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

Abstract

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

Description

Carbon dioxide adsorption wheel system and method

technical field

The present invention relates to a carbon dioxide adsorption runner system and its method, in particular to a system that can increase the concentration efficiency of carbon dioxide, has the efficiency of concentrating and recovering carbon dioxide, and is suitable for the semiconductor industry, optoelectronic industry, chemical related industries or manufacturing related industries Carbon dioxide treatment system or similar equipment.

Background technique

In recent years, environmental protection has become an issue 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 CO ₂ . Among them, carbon dioxide CO ₂ is a common compound in the air. It is composed of two oxygen An atom is connected to a carbon atom by a polar covalent bond.

Since the Industrial Revolution, humans 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 rainforests to increase agricultural areas, these improper human activities have produced excessive greenhouse gases, greatly enhancing The greenhouse effect destroys the long-term energy balance, resulting in an increase in the temperature of the earth's surface, leading to global warming.

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

In recent years, relevant personnel have attached great importance to air pollution, and therefore have established relevant air quality standards for chimney emission standards. At the same time, they will be reviewed periodically in accordance with the development of international control trends.

Therefore, in view of the above deficiencies, it is expected to propose a carbon dioxide adsorption runner system and its method capable of concentrating and recovering carbon dioxide, so that users can easily operate and assemble it. Or convenience, this is the research engine of the present invention.

Contents of the invention

The main purpose of the present invention is to provide a carbon dioxide adsorption rotor system and its method, which is mainly used in a carbon dioxide treatment system, and is provided with a pretreatment device, a first carbon dioxide adsorption rotor, a first heating device, a first Two carbon dioxide adsorption runners, a second heating device and a chimney, by connecting two carbon dioxide adsorption runners in series, desorbing and concentrating the carbon dioxide desorbed once generated in the desorption area of the first carbon dioxide adsorption runner Transported to the adsorption area of the second carbon dioxide adsorption wheel for secondary adsorption, and then the desorption area of the second carbon dioxide adsorption wheel to generate the second desorbed carbon dioxide desorbed and concentrated gas, so that the carbon dioxide can be increased Improve the concentration efficiency and have the ability to concentrate and recover carbon dioxide, thereby increasing the overall practicality.

Another object of the present invention is to provide a carbon dioxide adsorption runner system and method thereof, through which the other end of the second desorption gas pipeline of the second carbon dioxide adsorption runner is connected with a double-tower polymer tubular membrane device , the desorbed and concentrated carbon dioxide desorbed for the second time can be recompressed through the double-tower polymer tubular membrane equipment to form carbon dioxide compressed and dried gas, and the recompressed carbon dioxide compressed and dried gas can be Store through steel cylinders and steel tanks, or transport and supply to other places that need carbon dioxide, such as greenhouses or seaweed farms, soda cola fields, chemical plants, or food industry factories, etc., as raw materials to let carbon dioxide Compressed dry gas can have the effectiveness of subsequent applications, thereby increasing the overall usability.

Another object of the present invention is to provide a carbon dioxide adsorption rotor system and its method, a recirculation pipeline is connected through the second desorption gas pipeline, and one end of the recirculation pipeline is connected to the second desorption gas pipeline The other end of the recirculation pipeline is connected to the second heating intake pipeline, so that the gas desorbed and concentrated after secondary desorption of carbon dioxide can return to the second heating intake pipeline through the recirculation pipeline for mixing , and re-heated by the second heating device, and then transported to the desorption zone of the second carbon dioxide adsorption wheel for desorption, so as to have continuous recirculation performance, so that the desorption concentration of carbon dioxide can be obtained from the inlet Concentration increased from 6% to 40%-99% after desorption, thereby increasing the overall operability.

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

Description of drawings

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

Fig. 2 is a schematic diagram of the system architecture of the first variant of the main embodiment of the present invention.

Fig. 3 is a schematic diagram of the system architecture of the second variant of the main embodiment of the present invention.

Fig. 4 is a schematic diagram of the system architecture of the third variation of the main embodiment of the present invention.

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

FIG. 6 is a schematic diagram of a first variant system architecture according to another embodiment of the present invention.

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

Fig. 8 is a schematic diagram of the system architecture of the third variation and the first deformation according to another embodiment of the present invention.

FIG. 9 is a schematic diagram of the system architecture of the third variation and the second deformation system according to another embodiment of the present invention.

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

Fig. 11 is a schematic diagram of the system architecture of the fifth variation and the first variation of another embodiment of the present invention.

Fig. 12 is a schematic diagram of the system structure of the fifth variation and the second deformation system according to another embodiment of the present invention.

FIG. 13 is a schematic diagram of a system architecture of a sixth variation according to another embodiment of the present invention.

Fig. 14 is a schematic diagram of the system architecture of the seventh variation and the first variation of another embodiment of the present invention.

FIG. 15 is a schematic diagram of the system architecture of the seventh variation and the second deformation system according to another embodiment of the present invention.

Fig. 16 is a schematic diagram of the system architecture of the eighth variation according to another embodiment of the present invention.

Fig. 17 is a schematic diagram of the system architecture of the ninth variation, the first variation, according to another embodiment of the present invention.

Fig. 18 is a schematic diagram of the system architecture of the ninth variation and the second deformation system according to another embodiment of the present invention.

Fig. 19 is a flowchart of main steps of the present invention.

Fig. 20 is a flowchart of another step of the present invention.

Symbol Description:

10. Pretreatment equipment 11. Gas intake pipeline

20. First carbon dioxide adsorption runner 201. Adsorption zone

202. Desorption area 21. Pretreatment gas pipeline

211. Fan 22. First clean air discharge pipeline

221. Fan 23. First hot gas delivery pipeline

24. The first desorption gas pipeline 241. Fan

30. The first heating device 31. The first heating air intake pipeline

311, fan 40, second carbon dioxide adsorption runner

401, adsorption area 402, desorption area

41. Second net gas discharge pipeline 411. Fan

42. The second hot gas delivery pipeline 43. The second desorption gas pipeline

431. Fan 432. The first fan

432. Second blower fan 44. Recirculation pipeline

441, valve 50, second heating device

51. Second heating air intake pipeline 511. Fan

60. Chimney 70. Twin-tower polymer tubular membrane equipment

71. The first tower-type polymer tubular membrane group 711. The first adsorption tower

712. First air intake pipeline 7121. Valve

713. First exhaust pipeline 7131. Valve

714. First regeneration pipeline 7141. Valve

715. First compressed gas pipeline 7151. Valve

72. The second tower polymer tubular membrane group 721. The second adsorption tower

722. Second air intake pipeline 7221. Valve

723. Second exhaust pipeline 7231. Valve

724. Second regeneration pipeline 7241. Valve

725. First compressed gas pipeline 7251. Valve

73. Exhaust pipeline 74. Hot gas pipeline

75. Compressed gas output pipeline 76. First heater

77. Second heater 78. Heater

80. Cooling device 90. Heat exchanger

901, cold side pipeline 902, hot side pipeline

S100, gas input pretreatment equipment

S110, first carbon dioxide adsorption rotor adsorption

S120. Emission from the first carbon dioxide adsorption runner

S130, transporting the first hot gas for desorption

S140, outputting the gas after desorption and concentration of carbon dioxide

S150, second carbon dioxide adsorption rotor adsorption

S160. Emission from the second carbon dioxide adsorption runner

S170, transporting the second hot gas for desorption

S180, outputting the gas after desorption and concentration of carbon dioxide

S200, transported to the twin-tower polymer tubular membrane equipment

Detailed ways

In order to make the object, technical solution and advantages of the present invention clearer, the present invention will be further described in detail below in conjunction with specific embodiments and with reference to the accompanying drawings.

Please refer to Figures 1-20, which are schematic diagrams of embodiments of the present invention, and the best implementation of the carbon dioxide adsorption runner system and method of the present invention is to apply carbon dioxide in the semiconductor industry, optoelectronic industry, chemical related industries or manufacturing related industries Treatment system or similar equipment can mainly increase the efficiency of carbon dioxide enrichment, and has the performance of concentrating and recovering carbon dioxide.

The carbon dioxide adsorption runner system of the present invention mainly includes a pretreatment device 10, a first carbon dioxide adsorption runner 20, a first heating device 30, a second carbon dioxide adsorption runner 40, a second heating device 50 and A chimney 60 (as shown in Figures 1 to 18), wherein one side of the pretreatment equipment 10 is connected to a gas inlet pipeline 11, and one end of the gas inlet pipeline 11 is connected to the production site, office building, etc. The place of carbon dioxide or the area (not shown) that produces carbon dioxide indoors, so that the gas inlet pipeline 11 can transport gas containing carbon dioxide or other gases, and the pretreatment equipment 10 is a cooler, a condenser, a dehumidifier, Any one of the coolers is used to pre-treat the gas so that the gas can release heat energy to improve the adsorption efficiency. In addition, the first heating device 30 is provided with a first heating air intake pipeline 31, and the second heating device 50 is provided with a second heating air intake pipeline 51, and the first heating device 30 and the second heating device 50 are electric heaters. Any one of heater, natural gas heater, heat exchanger, heat medium oil heat exchanger, shell and tube heat exchanger, fin tube heat exchanger, plate heat exchanger or heat pipe heat exchanger.

In addition, the first carbon dioxide adsorption runner 20 of the present invention is provided with an adsorption zone 201 and a desorption zone 202, and the first carbon dioxide adsorption runner 20 is connected with a pretreatment gas pipeline 21, a first clean gas discharge pipeline 22, a The first hot gas delivery pipeline 23 and a first desorption gas pipeline 24 (as shown in FIGS. The two carbon dioxide adsorption wheels 40 are connected to a second clean gas discharge pipeline 41 , a second hot gas delivery pipeline 42 and a second desorption gas pipeline 43 (as shown in FIGS. 1 to 18 ). Wherein the first carbon dioxide adsorption rotor 20 and the second carbon dioxide adsorption rotor 40 are respectively zeolite concentration wheels or concentration wheels 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 side of the adsorption zone 201 of the first carbon dioxide adsorption wheel 20, The gas containing carbon dioxide or other gases pre-treated by the pretreatment device 10 can be transported to the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 through the pretreatment gas pipeline 21 for carbon dioxide adsorption (As shown in Figure 1 to Figure 4). Wherein the pretreatment gas pipeline 21 is provided with a blower fan 211 (as shown in Figure 3 and Figure 4 ), so that the pretreated gas containing carbon dioxide in the pretreatment gas pipeline 21 can be processed by the blower fan 211 or Other gases are pushed and pulled into the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 . In addition, one end of the first clean gas discharge pipeline 22 is connected to the other side of the adsorption area 201 of the first carbon dioxide adsorption wheel 20 , and the other end of the first clean gas discharge pipeline 22 is connected to the chimney 60 (As shown in FIGS. 1 to 4 ), the gas after adsorption of carbon dioxide produced by the adsorption zone 201 of the first carbon dioxide adsorption runner 20 can be transported through the first clean gas discharge pipeline 22 to the chimney 60 for discharge to atmosphere. Wherein the first clean gas discharge pipeline 22 is provided with a blower fan 221 (as shown in Figure 3 and Figure 4 ), so that the gas after the carbon dioxide adsorption in the first clean gas discharge pipeline 22 can be pushed and pulled by the blower fan 221 to the chimney 60 for discharge.

