TWI765783B - Tandem carbon dioxide adsorption rotor system and method thereof - Google Patents

Abstract

The present invention is a series carbon dioxide adsorption rotor system and its method, which are mainly used in carbon dioxide treatment systems, and are provided with a pretreatment device, a first carbon dioxide adsorption rotor, a first heating device, and a second carbon dioxide adsorption rotor. wheel, a second heating device and a chimney, through connecting two carbon dioxide adsorption runners in series, and the gas after desorption and concentration of carbon dioxide desorbed once generated in the desorption zone of the second carbon dioxide adsorption runner is transported to the first In the desorption zone of a carbon dioxide adsorption runner, the desorption zone of the first carbon dioxide adsorption runner is used to generate the gas after the desorption and concentration of carbon dioxide for secondary desorption, so that the concentration efficiency of carbon dioxide can be increased, and the energy The efficiency of concentration and recovery of carbon dioxide.

Description

Tandem carbon dioxide adsorption rotor system and method thereof

The present invention relates to a series-type carbon dioxide adsorption runner system and a method thereof, in particular to a system that can increase the concentration efficiency of carbon dioxide and has the effect of concentrating and recovering carbon dioxide, and is suitable for semiconductor industry, optoelectronic industry, chemical related industry or manufacturing related industry. Industrial CO2 treatment systems or similar equipment.

In recent years, environmental protection has become a topic of concern to every country in the world, especially the part of greenhouse gases. At present, the largest part of greenhouse gases is the emission of carbon dioxide ( _CO2 ), of which carbon dioxide ( _CO2) is a common compound in the air. It is composed of two An oxygen atom is connected to a carbon atom by a polar covalent bond.

Since the Industrial Revolution, human beings have used a large amount of fossil fuels (such as coal and oil) for the development of industry and civilization, coupled with the continuous deforestation of tropical rain forests to increase the area of farming, these improper human activities have produced excessive greenhouse gases, which greatly enhanced the The greenhouse effect disrupts the long-term energy balance, resulting in an increase in the temperature of the earth's surface, leading to global warming.

In order to cope with the impact of global warming, the United Nations adopted the United Nations Framework Convention on Climate Change (UNFCCC) in New York in 1992, hoping that through the efforts of various countries, the concentration of greenhouse gases in the atmosphere will be stabilized, so that human beings can develop economy and civilization. At the same time, it can also protect the earth's ecosystem from threats. Afterwards, many conferences on climate change were jointly held, and the goals of the Outline Convention on Climate Change were clearly defined in the following agreements: 1. Kyoto Protocol, 2. Paris Agreement. Other In addition, the European Union announced the European Green Policy in 2019, proposing to achieve the goal of "carbon neutrality" by 2050, which offsets the increase and decrease of carbon emissions, so as to control the global temperature rise within 1.5 degrees Celsius by the end of this century.

In recent years, the government has attached great importance to air pollution, so it has formulated relevant air quality standards in the emission standards of chimneys, and will review it periodically in accordance with the development of international control trends.

Therefore, in view of the above deficiencies, the present inventor hopes to propose a series-type carbon dioxide adsorption rotor system and a method thereof capable of concentrating and recovering carbon dioxide, so that users can easily operate and assemble. In order to provide user convenience, it is the motive of the invention that the inventor intends to develop.

The main purpose of the present invention is to provide a series carbon dioxide adsorption rotor system and method thereof, which are mainly used in carbon dioxide treatment systems, and are provided with a pretreatment equipment, a first carbon dioxide adsorption rotor, a first heating device, a The second carbon dioxide adsorption runner, a second heating device and a chimney are connected in series with two carbon dioxide adsorption runners to desorb and concentrate the desorbed carbon dioxide generated in the desorption zone of the second carbon dioxide adsorption runner. The gas is transported to the desorption zone of the first carbon dioxide adsorption runner, and then the desorption zone of the first carbon dioxide adsorption runner is used to generate the gas after the second desorption of carbon dioxide desorption and concentration, so that the concentration of carbon dioxide can be increased. efficiency, and has the effect of concentrating and recovering carbon dioxide, thereby increasing the overall practicability.

Another object of the present invention is to provide a series-type carbon dioxide adsorption runner system and method thereof. The membrane equipment is connected, so that the gas after the desorption and concentration of the secondary desorbed carbon dioxide can be recompressed through the double-tower polymer tubular membrane equipment to form a carbon dioxide compressed dry gas, and the recompressed carbon dioxide is compressed. dry gas permeable It can be stored in steel cylinders and steel tanks, or transported and supplied to other places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola farms, chemical plants, or food industry factories and other industries, as raw materials to let carbon dioxide The compressed dry gas can have the effect of subsequent application, thereby increasing the overall usability.

Another object of the present invention is to provide a series-type carbon dioxide adsorption rotor system and method thereof, wherein a recirculation pipeline is connected through the first desorption gas pipeline, and one end of the recirculation pipeline is connected to the first desorption gas pipeline. Attached gas pipeline, the other end of the recirculation pipeline is connected to the second desorption gas pipeline, so that the gas after the desorption and concentration of the secondary desorbed carbon dioxide can be returned to the second desorption through the recirculation pipeline The gas is mixed in the pipeline and reheated by the first heating device, and then transported to the desorption zone of the first carbon dioxide adsorption runner for desorption, so that it has the effect of continuous recirculation and allows the carbon dioxide to be desorbed. The desorption concentration can be increased from the inlet concentration of 6% to the post-desorption concentration of 40% to 99%, thereby increasing the overall operability.

In order to further understand the features, characteristics and technical content of the present invention, please refer to the following detailed description of the present invention and the accompanying drawings, but the accompanying drawings are only for reference and description, and are not intended to limit the present invention.

10: Pretreatment equipment

11: Gas intake line

20: The first carbon dioxide adsorption runner

201: Adsorption Zone

202: Desorption zone

21: Pretreatment gas pipeline

211: Fan

22: The first clean air pipeline

23: The first hot gas delivery pipeline

24: The first desorption gas pipeline

241: Fan

242: The first fan

243: Second fan

25: Recirculation line

251: Valve

30: The first heating device

40: Second carbon dioxide adsorption runner

401: adsorption zone

402: Desorption zone

41: Second clean air discharge pipeline

411: Fan

42: Second hot gas delivery pipeline

43: Second desorption gas pipeline

50: Second heating device

51: Second heated intake line

511: Fan

60: Chimney

70: Double tower polymer tubular membrane equipment

71: The first tower polymer tubular membrane group

711: The first adsorption tower

712: First intake line

7121: Valve

713: First exhaust line

7131: Valve

714: First regeneration line

7141: Valve

715: First compressed gas line

7151: Valve

72: The second tower polymer tubular membrane group

721: Second adsorption tower

722: Second intake line

7221: Valve

723: Second exhaust line

7231: Valve

724: Second regeneration line

7241: Valve

725: Second compressed gas line

7251: Valve

73: Exhaust output pipeline

74: Thermal energy pipeline

75: Compressed gas output pipeline

76: First heater

77: Second heater

78: Heater

S100: Gas input pretreatment equipment

S110: First carbon dioxide adsorption rotor adsorption

S120: Second carbon dioxide adsorption rotor adsorption

S130: Second carbon dioxide adsorption runner emissions

S140: transport the second hot gas for desorption

S150: output the gas after carbon dioxide desorption and concentration

S160: transporting the first hot gas for desorption

S170: output the gas after carbon dioxide desorption and concentration

S200: transported to double-tower polymer tubular membrane equipment

FIG. 1 is a schematic diagram of a system architecture according to a main embodiment of the present invention.

FIG. 2 is a schematic diagram of a system architecture with a fan according to a main embodiment of the present invention.

FIG. 3 is a schematic diagram of a first variation system architecture according to the main embodiment of the present invention.

FIG. 4 is a schematic diagram of a second variation system architecture according to the main embodiment of the present invention.

FIG. 5 is a schematic diagram of a system architecture according to another embodiment of the present invention.

FIG. 6 is a schematic diagram of a system structure with a fan according to another embodiment of the present invention.

FIG. 7 is a schematic diagram of a first variation system architecture according to another embodiment of the present invention.

FIG. 8 is a schematic diagram of a second variation system architecture according to another embodiment of the present invention.

FIG. 9 is a schematic diagram of a system architecture of another variant of the second variation of another embodiment of the present invention.

FIG. 10 is a schematic diagram of a third variation system architecture according to another embodiment of the present invention.

FIG. 11 is a schematic diagram of a fourth variation system architecture according to another embodiment of the present invention.

FIG. 12 is a schematic diagram of a system architecture of another modification of the fourth variation of another embodiment of the present invention.

Fig. 13 is a flow chart of the main steps of the present invention.

Fig. 14 is a flow chart of another step of the present invention.

Please refer to FIGS. 1 to 14, which are schematic diagrams of an embodiment of the present invention, and the best embodiment of the tandem carbon dioxide adsorption rotor system and method thereof of the present invention is applied in the semiconductor industry, optoelectronic industry, chemical-related industry or manufacturing The carbon dioxide treatment system or similar equipment of related industries can mainly increase the concentration efficiency of carbon dioxide, and have the effect of concentration and recovery of carbon dioxide.

