely introducing the pretreated flue gas into the absorption tower again, absorbing the carbon dioxide in the flue gas by using an absorption tower atomized and sprayed carbon dioxide absorption liquid to form a rich liquid, pumping the rich liquid out of the bottom of the absorption tower by using a rich liquid pump, pressurizing the rich liquid, and then introducing the pressurized rich liquid into a regenerated gas condenser 17 to exchange heat with the gas coming out of the top of a regeneration tower 19 so as to carry out primary heat recovery;
s3: exchanging lean and rich liquid, heating the rich liquid, then feeding the heated rich liquid into a heat recovery heater, spraying the heated rich liquid into a regeneration tower through a spray head at the top of the regeneration tower, decomposing a solution in the regeneration tower to release carbon dioxide, allowing the carbon dioxide to flow out of the top of the regeneration tower along with a large amount of steam, feeding the carbon dioxide into a regeneration gas condenser to exchange heat with the solution pumped by the rich liquid, and performing secondary heat recovery;
s4: recovering carbon dioxide, wherein most of water vapor in the gas discharged from the regenerated gas condenser is condensed, condensate and the gas enter a carbon dioxide water cooler 16 together to exchange heat with circulating water, the regenerated gas is cooled to be less than or equal to 40 ℃, then a carbon dioxide separator is arranged, the condensate carried by the gas is separated in the carbon dioxide separator, the separated carbon dioxide is sent to the next procedure for use after being specially defoamed and metered at the upper part of the carbon dioxide separator, and condensate in the carbon dioxide separator returns to an inlet of a barren liquid pump after entering an underground tank;
s5: reducing the content of the regenerated gas, pressurizing the regenerated gas at the tower top to over 180KPa.g from 20KPa.g by a special compressor, raising the temperature from 98 ℃ to over 160 ℃, heating the pressurized and heated gas by rich liquid or installing a process gas reboiler at the tower bottom of a regeneration tower, and continuing the condensation separation process in S4 after reboiling to reduce the regenerated steam again.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (5)
1. An energy-saving process for capturing and recovering carbon dioxide from stack gas is characterized in that the process is implemented by an energy-saving recovery device, and the energy-saving recovery device comprises an absorption tower for cooling high-temperature flue gas and recovering carbon dioxide, a washing liquid storage tank arranged on one side of the absorption tower, a washing liquid pump for pumping washing liquid, a washing liquid heat exchanger, an underground tank, a lean liquid pump, a rich liquid pump, a carbon dioxide separator, a carbon dioxide water cooler, a regenerated gas condenser, a heat recovery heater, a gas-liquid separator, a rich liquid reheater, a compressor, a regeneration tower, a steam reboiler and a process gas reboiler;
the energy-saving process for capturing and recovering carbon dioxide by using the chimney exhaust gas comprises the following steps:
s1: the method comprises the following steps of (1) flue gas pretreatment, namely introducing high-temperature flue gas into an absorption tower from the lower part of the absorption tower, and washing and cooling the high-temperature flue gas to 40-50 ℃ by cooling water atomized and sprayed from the inside of the tower top of the absorption tower;
s2: carbon dioxide absorption, namely introducing the pretreated flue gas into an absorption tower again, absorbing the carbon dioxide in the flue gas by using an absorption tower atomized and sprayed carbon dioxide absorption liquid to form a rich liquid, pumping the rich liquid out of the bottom of the absorption tower by using a rich liquid pump, pressurizing the rich liquid, then introducing the pressurized rich liquid into a regenerated gas condenser to exchange heat with the gas coming out of the top of the regeneration tower, and performing primary heat recovery;
s3: exchanging lean and rich liquid, heating the rich liquid, then feeding the heated rich liquid into a heat recovery heater, spraying the heated rich liquid into a regeneration tower through a spray head at the top of the regeneration tower, decomposing a solution in the regeneration tower to release carbon dioxide, allowing the carbon dioxide to flow out of the top of the regeneration tower along with a large amount of steam, feeding the carbon dioxide into a regeneration gas condenser to exchange heat with the solution pumped by the rich liquid, and performing secondary heat recovery;
s4: recovering carbon dioxide, wherein most of water vapor in the gas discharged from the regenerated gas condenser is condensed, condensate and the gas enter a carbon dioxide water cooler together to exchange heat with circulating water, the regenerated gas is cooled to be less than or equal to 40 ℃ and then enters a carbon dioxide separator, the condensate carried by the gas is separated in the carbon dioxide separator, the separated carbon dioxide is specially defoamed and metered at the upper part of the carbon dioxide separator and then is sent to the next procedure for use, and condensate in the carbon dioxide separator returns to an inlet of a barren liquid pump after entering an underground tank;
s5: reducing the content of the regenerated gas, pressurizing the regenerated gas at the tower top to over 180KPa.g from 20KPa.g by a special compressor, raising the temperature from 98 ℃ to over 160 ℃, heating the pressurized and heated gas by rich liquid or installing a process gas reboiler at the tower bottom of a regeneration tower, and continuing the condensation separation process in S4 after reboiling to reduce the regenerated steam again.