In addition, the other side of the desorption zone 202 of the first carbon dioxide adsorption wheel 20 is connected to one end of the first hot gas delivery pipeline 23, and the other end of the first hot gas delivery pipeline 23 is connected to the first heating device 30 connected (as shown in Figures 1 to 4), and the first heating device 30 is input with external air or other sources of gas through the first heating air intake line 31, so that the first heating device 30 can be controlled by the first heating device 30 The temperature of the external air or gas from other sources input by a heating intake pipeline 31 is raised to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is transported through the first hot gas delivery pipeline 23 to the desorption zone 202 of the first carbon dioxide adsorption wheel 20 for desorption. Wherein the first heating intake pipeline 31 is provided with a fan 311 (as shown in Figure 3 and Figure 4 ), so that the outside air in the first heating intake pipeline 31 or the gas from other sources can be passed through the fan 311 Push and pull into the first heating device 30 .

One side of the desorption area 202 of the first carbon dioxide adsorption wheel 20 is connected to one end of the first desorption gas pipeline 24, and the other end of the first desorption gas pipeline 24 is connected to the second carbon dioxide adsorption pipeline. One side of the adsorption zone 401 of the runner 40 is connected (as shown in FIGS. 1 to 4 ), so as to desorb the carbon dioxide desorbed once desorbed through the desorption zone 202 of the first carbon dioxide adsorption runner 20. The concentrated gas is delivered to the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 through the first desorption gas pipeline 24 for re-adsorption. Wherein the first desorption gas pipeline 24 is provided with a blower fan 241 (as shown in Figure 3 and Figure 4), so that the carbon dioxide desorbed once in the first desorption gas pipeline 24 can be desorbed by the blower fan 241 The concentrated gas is pushed and pulled into the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 .

In addition, the other side of the adsorption area 401 of the second carbon dioxide adsorption runner 40 is connected with the second clean gas discharge pipeline 41, and the other end of the second clean gas discharge pipeline 41 is connected with the chimney 60 (such as 1 to 4), the gas after the carbon dioxide adsorption produced after the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 is re-adsorbed can be transported to the second clean gas discharge pipeline 41. The chimney 60 to carry out the discharge to atmosphere. Wherein the second clean gas discharge pipeline 41 is provided with a blower fan 411 (as shown in Figure 3 and Figure 4 ), so that the gas after the carbon dioxide adsorption in the second clean gas discharge pipeline 41 can be pushed and pulled by the blower fan 411 to the chimney 60 for discharge.

In addition, the other side of the desorption zone 402 of the second carbon dioxide adsorption wheel 40 is connected to one end of the second hot gas delivery pipeline 42 , and the other end of the second hot gas delivery pipeline 42 is connected to the second heating device 50 connected (as shown in FIGS. 1 to 4 ), and the second heating device 50 is input with external air or gas from other sources through the second heating air intake pipeline 51, so that the second heating device 50 can be controlled by the second heating device 50 Second, the external air or other sources of gas input by the heating intake pipeline 51 is heated up to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 is transported through the second hot gas delivery pipeline 42 to the desorption zone 402 of the second carbon dioxide adsorption wheel 40 for desorption. Wherein the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 4 ), so that the outside air in the second heating intake pipeline 51 or the gas from other sources can be pushed and pulled to the second heating intake pipeline 51 by the fan 511. Inside the second heating device 50 .

And one side of the desorption area 402 of the second carbon dioxide adsorption runner 40 is connected with an end of the second desorption gas pipeline 43 (as shown in FIGS. The desorbed and concentrated carbon dioxide desorbed in the desorption area 402 of the runner 40 to produce secondary desorption is output through the second desorption gas pipeline 43 for subsequent treatment. Wherein the so-called follow-up treatment (not shown in the figure) includes that the desorbed and concentrated gas of carbon dioxide transported by the second desorbed gas pipeline 43 can be stored through a steel cylinder or a steel tank, or transported and supplied to other Places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola fields, chemical plants, or food industry factories, etc., as raw materials, so that the gas after secondary desorption of carbon dioxide desorption and concentration can have subsequent applications effectiveness. Wherein the second desorption gas pipeline 43 is provided with a fan 431 (as shown in Figure 3 and Figure 4 ), so that the carbon dioxide desorbed in the second desorption gas pipeline 43 can be desorbed by the fan 431 With concentrated gas push-pull output.

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 rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating The design of the 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. 2 ) is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43. The gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the gas energy after the second desorption gas pipeline 43 transports the carbon dioxide desorbed and concentrated Return from the recirculation pipeline 44 to the second heating intake pipeline 51, and then mix with the outside air in the second heating intake pipeline 51 or gas from other sources before entering the second heating device 50, Or the gas in the second heating intake pipeline 51 is not mixed with external air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In addition, the second variation of the main embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption rotor 20, the first heating device 30, the second carbon dioxide adsorption rotor 40, the second heating The design of the device 50 and a chimney 60 has already been described and will not be repeated here. Therefore, the second variation of the main embodiment (as shown in FIG. 3 ) is that the second desorption gas pipeline 43 is also provided with a recirculation pipeline 44 (please refer to the content of the first variation of the main embodiment, not in This is repeated), and the difference from the first variation of the main embodiment is that the front end and the rear end of the second desorption gas pipeline 43 are respectively provided with a first blower fan 432 and a rear end at one end of the recirculation pipeline 44. A second blower 433 is matched with the recirculation pipeline 44 to form a positive pressure pattern, so that the desorbed and concentrated carbon dioxide in the second desorbed gas pipeline 43 can be squeezed into the recirculation Pipeline 44, and returns to the second heating intake pipeline 51. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In addition, the third variation of the main embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second heating The design of the device 50 and a chimney 60 has already been described and will not be repeated here. Therefore, the third variation of the main embodiment (as shown in FIG. 4 ) is that the second desorption gas pipeline 43 is also provided with a recirculation pipeline 44 (please refer to the content of the first variation of the main embodiment, not in This repeats), and the difference from the first variation of the main embodiment is that the second desorption gas pipeline 43 is provided with a fan 431, and the second heating inlet pipeline 51 is provided with a fan 511, and the second heating inlet pipeline 51 is provided with a fan 511. The fan 511 provided by the gas pipeline 51 is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipe. The air fan 431 provided in the road 43 is in a negative pressure mode, so that the desorbed and concentrated gas of carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second desorbed gas pipeline by the recirculation pipeline 44. The inside of the intake pipe 51 is heated. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

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 in design, and its described related content has been described, and will not be repeated here. Therefore, another embodiment of the present invention is mainly that the other end of the second desorption gas pipeline 43 is connected with a double-tower polymer tubular membrane device 70 (as shown in FIGS. 5 and 6 ), so that the The carbon dioxide desorbed and concentrated gas desorbed for the second time in the second desorbed gas pipeline 43 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 polymer tubular membrane group 71 and a second tower 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 pipeline 712, a first exhaust pipeline 713, a first regeneration pipeline 714 and a first compressed gas pipe Road 715 (as shown in Fig. 5 and Fig. 6), and this second tower type macromolecule tubular membrane group 72 is provided with a second adsorption tower 721, a second inlet pipeline 722, a second exhaust pipeline 723 in addition , a second regeneration pipeline 724 and a second compressed gas pipeline 725 (as shown in Figure 5 and Figure 6), and the first gas inlet 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 are each provided with a valve 7121, 7131, 7141, 7151 (as shown in Figure 5 and Figure 6), and the second tower The second intake gas pipeline 722, the second exhaust pipeline 723, the second regeneration pipeline 724 and the second compressed gas pipeline 725 of the polymer tubular membrane group 72 are respectively provided with a valve 7221, 7231, 7241, 7251 ( As shown in Figure 5 and Figure 6), it is used to control the gas flow between the above-mentioned pipelines.

In addition, in the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 and the second adsorption tower 721 of the second tower-type polymer tubular membrane group 72, there are a plurality of hollow tubular polymer tubular membranes. The membrane adsorption material is filled (as shown in Figure 5 and Figure 6), and the hollow tubular polymer tubular membrane adsorption material is made of high molecular polymer and adsorbent, and the polymer is made of polysulfone ( polysulfone, PSF), polyethersulfone (polyethersulfone, PESF), polyvinylidene fluoride (polyvinylidene fluoride, PVDF), polyphenylsulfone (polyphenylsulfone, PPSU), polyacrylonitrile (polyacrylonitrile), cellulose acetate, cellulose diacetate , polyimide (polyimide, PI), polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-co-glycolic acid (polylactic-co-glycolic acid), polycaprolactone, polyethylene At least one selected from the group consisting of polyvinyl pyrrolidone, ethylenevinyl alcohol, polydimethylsiloxane, polytetrafluoroethylene and cellulose acetate (CA). The diameter and outer diameter of the hollow tubular polymer tubular membrane are more than 2mm, so it has a high specific surface area, is easy to adsorb, and is easy to desorb. Therefore, the amount of adsorbent is smaller than that of the traditional particle type, which can achieve 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 is 10% to 90%, and the adsorbent is any shape of granular body, powder body, hollow fiber body, 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 adsorption The agent is made of molecular sieve, activated carbon, modified alcohol amine, A-type zeolite (such as 3A, 4A or 5A), X-type zeolite (such as 13X), Y-type zeolite (such as ZSM-5), medium-porous molecular sieve (such as MCM- 41, 48, 50 and SBA-15), metal organic framework (Metal Organic Frameworks: MOF) or at least one of the group consisting of graphene.

In addition, the above-mentioned hollow tubular polymer tubular membrane adsorption material is made of inorganic materials (not shown in the figure), wherein the size of the added inorganic materials is from 0.01um to 100um, and the inorganic materials may contain adsorbents, such as adsorption When the agent is used, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the above-mentioned inorganic materials are iron oxide, copper oxide, barium titanate, lead titanate, aluminum oxide, silicon dioxide, aerogel (silica aerogel), bentonite (such as potassium bentonite, sodium bentonite, calcium bentonite and alumina 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 (such as Ca ₃ SiO ₅ , Ca ₃ Si ₂ O ₇ and CaSiO ₃ ), silicon Magnesium silicate (eg Mg ₃ Si ₄ O ₁₀ (OH) ₂ ), sodium silicate (eg Na ₂ SiO ₃ and its hydrates), anhydrous sodium sulfate, zirconium silicate (eg ZrSiO ₄ ), opaque zirconium (For example, 53.89% SiO ₂ .4.46% Al ₂ O ₃ .12.93% ZrO ₂ .9.42% CaO. 2.03% MgO. 12.96% ZnO. 3.73% K ₂ O. 0.58% Na ₂ O) and silicon carbide at least one of .

In another embodiment of the present invention, the first air inlet line 712 of the first tower-type polymer tubular membrane group 71 and the second air inlet line 722 of the second tower-type polymer tubular membrane group 72 are connected to The other end of the second desorption gas pipeline 43 is connected (as shown in FIGS. 5 to 18 ), so that the gas after secondary desorption of carbon dioxide desorption and concentration can be input to the double-tower polymer tube. Type membrane equipment 70 is used for recompression treatment, and the adsorption drying process and regeneration desorption process are respectively carried out through the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane group 72, and when When the first tower-type polymer tubular membrane group 71 is undergoing the adsorption drying procedure, the valve 7121 of the first air inlet pipeline 712 is in an open state (as shown in Figures 7 to 9), and the second tower-type polymer The tubular membrane group 72 then performs the regeneration desorption procedure, so the valve 7221 of the second intake pipeline 722 is in a closed state (as shown in FIGS. 7 to 9 ), and the valve 7121 of the first intake pipeline 712 is closed. Open, so that the gas after secondary desorption in the second desorption gas pipeline 43 is input into the first adsorption tower 711 in the first tower-type polymer tubular membrane group 71 after desorption and concentration of carbon dioxide, and Adsorption drying is performed by the hollow tubular polymer tubular membrane adsorbent in the first adsorption tower 711 .

