CN115634550A - Carbon dioxide adsorption rotating wheel system and method thereof - Google Patents

Carbon dioxide adsorption rotating wheel system and method thereof Download PDF

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Publication number
CN115634550A
CN115634550A CN202111010888.3A CN202111010888A CN115634550A CN 115634550 A CN115634550 A CN 115634550A CN 202111010888 A CN202111010888 A CN 202111010888A CN 115634550 A CN115634550 A CN 115634550A
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China
Prior art keywords
pipeline
gas
carbon dioxide
desorption
tubular membrane
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郑石治
扶亚民
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Shanghai Huamao Environmental Protection Energy Saving Equipment Co ltd
Desiccant Technology Corp
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Shanghai Huamao Environmental Protection Energy Saving Equipment Co ltd
Desiccant Technology Corp
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Abstract

The invention relates to a carbon dioxide adsorption rotating wheel system and a method thereof, which are mainly used for a carbon dioxide treatment system and are provided with pretreatment equipment, a first carbon dioxide adsorption rotating wheel, a first heating device, a second carbon dioxide adsorption rotating wheel, a second heating device and a chimney.

Description

Carbon dioxide adsorption rotating wheel system and method thereof
Technical Field
The present invention relates to a carbon dioxide adsorption rotating wheel system and a method thereof, and more particularly, to a carbon dioxide treatment system or the like which can increase the concentration efficiency of carbon dioxide and has the effect of concentrating and recovering carbon dioxide and is suitable for the semiconductor industry, the photoelectric industry, the chemical industry, or the manufacturing industry.
Background
In recent years, environmental protection is becoming a concern of every country around the world, especially a part of greenhouse gases, and the largest part of greenhouse gases is carbon dioxide CO emission 2 Content of carbon dioxide CO 2 Is a common compound in air and is formed by connecting two oxygen atoms and one carbon atom through a polar covalent bond.
Since the industrial revolution, the excessive greenhouse gas generated by the activities of mankind, which have been developing a great amount of fossil fuels (such as coal and oil) for industrial and civilized development and increasing the farming area by cutting down tropical rainforests continuously, greatly enhances the greenhouse effect, destroys the energy balance state for a long period of time, and consequently causes the rise of the surface temperature of the earth, resulting in global warming.
In order to cope with the influence of global warming, united in 1992 in new york through the united nations climate change agency convention (unccc), it is expected that the concentration of greenhouse gases in the atmosphere can be stabilized through the efforts of each country, so that the human can develop economy and civilization and protect the global ecosystem from threats. Then, a number of climate change meetings are held by the united nations, targeting the climate change treaty convention in the following protocols: 1. the kyoto protocol, 2, paris protocol. In addition, european Union 2019 announced European Green politics, and it was proposed that the global temperature rise could be controlled within 1.5 ℃ before the end of this century by aiming to achieve "carbon neutralization" with balanced increase and decrease of carbon emission in 2050.
In recent years, people pay more attention to air pollution, and therefore, relevant atmospheric quality standards are set on emission standards of chimneys, and the air pollution is developed and examined on a periodic basis according to the international regulatory trend.
Therefore, in view of the above-mentioned disadvantages, it is desirable to provide a carbon dioxide adsorbing rotor system and a method thereof capable of concentrating and recovering carbon dioxide, which can be easily assembled by a user, and is a research and design system for providing convenience to the user.
Disclosure of Invention
The main object of the present invention is to provide a carbon dioxide adsorption rotating wheel system and a method thereof, which is mainly used for a carbon dioxide treatment system, and is provided with a pretreatment device, a first carbon dioxide adsorption rotating wheel, a first heating device, a second carbon dioxide adsorption rotating wheel, a second heating device and a chimney, wherein two carbon dioxide adsorption rotating wheels are connected in series, and a gas obtained by a first desorption and concentration of carbon dioxide generated in a desorption region of the first carbon dioxide adsorption rotating wheel is transported to an adsorption region of the second carbon dioxide adsorption rotating wheel for a second adsorption, and a second desorption and concentration of carbon dioxide generated in a desorption region of the second carbon dioxide adsorption rotating wheel is used for a second desorption and concentration, so that the carbon dioxide concentration efficiency can be increased, the carbon dioxide concentration and recovery efficiency can be achieved, and the overall practicability can be increased.
Another objective of the present invention is to provide a carbon dioxide adsorbing rotating wheel system and a method thereof, wherein the other end of the second desorbing gas pipeline of the second carbon dioxide adsorbing rotating wheel is connected to a twin-tower type polymer tubular membrane device, so that the gas obtained after the second desorbing and concentrating of the carbon dioxide can be recompressed by the twin-tower type polymer tubular membrane device to form a carbon dioxide compressed and dried gas, and the recompressed carbon dioxide compressed and dried gas can be stored by a steel cylinder or a steel tank or delivered to other places requiring carbon dioxide, such as greenhouses or seaweed farms, soda water coke plants, chemical plants, or food industry plants, etc., as a raw material, so that the carbon dioxide compressed and dried gas can have the effect of subsequent application, thereby increasing the overall usability.
The present invention further provides a carbon dioxide adsorbing rotating wheel system and a method thereof, wherein the second desorption gas pipeline is connected to a recycling pipeline, one end of the recycling pipeline is connected to the second desorption gas pipeline, and the other end of the recycling pipeline is connected to the second heating gas inlet pipeline, so that the gas desorbed and concentrated by the carbon dioxide desorbed and secondarily desorbed can be returned to the second heating gas inlet pipeline via the recycling pipeline for mixing, heated again by the second heating device, and then conveyed to the desorption region of the second carbon dioxide adsorbing rotating wheel for desorption, such that the present invention has a continuous recycling efficiency, and the desorption concentration of the carbon dioxide can be increased from 6% of the inlet concentration to 40% -99% of the desorbed concentration, thereby increasing the overall operability.
For a better understanding of the nature, features and aspects of the present invention, reference should be made to the following detailed description of the invention, taken in conjunction with the accompanying drawings which are provided for purposes of illustration and description only and are not intended to be limiting.
Drawings
Fig. 1 is a system architecture diagram according to a main embodiment of the present invention.
Fig. 2 is a schematic diagram of a first variation system architecture according to the main embodiment of the present invention.
Fig. 3 is a schematic diagram of a second variation system architecture according to the main embodiment of the present invention.
Fig. 4 is a schematic diagram of a third system architecture according to a main embodiment of the present invention.
FIG. 5 is a system architecture diagram according to another embodiment of the present invention.
Fig. 6 is a schematic diagram of a first variant system architecture according to another embodiment of the present invention.
Fig. 7 is a schematic diagram of a second variant system architecture according to another embodiment of the present invention.
Fig. 8 is a schematic diagram of a first modified system according to another embodiment of the invention.
Fig. 9 is a schematic diagram of a system architecture of a third variation of the second embodiment of the present invention.
Fig. 10 is a schematic diagram of a fourth variant system architecture according to another embodiment of the present invention.
Fig. 11 is a schematic diagram of a fifth modified first modified system architecture according to another embodiment of the invention.
Fig. 12 is a schematic diagram of a system architecture of a fifth variation of the second embodiment of the present invention.
Fig. 13 is a schematic diagram of a sixth variant system architecture according to another embodiment of the present invention.
Fig. 14 is a schematic diagram of a system architecture of a seventh variation of the first embodiment of the present invention.
Fig. 15 is a schematic diagram of a system architecture of a seventh variation of the present invention.
Fig. 16 is a schematic diagram of an eighth variation system according to another embodiment of the present invention.
Fig. 17 is a schematic diagram of a system architecture of a ninth variation of the present invention.
Fig. 18 is a schematic diagram of a system architecture of a ninth variation according to another embodiment of the present invention.
FIG. 19 is a flow chart of the main steps of the present invention.
FIG. 20 is a flowchart illustrating another step of the present invention.
Description of the symbols:
10. pretreatment device 11 and gas inlet pipeline
20. First carbon dioxide adsorption rotating wheel 201 and adsorption area
202. Desorption zone 21, pre-treatment gas pipeline
211. Fan 22, first clean gas discharge line
221. Fan 23 and first hot gas conveying pipeline
24. First desorption gas pipeline 241 and fan
30. First heating device 31, first heating air inlet pipeline
311. Fan 40 and second carbon dioxide adsorption rotating wheel
401. Adsorption zone 402, desorption zone
41. Second purified gas discharge pipeline 411 and fan
42. Second hot gas conveying pipeline 43 and second desorption gas pipeline
431. Fan 432 and first fan
432. Second fan 44, recirculation line
441. Valve 50, second heating device
51. Second heating air inlet pipeline 511 and fan
60. Chimney 70, double tower type polymer tubular membrane equipment
71. First tower polymer tubular membrane group 711 and first adsorption tower
712. First air inlet pipeline 7121 and valve
713. First exhaust pipeline 7131 and valve
714. First regeneration pipeline 7141 and valve
715. First compressed gas pipeline 7151 and valve
72. Second tower polymer tubular membrane group 721, second adsorption tower
722. Second air inlet pipeline 7221 and valve
723. Second exhaust pipeline 7231 and valve
724. Second regeneration pipeline 7241, valve
725. First compressed gas pipeline 7251 and valve
73. Exhaust line 74, hot gas line
75. Compressed gas output line 76, primary heater
77. Second heater 78, heater
80. Cooling device 90 and heat exchanger
901. Cold side pipe 902, hot side pipe
S100, gas input pretreatment equipment
S110, adsorbing by a first carbon dioxide adsorption rotating wheel
S120, discharging the first carbon dioxide by using a first carbon dioxide adsorption runner
S130, conveying first hot gas for desorption
S140, outputting the gas after the desorption and concentration of the carbon dioxide
S150, adsorbing by a second carbon dioxide adsorption rotating wheel
S160, discharging the second carbon dioxide by the adsorption runner
S170, conveying second hot gas for desorption
S180, outputting the gas obtained after the desorption and concentration of the carbon dioxide
S200, conveying to double-tower type polymer tubular membrane equipment
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the accompanying drawings in combination with the embodiments.
Referring to fig. 1 to 20, there are shown schematic views of embodiments of the present invention, and a preferred embodiment of the carbon dioxide adsorption rotating wheel system and the method thereof is applied to a carbon dioxide treatment system or the like in the semiconductor industry, the photovoltaic industry, the chemical industry or the manufacturing industry, and mainly can increase the concentration efficiency of carbon dioxide and has the effect of concentrating and recovering carbon dioxide.
The present invention relates to a carbon dioxide adsorbing rotor system, which mainly comprises a pretreatment apparatus 10, a first carbon dioxide adsorbing rotor 20, a first heating device 30, a second carbon dioxide adsorbing rotor 40, a second heating device 50 and a chimney 60 (as shown in fig. 1 to 18), wherein one side of the pretreatment apparatus 10 is connected to a gas inlet pipeline 11, one end of the gas inlet pipeline 11 is connected to a place where carbon dioxide is generated or a region (not shown) where carbon dioxide is generated in a room, such as a production place, an office building, etc., so that the gas inlet pipeline 11 can deliver gas containing carbon dioxide or other gases, and the pretreatment apparatus 10 is any one of a cooler, a condenser, a dehumidifier and a cooler, so as to pretreat the gas and release heat energy to improve the adsorption efficiency. The first heating device 30 is provided with a first heating air inlet pipeline 31, the second heating device 50 is provided with a second heating air inlet pipeline 51, and the first heating device 30 and the second heating device 50 are any one of an electric heater, a natural gas heater, a heat exchanger, a heat transfer oil heat exchanger, a shell and tube heat exchanger, a fin tube heat exchanger, a plate heat exchanger or a heat pipe heat exchanger.
