CN105032113A - Process for capturing carbon dioxide in flue gas based on wet reclamation technology - Google Patents
Process for capturing carbon dioxide in flue gas based on wet reclamation technology Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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
Abstract
The invention discloses a process for capturing carbon dioxide in flue gas based on the wet reclamation technology. The process comprises pretreatment, adsorption treatment, washing displacement treatment, water spraying desorption treatment, product air purging treatment, displacement air purging treatment and drying reclamation treatment. A method for efficient and low-cost adsorption separation of high-purity carbon dioxide based on the wet reclamation technology by adopting a functional ion exchange resin membrane material through organic integration with a thermodynamic system of a power plant is provided by the invention.
Description
Technical field
The present invention relates to the technical field of carbon dioxide discharge-reduction, particularly a kind of method based on wet reclamation technology collecting carbon dioxide from fuel gas.
Background technology
Along with the aggravation of greenhouse effects, the discharge how controlling the greenhouse gases based on carbon dioxide causes global extensive concern.The data display that world energy sources tissue (IEA) is announced, global carbon dioxide in 2013 adds up discharge and reaches 36,000,000,000 tons, wherein accounts for 60% by the CO2 emission of the power system based on combustion of fossil fuel.And collecting carbonic anhydride and Plugging Technology Applied (CCS) are considered to one of most effective means controlling power system CO2 emission, wherein, the trapping of carbon dioxide is the important step of CCS technology.
For the environmental condition of power-plant flue gas, capture method conventional at present has: absorption and separation method, adsorption method of separation, membrane separation process, membranes, cryogenic fractionation etc.Current Technical comparing trapping technique that is ripe, that be expected to obtain large-scale industrial application has chemical absorption method and adsorption method of separation.But chemical absorption method ubiquity trapping cost is high, and regeneration energy consumption is large, the problems such as absorbent degraded, burn into volatilization.Such as utilize MEA solwution method capturing power plant carbon dioxide, its regeneration energy consumption is 3 ~ 4MJ/kgCO
2, cause power plant efficiency to decline about 12% thus.Adopt cold ammonia process that power plant efficiency can be made to decline about 10%, but there is the problems such as ammonia volatilization is serious.Adsorbing separation is expected to the trapping cost significantly reducing carbon dioxide, but the carbon dioxide purity that adsorbing separation obtains is lower, and regeneration technology is complicated, and its energy consumption is still higher with trapping cost.
In recent years, report a kind of by regulating environmental humidity in document, realize the method for adsorption-desorption cycle adsorbing separation, be called wet reclamation technology.In this method, by changing, there is the content of the surface water Heshui of the sorbing material of particular functional group, regulating its adsorption binding energy power with carbon dioxide, thus the adsorption equilibrium dividing potential drop of change carbon dioxide.Because the method is that chemisorbed is separated, the carbon dioxide purity therefore obtained is higher; Regenerate with alternating temperature or compared with pressure swing regeneration, wet reclamation technique is simple, and response is very fast.
If Sun Yimin is (based on Atmospheric CO
2the wet reclamation adsorbent experimental study of trapping, Zhejiang University's master thesis) adopt wet reclamation technology, have studied commercial anionic exchange resin membrane (I-200) material of surface modification to CO in air
2absorption property.But the super low concentration that the method for grandson is only applicable in dry air is carbon dioxide enriched, if directly apply to the flue gas trapping of power plant's high humility, high carbon dioxide dividing potential drop, the series of problems such as circulation volume reduces, regeneration difficulty, energy consumption surge will be produced.
Given this, this area is in the urgent need to a kind of method of new and effective capturing power plant carbon dioxide in flue gas.
Summary of the invention
The invention provides a kind of based on wet reclamation technology, adopt the ion exchange resin membrane material of functionalization, by with power plant thermal system organic combination, the method efficient, low cost adsorbing separation goes out high-pureness carbon dioxide.