After a period of time, the first tower-type polymer tubular membrane group 71 performs the adsorption and drying process. Before the adsorption is saturated, the second tower-type polymer tubular membrane group 72 is used to perform the adsorption and drying process. When the second tower-type polymer tubular membrane group 72 is undergoing the adsorption drying process, the valve 7221 of the second inlet pipeline 722 is in an open state (as shown in Figures 10 to 12), and the first tower-type polymer The tubular 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 (as shown in FIGS. 10 to 12 ), and the valve 7121 of the second intake line 722 is closed. The valve is opened, so that the gas after secondary desorption of carbon dioxide desorption and concentration in the second desorption gas pipeline 43 is input into the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72, Adsorption drying is carried out by the hollow tubular polymer tubular membrane adsorbent in the second adsorption tower 721 .

In another embodiment of the present invention, the first exhaust pipeline 713 of the first tower-type polymer tubular membrane group 71 and the second exhaust pipeline 723 of the second tower-type polymer tubular membrane group 72 It is connected with an exhaust output pipeline 73 (as shown in Figure 5 to Figure 18), and the other end of the exhaust output pipeline 73 is in the atmosphere or outside air, and when the first tower polymer tube When the type membrane group 71 carries out the adsorption drying process, the valve 7131 of the first exhaust pipeline 713 is in a closed state (as shown in Figures 7 to 9), and the second tower type polymer tube type membrane group 72 is In order to perform the regeneration desorption process, the valve 7231 of the second exhaust pipeline 723 is in an open state (as shown in FIGS. The gas in the second adsorption tower 721 of the membrane group 72 can be exhausted through the second exhaust pipeline 723, and when the second tower-type polymer tube-type membrane group 72 performs the adsorption drying process, the second The valve 7231 of the exhaust pipeline 723 is in a closed state (as shown in Figures 10 to 12), and the first tower-type polymer tubular membrane group 71 is performing regeneration and desorption procedures, so the first exhaust The valve 7131 of the pipeline 713 is in an open state (as shown in Figures 10 to 12), allowing the gas energy in the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 performing the regeneration desorption procedure The exhaust operation is performed through the first exhaust line 713 .

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 It is connected with a compressed gas output pipeline 75 (as shown in FIGS. 5 to 18 ). When the first tower-type polymer tubular membrane group 71 performs the adsorption drying process, the valve 7151 of the first compressed gas pipeline 715 Then it is in an open state (as shown in FIGS. 7 to 9 ), and the second tower-type polymer tubular membrane group 72 is performing regeneration and desorption procedures, so the valve 7251 of the second compressed gas pipeline 725 is It is in a closed state (as shown in Figures 7 to 9), so the gas after the carbon dioxide desorption and concentration through the secondary desorption can pass through the first adsorption tower 711 of the first tower polymer tubular membrane group 71 The hollow tubular polymer tubular membrane adsorbent inside is used for adsorption and drying, so that the gas after desorption and concentration of the secondary desorbed carbon dioxide can produce a low humidity dew point carbon dioxide compressed dry gas, wherein the low humidity dew point carbon dioxide is compressed and dried. The dew point of the dry gas can reach -40°C to -70°C, and then the compressed dry gas of carbon dioxide with a low humidity dew point flows to the compressed gas output line 75 through the first compressed gas line 715, and passes through the compressed gas output line Road 75 is used for output collection. In addition, when the second tower-type polymer tubular membrane group 72 is performing the adsorption drying process, the valve 7251 of the second compressed gas pipeline 725 is in an open state (as shown in FIGS. 10 to 12 ), and the first tower The type polymer tubular membrane group 71 is to perform the regeneration desorption procedure, so the valve 7151 of the first compressed gas pipeline 715 is in a closed state (as shown in Figures 10 to 12), and through the above-mentioned adsorption In the drying process, the compressed carbon dioxide gas with a low humidity dew point flows to the compressed gas output pipeline 75 through the second compressed gas pipeline 725 , and is output and collected through the compressed gas output pipeline 75 . The so-called collection and use (not shown in the figure) includes storing the compressed dry gas of carbon dioxide in steel cylinders and steel tanks for temporary storage, or directly transporting it to other places that need carbon dioxide, such as greenhouses or seaweed farms, soda cola fields, chemical industry Plants, or food industry factories and other industries as raw materials, so that the carbon dioxide compressed dry gas can have the efficiency of subsequent applications.

In another embodiment 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 The thermal energy pipeline 74 is connected (as shown in Figure 5 to Figure 18), and the first adsorption tower 711 in the first tower-type polymer tubular membrane group 71 or the first adsorption tower 711 in the first tower-type polymer tubular membrane group 71 is transported through the thermal energy pipeline 74. The second adsorption tower 721 in the two-tower polymer tubular membrane group 72 is used for regeneration and desorption. When the first tower polymer tubular membrane group 71 performs the adsorption drying process, the first regeneration pipeline 714 The valve 7141 is in a closed state (as shown in FIGS. 7 to 9 ), and the second tower-type polymer tubular membrane group 72 is performing regeneration and desorption procedures, so the valve 7241 of the second regeneration pipeline 724 is is in an open state (as shown in FIGS. 7 to 9 ), and when the second tower-type polymer tubular membrane group 72 is undergoing an adsorption drying procedure, the valve 7241 of the second regeneration pipeline 724 is in a closed state (as shown in FIGS. 10 to 12), and the first tower-type polymer tubular membrane group 71 is performing a regeneration desorption procedure, so the valve 7141 of the first regeneration pipeline 714 is in an open state (as shown in FIGS. 10 to 12 ). Figure 12).

In addition, the first variation of another 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 The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the first variation of another embodiment (as shown in FIG. 6 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80, and the cooling device 80 is a cooler, a condenser, a dehumidifier, a desuperheater Any one of them is used to treat the desorbed and concentrated gas of carbon dioxide desorbed once in the first desorbed gas pipeline 24, so that the desorbed carbon dioxide desorbed and concentrated gas can release heat energy , and reduce the temperature of the desorbed carbon dioxide desorbed and concentrated gas once desorbed, so as to improve the resorption efficiency when entering the adsorption zone 401 of the second carbon dioxide adsorption runner 40, so as to increase the adsorption of the second carbon dioxide adsorption runner 40 District 401 Potency.

In addition, the second variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the second variation of another embodiment (as shown in FIG. 7 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, not here Repeat), and the first change difference with another embodiment is that the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76, and the second tower-type high The second regeneration pipeline 724 of the molecular tubular membrane group 72 is provided with a second heater 77, wherein the first heater 76 and the second heater 77 are electric heaters, natural gas heaters, heat exchangers or heat medium Any one of the oil heat exchangers, and the first tower polymer tubular membrane can be When the group 71 performs the regeneration desorption process 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 second The first adsorption tower 711 in a tower-type polymer 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.

In addition, the third variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the third variation of another embodiment (as shown in FIGS. 8 and 9 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment. , not repeated here), and the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 7 is provided with a first heater 76, and the second tower-type polymer tubular membrane group 72 The regeneration pipeline 725 is provided with a second heater 77 (please refer to the content of the second variation of another embodiment, which will not be repeated here), and the difference from the second variation of another embodiment is that the second desorbed gas The pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorbed gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51 so that the second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can be returned to the second heating intake pipeline 51 by the recirculation pipeline 44, and then combined with the second The external air in the heated air intake line 51 or the gas from other sources enters the second heating device 50 after being mixed, or the gas in the second heated air intake line 51 is not mixed with the external air or other sources. The gas is mixed. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the third variation of another embodiment of the present invention described above, the second desorption gas pipeline 43 has two kinds of deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline The front end and the rear end of one end connection of 44 are respectively provided with a first blower fan 432 and a second blower fan 433 (as shown in Figure 8 ), and then cooperate with the recirculation pipeline 44 to form a positive pressure pattern, so that the second blower fan 432 The desorbed and concentrated carbon dioxide desorbed in the second desorption gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a fan 431, and the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 9), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the fourth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the fourth variation of another embodiment (as shown in FIG. 10 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, not here Repeat), and the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76, and the second regeneration pipeline of the second tower-type polymer tubular membrane group 72 724 is provided with a second heater 77 (please refer to the content of the second variation of another embodiment, not repeated here), and the fourth variation difference with another embodiment is that the first tower type polymer tube type The thermal energy pipeline 74 that the first regeneration pipeline 714 of the membrane group 71 is connected with the second regeneration pipeline 724 of the second tower type polymer tube membrane group 72 is connected with a heat exchanger 90, and the heat exchanger 90 is located on the first desorption gas pipeline 24 of the first carbon dioxide adsorption wheel 20, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein the heat exchanger 90 One end of the cold-side pipeline 901 is connected to the other end of the heat pipeline 74, and the other end of the cold-side pipeline 901 of the heat exchanger 90 is external air or connected to cooling air so as to enter the heat exchanger 90 After the cold side pipeline 901 for heat exchange, the high-temperature hot gas is delivered to the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 through the heat energy pipeline 74 and the second tower-type The second regeneration pipeline 724 of the polymer tubular membrane group 72 is used for desorption regeneration, and the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the first The desorbed and concentrated carbon dioxide desorbed once in the desorbed gas pipeline 24 can exchange heat through the hot side pipeline 902 of the heat exchanger 90, and then transport it to the cooler 80 for cooling, and finally transport it to the cooler 80 for cooling. Adsorption is carried out in the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 .

In addition, the fifth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the fifth variation of another embodiment (as shown in FIGS. 11 and 12 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment. , not repeated here), and the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 is provided with a first heater 76, and the second tower-type polymer tubular membrane group 72 The regeneration line 724 is provided with a second heater 77 (please refer to the content of the second variation of another embodiment, which is not repeated here), and the first regeneration tube of the first tower-type polymer tubular membrane group 71 The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the road 714 and the second tower-type polymer tubular membrane group 72 is connected to a heat exchanger 90, and the heat exchanger 90 is arranged in the first carbon dioxide adsorption On the first desorption gas pipeline 24 of the runner 20, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902 (please refer to the content of the fourth variation of another embodiment, not in This repeats), and the fourth change difference with another embodiment is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can be desorbed and concentrated by The recirculation pipeline 44 returns to the second heating intake pipeline 51, and then enters the second heating device 50 after mixing with the outside air in the second heating intake pipeline 51 or gas from other sources, or It is only when the gas in the second heating intake pipeline 51 is not mixed with outside air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the fifth variation of another embodiment of the present invention described above, the second desorption gas pipeline 43 has two deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline The front end and the rear end of one end connection of 44 are respectively provided with a first blower fan 432 and a second blower fan 433 (as shown in Figure 11 ), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second blower fan 432 The desorbed and concentrated carbon dioxide desorbed in the second desorption gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a blower 431, and the second heating intake pipeline 51 is provided with a blower 511 (as shown in Figure 12), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the sixth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the sixth variation of another embodiment (as shown in FIG. 13 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, not in This repetition), and the first change difference with another embodiment 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 72 The thermal energy pipeline 74 that the second regeneration pipeline 724 is connected is provided with a heater 78, and wherein this heater 78 is any one of electric heater, natural gas type heater, heat exchanger or heat medium oil heat exchanger, and passes through The high-temperature hot gas generated by the heater 78 of the heat pipeline 74 is transported to the first regeneration pipeline 714 or the second regeneration pipeline 724, and then enters the first tower-type polymer tubular membrane group 71 The first adsorption tower 711 or the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72 are used for regeneration and desorption, and the valve 7141 of the first regeneration pipeline 714 and the second The valve 7241 of the regeneration pipeline 724 is used to control the flow direction.