In addition, the first carbon dioxide adsorbing rotor 20 of the present invention is provided with an adsorbing region 201 and a desorbing region 202, the first carbon dioxide adsorbing rotor 20 is connected to a pretreating gas pipeline 21, a first clean gas discharging pipeline 22, a first hot gas conveying pipeline 23 and a first desorbing gas pipeline 24 (as shown in fig. 1 to 18), the second carbon dioxide adsorbing rotor 40 is provided with an adsorbing region 401 and a desorbing region 402, and the second carbon dioxide adsorbing rotor 40 is connected to a second clean gas discharging pipeline 41, a second hot gas conveying pipeline 42 and a second desorbing gas pipeline 43 (as shown in fig. 1 to 18). Wherein the first carbon dioxide adsorbing rotating wheel 20 and the second carbon dioxide adsorbing rotating wheel 40 are zeolite concentrating rotating wheels or concentrating rotating wheels made of other materials, respectively.
One end of the pretreatment gas line 21 is connected to the other side of the pretreatment device 10, and the other end of the pretreatment gas line 21 is connected to one side of the adsorption region 201 of the first carbon dioxide adsorption rotor 20, so that the gas containing carbon dioxide or other gases pretreated by the pretreatment device 10 can be transported to the adsorption region 201 of the first carbon dioxide adsorption rotor 20 through the pretreatment gas line 21 for carbon dioxide adsorption (as shown in fig. 1 to 4). The pre-processing gas pipeline 21 is provided with a blower 211 (as shown in fig. 3 and fig. 4), so that the blower 211 can push and pull the pre-processed gas containing carbon dioxide or other gases in the pre-processing gas pipeline 21 into the adsorption region 201 of the first carbon dioxide adsorption rotor 20. In addition, one end of the first purified gas discharge pipeline 22 is connected to the other side of the adsorption region 201 of the first carbon dioxide adsorption rotor 20, and the other end of the first purified gas discharge pipeline 22 is connected to the chimney 60 (as shown in fig. 1 to 4), so that the gas generated after the carbon dioxide is adsorbed by the adsorption region 201 of the first carbon dioxide adsorption rotor 20 can be transported to the chimney 60 through the first purified gas discharge pipeline 22 to be discharged to the atmosphere. The first clean gas discharging pipeline 22 is provided with a fan 221 (as shown in fig. 3 and fig. 4), so that the fan 221 can push and pull the gas after carbon dioxide adsorption in the first clean gas discharging pipeline 22 to the chimney 60 for discharging.
In addition, the other side of the desorption region 202 of the first carbon dioxide adsorbing rotor 20 is connected to one end of the first hot gas conveying pipeline 23, and the other end of the first hot gas conveying pipeline 23 is connected to the first heating device 30 (as shown in fig. 1 to 4), and the first heating device 30 inputs outside air or gas from other sources through the first heating air inlet pipeline 31, so that the first heating device 30 can heat the outside air or gas from other sources input through the first heating air inlet pipeline 31 to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is conveyed to the desorption region 202 of the first carbon dioxide adsorbing rotor 20 through the first hot gas conveying pipeline 23 for desorption. The first heating intake pipe 31 is provided with a blower 311 (as shown in fig. 3 and 4), so that the blower 311 can push and pull the external air or other source gas in the first heating intake pipe 31 into the first heating device 30.
One side of the desorption region 202 of the first carbon dioxide adsorption rotor 20 is connected to one end of the first desorption gas pipeline 24, and the other end of the first desorption gas pipeline 24 is connected to one side of the adsorption region 401 of the second carbon dioxide adsorption rotor 40 (as shown in fig. 1 to 4), so that the gas, which is desorbed and concentrated by the carbon dioxide generated by the desorption region 202 of the first carbon dioxide adsorption rotor 20 and is desorbed once, can be transported to the adsorption region 401 of the second carbon dioxide adsorption rotor 40 through the first desorption gas pipeline 24 for re-adsorption. The first desorption gas pipeline 24 is provided with a fan 241 (as shown in fig. 3 and 4), so that the fan 241 can push the concentrated gas desorbed from the carbon dioxide desorbed from the first desorption gas pipeline 24 to the adsorption region 401 of the second carbon dioxide adsorption rotor 40.
The other side of the adsorption region 401 of the second carbon dioxide adsorption rotor 40 is connected to the second purified gas discharge pipeline 41, and the other end of the second purified gas discharge pipeline 41 is connected to the chimney 60 (as shown in fig. 1 to 4), so that the gas generated after the carbon dioxide is re-adsorbed by the adsorption region 401 of the second carbon dioxide adsorption rotor 40 can be transported to the chimney 60 through the second purified gas discharge pipeline 41 to be discharged to the atmosphere. The second purified gas discharging pipeline 41 is provided with a fan 411 (as shown in fig. 3 and fig. 4), so that the fan 411 can push and pull the gas after carbon dioxide adsorption in the second purified gas discharging pipeline 41 to the chimney 60 for discharging.
In addition, the other side of the desorption region 402 of the second carbon dioxide adsorbing wheel 40 is connected to one end of the second hot gas conveying pipeline 42, and the other end of the second hot gas conveying pipeline 42 is connected to the second heating device 50 (as shown in fig. 1 to 4), and the second heating device 50 inputs outside air or gas from other sources through the second heating air inlet pipeline 51, so that the second heating device 50 can heat the outside air or gas from other sources input through the second heating air inlet pipeline 51 to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 is conveyed to the desorption region 402 of the second carbon dioxide adsorbing wheel 40 through the second hot gas conveying pipeline 42 for desorption. The second heating air intake pipeline 51 is provided with a blower 511 (as shown in fig. 4), so that the outside air or other source gas in the second heating air intake pipeline 51 can be pushed into the second heating device 50 by the blower 511.
One side of the desorption region 402 of the second carbon dioxide adsorbing rotor 40 is connected to one end of the second desorption gas pipeline 43 (as shown in fig. 1 to 4), so that the gas desorbed and concentrated by the carbon dioxide desorbed from the desorption region 402 of the second carbon dioxide adsorbing rotor 40 for the second desorption can be outputted through the second desorption gas pipeline 43 for the subsequent treatment. The post-treatment (not shown) includes storing the gas desorbed and concentrated by the second desorbed carbon dioxide delivered from the second desorption gas pipeline 43 through a steel cylinder or a steel tank, or delivering and supplying the gas to other places requiring carbon dioxide, such as greenhouses or seaweed farms, soda-water coke farms, chemical plants, or food factories, as a raw material, so that the gas desorbed and concentrated by the second desorbed carbon dioxide can have the effect of post-application. The second desorption gas pipeline 43 is provided with a blower 431 (as shown in fig. 3 and 4), so that the blower 431 can push and pull the gas obtained after the desorption and concentration of the carbon dioxide desorbed secondarily in the second desorption gas pipeline 43.
In addition, the first variation of the main embodiment of the present invention is based on the design of the main pretreatment device 10, the first carbon dioxide adsorption rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating device 50, and the stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, the first variation (as shown in fig. 2) of the main embodiment is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed twice desorbed and conveyed by the second desorption gas pipeline 43 can be returned to the second heating intake pipeline 51 through the recirculation pipeline 44, and then mixed with the outside air or other source gas in the second heating intake pipeline 51 and then enter the second heating device 50, or the gas alone in the second heating intake pipeline 51 is not mixed with the outside air or other source gas. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In addition, the second variation of the main embodiment of the present invention is based on the design of the main pretreatment device 10, the first carbon dioxide adsorption rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating device 50, and the stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, a second variation (as shown in fig. 3) of the main embodiment is that the second desorption gas pipeline 43 is further provided with a recirculation pipeline 44 (please refer to the content of the first variation of the main embodiment, which is not repeated here), and the difference from the first variation of the main embodiment is that the front end and the rear end of the second desorption gas pipeline 43 at the connection of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433, and the recirculation pipeline 44 is matched to form a positive pressure type, so that the gas after the second desorption and concentration of the carbon dioxide in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and then returned to the second heating gas inlet pipeline 51. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In addition, the third variation of the main embodiment of the present invention is based on the design of the main pretreatment device 10, the first carbon dioxide adsorption rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating device 50, and the stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, a third variation (as shown in fig. 4) of the main embodiment is that the second desorption gas pipeline 43 is further provided with a recirculation pipeline 44 (please refer to the content of the first variation of the main embodiment, which is not repeated here), and the difference from the first variation of the main embodiment is that the second desorption gas pipeline 43 is provided with a blower 431, the second heating gas inlet pipeline 51 is provided with a blower 511, and the blower 511 provided on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and near the second heating device 50, and the blower 431 provided on the second desorption gas pipeline 43 is further matched to form a negative pressure type, so that the gas after the carbon dioxide desorbed and concentrated in the second desorption gas pipeline 43 is returned to the second heating gas inlet pipeline 51 through the recirculation pipeline 44. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
Further, another embodiment of the present invention is based on the design of the pretreatment device 10, the first carbon dioxide adsorption rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating device 50, and a stack 60 according to the main embodiment, and the related contents thereof are described and will not be repeated here. Therefore, another embodiment of the present invention mainly includes that the other end of the second desorption gas pipeline 43 is connected to a twin-tower polymer tubular membrane apparatus 70 (as shown in fig. 5 and 6), so that the gas obtained after the desorption and concentration of the carbon dioxide desorbed in the second desorption gas pipeline 43 for the second time can be recompressed by the twin-tower polymer tubular membrane apparatus 70 to form the carbon dioxide compressed dry gas.
In another embodiment of the present invention, the dual-tower polymer tubular membrane apparatus 70 comprises a first tower polymer tubular membrane module 71 and a second tower polymer tubular membrane module 72, the first tower polymer tubular membrane module 71 comprises a first adsorption tower 711, a first air inlet pipeline 712, a first air outlet pipeline 713, a first regeneration pipeline 714 and a first compressed gas pipeline 715 (as shown in fig. 5 and 6), the second tower polymer tubular membrane module 72 comprises a second adsorption tower 721, a second air inlet pipeline 722, a second air outlet pipeline 723, a second regeneration pipeline 724 and a second compressed gas pipeline 725 (as shown in fig. 5 and 6), the first air inlet pipeline 712, the first air outlet pipeline 713, the first regeneration pipeline 714 and the first compressed gas pipeline 725 of the first tower polymer tubular membrane module 71 comprise a valve 7121, a valve 7131, a valve 71722, a valve 7151 (as shown in fig. 5 and 6), the second air inlet pipeline 7221, the valve 723, the second compressed gas pipeline 7251 of the second tower polymer tubular membrane module 72 are respectively arranged to control the flow direction of the first and the second compressed gas pipelines 7221, the second compressed gas pipeline 7251 and the valves 7221, the second compressed gas pipeline 7221, the exhaust pipeline 724 and the valves 7251 (as shown in fig. 5 and fig. 6).
The first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 and the second adsorption tower 721 of the second tower-type polymer tubular membrane group 72 are filled with a plurality of hollow tubular polymer tubular membrane adsorbing materials (as shown in fig. 5 and 6), and the hollow tubular polymer tubular membrane adsorbing materials are made of a polymer and an adsorbent, and the polymer is made of at least one of Polysulfone (PSF), polyethersulfone (PESF), polyvinylidene fluoride (PVDF), polyphenylsulfone (PPSU), polyacrylonitrile (polyacrylonitrile), cellulose acetate, cellulose diacetate, polyimide (PI), polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-glycolic acid (polylactic-co-glycolic acid), polycaprolactone, polyvinylpyrrolidone (polyvinyl pyrrolidone), ethylene-vinyl alcohol (silicone), and polytetrafluoroethylene (CA). The diameter and the outer diameter of the prepared hollow tubular polymer tubular membrane are more than 2mm, so that the membrane has a high specific surface area, is easy to adsorb and desorb, the dosage of the adsorbent is smaller than that of the traditional particle type, the same dynamic adsorption efficiency can be achieved, and the desorption can be completed by using less heat energy naturally during desorption, so that the membrane has an energy-saving effect.