The tandem carbon dioxide adsorption rotor system of the present invention mainly includes a pretreatment device 10, a first carbon dioxide adsorption rotor 20, a first heating device 30, a second carbon dioxide adsorption rotor 40, a second heating device The device 50 and a chimney 60 (as shown in Figures 1 to 12), wherein one side of the pretreatment equipment 10 is connected to a gas inlet pipe 11, and one end of the gas inlet pipe 11 is connected to To places where carbon dioxide is generated, such as manufacturing sites, office buildings, or areas where carbon dioxide is generated indoors (not shown in the figure), so that the gas The intake line 11 can transport gas containing carbon dioxide or other gases, and the pretreatment equipment 10 is any one of a cooler, a condenser, a dehumidifier, and a desuperheater, so as to pre-treat the gas so that the The gas can release thermal energy to improve the adsorption efficiency. In addition, the second heating device 50 is provided with a second heating air intake pipe 51 (as shown in FIG. 1 to FIG. 12 ), and the first heating device 30 and the second heating device 50 are electric heaters, Any of natural gas heaters, heat exchangers, heat medium oil heat exchangers, shell and tube heat exchangers, fin-and-tube heat exchangers, plate heat exchangers or heat pipe heat exchangers.

In addition, the first carbon dioxide adsorption rotor 20 of the present invention is provided with an adsorption zone 201 and a desorption zone 202. The first carbon dioxide adsorption rotor 20 is connected with a pretreatment gas pipeline 21, a first purification gas pipeline 22, a The first hot gas conveying pipeline 23 and a first desorption gas pipeline 24 (as shown in FIG. 1 to FIG. 12 ), and the second carbon dioxide adsorption runner 40 is provided with an adsorption zone 401 and a desorption zone 402 , the second carbon dioxide adsorption runner 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 Figures 1 to 12). ). The first carbon dioxide adsorption runner 20 and the second carbon dioxide adsorption runner 40 are respectively zeolite concentration runners or concentration runners made of other materials.

One end of the pretreatment gas pipeline 21 is connected to the other side of the pretreatment device 10 , and the other end of the pretreatment gas pipeline 21 is connected to one end of the adsorption zone 201 of the first carbon dioxide adsorption runner 20 . On the other hand, the carbon dioxide-containing gas or other gas that has been pretreated by the pretreatment equipment 10 can be transported to the adsorption zone 201 of the first carbon dioxide adsorption runner 20 through the pretreatment gas pipeline 21 to carry out Carbon dioxide adsorption (as shown in Figures 1 to 4). The pretreatment gas pipeline 21 is provided with an air The blower 211 (as shown in FIG. 2 and FIG. 4 ) enables the pre-treated gas containing carbon dioxide or other gas in the pretreatment gas pipeline 21 to be pushed and pulled to the first carbon dioxide through the fan 211 In the adsorption zone 201 of the adsorption wheel 20 . In addition, one end of the first clean air pipeline 22 is connected to the other side of the adsorption zone 201 of the first carbon dioxide adsorption runner 20 (as shown in FIG. 1 to FIG. 4 ), and the first clean air pipeline 22 The other end is connected to the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 (as shown in Figures 1 to 4), so that the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 is adsorbed. The produced carbon dioxide adsorbed gas can be transported to the adsorption zone 401 of the second carbon dioxide adsorption runner 40 through the first clean gas pipeline 22 for re-adsorption.

In addition, the other side of the adsorption area 401 of the second carbon dioxide adsorption runner 40 is connected to one end of the second clean gas discharge line 41 , and the other end of the second clean gas discharge line 41 is connected to the chimney 60 Connect (as shown in Figures 1 to 4), so that the gas after carbon dioxide adsorption generated by the adsorption zone 401 of the second carbon dioxide adsorption runner 40 after re-adsorption can be discharged through the second clean gas Line 41 is delivered to the stack 60 for venting to the atmosphere. The second clean air discharge line 41 is provided with a fan 411 (as shown in FIG. 2 and FIG. 4 ), so that the carbon dioxide in the second clean air discharge line 41 can be adsorbed through the fan 411 . The gas is pushed and pulled to the chimney 60 for discharge.

In addition, the other side of the desorption zone 402 of the second carbon dioxide adsorption runner 40 is connected to one end of the second hot gas conveying pipe 42, and the other end of the second hot gas conveying pipe 42 is connected to the second heating pipe The device 50 is connected (as shown in FIG. 1 to FIG. 4 ), and the second heating device 50 is inputted by the second heating air inlet line 51 to input external air or other sources of gas to allow the second heating The device 50 can convert the external input from the second heated intake line 51 The gas or gas from other sources is heated to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 is transported to the second carbon dioxide adsorption runner 40 through the second hot gas conveying pipeline 42 . Desorption zone 402 is used for desorption. The second heating air intake pipe 51 is provided with a fan 511 (as shown in FIG. 2 and FIG. 4 ), so that the outside air in the second heating air intake pipe 51 or the outside air in the second heating air intake pipe 51 can be passed through the fan 511 . The gas from other sources is pushed and pulled into the second heating device 50 .

One side of the desorption zone 402 of the second carbon dioxide adsorption runner 40 is connected to one end of the second desorption gas pipeline 43, and the other end of the second desorption gas pipeline 43 is connected to the first desorption gas pipeline 43. The heating device 30 is connected (as shown in FIG. 1 to FIG. 4 ), so as to be able to desorb and concentrate the desorbed carbon dioxide generated by the desorption zone 402 of the second carbon dioxide adsorption runner 40. It is sent to the first heating device 30 through the second desorption gas pipeline 43 for heating. In addition, the other side of the desorption zone 202 of the first carbon dioxide adsorption runner 20 is connected to one end of the first hot gas conveying pipe 23, and the other end of the first hot gas conveying pipe 23 is connected to the first heating pipe The device 30 is connected (as shown in FIG. 1 to FIG. 4 ), so that the first heating device 30 can heat the gas after the desorption and concentration of the desorbed carbon dioxide delivered by the second desorption gas pipeline 43 , to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is transported to the desorption zone 202 of the first carbon dioxide adsorption runner 20 through the first hot gas transport pipeline 23 for desorption use. .

And one side of the desorption zone 202 of the first carbon dioxide adsorption runner 20 is connected to one end of the first desorption gas pipeline 24 (as shown in FIG. 1 to FIG. 4 ), so that the A carbon dioxide adsorption runner 20 is desorbed in the desorption zone 202 to produce secondary desorbed carbon dioxide desorbed and concentrated gas, which is output through the first desorption gas pipeline 24 for output. Subsequent processing. The so-called follow-up treatment (not shown in the figure) includes that the gas after desorption and concentration of carbon dioxide delivered by the first desorption gas pipeline 24 for secondary desorption can be stored through steel cylinders and steel tanks, or transported and supplied to other Places that need carbon dioxide, such as greenhouses or seaweed farms, soda cola farms, chemical plants, or food factories and other industries, as raw materials, so that the desorbed and concentrated gas from the secondary desorption of carbon dioxide can have subsequent applications. the efficacy. The first desorption gas pipeline 24 is provided with a fan 241 (as shown in FIG. 2 and FIG. 4 ), which enables secondary desorption in the first desorption gas pipeline 24 through the fan 241 The gas push-pull output after desorption and concentration of carbon dioxide.

In addition, the first variation of the main embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10 , the first carbon dioxide adsorption wheel 20 , the first heating device 30 , the second carbon dioxide adsorption wheel 40 , the second carbon dioxide adsorption wheel 40 , and the second carbon dioxide adsorption wheel 40 . The design of the heating device 50 and a chimney 60 has already been described and will not be repeated here. Therefore, the first variation of the main embodiment (as shown in FIG. 3) is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25, and one end of the recirculation pipeline 25 is connected to the The first desorption gas pipeline 24, and the other end of the recirculation pipeline 25 is connected to the second desorption gas pipeline 43, so that the second desorbed carbon dioxide delivered by the first desorption gas pipeline 24 is desorbed The gas after desorption can be returned to the second desorption gas pipeline 43 through the recirculation pipeline 25 , and then desorb the concentrated gas with the first desorbed carbon dioxide in the second desorption gas pipeline 43 . After mixing, it enters the first heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

In addition, the second variation of the main embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, first carbon dioxide adsorption rotor 20, first heating device 30, The second carbon dioxide adsorption runner 40 , the second heating device 50 and a chimney 60 are designed, and the related contents thereof have been described and will not be repeated here. Therefore, the second variation of the main embodiment (as shown in FIG. 4 ) is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25 (please refer to the content of the first variation of the main embodiment) , 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 first desorption gas pipeline 24 at the connection of one end of the recirculation pipeline 25 are respectively provided with a first The fan 242 and a second fan 243 are combined with the recirculation pipeline 25 to form a positive pressure type, so that the desorbed and concentrated gas of the second desorbed carbon dioxide in the first desorption gas pipeline 24 can be squeezed into The recirculation line 25 is returned to the second desorption gas line 43 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

Furthermore, another embodiment of the present invention is based on the pretreatment equipment 10, the first carbon dioxide adsorption wheel 20, the first heating device 30, the second carbon dioxide adsorption wheel 40, and the second heating device of the main embodiment. 50 and a chimney 60 are designed, and the related content has been described, and will not be repeated here. Therefore, another embodiment of the present invention (as shown in Fig. 5 to Fig. 12) is mainly that the other end of the first desorption gas pipeline 24 is connected to a double-tower polymer tubular membrane device 70, The gas after desorption and concentration of the carbon dioxide desorbed for the second time in the first desorption gas pipeline 24 can be recompressed through the double-tower polymer tubular membrane device 70 to form carbon dioxide compressed dry gas.

