CN113491946A - Absorbent regeneration equipment and regeneration method - Google Patents

Absorbent regeneration equipment and regeneration method Download PDF

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Publication number
CN113491946A
CN113491946A CN202010270799.1A CN202010270799A CN113491946A CN 113491946 A CN113491946 A CN 113491946A CN 202010270799 A CN202010270799 A CN 202010270799A CN 113491946 A CN113491946 A CN 113491946A
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regeneration
absorbent
tower
membrane
catalytic reactor
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CN113491946B (en
Inventor
于品华
孔凡敏
赵运生
苏豪
徐莉
张叶
吴小莲
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • 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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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention provides absorbent regeneration equipment and a regeneration method, which remove carbon dioxide in absorbent pregnant solution by adopting a membrane catalytic pressurization and flash regeneration mode, and belong to the technical field of energy conservation and environmental protection. And (3) delivering the rich liquid absorbing the carbon dioxide into a tube pass of a membrane catalytic reactor at the upper part of the regeneration tower by using a pressure pump, and decomposing the rich liquid into the carbon dioxide and an absorbent under the catalysis of active components on the inner surface of the hollow fiber membrane and under the condition that heat is provided by low-pressure steam. The desorbed rich liquid is decompressed to normal pressure by a pressure reducing valve arranged at the top of the flash regeneration tower, carbon dioxide is desorbed from the solution and enters the flash regeneration tower through a gas-liquid distributor, wherein the flash carbon dioxide gas is discharged out of the tower through a regenerated gas pipeline arranged at the top of the flash regeneration tower, and the barren liquid passes through a packing layer and is then sent out of the tower through a barren liquid pipeline at the bottom of the flash regeneration tower. Compared with the existing thermal regeneration mode, the method has the advantages of low regeneration temperature, low energy consumption, high barren solution regeneration degree and the like, and is particularly suitable for the decarburization of chemical reaction or the desorption of the decarburization pregnant solution of physical and chemical reaction.