The ratio of the adsorbent in the hollow tubular polymeric tubular membrane adsorbent material is 10% -90%, and the adsorbent is any one of a granular form, a powdery form, a hollow fibrous form and a honeycomb form (not shown), wherein the plural particles of the powder have a particle size of 0.005-50 um, and the plural particles of the powder have a two-dimensional or three-dimensional pore structure, and the pores are regular or irregular, wherein the adsorbent is at least one selected from the group consisting of molecular sieves, activated carbon, alcohol amine modified, a-type zeolites (e.g., 3A, 4A or 5A), X-type zeolites (e.g., 13X), Y-type zeolites (e.g., ZSM-5), mesoporous molecular sieves (e.g., MCM-41, 48, 50 and SBA-15), metal Organic Frameworks (MOFs), and graphene.
The hollow tubular polymeric tubular membrane adsorbent is made of an inorganic material (not shown), wherein the size of the added inorganic material is from 0.01um to 100um, and the inorganic material may include an adsorbent, and if the adsorbent is contained, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the inorganic material is iron oxide, copper oxide, barium titanate, lead titanate, alumina, silica, aerogel (silica aerogel), bentonite (e.g., potassium bentonite, sodium bentonite, calcium bentonite, and aluminum bentonite), china clay (e.g., al bentonite) 2 O 3 .2SiO 2 .2H 2 O), hyplas soil (e.g. 20% Al) 2 O 3 .70％SiO 2 .0.8％Fe 2 O 3 .2.3％K 2 O.1.6％Na 2 O), calcium silicate (e.g. Ca) 3 SiO 5 、Ca 3 Si 2 O 7 And CaSiO 3 ) Magnesium silicate (e.g. Mg) 3 Si 4 O 10 (OH) 2 ) Sodium silicate (e.g. Na) 2 SiO 3 And hydrates (hydrates) thereof), anhydrous sodium sulfate, zirconium silicates (e.g. ZrSiO) 4 ) Opaque zirconium (e.g. 53.89% SiO) 2 .4.46％Al 2 O 3 .12.93％ZrO 2 .9.42％CaO.2.03％MgO.12.96％ZnO.3.73％K 2 O.0.58％Na 2 O) and silicon carbide.
In another embodiment of the present invention, the first air inlet pipeline 712 of the first tower type polymer tubular membrane module 71 and the second air inlet pipeline 722 of the second tower type polymer tubular membrane module 72 are connected to the other end of the second desorption gas pipeline 43 (as shown in fig. 5 to 18), so that the gas after the desorption and concentration of the carbon dioxide through the secondary desorption is input into the double-tower type polymer tubular membrane apparatus 70 for recompression treatment, and the first tower type polymer tubular membrane module 71 and the second tower type polymer tubular membrane module 72 respectively perform the adsorption drying procedure and the regeneration and desorption procedure, and when the first tower type polymer tubular membrane module 71 performs the adsorption drying procedure, the valve 7121 of the first air inlet pipeline 712 is in an open state (as shown in fig. 7 to 9), and the second tower type polymer tubular membrane module 72 performs the regeneration and desorption procedure, so that the valve 7221 of the second air inlet pipeline 722 is in a closed state (as shown in fig. 7 to 9), and the valve 7121 of the first air inlet pipeline 712 is opened, so that the gas after the desorption and concentration of the carbon dioxide in the second tower type polymer tubular membrane module 71 passes through the adsorption and the adsorption drying procedure, and the desorption of the second polymer tubular membrane module 71.
After a certain period of time, the first column type polymer tubular membrane module 71 is switched to the second column type polymer tubular membrane module 72 for adsorption drying before the adsorption saturation, and when the second column type polymer tubular membrane module 72 is subjected to adsorption drying, the valve 7221 of the second air inlet pipe 722 is opened (as shown in fig. 10 to 12), and the first column type polymer tubular membrane module 71 is switched to regeneration desorption, so that the valve 7121 of the first air inlet pipe 712 is closed (as shown in fig. 10 to 12), and the valve of the second air inlet pipe 722 is opened, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated by the second desorption in the second desorption gas pipe 43 is input into the second adsorption tower 721 in the second column type polymer tubular membrane module 72, and is adsorbed and dried by the hollow tubular polymer tubular membrane adsorption material in the second adsorption tower 721.
In another embodiment of the present invention, the first exhaust pipeline 713 of the first polymer tubular membrane module 71 and the second exhaust pipeline 723 of the second polymer tubular membrane module 72 are connected to an exhaust output pipeline 73 (as shown in fig. 5 to 18), and the other end of the exhaust output pipeline 73 is in the atmosphere or the outside air, and when the first polymer tubular membrane module 71 performs the adsorption drying procedure, the valve 7131 of the first exhaust pipeline 713 is in a closed state (as shown in fig. 7 to 9), while the second polymer tubular membrane module 72 performs the regeneration desorption procedure, so the valve 7231 of the second exhaust pipeline 723 is in an open state (as shown in fig. 7 to 9), so that the gas in the second adsorption tower 721 of the second polymer tubular membrane module 72 performing the regeneration procedure can perform the exhaust action through the second exhaust pipeline 723, and when the second polymer tubular membrane module 72 performs the adsorption drying procedure, the valve 7231 of the second exhaust pipeline 723 is in a closed state (as shown in fig. 10), and the valve 7131 of the first exhaust pipeline 71 performs the regeneration procedure (as shown in fig. 7 to 9), so that the first exhaust pipeline 71 performs the regeneration drying procedure, so that the first exhaust pipeline 71 performs the regeneration process of the first polymer tubular membrane module 713 (as shown in fig. 12).
In another embodiment of the present invention, the first compressed gas pipeline 715 of the first tower type polymer tubular membrane module 71 and the second compressed gas pipeline 725 of the second tower type polymer tubular membrane module 72 are connected to a compressed gas output pipeline 75 (as shown in fig. 5 to 18), when the first tower type polymer tubular membrane module 71 performs the adsorption and drying procedure, the valve 7151 of the first compressed gas pipeline 715 is opened (as shown in fig. 7 to 9), and the second tower type polymer tubular membrane module 72 performs the regeneration and desorption procedure, so the valve 7251 of the second compressed gas pipeline 725 is closed (as shown in fig. 7 to 9), so that the carbon dioxide desorbed and concentrated by the second desorption can pass through the hollow tubular polymer tubular membrane material in the first adsorption tower of the first tower type polymer tubular membrane module 71 to perform adsorption and drying, so that the carbon dioxide concentrated by the carbon dioxide desorbed by the second desorption can generate the low humidity compressed and dried carbon dioxide gas, wherein the low humidity compressed and dried carbon dioxide can reach a dew point of-40 ℃ to 70 ℃, and the low humidity compressed and dried carbon dioxide flows through the first adsorption pipeline 75 to output the compressed and dried carbon dioxide to the compressed gas with a dew point, and the compressed gas 75 is output to the compressed and the compressed gas. When the second column type polymer tubular membrane module 72 performs the adsorption drying process, the valve 7251 of the second compressed gas pipeline 725 is opened (as shown in fig. 10 to 12), and the first column type polymer tubular membrane module 71 performs the regeneration desorption process, so the valve 7151 of the first compressed gas pipeline 715 is closed (as shown in fig. 10 to 12), and by the adsorption drying process, the carbon dioxide compressed dry gas with low humidity dew point flows to the compressed gas output pipeline 75 through the second compressed gas pipeline 725, and is output and collected for use through the compressed gas output pipeline 75. The collection and use (not shown) includes storing the carbon dioxide compressed dry gas in a steel cylinder, a steel tank for temporary storage, or directly transporting the carbon dioxide compressed dry gas to other places requiring carbon dioxide, such as greenhouses or seaweed farms, soda-coke plants, chemical plants, or food industry plants.
In another embodiment of the present invention, the first regeneration pipeline 714 of the first polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second polymer tubular membrane module 72 are connected to a heat pipeline 74 (as shown in fig. 5 to 18), and the heat pipeline 74 is used to convey high-temperature hot gas to the first adsorption tower 711 in the first polymer tubular membrane module 71 or the second adsorption tower 721 in the second polymer tubular membrane module 72 for regeneration and desorption, when the first polymer tubular membrane module 71 performs an adsorption and drying procedure, the valve 7141 of the first regeneration pipeline 714 is closed (as shown in fig. 7 to 9), and the second polymer tubular membrane module 72 performs a regeneration and desorption procedure, so the valve 7241 of the second regeneration pipeline 724 is open (as shown in fig. 7 to 9), and when the second polymer tubular membrane module 72 performs an adsorption and drying procedure, the valve 7141 of the second regeneration pipeline 724 is closed (as shown in fig. 10 to 9), and the valve 7141 of the first regeneration pipeline 724 is open (as shown in fig. 10 to fig. 12), so that the first regeneration pipeline 7141 of the second regeneration pipeline 71 performs a regeneration and desorption (as shown in fig. 10).
In addition, the first variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50 and stack 60, and the related contents thereof have been described and will not be repeated here. Therefore, a first variation (as shown in fig. 6) of another embodiment is that a cooling device 80 is disposed in the first desorption gas pipeline 24, and the cooling device 80 is any one of a cooler, a condenser, a dehumidifier and a cooler, so as to process the gas after the carbon dioxide desorption concentration in the first desorption gas pipeline 24, so that the gas after the carbon dioxide desorption concentration can release heat energy, and reduce the temperature of the gas after the carbon dioxide desorption concentration, so as to improve the re-adsorption efficiency when entering the adsorption region 401 of the second carbon dioxide adsorption rotor 40, thereby increasing the effectiveness of the adsorption region 401 of the second carbon dioxide adsorption rotor 40.
In addition, a second variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50, and a chimney 60, and the related contents thereof are already described and will not be repeated here. Therefore, a second variation (as shown in fig. 7) of another embodiment is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, which is not repeated here), and the difference from the first variation of another embodiment is that the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 is provided with a first heater 76, and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a second heater 77, wherein the first heater 76 and the second heater 77 are any one of an electric heater, a natural gas type heater, a heat exchanger or a heat medium oil heat exchanger, and when the first heater 76 of the first regeneration pipeline 714 and the second heater 77 of the second regeneration pipeline 724 are used to perform the regeneration desorption process on the first polymer tubular membrane module 71 or the second polymer tubular membrane module 72, the first heater 76 or the second hot gas 77 can deliver the high temperature to the first polymer tubular membrane module 71 of the first polymer tubular membrane module 71 or the second polymer tubular membrane module 72 to perform the desorption process, and use the second polymer tubular membrane module 711 in the adsorption tower type polymer tubular membrane module 71 or the second regeneration tower 721 of the first polymer tubular membrane module 714.
