Carbon dioxide concentration system for combustion tail gas

Abstract

The utility model provides a carbon dioxide concentration system for combustion tail gas, which mainly adopts the combined design of an incineration device, a cooling device, a first adsorption and desorption device, a second adsorption and desorption device, a chimney and at least one purification device, the incineration device exhausts the combustion tail gas, the combustion tail gas contains carbon dioxide gas, and the cooling device is used for cooling the combustion tail gas. The combustion tail gas is cooled by the cooling device and then is fed into the first adsorption and desorption device for adsorption and desorption of carbon dioxide gas, and the desorbed carbon dioxide gas is fed into the at least one second adsorption region for re-adsorption of the carbon dioxide gas by the at least one first desorption region; and the at least one second desorption area sends the re-desorbed carbon dioxide gas into the purification equipment for purification treatment, so that the desorbed carbon dioxide gas is subjected to a secondary concentration procedure, and the effects of purifying and recycling the carbon dioxide are achieved.

Description

Technical Field

[0001] The utility model relates to a carbon dioxide concentration system for combustion tail gas, and specifically to a system which has the function of performing a secondary concentration procedure on desorbed carbon dioxide gas to achieve the efficiency of carbon dioxide purification and recovery and reuse, and is suitable for petrochemical plant areas, oil storage plant areas, scientific and technological manufacturing plant areas and similar areas. Background Art

[0002] Taiwan's semiconductor cluster is complete, advanced technology is developing rapidly, and the demand for related electronic chemicals and gases is growing. Chemical plants are striving to enter the supply chain. As the electronics industry grows, the demand for industrial gases will also increase simultaneously. The main domestic industrial gas suppliers are Lianhua Gas, Sanfu Gas, and Yadong Gas.

[0003] In response to the trend of green economy, OUCC starts with ethylene. The by-product of the process of manufacturing ethylene oxide is carbon dioxide. After carbon capture, the carbon dioxide is reused to produce high-purity liquid carbon dioxide. This product can be used in beverage and food grades, and can also enter the supply chain of the electronics and semiconductor industries. Currently, more than 70% of the carbon dioxide comes from reuse.

[0004] However, the electronics or semiconductor industries are prone to produce volatile organic gases (VOCs) when manufacturing products. Volatile organic gases (VOCs) are hydrocarbons. In addition, the burners use auxiliary fuels such as natural gas for heating, which will also produce carbon dioxide after combustion and oxidation. Currently, most of them are directly discharged through chimneys.

[0005] Therefore, in view of the above-mentioned shortcomings, the applicant hopes to propose a carbon dioxide concentration system for combustion exhaust gas with the efficiency of carbon dioxide purification and recycling and reuse, which can be easily operated and assembled by users. The applicant has devoted himself to research and design to provide user convenience, which is the creative motivation for the applicant's research and development. Utility Model Content

[0006] In view of the above technical problems, the present invention provides a carbon dioxide concentration system for combustion exhaust gas, in order to at least partially solve the above technical problems. The specific technical solutions provided by the present invention are as follows.

[0007] The main purpose of the utility model is to provide a carbon dioxide concentration system for combustion exhaust gas, which is mainly designed by combining an incineration device, a cooling device, a first adsorption and desorption device, a second adsorption and desorption device, a chimney and at least one purification device. The incineration device discharges a combustion exhaust gas, which contains carbon dioxide gas, and the combustion exhaust gas is first cooled by the cooling device and then sent to the first adsorption and desorption device for adsorption and desorption of carbon dioxide gas. The at least one first desorption zone sends the desorbed carbon dioxide gas to the at least one second adsorption zone for re-adsorption of carbon dioxide gas, and the at least one second desorption zone sends the re-desorbed carbon dioxide gas to the purification device for purification treatment, so that the desorbed carbon dioxide gas can be subjected to a secondary concentration procedure to achieve the efficiency of carbon dioxide purification and recycling, thereby increasing the overall practicality.

[0008] Another object of the utility model is to provide a carbon dioxide concentration system for combustion tail gas, wherein the purification equipment has two embodiments, wherein the first embodiment is that the purification equipment is connected to a compression and liquefaction device, wherein the compression and liquefaction device compresses and liquefies the purified carbon dioxide gas into liquid purified carbon dioxide, and the compression and liquefaction device is connected to at least one purification storage device, so that the compressed and liquefied liquid purified carbon dioxide is stored through the at least one purification storage device, and then sent to a factory area through the at least one purification storage device for use by the factory area. The second embodiment is that the purification equipment is provided with a purification pipeline, and the purification pipeline is connected to a factory area, so that the purified carbon dioxide gas is transported to the factory area through the purification pipeline for use by the factory area. The plant area referred to above is any one of a semiconductor process plant area, an electronic process plant area, an optoelectronic process plant area, a chemical process plant area, a petrochemical process plant area, an electroplating process plant area, a food process plant area, a drying and cleaning process plant area, and a pharmaceutical process plant area. For subsequent applications, it can be used in a process area that requires carbon dioxide gas or as one of the product raw materials, so that the purified carbon dioxide has the efficiency of recovery and can achieve the value of reuse, thereby increasing the overall usability.

[0009] Another object of the present invention is to provide a carbon dioxide concentration system for combustion exhaust gas, through the incineration equipment and a double-rotor volatile organic gas (VOC) treatment system or a single-rotor volatile organic gas (VOC) treatment system. Any combination design, wherein the incineration equipment is any one of a direct-fired incinerator (TO), a catalytic incinerator, and a regenerative thermal incinerator (RTO), enables the incineration equipment to perform high-temperature oxidation on the desorbed concentrated gas desorbed by the zeolite rotor to oxidize volatile organic compounds into main components including carbon dioxide and water, and then discharge the combustion exhaust gas to capture and utilize carbon dioxide gas, having the efficiency of simultaneously treating volatile organic gas (VOC) and carbon dioxide gas, so as to achieve the purpose of environmental protection, energy saving and carbon reduction, thereby increasing the overall operability.

[0010] In order to further understand the characteristics, features and technical contents of the present invention, please refer to the following detailed description and drawings of the present invention, but the attached drawings are only provided for reference and illustration and are not intended to limit the present invention. BRIEF DESCRIPTION OF THE DRAWINGS

[0011] Figure 1 A schematic diagram of the first embodiment of the connection method of the purification device;

[0012] Figure 2 Another schematic diagram of the second embodiment of the connection method of the purification device;

[0013] Figure 3 Design a schematic diagram for the first method of purification equipment;

[0014] Figure 4 Design a schematic diagram for the second method of purification equipment;

[0015] Figure 5 Design a schematic diagram for the third method of purification equipment;

[0016] Figure 6 A schematic diagram of the main system architecture of the first adsorption-desorption device and the second adsorption-desorption device using adsorption materials;

[0017] Figure 7 It is a schematic diagram of another system architecture in which the first adsorption-desorption device and the second adsorption-desorption device use adsorption materials.