In another embodiment of the present invention, the double-tower polymer tubular membrane equipment 70 is provided with a first tower-type polymer tubular membrane group 71 and a second tower-type polymer tubular membrane group 72, and the The first tower-type polymer tubular membrane group 71 is provided with a first adsorption tower 711, a first intake line 712, a first exhaust line 713, a first regeneration line 714, and a first regeneration line 714. The first compressed gas pipeline 715 (as shown in Figures 5 to 12), and the second tower polymer tubular membrane group 72 is provided with a second adsorption tower 721 and a second intake pipeline 722 , a second exhaust pipeline 723, a second regeneration pipeline 724 and a second compressed gas pipeline 725 (as shown in Figures 5 to 12), and the first tower-type polymer tubular membrane The first intake line 712, the first exhaust line 713, the first regeneration line 714 and the first compressed gas line 715 of the group 71 are each provided with a valve 7121, 7131, 7141, 7151 (as shown in FIG. 5). 12), and the second inlet pipe 722, the second exhaust pipe 723, the second regeneration pipe 724 and the second compressed gas pipe of the second tower polymer tubular membrane group 72 A valve 7221, 7231, 7241, 7251 (as shown in Fig. 5 to Fig. 12) is provided in each of the channels 725 to control the gas flow between the above-mentioned pipelines.

In addition, the first adsorption tower 711 of the first tower polymer tubular membrane group 71 and the second adsorption tower 721 of the second tower polymer tubular membrane group 72 are composed of a plurality of hollow tubular polymer tubes. (as shown in Figures 5 to 12), and the hollow tubular polymer tubular membrane adsorption material is made of high molecular polymer and adsorbent, and the polymer is By 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-co-glycolic acid, A group consisting of polycaprolactone, polyvinyl pyrrolidone, ethylene alcohol vinyl, polydimethylsiloxane, polytetrafluoroethylene and cellulose acetate (CA) at least one of the groups. and made The diameter and outer diameter of the hollow tubular polymer tubular membrane are more than 2mm, so as to have a high specific surface area, easy adsorption and easy desorption, so the dosage of adsorbent is smaller than that of traditional particle type, and the same dynamic adsorption performance can be achieved. , it will naturally use less heat energy to complete the desorption during desorption, so it has an energy-saving effect.

In addition, the adsorbent ratio of the above-mentioned hollow tubular polymer tubular membrane adsorbent material is 10% to 90%, and the adsorbent is in any shape of particle shape, powder shape, hollow fiber shape, and honeycomb shape. (not shown in the figure), wherein the plurality of particles of the powder have a particle size of 0.005 to 50um, and the plurality of particles of the powder have a two-dimensional or three-dimensional hole structure, and the holes are regular or irregular shapes, Wherein the adsorbent is modified by molecular sieve, activated carbon, alkanolamine, A-type zeolite (such as 3A, 4A or 5A), X-type zeolite (such as 13X), Y-type zeolite (such as ZSM-5), medium pore molecular sieve (eg MCM-41, 48, 50 and SBA-15), metal organic frameworks (Metal Organic Frameworks: MOF) or at least one of the group consisting of graphene.

In addition, the above-mentioned hollow tubular polymer tubular membrane adsorbent is made of inorganic materials (not shown in the figure), wherein the size of the added inorganic materials ranges from 0.01um to 100um, and the inorganic materials may contain adsorbents, such as containing When the adsorbent is used, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the above inorganic materials are iron oxide, copper oxide, barium titanate, lead titanate, aluminum oxide, silicon dioxide, gas gel (silica aerogel), bentonite (such as potassium bentonite, sodium bentonite, calcium bentonite and aluminum bentonite), china clay (such as Al 2 O 3.2SiO 2.2H 2 O), hyplas soil (such as 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 (eg Ca 3 SiO 5, Ca 3 Si 2 O 7 and CaSiO 3) , magnesium silicate (such as Mg 3 Si 4 O 10(OH) 2), sodium silicate (such as Na 2 SiO 3 and its hydrate), anhydrous sodium sulfate, zirconium silicate (such as ZrSiO 4), opaque Zirconium (eg 53.89%SiO2.4.46%Al2O3.12.93%ZrO2.9.42%CaO. 2.03%MgO. 12.96%ZnO. 3.73%K 2 O. 0.58% Na 2 O) and at least one of the group consisting of silicon carbide.

In another embodiment of the present invention, the first inlet line 712 of the first tower-type polymer tubular membrane group 71 and the second inlet line 722 of the second tower-type polymer tubular membrane group 72 It is connected with the other end of the first desorption gas pipeline 24 (as shown in Fig. 5 to Fig. 12), so that the gas after the desorption and concentration of the carbon dioxide desorbed by the secondary desorption can be input into the double towers The polymer tubular membrane equipment 70 is used for recompression treatment, and the adsorption drying process and regeneration and desorption are carried out through the first tower polymer tubular membrane group 71 and the second tower polymer tubular membrane group 72 respectively. process, and when the first tower-type polymer tubular membrane group 71 performs the adsorption drying process (as shown in FIG. 5), the valve 7121 of the first air inlet pipeline 712 is in an open state, and the second tower The polymer tubular membrane group 72 is in a regeneration and desorption process, so the valve 7221 of the second intake line 722 is in a closed state, and the valve 7121 of the first intake line 712 is opened for the The gas desorbed and concentrated by the second desorption of carbon dioxide in the first desorption gas pipeline 24 is input into the first adsorption tower 711 in the first tower polymer tubular membrane group 71, and passes through the first adsorption tower 711. The hollow tubular polymer tubular membrane adsorbent in the tower 711 is used for adsorption and drying.

After a period of time, the first tower-type polymer tubular membrane group 71 performs the adsorption drying process before the adsorption is saturated, that is, the second tower-type polymer tubular membrane group 72 is switched to perform the adsorption drying process (such as the first column). 6), and when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process, the valve 7221 of the second inlet line 722 is in an open state, and the first tower-type polymer tube The membrane group 71 is changed to perform the regeneration and desorption process, so the valve 7121 of the first intake line 712 is in a closed state, and the second intake line 712 is in a closed state. The valve of 22 is opened, for the second adsorption tower 721 in the second tower type macromolecule tubular membrane group 72 for the gas after the desorption and concentration of carbon dioxide in the first desorption gas pipeline 24 which has undergone secondary desorption. inside, and through the hollow tubular polymer tubular membrane adsorbent in the second adsorption tower 721 for adsorption and drying.

In another embodiment of the present invention, the first exhaust line 713 of the first tower-type polymer tubular membrane group 71 and the second exhaust line 723 of the second tower-type polymer tubular membrane group 72 are It is connected with an exhaust output pipeline 73 (as shown in Figures 5 to 12), and the other end of the exhaust output pipeline 73 is in the atmosphere or outside air, and when the first tower type When the polymer tubular membrane group 71 is performing the adsorption drying process (as shown in FIG. 5 ), the valve 7131 of the first exhaust pipe 713 is in a closed state, and the second tower-type polymer tubular membrane group 72 is in a closed state. In order to carry out the regeneration and desorption process, the valve 7231 of the second exhaust pipe 723 is in an open state, so that the second adsorption tower 721 of the second tower polymer tubular membrane group 72 for the regeneration and desorption process is carried out. The gas inside can pass through the second exhaust pipe 723 to perform the exhaust action, and when the second tower polymer tubular membrane group 72 performs the adsorption drying process (as shown in FIG. 6), the second row The valve 7231 of the gas pipeline 723 is in a closed state, and the first tower-type polymer tubular membrane group 71 is undergoing a regeneration and desorption process, so the valve 7131 of the first exhaust pipeline 713 is in an open state. , so that the gas in the first adsorption tower 711 of the first tower polymer tubular membrane group 71 performing the regeneration and desorption process can pass through the first exhaust pipe 713 to perform the exhaust action.

In another embodiment of the present invention, the first compressed gas pipeline 715 of the first tower-type polymer tubular membrane group 71 and the second compressed gas pipeline 725 of the second tower-type polymer tubular membrane group 72 are Connected to a compressed gas output line 75 (as shown in Figures 5 to 12 shown), when the first tower-type polymer tubular membrane group 71 performs the adsorption drying process (as shown in FIG. 5), the valve 7151 of the first compressed gas pipeline 715 is in an open state, and the first The two-tower polymer tubular membrane group 72 is in the regeneration and desorption process, so the valve 7251 of the second compressed gas pipeline 725 is in a closed state. The gas can be adsorbed and dried through the hollow tubular polymer tubular membrane adsorption material in the first adsorption tower 711 of the first tower polymer tubular membrane group 71, so that the secondary desorbed carbon dioxide is desorbed and concentrated. Then the gas can generate a low humidity dew point carbon dioxide compressed dry gas, wherein the low humidity dew point carbon dioxide compressed dry gas can reach -40 ℃ to -70 ℃ dew point, and then the carbon dioxide compressed dry gas with a low humidity dew point is passed through the first. The compressed gas pipeline 715 flows to the compressed gas output pipeline 75 , and is outputted and collected for use through the compressed gas output pipeline 75 . In addition, when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process (as shown in FIG. 6 ), the valve 7251 of the second compressed gas pipeline 725 is in an open state, and the first tower-type high The molecular tubular membrane group 71 is in the regeneration and desorption process, so the valve 7151 of the first compressed gas pipeline 715 is closed, and the carbon dioxide with low humidity dew point is compressed and dried through the adsorption and drying process as described above. The gas flows to the compressed gas output pipeline 75 through the second compressed gas pipeline 725 , and is outputted and collected for use through the compressed gas output pipeline 75 . The so-called collection and use (not shown) includes the storage of carbon dioxide compressed dry gas in steel cylinders and steel tanks for temporary storage, or directly transported to other places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola farms, chemical Factories, or food industry factories and other industries as raw materials, so that the carbon dioxide compressed dry gas can have the effect of subsequent applications.