Based on a technique for wet reclamation technology collecting carbon dioxide from fuel gas, step is as follows:
(1) pretreatment: flue gas is heated to 40 ~ 45 DEG C after cooling and dehumidifying, to adjust the relative humidity of flue gas for 8.7 ~ 11.8%;
(2) adsorb: pretreated flue gas is passed into adsorption tower, contacts with the sorbing material be placed on adsorbent bed, remove the carbon dioxide in flue gas;
Described sorbing material is anion-exchange resin membrane;
(3) rinse displacement: by concentration be 50 ~ 85% carbon dioxide pass into adsorption tower, forward flow through adsorbent bed, the nitrogen in displacement sorption bed, the displacement gas obtained send into displacement gas tank;
(4) water spray desorb: from adsorption tower top spray water, the gaseous mixture of the carbon dioxide that desorb obtains and water vapour enters product gas tank;
(5) gas product purges: the gaseous mixture in portioned product gas tank is passed into adsorption tower, and reverse purging adsorbent bed, reclaims remaining carbon dioxide, then leads to back product gas tank;
(6) displacement gas purges: the displacement gas in displacement gas tank is passed into adsorption tower, reverse purging adsorbent bed, leads to back displacement gas tank after reclaiming remaining carbon dioxide further;
(7) dry regeneration: the flue gas after step (2) carbon dioxide removal is passed into the adsorbent bed after displacement gas purging, elementary drying regeneration is carried out to sorbing material, reclaim the hot-air that in power plant, waste heat and used heat obtain again, secondary drying regeneration is carried out to sorbing material, after sorbing material drying regeneration, start next cyclic process.
The present invention adopts wet reclamation technology, by the equilibrium partial pressure regulating humidity to change sorbing material absorbing carbon dioxide, make full use of the waste heat in power plant and used heat, and adopt multi-tower type circulation absorption-desorb-regeneration techniques, realize the object being continuously separated carbon dioxide in flue gas.
In order to ensure being continuously separated of carbon dioxide in flue gas, the present invention adopts the circulation absorption process of multi-tower type, six steps.As preferably, comprise at least three adsorption towers in described technical process, adsorption tower series circulation carries out step (2) ~ (7).After last adsorption tower completes adsorption step, pretreated flue gas enters next adsorption tower, by that analogy, realizes being continuously separated of carbon dioxide in flue gas.
As preferably, described technical process is divided into three time periods, adsorption process required time is first time period, and rinse displacement, water spray desorb, gas product purge that to take time altogether be the second time period, displacement gas purges and dry regeneration takes time altogether was the 3rd time period.
In order to make its dynamic performance match, and ensure being continuously separated of carbon dioxide in flue gas, as preferably, first time period, the second time period are equal with the 3rd time period required time.
As preferably, in step (1), described flue gas exports from desulfurizing tower of electric power plant, gas concentration lwevel is 10 ~ 15%, temperature is 45 ~ 50 DEG C, and pressure is normal pressure, the saturated wet flue gas under relevant temperature that humidity is less than (namely close to) and pressure.
As preferably, in step (1), first described flue gas is cooled to 35 ~ 40 DEG C through regenerator, then through water-cooled to 25 ~ 30 DEG C, is again chilled to 4 ~ 8 DEG C through electricity, finally utilizes power plant's used heat and regenerator to flue gas to 40 ~ 45 DEG C after dehumidifying.
The flue gas of desulfurizing tower outlet is wet flue gas containing a large amount of saturated vapor, and by the cooling of regenerator and water cooler, flue-gas temperature can be cooled to 25 ~ 30 DEG C by 45 ~ 50 DEG C, now appoints in flue gas and contains more water vapour; By electric cooler, flue-gas temperature is down to 4 ~ 8 DEG C further, and a large amount of water vapour condensations, now steam dividing potential drop is only 0.81 ~ 1.07KPa.Lower flue-gas temperature can reduce the dynamic performance of adsorption process greatly, and the flue gas therefore after cooling and dehumidifying needs to reheat to 40 ~ 45 DEG C.Utilize the flue gas after power plant's used heat and regenerator heating cooling and dehumidifying, the heat-economy of whole system can be significantly improved.
As preferably, in step (2), described anion-exchange resin membrane, anion is selected from the one in fluorine ion, acetate ion, oxalate denominationby, phosphate anion, sulphur hydrogen radical ion.Above-mentioned preferred anion-exchange resin membrane material can be reach higher adsorption capacity in the dry environment of 10 ~ 15% at gas concentration lwevel, and its equilibrium partial pressure increases 1 ~ 2 order of magnitude in a wetted condition.
As preferably, in step (2), adsorption process 35 ~ 45 DEG C, relative humidity carries out under being the normal pressure of 8.7 ~ 11.8%.
Containing nitrogen in flue gas, after the adsorption process of step (2), part nitrogen also can absorb by exchanged resin molding, or be trapped in the hole of adsorbent bed, after the flushing displacement of step (3), nitrogen can be replaced into carbon dioxide, ensure the carbon dioxide obtaining higher concentration after water spray desorb.