[0018] Explanation of symbols:

[0019] 1. Double-rotor volatile organic gas (VOC) treatment system;

[0020] 10. Incineration equipment; 101. Direct-fired incinerator (TO);

[0021] 11. Exhaust gas delivery pipeline; 111. Cooling device; 112. Fan; 113. Dust removal device;

[0022] 20. first adsorption and desorption device; 201. adsorption material; 202. rotating wheel;

[0023] 21. at least one first adsorption zone;

[0024] 22. at least one first desorption zone;

[0025] 23. At least one first exhaust pipeline; 231. Fan;

[0026] 24. at least one first hot gas pipeline;

[0027] 25. At least one first desorption gas pipeline;

[0028] 26. Heater;

[0029] 30. Second adsorption and desorption device; 301. Adsorption material; 302. Rotating wheel;

[0030] 31. at least one second adsorption zone;

[0031] 32. at least one second desorption zone;

[0032] 33. at least one second exhaust pipeline; 331. fan;

[0033] 34. at least one second hot gas line;

[0034] 35. at least one second desorption gas pipeline;

[0035] 36. Heater;

[0036] 40. Chimney;

[0037] 50. Purification equipment; 504. Purification pipeline;

[0038] 51. Compression liquefaction device;

[0039] 52. Purification and storage equipment;

[0040] 53. Factory area;

[0041] 5011, raw material tank; 5012, purification tower; 50121, packed bed; 5013, heater; 5014, cooling facility; 5021, raw material tank; 5022, membrane contactor; 50221, membrane; 5023, heater; 5031, raw material tank; 5032, adsorption and desorption bed module; 5033, vacuum pump;

[0042] 60. first adsorption rotor; 601. adsorption zone; 602. cooling zone; 603. desorption zone;

[0043] 61. Exhaust gas intake pipeline; 611. Exhaust gas connecting pipeline; 6111. Exhaust gas connecting control valve;

[0044] 62. First clean gas discharge pipeline; 621. First clean gas communication pipeline; 6211. First clean gas communication control valve;

[0045] 63. First cooling air intake pipeline;

[0046] 64. A first cooling gas delivery pipeline;

[0047] 65. A first hot gas delivery pipeline;

[0048] 66. First desorption concentrated gas pipeline; 661. Fan;

[0049] 70, second adsorption rotor; 701, adsorption zone; 702, cooling zone; 703, desorption zone;

[0050] 72. Second clean air discharge pipeline; 721. Fan;

[0051] 73. Second cooling air intake pipeline;

[0052] 74. Second cooling gas delivery pipeline;

[0053] 75. Second hot gas delivery pipeline;

[0054] 76. Second desorption concentrated gas pipeline; 761. Fan;

[0055] 81. first heat exchanger; 811. first cold side pipeline; 812. first hot side pipeline;

[0056] 82. Second heat exchanger; 821. Second cold side pipeline; 822. Second hot side pipeline;

[0057] 83. a third heat exchanger; 831. a third cold side pipeline; 832. a third hot side pipeline;

[0058] 84, fourth heat exchanger; 841, fourth cold side pipeline; 842, fourth hot side pipeline;

[0059] 85. First cold side delivery pipeline;

[0060] 86. Fourth cold side delivery pipeline; DETAILED DESCRIPTION

[0061] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with specific embodiments and with reference to the accompanying drawings.

[0062] See also Figure 1-Figure 7, which is a schematic diagram of an embodiment of the utility model. The best implementation of the combustion tail gas carbon dioxide concentration system of the utility model is to be used in petrochemical plants, oil storage plants, scientific and technological manufacturing plants or similar areas, mainly having the function of performing a secondary concentration process on the desorbed carbon dioxide gas to achieve the efficiency of carbon dioxide purification and recycling.

[0063] The carbon dioxide enrichment system of combustion tail gas of the utility model mainly comprises a combination design of an incineration device 10, a cooling device 111, a first adsorption and desorption device 20, a second adsorption and desorption device 30, a chimney 40 and at least one purification device 50 (such as Figure 1 and Figure 2 As shown, the incineration equipment 10 discharges a combustion tail gas, and the combustion tail gas contains carbon dioxide gas. The incineration equipment 10 is provided with a tail gas delivery pipeline 11 to deliver the combustion tail gas. In addition, the incineration equipment 10 is any one of a direct-fired incinerator (TO) 101, a catalytic incinerator (not shown), and a regenerative thermal incinerator (RTO) (not shown). When the incineration equipment 10 is a direct-fired incinerator (TO) 101, the direct-fired incinerator (TO) 101 is provided with any one of two heat exchangers, three heat exchangers, and four heat exchangers. The incineration equipment 10 is designed in combination with any one of a double-rotor volatile organic gas (VOC) treatment system 1 or a single-rotor volatile organic gas (VOC) treatment system (not shown). Since volatile organic gas (VOC) is a hydrocarbon, carbon dioxide gas will be generated after combustion. In order to heat up the direct-fired incinerator (TO) 101, fuel is required. If the fuel is a fossil fuel, such as natural gas, it contains hydrocarbons, which will produce carbon dioxide gas after combustion. Therefore, the incineration equipment 10 can oxidize the volatile organic gas (VOC) desorbed by the zeolite wheel at a generally designed high temperature of about 732°C to oxidize the volatile organic compounds into main components including carbon dioxide and water, and then discharge the combustion exhaust gas to capture and utilize the carbon dioxide gas in the exhaust gas after combustion. It has the efficiency of simultaneously processing volatile organic gas (VOC) and carbon dioxide gas to achieve the purpose of environmental protection, energy saving and carbon reduction.

[0064] The combustion exhaust gas is transported to the first adsorption and desorption device 20 via the exhaust gas transport pipeline 11 to adsorb and desorb carbon dioxide gas. When transported to the first adsorption and desorption device 20, the exhaust gas transport pipeline 11 is provided with a cooling device 111 (such as Figure 1 and Figure 2As shown), the cooling device 111 is any one of a cooler, a condenser, a dehumidifier, a cooler, a cooling water tower, and a refrigerant compressor. When the cooling device 111 is a cooler, the cooler is any one of a shell and tube cooler, a fin tube cooler, and a plate heat exchanger cooler. The cooling device 111 cools the combustion exhaust gas. Since the combustion exhaust gas has a high temperature of about 200°C, it needs to be cooled first and then sent to the first adsorption and desorption device 20 for subsequent carbon dioxide gas adsorption and desorption. The exhaust gas delivery pipeline 11 is provided with a fan 112 (such as Figure 2 As shown), so that the combustion exhaust gas can be pushed and pulled into the first adsorption and desorption device 20.

[0065] Furthermore, for example, in a wafer manufacturing plant, organic compounds sometimes contain silicon as a component element, which generates silicon dioxide particles after combustion and oxidation. In addition to the cooling device 111, the exhaust gas delivery pipeline 11 may also be equipped with a dust removal device 113 (such as Figure 2 As shown), and the dust or oxides such as silicon dioxide (SiO2) contained in the combustion exhaust gas are removed and filtered through the dust removal device 113. The dust removal device 113 is any one of a bag dust collector, a pulse bag dust collector, an electric bag composite dust collector, a negative pressure back-blowing filter bag dust collector, a low-pressure long bag pulse dust collector, a cartridge pulse dust collector, a pulse filter element dust collector, a pulse jet bag dust collector, an inertial dust collector, an electrostatic dust collector, a horizontal electrostatic dust collector, a centrifugal dust collector, a cyclone separator, a multi-cyclone dust collector, a wet dust collector, a wet electrostatic dust collector, a charged water mist dust collector, a water film dust collector, a venturi tube dust collector, and a multi-layer dust collector. In addition, in addition to being equipped with a dust removal device 113, the exhaust gas conveying pipeline 11 can also be provided with a filter device (not shown), and the dust or oxides such as silicon dioxide (SiO2) contained in the combustion exhaust gas can be removed and filtered by the filter device for dust removal, wherein the filter device is any one of a non-woven filter and a fine mesh.

[0066] The first adsorption and desorption device 20 and the second adsorption and desorption device 30 have two embodiments. The first embodiment is that the first adsorption and desorption device 20 and the second adsorption and desorption device 30 are respectively provided with at least one adsorption material 201, 301 (such as Figure 6 and Figure 7As shown, the at least one adsorbent material 201, 301 is filled with multiple tubular hollow fiber tubular membrane adsorbent materials, and the filling rate is 65% to 95%, mainly to increase its adsorption area. The tubular hollow fiber tubular membrane is made of micron-grade powdered adsorbent material and polymer materials, and the adsorbent material contained therein is any one or a combination of zeolite (such as X-type zeolite (such as 13X)), anion exchange resin, and metal organic framework (Metal Organic Frameworks: MOF) materials. The above-mentioned tubular hollow fiber tubular membrane adsorbent material includes at least one channel and at least one adsorption layer (not shown in the figure), and the at least one adsorption layer surrounds the at least one channel, wherein the adsorption layer is adjacent to the channel, and multiple channels can also be arranged between the adsorption layers. The number of the channels and the number of adsorption layers are not limited to the present invention, and the gas is allowed to pass through the channel along the inside of the channel through the at least one channel, but does not penetrate the channel, wherein the inner diameter of the at least one channel is any one between 0.3 mm and 1.5 mm, so as to be designed to suit different applications. The diameter of the tubular hollow fiber tubular membrane adsorbent is D1, and the opening diameter of the at least one channel is d1, which satisfies the condition of 1<D1 / d1<99, and the tubular hollow fiber tubular membrane adsorbent can be arranged into any of a rectangular body (not shown), a fan-shaped body (not shown), and a cylinder, and is combined through the above-mentioned shapes to minimize the gaps between the tubular hollow fiber tubular membrane adsorbent combinations, wherein the porosity of the tubular hollow fiber tubular membrane adsorbent is 20%-80%. The so-called porosity is the ratio of the volume of the pores in the hollow part to the total volume of the material, and gas or liquid can enter only through the pores. The specific surface area of ​​the tubular hollow fiber tubular membrane adsorbent is greater than 500 square meters / cubic meter (m 2 / m 3 ), wherein the specific surface area refers to the surface area per unit volume of a porous solid substance, and the so-called surface area refers to the internal surface area, so as to have a better adsorption effect.