In another embodiment of the present invention, the first tower-type polymer tubular membrane group 7 The first regeneration pipeline 714 of 1 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 are connected to a heat energy pipeline 74 (as shown in Fig. 5 to Fig. 12), and pass through The thermal energy pipeline 74 is used to transport high temperature hot gas in the first adsorption tower 711 in the first tower-type polymer tubular membrane group 71 or the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72. For regeneration and desorption, when the first tower-type polymer tubular membrane group 71 performs the adsorption and drying process (as shown in Figure 5), the valve 7141 of the first regeneration pipeline 714 is closed, and the first The two-tower polymer tubular membrane group 72 is in the regeneration and desorption process, so the valve 7241 of the second regeneration pipeline 724 is in an open state, and the second tower-type polymer tubular membrane group 72 performs adsorption. During the drying process (as shown in Figure 6), the valve 7241 of the second regeneration pipeline 724 is closed, and the first tower-type polymer tubular membrane group 71 is in the regeneration and desorption process, so the The valve 7141 of the first regeneration line 714 is in an open state.

In addition, the first variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, first carbon dioxide adsorption runner 20, first heating device 30, second carbon dioxide adsorption runner 40, The two heating devices 50 and a chimney 60 are designed, and the related contents have been described, and will not be repeated here. Therefore, the first variation of another embodiment (as shown in FIG. 7 ) is that the first regeneration line 714 of the first tower-type 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, wherein the first heater 76 and the second heater 77 are electric heaters and natural gas heaters. The first heater 76 of the first regeneration line 714 and the second heater 77 of the second regeneration line 724 allow the One tower polymer tubular membrane group 71 When the regeneration desorption process is performed or the second tower polymer tubular membrane group 72 performs the regeneration desorption process, the first heater 76 or the second heater 77 can deliver high-temperature hot gas to the first tower. The first adsorption tower 711 in the polymer tubular membrane group 71 or the second adsorption tower 721 in the second tower polymer tubular membrane group 72 is used for regeneration and desorption.

In addition, the second variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, first carbon dioxide adsorption runner 20, first heating device 30, second carbon dioxide adsorption runner 40, The two heating devices 50 and a chimney 60 are designed, and the related contents have been described, and will not be repeated here. Therefore, the second variation of another embodiment (as shown in FIG. 8 ) is that the first regeneration line 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76 , and The second regeneration line 724 of the second tower-type polymer tubular membrane group 72 is provided with a second heater 77 (please refer to the content of the first variation of another embodiment, which will not be repeated here), which is different from the other The first variation of an embodiment is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25, and one end of the recirculation pipeline 25 is connected to the first desorption gas pipeline 24, and The other end of the recirculation pipeline 25 is connected to the second desorption gas pipeline 43 , so that the desorbed and concentrated gas from the second desorption of carbon dioxide delivered by the first desorption gas pipeline 24 can be recycled through the recirculation pipeline 25 . The pipeline 25 returns to the second desorption gas pipeline 43 , and is mixed with the desorbed and concentrated gas of the first desorbed carbon dioxide in the second desorption gas pipeline 43 , and then enters the first heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The second variation of the above-mentioned another embodiment of the present invention has another variation (as shown in FIG. 9 ), that is, the connection between the first desorption gas pipeline 24 and one end of the recirculation pipeline 25 is The front end and the rear end are respectively provided with a first fan 242 and a second fan 243, and then matched with the recirculation pipeline 25 to form a positive pressure type, so that the gas after desorption and concentration of the carbon dioxide desorbed for the second time in the first desorption gas pipeline 24 can be squeezed into the recirculation pipeline 25, It returns to the second desorption gas pipeline 43 , and is mixed with the desorbed and concentrated gas from the first desorption of carbon dioxide in the second desorption gas pipeline 43 , and then enters the first heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

In addition, the third variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, first carbon dioxide adsorption runner 20, first heating device 30, second carbon dioxide adsorption runner 40, The two heating devices 50 and a chimney 60 are designed, and the related contents have been described, and will not be repeated here. Therefore, the third variation of another embodiment (as shown in FIG. 10 ) is that the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane group 71 The heat energy pipeline 74 connected to the second regeneration pipeline 724 of the membrane group 72 is provided with a heater 78, wherein the heater 78 is one of an electric heater, a natural gas heater, a heat exchanger or a heat medium oil heat exchanger. Any of them, and the high-temperature hot gas generated by the heater 78 of the thermal energy pipeline 74 is transported to the first regeneration pipeline 714 or the second regeneration pipeline 724, and then enters the first tower polymer The first adsorption tower 711 in the tubular membrane group 71 or the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72 is used for regeneration and desorption, and through the first regeneration pipeline 714 The valve 7141 and the valve 7241 of the second regeneration line 724 control the flow direction.

In addition, the fourth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, first carbon dioxide adsorption runner 20, first heating device 30, second carbon dioxide adsorption runner 40, Two heating devices 50 and a chimney 60 are designed, and The related content mentioned above has been explained and will not be repeated here. Therefore, the fourth variation of another embodiment (as shown in FIG. 11 ) is that the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane group 71 The heat energy pipeline 74 connected to the second regeneration pipeline 724 of the membrane group 72 is provided with a heater 78 (please refer to the content of the third variation of the other embodiment, which will not be repeated here), which is different from that of the other embodiment. The third variation is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25, and one end of the recirculation pipeline 25 is connected to the first desorption gas pipeline 24, and the recirculation pipeline The other end of the pipeline 25 is connected to the second desorption gas pipeline 43 , so that the desorbed and concentrated gas of the second desorbed carbon dioxide transported by the first desorption gas pipeline 24 can be returned by the recirculation pipeline 25 . into the second desorption gas pipeline 43 , and then mixed with the desorbed and concentrated gas from the first desorption of carbon dioxide in the second desorption gas pipeline 43 , and then enters the first heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The fourth variation of the above-mentioned another embodiment of the present invention has another variation (as shown in FIG. 12 ), that is, the connection between the first desorption gas pipeline 24 and one end of the recirculation pipeline 25 is The front end and the rear end are respectively provided with a first fan 242 and a second fan 243, which are combined with the recirculation pipeline 25 to form a positive pressure type, so that the first desorption gas pipeline 24 can be desorbed twice The gas after desorption and concentration of the carbon dioxide can be squeezed into the recirculation pipeline 25, and returned to the second desorption gas pipeline 43, and then desorbed with the carbon dioxide desorbed once in the second desorption gas pipeline 43. The concentrated gas enters the first heating device 30 after being mixed. The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The tandem carbon dioxide adsorption rotor treatment method of the present invention is mainly used for The carbon dioxide adsorption rotor system is provided with a pretreatment device 10, a first carbon dioxide adsorption rotor 20, a first heating device 30, a second carbon dioxide adsorption rotor 40, a second heating device 50 and a chimney 60 ( 1 to 12), the first carbon dioxide adsorption rotor 20 is provided with an adsorption zone 201 and a desorption zone 202, and the first carbon dioxide adsorption rotor 20 is connected to a pretreatment gas pipeline 21 , a first clean gas pipeline 22, a first hot gas delivery pipeline 23 and a first desorption gas pipeline 24 (as shown in Figures 1 to 12), and the second carbon dioxide adsorption runner 40 is a series of There is an adsorption zone 401 and a desorption zone 402, and the second carbon dioxide adsorption runner 40 is connected to a second clean gas discharge pipeline 41, a second hot gas conveying pipeline 42 and a second desorption gas pipeline 43 ( As shown in Figures 1 to 12), and the second heating device 50 is provided with a second heating intake line 51 (as shown in Figures 1 to 12), and the first heating device 30 The second heating device 50 is an electric heater, a natural gas heater, a heat exchanger, a heat medium oil heat exchanger, a shell and tube heat exchanger, a fin and tube heat exchanger, a plate heat exchanger or a heat pipe heat exchanger. Any one of the devices, and the pretreatment equipment 10 is provided with a gas inlet line 11 (as shown in Figs. 1 to 12). The first carbon dioxide adsorption rotor 20 and the second carbon dioxide adsorption rotor 40 are respectively a zeolite concentration rotor or a concentration rotor made of other materials.

The main steps of the processing method (as shown in FIG. 13 ) include: step S100 , inputting the gas into the pre-processing equipment: sending the gas through the gas inlet line 11 into the pre-processing equipment 10 for processing. After the above step S100 is completed, the next step S110 is performed.

One end of the above-mentioned gas inlet pipeline 11 is connected to the production site, office building, etc. where carbon dioxide is generated, or the area where carbon dioxide is generated indoors (not shown in the figure). shown), so that the gas inlet line can transport gas containing carbon dioxide or other gases, and the pretreatment equipment 10 is any one of a cooler, a condenser, a dehumidifier, and a desuperheater, which is used to convert the gas Pre-treatment enables the gas to release thermal energy to improve the adsorption efficiency.

In addition, the next step S110 is the first carbon dioxide adsorption runner adsorption: the gas processed by the pretreatment equipment 10 is output to the first carbon dioxide adsorption runner 20 from the other end of the pretreatment gas pipeline 21 one side of the adsorption zone 201 for carbon dioxide adsorption. After the above step S110 is completed, the next step S120 is performed.

One end of the pretreatment gas pipeline 21 is connected to the other side of the pretreatment device 10 , and the other end of the pretreatment gas pipeline 21 is connected to the adsorption zone 201 of the first carbon dioxide adsorption runner 20 . On one side, the gas containing carbon dioxide or other gas that has been pretreated by the pretreatment equipment 10 can be transported into the adsorption zone 201 of the first carbon dioxide adsorption runner 20 through the pretreatment gas pipeline 21, so as to Carbon dioxide adsorption is performed (as shown in Figures 1 to 4). The pretreatment gas pipeline 21 is provided with a fan 211 (as shown in FIG. 2 and FIG. 4 ), so that the pretreated carbon dioxide-containing gas in the pretreatment gas pipeline 21 can pass through the fan 211 . The gas or other gas is pushed and pulled into the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 .