As preferably, in step (4), desorption process 35 ~ 45 DEG C, carry out under condition of normal pressure, the water temperature of adsorption tower top spray is 40 ~ 45 DEG C.
In step (6), utilize carbon dioxide remaining in the nitrogen displacement sorption bed in displacement gas, then reclaim carbon dioxide further.As preferably, the displacement gas in displacement gas tank is back to use in step (3), carries out flushings displacement, after the gas concentration lwevel in displacement gas tank is higher than 85%, and the medium carbon dioxide to be recycled of feeding product gas tank.
Compared with prior art, tool of the present invention has the following advantages:
Compared with conventional physical adsorbing separation, the carbon dioxide that wet reclamation technology separation is produced has higher purity; Compared with regenerating with alternating temperature, the wet reclamation response time is short, and equipment is simple; Fully utilized the waste heat in power plant and used heat, heat-economy is better; Corrosion-free, non-toxic, can not secondary pollution be produced.
Accompanying drawing illustrates:
Fig. 1 carries out cooling and dehumidifying to flue gas and the process chart of backheat heating, wherein 1-pressure fan, 2-regenerator, 3-water cooler, 4-point cooler, 5-heater utilizing waste heat;
Fig. 2 is the block diagram of the circulation absorption-desorb-Regenerating Trap carbon dioxide based on wet reclamation;
Fig. 3 is the process chart of three tower circulation absorption-desorb-Regenerating Trap carbon dioxide, the valve that in figure, each digitized representation is different.
Detailed description of the invention
Below in conjunction with accompanying drawing, further detailed description is done to the present invention.
In order to adapt to the sorbent used working environment of wet reclamation, first cooling and dehumidifying process is carried out to the flue gas of desulfurizing tower outlet, as shown in Figure 1.The flue gas of desulfurizing tower outlet is wet flue gas containing a large amount of saturated vapor, and by the cooling of regenerator and water cooler, flue-gas temperature can be cooled to 25 ~ 30 DEG C by 45 ~ 50 DEG C, now still contains more water vapour in flue gas.By electric cooler, flue-gas temperature can be down to 4 ~ 8 DEG C, and a large amount of water vapour condensations, now steam dividing potential drop is only 0.81 ~ 1.07KPa.Lower flue-gas temperature can reduce the dynamic performance of adsorption process greatly, and the flue gas therefore after cooling and dehumidifying needs to reheat to 40 ~ 45 DEG C.Utilize the flue gas after power plant's used heat and regenerator heating cooling and dehumidifying, the heat-economy of whole system can be significantly improved.
In order to ensure being continuously separated of carbon dioxide in flue gas, the present invention adopts three-tower type circulation absorption-desorb-regeneration techniques, and three adsorption tower series circulation carry out following six steps of step, as shown in Figure 2:
Adsorption treatment: pretreated flue gas is passed into adsorption tower, be 35 ~ 45 DEG C in temperature, pressure is in the dry environment of normal pressure, and the anion-exchange resin membrane being fluorine ion with the functional group be placed on adsorbent bed contacts, remove the carbon dioxide in flue gas, the flue gas after carbon dioxide removal is stand-by.
The preparation process of this anion-exchange resin membrane is:
Carry out oven dry pretreatment by from the I type strong-base anion-exchange resin film purchased on the market, then put into the NaOH solution repeated washing of 1mol/L, until Cl
-by OH
-cement out completely.After washing residual NaOH with water, this resin molding material is put into the HF solution of 1mol/L, make OH
-completely by F
-substitute, wash residual HF with water, the anion-exchange resin membrane that functional group is fluorine ion after drying, can be obtained.
The adsorption mechanism of anion-exchange resin membrane used in the present invention is chemisorbed, can reach higher adsorption saturation under the gas concentration lwevel condition of 10 ~ 15%.
Rinse replacement Treatment: the carbon dioxide of high concentration is passed into adsorption tower, forward flows through adsorbent bed, the nitrogen in displacement sorption bed, the displacement gas obtained sends into displacement gas tank, in displacement gas purge step.