Description

Absorbent regeneration equipment and regeneration method
Technical Field
A method and equipment for regenerating an absorbent belong to the technical field of energy conservation and environmental protection and are used for desorbing carbon dioxide from absorbent pregnant solution absorbing the carbon dioxide.
Background
The absorption method is the most mature separation technique with the widest application and the best purification effect no matter the capture and separation of carbon dioxide or the removal of carbon dioxide in industrial gas.
The absorption method for capturing carbon dioxide can be roughly classified into a physical absorption method in which CO is physically dissolved in a pure solvent and a chemical absorption method2And the energy consumption is low by a mode of pressurizing, absorbing and decompressing regeneration.
The chemical absorption principle is to realize the transfer process of carbon dioxide from gas phase to liquid phase by utilizing the chemical reaction of absorbent molecules and carbon dioxide molecules, and has the advantages of high gas purification degree, large absorption capacity and high absorption rate.
However, the rich solution regeneration requires steam to heat the rich solution to a higher temperature, and the energy consumption is very high. If the desorption temperature of the potassium carbonate pregnant solution is usually 105-125 ℃, the MEA pregnant solution needs to be heated to more than 120 ℃, and the energy consumption of the MEA thermal regeneration is about 4 MJ/kgCO2And the energy consumption of the whole process is about more than 80%.
Researchers at home and abroad reduce the regeneration energy consumption by adopting various measures such as developing a novel absorbent, improving a regeneration method and the like.
For example, domestic patent CN200680052594.4 discloses a method for regenerating amines in carbon dioxide recovery by performing two or more stages of vaporization at decreasing pressure to regenerate alkanolamine absorbent solution used for recovering carbon dioxide from feed gas.
Patent CN200810168382.3 discloses a method for regenerating a carbon dioxide absorbent, which is to use a preheated absorbent generated in the process of compressing and separating carbon dioxide in a compressor before the used absorbent is transferred to a regeneration tower, and the preheated absorbent is transferred to an absorbent flow control tank, improving energy efficiency. The absorbent regeneration is carried out by a method based on heating absorbent rich liquid, the consumption reduction range is not obvious, and the absorbent is degraded due to higher thermal regeneration temperature.
CN201010169524.5 discloses a pressure reduction regeneration system and method using a hollow fiber membrane contactor, in which a carbon dioxide-rich absorbent is heated and pumped to the tube side of the hollow fiber membrane contactor, and the shell side is purged with purge steam and a negative pressure is provided by a vacuum pump, so that the regeneration temperature can be reduced. Although the method can reduce the regeneration temperature, the method cannot achieve higher regeneration effect.
As reported in the literature (Chinese Motor engineering report, 2013, 33 (5): 61-67), the regeneration degree of the membrane reduced pressure regeneration is not high, the load of the barren solution entering the absorption tower is still high, the speed of the reabsorption process is reduced, and 0.5mol CO is used at the initial load2At a maximum of only 45% of the regeneration per mol of MEA, i.e. 55% of CO is still present2Remains in the absorbent. CO is not reduced or increased because the circulation volume of the solution is not reduced2The trapping energy consumption is not greatly reduced.
In fact, during the regeneration of the rich solution, because of the normal pressure operation, a large amount of water needs to be vaporized, and a large amount of heat energy is consumed. On the other hand, a higher desorption temperature is required because of the CO2The activation energy required for desorption of the complex formed by reaction with the absorbent is higher.
Disclosure of Invention
The invention aims to provide a method and equipment for regenerating an absorbent, belonging to the technical field of energy conservation and environmental protection. The regeneration tower is divided into an upper membrane catalytic reactor and a lower flash evaporation regeneration tower by adopting a catalytic pressurization regeneration method, the rich solution is heated and catalytically desorbed in the membrane catalytic reactor, and the gas-liquid separation is carried out in the flash evaporation regeneration tower by reducing the pressure. Has the advantages of low regeneration temperature, low energy consumption, high regeneration degree and the like.
In order to overcome the desorption temperature required for conventional rich liquid regeneration, and simultaneously reduce the latent heat taken away by the evaporation of a large amount of water. The idea of the invention is to adopt a membrane catalysis scheme to reduce the regeneration activation energy of the absorbent carbon dioxide compound and reduce the desorption temperature, and adopt a pressurization regeneration scheme to reduce the heat loss caused by water evaporation. The membrane catalytic reactor at the upper part of the regeneration tower is activated and desorbed into a gas-liquid mixture under pressurization, and the flash evaporation regeneration tower at the lower part of the regeneration tower separates gas and liquid in the pregnant solution through a pressure reducing valve and a gas-liquid distributor, thereby greatly reducing the energy consumption, improving the purification degree of the barren solution and effectively overcoming the defects of the prior art
The invention is realized by the following steps: the absorbent regeneration equipment is characterized by comprising an absorbent rich liquid storage tank, a low-pressure steam source, a rich liquid pump, a regeneration tower, a pressure reducing valve and a gas-liquid distributor, wherein the upper section of the regeneration tower is a membrane catalytic reactor, and the lower section of the regeneration tower is a pressure reducing flash tower; the absorbent rich liquid storage tank is connected with a rich liquid pump, and the rich liquid pump is connected with the top tube pass of the membrane catalytic reactor; the low-pressure steam source is connected with the upper shell side of the membrane catalytic reactor, and the bottom of the tube side of the membrane catalytic reactor is sequentially connected with the pressure reducing valve and the gas-liquid distributor.
The invention also provides an absorbent regeneration method, wherein the regeneration tower is divided into an upper membrane catalytic reactor and a lower flash evaporation regeneration tower, the rich liquid absorbing the carbon dioxide is pumped to the tube pass of the membrane catalytic reactor by a booster pump, the shell pass is heated by low-pressure steam to provide energy for the rich liquid, and the absorbent compound in the rich liquid is desorbed into the absorbent and the carbon dioxide under the catalytic action of the active sites on the inner surface of the tube pass of the membrane catalytic reactor and the energy provided by the low-pressure steam, and the gas is not separated out due to the pressurized state. The rich liquid after catalytic reaction is pressurized to normal pressure through a pressure reducing valve arranged at the bottom of the membrane catalytic reactor, carbon dioxide gas is separated out from the liquid and is subjected to gas-liquid separation through a gas-liquid distributor and a space between a pressure reduction regeneration tower and the membrane catalytic reactor, the gas is regenerated gas and is sent out of the tower, and the liquid is regenerated barren liquid and is sent out of the tower through a barren liquid pipeline arranged at the bottom of the tower.
