CN105749696B - A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy - Google Patents
A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy Download PDFInfo
- Publication number
- CN105749696B CN105749696B CN201610264710.4A CN201610264710A CN105749696B CN 105749696 B CN105749696 B CN 105749696B CN 201610264710 A CN201610264710 A CN 201610264710A CN 105749696 B CN105749696 B CN 105749696B
- Authority
- CN
- China
- Prior art keywords
- adsorption
- flue gas
- carbon dioxide
- desorption device
- valve group
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 198
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 104
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000002336 sorption--desorption measurement Methods 0.000 title abstract description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 107
- 239000003546 flue gas Substances 0.000 claims abstract description 106
- 238000010521 absorption reaction Methods 0.000 claims abstract description 37
- 239000003463 adsorbent Substances 0.000 claims abstract description 21
- 230000008569 process Effects 0.000 claims abstract description 13
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000010457 zeolite Substances 0.000 claims abstract description 6
- 238000003795 desorption Methods 0.000 claims description 168
- 238000001179 sorption measurement Methods 0.000 claims description 164
- 239000007789 gas Substances 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 238000004458 analytical method Methods 0.000 claims description 3
- 238000004804 winding Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000003912 environmental pollution Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 2
- 229960004424 carbon dioxide Drugs 0.000 abstract 6
- 235000011089 carbon dioxide Nutrition 0.000 abstract 2
- 230000009977 dual effect Effects 0.000 abstract 1
- 230000001360 synchronised effect Effects 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0454—Controlling adsorption
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/4002—Production
- B01D2259/40022—Production with two sub-steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/4006—Less than four
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy of the present invention, belongs to collecting carbonic anhydride technical field；The system includes air compressor machine, flue gas analyzer, carbon dioxide collection tank, adsorption desorption device, the first valve group, the second valve group, two pressure gauges, three flowmeters and three thermometers；The present invention is using reusable edible and the zeolite 13X of economic and reliable is as adsorbent, and while using low grade heat energy, it is synchronous to carry out carbon dioxide adsorption desorption process, heat exchange efficiency is improved, realizes the effect of UTILIZATION OF VESIDUAL HEAT IN and collecting carbonic anhydride dual-effect energy-saving；The present invention is used as energy source using the low grade heat energy in flue gas, circulation adsorption desorption is realized with reference to physics alternating temperature, improve efficiency, system operation time is saved, reduce about sixty percent system energy consumption, environmental pollution caused by reducing the flue gas of thermal power plant, and the trapping concentration of carbon dioxide can reach 90 percent after the absorption of three steps.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide capture, and particularly relates to a carbon dioxide temperature-changing adsorption and desorption system and method based on low-grade heat energy.
Background
In recent years, CO2The emission is in a growing trend and is huge, wherein 2014 is global CO2The discharge amount is 323 hundred million tons; to cope with the problem of global warming caused by greenhouse gases, CO2Trapping technology is constantly evolving; CO 22The trapping technology mainly comprises a physical adsorption method, a chemical absorption method, a membrane separation technology and a low-temperature separation technology; wherein the physical adsorption method is to use gas and adsorbentThe attraction between the surface active points is realized in the filling fluidized bed, and the method has the characteristics of simple equipment, no corrosion, wide pressure range, low energy consumption and environmental pollution and recyclable adsorbent, is more in line with the idea of energy conservation and emission reduction compared with other adsorption modes, and is more beneficial to realization in the technical field; at present, CO2The physical trapping method of (3) is mainly a pressure swing adsorption method, a temperature swing adsorption method, a power transformation adsorption method, a temperature swing pressure coupling adsorption method and the like.
In the physical adsorption method, the temperature swing adsorption method is realized by utilizing the difference of the adsorption performance of gas components on a solid material and the change of adsorption capacity at different temperatures, has the advantages of simple process flow, strong desorption capacity of an adsorbent and the like, and is widely applied to engineering; usually, at low temperature, the adsorption and desorption bed is used for CO2Carrying out adsorption; after adsorption saturation, the adsorption column is heated to reach CO2Under the desorption condition, completing the desorption process so as to regenerate the adsorbent; after complete desorption, cooling operation is carried out, and CO is adsorbed at low temperature2So as to circulate; at present, an adsorption and desorption device designed based on a temperature swing adsorption method is mainly composed of two adsorption towers, a regenerative heater, a regenerative cooler and a regenerated water separator; one tower is used for adsorption, the other tower is used for regeneration, and the synthetic gas passes through the adsorbent, trace water and CO from the bottom of the adsorption tower to the top2Are sequentially adsorbed; taking the raw synthesis gas obtained by steam reforming of natural gas as an example, the main gas components are as follows: hydrogen, carbon monoxide, carbon dioxide, methane; removing most of carbon dioxide by using a methyl diethanolamine solvent, cooling and separating liquid by using a cooling dryer, and purifying by using a TSA adsorption tower; the synthesis gas entering the adsorption tower also contains saturated steam and impurities such as carbon dioxide of about 20mg/kg, and the impurities can be frozen out in the subsequent cryogenic separation process of the cold box, so that cold box equipment and pipelines are blocked, and the device cannot be normally produced, so that the substances need to be removed before the synthesis gas enters the cold box. The gas regenerated by the adsorption tower comes from the cold box, and the gas mainly comprises methane, hydrogen and a small amount of nitrogen. The regenerated gas is sent to steam reformingThe system serves as the primary fuel for the reformer.