Water spray desorb process: from the warm water of adsorption tower top spray 40 ~ 45 DEG C, 35 ~ 45 DEG C, carry out the desorb of anion-exchange resin membrane under condition of normal pressure, the gaseous mixture of the carbon dioxide that desorb obtains and water vapour enters product gas tank;
Gas product purge: the gaseous mixture in product gas tank is passed into adsorption tower, reverse purging adsorbent bed, reclaims remaining carbon dioxide, then leads to back product gas tank;
Displacement gas purge: the displacement gas in displacement gas tank is passed into adsorption tower, reverse purging adsorbent bed, leads to back displacement gas tank after reclaiming remaining carbon dioxide further; Displacement gas can be back to use and rinse in displacement step, after the gas concentration lwevel in displacement gas tank is higher than 85%, sends into the medium carbon dioxide to be recycled of product gas tank.
Dry regeneration process: the flue gas after carbon dioxide removal after adsorption treatment is passed into the adsorbent bed after displacement gas purging, elementary drying regeneration is carried out to sorbing material, reclaim the hot-air that in power plant, waste heat and used heat obtain again, secondary drying regeneration is carried out to sorbing material, after sorbing material drying regeneration, start next cyclic process.
The technological process of the continuous collecting carbon dioxide from fuel gas of three tower six steps, as shown in Figure 3.Function and the mode of operation of each valve are as shown in table 1.Match to make its dynamic performance, six operating procedures of each circulation are divided into equal three time periods time, (1) adsorption time section, (2) rinse displacement, water spray desorb, gas product purge time section, (3) displacement gas purges and dry recovery time section.
In three tower circulation absorption-desorb-regeneration technology flow processs, each adsorbent bed mode of operation illustrates as shown in table 2, first adsorption tower adsorbs, second adsorption tower carries out flushing displacement, water spray desorb, gas product purging, and the 3rd adsorption tower carries out displacement gas and purges and dry regeneration.Sequencing valve controls automatically, subsequent time period, and the first adsorption tower carries out flushing displacement, water spray desorb, gas product purging, and the second adsorption tower carries out displacement gas and purges and dry regeneration, and the 3rd adsorption tower adsorbs.Subsequent time period again, sequencing valve regulates automatically, and make the first adsorption tower carry out displacement gas and purge and dry regeneration, the second adsorption tower adsorbs, and the 3rd adsorption tower carries out flushing displacement, water spray desorb, gas product purging.By the auto-control of sequencing valve, each adsorbent bed will repeat aforesaid operations, be separated with the continuous adsorption realizing carbon dioxide in flue gas.
Table 1
Table 2
As the above analysis, the method based on wet reclamation technology capturing power plant carbon dioxide in flue gas proposed by the invention significantly can reduce the energy consumption of trapping process.In whole technological process, except the power consumption of electric cooler dehumidifying, pump, blower fan and various magnetic valve, all the other institute's energy requirements are all provided by its waste heat or used heat by the integration with power plant thermal system, and comprehensive outside energy consumption is less than 2.3MJ/kgCO
2, compared with traditional MEA removing sulfuldioxide, energy consumption declines about 20%.And trap the carbon dioxide purity obtained higher (more than 99%) by method proposed by the invention, also significantly can lower and follow-uply carry out that carbon dioxide compression is liquefied, transported, the energy consumption of sealing up for safekeeping and cost.
Claims (9)
1. based on a technique for wet reclamation technology collecting carbon dioxide from fuel gas, it is characterized in that, step is as follows:
(1) pretreatment: flue gas is heated to 40 ~ 45 DEG C after cooling and dehumidifying, to adjust the relative humidity of flue gas for 8.7 ~ 11.8%;
(2) adsorb: pretreated flue gas is passed into adsorption tower, contacts with the sorbing material be placed on adsorbent bed, remove the carbon dioxide in flue gas;
Described sorbing material is anion-exchange resin membrane;
(3) rinse displacement: by concentration be 50 ~ 85% carbon dioxide pass into adsorption tower, forward flow through adsorbent bed, the nitrogen in displacement sorption bed, the displacement gas obtained send into displacement gas tank;
(4) water spray desorb: from adsorption tower top spray water, the gaseous mixture of the carbon dioxide that desorb obtains and water vapour enters product gas tank;
(5) gas product purges: the gaseous mixture in portioned product gas tank is passed into adsorption tower, and reverse purging adsorbent bed, reclaims remaining carbon dioxide, then leads to back product gas tank;
(6) displacement gas purges: the displacement gas in displacement gas tank is passed into adsorption tower, reverse purging adsorbent bed, leads to back displacement gas tank after reclaiming remaining carbon dioxide further;
(7) dry regeneration: the flue gas after step (2) carbon dioxide removal is passed into the adsorbent bed after displacement gas purging, elementary drying regeneration is carried out to sorbing material, reclaim the hot-air that in power plant, waste heat and used heat obtain again, secondary drying regeneration is carried out to sorbing material, after sorbing material drying regeneration, start next cyclic process.