The heating low-pressure steam can adopt waste heat or other low-grade heat sources, and the absorbent rich solution is only required to be heated to 70-90 ℃.
The rich solution is absorbent aqueous solution absorbing carbon dioxide, and the absorbent can be one of potassium carbonate, sodium hydroxide, ammonia water and alcohol amine.
The membrane catalytic reactor at the top of the regeneration tower is a hollow fiber compact composite membrane, low-pressure steam is fed on the shell side, and rich liquid is fed on the tube side.
The inner surface material of the hollow fiber compact membrane adopts zeolite molecular sieve Al2O3、ZrO2、SiO2Is a basal membrane skeleton and is doped with TiO2And (3) nanoparticles.
The outer surface of the hollow fiber compact membrane adopts a plating layer of a metal copper, silver and gold heat conduction material, low-pressure steam is condensed and released on the outer surface of the shell side hollow fiber compact membrane, and rich liquid is heated through metal thin wall heat conduction.
The operation pressure of the tube side of the membrane catalytic reactor at the upper part of the regeneration tower is 0.3-0.5 MPa.
And heating the rich solution to 70-90 ℃ by low-pressure steam in the shell pass of the membrane catalytic reactor at the upper part of the regeneration tower.
And the pressure of the rich solution from the membrane catalytic reactor at the lower part of the regeneration tower is reduced to 0-10 kPa through a pressure reducing valve.
The residence time of the rich solution in the membrane catalytic reactor is 80-120 s.
The residence time of the rich solution in the decompression regeneration tower is 150-300 s.
CO in the regenerated barren solution2The residual amount is less than 10% of the saturated absorption amount.
Technical effects of the invention
The invention relates to absorbent regeneration equipment and a method, which are characterized in that rich liquid absorbing carbon dioxide is pressurized by a rich liquid pump and then is sent to a tube pass of a membrane catalytic reactor at the upper part of a regeneration tower, carbon dioxide is desorbed to form a gas-liquid mixture under the catalytic action of membrane materials on the inner wall of the tube pass and the action of low-pressure steam heat on the outer surface of shell pass fibers, the rich liquid is decompressed to normal pressure by a decompression valve and a gas-liquid distributor at the bottom of the membrane catalytic reactor, the rich liquid enters a decompression flash tower at the lower part of the regeneration tower after gas-liquid separation, the separated regeneration gas is discharged from a pipeline at the middle part of the regeneration tower, and lean liquid after gas-liquid separation is sent out of the tower by a lean liquid pipeline arranged at the bottom of the decompression flash tower.
Compared with the conventional thermal regeneration, the catalytic pressure flash regeneration has the advantages of low regeneration temperature, low energy consumption, high barren solution regeneration degree and the like. It is especially suitable for regeneration of pregnant solution after removing carbon dioxide by chemical method or physical chemical method.
Drawings
FIG. 1 is a schematic diagram showing the connection of the absorbent regeneration method in the example of the present invention.
In the figure, 1 is an absorbent rich liquid storage tank, 2 is a low-pressure steam source, 3 is a rich liquid pump, 4 is a regeneration tower, 5 is a membrane catalytic reactor, 6 is a reduced-pressure flash tower, 7 is a pressure reducing valve, and 8 is a gas-liquid distributor.
Detailed Description
The invention is described in further detail below with reference to the figures and examples.
Example 1
As shown in the figure, the absorbent regeneration equipment mainly comprises an absorbent rich liquid storage tank 1, a low-pressure steam source 2, a rich liquid pump 3, a regeneration tower 4, a membrane catalytic reactor 5, a reduced-pressure flash tower 6, a pressure reducing valve 7 and a gas-liquid distributor 8; the absorbent rich liquid storage tank 1 is connected with a rich liquid pump 3, and the rich liquid pump 3 is connected with the top tube pass of the membrane catalytic reactor 5; the low pressure steam source 1 is connected with the upper shell side of the membrane catalytic reactor 5. The bottom of the tube pass of the membrane catalytic reactor 5 is connected with a pressure reducing valve 7 and a gas-liquid distributor 8 in sequence.
Example 2
The absorbent regeneration method adopts the regeneration equipment in the embodiment 1.
Pressurizing the carbon dioxide-rich absorbent solution in the rich solution storage tank 1 to 0.3-0.5 MPa through a rich solution pump 3, enabling the rich solution to enter a tube pass of a membrane catalytic reactor 5 on the upper part of a regeneration tower in a pressurized state, reducing the desorption activation energy of compound molecules absorbing carbon dioxide under the action of the inner surface catalyst active component of a hollow fiber membrane of the membrane catalytic reactor 5, desorbing the compound molecules into carbon dioxide and absorbent molecules at the temperature of 70-90 ℃, and enabling the retention time of the rich solution in the membrane catalytic reactor to be 80-120 s. The low-pressure steam from the low-pressure steam source 2 can be steam with low waste heat and waste heat energy grade, the low-pressure steam enters the upper shell pass of the membrane catalytic reactor 5, and the heated condensate water is discharged from a pipeline arranged at the lower shell pass of the membrane catalytic reactor 5.
The rich liquid is desorbed into carbon dioxide and an absorbent by the membrane catalytic reactor 5, and exists in a gas-liquid mixture state because it is in a pressurized state. The desorbed rich liquid-gas mixture passes through a pressure reducing valve 7 arranged at the bottom of the membrane catalytic reactor 5, namely at the top of a pressure reducing flash tower 6 arranged at the lower part of the regeneration tower 4, the pressure drops suddenly to 0 kPa-10 kPa, and a large amount of CO is generated due to the pressure drop2The gas is evolved while the rich liquid becomes lean. CO after flash evaporation2And after the lean solution passes through a gas-liquid distributor 8 arranged behind a pressure reducing valve 7, the gas enters the top of the pressure reducing regeneration tower through a gap between the gas-liquid distributor 8 and the tower wall of the regeneration tower 4 and is discharged out of the tower through a regeneration gas pipeline. And uniformly spraying the regenerated barren solution onto a packing layer at the lower part of the reduced-pressure regeneration tower 6 by the gas-liquid distributor 8, wherein the retention time of the barren solution in the reduced-pressure regeneration tower 6 is 150-300 s for fully flashing the barren solution. The flashed barren solution is sent out of the tower by a barren solution pipeline arranged at the bottom of the decompression regeneration tower 6 for recycling. Due to the lower heating temperature, only a small amount of water evaporates. CO in regenerated barren solution2The content is less than 10% of the saturated absorption capacity of the absorbent, and the solution circulation amount can be greatly reduced.