In addition, the seventh variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the seventh variation of another embodiment (as shown in Figure 14 and Figure 15) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment , not repeated here), and the thermal energy of the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 connected to the second regeneration pipeline 724 of the second tower-type polymer tubular membrane group 72 The pipeline 74 is provided with a heater 78 (please refer to the content of the sixth variation of another embodiment, which will not be repeated here), and the difference from the sixth variation of another embodiment is that the second desorption gas pipeline 43 A recirculation pipeline 44 is provided, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the The second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can be returned to the second heated intake pipeline 51 by the recirculation pipeline 44, and then connected with the second heated intake pipeline. The external air in the pipeline 51 or the gas from other sources enters the second heating device 50 after being mixed, or the gas in the second heating intake pipeline 51 is not mixed with the external air or the gas from other sources . Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the seventh variation of another embodiment of the present invention described above, the second desorption gas pipeline 43 has two deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline The front end and the rear end of one end connection of 44 are respectively provided with a first blower fan 432 and a second blower fan 433 (as shown in Figure 14 ), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second blower fan 432 The desorbed and concentrated carbon dioxide desorbed in the second desorption gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a blower 431, and the second heating intake pipeline 51 is provided with a blower 511 (as shown in Figure 15), and the second heating intake pipeline 511 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the eighth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the eighth variation of another embodiment (as shown in FIG. 16 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment, not here Repeat), and the thermal energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 A heater 78 is provided (please refer to the content of the sixth variation of another embodiment, which will not be repeated here), and the difference from the sixth variation of another embodiment is that the first tower-type polymer tubular membrane group 71 The thermal energy pipeline 74 connected to the first regeneration pipeline 714 of the second tower type polymer tubular membrane group 72 and the second regeneration pipeline 724 is connected to a heat exchanger 90, and the heat exchanger 90 is located at On the first desorption gas pipeline 24 of the first carbon dioxide adsorption wheel 20, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein the cold side pipeline of the heat exchanger 90 One end of the road 901 is connected to the other end of the heat pipeline 74, and the other end of the cold side pipeline 901 of the heat exchanger 90 is external air or connected to cooling air so as to enter the cold side of the heat exchanger 90. Pipeline 901 for heat exchange, and then through the heat pipeline 74 to send high-temperature hot gas to the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tube The second regeneration pipeline 724 of the membrane group 72 is used for desorption and regeneration, and the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the first desorption gas The desorbed carbon dioxide desorbed and concentrated gas in the pipeline 24 can pass through the hot side pipeline 902 of the heat exchanger 90 for heat exchange, and then transported to the cooler 80 for cooling, and finally transported to the second Two carbon dioxide adsorption wheels 40 are used for adsorption in the adsorption area 401 .

In addition, the ninth variation of another embodiment of the present invention is based on the above-mentioned main pretreatment equipment 10, the first carbon dioxide adsorption runner 20, the first heating device 30, the second carbon dioxide adsorption runner 40, the second The heating device 50 and a chimney 60 are designed, and the relevant content has been described and will not be repeated here. Therefore, the ninth variation of another embodiment (as shown in Figure 17 and Figure 18) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another embodiment , not repeated here), and the thermal energy of the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 connected to the second regeneration pipeline 724 of the second tower-type polymer tubular membrane group 72 The pipeline 74 is provided with a heater 78 (please refer to the content of the sixth variation of another embodiment, which is not repeated here), and the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 is connected with the The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the second tower-type polymer tubular membrane group 72 is connected to a heat exchanger 90, and the heat exchanger 90 is arranged on the first carbon dioxide adsorption runner 20 On the first desorption gas pipeline 24, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902 (please refer to the content of the eighth variation of another embodiment, not repeated here), And the eighth variation difference from another embodiment is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, And the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can pass through the recirculation pipe. The road 44 returns to the second heating intake pipeline 51, and then enters the second heating device 50 after being mixed with the outside air in the second heating intake pipeline 51 or gas from other sources, or when the The second heating gas in the intake pipe 51 does not mix with external air or other sources of gas. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the ninth variation of another embodiment of the present invention, the second desorption gas pipeline 43 has two kinds of deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline The front end and the rear end of one end connection of 44 are respectively provided with a first fan 432 and a second fan 433 (as shown in Figure 17), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second The desorbed and concentrated carbon dioxide desorbed in the second desorption gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a fan 431, and the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 18), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

And the carbon dioxide adsorption runner treatment method of the present invention is mainly used in the carbon dioxide adsorption runner system, and is provided with a pretreatment device 10, a first carbon dioxide adsorption runner 20, a first heating device 30, a second carbon dioxide adsorption Runner 40, a second heating device 50 and a chimney 60 (as shown in Figure 1 to Figure 18), and this first carbon dioxide adsorption runner 20 is provided with adsorption area 201 and desorption area 202 in addition, and this first carbon dioxide adsorption The runner 20 is connected to a pretreatment intake pipeline 21, a first clean gas discharge pipeline 22, a first hot gas delivery pipeline 23 and a first desorption gas pipeline 24 (as shown in Figures 1 to 18) , In addition, the second carbon dioxide adsorption runner 40 is provided with an adsorption zone 401 and a desorption zone 402, and 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 The second desorption gas pipeline 43 (as shown in Figures 1 to 18), and the first heating device 30 is provided with a first heating inlet pipeline 31, and the second heating device 50 is provided with a second heating inlet pipeline 51, and the first heating device 30 and the second heating device 50 are electric heaters, natural gas heaters, heat exchangers, heat medium oil heat exchangers, shell and tube heat exchangers, fin tube heat exchangers, Any one of a plate heat exchanger or a heat pipe heat exchanger, and the pretreatment equipment 10 is provided with a gas inlet pipeline 11 (as shown in FIGS. 1 to 18 ). The first carbon dioxide adsorption wheel 20 and the second carbon dioxide adsorption wheel 40 are respectively zeolite concentration wheels or concentration wheels made of other materials.

The main steps of the processing method (as shown in FIG. 19 ) include: Step S100 gas input into the pre-processing equipment: the gas is sent into the pre-processing equipment 10 through the gas inlet pipeline 11 for processing. After the above step S100 is completed, the next step S110 is performed.

Wherein one end of the above-mentioned gas inlet pipeline 11 is to be connected to a place where carbon dioxide is produced such as a manufacturing site, an office building, or an indoor area (not shown) where carbon dioxide is produced, so that the gas inlet pipeline can transport gas containing carbon dioxide or It is other gases, and the pretreatment equipment 10 is any one of cooler, condenser, dehumidifier, and desuperheater, which is used to pre-treat the gas so that the gas can release heat energy to improve the adsorption efficiency.

In addition, the next step S110 is the first carbon dioxide adsorption rotor adsorption: the gas processed by the pretreatment equipment 10 is output to the first carbon dioxide adsorption rotor 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 above-mentioned pretreatment gas pipeline 21 is connected to the other side of the pretreatment equipment 10, and the other end of the pretreatment gas pipeline 21 is connected to one side of the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 , so that the gas containing carbon dioxide or other gases that have been pre-treated by the pretreatment device 10 can be transported to the adsorption zone 201 of the first carbon dioxide adsorption runner 20 through the pretreatment gas pipeline 21 to remove carbon dioxide Adsorption (as shown in Figures 1 to 4). Wherein the pretreatment gas pipeline 21 is provided with a blower fan 211 (as shown in Figure 3 and Figure 4 ), so that the pretreated gas containing carbon dioxide in the pretreatment gas pipeline 21 can be processed by the blower fan 211 or Other gases are pushed and pulled into the adsorption zone 201 of the first carbon dioxide adsorption wheel 20 .

In addition, step S120, which is carried out in the next step, is discharged by the first carbon dioxide adsorption runner: the gas adsorbed by the carbon dioxide produced by the adsorption area 201 of the first carbon dioxide adsorption runner 20 is discharged from the first clean gas discharge pipeline 22 The other end is output to the chimney 60 for discharge. After the above step S120 is completed, the next step S130 is performed.

Wherein one end of the above-mentioned first clean gas discharge pipeline 22 is connected with the other side of the adsorption area 201 of the first carbon dioxide adsorption runner 20, and the other end of the first clean gas discharge pipeline 22 is connected with the chimney 60 connection (as shown in FIGS. 1 to 4 ), so that the gas after the adsorption of carbon dioxide produced by the adsorption zone 201 of the first carbon dioxide adsorption runner 20 can be discharged through the first clean gas discharge pipeline 22 It is sent to the chimney 60 for discharge to the atmosphere. Wherein the first clean gas discharge pipeline 22 is provided with a blower fan 221 (as shown in Figure 3 and Figure 4 ), so that the gas after the carbon dioxide adsorption in the first clean gas discharge pipeline 22 can be pushed and pulled by the blower fan 221 to the chimney 60 for discharge.

In addition, the step S130 carried out in the next step transports the first hot gas for desorption: through the first hot gas delivery pipeline 23 connected to the first heating device 30, the high-temperature hot gas is delivered to the desorption of the first carbon dioxide adsorption runner 20 Desorption is carried out in the attachment area 202. After the above step S130 is completed, the next step S140 is performed.

Wherein the other side of the desorption zone 202 of the first carbon dioxide adsorption wheel 20 is connected to one end of the first hot gas delivery pipeline 23, and the other end of the first hot gas delivery pipeline 23 is connected to the first heating device 30 connection (as shown in Figures 1 to 4), and the first heating device 30 is input with external air or other sources of gas through the first heating intake pipeline 31, so that the first heating device 30 can be controlled by the first heating device 30 The temperature of the outside air or gas from other sources input by the first heating intake pipeline 31 is raised to form high-temperature hot gas, and then the high-temperature hot gas generated by the first heating device 30 is passed through the first hot gas delivery pipeline 23 to It is sent to the desorption zone 202 of the first carbon dioxide adsorption wheel 20 to be used for desorption. Wherein the first heating intake pipeline 31 is provided with a fan 311 (as shown in Figure 3 and Figure 4 ), so that the outside air in the first heating intake pipeline 31 or the gas from other sources can be passed through the fan 311 Push and pull into the first heating device 30 .

In addition, step S140 carried out in the next step outputs the desorbed and concentrated gas of carbon dioxide: the desorbed and concentrated gas of carbon dioxide desorbed once through the desorption zone 202 of the first carbon dioxide adsorption runner 20 is produced by the The other end of the first desorption gas pipeline 24 is output. After the above step S140 is completed, the next step S150 is performed.