[0067] Furthermore, the material of the tubular hollow fiber tubular membrane adsorbent material at least includes an amine-modified anion exchange resin material and a polymer material (not shown), and is mainly made of the amine-modified anion exchange resin material and the polymer material, wherein the polymer material is at least one of the group consisting of polysulfone, polyethersulfone, polyvinylidene fluoride, polyphenylsulfone, polyacrylonitrile, cellulose acetate, cellulose diacetate, polyimide, polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic acid-glycolic acid, polycaprolactone, polyvinyl hydropyrrolidone, ethylene-vinyl alcohol, polydimethylsiloxane, polytetrafluoroethylene and cellulose acetate. The amine-modified anion exchange resin is for mutual exchange with negatively charged ions. According to the reversible equilibrium principle of ion exchange reaction, the combined exchange ion is hydroxyl (OH - ) or carbonate (CO3 2- ) can be used to restore the resin to its original state by using the replacement reaction of the ion exchange resin. The amine-modified anion exchange resin material is an anion exchange resin modified by any one of primary amine (-NH2), secondary amine (-NHR), tertiary amine (-NR2), quaternary ammonium salt (-NR3OH) or a combination thereof. The so-called modification is to change the properties of the material, and improve the performance through physical processes such as heating, cooling, ion bombardment and injection, as well as chemical treatment. The so-called amine group (-NH2) is the functional group of amine, and amine can also be divided into primary amine (-NH2), secondary amine (-NHR), tertiary amine (-NR2), quaternary ammonium salt (-NR3OH), etc. according to the number of hydrogen atoms replaced on the nitrogen molecule. Among them, the primary amine (-NH2), secondary amine (-NHR) and tertiary amine (-NR2) are weakly alkaline functional groups, which can dissociate OH in water - The positively charged groups of this resin can adsorb and combine with anions in the solution, thereby producing anion exchange. The quaternary ammonium salt (-NR3OH) is a strong alkaline functional group, which can dissociate into OH in water. - The positively charged groups of this resin can adsorb and combine with the anions in the solution, thus producing anion exchange.

[0068] The tubular hollow fiber tubular membrane adsorbent used in the present invention is not only provided with the polymer material mentioned above, but also with at least one adsorbent (not shown), such as zeolite powder, resin, activated carbon, etc. The adsorbent is in powder form, in micron size, and has an average particle size of 1 to 99 microns, where 1 micron is equal to 1*10 -6Meters. The membrane body of the tubular hollow fiber tubular membrane adsorbent is made by a dry-wet spinning phase transfer process. The membrane body structure of the tubular hollow fiber tubular membrane adsorbent is similar to a sponge or foam structure, with interconnected micron-sized small and medium-sized pores, and gas molecules can move and diffuse between the micron-sized small and medium-sized pores, wherein the gas molecules are sub-nanometer or angstrom (Ångström, abbreviated as angstrom, symbol Å) molecular size. In addition, the content of polymer materials is less than that of adsorbents, and the polymer materials account for 5wt%~55wt%, and the adsorbents (such as zeolites) account for 95wt%~45wt%. Generally speaking, the polymer materials account for 10wt%~30wt% in a better ratio. The tubular hollow fiber tubular membrane adsorbent used in the utility model is mainly used to separate or purify a mixed gas containing two or more gases through the principle of adsorption. The principle is that the source feed gas flows through the surface of the membrane body of the tubular hollow fiber tubular membrane adsorbent and is output as concentrated gas. Through the diffusion of the source feed gas flowing through the surface of the membrane body of the tubular hollow fiber tubular membrane adsorbent, one or more gases are easily adsorbed by the adsorbent contained in the membrane body of the tubular hollow fiber tubular membrane adsorbent, while other gas components are less likely to be adsorbed. Therefore, part of the gas that is more easily adsorbed will be adsorbed on the adsorbent in the membrane body of the tubular hollow fiber tubular membrane adsorbent to achieve the effect of separation or purification. The factors of adsorption of the source feed gas include the micropore size of the adsorbent, the size of the gas molecule, the van der Waals force, the polarity, the hydrophilicity or hydrophobicity of the adsorbent, etc. The flow rate of the source feed gas passing through the membrane surface of the tubular hollow fiber tubular membrane adsorbent material is usually controlled at 0.01m / s~1m / s. Sometimes, when the processing efficiency requirement is lower or the purification separation requirement is lower, it can be adjusted to a maximum of 2.5m / s.

[0069] The second embodiment of the first adsorption and desorption device 20 and the second adsorption and desorption device 30 is that each of them is provided with at least one rotating wheel 202, 302 (such as Figure 1 and Figure 2 As shown in FIG. 1 ), the rotor 202, 302 is any one of a turret type, a horizontal type, and a cylindrical type, and the rotor 202, 302 is filled with any one of activated carbon, zeolite, silica gel, activated alumina, molecular sieve, manganese oxide, calcium hydroxide, graphene, and hollow fiber. In addition, the first adsorption and desorption device 20 of the utility model has at least one first adsorption area 21 and at least one first desorption area 22. When the first adsorption and desorption device 20 is at least one adsorption material 201 (such as Figure 6 and Figure 7As shown), the at least one adsorbent material 201 is filled with a plurality of tubular hollow fiber tubular membrane adsorbent materials, and the tubular hollow fiber tubular membrane adsorbent material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material. The at least one adsorbent material 201 can be set as two adsorbent materials 201. Taking two adsorbent materials 201 as an example, one adsorbent material 201 is at least one first adsorption zone 21, and the other adsorbent material is at least one first desorption zone 22. After a period of time, one adsorbent material 201 is converted into at least one first desorption zone 22, and the other adsorbent material 201 is converted into at least one first adsorption zone 21 to facilitate adsorption and desorption. When the first adsorption and desorption device 20 is at least one rotor 202 having the second embodiment (as shown in FIG. 1 ), the at least one adsorbent material 201 is filled with a plurality of tubular hollow fiber tubular membrane adsorbent materials, and the tubular hollow fiber tubular membrane adsorbent material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material. The at least one adsorbent material 201 can be set as two adsorbent materials 201. Taking two adsorbent materials 201 as an example, one adsorbent material 201 is at least one first adsorption zone 21, and the other adsorbent material 201 is at least one first desorption zone 22, and the other adsorbent material 201 is converted into at least one first adsorption zone 21 to facilitate adsorption and desorption. Figure 1 and Figure 2 As shown in FIG. 2 , the rotating wheel 202 is divided into at least one first adsorption zone 21 and at least one first desorption zone 22. After a period of time, the rotating wheel 202 rotates to rotate at least one first adsorption zone 21 into at least one first desorption zone 22, and at least one first desorption zone 22 into at least one first adsorption zone 21, so as to facilitate adsorption and desorption. The second adsorption and desorption device 30 of the utility model has at least one second adsorption zone 31 and at least one second desorption zone 32. When the second adsorption and desorption device 30 is at least one adsorption material 301 of the first embodiment (as shown in FIG. 2 ), the rotating wheel 202 is divided into at least one first adsorption zone 21 and at least one first desorption zone 22. Figure 6 and Figure 7 As shown), the at least one adsorbent material 301 is filled with a plurality of tubular hollow fiber tubular membrane adsorbent materials, and the tubular hollow fiber tubular membrane adsorbent material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material. The at least one adsorbent material 301 can be set as two adsorbent materials 301. Taking two adsorbent materials 301 as an example, one adsorbent material 301 is at least one second adsorption zone 31, and the other adsorbent material 301 is at least one second desorption zone 32. After a period of time, one adsorbent material 301 is converted into at least one second desorption zone 32, and the other adsorbent material 301 is converted into at least one second adsorption zone 31 to facilitate adsorption and desorption. When the second adsorption and desorption device 30 is at least one rotor 302 having a second embodiment (such as Figure 1 and Figure 2 As shown in the figure, the rotating wheel 302 is divided into at least one second adsorption zone 31 and at least one second desorption zone 32. After a period of time, the rotating wheel 302 rotates, so that the at least one second adsorption zone 31 rotates into at least one second desorption zone 32, and the at least one second desorption zone 32 rotates into at least one second adsorption zone 31, so as to facilitate adsorption and desorption.