Claims (10)

1. The absorbent regeneration equipment is characterized by comprising an absorbent rich liquid storage tank, a low-pressure steam source, a rich liquid pump, a regeneration tower, a pressure reducing valve and a gas-liquid distributor, wherein the upper section of the regeneration tower is a membrane catalytic reactor, and the lower section of the regeneration tower is a pressure reducing flash tower; the absorbent rich liquid storage tank is connected with a rich liquid pump, and the rich liquid pump is connected with the top tube pass of the membrane catalytic reactor; the low-pressure steam source is connected with the upper shell side of the membrane catalytic reactor, and the bottom of the tube side of the membrane catalytic reactor is sequentially connected with the pressure reducing valve and the gas-liquid distributor.
2. A process for regenerating absorbent includes pumping the rich liquid to the top of regenerating tower, two-stage regeneration, catalytic pressurizing regeneration of membrane in the upper part of regenerating tower, loading the rich liquid in the tube pass of catalytic reactor, and loading the catalyst on the surface of membrane2Dissociating from the absorbent molecules, heating the shell pass of the membrane catalytic reactor by adopting low-pressure steam, and discharging condensed water; the lower part of the regeneration tower is decompression flash evaporation regeneration, the rich liquid from the bottom of the membrane catalytic reactor is decompressed to normal pressure by a decompression valve in one step, then is flash evaporated and regenerated by a gas-liquid distributor, the gas enters a regeneration gas pipeline discharge system arranged in the middle of the tower through the annular gap between the gas-liquid distributor and the wall of the regeneration tower, the liquid is sprayed to the filler at the bottom of the tower and finally converged to the tower bottom, and the liquid is discharged from the system through a lean liquid pipeline.
3. The method for regenerating the absorbent according to claim 2, wherein the membrane catalytic reactor at the top of the regeneration tower is a hollow fiber dense membrane, low-pressure steam is fed on the shell side, and rich liquid is fed on the tube side; the pregnant solution is absorbent aqueous solution absorbing carbon dioxide, and the absorbent is one of potassium carbonate, alcohol amine, ammonia water and sodium hydroxide.
4. The method of claim 3, wherein the hollow fiber dense membrane has an inner surface material of zeolite molecular sieve Al2O3、ZrO2、SiO2Is a basal membrane skeleton and is doped with TiO2And (3) nanoparticles.
5. A method for regenerating an absorbent as claimed in claim 3, wherein said hollow fiber dense membrane has an outer surface coated with a thermally conductive material selected from the group consisting of copper, silver and gold.
6. The method for regenerating the absorbent as claimed in claim 2, wherein the operating pressure of the tube side of the membrane catalytic reactor at the upper part of the regeneration tower is 0.3-0.5 MPa, and the temperature of the rich solution is heated to 70-90 ℃ by low-pressure steam at the shell side.
7. The method for regenerating the absorbent as set forth in claim 2, wherein the pressure of the rich liquid from the membrane catalytic reactor at the lower part of the regeneration tower is reduced to 0 to 10kPa by a pressure reducing valve.
8. The method for regenerating the absorbent according to claim 2, wherein the residence time of the rich solution in the membrane catalytic reactor is 80s to 120 s.
9. The method for regenerating the absorbent according to claim 2, wherein the residence time of the rich liquid in the vacuum flash tower is 150s to 300 s.
10. The method of claim 2, wherein the CO in the regenerated lean solution is regenerated2The residual amount is less than 10% of the saturated absorption amount.
CN202010270799.1A 2020-04-08 2020-04-08 Absorbent regeneration equipment and regeneration method Active CN113491946B (en)