In addition, the second step S150 carried out in the next step is adsorbed by the second carbon dioxide adsorption wheel: the desorbed and concentrated carbon dioxide desorbed once in the first desorbed gas pipeline 24 is transported to the adsorption of the second carbon dioxide adsorption wheel 40 One side of zone 401 for resorption. After the above step S150 is completed, the next step S160 is performed.

Wherein one side of the desorption zone 202 of the first carbon dioxide adsorption wheel 20 is connected to one end of the first desorption gas pipeline 24, and the other end of the first desorption gas pipeline 24 is connected to the second carbon dioxide One side of the adsorption area 401 of the adsorption wheel 40 is connected (as shown in FIGS. 1 to 4 ), so as to desorb the carbon dioxide desorbed once desorbed through the desorption area 202 of the first carbon dioxide adsorption wheel 20. The concentrated gas is transported to the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 through the first desorption gas pipeline 24 for re-adsorption. Wherein the first desorption gas pipeline 24 is provided with a blower fan 241 (as shown in Figure 3 and Figure 4), so that the carbon dioxide desorbed once in the first desorption gas pipeline 24 can be desorbed by the blower fan 241 The concentrated gas is pushed and pulled into the adsorption zone 401 of the second carbon dioxide adsorption wheel 40 .

In addition, step S160, which is carried out in the next step, is discharged from the second carbon dioxide adsorption runner: the gas adsorbed by the carbon dioxide produced by the adsorption area 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 S160 is completed, the next step S170 is performed.

Wherein the other side of the adsorption zone 401 of the second carbon dioxide adsorption runner 40 is connected with the second clean gas discharge pipeline 41, and the other end of the second clean gas discharge pipeline 41 is connected with the chimney 60 ( As shown in Figures 1 to 4), the gas after the carbon dioxide adsorption produced after the adsorption zone 401 of the second carbon dioxide adsorption runner 40 is re-adsorbed can be transported through the second clean gas discharge pipeline 41 to the chimney 60 for discharge to atmosphere. Wherein the second clean gas discharge pipeline 41 is provided with a blower fan 411 (as shown in Figure 3 and Figure 4 ), so that the carbon dioxide in the second clean gas discharge pipeline 41 can be adsorbed and pushed and pulled by the blower fan 411 to the chimney 60 for discharge.

In addition, in the next step S170, the second hot gas is delivered for desorption: through the second hot gas delivery pipeline 42 connected to the second heating device 50, the high-temperature hot gas is delivered to the second carbon dioxide adsorption wheel 40 for desorption. Attachment zone 402 performs desorption. After the above step S170 is completed, the next step S180 is performed.

Wherein the other side of the desorption zone 402 of the second carbon dioxide adsorption wheel 40 is connected to one end of the second hot gas delivery pipeline 42, and the other end of the second hot gas delivery pipeline 42 is connected to the second heating device 50 connection (as shown in Figures 1 to 4), and the second heating device 50 is input from the second heating air intake line 51 or other sources of gas, so that the second heating device 50 can be controlled by the second heating device 50 The temperature of the outside air or gas from other sources input by the second heating intake pipeline 51 is raised to form high-temperature hot gas, and then the high-temperature hot gas generated by the second heating device 50 is passed through the second hot gas delivery pipeline 42 to It is sent to the desorption zone 402 of the second carbon dioxide adsorption wheel 40 to be used for desorption. Wherein the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 4 ), so that the outside air in the second heating intake pipeline 51 or the gas from other sources can be pushed and pulled to the second heating intake pipeline 51 by the fan 511. Inside the second heating device 50 .

In addition, the step S180 carried out in the next step outputs the gas after desorption and concentration of carbon dioxide: the gas after desorption and concentration of carbon dioxide generated by the second desorption through the desorption zone 402 of the second carbon dioxide adsorption wheel 40 is obtained by the second carbon dioxide adsorption wheel 40. The other end of the two desorption gas pipelines 43 is output.

Wherein one side of the desorption zone 402 of the above-mentioned second carbon dioxide adsorption runner 40 is connected with an end of the second desorption gas pipeline 43 (as shown in FIGS. 1 to 4 ), so that the second carbon dioxide can be passed through The desorbed and concentrated carbon dioxide desorbed in the desorption zone 402 of the adsorption wheel 40 to produce secondary desorption is output through the second desorption gas pipeline 43 for subsequent treatment. Wherein the so-called follow-up treatment (not shown in the figure) includes that the desorbed and concentrated gas of carbon dioxide transported by the second desorbed gas pipeline 43 can be stored through a steel cylinder or a steel tank, or transported and supplied to other Places that require carbon dioxide, such as greenhouses or seaweed farms, soda cola fields, chemical plants, or food industry factories, etc., as raw materials, so that the gas after secondary desorption of carbon dioxide desorption and concentration can have subsequent applications effectiveness. Wherein the second desorption gas pipeline 43 is provided with a blower fan 431 (as shown in Figure 3 and Figure 4 ), so that the second desorption carbon dioxide in the second desorption gas pipeline 43 can be penetrated through the blower fan 431 Push-pull output of desorbed and concentrated gas.

In addition, in the main steps of the present invention, the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43 (as shown in Fig. 3 and Fig. 4), and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the second desorbed carbon dioxide desorbed and concentrated gas can be transported by the second desorbed gas pipeline 43 Return from the recirculation pipeline 44 to the second heating intake pipeline 51, and then mix with the outside air in the second heating intake pipeline 51 or gas from other sources before entering the second heating device 50, Or the gas in the second heating intake pipeline 51 is not mixed with external air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the above-mentioned main steps of the present invention, the second desorption gas pipeline 43 has two kinds of deformations, wherein the first deformation is the front end of the second desorption gas pipeline 43 at the connection of one end of the recirculation pipeline 44 and the rear end are respectively provided with a first blower 432 and a second blower 433 (as shown in Figure 3 ), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second desorption gas pipeline 43 The desorbed and concentrated carbon dioxide desorbed for the second time can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a blower 431, and the second heating intake pipeline 51 is provided with a blower 511 (as shown in Figure 4), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

Furthermore, another step of the present invention is based on the above step S100 gas input pretreatment equipment, step S110 first carbon dioxide adsorption runner adsorption, step S120 first carbon dioxide adsorption runner discharge, step S130 transporting the first hot gas for desorption Attachment, step S140 output the gas after carbon dioxide desorption and concentration, step S150 second carbon dioxide adsorption rotor adsorption, step S160 second carbon dioxide adsorption rotor discharge, step S170 transport the second hot gas for desorption, step S180 output carbon dioxide desorption concentration In terms of the design of the latter gas, the relevant content has been explained and will not be repeated here. Therefore, the present invention includes the following steps (as shown in FIG. 20 ) after outputting the gas after carbon dioxide desorption and concentration in step S180, and step S200 is transported to the double-tower polymer tubular membrane equipment: the second desorption gas pipeline The desorbed and concentrated carbon dioxide in 43 is transported to a double-tower polymer tubular membrane device 70 for processing. The desorbed and concentrated carbon dioxide desorbed through the second desorbed gas pipeline 43 can be recompressed through the double-tower polymer tubular membrane device 70 to form a compressed dry gas of carbon dioxide (such as Figure 5 and Figure 6).

Wherein the above-mentioned double-tower polymer tubular membrane equipment 70 is provided with a first tower polymer tubular membrane group 71 and a second tower polymer tubular membrane group 72, and the first tower polymer tubular membrane Membrane group 71 is provided with a first adsorption tower 711, a first inlet pipeline 712, a first exhaust pipeline 713, a first regeneration pipeline 714 and a first compressed gas pipeline 715 (as shown in Fig. 5 and Fig. 6), and the second tower-type polymer tubular membrane group 72 is provided with a second adsorption tower 721, a second intake pipeline 722, a second exhaust pipeline 723, and a second regeneration pipeline 724 And a second compressed gas pipeline 725 (as shown in Figure 5 and Figure 6), and the first gas inlet pipeline 712, the first exhaust pipeline 713, The first regeneration pipeline 714 and the first compressed gas pipeline 715 are each provided with a valve 7121, 7131, 7141, 7151 (as shown in Figure 5 and Figure 6), and the second tower polymer tubular membrane group 72 The second intake gas pipeline 722, the second exhaust pipeline 723, the second regeneration pipeline 724 and the second compressed gas pipeline 725 are each provided with a valve 7221, 7231, 7241, 7251 (as shown in Figure 5 and Figure 6 ) to control the gas flow between the above-mentioned pipelines.

In addition, in the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 and in the second adsorption tower 721 of the second tower-type polymer tubular membrane group 72, there are a plurality of hollow tubular polymer tubes. (as shown in Figure 5 and Figure 6), and the hollow tubular polymer tubular membrane adsorption material is made of high molecular polymer and adsorbent, and the polymer is made of polysulfone ( polysulfone, PSF), polyethersulfone (polyethersulfone, PESF), polyvinylidene fluoride (polyvinylidene fluoride, PVDF), polyphenylsulfone (polyphenylsulfone, PPSU), polyacrylonitrile (polyacrylonitrile), cellulose acetate, cellulose diacetate , polyimide (polyimide, PI), polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-co-glycolic acid (polylactic-co-glycolic acid), polycaprolactone, polyethylene At least one selected from the group consisting of polyvinyl pyrrolidone, ethylenevinyl alcohol, polydimethylsiloxane, polytetrafluoroethylene and cellulose acetate (CA). The diameter and outer diameter of the hollow tubular polymer tubular membrane are more than 2mm, so it has a high specific surface area, is easy to adsorb, and is easy to desorb. Therefore, the amount of adsorbent is smaller than that of the traditional particle type, which can achieve 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 is 10% to 90%, and the adsorbent is any shape of granular body, powder body, hollow fiber body, 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 adsorption The agent is made of molecular sieve, activated carbon, modified alcohol amine, A-type zeolite (such as 3A, 4A or 5A), X-type zeolite (such as 13X), Y-type zeolite (such as ZSM-5), medium-porous molecular sieve (such as MCM- 41, 48, 50 and SBA-15), metal organic framework (Metal Organic Frameworks: MOF) or at least one of the group consisting of graphene.

In addition, the above-mentioned hollow tubular polymer tubular membrane adsorption material is made of inorganic materials (not shown in the figure), wherein the size of the added inorganic materials is from 0.01um to 100um, and the inorganic materials may contain adsorbents, such as adsorption When the agent is used, the ratio of the adsorbent to the inorganic material is 1:20 to 20:1, and the above-mentioned inorganic materials are iron oxide, copper oxide, barium titanate, lead titanate, aluminum oxide, silicon dioxide, aerogel (silica aerogel), bentonite (such as potassium bentonite, sodium bentonite, calcium bentonite and alumina 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 (such as Ca ₃ SiO ₅ , Ca ₃ Si ₂ O ₇ and CaSiO ₃ ), silicon Magnesium silicate (eg Mg ₃ Si ₄ O ₁₀ (OH) ₂ ), sodium silicate (eg Na ₂ SiO ₃ and its hydrates), anhydrous sodium sulfate, zirconium silicate (eg ZrSiO ₄ ), opaque zirconium (For example, 53.89% SiO ₂ .4.46% Al ₂ O ₃ .12.93% ZrO ₂ .9.42% CaO. 2.03% MgO. 12.96% ZnO. 3.73% K ₂ O. 0.58% Na ₂ O) and silicon carbide at least one of .