In addition, the next step S120 is the second carbon dioxide adsorption rotor adsorption: the gas after carbon dioxide adsorption generated by the adsorption zone 201 of the first carbon dioxide adsorption rotor 20 is absorbed from the other end of the first clean gas pipeline 22. to output to one side of the adsorption zone 401 of the second carbon dioxide adsorption rotor 40 for re-adsorption. After the above step S120 is completed, the next step S130 is performed.

One end of the first clean gas pipeline 22 is connected to the other side of the adsorption zone 201 of the first carbon dioxide adsorption runner 20 (as shown in FIG. 1 to FIG. 4 ), and the first clean gas pipeline The other end of 22 is connected with the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 (as shown in Figures 1 to 4), so that the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 is adsorbed. The produced carbon dioxide adsorption gas can be transported to the adsorption zone 401 of the second carbon dioxide adsorption runner 40 through the first purification gas pipeline 22 for re-adsorption.

In addition, in the next step S130, the second carbon dioxide adsorption runner is discharged: the gas after carbon dioxide adsorption generated by the adsorption zone 401 of the second carbon dioxide adsorption runner 40 is discharged from the second clean gas discharge pipeline 41. The other end is output to the chimney 60 for discharge. After the above step S130 is completed, the next step S140 is performed.

The other side of the adsorption area 401 of the second carbon dioxide adsorption runner 40 is connected to one end of the second clean gas discharge pipeline 41, and the other end of the second clean gas discharge pipeline 41 is connected to the chimney 60 is connected (as shown in Figures 1 to 4), so that the gas after carbon dioxide adsorption generated by the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 after re-adsorption can pass through the second filter. The gas discharge line 41 is sent to the stack 60 for discharge to the atmosphere. The second clean air discharge line 41 is connected with a fan 411 (as shown in FIG. 2 and FIG. 4 ), so that the carbon dioxide in the second clean air discharge line 41 can be adsorbed through the fan 411 Then the gas is pushed and pulled to the chimney 60 for discharge.

In addition, the next step S140 is to transport the second hot gas for desorption: the high temperature hot gas is transported to the second carbon dioxide adsorption runner 40 through the second hot gas transport pipeline 42 connected to the second heating device 50 for desorption. Desorption takes place within the additional zone 402 . and finish on After the above step S140, the next step S150 is performed.

The other side of the desorption zone 402 of the second carbon dioxide adsorption runner 40 is connected to one end of the second hot gas conveying pipe 42, and the other end of the second hot gas conveying pipe 42 is connected to the second hot gas conveying pipe 42. The heating device 50 is connected (as shown in FIG. 1 to FIG. 4 ), and the second heating device 50 is supplied with external air or other sources of gas through the second heating air inlet pipe 51 , so that the first heating device 50 is The second heating device 50 can increase the temperature of the external air or other sources of gas input from the second heating air inlet pipe 51 to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 can pass through the second heating device 50. The second hot gas conveying pipeline 42 is conveyed to the desorption zone 402 of the second carbon dioxide adsorption runner 40 for use in desorption. The second heating intake line 51 is connected with a fan 511 (as shown in FIG. 2 and FIG. 5 ), so that the outside air in the second heating intake line 51 can pass through the fan 511 Or the gas from other sources is pushed and pulled into the second heating device 50 .

In addition, the next step S150 is to output the gas after carbon dioxide desorption and concentration: the gas after desorption and concentration of carbon dioxide generated by the desorption of the first desorption generated by the desorption zone 402 of the second carbon dioxide adsorption runner 40 is obtained from the The other end of the second desorption gas pipeline 43 is output to the first heating device 30 . After the above step S150 is completed, the next step S160 is performed.

One side of the desorption zone 402 of the second carbon dioxide adsorption runner 40 is connected to one end of the second desorption gas pipeline 43, and the other end of the second desorption gas pipeline 43 is connected to the second desorption gas pipeline 43. A heating device 30 is connected (as shown in FIG. 1 to FIG. 4 ), so as to desorb and concentrate the desorbed carbon dioxide generated by the desorption of the desorption zone 402 of the second carbon dioxide adsorption rotor 40 . gas to be transported through the second desorption gas line 43 The temperature is raised in the first heating device 30 .

In addition, in the next step S160, the first hot gas is transported for desorption: the high-temperature hot gas is transported to the first carbon dioxide adsorption runner 20 through the first hot gas transport pipeline 23 connected to the first heating device 30. Desorption zone 202 performs desorption. After the above step S160 is completed, the next step S170 is performed.

The other side of the desorption zone 202 of the first carbon dioxide adsorption runner 20 is connected to one end of the first hot gas conveying pipe 23, and the other end of the first hot gas conveying pipe 23 is connected to the first hot gas conveying pipe 23. The heating device 30 is connected (as shown in FIG. 1 to FIG. 4 ), so that the first heating device 30 can desorb the gas after the first desorption of carbon dioxide delivered by the second desorption gas pipeline 43 The temperature is raised to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is transported to the desorption zone 202 of the first carbon dioxide adsorption runner 20 through the first hot gas transport pipeline 23 for desorption. Attached to use.

In addition, the next step S170 is to output the gas after desorption and concentration of carbon dioxide: the gas after the desorption and concentration of carbon dioxide generated by the second desorption generated by the desorption zone 202 of the first carbon dioxide adsorption runner 20 is passed through the second carbon dioxide adsorption runner 20. The other end of a desorbed gas line 24 is output.

One side of the desorption zone 202 of the first carbon dioxide adsorption runner 20 is connected to one end of the first desorption gas pipeline 24 (as shown in FIG. 1 to FIG. 4 ), so that the The carbon dioxide desorbed and concentrated gas generated by the desorption in the desorption zone 202 of the first carbon dioxide adsorption runner 20 is desorbed to pass through the first desorption gas pipeline 24 and output for subsequent processing. The so-called follow-up treatment (not shown in the figure) includes desorbing and concentrating the second desorbed carbon dioxide delivered by the first desorbing gas pipeline 24 to be able to pass through the steel cylinder and the steel tank. Storage, or transport and supply to other places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola farms, chemical plants, or food industry factories and other industries, as raw materials to desorb the secondary desorbed carbon dioxide. The concentrated gas can have the effect of subsequent application. The first desorption gas pipeline 24 is connected with a fan 241 (as shown in Figures 2 and 4), so that the second desorption in the first desorption gas pipeline 24 can pass through the fan 241. The attached carbon dioxide is desorbed and concentrated, and the gas is pushed and pulled out.

In addition, the first variation in the main steps of the present invention is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25 (as shown in FIG. 3 ), and the recirculation pipeline 25 is One end is connected to the first desorption gas pipeline 24 , and the other end of the recirculation pipeline 25 is connected to the second desorption gas pipeline 43 , so that the second desorption gas pipeline 24 conveys the second desorption gas. The gas after the desorption and concentration of the desorbed carbon dioxide can be returned to the second desorption gas pipeline 43 through the recirculation pipeline 25, and then desorbed with the first desorbed carbon dioxide in the second desorption gas pipeline 43. The concentrated gas enters the first heating device 30 after being mixed. The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The second variation of the above-mentioned main steps of the present invention is that a first fan 242 is respectively provided at the front end and the rear end of the first desorption gas pipeline 24 at the connection at one end of the recirculation pipeline 25 . and a second fan 243 (as shown in FIG. 4 ), and then matched with the recirculation pipeline 25 to form a positive pressure type, so that the carbon dioxide desorbed for the second time in the first desorption gas pipeline 24 is desorbed and concentrated The gas can then be squeezed into the recirculation line 25 and back into the second desorption gas line 43 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

Furthermore, another step of the present invention is based on the above-mentioned step S100 gas input pretreatment equipment, step S110 first carbon dioxide adsorption rotor adsorption, step S120 second carbon dioxide adsorption rotor adsorption, step S130 second carbon dioxide adsorption rotor adsorption. round discharge, step S140 transports the second hot gas for desorption, step S150 outputs the gas after carbon dioxide desorption and concentration, step S160 transports the first hot gas for desorption, and step S170 outputs the gas after carbon dioxide desorption and concentration. The related content has been described and will not be repeated here. Therefore, the present invention includes the following steps (as shown in FIG. 14 ) after outputting the desorbed and concentrated gas of carbon dioxide in step S170 . The desorbed and concentrated gas from the secondary desorbed carbon dioxide in the pipeline 24 is transported to a double-tower polymer tubular membrane device 70 for processing. The desorbed and concentrated gas of the second desorbed carbon dioxide in the first desorption gas pipeline 24 can be recompressed through the double-tower polymer tubular membrane device 70 to form carbon dioxide compressed dry gas.

The above-mentioned double-tower polymer tubular membrane equipment 70 is provided with a first tower-type polymer tubular membrane group 71 and a second tower-type polymer tubular membrane group 72, and the first tower-type polymer tubular membrane group 72 is provided. The membrane group 71 is provided with a first adsorption tower 711, a first intake line 712, a first exhaust line 713, a first regeneration line 714 and a first compressed gas line 715 (such as the first gas line 715). 5 to 12), in addition, the second tower polymer tubular membrane group 72 is provided with a second adsorption tower 721, a second intake line 722, a second exhaust line 723, A second regeneration pipeline 724 and a second compressed gas pipeline 725 (as shown in FIG. 5 to FIG. 12 ), and the first inlet gas pipeline 712 of the first tower-type polymer tubular membrane group 71 , the first exhaust pipeline 713, the first regeneration pipeline 714 and the first compressed gas pipeline 715 is provided with a valve 7121, 7131, 7141, 7151 (as shown in Figures 5 to 12), and the second inlet gas pipeline 722 of the second tower polymer tubular membrane group 72, the second The exhaust line 723, the second regeneration line 724 and the second compressed gas line 725 are each provided with a valve 7221, 7231, 7241, 7251 (as shown in Fig. 5 to Fig. 12) to control the above gas flow between pipes.