In addition, a third variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50 and a chimney 60, and the related contents thereof are already described and will not be repeated here. Therefore, a third variation (as shown in fig. 8 and 9) of the other embodiment is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other embodiment, which is not repeated here), and the first regeneration pipeline 714 of the first tower polymer tubular membrane group 7 is provided with a first heater 76, and the second regeneration pipeline 725 of the second tower polymer tubular membrane group 72 is provided with a second heater 77 (please refer to the content of the second variation of the other embodiment, which is not repeated here), and the difference from the second variation of the other embodiment is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the carbon dioxide desorbed and concentrated gas delivered by the second desorption gas pipeline 43 can return to the second heating gas pipeline 51 from the recirculation pipeline 44, and then enters the second heating gas pipeline 51 alone or other external gas mixed with the second heating gas 50. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the third variation of the above-mentioned another embodiment of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 8), and the second desorption gas pipeline 43 is matched with the recirculation pipeline 44 to form a positive pressure type, so that the gas after the carbon dioxide desorbed and concentrated for the second time in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and returned to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 9), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, a fourth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorbing rotor 20, first heating device 30, second carbon dioxide adsorbing rotor 40, second heating device 50 and a chimney 60, and the related contents thereof are already described and will not be repeated here. Therefore, a fourth variation of the present embodiment (as shown in fig. 10) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other embodiment, which is not repeated here), and the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 is provided with a first heater 76, while the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 is provided with a second heater 77 (please refer to the content of the second variation of the other embodiment, which is not repeated here), and the difference from the fourth variation of the other embodiment is that the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 are connected with a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas pipeline 24 of the first carbon dioxide adsorption rotor 20, and the heat exchanger 90 is provided with a hot side pipeline 901 and a cold side pipeline 902, wherein one end of the hot side pipeline 90 is connected with the second regeneration pipeline 74 of the first carbon dioxide adsorption rotor 20, and the other end of the hot side pipeline 901 is connected with the cold side pipeline 901 of the first desorption gas pipeline 902 to form a hot side heat exchanger after the desorption gas pipeline 90 is connected with the first desorption gas pipeline 902, and the first desorption gas pipeline 90, and the cold side pipeline 90 is connected with the cold side pipeline 901 of the first desorption gas pipeline 902 to form a cold side of the first desorption gas pipeline 902, and the cold side pipeline 90 to form a cold side pipeline 902, and the cold side pipeline 90, after the first desorption gas pipeline 90, the first desorption gas pipeline 90 of the first desorption gas pipeline 90 is connected with the first desorption gas pipeline 902, and the first desorption gas pipeline 901 of the first desorption gas pipeline 902, and the cold side pipeline 902 to desorbs the cold side pipeline 902 to form the cold side pipeline 902, and the cold side pipeline 902 to form the cold side pipeline 902 to desorbs the cold side pipeline 902 to form the cold side pipeline 902, then sent to the cooler 80 for cooling, and finally sent to the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 for adsorption.
In addition, a fifth modification of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50, and stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, a fifth variation of the other embodiment (as shown in fig. 11 and 12) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other embodiment, which is not repeated here), and the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 is provided with a first heater 76, the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a second heater 77 (please refer to the content of the second variation of another embodiment, which is not repeated here), and the heat energy pipeline 74 connected with the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is connected with a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas line 24 of the first carbon dioxide adsorption rotor 20, and the heat exchanger 90 is provided with a cold side pipe 901 and a hot side pipe 902 (please refer to the fourth variation of the other embodiment, which is not repeated here), a fourth variant difference from the other embodiment is that the second desorption gas line 43 is provided with a recirculation line 44, one end of the recycling pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recycling pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed twice by the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recycling pipeline 44, and then enter the second heating device 50 after being mixed with the outside air or other source gas in the second heating gas inlet pipeline 51, or when the second heating air intake line 51 gas alone is not mixed with outside air or other sources of gas. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the fifth variation of the above-mentioned another embodiment of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 11), and the second desorption gas pipeline 43 is matched with the recirculation pipeline 44 to form a positive pressure type, so that the gas after the carbon dioxide desorbed and concentrated in the second desorption gas pipeline 43 for the second time can be squeezed into the recirculation pipeline 44 and returned to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 12), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, a sixth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50, and a chimney 60, and the related contents thereof are already described and will not be repeated here. Therefore, a sixth variation (as shown in fig. 13) of another embodiment is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, which is not repeated here), and the difference from the first variation of another embodiment is that the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane module 72 is provided with a heater 78, wherein the heater 78 is any one of an electric heater, a natural gas heater, a heat exchanger or a heat medium oil heat exchanger, and the high-temperature hot gas generated by the heater 78 of the heat energy pipeline 74 is conveyed into the first regeneration pipeline 714 or the second regeneration pipeline 724 and then conveyed into the first adsorption tower 711 in the first tower polymer tubular membrane module 71 or the second adsorption tower 721 in the second polymer tubular membrane module 72 for regeneration, and the flow direction of the first regeneration pipeline 7141 and the second regeneration pipeline 7241 of the first regeneration pipeline 714 is controlled.
In addition, a seventh modification of another embodiment of the present invention is based on the above-described main pretreatment device 10, first carbon dioxide adsorbing rotor 20, first heating device 30, second carbon dioxide adsorbing rotor 40, second heating device 50, and stack 60, and the related contents thereof have been described and will not be repeated here. Therefore, a seventh variation of the other embodiment (as shown in fig. 14 and 15) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other embodiment, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 is provided with a heater 78 (please refer to the content of the sixth variation of the other embodiment, which is not repeated here), and the difference from the sixth variation of the other embodiment is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide delivered by the second desorption gas pipeline 43 can be returned to the second heating gas pipeline 51 from the recirculation pipeline 44, and then mixed with the other heating gas in the second heating gas pipeline 51 to heat the second external gas or heat the other external gas alone or without entering the second external gas 50. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the seventh variation of the above-mentioned another embodiment of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 14), and the second desorption gas pipeline 43 is matched with the recirculation pipeline 44 to form a positive pressure type, so that the gas obtained after the second desorption and concentration of the carbon dioxide in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and return to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 15), and the fan 511 disposed on the second heating gas inlet pipeline 511 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, an eighth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorbing rotor 20, first heating device 30, second carbon dioxide adsorbing rotor 40, second heating device 50, and stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, an eighth variation of another embodiment (as shown in fig. 16) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a heater 78 (please refer to the content of the sixth variation of another embodiment, which is not repeated here), and the difference from the sixth variation of another embodiment is that the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is connected to a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas pipeline 24 of the first carbon dioxide adsorption rotor 20, the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein one end of the cold side pipeline 901 of the heat exchanger 90 is connected with the other end of the heat energy pipeline 74, the other end of the cold side pipeline 901 of the heat exchanger 90 is external air or connected with cooling gas so as to enter the cold side pipeline 901 of the heat exchanger 90 for heat exchange, then the heat energy pipeline 74 is used for conveying high-temperature hot gas into the first regeneration pipeline 714 of the first tower type polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane group 72 for desorption and regeneration, the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the gas after carbon dioxide desorption and concentration at the hot side once in the first desorption gas pipeline 24 can be subjected to heat exchange through the pipeline 902 of the heat exchanger 90, then sent to the cooler 80 for cooling, and finally sent to the adsorption area 401 of the second carbon dioxide adsorption rotor 40 for adsorption.
In addition, a ninth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment device 10, first carbon dioxide adsorption rotor 20, first heating device 30, second carbon dioxide adsorption rotor 40, second heating device 50, and stack 60, and the related contents thereof are already described and will not be repeated here. Therefore, a ninth variation of the other embodiment (as shown in fig. 17 and 18) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other embodiment, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a heater 78 (please refer to the content of the sixth variation of another embodiment, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is connected to a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas line 24 of the first carbon dioxide adsorption rotor 20, and the heat exchanger 90 is provided with a cold side pipe 901 and a hot side pipe 902 (please refer to the eighth variation of the other embodiment, which is not repeated here), an eighth variation from the alternative embodiment is that the second desorption gas line 43 is provided with a recirculation line 44, one end of the recycling pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recycling pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed twice by the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recycling pipeline 44, and then enter the second heating device 50 after being mixed with the outside air or other source gas in the second heating gas inlet pipeline 51, or when the second heating air intake line 51 gas alone is not mixed with outside air or other sources of gas. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the ninth variation of the above-mentioned another embodiment of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 17), and the second desorption gas pipeline 43 is matched with the recirculation pipeline 44 to form a positive pressure type, so that the gas after the carbon dioxide desorbed and concentrated for the second time in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and returned to the second heating gas inlet pipeline 51. A second modification is that the second desorption gas pipeline 43 is provided with a blower 431, the second heating gas inlet pipeline 51 is provided with a blower 511 (as shown in fig. 18), and the blower 511 of the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and is close to the second heating device 50, and is matched with the blower 431 of the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated for the second time in the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
The carbon dioxide adsorbing rotary wheel processing method of the present invention is mainly used for a carbon dioxide adsorbing rotary wheel system, and is provided with a pretreatment apparatus 10, a first carbon dioxide adsorbing rotary wheel 20, a first heating device 30, a second carbon dioxide adsorbing rotary wheel 40, a second heating device 50 and a chimney 60 (as shown in fig. 1 to 18), the first carbon dioxide adsorbing rotary wheel 20 is provided with an adsorption region 201 and a desorption region 202, the first carbon dioxide adsorbing rotary wheel 20 is connected with a pretreatment air inlet pipeline 21, a first clean gas discharge pipeline 22, a first hot gas delivery pipeline 23 and a first desorption gas pipeline 24 (as shown in fig. 1 to 18), the second carbon dioxide adsorbing rotary wheel 40 is provided with an adsorption region 401 and a desorption region 402, the second carbon dioxide adsorbing rotary wheel 40 is connected with a second clean gas discharge pipeline 41, a second hot gas delivery pipeline 42 and a second desorption gas pipeline 43 (as shown in fig. 1 to 18), the first heating device 30 is provided with a first heating air inlet pipeline 31, the second heating device 50 is provided with a second heating device 51, and the first fin-type heat exchanger 51 and the heat exchanger apparatus or the heat exchanger for heating the natural gas inlet pipeline 10 and the heat exchanger 50 (as shown in fig. 1 to 18). The first carbon dioxide adsorbing rotor 20 and the second carbon dioxide adsorbing rotor 40 are zeolite concentrating rotors or concentrating rotors made of other materials, respectively.
The main steps of the processing method (as shown in fig. 19) include: step S100 gas input pretreatment device: gas is fed through the gas inlet line 11 to the pre-treatment apparatus 10 for treatment. After the step S100 is completed, the next step S110 is performed.
One end of the gas inlet pipeline 11 is connected to a place where carbon dioxide is generated, such as a production place, an office building, or the like, or a region (not shown) where carbon dioxide is generated indoors, so that the gas inlet pipeline can convey gas containing carbon dioxide or other gases, and the pretreatment apparatus 10 is any one of a cooler, a condenser, a dehumidifier, and a cooler, so as to pretreat the gas, so that the gas can release heat energy, thereby improving the adsorption efficiency.
In addition, the next step is that the first carbon dioxide adsorption rotating wheel in step S110 adsorbs: the gas treated by the pretreatment apparatus 10 is outputted from the other end of the pretreatment gas pipe 21 to one side of the adsorption zone 201 of the first carbon dioxide adsorption rotor 20 to be adsorbed by carbon dioxide. After the step S110 is completed, the next step S120 is performed.
One end of the pretreatment gas line 21 is connected to the other side of the pretreatment device 10, and the other end of the pretreatment gas line 21 is connected to one side of the adsorption region 201 of the first carbon dioxide adsorption rotor 20, so that the gas containing carbon dioxide or other gases pretreated by the pretreatment device 10 can be transported into the adsorption region 201 of the first carbon dioxide adsorption rotor 20 through the pretreatment gas line 21 to be subjected to carbon dioxide adsorption (as shown in fig. 1 to 4). The pre-processing gas pipeline 21 is provided with a blower 211 (as shown in fig. 3 and fig. 4), so that the blower 211 can push and pull the pre-processed gas containing carbon dioxide or other gases in the pre-processing gas pipeline 21 into the adsorption region 201 of the first carbon dioxide adsorption rotor 20.
Further, the next step is step S120 of the first carbon dioxide adsorbing wheel emitting: the gas generated by the adsorption of the carbon dioxide generated in the adsorption region 201 of the first carbon dioxide adsorption rotor 20 is output from the other end of the first clean gas discharge pipeline 22 to the stack 60 for discharge. After the step S120 is completed, the next step S130 is performed.