And in another step of the present invention, the first inlet pipeline 712 of the first tower-type polymer tubular membrane group 71 and the second inlet pipeline 722 of the second tower-type polymer tubular membrane group 72 are connected to the first gas inlet pipeline 722 of the second tower-type polymer tubular membrane group 72. The other end of the second desorption gas pipeline 43 forms a connection (as shown in Figures 5 to 18), so that the gas after the desorption and concentration of carbon dioxide through the secondary desorption can be input to the double-tower polymer tubular membrane Equipment 70 to carry out recompression treatment, and through the first tower type polymer tubular membrane group 71 and the second tower type polymer tubular membrane group 72 to carry out the adsorption drying process and the regeneration desorption process respectively, and when the first When a tower-type polymer tubular membrane group 71 is carrying out the adsorption drying process, the valve 7121 of the first air inlet pipeline 712 is in an open state (as shown in Figures 7 to 9), and the second tower-type polymer tubular membrane The membrane group 72 then performs the regeneration desorption process, so the valve 7221 of the second air intake line 722 is in a closed state (as shown in FIGS. 7 to 9 ), and the valve 7121 of the first air intake line 712 is opened. The carbon dioxide desorbed and concentrated gas that has been desorbed for the second time in the second desorbed gas pipeline 43 is input into the first adsorption tower 711 in the first tower-type polymer tubular membrane group 71, and passes through the The hollow tubular polymer tubular membrane adsorbent in the first 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 and drying process. Before the adsorption is saturated, the second tower-type polymer tubular membrane group 72 is used to perform the adsorption and drying process. When the second tower-type polymer tubular membrane group 72 is undergoing the adsorption drying process, the valve 7221 of the second inlet pipeline 722 is in an open state (as shown in Figures 10 to 12), and the first tower-type polymer The tubular 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 (as shown in FIGS. 10 to 12 ), and the valve 7121 of the second intake line 722 is closed. The valve is opened, so that the gas after secondary desorption of carbon dioxide desorption and concentration in the second desorption gas pipeline 43 is input into the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72, Adsorption drying is carried out by the hollow tubular polymer tubular membrane adsorbent in the second adsorption tower 721 .

And in another step of the present invention, the first exhaust pipeline 713 of the first tower-type polymer tubular membrane group 71 and the second exhaust pipeline 723 of the second tower-type polymer tubular membrane group 72 are connected with a The exhaust output pipeline 73 is connected (as shown in Figure 5 to Figure 18), and the other end of the exhaust output pipeline 73 is in the atmosphere or outside air, and when the first tower type polymer tubular membrane When the group 71 is carrying out the adsorption drying process, the valve 7131 of the first exhaust pipeline 713 is in a closed state (as shown in Figures 7 to 9), and the second tower-type polymer tubular membrane group 72 is for performing Regeneration desorption program, so the valve 7231 of the second exhaust pipeline 723 is in an open state (as shown in Figures 7 to 9), allowing the second tower polymer tubular membrane group that performs the regeneration desorption program The gas in the second adsorption tower 721 of 72 can be exhausted through the second exhaust pipeline 723, and when the second tower-type polymer tubular membrane group 72 performs the adsorption drying process, the second exhaust The valve 7231 of the pipeline 723 is in a closed state (as shown in Figures 10 to 12), and the first tower-type polymer tubular membrane group 71 is performing regeneration and desorption procedures, so the first exhaust pipeline The valve 7131 of 713 is in an open state (as shown in Figures 10 to 12), allowing the gas in the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 performing the regeneration desorption procedure to pass through the first adsorption tower 711. The first exhaust pipeline 713 is used for exhausting.

And 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 The compressed gas output pipeline 75 is connected (as shown in Figure 5 to Figure 18), when the first tower-type polymer tubular membrane group 71 is undergoing the adsorption drying process, the valve 7151 of the first compressed gas pipeline 715 is In the open state (as shown in Figures 7 to 9), the second tower-type polymer tubular membrane group 72 is performing regeneration and desorption procedures, so the valve 7251 of the second compressed gas pipeline 725 is closed State (as shown in Figure 7 to Figure 9), therefore, the gas after the desorption and concentration of carbon dioxide desorbed through the secondary desorption can pass through the first adsorption tower 711 of the first tower-type polymer tubular membrane group 71 The hollow tubular polymer tubular membrane adsorbent is used for adsorption and drying, so that the desorbed carbon dioxide desorbed and concentrated gas can produce a low humidity dew point carbon dioxide compressed dry gas, wherein the low humidity dew point carbon dioxide compressed dry gas The dew point can reach -40°C to -70°C, and then the compressed dry gas of carbon dioxide with a low humidity dew point flows to the compressed gas output line 75 through the first compressed gas line 715, and passes through the compressed gas output line 75 To output collection use. In addition, when the second tower-type polymer tubular membrane group 72 is performing the adsorption drying process, the valve 7251 of the second compressed gas pipeline 725 is in an open state (as shown in FIGS. 10 to 12 ), and the first tower The type polymer tubular membrane group 71 is to perform the regeneration desorption procedure, so the valve 7151 of the first compressed gas pipeline 715 is in a closed state (as shown in Figures 10 to 12), and through the above-mentioned adsorption In the drying process, the compressed carbon dioxide gas with a low humidity dew point flows to the compressed gas output pipeline 75 through the second compressed gas pipeline 725 , and is output and collected through the compressed gas output pipeline 75 . The so-called collection and use (not shown in the figure) includes storing the compressed dry gas of carbon dioxide in steel cylinders and steel tanks for temporary storage, or directly transporting it to other places that need carbon dioxide, such as greenhouses or seaweed farms, soda cola fields, chemical industry Plants, or food industry factories and other industries as raw materials, so that the carbon dioxide compressed dry gas can have the efficiency of subsequent applications.

And 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 heat pipe Road 74 is connected (as shown in Figure 5 to Figure 18), and the first adsorption tower 711 or the second tower in the first tower-type polymer tubular membrane group 71 are transported through the thermal energy pipeline 74 The second adsorption tower 721 in the polymer tubular membrane group 72 is used for regeneration and desorption. When the first tower polymer tubular membrane group 71 is performing the adsorption drying process, the valve 7141 of the first regeneration pipeline 714 Then it is in a closed state (as shown in Figures 7 to 9), and the second tower-type polymer tubular membrane group 72 is performing a regeneration and desorption procedure, so the valve 7241 of the second regeneration pipeline 724 is in a state of open state (as shown in Figures 7 to 9), and when the second tower-type polymer tubular membrane group 72 is undergoing an adsorption drying process, the valve 7241 of the second regeneration pipeline 724 is in a closed state (as shown in Figure 10 12), and the first tower-type polymer tubular membrane group 71 is performing a regeneration desorption procedure, so the valve 7141 of the first regeneration pipeline 714 is in an open state (as shown in Figures 10 to 12 Show).

In addition, the first variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the first variation of another step (as shown in FIG. 6 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80, which is a cooler, a condenser, a dehumidifier, and a cooler. Any one of them is used to treat the desorbed and concentrated gas of the first desorbed carbon dioxide in the first desorbed gas pipeline 24, so that the desorbed and concentrated gas of the first desorbed carbon dioxide can release heat energy, And reduce the temperature of the desorbed carbon dioxide desorbed and concentrated gas once desorbed, so as to improve the resorption efficiency when entering the adsorption zone 401 of the second carbon dioxide adsorption runner 40, so as to increase the adsorption zone of the second carbon dioxide adsorption runner 40 401 performance.

In addition, the second variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the second variation of another step (as shown in FIG. 7 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which will not be repeated here) , and the first change difference with another step is that the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 is provided with a first heater 76, and the second tower polymer tubular membrane The second regeneration pipeline 724 of the membrane group 72 is provided with a second heater 77, wherein the first heater 76 and the second heater 77 are electric heaters, natural gas heaters, heat exchangers or heat medium oil heat exchange Any one of the device, and through the first heater 76 of the first regeneration pipeline 714 and the second heater 77 of the second regeneration pipeline 724 to allow the first tower polymer tubular membrane group 71 to perform When the regenerative desorption program or the second tower polymer tubular membrane group 72 is performing the regenerative desorption program, the first heater 76 or the second heater 77 can be used to 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 third variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the third variation of another step (as shown in FIGS. 8 and 9 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, not in This repeats), and 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 pipe of the second tower-type polymer tubular membrane group 72 Road 724 is provided with a second heater 77 (please refer to the content of the second variation of another step, not repeated here), and the second variation difference with another step is that the second desorption gas pipeline 43 is set There is a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the first The gas after the desorption and concentration of carbon dioxide desorbed by the second desorption gas pipeline 43 can be returned to the second heating intake pipeline 51 by the recirculation pipeline 44, and then combined with the second heating intake pipeline The outside air in 51 or the gas from other sources enters the second heating device 50 after being mixed, or the gas in the second heating intake line 51 is not mixed with the outside air or the gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the third change of another step of the present invention described above, the second desorption gas pipeline 43 has two deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline 44 The front end and the rear end of one end of the joint are respectively provided with a first blower fan 432 and a second blower fan 433 (as shown in FIG. 8 ), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second blower fan 432 The desorbed and concentrated carbon dioxide in the desorbed gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a fan 431, and the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 9), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the fourth variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the fourth variation of another step (as shown in FIG. 10 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which will not be repeated here) , and the first regeneration pipeline 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-type polymer tubular membrane group 72 is provided with There is a second heater 77 (please refer to the content of the second variation of another step, not repeated here), and the fourth variation difference with another step is the difference of the first tower type polymer tubular membrane group 71 The heat energy pipeline 74 that the first regeneration pipeline 714 is connected with the second regeneration pipeline 724 of the second tower type polymer tubular membrane group 72 is connected with a heat exchanger 90, and the heat exchanger 90 is located at the On the first desorption gas pipeline 24 of the first carbon dioxide adsorption wheel 20, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein the cold side pipeline of the heat exchanger 90 One end of 901 is connected to the other end of the heat pipeline 74, and the other end of the cold side pipeline 901 of the heat exchanger 90 is external air or connected to cooling air so as to enter the cold side pipe of the heat exchanger 90. After heat exchange through the pipeline 901, the high-temperature hot gas is delivered to 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 through the heat energy pipeline 74. The second regeneration pipeline 724 of the membrane group 72 is used for desorption regeneration, and the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the first desorption gas pipeline The desorbed carbon dioxide desorbed and concentrated gas in the road 24 can pass through the heat side pipeline 902 of the heat exchanger 90 for heat exchange, then transported to the cooler 80 for cooling, and finally transported to the second The adsorption zone 401 of the carbon dioxide adsorption wheel 40 performs adsorption.