In addition, the first adsorption tower 711 of the first tower polymer tubular membrane group 71 and the second adsorption tower 721 of the second tower polymer tubular membrane group 72 are composed of a plurality of hollow tubular polymer tubes. (as shown in Figures 5 to 12), and the hollow tubular polymer tubular membrane adsorption material is made of high molecular polymer and adsorbent, and the polymer is By 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-co-glycolic acid, A group consisting of polycaprolactone, polyvinyl pyrrolidone, ethylene alcohol vinyl, polydimethylsiloxane, polytetrafluoroethylene and cellulose acetate (CA) at least one of the groups. The diameter and outer diameter of the hollow tubular polymer tubular membrane produced are more than 2 mm, so as to have a high specific surface area, easy adsorption and easy desorption, so the amount of adsorbent is smaller than that of the traditional particle type. With the same dynamic adsorption performance, it will naturally use less heat energy to complete the desorption during desorption, so it has an energy-saving effect.

In addition, the adsorbent ratio of the above-mentioned hollow tubular polymer tubular membrane adsorbent material is 10% to 90%, and the adsorbent is in the form of granules, powder, hollow fiber, and honeycomb. Any of the shapes (not shown), wherein the plurality of particles of the powder have a particle size of 0.005 to 50um, and the plurality of particles of the powder have a two-dimensional or three-dimensional pore structure, and the pores are regular or Irregular shape, wherein the adsorbent is modified by molecular sieve, activated carbon, alcohol amine, A-type zeolite (such as 3A, 4A or 5A), X-type zeolite (such as 13X), Y-type zeolite (such as ZSM-5) ), mesoporous molecular sieves (such as MCM-41, 48, 50 and SBA-15), metal organic frameworks (Metal Organic Frameworks: MOF) or at least one of the group consisting of graphene.

In addition, the above-mentioned hollow tubular polymer tubular membrane adsorbent is made of inorganic materials (not shown in the figure), wherein the size of the added inorganic materials ranges from 0.01um to 100um, and the inorganic materials may contain adsorbents, such as containing When the adsorbent is used, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the above inorganic materials are iron oxide, copper oxide, barium titanate, lead titanate, aluminum oxide, silicon dioxide, gas gel (silica aerogel), bentonite (such as potassium bentonite, sodium bentonite, calcium bentonite and aluminum bentonite), china clay (such as Al 2 O 3.2SiO 2.2H 2 O), hyplas soil (such as 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 (eg Ca 3 SiO 5, Ca 3 Si 2 O 7 and CaSiO 3) , magnesium silicate (such as Mg 3 Si 4 O 10(OH) 2), sodium silicate (such as Na 2 SiO 3 and its hydrate), anhydrous sodium sulfate, zirconium silicate (such as ZrSiO 4), opaque Zirconium (such as 53.89%SiO2.4.46%Al2O3.12.93%ZrO2.9.42%CaO.2.03%MgO.12.96%ZnO.3.73%K2O.0.58%Na2O) and silicon carbide at least one of the groups.

In another step of the present invention, the first inlet line 712 of the first tower-type polymer tubular membrane group 71 and the second inlet line 722 of the second tower-type polymer tubular membrane group 72 are connected to each other. A connection is formed with the other end of the first desorption gas pipeline 24 (as shown in Fig. 5 to Fig. 12), so that the gas after desorption and concentration of the carbon dioxide desorbed by the secondary desorption can be input into the double desorption gas. The tower-type polymer tubular membrane equipment 70 is used for recompression treatment, and the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane group 72 are respectively used for adsorption drying process and regeneration and dehydration. The procedure is attached, and when the first tower-type polymer tubular membrane group 71 performs the adsorption drying procedure (as shown in FIG. 5 ), the valve 7121 of the first air inlet line 712 is in an open state, and the second The tower-type polymer tubular membrane group 72 is undergoing a regeneration and desorption process, so the valve 7221 of the second intake line 722 is in a closed state, and the valve 7121 of the first intake line 712 is opened for supplying The gas desorbed and concentrated by the second desorption of carbon dioxide in the first desorption gas pipeline 24 is input into the first adsorption tower 711 in the first tower polymer tubular membrane group 71, and passes through the first adsorption tower 711. The hollow tubular polymer tubular membrane adsorbent in the adsorption tower 711 is used for adsorption and drying.

After a period of time, the first tower-type polymer tubular membrane group 71 performs the adsorption drying process before the adsorption is saturated, that is, the second tower-type polymer tubular membrane group 72 is switched to perform the adsorption drying process (such as the first column). 6), and when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process, the valve 7221 of the second inlet line 722 is in an open state, and the first tower-type polymer tube The membrane group 71 is changed to perform the regeneration and desorption process, so the valve 7121 of the first intake line 712 is in a closed state, and the valve of the second intake line 722 is opened for the first desorption process. The gas after the desorption and concentration of the carbon dioxide desorbed for the second time in the attached gas pipeline 24 is input into the second adsorption tower 721 in the second tower polymer tubular membrane group 72, and passes through the second adsorption tower 721 The hollow tubular polymer tubular membrane adsorbent is used for adsorption and drying.

In another step of the present invention, the first exhaust line 713 of the first tower-type polymer tubular membrane group 71 and the second exhaust line 72 of the second tower-type polymer tubular membrane group 72 3 is connected to an exhaust output pipe 73 (as shown in Figures 5 to 12), and the other end of the exhaust output pipe 73 is in the atmosphere or outside air, and when the first When the tower-type polymer tubular membrane group 71 performs the adsorption drying process (as shown in FIG. 5), the valve 7131 of the first exhaust pipe 713 is closed, and the second tower-type polymer tubular membrane The group 72 is performing the regeneration and desorption process, so the valve 7231 of the second exhaust pipe 723 is in an open state, so that the second adsorption of the second tower polymer tubular membrane group 72 in the regeneration and desorption process is performed. The gas in the tower 721 can be exhausted through the second exhaust pipe 723, and when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process (as shown in FIG. 6), the first The valve 7231 of the second exhaust line 723 is in a closed state, and the first tower-type polymer tubular membrane group 71 is undergoing regeneration and desorption process, so the valve 7131 of the first exhaust line 713 is in the state of being closed. In the open state, the gas in the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 performing the regeneration and desorption process can pass through the first exhaust line 713 to perform the exhaust operation.

In another step of the present invention, the first compressed gas pipeline 715 of the first tower-type polymer tubular membrane group 71 and the second compressed gas pipeline 725 of the second tower-type polymer tubular membrane group 72 are connected with A compressed gas output pipeline 75 is connected (as shown in FIG. 5 to FIG. 12 ). When the first tower-type polymer tubular membrane group 71 performs the adsorption drying process (as shown in FIG. 5 ), the first The valve 7151 of a compressed gas pipeline 715 is in an open state, and the second tower-type polymer tubular membrane group 72 is undergoing a regeneration and desorption process, so the valve 7251 of the second compressed gas pipeline 725 is in the open state. In the closed state, therefore, the gas after the desorption and concentration of carbon dioxide desorbed for the second time can be adsorbed through the hollow tubular polymer tubular membrane in the first adsorption tower 711 of the first tower polymer tubular membrane group 71 material for adsorption drying, so that the The desorbed and concentrated gas of the second desorbed carbon dioxide can produce a low-humidity dew point carbon dioxide compressed dry gas, wherein the low-humidity dew point of the carbon dioxide compressed dry gas can reach -40°C to -70°C dew point, and then has a low humidity dew point. The carbon dioxide compressed drying gas flows to the compressed gas output line 75 through the first compressed gas line 715 , and is outputted and collected for use through the compressed gas output line 75 . In addition, when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process (as shown in FIG. 6 ), the valve 7251 of the second compressed gas pipeline 725 is in an open state, and the first tower-type high The molecular tubular membrane group 71 is in the regeneration and desorption process, so the valve 7151 of the first compressed gas pipeline 715 is closed, and the carbon dioxide with low humidity dew point is compressed and dried through the adsorption and drying process as described above. The gas flows to the compressed gas output pipeline 75 through the second compressed gas pipeline 725 , and is outputted and collected for use through the compressed gas output pipeline 75 . The so-called collection and use (not shown) includes the storage of carbon dioxide compressed dry gas in steel cylinders and steel tanks for temporary storage, or directly transported to other places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola farms, chemical Factories, or food industry factories and other industries as raw materials, so that the carbon dioxide compressed dry gas can have the effect of subsequent applications.

In another step of the present invention, 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 are connected with a thermal energy The pipeline 74 is connected (as shown in FIG. 5 to FIG. 12 ), and the high-temperature hot gas is transported through the thermal energy pipeline 74 . The first adsorption tower 711 in the first tower polymer tubular membrane group 71 or the The second adsorption tower 721 in the second tower polymer tubular membrane group 72 is used for regeneration and desorption. When the first tower polymer tubular membrane group 71 is subjected to the adsorption drying process (as shown in Figure 5) , the valve 7141 of the first regeneration pipeline 714 is closed, and The second tower-type polymer tubular membrane group 72 is in the regeneration and desorption process, so the valve 7241 of the second regeneration line 724 is in an open state, and the second tower-type polymer tubular membrane group 72 is in the open state. During the adsorption drying process (as shown in FIG. 6 ), the valve 7241 of the second regeneration pipeline 724 is in a closed state, and the first tower-type polymer tubular membrane group 71 is used for the regeneration and desorption process. Therefore, the valve 7141 of the first regeneration pipeline 714 is in an open state.