One end of the first net gas discharge pipeline 22 is connected to the other side of the adsorption region 201 of the first carbon dioxide adsorption rotor 20, and the other end of the first net gas discharge pipeline 22 is connected to the chimney 60 (as shown in fig. 1 to 4), so that the gas generated after the carbon dioxide is adsorbed by the adsorption region 201 of the first carbon dioxide adsorption rotor 20 can be transported to the chimney 60 through the first net gas discharge pipeline 22 for being discharged to the atmosphere. The first clean gas discharging pipeline 22 is provided with a fan 221 (as shown in fig. 3 and fig. 4), so that the fan 221 can push and pull the gas after carbon dioxide adsorption in the first clean gas discharging pipeline 22 to the chimney 60 for discharging.
In addition, the next step S130 is to deliver the first hot gas for desorption: the high-temperature hot gas is delivered to the desorption region 202 of the first carbon dioxide adsorption rotor 20 for desorption through the first hot gas delivery line 23 connected to the first heating device 30. After the step S130 is completed, the next step S140 is performed.
The other side of the desorption region 202 of the first carbon dioxide adsorbing rotor 20 is connected to one end of the first hot gas conveying pipeline 23, and the other end of the first hot gas conveying pipeline 23 is connected to the first heating device 30 (as shown in fig. 1 to 4), and the first heating device 30 inputs outside air or gas from other sources through the first heating air inlet pipeline 31, so that the first heating device 30 can heat the outside air or gas from other sources input through the first heating air inlet pipeline 31 to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is conveyed to the desorption region 202 of the first carbon dioxide adsorbing rotor 20 through the first hot gas conveying pipeline 23 to be desorbed for use. The first heating intake pipe 31 is provided with a blower 311 (as shown in fig. 3 and 4), so that the blower 311 can push and pull the external air or other source gas in the first heating intake pipe 31 into the first heating device 30.
In addition, the next step S140 is to output the gas after carbon dioxide desorption and concentration: the gas obtained by desorbing and concentrating the carbon dioxide which is desorbed and generated once through the desorption region 202 of the first carbon dioxide adsorption rotor 20 is outputted from the other end of the first desorption gas pipeline 24. After the step S140 is completed, the next step S150 is performed.
Further, the next step is a step S150 of adsorbing by the second carbon dioxide adsorbing wheel: the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated once in the first desorbed gas pipeline 24 is delivered to one side of the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 for re-adsorption. After the step S150 is completed, the next step S160 is performed.
Wherein one side of the desorption region 202 of the first carbon dioxide adsorption rotor 20 is connected to one end of the first desorption gas pipeline 24, and the other end of the first desorption gas pipeline 24 is connected to one side of the adsorption region 401 of the second carbon dioxide adsorption rotor 40 (as shown in fig. 1 to 4), so that the concentrated gas desorbed from the carbon dioxide desorbed and generated by the desorption region 202 of the first carbon dioxide adsorption rotor 20 can be transported to the adsorption region 401 of the second carbon dioxide adsorption rotor 40 through the first desorption gas pipeline 24 for re-adsorption. The first desorption gas pipeline 24 is provided with a fan 241 (as shown in fig. 3 and 4), so that the fan 241 can push the concentrated gas desorbed from the carbon dioxide desorbed from the first desorption gas pipeline 24 to the adsorption region 401 of the second carbon dioxide adsorption rotor 40.
Further, the next step proceeds to step S160 where the second carbon dioxide adsorption rotor discharges: the gas generated by the adsorption of the carbon dioxide generated in the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 is output from the other end of the second clean gas discharge pipe 41 to the stack 60 for discharge. After the step S160 is completed, the next step S170 is performed.
The other side of the adsorption region 401 of the second carbon dioxide adsorbing rotor 40 is connected to the second clean gas discharging pipeline 41, and the other end of the second clean gas discharging pipeline 41 is connected to the chimney 60 (as shown in fig. 1 to 4), so that the gas generated after the carbon dioxide is re-adsorbed by the adsorption region 401 of the second carbon dioxide adsorbing rotor 40 can be transported to the chimney 60 through the second clean gas discharging pipeline 41 to be discharged to the atmosphere. The second purified gas discharging pipeline 41 is provided with a fan 411 (as shown in fig. 3 and fig. 4), so that the fan 411 can push the generated gas after the carbon dioxide in the second purified gas discharging pipeline 41 is adsorbed to the chimney 60 for discharging.
In addition, the next step S170 is to deliver the second hot gas for desorption: the high-temperature hot gas is delivered to the desorption region 402 of the second carbon dioxide adsorption rotor 40 for desorption through the second hot gas delivery line 42 connected to the second heating device 50. After the step S170 is completed, the next step S180 is performed.
The other side of the desorption region 402 of the second carbon dioxide adsorbing wheel 40 is connected to one end of the second hot gas conveying pipeline 42, and the other end of the second hot gas conveying pipeline 42 is connected to the second heating device 50 (as shown in fig. 1 to 4), and the second heating device 50 inputs outside air or gas from other sources through the second heating air inlet pipeline 51, so that the second heating device 50 can heat the outside air or gas from other sources input through the second heating air inlet pipeline 51 to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 is conveyed to the desorption region 402 of the second carbon dioxide adsorbing wheel 40 through the second hot gas conveying pipeline 42 to be desorbed for use. The second heating air intake pipe 51 is provided with a blower 511 (as shown in fig. 4), so that the blower 511 can push and pull the outside air or other source gas in the second heating air intake pipe 51 into the second heating device 50.
In addition, the next step, step S180, is to output the gas after carbon dioxide desorption and concentration: the gas obtained by desorbing and concentrating the carbon dioxide which is secondarily desorbed and generated in the desorption region 402 of the second carbon dioxide adsorption rotor 40 is output from the other end of the second desorption gas line 43.
One side of the desorption region 402 of the second carbon dioxide adsorption rotor 40 is connected to one end of the second desorption gas pipeline 43 (as shown in fig. 1 to 4), so that the gas after desorption and concentration of carbon dioxide desorbed and secondarily desorbed by the desorption region 402 of the second carbon dioxide adsorption rotor 40 can be output through the second desorption gas pipeline 43 for subsequent processing. The post-treatment (not shown) includes storing the gas desorbed and concentrated by the second desorbed carbon dioxide delivered from the second desorption gas pipeline 43 through a steel cylinder or a steel tank, or delivering and supplying the gas to other places requiring carbon dioxide, such as greenhouses or seaweed farms, soda-water coke farms, chemical plants, or food factories, as a raw material, so that the gas desorbed and concentrated by the second desorbed carbon dioxide can have the effect of post-application. The second desorption gas pipeline 43 is provided with a blower 431 (as shown in fig. 3 and fig. 4), so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated in the second desorption gas pipeline 43 can be pushed and pulled out by the blower 431.
In addition, in the main steps of the present invention, a recycling pipeline 44 is disposed on the second desorption gas pipeline 43, one end of the recycling pipeline 44 is connected to the second desorption gas pipeline 43 (as shown in fig. 3 and 4), and the other end of the recycling pipeline 44 is connected to the second heating intake pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed and secondarily desorbed by the second desorption gas pipeline 43 can be returned to the second heating intake pipeline 51 through the recycling pipeline 44, and then mixed with the outside air or other source gas in the second heating intake pipeline 51 and then enter the second heating device 50, or the gas alone in the second heating intake pipeline 51 is not mixed with the outside air or other source gas. Wherein the recycling line 44 is provided with a valve 441, so that the gas flow direction of the recycling line 44 is controlled by the valve 441.
In the main steps of the present invention, the second desorption gas pipeline 43 has two variants, wherein the first variant is that the front end and the rear end of the second desorption gas pipeline 43 at the connection of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 3), and the recirculation pipeline 44 is matched to form a positive pressure type, so that the gas desorbed and concentrated by the carbon dioxide in the second desorption gas pipeline 43 for the second desorption can be squeezed into the recirculation pipeline 44 and return to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 4), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, another step of the present invention is established in the design of the gas input pretreatment device in the step S100, the first carbon dioxide adsorption rotor adsorption in the step S110, the first carbon dioxide adsorption rotor discharge in the step S120, the first hot gas delivery for desorption in the step S130, the gas after carbon dioxide desorption and concentration output in the step S140, the second carbon dioxide adsorption rotor adsorption in the step S150, the second carbon dioxide adsorption rotor discharge in the step S160, the second hot gas delivery for desorption in the step S170, and the gas after carbon dioxide desorption and concentration output in the step S180, and the related contents thereof are explained and will not be repeated here. Therefore, the present invention includes the following steps (as shown in fig. 20) after outputting the gas after carbon dioxide desorption and concentration in step S180, and step S200 is transmitted to the double-tower type polymer tubular membrane device: the gas obtained after the desorption and concentration of the carbon dioxide desorbed and concentrated secondarily in the second desorption gas pipeline 43 is conveyed to a twin-tower type polymer tubular membrane device 70 for treatment. The gas desorbed and concentrated by the carbon dioxide desorbed and concentrated for the second time in the second desorbed gas pipeline 43 can be recompressed by the double-tower type polymer tubular membrane apparatus 70 to form a carbon dioxide compressed dry gas (as shown in fig. 5 and 6).
The double-tower polymer tubular membrane apparatus 70 is provided with a first tower polymer tubular membrane group 71 and a second tower polymer tubular membrane group 72, the first tower polymer tubular membrane group 71 is provided with a first adsorption tower 711, a first air inlet pipeline 712, a first air outlet pipeline 713, a first regeneration pipeline 714 and a first compressed gas pipeline 715 (as shown in fig. 5 and 6), the second tower polymer tubular membrane group 72 is provided with a second adsorption tower 721, a second air inlet pipeline 722, a second air outlet pipeline 723, a second regeneration pipeline 724 and a second compressed gas pipeline 725 (as shown in fig. 5 and 6), the first air inlet pipeline 712, the first air outlet pipeline 713, the first regeneration pipeline 714 and the first compressed gas pipeline 715 of the first tower polymer tubular membrane group 71 are respectively provided with a valve 7121, a valve 7131, a valve 7141, a valve 7151 (as shown in fig. 5 and 6), and the second air inlet pipeline 723, the second compressed gas pipeline 7251 and the second compressed gas pipeline 724 and the compressed gas pipeline 725 of the second tower polymer tubular membrane group 72 are respectively provided with a valve 7131, a valve 7231, a valve 7251 and a valve 7231, as shown in fig. 6.
In addition, the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 and the second adsorption tower 721 of the second tower-type polymer tubular membrane group 72 are filled with a plurality of hollow tubular polymer tubular membrane adsorbing materials (as shown in fig. 5 and fig. 6), and the hollow tubular polymer tubular membrane adsorbing materials are made of a polymer and an adsorbent, and the polymer is made of at least one of Polysulfone (PSF), polyethersulfone (PESF), polyvinylidene fluoride (PVDF), polyphenylsulfone (PPSU), polyacrylonitrile (polyacrylonitrile), cellulose acetate, cellulose diacetate, polyimide (PI), polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-glycolic acid (polylactic-co-glycolic acid), polycaprolactone, polyvinylpyrrolidone (polyvinyl pyrrolidone), ethylene-polysiloxane (polyvinyl alcohol), and polytetrafluoroethylene (CA). The diameter and the outer diameter of the prepared hollow tubular polymer tubular membrane are more than 2mm, so that the membrane has a high specific surface area, is easy to adsorb and desorb, the dosage of the adsorbent is smaller than that of the traditional particle type, the same dynamic adsorption efficiency can be achieved, and the desorption can be completed by using less heat energy naturally during desorption, so that the membrane has an energy-saving effect.