[0070] The first adsorption and desorption device 20 of the present invention is provided with at least one first exhaust pipeline 23, at least one first hot gas pipeline 24, and at least one first desorption gas pipeline 25, wherein the at least one first adsorption zone 21 is connected to the tail gas delivery pipeline 11 of the incineration equipment 10 (such as Figure 1 , Figure 2, Figure 6 and Figure 7 As shown), the combustion exhaust gas of the exhaust gas delivery pipeline 11 is sent to the at least one first adsorption zone 21 for carbon dioxide gas adsorption, and the at least one first adsorption zone 21 is connected to the at least one first exhaust pipeline 23, so that the adsorbed gas generated by the at least one first adsorption zone 21 is discharged through the at least one first exhaust pipeline 23, and the at least one first exhaust pipeline 23 is connected to the chimney 40, and the at least one first exhaust pipeline 23 is provided with a fan 231 (as shown Figure 2 and Figure 7 As shown), so that the adsorbed gas is pushed and pulled into the chimney 40 through the at least one first exhaust pipe 23 for discharge. In addition, the at least one first desorption zone 22 is connected to the at least one first hot gas pipe 24, so that at least one heat source is transported to the at least one first desorption zone 22 through the at least one first hot gas pipe 24, wherein the at least one first hot gas pipe 24 has two implementation modes, the first implementation mode is that the at least one first hot gas pipe 24 is connected to a heat exchanger (not shown), and the heat exchanger is any one of a fin-tube heat exchanger, a shell-and-tube heat exchanger, a plate heat exchanger, a gas-to-gas heat exchanger, and a liquid-to-gas heat exchanger, and the second implementation mode is that the at least one first hot gas pipe 24 is connected to a heater 26 (as shown). Figure 1 , Figure 2 , Figure 6 and Figure 7 As shown in the figure), the heater 26 is any one of an electric heater, a gas heater, a thermal oil heater, and a hot water heater, so that the at least one first hot gas pipeline 24 can transport at least one heat source to the at least one first desorption zone 22 for desorption through a heat exchanger (not shown) or the heater 26, and the at least one first desorption zone 22 is connected to the at least one first desorption gas pipeline 25 to output the carbon dioxide gas after desorption in the at least one first desorption zone 22 through the at least one first desorption gas pipeline 25.

[0071] The second adsorption and desorption device 30 of the present invention is provided with at least one second exhaust pipeline 33, at least one second hot gas pipeline 34, and at least one second desorption gas pipeline 35, wherein the at least one second adsorption zone 31 is connected to the at least one first desorption gas pipeline 25 (such as Figure 1 , Figure 2 , Figure 6 and Figure 7As shown), the desorbed carbon dioxide gas generated in the at least one first desorption zone 22 is sent to the at least one second adsorption zone 31 for re-adsorption of carbon dioxide gas, and the at least one second adsorption zone 31 is connected to the at least one second exhaust pipeline 33, so that the re-adsorbed gas generated in the at least one second adsorption zone 31 is discharged through the at least one second exhaust pipeline 33, and the at least one second exhaust pipeline 33 is connected to the chimney 40, and the at least one second exhaust pipeline 33 is provided with a fan 331 (as shown in FIG. Figure 2 and Figure 7 As shown), so that the re-adsorbed gas is pushed and pulled into the chimney 40 through the at least one second exhaust pipe 33 for discharge. In addition, the at least one second desorption zone 32 is connected to the at least one second hot gas pipe 34, so that at least one heat source is transported to the at least one second desorption zone 32 through the at least one second hot gas pipe 34, wherein the at least one second hot gas pipe 34 has two implementation modes, the first implementation mode is that the at least one second hot gas pipe 34 is connected to a heat exchanger (not shown), and the heat exchanger is any one of a fin-tube heat exchanger, a shell-and-tube heat exchanger, a plate heat exchanger, a gas-to-gas heat exchanger, and a liquid-to-gas heat exchanger, and the second implementation mode is that the at least one second hot gas pipe 34 is connected to a heater 36 (as shown). Figure 1 , Figure 2 , Figure 6 and Figure 7 As shown), the heater 36 is any one of an electric heater, a gas heater, a thermal oil heater, and a hot water heater, so that the at least one second hot gas pipeline 34 can transport at least one heat source to the at least one second desorption zone 32 for desorption through a heat exchanger (not shown) or the heater 36, and the at least one second desorption zone 32 is connected to the at least one second desorption gas pipeline 35 so that the carbon dioxide gas after re-desorption in the at least one second desorption zone 32 is output through the at least one second desorption gas pipeline 35.

[0072] The at least one second desorption gas pipeline 35 is connected to the purification device 50 (such as Figure 1 , Figure 2 , Figure 6 and Figure 7 As shown in FIG. 1 ), the desorbed carbon dioxide gas produced in the at least one second desorption zone 32 is sent to the purification device 50 for purification treatment, so that the desorbed carbon dioxide gas is subjected to a secondary concentration process to achieve the efficiency of carbon dioxide purification and recycling. The connection method of the purification device 50 has two implementation methods, wherein the first implementation method is that the purification device 50 is connected to a compression liquefaction device 51 (as shown in FIG. Figure 1 and Figure 6As shown in the figure, the compression liquefaction device 51 compresses and liquefies the purified carbon dioxide gas into liquid purified carbon dioxide. Carbon dioxide is one of the gases that is easier to liquefy. The liquefaction temperature is 15°C and the pressure is about 14.7Pa. When the carbon dioxide pressure is higher than 7.4MPa and the temperature is higher than 31°C, carbon dioxide will turn into a supercritical fluid. Its physical properties are between the gas and liquid phases. It also has the characteristics of gas and liquid, low viscosity, and almost no surface tension. In addition, the compression liquefaction device 51 is provided with a compressor (not shown in the figure), wherein the compressor can be divided into two types: one that changes the gas volume and one that changes the gas speed. The compressor that changes the gas volume first introduces the gas into a closed space, and then increases the gas pressure by compressing the gas volume. The compressor that changes the gas speed allows the gas to flow at a high speed through the rotation of the impeller, and then passes through the outer boost ring. Later, due to the increase in the cross-sectional area of ​​the boost ring, the gas flow rate gradually decreases, so that the gas energy is converted from kinetic energy to pressure energy, and the pressure increases.

[0073] The compressor has a cooling pipeline (not shown) for a liquid or a gas to enter. The liquid is any one of water, ice water, and refrigerant. The gas is any one of air and cold air. The compression liquefaction device 51 is connected to at least one purification storage device 52 (such as Figure 1 and Figure 6 As shown in FIG. 1 ), the compressed liquefied carbon dioxide is stored in the at least one purified storage device 52. The at least one purified storage device 52 is any one of a tank truck, a steel cylinder, a barrel tank, a storage tank, and a container, which can facilitate the handling or transportation of the liquid purified carbon dioxide. The at least one purified storage device 52 is sent to a factory area 53 (such as Figure 1 Figure 6 As shown), the purified liquid purified carbon dioxide is sent to the plant 53 for use, wherein the plant 53 is any one of a semiconductor process plant, an electronic process plant, an optoelectronic process plant, a chemical process plant, a petrochemical process plant, an electroplating process plant, a food process plant, a dry cleaning process plant, and a pharmaceutical process plant. For example, the purified carbon dioxide is sent back to the semiconductor process plant for use as a laser light source in deep extreme ultraviolet lithography, or is sent back to the semiconductor process plant for cleaning processes, static electricity removal, and the like.