In addition, the first variation of another step of the present invention is based on the design of delivering the above-mentioned step S200 to the double-tower polymer tubular membrane equipment, and the related content has been described and will not be repeated here. . Therefore, the first variation of another step (as shown in FIG. 57) is that the first regeneration line 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76, and the The second regeneration line 724 of the second tower polymer tubular membrane group 72 is provided with a second heater 77, wherein the first heater 76 and the second heater 77 are electric heaters and natural gas heaters , heat exchanger or heat medium oil heat exchanger, and through the first heater 76 of the first regeneration line 714 and the second heater 77 of the second regeneration line 724 to make the first When the tower-type polymer tubular membrane group 71 performs the regeneration and desorption process or the second tower-type polymer tubular membrane group 72 performs the regeneration and desorption process, the first heater 76 or the second heater 77 can be used. To transport high temperature hot gas to the first adsorption tower 711 in the first tower polymer tubular membrane group 71 or the second adsorption tower 721 in the second tower polymer tubular membrane group 72 for regeneration and desorption. .

In addition, the second variation of another step of the present invention is based on the design of delivering the above-mentioned step S200 to the double-tower polymer tubular membrane equipment, and the related content has been described and will not be repeated here. . Therefore, the second variation of another step (as shown in Figure 8 shown) is that the first regeneration pipe 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76, and the second regeneration pipe of the second tower-type polymer tubular membrane group 72 The circuit 724 is provided with a second heater 77 (please refer to the content of the first variation of another step, which will not be repeated here), and the difference from the first variation of another step is the first desorption gas pipeline 24 There is a recirculation pipeline 25, one end of the recirculation pipeline 25 is connected to the first desorption gas pipeline 24, and the other end of the recirculation pipeline 25 is connected to the second desorption gas pipeline 43, so that the desorbed and concentrated gas of the second desorbed carbon dioxide transported by the first desorption gas pipeline 24 can be returned to the second desorption gas pipeline 43 through the recirculation pipeline 25, and then communicated with the second desorption gas pipeline 43. The carbon dioxide desorbed and concentrated gas in the second desorption gas pipeline 43 is mixed and then enters the first heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The second variation of the above-mentioned another step of the present invention has another variation (as shown in FIG. 9 ), that is, the front end of the first desorption gas pipeline 24 at the connection of one end of the recirculation pipeline 25 and the The rear end is respectively provided with a first fan 242 and a second fan 243 , which are combined with the recirculation pipeline 25 to form a positive pressure type, so that the carbon dioxide desorbed in the first desorption gas pipeline 24 is desorbed for the second time. The gas after desorption and concentration can be squeezed into the recirculation pipeline 25 and returned to the second desorption gas pipeline 43 , and then desorbed and concentrated with the carbon dioxide desorbed once in the second desorption gas pipeline 43 The gas then enters the first heating device 30 after being mixed. The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

In addition, the third variation of another step of the present invention is based on the design of delivering the above-mentioned step S200 to the double-tower polymer tubular membrane equipment, and the related internal The content has already been explained and will not be repeated here. Therefore, the third variation of another step (as shown in FIG. 10 ) is the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second tower polymer tubular membrane The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the group 72 is provided with a heater 78, wherein the heater 78 is one of an electric heater, a natural gas heater, a heat exchanger or a heat medium oil heat exchanger Either, and the high-temperature hot gas generated by the heater 78 of the thermal energy pipeline 74 is transported to the first regeneration pipeline 714 or the second regeneration pipeline 724, and then enters the first tower-type polymer tube The first adsorption tower 711 in the membrane group 71 or the second adsorption tower 721 in the second tower type polymer tubular membrane group 72 is used for regeneration and desorption, and passes through the valve of the first regeneration pipeline 714 7141 and the valve 7241 of the second regeneration line 724 to control the flow direction.

In addition, the fourth variation of another step of the present invention is based on the design of delivering the above-mentioned step S200 to the double-tower polymer tubular membrane equipment, and the related content has been described and will not be repeated here. . Therefore, the fourth variation of another step (as shown in FIG. 11 ) is the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane The heat pipe 74 connected to the second regeneration pipe 724 of the group 72 is provided with a heater 78 (please refer to the content of the third variation of another step, which will not be repeated here), which is different from the third variation of another step. The difference is that the first desorption gas pipeline 24 is provided with a recirculation pipeline 25, and one end of the recirculation pipeline 25 is connected to the first desorption gas pipeline 24, and the other end of the recirculation pipeline 25 is connected to the first desorption gas pipeline 24. The other end is connected to the second desorption gas pipeline 43 , so that the desorbed and concentrated gas of the second desorbed carbon dioxide transported by the first desorption gas pipeline 24 can be returned to the second desorption pipeline 25 through the recirculation pipeline 25 . In the second desorption gas pipeline 43, it is mixed with the desorbed and concentrated gas of the first desorbed carbon dioxide in the second desorption gas pipeline 43, and then enters the first desorption gas pipeline 43. Heating device 30 . The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

The fourth variation of the above-mentioned other step of the present invention has another variation (as shown in FIG. 12 ), that is, the front end of the first desorption gas pipeline 24 where one end of the recirculation pipeline 25 is connected and the rear end are respectively provided with a first fan 242 and a second fan 243, which are combined with the recirculation pipeline 25 to form a positive pressure type, so that the second desorption gas in the first desorption gas pipeline 24 is formed. The gas after carbon dioxide desorption and concentration can be squeezed into the recirculation pipeline 25 and returned to the second desorption gas pipeline 43 , and then desorbed with the carbon dioxide desorbed in the second desorption gas pipeline 43 The concentrated gas enters the first heating device 30 after being mixed. The recirculation pipeline 25 is provided with a valve 251 to control the gas flow of the recirculation pipeline 25 through the valve 251 .

From the above detailed description, it can be understood by those skilled in the art that the present invention can indeed achieve the aforesaid object, and it is in compliance with the provisions of the Patent Law, and an application for a patent for invention can be filed.

However, the above are only preferred embodiments of the present invention, and should not limit the scope of implementation of the present invention; therefore, any simple equivalent changes and modifications made according to the scope of the patent application of the present invention and the contents of the description of the invention , shall still fall within the scope covered by the patent of the present invention.

10: Pretreatment equipment

11: Gas intake line

20: The first carbon dioxide adsorption runner

201: Adsorption Zone

202: Desorption zone

21: Pretreatment gas pipeline

22: The first clean air pipeline

23: The first hot gas delivery pipeline

24: The first desorption gas pipeline

30: The first heating device

40: Second carbon dioxide adsorption runner

401: adsorption zone

402: Desorption zone

41: Second clean air discharge pipeline

42: Second hot gas delivery pipeline

43: Second desorption gas pipeline

50: Second heating device

51: Second heated intake line

60: Chimney

Claims (33)