The ratio of the adsorbent in the hollow tubular polymeric tubular membrane adsorbent material is 10% -90%, and the adsorbent is any one of a granular form, a powdery form, a hollow fibrous form and a honeycomb form (not shown), wherein the plural particles of the powder have a particle size of 0.005-50 um, and the plural particles of the powder have a two-dimensional or three-dimensional pore structure, and the pores are regular or irregular, wherein the adsorbent is at least one selected from the group consisting of molecular sieves, activated carbon, alcohol amine modified, a-type zeolites (e.g., 3A, 4A or 5A), X-type zeolites (e.g., 13X), Y-type zeolites (e.g., ZSM-5), mesoporous molecular sieves (e.g., MCM-41, 48, 50 and SBA-15), metal Organic Frameworks (MOFs), and graphene.
The hollow tubular polymeric tubular membrane adsorbent is made of an inorganic material (not shown), wherein the size of the added inorganic material is from 0.01um to 100um, and the inorganic material may include an adsorbent, and if the adsorbent is contained, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the inorganic material is iron oxide, copper oxide, barium titanate, lead titanate, alumina, silica, aerogel (silica aerogel), bentonite (e.g., potassium bentonite, sodium bentonite, calcium bentonite, and aluminum bentonite), china clay (e.g., al bentonite) 2 O 3 .2SiO 2 .2H 2 O), hyples earth (e.g. 20% Al) 2 O 3 .70％SiO 2 .0.8％Fe 2 O 3 .2.3％K 2 O.1.6％Na 2 O), calcium silicate (e.g. Ca) 3 SiO 5 、Ca 3 Si 2 O 7 And CaSiO 3 ) Magnesium silicate (e.g. Mg) 3 Si 4 O 10 (OH) 2 ) Sodium silicate (e.g. Na) 2 SiO 3 And hydrates (hydrates) thereof), anhydrous sodium sulfate, zirconium silicates (e.g. ZrSiO) 4 ) Opaque zirconium (e.g. 53.89% SiO) 2 .4.46％Al 2 O 3 .12.93％ZrO 2 .9.42％CaO.2.03％MgO.12.96％ZnO.3.73％K 2 O.0.58％Na 2 O) and silicon carbide.
In another step of the present invention, the first air inlet pipeline 712 of the first tower type polymer tubular membrane module 71 and the second air inlet pipeline 722 of the second tower type polymer tubular membrane module 72 are connected to the other end of the second desorption gas pipeline 43 (as shown in fig. 5 to 18), so that the gas after the desorption and concentration of the carbon dioxide through the secondary desorption is input into the double-tower type polymer tubular membrane apparatus 70 for recompression treatment, and the first tower type polymer tubular membrane module 71 and the second tower type polymer tubular membrane module 72 respectively perform the adsorption drying procedure and the regeneration and desorption procedure, and when the first tower type polymer tubular membrane module 71 performs the adsorption drying procedure, the valve 7121 of the first air inlet pipeline 712 is in an open state (as shown in fig. 7 to 9), and the second tower type polymer tubular membrane module 72 performs the regeneration and desorption procedure, so that the valve 7221 of the second air inlet pipeline 722 is in a hollow closed state (as shown in fig. 7 to 9), and the valve 7121 of the first air inlet pipeline 712 is opened, so that the gas in the second tower type polymer tubular membrane module 43 passes through the adsorption and the desorption gas in the adsorption tower 71 for desorption and the desorption of the second polymer tubular membrane module 71 for desorption.
After a certain period of time, the first column type polymer tubular membrane module 71 is switched to the second column type polymer tubular membrane module 72 for adsorption drying before the adsorption saturation, and when the second column type polymer tubular membrane module 72 is subjected to adsorption drying, the valve 7221 of the second air inlet pipe 722 is opened (as shown in fig. 10 to 12), and the first column type polymer tubular membrane module 71 is switched to regeneration desorption, so that the valve 7121 of the first air inlet pipe 712 is closed (as shown in fig. 10 to 12), and the valve of the second air inlet pipe 722 is opened, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated by the second desorption in the second desorption gas pipe 43 is input into the second adsorption tower 721 in the second column type polymer tubular membrane module 72, and is adsorbed and dried by the hollow tubular polymer tubular membrane adsorption material in the second adsorption tower 721.
In another step of the present invention, the first exhaust pipeline 713 of the first polymer tubular membrane module 71 and the second exhaust pipeline 723 of the second polymer tubular membrane module 72 are connected to an exhaust output pipeline 73 (as shown in fig. 5 to 18), and the other end of the exhaust output pipeline 73 is in the atmosphere or the outside air, and when the first polymer tubular membrane module 71 performs the adsorption drying procedure, the valve 7131 of the first exhaust pipeline 713 is in a closed state (as shown in fig. 7 to 9), while the second polymer tubular membrane module 72 performs the regeneration desorption procedure, so the valve 7231 of the second exhaust pipeline 723 is in an open state (as shown in fig. 7 to 9), so that the gas in the second adsorption tower 721 of the second polymer tubular membrane module 72 performing the regeneration procedure can perform the exhaust action through the second exhaust pipeline 723, and when the second polymer tubular membrane module 72 performs the adsorption drying procedure, the valve 7231 of the second exhaust pipeline 723 is in a closed state (as shown in fig. 10), and the valve 7131 of the first exhaust pipeline 71 performs the regeneration procedure (as shown in fig. 7 to 9), so that the first exhaust pipeline 71 performs the desorption procedure, and the desorption procedure from the first exhaust pipeline 71 in fig. 71, so that the first exhaust pipeline 71 performs the desorption procedure, and the second polymer tubular membrane module 71 performs the desorption procedure, and the desorption procedure, as shown in fig. 12.
In another step of the present invention, the first compressed gas pipeline 715 of the first tower polymer tubular membrane module 71 and the second compressed gas pipeline 725 of the second tower polymer tubular membrane module 72 are connected to a compressed gas output pipeline 75 (as shown in fig. 5 to 18), when the first tower polymer tubular membrane module 71 performs the adsorption and drying process, the valve 7151 of the first compressed gas pipeline 715 is in an open state (as shown in fig. 7 to 9), and the second tower polymer tubular membrane module 72 performs the regeneration and desorption process, so the valve 7251 of the second compressed gas pipeline 725 is in a closed state (as shown in fig. 7 to 9), so that the gas after the secondary desorption and concentration of the carbon dioxide can pass through the hollow tubular polymer tubular membrane material in the first adsorption tower 711 of the first tower polymer tubular membrane module 71 for adsorption and drying, so that the gas after the secondary desorption and concentration of the carbon dioxide can generate the low humidity compressed and dried carbon dioxide gas 715, wherein the low humidity gas can reach a dew point of 40-70 ℃, and the low humidity gas can be output to the first compressed and dried carbon dioxide is collected to the first compressed and dried carbon dioxide output to the compressed gas 75 at a dew point. When the second column type polymer tubular membrane module 72 is performing the adsorption drying process, the valve 7251 of the second compressed gas pipeline 725 is opened (as shown in fig. 10 to 12), and the first column type polymer tubular membrane module 71 is performing the regeneration desorption process, so the valve 7151 of the first compressed gas pipeline 715 is closed (as shown in fig. 10 to 12), and the above adsorption drying process allows the carbon dioxide compressed dry gas with low humidity dew point to flow to the compressed gas output pipeline 75 through the second compressed gas pipeline 725, and is output and collected for use through the compressed gas output pipeline 75. The collection and use (not shown) includes storing the carbon dioxide compressed dry gas in a steel cylinder, a steel tank for temporary storage, or directly transporting the carbon dioxide compressed dry gas to other places requiring carbon dioxide, such as greenhouses or seaweed farms, soda-coke plants, chemical plants, or food industry plants.
In another step of the present invention, the first regeneration pipeline 714 of the first polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second polymer tubular membrane module 72 are connected to a heat energy pipeline 74 (as shown in fig. 5 to 18), and the heat energy pipeline 74 is used to convey high-temperature hot gas to the first adsorption tower 711 in the first polymer tubular membrane module 71 or the second adsorption tower 721 in the second polymer tubular membrane module 72 for regeneration and desorption, when the first polymer tubular membrane module 71 performs an adsorption and drying procedure, the valve 7141 of the first regeneration pipeline 714 is closed (as shown in fig. 7 to 9), and the second polymer tubular membrane module 72 performs a regeneration and desorption procedure, so the valve 7241 of the second regeneration pipeline 724 is open (as shown in fig. 7 to 9), and when the second polymer tubular membrane module 72 performs an adsorption and drying procedure, the valve 7141 of the second regeneration pipeline 724 is closed (as shown in fig. 10 to 9), and the valve 7141 of the second regeneration pipeline 724 is open (as shown in fig. 10 to 714, so that the regeneration pipeline 7141 is open (as shown in fig. 10).
In addition, the first variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane equipment, and the related contents thereof are already described and will not be repeated here. Therefore, a first variation of the other step (as shown in fig. 6) is that the first desorption gas pipeline 24 is provided with a cooling device 80, and the cooling device 80 is any one of a cooler, a condenser, a dehumidifier and a cooler, so as to process the gas after the carbon dioxide desorption concentration in the first desorption gas pipeline 24 is once desorbed, so that the gas after the carbon dioxide desorption concentration once can release heat energy, and reduce the temperature of the gas after the carbon dioxide desorption concentration once, so as to improve the re-adsorption efficiency when entering the adsorption area 401 of the second carbon dioxide adsorption rotor 40, thereby increasing the effectiveness of the adsorption area 401 of the second carbon dioxide adsorption rotor 40.
In addition, the second variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane equipment, and the related contents thereof are already described and will not be repeated here. Therefore, a second variation of another step (as shown in fig. 7) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which is not repeated here), and the difference from the first variation of another step is that the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 is provided with a first heater 76, and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a second heater 77, wherein the first heater 76 and the second heater 77 are any one of an electric heater, a natural gas heater, a heat exchanger or a heat medium oil heat exchanger, and when the first heater 76 of the first regeneration pipeline 714 and the second heater 77 of the second regeneration pipeline 724 are used to perform the regeneration desorption procedure on the first tower type polymer tubular membrane module 71 or the regeneration desorption procedure on the second tower type polymer tubular membrane module 72, the first heater 76 or the second heater 77 can deliver high-temperature hot gas to the second heater 71 of the first polymer tubular membrane module 71 to perform the desorption procedure or the second polymer tubular membrane module 721 in the first tower type polymer tubular membrane module 71 or the second regeneration tower type polymer tubular membrane module 721.
In addition, the third variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane equipment, and the related contents thereof are already described and will not be repeated here. Therefore, a third variation of the other step (as shown in fig. 8 and 9) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other step, which is not repeated here), and the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 is provided with a first heater 76, and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 is provided with a second heater 77 (please refer to the content of the second variation of the other step, which is not repeated here), and the second variation of the other step is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the second desorption gas pipeline 43 can be returned to the second heating gas pipeline 51 from the recirculation pipeline 44, and then enters the second heating gas inlet pipeline 51 or other external gas mixed with the other external gas or external gas from the other heating gas inlet pipeline 51. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the third variation of the another step of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection of the one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 8), and the recirculation pipeline 44 is further matched to form a positive pressure type, so that the gas obtained after the second desorption and concentration of the carbon dioxide in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and return to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 9), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, a fourth variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane equipment, and the related contents thereof are already described and will not be repeated here. Therefore, a fourth variation of the other step (as shown in fig. 10) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other step, which is not repeated here), and the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 is provided with a first heater 76, and the second regeneration pipeline 724 of the second tower polymer tubular membrane module 72 is provided with a second heater 77 (please refer to the content of the second variation of the other step, which is not repeated here), and the difference from the fourth variation of the other step is that the heat energy pipeline 74 connected with the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second polymer tubular membrane module 72 is connected with a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas pipeline 24 of the first carbon dioxide adsorption rotor 20, the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein one end of the cold side pipeline 901 of the heat exchanger 90 is connected with the other end of the heat energy pipeline 74, the other end of the cold side pipeline 901 of the heat exchanger 90 is external air or connected with cooling gas so as to enter the cold side pipeline 901 of the heat exchanger 90 for heat exchange, then the heat energy pipeline 74 is used for conveying high-temperature hot gas into the first regeneration pipeline 714 of the first tower type polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane group 72 for desorption and regeneration, the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the gas after carbon dioxide desorption and concentration at the hot side once in the first desorption gas pipeline 24 can be subjected to heat exchange through the pipeline 902 of the heat exchanger 90, then sent to the cooler 80 for cooling, and finally sent to the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 for adsorption.