[0074] The second embodiment is that the purification device 50 is provided with a purification pipeline 504 (such as Figure 2 and Figure 7As shown in the figure, the purification pipeline 504 is connected to a factory area 53 to transport the purified carbon dioxide gas to the factory area 53 through the purification pipeline 504, wherein the factory area 53 is any one of a semiconductor process plant, an electronic process plant, an optoelectronic process plant, a chemical process plant, a petrochemical process plant, an electroplating process plant, a food process plant, a drying and cleaning process plant, and a pharmaceutical process plant, for example: sending it back to the semiconductor process plant for use as a laser light source in deep extreme ultraviolet lithography, or sending it back to the semiconductor process plant for cleaning process, static electricity removal, etc.

[0075] The purification device 50 described above has three design modes, the first design mode (such as Figure 3 ) is a purification device 50 provided with a raw material tank 5011, a purification tower 5012, a heater 5013 and a cooling facility 5014, the raw material tank 5011 is connected to the purification tower 5012, the heater 5013 is connected to the purification tower 5012, the cooling facility 5014 is connected to the purification tower 5012, the at least one second desorption gas pipeline 35 of the second adsorption and desorption device 30 is connected to the raw material tank 5011 of the purification device 50, and the raw material tank 5011 receives the gas supplied by the at least one second desorption gas pipeline 35. The desorbed carbon dioxide gas is sent to the purification tower 5012 for convection heat exchange with the hot gas sent by the heater 5013, wherein the heater 5013 is any one of an electric heater, a gas heater, a thermal oil heater, and a hot water heater, so that the desorbed carbon dioxide gas undergoes convection heat exchange to evaporate and rise the lower boiling point substances, and the higher boiling point substances sink in liquid form, and the evaporated and rising lower boiling point substances are cooled into high-concentration liquid carbon dioxide by the cooling facility 5014. The cooling facility 5014 is any one of a cooler, a condenser, a dehumidifier, a cooler, a cooling water tower, and a refrigerant compressor for filtering and purification. In addition, the purification tower 5012 is provided with at least one packed bed 50121, and the packed bed 50121 is made of any one of a Dixon packing, a McMahon packing, and a double-layer wire mesh corrugated (Sulyer) packing, so that the desorbed carbon dioxide gas enters the top of the purification tower 5012 and passes through the packed bed 50121 to perform convection heat exchange with a hot gas previously generated by the heater 5013.

[0076] The second design of the purification device 50 (eg Figure 4As shown in FIG. 1 , the purification device 50 is provided with a raw material tank 5021, a film contactor 5022 and a heater 5023, wherein the raw material tank 5021 is connected to the film contactor 5022, wherein the film contactor 5022 is provided with at least one film 50221, and the at least one film 50221 is any one of a hollow fiber tubular membrane, a nanoporous carbon membrane, a polyetheretherketone membrane, a polyimide membrane, a monoethanolamine membrane, a rubber-like polymer membrane, and a polyimide hollow fiber membrane, and the heater 5023 is connected to The membrane contactor 5022, wherein the heater 5023 is any one of an electric heater, a gas heater, a thermal oil heater, and a hot water heater. The raw material tank 5021 receives the desorbed carbon dioxide gas transported by the at least one second desorption gas pipeline 35, and transports the desorbed carbon dioxide gas to the membrane contactor 5022 for convection heat exchange with the hot gas transported by the heater 5023, so that the desorbed carbon dioxide gas can form a high concentration of gaseous carbon dioxide for filtration and purification.

[0077] Furthermore, the third design of the purification device 50 (eg Figure 5 As shown in the figure, the purification device 50 is provided with a raw material tank 5031, at least one adsorption-desorption bed module 5032 and a vacuum pump 5033, wherein the raw material tank 5031 is connected to the at least one adsorption-desorption bed module 5032, and the vacuum pump 5033 is connected to the at least one adsorption-desorption bed module 5032, wherein the adsorption-desorption bed module 5032 is filled with a plurality of tubular hollow fiber tubular membrane adsorbent materials, wherein the tubular hollow fiber tubular membrane adsorbent material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material, wherein the tubular hollow fiber tubular membrane adsorbent material comprises at least one pore and at least one adsorption layer (not shown), wherein the adsorption layer comprises an amine-modified anion exchange resin The material and a polymer material (please refer to the content of the tubular hollow fiber tubular membrane adsorption material in the previous paragraph), the raw material tank 5031 receives the desorbed carbon dioxide gas transported by the at least one second desorption gas pipeline 35, and transports the desorbed carbon dioxide gas to the at least one adsorption and desorption bed module 5032 for pressurized adsorption or reduced pressure desorption, wherein the at least one adsorption and desorption bed module 5032 adopts a combined structure of an absorption tower and a desorption tower, the desorbed carbon dioxide gas enters the absorption tower of the at least one adsorption and desorption bed module 5032, and forms a convection contact with the ethanolamine (MEA) solution entering from the top, so as to carry out the adsorption process of the desorbed carbon dioxide gas. The saturated solution after adsorption is input into the desorption tower of the at least one adsorption-desorption bed module 5032 for heating to evaporate the carbon dioxide gas, thereby separating the carbon dioxide gas from the ethanolamine (MEA) solution for desorption. During the reduced pressure desorption, the vacuum pump 5033 is used to evacuate the high-concentration gaseous carbon dioxide (performing a heated vacuum desorption (TVSA) procedure) for filtration and purification.

[0078] Furthermore, the utility model describes in the preceding paragraph any combination design of the incineration equipment 10 and a double-rotor volatile organic gas (VOC) treatment system 1 or a single-rotor volatile organic gas (VOC) treatment system (not shown). When the incineration equipment 10 is combined with a double-rotor volatile organic gas (VOC) treatment system 1, the incineration equipment 10 is a direct-fired incinerator (TO) 101, and the double-rotor volatile organic gas (VOC) treatment system 1 is provided with a first heat exchanger 81, a second heat exchanger 82, a third heat exchanger 83, a fourth heat exchanger 84, a first cold side delivery pipeline 85, a fourth cold side delivery pipeline 85, a first adsorption rotor 60, a second adsorption rotor 70 and a chimney 40 (such as Figure 1 and Figure 2 As shown in the figure), the first heat exchanger 81 is provided with a first cold side pipeline 811 and a first hot side pipeline 812, the second heat exchanger 82 is provided with a second cold side pipeline 821 and a second hot side pipeline 822, the third heat exchanger 83 is provided with a third cold side pipeline 831 and a third hot side pipeline 832, and the fourth heat exchanger 84 is provided with a fourth cold side pipeline 841 and a fourth hot side pipeline 842. The direct-fired incinerator (TO) 101 is provided with a burner head and a furnace (not shown in the figure), the burner head is communicated with the furnace, the first heat exchanger 81, the second heat exchanger 82, the third heat exchanger 83 and the fourth heat exchanger 84 are respectively arranged in the furnace of the direct-fired incinerator (TO) 101, and the direct-fired incinerator (TO) 101 is provided with an inlet and an outlet, the inlet is provided at the burner head, and the inlet is connected to the other end of the fourth cold side pipeline 841 of the fourth heat exchanger 84.

[0079] The burner head of the above-mentioned direct-fired incinerator (TO) 101 can first transport the incinerated high-temperature gas to one side of the first hot side pipeline 812 of the first heat exchanger 81 for heat exchange, and then transport the incinerated high-temperature gas to one side of the second hot side pipeline 822 of the second heat exchanger 82 for heat exchange from the other side of the first hot side pipeline 812 of the first heat exchanger 81, and then transport the incinerated high-temperature gas to one side of the third hot side pipeline 832 of the third heat exchanger 83 for heat exchange from the other side of the second hot side pipeline 822 of the second heat exchanger 82, and then transport the incinerated high-temperature gas to one side of the fourth hot side pipeline 842 of the fourth heat exchanger 84 from the other side of the third hot side pipeline 832 of the third heat exchanger 83 for heat exchange, and finally transport it to the outlet of the furnace from the other side of the fourth hot side pipeline 842 of the fourth heat exchanger 84.