However, in the temperature swing adsorption process, due to the large specific heat capacity of the adsorbent, the energy consumption is large in the process of continuously heating and cooling the adsorption column, and the heating and cooling time of the adsorption bed is also long, so that the adsorption bed becomes a main factor for limiting the development of temperature swing adsorption and becomes a problem which is addressed by the scholars; the chemical adsorbent is selected to bring certain environmental pollution, which is not beneficial to the development of circular economy; the principle of the electric transformation adsorption method proposed in recent years is to electrify and heat an adsorbent with conductivity, so that the heating rate of the adsorbent is increased, and the desorption process under the high-temperature condition has the advantages of high heating speed, low energy consumption and convenience for automatic control, but as additional electric energy is also consumed for a part of energy, the problems of energy consumption and resource waste still exist in the process; meanwhile, a large amount of low-temperature (100-200 ℃) flue gas is generated in the production of the thermal power plant, the low-level heat energy content is huge, but the flue gas is difficult to directly recycle in the actual production and is often directly discharged into the environment, so that the thermal pollution to the environment is caused, and the energy is wasted.
At present, most of existing carbon dioxide temperature-changing absorption and desorption systems adopt a heat pump mode, however, high-temperature hot water combined with the existing high-temperature heat and power combined supply system cannot be provided by singly using the first-type or second-type absorption heat pump, energy consumption is too high, resources are wasted, an absorption material cannot be recycled, an absorption and desorption process cannot be matched and controlled, absorption and desorption efficiency is low, equipment operation time is long, and cost is high.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a carbon dioxide temperature-changing adsorption and desorption system and a carbon dioxide temperature-changing adsorption and desorption method based on low-grade heat energy, so as to achieve the purposes of reducing energy consumption, realizing cyclic utilization of an adsorption material, improving adsorption and desorption efficiency and reducing environmental pollution.
A carbon dioxide variable temperature adsorption and desorption system based on low-grade heat energy comprises an air compressor, a flue gas analyzer, a carbon dioxide collecting tank, an adsorption and desorption device, a first valve group, a second valve group, two pressure gauges, three flow meters and three thermometers;
the air compressor and the flue gas exhaust pipeline of the thermal power plant are respectively connected with a first valve group through pipelines, and the first valve group is connected with an inlet of the adsorption and desorption device through a pipeline; the outlet of the adsorption and desorption device is connected with a second valve group through a pipeline, and the second valve group is respectively connected with a carbon dioxide collecting tank and a flue gas analyzer through pipelines; setting an outlet of a flue gas analyzer as a gas discharge channel; the first pressure gauge, the first flowmeter and the first thermometer are installed at an outlet of a flue gas exhaust pipeline of a thermal power plant, the second pressure gauge, the second flowmeter and the second thermometer are installed at an exhaust outlet of an air compressor, the third flowmeter is installed at an inlet of a carbon dioxide collecting tank, and the third thermometer is installed at an inlet of a flue gas analyzer;
the adsorption and desorption device comprises a first adsorption and desorption device, a second adsorption and desorption device, a third valve group and a fourth valve group; the first adsorption and desorption device and the second adsorption and desorption device respectively comprise an inner tube, a fin, an adsorbent and an outer tube; the inner pipe is arranged in the pipeline of the outer pipe, fins are wound on the outer wall of the inner pipe, and the inner part of the inner pipe is filled with the adsorbent; the inner pipe and the outer pipe are both provided with an inlet and an outlet; the outlet of the outer pipe of the first adsorption and desorption device and the outlet of the outer pipe of the second adsorption and desorption device are respectively connected with a third valve group through pipelines, the third valve group is respectively connected with a gas discharge channel and a fourth valve group through pipelines, and the fourth valve group is respectively connected with the inlet of the inner pipe of the first adsorption and desorption device and the inlet of the inner pipe of the second adsorption and desorption device through pipelines; the outer tube inlet of the first adsorption and desorption device and the outer tube inlet of the second adsorption and desorption device are arranged as the inlets of the adsorption and desorption devices, and the inner tube outlet of the first adsorption and desorption device and the inner tube outlet of the second adsorption and desorption device are arranged as the outlets of the adsorption and desorption devices.
The adsorbent adopts zeolite 13X molecular sieve.
The fins are high-frequency winding fin.
The number of the valves of the first valve group, the second valve group, the third valve group and the fourth valve group is more than or equal to the number of the pipelines connected with the valve groups.
Each valve of the first valve group, the second valve group, the third valve group and the fourth valve group is independent.