In addition, a fifth variation of another step of the present invention is based on the design of the transportation to the double-tower type polymer tubular membrane apparatus in step S200, and the related contents thereof have been described and will not be repeated here. Therefore, a fifth variation of the other step (as shown in fig. 11 and 12) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of the other step, which is not repeated here), and the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 is provided with a first heater 76, the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a second heater 77 (please refer to the content of the second variation of another step, which is not repeated here), and the heat energy pipeline 74 connected with the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is connected with a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas line 24 of the first carbon dioxide adsorption rotor 20, and the heat exchanger 90 is provided with a cold side duct 901 and a hot side duct 902 (please refer to the content of the fourth variation of the other step, which is not repeated here), a fourth variant difference from the other step is that the second desorption gas line 43 is provided with a recirculation line 44, one end of the recycling pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recycling pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed twice by the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recycling pipeline 44, and then enter the second heating device 50 after being mixed with the outside air or other source gas in the second heating gas inlet pipeline 51, or when the second heating air intake line 51 gas alone is not mixed with outside air or other sources of gas. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the fifth variation of the other step of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 11), and the recirculation pipeline 44 is matched to form a positive pressure type, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorption gas pipeline 43 can be squeezed into the recirculation pipeline 44 and returned to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 12), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, a sixth variation of another step of the present invention is based on the design of the transportation to the double-column type polymeric pipe membrane apparatus in the above step S200, and the related contents thereof have been described and will not be repeated here. Therefore, a sixth variation of another step (as shown in fig. 13) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which is not repeated here), and the difference from the first variation of another step is that the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane module 72 is provided with a heater 78, wherein the heater 78 is any one of an electric heater, a natural gas heater, a heat exchanger or a heat medium oil heat exchanger, and the high-temperature hot gas generated by the heater 78 of the heat energy pipeline 74 is delivered into the first regeneration pipeline 714 or the second regeneration pipeline 724 and then re-enters the first adsorption tower 711 in the first tower polymer tubular membrane module 71 or the second adsorption tower 721 in the second tower polymer tubular membrane module 72 for regeneration, and the flow direction is controlled by the valve 7141 of the first regeneration pipeline 714 and the valve 7241 of the second regeneration pipeline 7241.
In addition, a seventh variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane device, and the related contents thereof are already described and will not be repeated here. Therefore, a seventh variation of another step (as shown in fig. 14 and 15) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 is provided with a heater 78 (please refer to the content of the sixth variation of another step, which is not repeated here), and the difference from the sixth variation of another step is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating inlet pipeline 51, so that the gas desorbed and concentrated by the secondary carbon dioxide delivered by the second desorption gas pipeline 43 can be returned to the second heating inlet pipeline 51 from the recirculation pipeline 44, and then enters the second heating inlet pipeline 51 or other external gas mixed with the other external gas or external gas from the second heating inlet pipeline 51 for heating. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the seventh variation of the above-mentioned another step of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 14), and the second desorption gas pipeline 43 is matched with the recirculation pipeline 44 to form a positive pressure type, so that the gas obtained after the second desorption of carbon dioxide in the second desorption gas pipeline 43 and the concentration thereof can be pushed into the recirculation pipeline 44 and return to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 15), and the fan 511 disposed on the second heating gas inlet pipeline 511 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
In addition, an eighth variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane device, and the related contents thereof are already described and will not be repeated here. Therefore, an eighth variation of another step (as shown in fig. 16) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane module 72 is provided with a heater 78 (please refer to the content of the sixth variation of another step, which is not repeated here), and the difference from the sixth variation of another step is that the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second polymer tubular membrane module 72 is connected to a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas pipeline 24 of the first carbon dioxide adsorption rotor 20, the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein one end of the cold side pipeline 901 of the heat exchanger 90 is connected with the other end of the heat energy pipeline 74, the other end of the cold side pipeline 901 of the heat exchanger 90 is external air or connected with cooling gas so as to enter the cold side pipeline 901 of the heat exchanger 90 for heat exchange, then the heat energy pipeline 74 is used for conveying high-temperature hot gas into the first regeneration pipeline 714 of the first tower type polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane group 72 for desorption and regeneration, the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the gas after carbon dioxide desorption and concentration at the hot side once in the first desorption gas pipeline 24 can be subjected to heat exchange through the pipeline 902 of the heat exchanger 90, then sent to the cooler 80 for cooling, and finally sent to the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 for adsorption.
In addition, a ninth variation of another step of the present invention is based on the design of the transportation of the step S200 to the twin-column type polymer tubular membrane equipment, and the related contents thereof are already described and will not be repeated here. Therefore, a ninth variation of another step (as shown in fig. 17 and 18) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is provided with a heater 78 (please refer to the content of the sixth variation of another step, which is not repeated here), and the heat energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower type polymer tubular membrane module 71 and the second regeneration pipeline 724 of the second tower type polymer tubular membrane module 72 is connected to a heat exchanger 90, and the heat exchanger 90 is provided on the first desorption gas line 24 of the first carbon dioxide adsorption rotor 20, and the heat exchanger 90 is provided with a cold side duct 901 and a hot side duct 902 (please refer to the content of the eighth variation of the further step, which is not repeated here), an eighth variation from the other step is that the second desorption gas line 43 is provided with a recirculation line 44, one end of the recycling pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recycling pipeline 44 is connected to the second heating gas inlet pipeline 51, so that the gas desorbed and concentrated by the carbon dioxide desorbed twice by the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recycling pipeline 44, and then enter the second heating device 50 after being mixed with the outside air or other source gas in the second heating gas inlet pipeline 51, or when the second heating air intake line 51 gas alone is not mixed with outside air or other sources of gas. Wherein the recirculation line 44 is provided with a valve 441, so that the gas flow direction of the recirculation line 44 is controlled by the valve 441.
In the ninth variation of the above another step of the present invention, the second desorption gas pipeline 43 has two variations, wherein the first variation is that the front end and the rear end of the second desorption gas pipeline 43 at the connection position of one end of the recirculation pipeline 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in fig. 17), and the recirculation pipeline 44 is further matched to form a positive pressure type, so that the gas after the carbon dioxide desorbed and concentrated in the second desorption gas pipeline 43 for the second time can be squeezed into the recirculation pipeline 44 and returned to the second heating gas inlet pipeline 51. In a second modification, a fan 431 is disposed on the second desorption gas pipeline 43, a fan 511 is disposed on the second heating gas inlet pipeline 51 (as shown in fig. 18), and the fan 511 disposed on the second heating gas inlet pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating gas inlet pipeline 51 and close to the second heating device 50, and is matched with the fan 431 disposed on the second desorption gas pipeline 43 to form a negative pressure state, so that the gas desorbed and concentrated by the carbon dioxide desorbed and concentrated secondarily from the second desorption gas pipeline 43 can return to the second heating gas inlet pipeline 51 through the recirculation pipeline 44.
From the above detailed description, it will be apparent to those skilled in the art that the foregoing objects and advantages of the invention are achieved and attained by a method in accordance with the specification of the patent claims.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (45)

1. A carbon dioxide adsorption rotary wheel processing system comprising:
one side of the pretreatment equipment is connected with a gas inlet pipeline;
the first carbon dioxide adsorption rotating wheel is provided with an adsorption area and a desorption area, the first carbon dioxide adsorption rotating wheel is connected with a pretreatment gas pipeline, a first purified gas discharge pipeline, a first hot gas conveying pipeline and a first desorption gas pipeline, one end of the pretreatment gas pipeline is connected with the other side of the pretreatment equipment, the other end of the pretreatment gas pipeline is connected to one side of the adsorption area of the first carbon dioxide adsorption rotating wheel, one end of the first purified gas discharge pipeline is connected with the other side of the adsorption area of the first carbon dioxide adsorption rotating wheel, one end of the first hot gas conveying pipeline is connected with the other side of the desorption area of the first carbon dioxide adsorption rotating wheel, and one end of the first desorption gas pipeline is connected with one side of the desorption area of the first carbon dioxide adsorption rotating wheel;
the first heating device is provided with a first heating air inlet pipeline and is connected with the other end of the first hot air conveying pipeline of the first carbon dioxide adsorption rotating wheel;
the second carbon dioxide adsorption rotating wheel is provided with an adsorption area and a desorption area, the second carbon dioxide adsorption rotating wheel is connected with a second purified gas discharge pipeline, a second hot gas conveying pipeline and a second desorption gas pipeline, one side of the adsorption area of the second carbon dioxide adsorption rotating wheel is connected with the other end of the first desorption gas pipeline, one end of the second purified gas discharge pipeline is connected with the other side of the adsorption area of the second carbon dioxide adsorption rotating wheel, one end of the second hot gas conveying pipeline is connected with the other side of the desorption area of the second carbon dioxide adsorption rotating wheel, and one end of the second desorption gas pipeline is connected with one side of the desorption area of the second carbon dioxide adsorption rotating wheel;
the second heating device is provided with a second heating air inlet pipeline and is connected with the other end of the second hot air conveying pipeline of the second carbon dioxide adsorption rotating wheel; and
and the chimney is connected with the other end of the first purified gas discharge pipeline of the first carbon dioxide adsorption rotating wheel and the other end of the second purified gas discharge pipeline of the second carbon dioxide adsorption rotating wheel.
2. The carbon dioxide adsorbing rotary wheel processing system according to claim 1, wherein the pre-processing gas pipeline is further provided with a blower.
3. The carbon dioxide adsorption rotor processing system of claim 1, wherein the first clean gas discharge line is further provided with a fan.
4. The carbon dioxide adsorption rotor processing system of claim 1, wherein the second clean gas discharge line is further provided with a fan.
5. The carbon dioxide adsorption rotary wheel processing system according to claim 1, wherein the first desorption gas pipeline is further provided with a fan.
6. The carbon dioxide adsorption rotary wheel processing system according to claim 1, wherein the second desorption gas pipeline is further provided with a fan.
7. The carbon dioxide adsorbing rotor processing system according to claim 1, wherein the first heated inlet conduit is further provided with a blower.
8. The carbon dioxide adsorbing rotor processing system according to claim 1, wherein the second heated inlet conduit is further provided with a fan.
9. The carbon dioxide adsorption rotary processing system of claim 1, wherein the pre-processing equipment is further any one of a chiller, a condenser, a dehumidifier, and a desuperheater.
10. The carbon dioxide adsorption rotary wheel processing system according to claim 1, wherein the second desorption gas pipeline is further provided with a recirculation pipeline, one end of the recirculation pipeline is connected with the second desorption gas pipeline, and the other end of the recirculation pipeline is connected with the second heating air inlet pipeline.
11. The carbon dioxide adsorbing rotary wheel processing system according to claim 10, wherein the second desorption gas pipeline further comprises a first fan and a second fan respectively disposed at the front end and the rear end of the connection of one end of the recirculation pipeline.