[0080] The first adsorption rotor 60 of the present invention is provided with an adsorption zone 601, a cooling zone 602 and a desorption zone 603. The first adsorption rotor 60 is connected with an exhaust gas intake pipeline 61, a first clean gas exhaust pipeline 62, a first cooling gas intake pipeline 63, a first cooling gas delivery pipeline 64, a first hot gas delivery pipeline 65 and a first desorption concentrated gas pipeline 66 (such as Figure 1 and Figure 2 As shown in FIG. 1 , the second adsorption rotor 70 is provided with an adsorption zone 701, a cooling zone 702 and a desorption zone 703. The second adsorption rotor 70 is connected with a second clean gas discharge pipeline 72, a second cooling gas intake pipeline 73, a second cooling gas delivery pipeline 74, a second hot gas delivery pipeline 75 and a second desorption concentrated gas pipeline 76. The first adsorption rotor 60 and the second adsorption rotor 70 are respectively zeolite concentration rotors or concentration rotors of other materials.

[0081] One end of the exhaust gas intake pipeline 61 is connected to one side of the adsorption zone 601 of the first adsorption rotor 60, so that the exhaust gas intake pipeline 61 can transport the organic waste gas to one side of the adsorption zone 601 of the first adsorption rotor 60, one end of the first clean gas discharge pipeline 62 is connected to the other side of the adsorption zone 601 of the first adsorption rotor 60, and one end of the first clean gas discharge pipeline 62 is connected to one side of the adsorption zone 701 of the second adsorption rotor 70 (such as Figure 1 and Figure 2 As shown in FIG. 1 ), the organic waste gas can be transported to the adsorption zone 701 of the second adsorption wheel 70 through the first clean gas discharge pipeline 62 after the organic matter is adsorbed by the adsorption zone 601 of the first adsorption wheel 60. The other side of the adsorption zone 701 of the second adsorption wheel 70 is connected to the second clean gas discharge pipeline 72, so as to be connected to the chimney 40 through the other end of the second clean gas discharge pipeline 72. The second clean gas discharge pipeline 72 is provided with a fan 721 (as shown in FIG. Figure 2 As shown), so that the adsorbed gas in the second clean air exhaust pipeline 72 can be pushed and pulled into the chimney 40 through the fan 721 for discharge.

[0082] One side of the cooling zone 602 of the first adsorption wheel 60 is connected to the first cooling air inlet pipeline 63, so that the gas enters the cooling zone 602 of the first adsorption wheel 60 for cooling. The other side of the cooling zone 602 of the first adsorption wheel 60 is connected to one end of the first cooling air delivery pipeline 64, and the other end of the first cooling air delivery pipeline 64 is connected to one end of the second cold side pipeline 821 of the second heat exchanger 82 (such as Figure 1 and Figure 2As shown), the gas after entering the cooling zone 602 of the first adsorption rotor 60 is transported to the second heat exchanger 82 for heat exchange. In addition, one end of the first hot gas transport pipeline 65 is connected to the other side of the desorption zone 603 of the first adsorption rotor 60, and the other end of the first hot gas transport pipeline 65 is connected to the other end of the second cold side pipeline 821 of the second heat exchanger 82, so that the high-temperature hot gas that undergoes heat exchange through the second heat exchanger 82 can be transported to the desorption zone 603 of the first adsorption rotor 60 through the first hot gas transport pipeline 65 for desorption.

[0083] The cooling zone 602 of the first adsorption rotor 60 is provided with two embodiments, wherein the first embodiment is that the first cooling air intake pipe 63 connected to one side of the cooling zone 602 of the first adsorption rotor 60 is provided with fresh air or external air (not shown), and the cooling zone 602 of the first adsorption rotor 60 is cooled by the fresh air or external air. The second embodiment is that the exhaust gas intake pipe 61 is provided with an exhaust gas connecting pipe 611 (such as Figure 1 As shown in the figure), the other end of the exhaust gas connecting pipe 611 is connected to the first cooling air intake pipe 63, so that the exhaust gas in the exhaust gas intake pipe 61 can be transported to the cooling zone 601 of the first adsorption wheel 60 through the exhaust gas connecting pipe 611 for cooling. The exhaust gas connecting pipe 611 is provided with an exhaust gas connecting control valve 6111 to control the air volume of the exhaust gas connecting pipe 611.

[0084] One side of the cooling zone 702 of the second adsorption wheel 70 is connected to the second cooling air inlet pipeline 73, so that the gas enters the cooling zone 702 of the second adsorption wheel 70 for cooling. The other side of the cooling zone 702 of the second adsorption wheel 70 is connected to one end of the second cooling air delivery pipeline 74, and the other end of the second cooling air delivery pipeline 74 is connected to one end of the third cold side pipeline 831 of the third heat exchanger 83 (such as Figure 1 and Figure 2 As shown), the gas after entering the cooling zone 702 of the second adsorption rotor 70 is transported to the third heat exchanger 83 for heat exchange. In addition, one end of the second hot gas transport pipeline 75 is connected to the other side of the desorption zone 703 of the second adsorption rotor 70, and the other end of the second hot gas transport pipeline 75 is connected to the other end of the third cold side pipeline 831 of the third heat exchanger 83, so that the high-temperature hot gas that undergoes heat exchange through the third heat exchanger 83 can be transported to the desorption zone 703 of the second adsorption rotor 70 through the second hot gas transport pipeline 75 for desorption.

[0085] The cooling zone 702 of the second adsorption rotor 70 is provided with two implementation modes, wherein the first implementation mode is that the second cooling air intake pipe 73 connected to one side of the cooling zone 702 of the second adsorption rotor 70 is used to supply fresh air or external air (such as Figure 2 As shown in FIG. 1 ), the fresh air or external air is used to cool the cooling area 702 of the second adsorption rotor 70. In a second embodiment, the first clean air discharge pipeline 62 is provided with a first clean air communication pipeline 621 (as shown in FIG. 1 ). Figure 1 As shown in the figure), the other end of the first clean air connecting pipeline 621 is connected to the second cooling air inlet pipeline 73, so that the gas in the first clean air discharge pipeline 62 can be transported to the cooling zone 702 of the second adsorption wheel 70 through the first clean air connecting pipeline 621 for cooling. The first clean air connecting pipeline 621 is provided with a first clean air connecting control valve 6211 to control the air volume of the first clean air connecting pipeline 621.

[0086] One end of the first desorption concentrated gas pipeline 66 is connected to one side of the desorption zone 603 of the first adsorption rotor 60, and the other end of the first desorption concentrated gas pipeline 66 is connected to one end of the fourth cold side pipeline 841 of the fourth heat exchanger 84 (such as Figure 1 and Figure 2 As shown), the other end of the fourth cold side pipeline 841 of the fourth heat exchanger 84 is connected to one end of the fourth cold side delivery pipeline 86, and the other end of the fourth cold side delivery pipeline 86 is connected to one end of the first cold side pipeline 811 of the first heat exchanger 81. In addition, the other end of the first cold side pipeline 811 of the first heat exchanger 81 is connected to one end of the first cold side delivery pipeline 85, and the other end of the first cold side delivery pipeline 85 is connected to the inlet of the direct-fired incinerator (TO) 101, so that the desorbed concentrated gas desorbed by high temperature can be transported to one end of the fourth cold side pipeline 841 of the fourth heat exchanger 84 through the first desorbed concentrated gas pipeline 66, and the fourth cold side pipeline 841 of the fourth heat exchanger 84 The other end of the pipeline 841 is transported to one end of the fourth cold side transport pipeline 86, and the other end of the fourth cold side transport pipeline 86 is transported to one end of the first cold side pipeline 811 of the first heat exchanger 81, and then the other end of the first cold side pipeline 811 of the first heat exchanger 81 is transported to one end of the first cold side transport pipeline 85, and finally the other end of the first cold side transport pipeline 85 is transported to the inlet of the direct-fired incinerator (TO) 101 (such as Figure 1 and Figure 2As shown), the burner head of the direct-fired incinerator (TO) 101 can be subjected to high-temperature cracking to reduce volatile organic compounds. The first desorbed concentrated gas pipeline 66 is provided with a fan 661 to push and pull the desorbed concentrated gas into one end of the first cold side pipeline 811 of the first heat exchanger 81.