The absorption and desorption method adopting the carbon dioxide variable temperature absorption and desorption system based on low-grade heat energy comprises the following steps:
step 1, setting a carbon dioxide content threshold;
step 2, communicating all devices of the system through each valve group, and adsorbing carbon dioxide by adopting a first adsorption and desorption device, wherein the method comprises the following specific steps:
2.1, communicating a flue gas exhaust pipeline with an outer pipe inlet of a second adsorption and desorption device by adopting a first valve group, and communicating an air compressor with an outer pipe inlet of a first adsorption and desorption device;
2.2, communicating an outlet of an inner pipe of the first absorption and desorption device with a flue gas analyzer by adopting a second valve group; an outlet of an inner pipe of the second adsorption and desorption device is communicated with a carbon dioxide collecting tank;
2.3, communicating an outlet of an outer pipe of the first adsorption and desorption device with a gas discharge channel by adopting a third valve group, and communicating an outlet of an outer pipe of the second adsorption and desorption device with an inlet of an inner pipe of the first adsorption and desorption device by adopting the third valve group and a fourth valve group;
2.4, enabling the flue gas in the flue gas exhaust pipeline to enter an inner pipe of a first absorption and desorption device through an outer pipe of a second absorption and desorption device, adsorbing the flue gas with carbon dioxide by adopting an adsorbent, and enabling the adsorbed flue gas to enter a flue gas analyzer;
step 2.5, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer is larger than or equal to a set threshold value, if so, discharging the flue gas, and executing the step 3, otherwise, returning to execute the step 2.4;
step 3, setting the first adsorption and desorption device to perform carbon dioxide desorption, setting the second adsorption and desorption device to perform carbon dioxide adsorption, and communicating each device of the system again through each valve group, wherein the method comprises the following specific steps:
step 3.1, setting a first absorption and desorption device to perform carbon dioxide desorption, and setting a second absorption and desorption device to perform carbon dioxide absorption;
3.2, communicating a flue gas exhaust pipeline with an outer pipe inlet of the first adsorption and desorption device by adopting a first valve group, and communicating an air compressor with an outer pipe inlet of the second adsorption and desorption device;
3.3, communicating an outlet of an inner pipe of the first absorption and desorption device with a carbon dioxide collection tank by adopting a second valve group, and communicating an outlet of an inner pipe of the second absorption and desorption device with a flue gas analyzer;
3.4, communicating an outlet of the outer pipe of the second adsorption and desorption device with a gas discharge channel by adopting a third valve group, and communicating an outlet of the outer pipe of the first adsorption and desorption device with an inlet of the inner pipe of the second adsorption and desorption device by adopting the third valve group and a fourth valve group;
step 4, detecting and displaying the pressure of the flue gas in the flue gas exhaust pipeline by adopting a first pressure gauge, detecting and displaying the flow of the flue gas in the flue gas exhaust pipeline by adopting a first flowmeter, and detecting and displaying the temperature of the flue gas in the flue gas exhaust pipeline by adopting a first thermometer;
step 5, detecting and displaying the pressure of the air blown out by the air compressor by adopting a second pressure gauge, detecting and displaying the flow of the air blown out by the air compressor by adopting a second flowmeter, and detecting and displaying the temperature of the air blown out by the air compressor by adopting a second thermometer;
step 6, enabling the flue gas in the flue gas exhaust pipeline to enter an outer pipe of a first adsorption and desorption device, heating the inner pipe, desorbing the carbon dioxide in the inner pipe, enabling the desorbed carbon dioxide to enter a carbon dioxide collecting tank for collecting, and detecting and displaying the flow of the desorbed carbon dioxide by adopting a third flow meter;
step 7, allowing air cold air blown out by the air compressor to enter an outer pipe of the second adsorption and desorption device, cooling the inner pipe, and discharging the air subjected to heat exchange into the atmosphere from the gas discharge channel;
step 8, allowing the flue gas subjected to heat exchange in the outer pipe of the first adsorption and desorption device to enter an inner pipe of a second adsorption and desorption device for carbon dioxide adsorption, allowing the adsorbed flue gas to enter a flue gas analyzer for analysis, and detecting and displaying the temperature of the adsorbed flue gas by using a third thermometer;
step 9, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer is larger than or equal to a set threshold value, if so, finishing the carbon dioxide adsorption and desorption process, and executing step 10, otherwise, returning to execute step 3;
and step 10, according to the device communication mode in the step 2, communicating all devices of the system again through each valve group, so that the first adsorption and desorption device can adsorb carbon dioxide, and the second adsorption and desorption device can desorb carbon dioxide.
The invention has the advantages that:
the invention provides a carbon dioxide temperature swing adsorption and desorption system based on low-grade heat energy, which adopts recycled, economic and reliable zeolite 13X as an adsorbent, can synchronously carry out carbon dioxide adsorption and desorption processes while utilizing the low-grade heat energy, improves the heat exchange efficiency, and realizes the double-effect energy-saving effect of waste heat utilization and carbon dioxide capture; according to the invention, low-grade heat energy in the flue gas is used as an energy source, cyclic absorption and desorption are realized by combining physical temperature swing adsorption, the absorption and desorption efficiency is improved, the system operation time is saved, the six-component system energy consumption is reduced, the environmental pollution caused by the flue gas of a thermal power plant is reduced, and the capture concentration of carbon dioxide after three-step adsorption can reach ninety percent.