12. The carbon dioxide adsorption rotary wheel processing system according to claim 10, wherein the second desorption gas pipeline is further provided with a fan, the second heating air inlet pipeline is further provided with a fan, and the fan of the second heating air inlet pipeline is located at the rear end of the connection of the recirculation pipeline and the second heating air inlet pipeline and close to the second heating device.
13. The carbon dioxide adsorption rotary wheel processing system according to claim 1, wherein the first desorption gas pipeline is further provided with a cooling device.
14. The carbon dioxide adsorption rotary wheel processing system according to claim 1, wherein the other end of the second desorption gas pipeline of the second carbon dioxide adsorption rotary wheel is further connected to a double-tower type polymer tubular membrane device, the double-tower type polymer tubular membrane device is provided with a first tower type polymer tubular membrane group and a second tower type polymer tubular membrane group, the first tower type polymer tubular membrane group is provided with a first adsorption tower, a first air inlet pipeline, a first exhaust pipeline, a first regeneration pipeline and a first compressed gas pipeline, and the second tower type polymer tubular membrane group is provided with a second adsorption tower, a second air inlet pipeline, a second exhaust pipeline, a second regeneration pipeline and a second compressed gas pipeline.
15. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first exhaust pipeline of the first tower polymer tubular membrane module and the second exhaust pipeline of the second tower polymer tubular membrane module are further connected to an exhaust output pipeline.
16. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first compressed gas pipeline of the first tower polymer tubular membrane module and the second compressed gas pipeline of the second tower polymer tubular membrane module are further connected to a compressed gas output pipeline.
17. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first regeneration pipeline of the first tower type polymer tubular membrane module is further provided with a first heater, and the second regeneration pipeline of the second tower type polymer tubular membrane module is further provided with a second heater.
18. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first gas inlet pipeline, the first gas outlet pipeline, the first regeneration pipeline and the first compressed gas pipeline of the first tower type polymer tubular membrane module are further provided with valves, and the second gas inlet pipeline, the second gas outlet pipeline, the second regeneration pipeline and the second compressed gas pipeline of the second tower type polymer tubular membrane module are further provided with valves.
19. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first adsorption tower of the first tower type polymer tubular membrane module and the second adsorption tower of the second tower type polymer tubular membrane module are further filled with a plurality of hollow tubular polymer tubular membrane adsorbing materials, and the hollow tubular polymer tubular membrane adsorbing materials are made of polymer and adsorbent.
20. The carbon dioxide adsorption rotary wheel processing system according to claim 14, wherein the first regeneration pipeline of the first tower type polymer tubular membrane module and the second regeneration pipeline of the second tower type polymer tubular membrane module are further connected to a heat energy pipeline.
21. The carbon dioxide adsorption rotary wheel processing system according to claim 20, wherein the heat energy pipeline is further provided with a heater, and the heater is any one of an electric heater, a natural gas type heater, a heat exchanger or a heat transfer oil heat exchanger.
22. The system of claim 20, wherein the thermal pipeline is further connected to a heat exchanger, the heat exchanger is disposed on the first desorption gas pipeline of the first carbon dioxide adsorption rotor, the heat exchanger is provided with a cold side pipeline and a hot side pipeline, the thermal pipeline is connected to the cold side pipeline of the heat exchanger, and the first desorption gas pipeline is connected to the hot side pipeline of the heat exchanger.
23. A carbon dioxide adsorption rotating wheel processing method is mainly used for a carbon dioxide adsorption rotating wheel system and is provided with pretreatment equipment, a first carbon dioxide adsorption rotating wheel, a first heating device, a second carbon dioxide adsorption rotating wheel, a second heating device and a chimney, wherein the first carbon dioxide adsorption rotating wheel is provided with an adsorption area and a desorption area, the first carbon dioxide adsorption rotating wheel is connected with a pretreatment air inlet pipeline, a first purified gas discharge pipeline, a first hot gas conveying pipeline and a first desorption gas pipeline, the second carbon dioxide adsorption rotating wheel is provided with an adsorption area and a desorption area, the second carbon dioxide adsorption rotating wheel is connected with a second purified gas discharge pipeline, a second hot gas conveying pipeline and a second desorption gas pipeline, the first heating device is provided with a first heating air inlet pipeline, the second heating device is provided with a second heating air inlet pipeline, the pretreatment equipment is provided with a gas inlet pipeline, and the main steps of the processing method comprise:
gas input into the pretreatment apparatus: sending the gas into the pretreatment equipment through the gas inlet pipeline for treatment;
the first carbon dioxide adsorption rotating wheel is used for adsorption: outputting the gas treated by the pretreatment equipment to one side of the adsorption area of the first carbon dioxide adsorption rotating wheel from the other end of the pretreatment gas pipeline so as to adsorb carbon dioxide;
first carbon dioxide adsorption wheel emission: outputting the gas generated by the adsorption zone of the first carbon dioxide adsorption rotating wheel after carbon dioxide adsorption to the chimney for emission from the other end of the first purified gas emission pipeline;
conveying first hot gas for desorption: high-temperature hot gas is conveyed to a desorption area of the first carbon dioxide adsorption rotating wheel through a first hot gas conveying pipeline connected with the first heating device for desorption;
outputting the gas after carbon dioxide desorption and concentration: the gas which is subjected to carbon dioxide desorption concentration and is desorbed once and generated in the desorption area of the first carbon dioxide adsorption rotating wheel is output from the other end of the first desorption gas pipeline;
and (3) adsorbing by a second carbon dioxide adsorption rotating wheel: conveying the gas subjected to the desorption and concentration of the carbon dioxide desorbed and concentrated once in the first desorption gas pipeline to one side of the adsorption area of the second carbon dioxide adsorption rotating wheel for re-adsorption;
and (3) discharging the second carbon dioxide adsorption runner: outputting the gas generated by the adsorption zone of the second carbon dioxide adsorption rotating wheel after carbon dioxide adsorption to the chimney for emission from the other end of the second purified gas emission pipeline;
conveying second hot gas for desorption: high-temperature hot gas is conveyed to a desorption area of the second carbon dioxide adsorption rotating wheel through a second hot gas conveying pipeline connected with the second heating device for desorption; and
outputting the gas after carbon dioxide desorption and concentration: the gas which is subjected to the desorption concentration of the carbon dioxide and is subjected to secondary desorption generated in the desorption area of the second carbon dioxide adsorption rotating wheel is output from the other end of the second desorption gas pipeline.
24. The carbon dioxide adsorbing rotary wheel processing method as claimed in claim 23, wherein the pre-processing gas pipeline is further provided with a blower.
25. The carbon dioxide adsorption rotary wheel processing method according to claim 23, wherein the first clean gas discharge pipeline is further provided with a fan.
26. The carbon dioxide adsorption rotary wheel processing method according to claim 23, wherein the second clean gas discharge pipeline is further provided with a fan.
27. The process for treating a carbon dioxide adsorbing rotary wheel according to claim 23, wherein the first desorption gas pipeline is further provided with a fan.
28. The carbon dioxide adsorption rotary wheel processing method according to claim 23, wherein the second desorption gas line is further provided with a fan.
29. The carbon dioxide adsorbing rotary wheel processing method as recited in claim 23, wherein the first heating inlet pipeline is further provided with a fan.
30. The carbon dioxide adsorbing rotary wheel processing method as recited in claim 23, wherein the second heating inlet pipeline is further provided with a fan.
31. The method as claimed in claim 23, wherein the pre-treatment equipment is any one of a cooler, a condenser, a dehumidifier and a desuperheater.
32. The method as claimed in claim 23, wherein the second desorption gas pipeline is further provided with a recirculation pipeline, one end of the recirculation pipeline is connected to the second desorption gas pipeline, and the other end of the recirculation pipeline is connected to the second heating gas inlet pipeline.
33. The method for processing a carbon dioxide adsorbing rotor according to claim 32, wherein the second desorption gas line further comprises a first fan and a second fan respectively disposed at the front end and the rear end of the connection of one end of the recycle line.
34. The process for carbon dioxide adsorption rotor processing according to claim 32, wherein the second desorption gas line is further provided with a fan, and the second heating gas inlet line is further provided with a fan, and the fan of the second heating gas inlet line is located at the rear end of the connection of the recirculation line and the second heating gas inlet line and near the second heating device.
35. The process for treating a carbon dioxide adsorbing wheel according to claim 23, wherein the first desorption gas pipeline is further provided with a cooling device.
36. The carbon dioxide adsorption rotary wheel processing method according to claim 23, further comprising the following steps after the step of outputting the carbon dioxide desorption concentrated gas:
conveying to a double-tower type polymer tubular membrane device: and conveying the gas subjected to the desorption and concentration of the carbon dioxide desorbed and concentrated for the second time in the second desorption gas pipeline into double-tower type polymer tubular membrane equipment for treatment.
37. The process of claim 36, wherein the twin-tower polymer tubular membrane facility comprises a first tower polymer tubular membrane module and a second tower polymer tubular membrane module, the first tower polymer tubular membrane module comprises a first adsorption tower, a first gas inlet pipeline, a first gas outlet pipeline, a first regeneration pipeline and a first compressed gas pipeline, and the second tower polymer tubular membrane module comprises a second adsorption tower, a second gas inlet pipeline, a second gas outlet pipeline, a second regeneration pipeline and a second compressed gas pipeline.
38. The method for processing the carbon dioxide adsorbing rotor as recited in claim 37, wherein the first exhaust line of the first tower polymer tubular membrane module and the second exhaust line of the second tower polymer tubular membrane module are further connected to the exhaust outlet line.
39. The carbon dioxide adsorption rotary wheel processing method according to claim 37, wherein the first compressed gas pipeline of the first tower polymer tubular membrane module and the second compressed gas pipeline of the second tower polymer tubular membrane module are further connected to a compressed gas output pipeline.
40. The carbon dioxide adsorption rotary wheel processing method according to claim 37, wherein the first regeneration pipeline of the first tower type polymer tubular membrane module is further provided with a first heater, and the second regeneration pipeline of the second tower type polymer tubular membrane module is further provided with a second heater.
41. The method for processing a carbon dioxide adsorbing rotor as recited in claim 37, wherein the first inlet gas line, the first exhaust gas line, the first regeneration line and the first compressed gas line of the first tower type polymer tubular membrane module are further provided with valves, and the second inlet gas line, the second exhaust gas line, the second regeneration line and the second compressed gas line of the second tower type polymer tubular membrane module are further provided with valves.
42. The method as claimed in claim 37, wherein the first adsorption tower of the first tower type polymer tubular membrane module and the second adsorption tower of the second tower type polymer tubular membrane module are further filled with a plurality of hollow tubular polymer tubular membrane adsorbing materials, and the hollow tubular polymer tubular membrane adsorbing materials are made of polymer and adsorbent.
43. The carbon dioxide adsorption rotary wheel processing method according to claim 37, wherein the first regeneration pipeline of the first tower type polymer tubular membrane module and the second regeneration pipeline of the second tower type polymer tubular membrane module are further connected with a heat energy pipeline.
44. The carbon dioxide adsorption rotary wheel processing method according to claim 43, wherein the heat energy pipeline is further provided with a heater, and the heater is any one of an electric heater, a natural gas type heater, a heat exchanger or a heat transfer oil heat exchanger.
45. The process of claim 43, wherein the thermal energy pipeline is further connected to a heat exchanger, the heat exchanger is disposed on the first desorption gas pipeline of the first carbon dioxide adsorption rotor, the heat exchanger is provided with a cold side pipeline and a hot side pipeline, the thermal energy pipeline is connected to the cold side pipeline of the heat exchanger, and the first desorption gas pipeline is connected to the hot side pipeline of the heat exchanger.
CN202111010888.3A 2021-07-20 2021-08-31 Carbon dioxide adsorption rotating wheel system and method thereof Pending CN115634550A (en)

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