[0087] One end of the second desorption concentrated gas pipeline 76 is connected to one side of the desorption zone 703 of the second adsorption rotor 70, wherein the other end of the second desorption concentrated gas pipeline 76 has two implementation modes. The first implementation mode is that the other end of the second desorption concentrated gas pipeline 76 is connected to the exhaust gas intake pipeline 61 (such as Figure 1 As shown in FIG. 1 ), the concentrated gas can enter the adsorption zone 601 of the first adsorption wheel 60 through the exhaust gas intake pipe 61 for re-adsorption. The second embodiment is that the other end of the second desorption concentrated gas pipeline 76 is connected to the first cooling gas intake pipe 63 (as shown in FIG. Figure 2 As shown in FIG. 1 ), the concentrated gas can then enter the cooling zone 602 of the first adsorption rotor 60 through the first cooling gas inlet pipeline 63 for cooling. In addition, the second desorption concentrated gas pipeline 76 is provided with a fan 761 (as shown in FIG. Figure 2 As shown in the figure, the desorbed concentrated gas can be pushed and pulled into the exhaust gas intake pipe 61 or the first cooling gas intake pipe 63. The desorbed gas generated by the desorption zone 703 of the second adsorption rotor 70 can enter the adsorption zone 601 of the first adsorption rotor 60 or the cooling zone 602 of the first adsorption rotor 60 for recycling.

[0088] Finally, the dual-rotor volatile organic gas (VOC) treatment system 1 may be provided with only the first heat exchanger 81, the second heat exchanger 82, the third heat exchanger 83, and the fourth heat exchanger 84 in the direct-fired incinerator (TO) 101 (e.g., Figure 6 and Figure 7As shown), the difference is that the fourth heat exchanger 84 is subtracted, and the other end of the first desorption concentrated gas pipeline 66 is connected to one end of the first cold side pipeline 811 of the first heat exchanger 81, wherein the other end of the first cold side pipeline 811 of the first heat exchanger 81 is connected to one end of the first cold side transport pipeline 85, and the other end of the first cold side transport pipeline 85 is connected to the inlet of the direct-fired incinerator (TO) 101, so that the desorbed concentrated gas desorbed by high temperature can be transported to one end of the first cold side pipeline 811 of the first heat exchanger 81 through the first desorption concentrated gas pipeline 66, and transported from the other end of the first cold side pipeline 811 of the first heat exchanger 81 to one end of the first cold side transport pipeline 85, and transported from the other end of the first cold side transport pipeline 85 to the inlet of the direct-fired incinerator (TO) 101. The rest of the first adsorption rotor 60 and the second adsorption rotor 70 adopt the same design. Therefore, the above-mentioned direct-fired incinerator (TO) 101, the first heat exchanger 81, the second heat exchanger 82, the third heat exchanger 83, the first cold side transport pipeline 85, the first adsorption rotor 60, the second adsorption rotor 70 and the chimney 40 are not repeated. Please refer to the above-mentioned description.

[0089] In addition to being designed in combination with the double-rotor volatile organic gas (VOC) treatment system 1 as described above, the incineration equipment 10 of the present invention can also be designed in combination with a single-rotor volatile organic gas (VOC) treatment system (not shown). The difference between the single-rotor volatile organic gas (VOC) treatment system (not shown) and the double-rotor volatile organic gas (VOC) treatment system described above is that the second adsorption rotor 70 is missing. The direct-fired incinerator (TO) 101 can be replaced with two heat exchangers or three heat exchangers. The configuration can refer to the design of the first adsorption rotor 60 in the double-rotor volatile organic gas (VOC) treatment system 1, and its content will not be repeated. Please refer to the above description.

[0090] Through the above detailed description, it can be understood by those skilled in the art that the utility model can indeed achieve the aforementioned purpose and actually complies with the provisions of the Patent Law, and thus a patent application is filed.

[0091] However, the above is only a preferred embodiment of the present utility model, and should not be used to limit the scope of implementation of the present utility model; therefore, all simple equivalent changes and modifications made according to the protection scope of the claims of the present utility model and the contents of the utility model specification should still fall within the scope of protection of the present utility model.

[0092] The embodiments of the present invention are described above. However, these embodiments are for illustrative purposes only and are not intended to limit the scope of the present invention. Although the embodiments are described above separately, this does not mean that the measures in the various embodiments cannot be used in combination to advantage. The scope of the present invention is defined by the attached claims and their equivalents. Without departing from the scope of the present invention, a person skilled in the art may make a variety of substitutions and modifications, which should all fall within the scope of the present invention.

Claims

1. A system for enriching carbon dioxide from combustion tail gas, characterized in that: include: An incineration device, which emits a combustion tail gas, the combustion tail gas contains carbon dioxide gas, and the incineration device is provided with a tail gas delivery pipeline to deliver the combustion tail gas; a cooling device, which is arranged on the exhaust gas delivery pipeline to cool the combustion exhaust gas; A first adsorption and desorption device, the first adsorption and desorption device has at least one first adsorption zone and at least one first desorption zone, the first adsorption and desorption device is provided with at least one first exhaust pipeline, at least one first hot gas pipeline, and at least one first desorption gas pipeline, the at least one first adsorption zone is connected to the exhaust gas conveying pipeline of the incineration equipment, so as to deliver the combustion exhaust gas of the exhaust gas conveying pipeline to the at least one first adsorption zone for carbon dioxide gas adsorption, the at least one first adsorption zone is connected to the at least one first exhaust pipeline, so as to discharge the adsorbed gas generated by the at least one first adsorption zone through the at least one first exhaust pipeline, the at least one first desorption zone is connected to the at least one first desorption gas pipeline, so as to output the carbon dioxide gas desorbed from the at least one first desorption zone through the at least one first desorption gas pipeline, and the at least one first desorption zone is connected to the at least one first hot gas pipeline, so as to transport at least one heat source to the at least one first desorption zone through the at least one first hot gas pipeline; A second adsorption and desorption device, the second adsorption and desorption device having at least one second adsorption zone and at least one second desorption zone, the second adsorption and desorption device being provided with at least one second exhaust pipeline, at least one second hot gas pipeline, and at least one second desorption gas pipeline, the at least one second adsorption zone being connected to the at least one first desorption gas pipeline so as to deliver the desorbed carbon dioxide gas generated in the at least one first desorption zone to the at least one second adsorption zone for re-adsorption of carbon dioxide gas, the at least one second adsorption zone being connected to the at least one second exhaust pipeline so as to discharge the re-adsorbed gas generated in the at least one second adsorption zone through the at least one second exhaust pipeline, the at least one second desorption zone being connected to the at least one second desorption gas pipeline so as to output the carbon dioxide gas re-desorbed in the at least one second desorption zone through the at least one second desorption gas pipeline, and the at least one second desorption zone being connected to the at least one second hot gas pipeline so as to transport at least one heat source to the at least one second desorption zone through the at least one second hot gas pipeline; a chimney, the chimney being connected to the at least one first exhaust pipeline and the at least one second exhaust pipeline respectively; as well as At least one purification device is connected to the at least one second desorption gas pipeline to deliver the desorbed carbon dioxide gas generated in the at least one second desorption zone into the purification device for purification.

2. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The tail gas delivery pipeline is also provided with a filter device, which is used for dust removal.