Drawings
Fig. 1 is a schematic structural diagram of a carbon dioxide temperature swing adsorption and desorption system based on low-grade thermal energy according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a first adsorption and desorption device according to an embodiment of the present invention;
FIG. 3 is a flow chart of a method of an adsorption and desorption method according to an embodiment of the present invention;
wherein, 1 is a flue gas exhaust pipeline, 2 is a first pressure gauge, 3 is a first temperature gauge, 4 is a first flow meter, 5 is a first valve group, 6 is a first valve, 7 is a second valve, 8 is a third valve, 9 is a fourth valve, 10 is a second valve group, 11 is a fifth valve, 12 is a sixth valve, 13 is a seventh valve, 14 is an eighth valve, 15 is a first adsorption and desorption device, 16 is a first outer pipe inlet, 17 is a first outer pipe outlet, 18 is a first inner pipe inlet, 19 is a first inner pipe outlet, 20 is a second adsorption and desorption device, 21 is a second outer pipe inlet, 22 is a second outer pipe outlet, 23 is a second inner pipe inlet, 24 is a second inner pipe outlet, 25 is a third valve group, 26 is a ninth valve, 27 is a tenth valve, 28 is an eleventh valve, 29 is a twelfth valve, 30 is a fourth valve group, 31 is a thirteenth valve, 32 is a fourteenth valve, 33 is a second flowmeter, 34 is a carbon dioxide collecting tank, 35 is a flue gas analyzer, 36 is an air compressor, 37 is a second pressure gauge, 38 is a second thermometer, 39 is a third flowmeter, 40 is a third thermometer, 41 is a fin, 42 is an outer tube, 43 is an inner tube, and 44 is a gas discharge passage.
Detailed Description
An embodiment of the present invention will be further described with reference to the accompanying drawings.
In the embodiment of the invention, a schematic structural diagram of a system of a carbon dioxide temperature-changing adsorption and desorption system based on low-grade heat energy is shown in fig. 1, and the system includes an air compressor 36, a flue gas analyzer 35, a carbon dioxide collection tank 34, an adsorption and desorption device, a first valve group 5, a second valve group 10, a first pressure gauge 2, a second pressure gauge 37, a first flowmeter 4, a second flowmeter 33, a third flowmeter 39, a first temperature gauge 3, a second temperature gauge 38 and a third temperature gauge 40;
in the embodiment of the present invention, the first valve group 5 includes four independent valves, which are respectively: a first valve 6, a second valve 7, a third valve 8 and a fourth valve 9, any two of which can be communicated with each other; the second valve group 10 comprises four independent valves, respectively: a fifth valve 11, a sixth valve 12, a seventh valve 13 and an eighth valve 14, any two of which can be in communication with each other;
in the embodiment of the present invention, as shown in fig. 1 and fig. 2, the adsorption and desorption devices include a first adsorption and desorption device 15, a second adsorption and desorption device 20, a third valve group 25, and a fourth valve group 30; the first adsorption and desorption device 15 and the second adsorption and desorption device 20 both comprise an inner tube 43, an outer tube 42, fins 41 and an adsorbent; wherein,
the third valve group 25 comprises 4 independent valves, respectively: a ninth valve 26, a tenth valve 27, an eleventh valve 28, and a twelfth valve 29, any two of which can communicate with each other; the fourth valve group comprises two independent valves which are respectively: a thirteenth valve 31 and a fourteenth valve 32, any two of which can communicate with each other;
the inner pipe 43 is arranged in the pipeline of the outer pipe, fins 41 are uniformly wound and welded on the outer wall of the inner pipe 43, and the inner part of the inner pipe 43 is filled with the adsorbent; the inner tube 43 and the outer tube 42 are both provided with an inlet and an outlet; the first outer pipe outlet 17 of the first adsorption-desorption device 15 is connected with the ninth valve 26 of the third valve set 25 through a pipeline, the second outer pipe outlet 22 of the second adsorption-desorption device 20 is connected with the tenth valve 27 of the third valve set 25 through a pipeline, the eleventh valve 28 of the third valve set 25 is connected with the inlet of the fourth valve set 30 through a pipeline, and the twelfth valve 29 of the third valve set 25 is connected with the gas discharge channel 44 through a pipeline; a thirteenth valve 31 of the fourth valve group 30 is connected with the first inner tube inlet 18 of the first adsorption and desorption device 15 through a pipeline, and a fourteenth valve 32 is connected with the second inner tube inlet 23 of the second adsorption and desorption device 20 through a pipeline; setting a first outer pipe inlet 16 of the first adsorption and desorption device 15 and a second outer pipe inlet 21 of the second adsorption and desorption device 20 as inlets of the adsorption and desorption devices, and setting a first inner pipe outlet 19 of the first adsorption and desorption device 15 and a second inner pipe outlet 24 of the second adsorption and desorption device 20 as outlets of the adsorption and desorption devices;
in the embodiment of the invention, the fins 41 on the outer wall of the inner tube 43 adopt high-frequency wound stainless steel fins with the fin height of 12.5mm, or high-frequency wound stainless steel finned tubes can be directly adopted, so that the heat exchange area can be increased compared with a single adsorption column; the specification of the inner tube is 32mm of inner diameter, 36.4mm of outer diameter and 2.2mm of wall thickness; the outer pipe is a common aluminum pipe with the inner diameter of 70mm and the outer diameter of 80mm, and the wall thickness is 5 mm; the first inner tube inlet 18, the first inner tube outlet 19, the second inner tube inlet 23, the second inner tube outlet 24, the first outer tube inlet 16, the first outer tube outlet 17, the second outer tube inlet 21 and the second outer tube outlet 22 are all 4 branched tubes with the inner diameter of 15mm, the outer diameter of 21.3mm and the wall thickness of 2.75 mm; the adsorbent adopts zeolite 13X molecular sieve;