In addition, the fifth variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the fifth variation of another step (as shown in FIGS. 11 and 12 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, not in This repeats), and 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 pipe of the second tower-type polymer tubular membrane group 72 Road 724 is provided with a second heater 77 (please refer to the content of the second variation of another step, not repeated here), and the first regeneration pipeline 714 and the first tower-type polymer tubular membrane group 71 and The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the second tower-type polymer tubular membrane group 72 is connected to a heat exchanger 90, and the heat exchanger 90 is arranged on the first carbon dioxide adsorption runner 20 On the first desorption gas pipeline 24, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902 (please refer to the content of the fourth variation of another step, not repeated here), And the fourth change difference from another step is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and The other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can pass through the recirculation pipeline. 44 returns to the second heating intake pipeline 51, and then enters the second heating device 50 after being mixed with the outside air in the second heating intake pipeline 51 or gas from other sources, or when the second heating intake pipeline 51 is used alone The second is to heat the gas in the intake pipe 51 without mixing with outside air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the fifth variation of another step of the present invention described above, the second desorption gas pipeline 43 has two kinds of deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline 44 The front end and the rear end of one end of the joint are respectively provided with a first fan 432 and a second fan 433 (as shown in Figure 11), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second The desorbed and concentrated carbon dioxide in the desorbed gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a blower 431, and the second heating intake pipeline 51 is provided with a blower 511 (as shown in Figure 12), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the sixth variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the related content has been described and will not be repeated here. Therefore, the sixth variation of another step (as shown in FIG. 13 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which will not be repeated here) , and the first change difference with another step is that the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second regeneration pipe of the second tower-type polymer tubular membrane group 72 The thermal energy pipeline 74 that road 724 is connected is provided with a heater 78, and wherein this heater 78 is any one of electric heater, natural gas type heater, heat exchanger or heat medium oil heat exchanger, and passes through this thermal energy pipeline The high-temperature hot gas generated by the heater 78 of 74 is transported to the first regeneration pipeline 714 or the second regeneration pipeline 724, and then enters the first adsorbent in the first tower-type polymer tubular membrane group 71. Tower 711 or the second adsorption tower 721 in the second tower-type polymer tubular membrane group 72 are used for regeneration and desorption, and the valve 7141 of the first regeneration pipeline 714 and the second regeneration pipeline 724 The valve 7241 to control the flow direction.

In addition, the seventh variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the related content has been described and will not be repeated here. Therefore, the seventh variation of another step (as shown in FIGS. 14 and 15 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, not in This repeats), and the thermal energy pipeline that the first regeneration pipeline 714 of this first tower type polymer tubular membrane group 71 is connected with the second regeneration pipeline 724 of this second tower type polymer tubular membrane group 72 74 is provided with a heater 78 (please refer to the content of the sixth variation of another step, not repeated here), and the sixth variation difference with another step is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the other end of the recirculation pipeline 44 is connected to the second heating intake pipeline 51, so that the second desorption gas The carbon dioxide desorbed and concentrated gas transported by the gas pipeline 43 can be returned to the second heating intake pipeline 51 by the recirculation pipeline 44, and then combined with the gas in the second heating intake pipeline 51. The external air or gas from other sources enters the second heating device 50 after being mixed, or the gas in the second heating intake line 51 is not mixed with external air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the seventh variation of another step of the present invention described above, the second desorption gas pipeline 43 has two deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline 44 The front end and the rear end of one end of the joint are respectively provided with a first fan 432 and a second fan 433 (as shown in Figure 14), and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second The desorbed and concentrated carbon dioxide in the desorbed gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a blower 431, and the second heating intake pipeline 51 is provided with a blower 511 (as shown in Figure 15), and the second heating intake pipeline 511 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

In addition, the eighth variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the eighth variation of another step (as shown in FIG. 16 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, which will not be repeated here) , and the thermal energy pipeline 74 connected to the first regeneration pipeline 714 of the first tower polymer tubular membrane group 71 and the second regeneration pipeline 724 of the second tower polymer tubular membrane group 72 is provided with a Heater 78 (please refer to the content of the sixth change of another step, not repeated here), and the sixth change difference with another step is the first regeneration of the first tower polymer tubular membrane group 71 The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the pipeline 714 and the second tower-type polymer tubular membrane group 72 is connected to a heat exchanger 90, and the heat exchanger 90 is arranged on the first carbon dioxide On the first desorption gas pipeline 24 of the adsorption wheel 20, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902, wherein one end of the cold side pipeline 901 of the heat exchanger 90 Form connection with the other end of this heat pipeline 74, the other end of the cold side pipeline 901 of this heat exchanger 90 is external air or connects cooling air, so that can enter the cold side pipeline 901 of this heat exchanger 90 After heat exchange, the high-temperature hot gas is sent to the first regeneration pipeline 714 of the first tower-type polymer tubular membrane group 71 and the second tower-type polymer tubular membrane group 72 through the heat energy pipeline 74 The second regeneration pipeline 724 is used for desorption regeneration, and the first desorption gas pipeline 24 is connected with the hot side pipeline 902 of the heat exchanger 90, so that the first desorption gas pipeline 24 The desorbed carbon dioxide desorbed and concentrated gas can be heat-exchanged through the hot side pipeline 902 of the heat exchanger 90, then transported to the cooler 80 for cooling, and finally transported to the second carbon dioxide adsorption converter. The adsorption zone 401 of the wheel 40 performs adsorption.

In addition, the ninth variation of another step of the present invention is based on the design of the above-mentioned step S200 conveying to the double-tower polymer tubular membrane equipment, and the relevant content has been described and will not be repeated here. Therefore, the ninth variation of another step (as shown in FIGS. 17 and 18 ) is that the first desorption gas pipeline 24 is provided with a cooling device 80 (please refer to the content of the first variation of another step, not in This repeats), and the thermal energy pipeline that the first regeneration pipeline 714 of this first tower type polymer tubular membrane group 71 is connected with the second regeneration pipeline 724 of this second tower type polymer tubular membrane group 72 74 is provided with a heater 78 (please refer to the content of the 6th kind of variation of another step, do not repeat at this), also have the first regeneration line 714 of the first tower type macromolecule tubular membrane group 71 and the second tower The thermal energy pipeline 74 connected to the second regeneration pipeline 724 of the type polymer tubular membrane group 72 is connected with a heat exchanger 90, and the heat exchanger 90 is arranged on the first desorption of the first carbon dioxide adsorption runner 20. Attached to the gas pipeline 24, and the heat exchanger 90 is provided with a cold side pipeline 901 and a hot side pipeline 902 (please refer to the content of the eighth change in another step, not repeated here), and another The eighth variation of the steps is that the second desorption gas pipeline 43 is provided with a recirculation pipeline 44, and one end of the recirculation pipeline 44 is connected to the second desorption gas pipeline 43, and the recirculation pipeline The other end of the road 44 is connected to the second heating intake pipeline 51, so that the second desorbed carbon dioxide desorbed and concentrated gas transported by the second desorbed gas pipeline 43 can return to the recirculation pipeline 44. In the second heating intake pipeline 51, it is mixed with the outside air in the second heating intake pipeline 51 or the gas from other sources before entering the second heating device 50, or when the second heating intake pipeline is used alone The gas in path 51 is not mixed with outside air or gas from other sources. Wherein the recirculation pipeline 44 is provided with a valve 441 to control the gas flow direction of the recirculation pipeline 44 through the valve 441 .

In the ninth variation of another step of the present invention described above, the second desorption gas pipeline 43 has two kinds of deformations, wherein the first deformation is that the second desorption gas pipeline 43 is in the recirculation pipeline 44 A first fan 432 and a second fan 433 (as shown in FIG. 17 ) are respectively provided at the front end and the rear end of one end of the joint, and the recirculation pipeline 44 is matched to form a positive pressure pattern, so that the second fan The desorbed and concentrated carbon dioxide in the desorbed gas pipeline 43 can squeeze into the recirculation pipeline 44 and return to the second heating intake pipeline 51 . And the second modification is that the second desorption gas pipeline 43 is provided with a fan 431, and the second heating intake pipeline 51 is provided with a fan 511 (as shown in Figure 18), and the second heating intake pipeline 51 is provided with a fan 511. The fan 511 provided is located at the rear end of the connection between the recirculation pipeline 44 and the second heating intake pipeline 51, and is close to the second heating device 50, and cooperates with the second desorption gas pipeline 43. The blower 431 of the fan 431 is in a negative pressure mode, so that the gas desorbed and concentrated by the carbon dioxide desorbed for the second time in the second desorbed gas pipeline 43 can return to the second heating intake pipeline through the recirculation pipeline 44 within 51.

From the above detailed description, those skilled in the art can understand that the present invention can indeed achieve the above-mentioned purpose, and has complied with the provisions of the patent law. Therefore, an application for a patent for invention is filed.

The specific embodiments described above have further described the purpose, technical solutions and beneficial effects of the present invention in detail. It should be understood that the above descriptions are only specific embodiments of the present invention, and are not intended to limit the present invention. Within the spirit and principles of the present invention, any modifications, equivalent replacements, improvements, etc., shall be included in the protection scope of the present invention.

Claims (45)