3. The system for enriching carbon dioxide from combustion tail gas according to claim 1, characterized in that: The exhaust gas conveying pipeline is also provided with a dust removal device, which is any one of a bag dust collector, a pulse bag dust collector, an electric bag composite dust collector, a negative pressure back-blowing filter bag dust collector, a low-pressure long bag pulse dust collector, a cartridge pulse dust collector, a pulse filter element dust collector, a pulse spray bag dust collector, an inertial dust collector, an electrostatic dust collector, a horizontal electrostatic dust collector, a centrifugal dust collector, a cyclone separator, a multi-cyclone dust collector, a wet dust collector, a wet electrostatic dust collector, a charged water mist dust collector, a water film dust collector, a Venturi tube dust collector, and a multi-layer dust collector.

4. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The cooling device is any one of a cooler, a condenser, a dehumidifier, a cooler, a cooling water tower, and a refrigerant compressor.

5. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The tail gas delivery pipeline is also provided with a fan.

6. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The at least one first exhaust pipeline is further provided with a fan, and the at least one second exhaust pipeline is further provided with a fan.

7. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The at least one first hot gas pipeline is also connected to a heat exchanger or a heater.

8. The system for enriching carbon dioxide from combustion tail gas according to claim 1, characterized in that: The at least one second hot gas pipeline is also connected to a heat exchanger or a heater.

9. The system for enriching carbon dioxide from combustion tail gas according to claim 1, characterized in that: The purification equipment is also connected to a compression and liquefaction device, which compresses and liquefies the purified carbon dioxide gas into liquid purified carbon dioxide.

10. The system for enriching carbon dioxide from combustion tail gas according to claim 9, characterized in that: The compression liquefaction device is also provided with a compressor having a cooling pipeline for either a liquid or a gas to enter the cooling pipeline so as to compress and liquefy the purified carbon dioxide gas into liquid purified carbon dioxide.

11. The system for enriching carbon dioxide from combustion exhaust gas according to claim 9, characterized in that: The compression and liquefaction device is also connected to at least one purification storage device to compress and liquefy the liquid purified carbon dioxide and store it in the at least one purification storage device.

12. The system for enriching carbon dioxide from combustion exhaust gas according to claim 11, characterized in that: The at least one purification storage device is any one of a tank truck, a steel cylinder, a barrel, a storage tank, and a container.

13. The system for enriching carbon dioxide from combustion exhaust gas according to claim 11, characterized in that: The at least one purification storage device is sent to a plant area to compress and liquefy the liquid purified carbon dioxide and send it to the plant area for use.

14. The system for enriching carbon dioxide from combustion exhaust gas according to claim 13, characterized in that: The plant is any one of a semiconductor process plant, an electronic process plant, an optoelectronic process plant, a chemical process plant, a petrochemical process plant, an electroplating process plant, a food process plant, a drying and cleaning process plant, and a pharmaceutical process plant.

15. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The purification equipment is also provided with a purification pipeline, which is connected to a factory area so as to transport the purified carbon dioxide gas to the factory area through the purification pipeline.

16. The system for enriching carbon dioxide from combustion exhaust gas according to claim 15, characterized in that: The plant is any one of a semiconductor process plant, an electronic process plant, an optoelectronic process plant, a chemical process plant, a petrochemical process plant, an electroplating process plant, a food process plant, a drying and cleaning process plant, and a pharmaceutical process plant.

17. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The purification equipment is also provided with a raw material tank, a purification tower, a heater and a cooling facility. The raw material tank is connected to the purification tower, the heater is connected to the purification tower, and the cooling facility is connected to the purification tower. The raw material tank receives the desorbed carbon dioxide gas transported by the at least one second desorption gas pipeline, and transports the desorbed carbon dioxide gas to the purification tower for convection heat exchange with the hot gas transported by the heater, so that the desorbed carbon dioxide gas is subjected to convection heat exchange to evaporate and rise the lower boiling point substances, and the higher boiling point substances sink in liquid form. The evaporated and rising lower boiling point substances are cooled by the cooling facility into high-concentration liquid carbon dioxide for filtration and purification.

18. The system for enriching carbon dioxide from combustion tail gas according to claim 17, characterized in that: The purification tower is also provided with at least one packing bed, and the packing bed is made of any one of mesh ring packing, mesh saddle packing, and double-layer wire mesh corrugated packing.

19. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The purification equipment is also provided with a raw material tank, at least one adsorption-desorption bed module and a vacuum pump. The raw material tank is connected to the at least one adsorption-desorption bed module, and the vacuum pump is connected to the at least one adsorption-desorption bed module. The raw material tank receives the desorbed carbon dioxide gas transported by the at least one second desorption gas pipeline, and transports the desorbed carbon dioxide gas to the at least one adsorption-desorption bed module for pressurized adsorption or reduced pressure desorption. During reduced pressure desorption, the vacuum pump is used to desorb high-concentration gaseous carbon dioxide in a vacuum manner for filtration and purification.

20. The system for enriching carbon dioxide from combustion exhaust gas according to claim 19, characterized in that: The adsorption-desorption bed module is filled with a plurality of tubular hollow fiber tubular membrane adsorbents, and the tubular hollow fiber tubular membrane adsorbent is any one or a combination of zeolite, anion exchange resin, and metal organic framework material.

21. The system for enriching carbon dioxide from combustion exhaust gas according to claim 20, characterized in that: The tubular hollow fiber tubular membrane adsorbent also comprises at least one pore and at least one adsorption layer. The adsorption layer comprises an amine-modified anion exchange resin material and a polymer material.

22. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The purification equipment is also provided with a raw material tank, a membrane contactor and a heater. The raw material tank is connected to the membrane contactor, and the heater is connected to the membrane contactor. The raw material tank receives the desorbed carbon dioxide gas transported by the at least one second desorption gas pipeline, and transports the desorbed carbon dioxide gas to the membrane contactor for convection heat exchange with the hot gas transported by the heater, so that the desorbed carbon dioxide gas can form a high-concentration gaseous carbon dioxide for filtration and purification.

23. The system for enriching carbon dioxide from combustion exhaust gas according to claim 22, characterized in that: The membrane contactor is also provided with at least one membrane, which is any one of a hollow fiber tubular membrane, a nanoporous carbon membrane, a polyetheretherketone membrane, a polyimide membrane, a monoethanolamine membrane, a rubber-like polymer membrane, and a polyimide hollow fiber membrane.

24. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The first adsorption and desorption device is also provided with a rotating wheel, which is filled with any one of activated carbon, zeolite, silica gel, activated alumina, molecular sieve, manganese oxide, calcium hydroxide, graphene, and hollow fiber.

25. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The second adsorption and desorption device is also provided with a rotating wheel, which is filled with any one of activated carbon, zeolite, silica gel, activated alumina, molecular sieve, manganese oxide, calcium hydroxide, graphene, and hollow fiber.

26. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The first adsorption and desorption device is also provided with at least one adsorption material, which is filled with a plurality of tubular hollow fiber tubular membrane adsorption materials. The tubular hollow fiber tubular membrane adsorption material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material.

27. The system for enriching carbon dioxide from combustion tail gas according to claim 1, characterized in that: The second adsorption-desorption device is also provided with at least one adsorption material, which is filled with a plurality of tubular hollow fiber tubular membrane adsorption materials. The tubular hollow fiber tubular membrane adsorption material is any one or a combination of zeolite, anion exchange resin, and metal organic framework material.

28. The system for enriching carbon dioxide from combustion tail gas according to claim 26 or 27, characterized in that: The tubular hollow fiber tubular membrane adsorbent also comprises at least one pore and at least one adsorption layer. The adsorption layer comprises an amine-modified anion exchange resin material and a polymer material.

29. The system for enriching carbon dioxide from combustion exhaust gas according to claim 1, characterized in that: The incineration equipment is any one of a direct-fired incinerator, a catalytic incinerator, and a thermal storage incinerator.

30. The system for enriching carbon dioxide from combustion tail gas according to claim 1, characterized in that: The incineration device is also designed to be combined with either a double-rotor volatile organic gas treatment system or a single-rotor volatile organic gas treatment system.

31. The system for enriching carbon dioxide from combustion tail gas according to claim 29, characterized in that: The direct-fired incinerator is also provided with any one of two heat exchangers, three heat exchangers, and four heat exchangers.

Images