in the embodiment of the present invention, as shown in fig. 1, the flue gas exhaust pipeline 1 of the thermal power plant is connected to the first valve 6 of the first valve group 5 through a pipeline, the exhaust outlet of the air compressor 36 is connected to the second valve 7 of the first valve group 5 through a pipeline, the third valve 8 of the first valve group 5 is connected to the first outer pipe inlet 16 of the first adsorption and desorption device 15 through a pipeline, the fourth valve 9 of the first valve group 5 is connected to the second outer pipe inlet 21 of the second adsorption and desorption device 20 through a pipeline, the first inner pipe outlet 19 of the first adsorption and desorption device 15 is connected to the fifth valve 11 of the second valve group 10 through a pipeline, the second inner pipe outlet 24 of the second adsorption and desorption device 20 is connected to the sixth valve 12 of the second valve group 10 through a pipeline, the seventh valve 13 of the second valve group 10 is connected to the carbon dioxide collection tank 34 through a pipeline, the eighth valve 14 of the second valve group 10 is connected to the flue gas analyzer 35 through a pipeline, the outlet of the flue gas analyzer 35 is provided as a gas discharge channel 44; the measuring probes of the first pressure gauge 2, the first flowmeter 4 and the first thermometer 3 are respectively arranged on the inner wall of the outlet of the flue gas exhaust pipeline 1 of the thermal power plant through a three-way valve, and the display screen is fixed on the outer wall; the measuring probes of the second pressure gauge 37, the second flowmeter 33 and the second thermometer 38 are respectively arranged on the inner wall of the exhaust outlet of the air compressor through a three-way valve, and the display screen is fixed on the outer wall; the measuring probes of the third flow meter 39 are respectively arranged on the inner wall of the inlet of the carbon dioxide collecting tank 34 through a three-way valve, and the display screen is fixed on the outer wall; a measuring probe of the third thermometer 40 is arranged on the inner wall of the inlet of the flue gas analyzer 35 through a three-way valve, and a display screen is fixed on the outer wall;
in the embodiment of the invention, each thermometer adopts a thermometer with the measuring range of 0-300 ℃; each flow meter adopts a flow meter with the measuring range of 0-20L/min; each pressure gauge adopts a pressure gauge with the measuring range of 0.6 MPa;
in the embodiment of the invention, the absorption and desorption method implemented by the carbon dioxide variable temperature absorption and desorption system based on low-grade heat energy has a flow chart as shown in fig. 3, and comprises the following steps:
step 1, setting a carbon dioxide content threshold value to be 15%;
step 2, communicating all devices of the system through each valve group, and adsorbing carbon dioxide by adopting a first adsorption and desorption device, wherein the method comprises the following specific steps:
step 2.1, connecting a first valve 6 and a fourth valve 9 of a first valve group 5 to enable a flue gas exhaust pipeline 1 to be communicated with a second outer pipe inlet 21, and connecting a second valve 7 and a third valve 8 to enable an air compressor 36 to be communicated with a first outer pipe inlet 16;
step 2.2, connecting the fifth valve 11 and the eighth valve 14 of the second valve group 10 to enable the first inner tube outlet 19 to be communicated with a flue gas analyzer 35, and connecting the sixth valve 12 and the seventh valve 13 to enable the second inner tube outlet 24 to be communicated with a carbon dioxide collecting tank 34;
step 2.3, connecting the ninth valve 26 and the twelfth valve 29 of the third valve group 25, connecting the first outer tube outlet 17 with the gas discharge channel, connecting the tenth valve 27 and the eleventh valve 28, connecting the inlet of the fourth valve group 30 with the thirteenth valve 31, and connecting the second outer tube outlet 22 with the first inner tube inlet 18;
step 2.4, enabling 100-200 ℃ flue gas discharged from the flue gas exhaust pipeline 1 of the thermal power plant to enter an inner pipe 43 of a first absorption and desorption device 15 through an outer pipe 42 of a second absorption and desorption device 20, performing carbon dioxide adsorption by adopting a zeolite 13X molecular sieve, and enabling the adsorbed flue gas to enter a flue gas analyzer 35;
in the embodiment of the invention, the flue gas is a mixed gas of 15% of carbon dioxide, 80% of nitrogen and 5% of other gases;
step 2.5, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer 35 is more than or equal to 15%, if so, finishing the carbon dioxide adsorption and desorption process, discharging the adsorbed and desorbed flue gas, and executing step 3, otherwise, returning to execute step 2.4;
step 3, setting the first adsorption and desorption device to perform carbon dioxide desorption, setting the second adsorption and desorption device to perform carbon dioxide adsorption, and communicating each device of the system again through each valve group, wherein the method comprises the following specific steps:
step 3.1, setting a first absorption and desorption device to perform carbon dioxide desorption, and setting a second absorption and desorption device to perform carbon dioxide absorption;
step 3.2, connecting the first valve 6 and the third valve 8 of the first valve group 5 to enable the flue gas exhaust pipeline 1 to be communicated with the first outer pipe inlet 16, and connecting the second valve 7 and the fourth valve 9 to enable the air compressor 36 to be communicated with the second outer pipe inlet 23;
step 3.3, connecting the fifth valve 11 and the seventh valve 13 of the second valve group 10 to communicate the first inner tube outlet 19 with the carbon dioxide collecting tank 34, and connecting the sixth valve 12 with the eighth valve 14 to communicate the second inner tube outlet 24 with the flue gas analyzer 35;