A tandem carbon dioxide adsorption runner system, comprising: a pretreatment device, one side of the pretreatment device is connected to a gas inlet pipeline; A first carbon dioxide adsorption runner, the first carbon dioxide adsorption runner is equipped with an adsorption zone and a desorption zone, and the first carbon dioxide adsorption runner is connected with a pretreatment gas pipeline, a first purification gas pipeline, a first A hot gas delivery pipeline and a first desorption gas pipeline, one end of the pretreatment gas pipeline is connected to the other side of the pretreatment equipment, and the other end of the pretreatment gas pipeline is connected to the first carbon dioxide One side of the adsorption area of the adsorption runner, one end of the first clean gas pipeline is connected to the other side of the adsorption area of the first carbon dioxide adsorption runner, and one end of the first hot gas conveying pipeline is connected to the first The other side of the desorption zone of the carbon dioxide adsorption runner is connected, and one end of the first desorption gas pipeline is connected to one side of the desorption zone of the first carbon dioxide adsorption runner; a first heating device, the first heating device is connected to the other end of the first hot gas conveying pipeline of the first carbon dioxide adsorption runner; A second carbon dioxide adsorption runner, the second carbon dioxide adsorption runner is equipped with an adsorption zone and a desorption zone, and the second carbon dioxide adsorption runner is connected with a second clean gas discharge pipeline and a second hot gas conveying pipeline and a second desorption gas pipeline, one side of the adsorption zone of the second carbon dioxide adsorption runner is connected with the other end of the first clean gas pipeline of the first carbon dioxide adsorption runner, the second clean gas discharge pipe One end of the road is connected with the other side of the adsorption zone of the second carbon dioxide adsorption runner, one end of the second hot gas conveying pipeline is connected with the other side of the desorption zone of the second carbon dioxide adsorption runner, the One end of the second desorption gas pipeline is connected to the second carbon dioxide One side of the desorption zone of the adsorption runner is connected, and the other end of the second desorption gas pipeline is connected with the first heating device; a second heating device, the second heating device is provided with a second heating inlet pipeline, the second heating device is connected to the other end of the second hot gas conveying pipeline of the second carbon dioxide adsorption runner; and a chimney, the chimney is connected with the other end of the second clean gas discharge pipeline of the second carbon dioxide adsorption runner. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the pretreatment gas pipeline system is further provided with a fan. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the second clean air discharge line is further provided with a fan. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the first desorption gas pipeline system is further provided with a fan. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the second heating intake line system is further provided with a fan. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the pretreatment device is further any one of a cooler, a condenser, a dehumidifier, and a desuperheater. The tandem carbon dioxide adsorption rotor system as described in claim 1, wherein the first desorption gas pipeline system is further provided with a recirculation pipeline, and one end of the recirculation pipeline is connected to the first desorption gas pipeline A gas pipeline, the other end of the recirculation pipeline is connected to the second desorption gas pipeline. The tandem carbon dioxide adsorption rotor system as described in item 7 of the scope of application, wherein the A desorption gas pipeline system is further provided with a first fan and a second fan respectively at the front end and the rear end of one end connection of the recirculation pipeline. The tandem carbon dioxide adsorption runner system as described in claim 1, wherein the other end of the first desorption gas pipeline of the first carbon dioxide adsorption runner is further connected to a double-tower polymer tubular membrane device Connected, the double-tower polymer tubular membrane equipment is provided with a first tower-type polymer tubular membrane group and a second tower-type polymer tubular membrane group, and the first tower-type polymer tubular membrane group is There is a first adsorption tower, a first inlet pipeline, a first exhaust pipeline, a first regeneration pipeline and a first compressed gas pipeline, and the second tower-type polymer tubular membrane system is A second adsorption tower, a second intake pipeline, a second exhaust pipeline, a second regeneration pipeline and a second compressed gas pipeline are provided. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first exhaust pipe of the first tower-type polymer tubular membrane group and the first exhaust pipe of the second tower-type polymer tubular membrane group The second exhaust pipeline system is further connected with an exhaust output pipeline. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first compressed gas pipeline of the first tower-type polymer tubular membrane group and the first compressed gas pipeline of the second tower-type polymer tubular membrane group The two compressed gas pipeline systems are further connected with a compressed gas output pipeline. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first regeneration pipe system of the first tower-type polymer tubular membrane group is further provided with a first heater, and the second tower-type membrane group is further provided with a first heater. The second regeneration pipeline system of the polymer tubular membrane group is further provided with a second heater. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first inlet gas pipeline, the first exhaust pipeline and the first regeneration pipeline of the first tower-type polymer tubular membrane group And the first compressed gas pipeline system is further provided with a valve, the second inlet gas pipeline, the second exhaust pipeline, the second regeneration pipeline and the second compressed gas of the second tower polymer tubular membrane group The pipeline system is further provided with a valve. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first adsorption tower of the first tower-type polymer tubular membrane group and the second tower of the second tower-type polymer tubular membrane group The inside of the adsorption tower is further filled with a plurality of hollow tubular polymer tubular membrane adsorption materials, and the hollow tubular polymer tubular membrane adsorption materials are made of high molecular polymers and adsorbents. The tandem carbon dioxide adsorption rotor system as described in claim 9, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group and the second regeneration line of the second tower-type polymer tubular membrane group The regeneration line system is further connected with a heat energy line. The tandem carbon dioxide adsorption rotor system as described in claim 15, wherein the heat energy pipeline system is further provided with a heater, and the heater is an electric heater, a natural gas heater, a heat exchanger or a heat medium oil Any of the heat exchangers. A tandem carbon dioxide adsorption runner treatment method is mainly used in a carbon dioxide adsorption runner system, and is provided with a pretreatment device, a first carbon dioxide adsorption runner, a first heating device, a second carbon dioxide adsorption runner, a The second heating device and a chimney, the first carbon dioxide adsorption runner is provided with an adsorption zone and a desorption zone, and the first carbon dioxide adsorption runner is connected with a pretreatment gas pipeline, a first clean gas pipeline, a first A hot gas conveying pipeline and a first desorption gas pipeline, the second carbon dioxide adsorption runner is provided with an adsorption zone and a desorption zone, and the second carbon dioxide adsorption runner is connected to a second clean gas discharge pipeline, A second hot gas conveying pipeline and a second desorption gas pipeline, the second heating device is provided with a second heating intake pipeline, the pretreatment equipment is provided with a gas intake pipeline, and the processing method The main steps include: Gas input pretreatment equipment: the gas is sent to the pretreatment equipment for processing through the gas inlet pipeline; The first carbon dioxide adsorption rotor adsorption: the gas processed by the pretreatment equipment is output from the other end of the pretreatment gas pipeline to one side of the adsorption zone of the first carbon dioxide adsorption rotor for carbon dioxide adsorption. ; Second carbon dioxide adsorption rotor adsorption: the gas after carbon dioxide adsorption generated by the adsorption zone of the first carbon dioxide adsorption rotor is output to the second carbon dioxide adsorption rotor from the other end of the first purification gas pipeline one side of the adsorption zone for resorption; The second carbon dioxide adsorption runner discharge: the gas after carbon dioxide adsorption generated by the adsorption zone of the second carbon dioxide adsorption runner is output to the chimney from the other end of the second clean gas discharge pipeline; Transporting the second hot gas for desorption: transporting the high-temperature hot gas to the desorption zone of the second carbon dioxide adsorption runner through the second hot gas transport pipeline connected to the second heating device for desorption; Output the gas after desorption and concentration of carbon dioxide: the gas after desorption and concentration of carbon dioxide generated by the desorption of the second carbon dioxide adsorption runner through the desorption of the first desorption is sent from the other end of the second desorption gas pipeline. to output to the first heating device; Transporting the first hot gas for desorption: then transporting the high-temperature hot gas to the desorption zone of the first carbon dioxide adsorption runner through the first hot gas transport pipeline connected to the first heating device for desorption; and Output the gas after desorption and concentration of carbon dioxide: the gas after desorption and concentration of carbon dioxide generated by the secondary desorption generated by the desorption zone of the first carbon dioxide adsorption runner is sent from the other end of the first desorption gas pipeline. output. The tandem carbon dioxide adsorption rotor processing method as described in the claim 17 of the patent application scope, wherein the pretreatment gas pipeline system is further provided with a fan. The tandem carbon dioxide adsorption runner treatment method as described in claim 17, wherein the second clean air discharge pipeline system is further provided with a fan. The tandem carbon dioxide adsorption rotor treatment method as described in the claim 17, wherein the first desorption gas pipeline system is further provided with a fan. The tandem carbon dioxide adsorption rotor processing method as described in claim 17, wherein the second heating air inlet line system is further provided with a fan. The tandem carbon dioxide adsorption rotor treatment method as described in claim 17, wherein the pretreatment equipment is further any one of a cooler, a condenser, a dehumidifier, and a desuperheater. The tandem carbon dioxide adsorption rotor treatment method as described in claim 17, wherein the first desorption gas pipeline system is further provided with a recirculation pipeline, and one end of the recirculation pipeline is connected to the first desorption gas pipeline A gas pipeline is attached, and the other end of the recirculation pipeline is connected to the second desorption gas pipeline. The tandem carbon dioxide adsorption rotor treatment method as described in claim 23, wherein the first desorption gas pipeline system is further provided with a first desorption gas pipe at the front end and the rear end of one end connection of the recirculation pipeline, respectively. A fan and a second fan. The tandem carbon dioxide adsorption runner treatment method as described in item 17 of the patent application scope method, wherein after the gas step of outputting carbon dioxide desorption and concentration, it further comprises the following steps: Transport to double-tower polymer tubular membrane equipment: The gas after desorption and concentration of carbon dioxide desorbed for the second time in the first desorption gas pipeline is transported to a double-tower polymer tubular membrane equipment for processing. The tandem carbon dioxide adsorption rotor treatment method as described in claim 25, wherein the double tower polymer tubular membrane equipment is provided with a first tower polymer tubular membrane group and a second tower height Molecular tubular membrane group, the first tower-type polymer tubular membrane group is provided with a first adsorption tower, a first intake pipeline, a first exhaust pipeline, a first regeneration pipeline and a first A compressed gas pipeline, the second tower-type polymer tubular membrane group is provided with a second adsorption tower, a second intake pipeline, a second exhaust pipeline, a second regeneration pipeline and a first Two compressed gas pipelines. The tandem carbon dioxide adsorption rotor treatment method as described in claim 26, wherein the first exhaust pipe of the first tower-type polymer tubular membrane group and the connection of the second tower-type polymer tubular membrane group The second exhaust line system is further connected with an exhaust output line. The tandem carbon dioxide adsorption rotor treatment method as described in claim 26, wherein the first compressed gas pipeline of the first tower-type polymer tubular membrane group and the connection of the second tower-type polymer tubular membrane group The second compressed gas pipeline system is further connected with a compressed gas output pipeline. The tandem carbon dioxide adsorption rotor treatment method as described in the claim 26, wherein the first regeneration pipe system of the first tower-type polymer tubular membrane group is further provided with a first heater, and the second tower is further provided with a first heater. The second regeneration pipeline system of the polymer tubular membrane group is further provided with a second heater. The tandem carbon dioxide adsorption rotor treatment method as described in item 26 of the patent application scope, wherein the first inlet gas pipeline, the first exhaust pipeline and the first regeneration tube of the first tower-type polymer tubular membrane group The pipeline and the first compressed gas pipeline system are further provided with a valve, the second inlet gas pipeline, the second exhaust pipeline, the second regeneration pipeline and the second compression pipeline of the second tower polymer tubular membrane group The gas pipeline system is further provided with a valve. The tandem carbon dioxide adsorption rotor treatment method as described in claim 26, wherein the first adsorption tower of the first tower-type polymer tubular membrane group and the first adsorption tower of the second tower-type polymer tubular membrane group The inside of the two adsorption towers is further filled with a plurality of hollow tubular polymer tubular membrane adsorption materials, and the hollow tubular polymer tubular membrane adsorption materials are made of high molecular polymers and adsorbents. The tandem carbon dioxide adsorption rotor treatment method as described in claim 26, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group and the first regeneration line of the second tower-type polymer tubular membrane group The second regeneration pipeline system is further connected with a heat energy pipeline. The tandem carbon dioxide adsorption rotor treatment method as described in item 32 of the patent application scope, wherein the heat energy pipeline system is further provided with a heater, and the heater is an electric heater, a natural gas heater, a heat exchanger or a heat medium Either of the oil heat exchangers.

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