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Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101822931A (en) * 2010-05-11 2010-09-08 浙江大学 Decompression regeneration system and method for hollow fiber membrane contactor of carbon dioxide enriched absorbent solution
AU2012216559A1 (en) * 2008-03-21 2012-09-20 Alstom Technology Ltd A system and method for enhanced removal of CO2 from a mixed gas stream
CN102917773A (en) * 2010-03-30 2013-02-06 里贾纳大学 Catalytic method and apparatus for separating a gaseous component from an incoming gas stream
CN203620479U (en) * 2014-02-27 2014-06-04 三江湖石化工有限公司 Regeneration structure for processing carbonate-rich solution
CN103877828A (en) * 2012-12-21 2014-06-25 中国科学院大连化学物理研究所 Absorption liquid regeneration method and special-purpose absorption liquid regeneration device
CN105771550A (en) * 2014-12-22 2016-07-20 北京化工大学 Method using throttling expansion principle to promote regeneration of carbon dioxide absorbent
CN107149865A (en) * 2017-05-24 2017-09-12 华中农业大学 CO based on vapor mass transfer enhancement waste heat recovery2Chemical absorbing System and method for
CN109351125A (en) * 2018-09-20 2019-02-19 湖南大学 One kind is for reducing rich CO2The new catalytic desorber of amine aqueous solution regeneration energy consumption
CN109513313A (en) * 2017-09-20 2019-03-26 中国石油化工股份有限公司 A kind of low-temperature catalyzed regeneration method of collecting carbonic anhydride solvent
CN109589792A (en) * 2018-12-29 2019-04-09 北京博奇电力科技有限公司 A kind of device and method of low temperature wet flue gas denitration
KR20200011761A (en) * 2018-07-25 2020-02-04 한국에너지기술연구원 Method for distillation regeneration of amine-based CO2 absorbents using metal oxide catalyst

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2012216559A1 (en) * 2008-03-21 2012-09-20 Alstom Technology Ltd A system and method for enhanced removal of CO2 from a mixed gas stream
CN102917773A (en) * 2010-03-30 2013-02-06 里贾纳大学 Catalytic method and apparatus for separating a gaseous component from an incoming gas stream
CN101822931A (en) * 2010-05-11 2010-09-08 浙江大学 Decompression regeneration system and method for hollow fiber membrane contactor of carbon dioxide enriched absorbent solution
CN103877828A (en) * 2012-12-21 2014-06-25 中国科学院大连化学物理研究所 Absorption liquid regeneration method and special-purpose absorption liquid regeneration device
CN203620479U (en) * 2014-02-27 2014-06-04 三江湖石化工有限公司 Regeneration structure for processing carbonate-rich solution
CN105771550A (en) * 2014-12-22 2016-07-20 北京化工大学 Method using throttling expansion principle to promote regeneration of carbon dioxide absorbent
CN107149865A (en) * 2017-05-24 2017-09-12 华中农业大学 CO based on vapor mass transfer enhancement waste heat recovery2Chemical absorbing System and method for
CN109513313A (en) * 2017-09-20 2019-03-26 中国石油化工股份有限公司 A kind of low-temperature catalyzed regeneration method of collecting carbonic anhydride solvent
KR20200011761A (en) * 2018-07-25 2020-02-04 한국에너지기술연구원 Method for distillation regeneration of amine-based CO2 absorbents using metal oxide catalyst
CN109351125A (en) * 2018-09-20 2019-02-19 湖南大学 One kind is for reducing rich CO2The new catalytic desorber of amine aqueous solution regeneration energy consumption
CN109589792A (en) * 2018-12-29 2019-04-09 北京博奇电力科技有限公司 A kind of device and method of low temperature wet flue gas denitration

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