step 3.4, connecting the ninth valve 26 and the eleventh valve 28 of the third valve group 25, connecting the second outer tube outlet 22 with the gas discharge channel, connecting the tenth valve 27 and the twelfth valve 29, connecting the inlet of the fourth valve group 30 with the fourteenth valve 32, and connecting the first outer tube outlet 17 with the second inner tube inlet 23;
step 4, detecting and displaying the pressure of the flue gas in the flue gas exhaust pipeline 1 by using a first pressure gauge 2, detecting and displaying the flow of the flue gas in the flue gas exhaust pipeline 1 by using a first flowmeter 4, and detecting and displaying the temperature of the flue gas in the flue gas exhaust pipeline 1 by using a first thermometer 3;
step 5, detecting and displaying the pressure of the air blown out by the air compressor 36 by using a second pressure gauge 37, detecting and displaying the flow rate of the air blown out by the air compressor 36 by using a second flow meter 33, and detecting and displaying the temperature of the air blown out by the air compressor 36 by using a second temperature gauge 38;
step 6, enabling 100-200 ℃ flue gas discharged from the flue gas exhaust pipeline 1 of the thermal power plant to enter an outer pipe 42 of the first adsorption and desorption device 15, heating an inner pipe 43, desorbing carbon dioxide in the inner pipe 43, enabling the desorbed carbon dioxide to enter a carbon dioxide collection tank 34 for collection, and detecting and displaying the flow of the desorbed carbon dioxide by using a third flow meter 39;
step 7, the air cold air blown out by the air compressor 36 enters the outer pipe 42 of the second adsorption and desorption device 20, the inner pipe 43 is cooled, and the air after heat exchange is discharged into the atmosphere from the air discharge channel 44;
step 8, the flue gas after heat exchange in the outer tube 42 of the first adsorption and desorption device 15 enters the inner tube 43 of the second adsorption and desorption device 20 for carbon dioxide adsorption, the adsorbed flue gas enters the flue gas analyzer 35 for analysis, and the temperature of the adsorbed flue gas is detected and displayed by adopting the third thermometer 40;
step 9, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer 35 is greater than or equal to 15%, if so, finishing the carbon dioxide adsorption and desorption process, discharging the flue gas, and executing step 10, otherwise, returning to execute step 3;
and step 10, according to the device communication mode in the step 2, communicating all devices of the system again through each valve group, so that the first adsorption and desorption device can adsorb carbon dioxide, and the second adsorption and desorption device can desorb carbon dioxide.
Claims (6)
1. The utility model provides a desorption system is inhaled to carbon dioxide alternating temperature based on low-grade heat energy which characterized in that: the system comprises an air compressor, a flue gas analyzer, a carbon dioxide collecting tank, an absorption and desorption device, a first valve group, a second valve group, two pressure gauges, three flow meters and three thermometers;
the air compressor and the flue gas exhaust pipeline of the thermal power plant are respectively connected with a first valve group through pipelines, and the first valve group is connected with an inlet of the adsorption and desorption device through a pipeline; the outlet of the adsorption and desorption device is connected with a second valve group through a pipeline, and the second valve group is respectively connected with a carbon dioxide collecting tank and a flue gas analyzer through pipelines; setting an outlet of a flue gas analyzer as a gas discharge channel; the first pressure gauge, the first flowmeter and the first thermometer are installed at an outlet of a flue gas exhaust pipeline of a thermal power plant, the second pressure gauge, the second flowmeter and the second thermometer are installed at an exhaust outlet of an air compressor, the third flowmeter is installed at an inlet of a carbon dioxide collecting tank, and the third thermometer is installed at an inlet of a flue gas analyzer;
the adsorption and desorption device comprises a first adsorption and desorption device, a second adsorption and desorption device, a third valve group and a fourth valve group; the first adsorption and desorption device and the second adsorption and desorption device respectively comprise an inner tube, a fin, an adsorbent and an outer tube; the inner pipe is arranged in the pipeline of the outer pipe, fins are wound on the outer wall of the inner pipe, and the inner part of the inner pipe is filled with the adsorbent; the inner pipe and the outer pipe are both provided with an inlet and an outlet; the outlet of the outer pipe of the first adsorption and desorption device and the outlet of the outer pipe of the second adsorption and desorption device are respectively connected with a third valve group through pipelines, the third valve group is respectively connected with a gas discharge channel and a fourth valve group through pipelines, and the fourth valve group is respectively connected with the inlet of the inner pipe of the first adsorption and desorption device and the inlet of the inner pipe of the second adsorption and desorption device through pipelines; the outer tube inlet of the first adsorption and desorption device and the outer tube inlet of the second adsorption and desorption device are arranged as the inlets of the adsorption and desorption devices, and the inner tube outlet of the first adsorption and desorption device and the inner tube outlet of the second adsorption and desorption device are arranged as the outlets of the adsorption and desorption devices.
2. The carbon dioxide temperature swing adsorption and desorption system based on low-grade heat energy according to claim 1, characterized in that: the adsorbent adopts zeolite 13X molecular sieve.
3. The carbon dioxide temperature swing adsorption and desorption system based on low-grade heat energy according to claim 1, characterized in that: the fins are high-frequency winding fin.