2. the technique based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, it is characterized in that, in step (6), displacement gas in displacement gas tank is back to use in step (3), carry out flushing displacement, after the gas concentration lwevel in displacement gas tank is higher than 85%, send into the medium carbon dioxide to be recycled of product gas tank.
3. the technique based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, is characterized in that, comprises at least three adsorption towers in described technical process, and adsorption tower series circulation carries out step (2) ~ (7).
4. the technique based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1 or 3, it is characterized in that, described technical process is divided into three time periods, adsorption process required time is first time period, rinse displacement, water spray desorb, gas product purge that to take time altogether be the second time period, displacement gas purges and dry regeneration takes time altogether was the 3rd time period, and first time period, the second time period are equal with the 3rd time period required time.
5. the technique based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, it is characterized in that, in step (1), described flue gas exports from desulfurizing tower of electric power plant, gas concentration lwevel is 10 ~ 15%, temperature is 45 ~ 50 DEG C, and pressure is normal pressure, and humidity is less than the saturated wet flue gas under relevant temperature and pressure.
6. the method based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, it is characterized in that, in step (1), first described flue gas is cooled to 35 ~ 40 DEG C through regenerator, again through water-cooled to 25 ~ 30 DEG C, again be chilled to 4 ~ 8 DEG C through electricity, finally utilize power plant's used heat and regenerator to flue gas to 40 ~ 45 DEG C after dehumidifying.
7. the method based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, it is characterized in that, in step (2), described anion-exchange resin membrane, anion is selected from the one in fluorine ion, acetate ion, oxalate denominationby, phosphate anion, sulphur hydrogen radical ion.
8. the method based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, is characterized in that, in step (2), adsorption process 35 ~ 45 DEG C, relative humidity carries out under being the normal pressure of 8.7 ~ 11.8%.
9. the method based on wet reclamation technology collecting carbon dioxide from fuel gas according to claim 1, is characterized in that, in step (4), desorption process 35 ~ 45 DEG C, carry out under condition of normal pressure, the water temperature of adsorption tower top spray is 40 ~ 45 DEG C.
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| CN109475806A (en) * | 2016-04-18 | 2019-03-15 | 梅克斯公司 | Sulfate radical is removed from solvent solution using anion exchange resin |
| CN114290511A (en) * | 2021-12-23 | 2022-04-08 | 湖南大学 | Method for enhancing carbon dioxide solid existence in cement-based material |
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| CN109475806A (en) * | 2016-04-18 | 2019-03-15 | 梅克斯公司 | Sulfate radical is removed from solvent solution using anion exchange resin |
| CN109475806B (en) * | 2016-04-18 | 2021-09-24 | 孟莫克公司 | Removal of sulfate from solvent solutions using anion exchange resins |
| CN106178828A (en) * | 2016-09-11 | 2016-12-07 | 上海穗杉实业有限公司 | A kind of on-consumable type carbon dioxide and the integrated treatment unit of moisture content and method |
| CN108821288A (en) * | 2018-07-03 | 2018-11-16 | 杭州快凯高效节能新技术有限公司 | A kind of preparation facilities producing high quality liquid carbon dioxide and its preparation process |
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| CN114290511B (en) * | 2021-12-23 | 2023-01-03 | 湖南大学 | Method for enhancing carbon dioxide solid existence in cement-based material |
| CN114452768A (en) * | 2022-03-03 | 2022-05-10 | 霖和气候科技(北京)有限公司 | CO based on wet-process regenerated adsorption material2Direct air capture system and method |
| CN114558414A (en) * | 2022-03-09 | 2022-05-31 | 霖和气候科技(北京)有限公司 | Method for decarbonizing concentrated carbon dioxide emission source based on wet-process regeneration carbon dioxide capture material |
| CN117463111A (en) * | 2023-12-28 | 2024-01-30 | 山西格瑞思科技有限公司 | CO (carbon monoxide) 2 Gas separation apparatus and method of use thereof |
| CN117463111B (en) * | 2023-12-28 | 2024-03-05 | 山西格瑞思科技有限公司 | CO (carbon monoxide) 2 Gas separation apparatus and method of use thereof |
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