1. A carbon dioxide adsorption runner treatment system, comprising: Pretreatment equipment, one side of the pretreatment equipment is connected to the gas inlet pipeline; The first carbon dioxide adsorption wheel, the first carbon dioxide adsorption wheel is provided with an adsorption area and a desorption area, and the first carbon dioxide adsorption wheel is connected to the pretreatment gas pipeline, the first clean gas discharge pipeline, and the first hot gas delivery pipe Road and the 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 adsorption zone of the first carbon dioxide adsorption wheel One end of the first clean gas discharge pipeline is connected to the other side of the adsorption area of the first carbon dioxide adsorption wheel, and one end of the first hot gas delivery pipeline is connected to the desorption area of the first carbon dioxide adsorption wheel. The other side of the zone 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 wheel; A first heating device, the first heating device is provided with a first heating intake pipeline, and the first heating device is connected to the other end of the first hot gas delivery pipeline of the first carbon dioxide adsorption wheel; The second carbon dioxide adsorption wheel, the second carbon dioxide adsorption wheel is provided with an adsorption area and a desorption area, and the second carbon dioxide adsorption wheel is connected to the second clean gas discharge pipeline, the second hot gas delivery pipeline and the second desorption Gas pipeline, one side of the adsorption area of the second carbon dioxide adsorption wheel is connected to the other end of the first desorption gas pipeline, one end of the second net gas discharge pipeline is connected to the second carbon dioxide adsorption wheel The other side of the adsorption zone is connected, one end of the second hot gas delivery pipeline is connected to the other side of the desorption zone of the second carbon dioxide adsorption wheel, 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; A second heating device, the second heating device is provided with a second heating intake pipeline, and the second heating device is connected to the other end of the second hot gas delivery pipeline of the second carbon dioxide adsorption wheel; and A chimney, the chimney is connected with the other end of the first net gas discharge pipeline of the first carbon dioxide adsorption wheel and the other end of the second net gas discharge pipeline of the second carbon dioxide adsorption wheel. 2. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the pretreatment gas pipeline is further provided with a fan. 3. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the first clean gas discharge pipeline is further provided with a fan. 4. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the second clean gas discharge pipeline is further provided with a fan. 5. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the first desorption gas pipeline is further provided with a fan. 6. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the second desorption gas pipeline is further provided with a fan. 7. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the first heated air intake pipeline is further provided with a fan. 8. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the second heated air intake pipeline is further provided with a fan. 9. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the pretreatment equipment is further any one of a cooler, a condenser, a dehumidifier, and a desuperheater. 10. The carbon dioxide adsorption wheel treatment system according to claim 1, wherein the second desorption gas pipeline is further provided with a recirculation pipeline, and one end of the recirculation pipeline is connected to the second desorption gas pipeline, The other end of the recirculation pipeline is connected to the second heating intake pipeline. 11. The carbon dioxide adsorption wheel treatment system according to claim 10, wherein the second desorbed gas pipeline is further provided with a first blower fan and a second fan respectively at the front end and the rear end of one end connection of the recirculation pipeline. Two fans. 12. The carbon dioxide adsorption wheel treatment system according to claim 10, wherein the second desorbed gas pipeline is further provided with a fan, and the second heating intake pipeline is further provided with a fan, and the second heating intake pipe The fan provided by the pipeline is located at the rear end of the connection between the recirculation pipeline and the second heating air intake pipeline, and is close to the second heating device. 13. The carbon dioxide adsorption rotary treatment system according to claim 1, wherein the first desorption gas pipeline is further provided with a cooling device. 14. The carbon dioxide adsorption rotor treatment system according to claim 1, wherein the other end of the second desorption gas pipeline of the second carbon dioxide adsorption rotor is further connected with a double-tower polymer tubular membrane device, the double The tower-type polymer tubular membrane equipment is equipped with a first tower-type polymer tubular membrane group and a second tower-type polymer tubular membrane group. The first tower-type polymer tubular membrane group is equipped with a first adsorption tower, The first intake pipeline, the first exhaust pipeline, the first regeneration pipeline and the first compressed gas pipeline, the second tower-type polymer tubular membrane group is provided with a second adsorption tower, a second intake pipeline, The second exhaust pipeline, the second regeneration pipeline and the second compressed gas pipeline. 15. The carbon dioxide adsorption runner treatment system according to claim 14, wherein the first exhaust pipeline of the first tower-type polymer tubular membrane group and the second row of the second tower-type polymer tubular membrane group The gas pipeline is further connected with the exhaust output pipeline. 16. The carbon dioxide adsorption rotor treatment system according to claim 14, wherein the first compressed gas line of the first tower-type polymer tubular membrane group and the second compression gas line of the second tower-type polymer tubular membrane group The gas pipeline is further connected with the compressed gas output pipeline. 17. The carbon dioxide adsorption wheel treatment system according to claim 14, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group is further provided with a first heater, and the second tower-type polymer tube The second regeneration pipeline of the type membrane group is further provided with a second heater. 18. The carbon dioxide adsorption runner treatment system according to claim 14, wherein the first gas inlet pipeline, the first exhaust pipeline, the first regeneration pipeline and the second A compressed gas pipeline is further provided with a valve, and the second gas inlet pipeline, the second exhaust pipeline, the second regeneration pipeline and the second compressed gas pipeline of the second tower-type polymer tubular membrane group are further Each has a valve. 19. The carbon dioxide adsorption runner treatment system according to claim 14, wherein in the first adsorption tower of the first tower-type polymer tubular membrane group and the second adsorption tower of the second tower-type polymer tubular membrane group The inside is further filled with a plurality of hollow tubular polymer tubular membrane adsorbents, and the hollow tubular polymer tubular membrane adsorbents are made of polymer and adsorbent. 20. The carbon dioxide adsorption runner treatment system according to claim 14, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group and the second regeneration pipe of the second tower-type polymer tubular membrane group The road is further connected with the heat pipeline. 21. The carbon dioxide adsorption wheel treatment system according to claim 20, wherein the thermal energy pipeline 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 heat exchanger either. 22. The carbon dioxide adsorption wheel processing system according to claim 20, wherein the thermal energy pipeline is further connected to a heat exchanger, and the heat exchanger is arranged on the first desorption gas pipeline of the first carbon dioxide adsorption wheel, The heat exchanger is provided with a cold side pipeline and a hot side pipeline, the thermal energy pipeline is connected with the cold side pipeline of the heat exchanger, and the first desorbed gas pipeline is connected with the hot side pipeline of the heat exchanger way to form a connection. 23. A carbon dioxide adsorption wheel treatment method, mainly used in the carbon dioxide adsorption wheel system, and equipped with pretreatment equipment, a first carbon dioxide adsorption wheel, a first heating device, a second carbon dioxide adsorption wheel, and a 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 to the pretreatment intake pipeline, the first clean gas discharge pipeline, the first hot gas delivery pipeline and the first Desorption gas pipeline, the second carbon dioxide adsorption wheel is provided with an adsorption area and a desorption area, and the second carbon dioxide adsorption wheel is connected to the second clean gas discharge pipeline, the second hot gas delivery pipeline and the second desorption gas Pipeline, the first heating device is provided with a first heating intake 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 main steps of the treatment method include : Gas input pretreatment equipment: the gas is sent to the pretreatment equipment through the gas inlet pipeline for processing; The first carbon dioxide adsorption wheel adsorption: the gas treated by the pretreatment equipment is output from the other end of the pretreatment gas pipeline to one side of the adsorption area of the first carbon dioxide adsorption wheel for carbon dioxide adsorption ; Discharge from the first carbon dioxide adsorption runner: output the gas after the carbon dioxide adsorption generated by the adsorption zone of the first carbon dioxide adsorption runner to the chimney from the other end of the first clean gas discharge pipeline; Transporting the first hot gas for desorption: transporting the high-temperature hot gas to the desorption zone of the first carbon dioxide adsorption wheel through the first hot gas delivery pipeline connected to the first heating device for desorption; Output the desorbed and concentrated gas of carbon dioxide: the desorbed carbon dioxide desorbed and concentrated gas that is desorbed once through the desorption zone of the first carbon dioxide adsorption runner is sent from the other end of the first desorbed gas pipeline to output; Adsorption by the second carbon dioxide adsorption wheel: transport the desorbed and concentrated carbon dioxide once desorbed in the first desorption gas pipeline to one side of the adsorption area of the second carbon dioxide adsorption wheel for re-adsorption; Discharge from the second carbon dioxide adsorption runner: output the gas after the carbon dioxide adsorption produced by the adsorption zone of the second carbon dioxide adsorption runner 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 wheel through the second hot gas delivery pipeline connected to the second heating device for desorption; and Output the desorbed and concentrated gas of carbon dioxide: the desorbed and concentrated gas of carbon dioxide generated through the desorption zone of the second carbon dioxide adsorption wheel is sent from the other end of the second desorbed gas pipeline output. 24. The carbon dioxide adsorption rotor treatment method according to claim 23, wherein the pretreatment gas pipeline is further provided with a fan. 25. The carbon dioxide adsorption rotary treatment method according to claim 23, wherein the first clean gas discharge pipeline is further provided with a fan. 26. The carbon dioxide adsorption rotary treatment method according to claim 23, wherein the second net gas discharge pipeline is further provided with a fan. 27. The carbon dioxide adsorption rotary treatment method according to claim 23, wherein the first desorption gas pipeline is further provided with a fan. 28. The carbon dioxide adsorption rotor treatment method according to claim 23, wherein the second desorption gas pipeline is further provided with a fan. 29. The carbon dioxide adsorption rotary treatment method according to claim 23, wherein the first heated intake pipeline is further provided with a fan. 30. The carbon dioxide adsorption rotary treatment method according to claim 23, wherein the second heated intake pipeline is further provided with a fan. 31. The carbon dioxide adsorption rotary wheel treatment method according to claim 23, wherein the pretreatment equipment is further any one of a cooler, a condenser, a dehumidifier, and a desuperheater. 32. The carbon dioxide adsorption rotor treatment method according to claim 23, wherein the second desorption gas pipeline is further provided with a recirculation pipeline, and one end of the recirculation pipeline is connected to the second desorption gas pipeline, The other end of the recirculation pipeline is connected to the second heating intake pipeline. 33. The carbon dioxide adsorption rotor treatment method according to claim 32, wherein the second desorbed gas pipeline is further provided with a first blower fan and a second fan respectively at the front end and the rear end of one end connection of the recirculation pipeline. Two fans. 34. The carbon dioxide adsorption rotor treatment method according to claim 32, wherein the second desorbed gas pipeline is further provided with a fan, and the second heating intake pipeline is further provided with a fan, and the second heating intake pipe The fan provided by the pipeline is located at the rear end of the connection between the recirculation pipeline and the second heating air intake pipeline, and is close to the second heating device. 35. The carbon dioxide adsorption rotor treatment method according to claim 23, wherein the first desorption gas pipeline is further provided with a cooling device. 36. The carbon dioxide adsorption rotor treatment method according to claim 23, further comprising the following steps after the step of exporting the gas after desorption and concentration of carbon dioxide: Delivery to twin-tower polymer tubular membrane equipment: The desorbed and concentrated carbon dioxide desorbed for the second time in the second desorption gas pipeline is transported to the twin-tower polymer tubular membrane equipment for processing. 37. The carbon dioxide adsorption runner treatment method according to claim 36, wherein the double-tower polymer tubular membrane equipment is provided with a first tower polymer tubular membrane group and a second tower polymer tubular membrane group , the first tower-type polymer tubular membrane group is provided with 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 The polymer tubular membrane group is provided with a second adsorption tower, a second inlet pipeline, a second exhaust pipeline, a second regeneration pipeline and a second compressed gas pipeline. 38. The carbon dioxide adsorption runner treatment method according to claim 37, wherein the first exhaust line of the first tower-type polymer tubular membrane group and the second row of the second tower-type polymer tubular membrane group The gas pipeline is further connected with the exhaust output pipeline. 39. The carbon dioxide adsorption rotor wheel treatment method according to claim 37, wherein the first compressed gas line of the first tower-type polymer tubular membrane group and the second compression of the second tower-type polymer tubular membrane group The gas pipeline is further connected with a compressed gas output pipeline. 40. The carbon dioxide adsorption rotary wheel treatment method according to claim 37, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group is further provided with a first heater, and the second tower-type polymer tube The second regeneration pipeline of the type membrane group is further provided with a second heater. 41. The carbon dioxide adsorption runner treatment method according to claim 37, wherein the first air intake pipeline, the first exhaust pipeline, the first regeneration pipeline and the second A compressed gas pipeline is further provided with a valve, and the second gas inlet pipeline, the second exhaust pipeline, the second regeneration pipeline and the second compressed gas pipeline of the second tower-type polymer tubular membrane group are further Each has a valve. 42. The carbon dioxide adsorption runner treatment method according to claim 37, wherein the first adsorption tower of the first tower-type polymer tubular membrane group and the second adsorption tower of the second tower-type polymer tubular membrane group The inside is further filled with a plurality of hollow tubular polymer tubular membrane adsorbents, and the hollow tubular polymer tubular membrane adsorbents are made of polymer and adsorbent. 43. The carbon dioxide adsorption runner treatment method according to claim 37, wherein the first regeneration pipeline of the first tower-type polymer tubular membrane group and the second regeneration pipe of the second tower-type polymer tubular membrane group The road is further connected with the heat pipeline. 44. The carbon dioxide adsorption wheel treatment method according to claim 43, wherein the thermal energy pipeline 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 heat exchanger. either. 45. The carbon dioxide adsorption rotor treatment method according to claim 43, wherein the thermal energy pipeline is further connected with a heat exchanger, and the heat exchanger is arranged on the first desorption gas pipeline of the first carbon dioxide adsorption rotor, The heat exchanger is provided with a cold side pipeline and a hot side pipeline, the thermal energy pipeline is connected with the cold side pipeline of the heat exchanger, and the first desorbed gas pipeline is connected with the hot side pipeline of the heat exchanger way to form a connection.

Images