4. The carbon dioxide temperature swing adsorption and desorption system based on low-grade heat energy according to claim 1, characterized in that: the number of the valves of the first valve group, the second valve group, the third valve group and the fourth valve group is more than or equal to the number of the pipelines connected with the valve groups.
5. The carbon dioxide temperature swing adsorption and desorption system based on low-grade heat energy according to claim 1, characterized in that: each valve of the first valve group, the second valve group, the third valve group and the fourth valve group is independent.
6. The absorption and desorption method by using the low-grade heat energy-based carbon dioxide temperature-variable absorption and desorption system according to claim 1 is characterized in that: the method comprises the following steps:
step 1, setting a carbon dioxide content threshold;
step 2, communicating all devices of the system through each valve group, and adsorbing carbon dioxide by adopting a first adsorption and desorption device, wherein the method comprises the following specific steps:
2.1, communicating a flue gas exhaust pipeline with an outer pipe inlet of a second adsorption and desorption device by adopting a first valve group, and communicating an air compressor with an outer pipe inlet of a first adsorption and desorption device;
2.2, communicating an outlet of an inner pipe of the first absorption and desorption device with a flue gas analyzer by adopting a second valve group; an outlet of an inner pipe of the second adsorption and desorption device is communicated with a carbon dioxide collecting tank;
2.3, communicating an outlet of an outer pipe of the first adsorption and desorption device with a gas discharge channel by adopting a third valve group, and communicating an outlet of an outer pipe of the second adsorption and desorption device with an inlet of an inner pipe of the first adsorption and desorption device by adopting the third valve group and a fourth valve group;
2.4, enabling the flue gas in the flue gas exhaust pipeline to enter an inner pipe of a first absorption and desorption device through an outer pipe of a second absorption and desorption device, adsorbing the flue gas with carbon dioxide by adopting an adsorbent, and enabling the adsorbed flue gas to enter a flue gas analyzer;
step 2.5, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer is larger than or equal to a set threshold value, if so, discharging the flue gas, and executing the step 3, otherwise, returning to execute the step 2.4;
step 3, setting the first adsorption and desorption device to perform carbon dioxide desorption, setting the second adsorption and desorption device to perform carbon dioxide adsorption, and communicating each device of the system again through each valve group, wherein the method comprises the following specific steps:
step 3.1, setting a first absorption and desorption device to perform carbon dioxide desorption, and setting a second absorption and desorption device to perform carbon dioxide absorption;
3.2, communicating a flue gas exhaust pipeline with an outer pipe inlet of the first adsorption and desorption device by adopting a first valve group, and communicating an air compressor with an outer pipe inlet of the second adsorption and desorption device;
3.3, communicating an outlet of an inner pipe of the first absorption and desorption device with a carbon dioxide collection tank by adopting a second valve group, and communicating an outlet of an inner pipe of the second absorption and desorption device with a flue gas analyzer;
3.4, communicating an outlet of the outer pipe of the second adsorption and desorption device with a gas discharge channel by adopting a third valve group, and communicating an outlet of the outer pipe of the first adsorption and desorption device with an inlet of the inner pipe of the second adsorption and desorption device by adopting the third valve group and a fourth valve group;
step 4, detecting and displaying the pressure of the flue gas in the flue gas exhaust pipeline by adopting a first pressure gauge, detecting and displaying the flow of the flue gas in the flue gas exhaust pipeline by adopting a first flowmeter, and detecting and displaying the temperature of the flue gas in the flue gas exhaust pipeline by adopting a first thermometer;
step 5, detecting and displaying the pressure of the air blown out by the air compressor by adopting a second pressure gauge, detecting and displaying the flow of the air blown out by the air compressor by adopting a second flowmeter, and detecting and displaying the temperature of the air blown out by the air compressor by adopting a second thermometer;
step 6, enabling the flue gas in the flue gas exhaust pipeline to enter an outer pipe of a first adsorption and desorption device, heating the inner pipe, desorbing the carbon dioxide in the inner pipe, enabling the desorbed carbon dioxide to enter a carbon dioxide collecting tank for collecting, and detecting and displaying the flow of the desorbed carbon dioxide by adopting a third flow meter;
step 7, allowing air cold air blown out by the air compressor to enter an outer pipe of the second adsorption and desorption device, cooling the inner pipe, and discharging the air subjected to heat exchange into the atmosphere from the gas discharge channel;
step 8, allowing the flue gas subjected to heat exchange in the outer pipe of the first adsorption and desorption device to enter an inner pipe of a second adsorption and desorption device for carbon dioxide adsorption, allowing the adsorbed flue gas to enter a flue gas analyzer for analysis, and detecting and displaying the temperature of the adsorbed flue gas by using a third thermometer;
step 9, judging whether the carbon dioxide content of the flue gas in the flue gas analyzer is larger than or equal to a set threshold value, if so, finishing the carbon dioxide adsorption and desorption process, and executing step 10, otherwise, returning to execute step 3;