2. The process of claim 1, wherein the rich liquid pump is connected with a regeneration gas condenser through a control valve, and a heat recovery heater is connected below the regeneration gas condenser.
3. The process of claim 1, wherein one side of the heat recovery heater is connected with a barren liquor pump through a conduit, the top of the barren liquor pump is connected with a carbon dioxide water cooler through a control valve, and the upper end of the carbon dioxide water cooler is connected to the upper part of the interior of the absorption tower.
4. The process of claim 1, wherein the lower end of the heat recovery heater is connected to the upper part of the regeneration tower, the bottom of the regeneration tower is connected to the heat recovery heater through a pipe, the steam reboiler is fixedly installed on the outer wall of the bottom of the regeneration tower, and the top of the regeneration tower is communicated with the regeneration gas condenser.
5. The process of claim 1, wherein the lower part of the regeneration gas condenser is fixedly connected with a carbon dioxide water cooler through a connecting pipe, the lower part of the carbon dioxide water cooler is communicated with the inside of the carbon dioxide separator, and the bottom of the carbon dioxide separator is communicated with the barren liquor pump through a control valve.
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| CN202110740127.7A CN113457381A (en) | 2021-06-30 | 2021-06-30 | Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114522513A (en) * | 2022-03-07 | 2022-05-24 | 王清 | Low partial pressure carbon dioxide capture process |
| CN114570164A (en) * | 2022-03-31 | 2022-06-03 | 四川益能康生环保科技有限公司 | CO2Or SO2Pressure-swing regeneration energy-saving process for organic amine solution of trapping system |
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| WO2010010720A1 (en) * | 2008-07-23 | 2010-01-28 | 三菱重工業株式会社 | Apparatus for recovering carbon dioxide from discharge gas |
| CN108211671A (en) * | 2018-03-15 | 2018-06-29 | 中国华能集团清洁能源技术研究院有限公司 | A kind of energy-saving carbon dioxide regeneration and compressibility and method |
| CN209630847U (en) * | 2019-03-06 | 2019-11-15 | 重庆朗福环保科技有限公司 | A kind of smoke stack emission gas collecting carbonic anhydride recyclable device |
| CN111662754A (en) * | 2020-07-03 | 2020-09-15 | 上海六谦工程科技有限公司 | Novel coke oven gas desulfurization method |
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2021
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010010720A1 (en) * | 2008-07-23 | 2010-01-28 | 三菱重工業株式会社 | Apparatus for recovering carbon dioxide from discharge gas |
| CN108211671A (en) * | 2018-03-15 | 2018-06-29 | 中国华能集团清洁能源技术研究院有限公司 | A kind of energy-saving carbon dioxide regeneration and compressibility and method |
| CN209630847U (en) * | 2019-03-06 | 2019-11-15 | 重庆朗福环保科技有限公司 | A kind of smoke stack emission gas collecting carbonic anhydride recyclable device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114522513A (en) * | 2022-03-07 | 2022-05-24 | 王清 | Low partial pressure carbon dioxide capture process |
| CN114570164A (en) * | 2022-03-31 | 2022-06-03 | 四川益能康生环保科技有限公司 | CO2Or SO2Pressure-swing regeneration energy-saving process for organic amine solution of trapping system |
| CN114570164B (en) * | 2022-03-31 | 2022-12-30 | 四川益能康生环保科技有限公司 | CO 2 Or SO 2 Pressure swing regeneration energy-saving process for organic amine solution of trapping system |
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Application publication date: 20211001 |