and step 10, according to the device communication mode in the step 2, communicating all devices of the system again through each valve group, so that the first adsorption and desorption device can adsorb carbon dioxide, and the second adsorption and desorption device can desorb carbon dioxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610264710.4A CN105749696B (en) | 2016-04-25 | 2016-04-25 | A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610264710.4A CN105749696B (en) | 2016-04-25 | 2016-04-25 | A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105749696A CN105749696A (en) | 2016-07-13 |
| CN105749696B true CN105749696B (en) | 2018-05-04 |
Family
ID=56325896
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610264710.4A Active CN105749696B (en) | 2016-04-25 | 2016-04-25 | A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105749696B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582200B (en) * | 2017-01-25 | 2022-07-29 | 天津大学 | Temperature swing adsorption power plant flue gas carbon capture system utilizing middle extraction |
| CN106582201A (en) * | 2017-01-25 | 2017-04-26 | 天津大学 | Carbon dioxide capturing compression system using flue gas and multistage compressing waste heat |
| CN106823684B (en) * | 2017-03-30 | 2019-07-05 | 东北大学 | The temperature swing adsorption system and method for carbon dioxide in energy-saving separation industrial smoke |
| CN115077130B (en) * | 2022-05-31 | 2023-03-10 | 上海交通大学 | Double-heat-source heat pump type air carbon direct trapping system |
| CN115055028B (en) * | 2022-08-08 | 2022-11-29 | 中国华能集团清洁能源技术研究院有限公司 | Carbon capture system and method |
| CN118281257B (en) * | 2024-06-03 | 2024-09-13 | 北京科技大学 | Low-concentration gas enrichment solid oxide fuel cell power generation system |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS522867A (en) * | 1975-06-24 | 1977-01-10 | Taikisha Ltd | Exhaust gas treatment apparatus for organic gases |
| JP4496208B2 (en) * | 2006-09-27 | 2010-07-07 | 株式会社東芝 | Carbon dioxide absorbent, carbon dioxide separator and reformer |
| CN102101003B (en) * | 2011-01-28 | 2013-11-13 | 西安超滤净化工程有限公司 | Process and device for drying adsorption type compressed gas regenerated by using compression heat |
| CN102743957A (en) * | 2011-04-22 | 2012-10-24 | 李劲松 | High temperature oil-containing compressed air waste heat regeneration drying device |
| JP5776672B2 (en) * | 2012-11-29 | 2015-09-09 | 栗田工業株式会社 | Activated carbon cartridge and gas purification device |
| CN103272455B (en) * | 2013-06-14 | 2015-02-04 | 泉州市天龙环境工程有限公司 | Device and method for recycling organic solvents from painting waste gas |
| CN204051371U (en) * | 2014-05-31 | 2014-12-31 | 蔡博 | A kind of purification recovery device of volatile organic waste gas |
| CN205700031U (en) * | 2016-04-25 | 2016-11-23 | 东北大学 | A kind of carbon dioxide alternating temperature adsorption desorption system based on low grade heat energy |
-
2016
- 2016-04-25 CN CN201610264710.4A patent/CN105749696B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN105749696A (en) | 2016-07-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105749696B (en) | A kind of carbon dioxide alternating temperature adsorption desorption system and method based on low grade heat energy | |
| CN102039083B (en) | Isotonic purifying and drying system without resurgent gas loss and technological process thereof | |
| CN103254955B (en) | Closed-type three-tower molecular sieve dehydration device | |
| CN107741103B (en) | Ammonia water absorption type refrigeration combined carbon trapping device | |
| CN113477051B (en) | Device and method for continuously capturing CO2 by double-bed hydrate method | |
| CN108211671B (en) | Energy-saving carbon dioxide regeneration and compression system and method | |
| CN103409188B (en) | Process unit and method for removing heavy hydrocarbon during liquefaction process of natural gas | |
| CN103274359A (en) | Method and device for recycling hydrogen from synthesis ammonia released air and preparing LNG (liquefied natural gas) with membrane separation and cryogenic integration technology | |
| Wu et al. | Preliminary experimental study on the performance of CO2 capture prototype based on temperature swing adsorption (TSA) | |
| CN108641765A (en) | Remove the process system and method for carbon dioxide in natural | |
| CN201776068U (en) | Isopiestic pressure purification drying system with no regeneration gas loss | |
| CN206492366U (en) | The compact ammonia process carbon trapping system of ammoniacal liquor second-kind absorption-type heat pump driving | |
| CN107138024B (en) | Integrated particle fluidized carbon dioxide capture method and apparatus for power plants | |
| CN205700031U (en) | A kind of carbon dioxide alternating temperature adsorption desorption system based on low grade heat energy | |
| CN202785638U (en) | Device for purifying ordinary hydrogen to be high-purity hydrogen | |
| CN204347000U (en) | Variable working condition thick slurry type carbon dioxide capture process testing device | |
| CN203443264U (en) | Device for extracting methane liquid from purified garbage landfill gas | |
| CN207300605U (en) | A kind of device of definite space division purification system regeneration period | |
| CN103353207B (en) | Device for purifying methane liquid from purified landfill gas | |
| CN203379780U (en) | Multi-tower type temperature swing adsorption concentration device of ventilation air marsh gas | |
| CN205482015U (en) | Natural gas liquefaction system | |
| CN210892361U (en) | Device for preparing liquid carbon dioxide by utilizing surplus cold energy for refrigeration | |
| CN112439398B (en) | Method and device for regenerating gas adsorption column and tail gas recovery system | |
| CN203971683U (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN203247242U (en) | Closed three-tower molecular sieve dehydration device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |