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WO2011155058A1 - Appareil permettant de séparer des gaz - Google Patents

Appareil permettant de séparer des gaz Download PDF

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Publication number
WO2011155058A1
WO2011155058A1 PCT/JP2010/059931 JP2010059931W WO2011155058A1 WO 2011155058 A1 WO2011155058 A1 WO 2011155058A1 JP 2010059931 W JP2010059931 W JP 2010059931W WO 2011155058 A1 WO2011155058 A1 WO 2011155058A1
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Prior art keywords
adsorption
heat
gas
tower
adsorption tower
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Ceased
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PCT/JP2010/059931
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English (en)
Japanese (ja)
Inventor
丸山　一孝
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ENERGY PRODUCTS Co Ltd
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ENERGY PRODUCTS Co Ltd
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Priority to JP2012519187A priority Critical patent/JP5669835B2/ja
Priority to PCT/JP2010/059931 priority patent/WO2011155058A1/fr
Publication of WO2011155058A1 publication Critical patent/WO2011155058A1/fr
Anticipated expiration legal-status Critical
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0438—Cooling or heating systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/40098—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating with other heating means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a gas separation device.
  • biogas generated in sewage treatment plants, livestock manure, garbage, and fermenters that produce alcoholic beverages is mainly composed of methane (CH 4 ) gas and carbon dioxide (CO 2 ) gas.
  • CH 4 methane
  • CO 2 carbon dioxide
  • Biogas has a methane content of approximately 55 to 65% and a carbon dioxide content of approximately 35 to 45%, although it varies depending on the composition of the organic material from which it is generated.
  • PSA Pressure-Swing-Adsorption
  • biogas is passed through a tower packed with physical adsorbents (molecular sieves) such as synthetic zeolite, activated alumina, ceramics, porous glass, porous resin, etc., and methane is separated and purified.
  • physical adsorbents molecular sieves
  • Carbon dioxide and water are adsorbed and desorbed by using the difference in adsorption capacity with respect to the pressure of water.
  • a plurality of adsorption towers are prepared, and biogas is continuously processed by switching to an adsorption process and a regeneration process, or an adsorption process, a depressurization process, a regeneration process, and a pressure equalization process.
  • a part of the product gas for example, about 15 to 20%
  • the TSA (Thermal Swing Adsorption) method can be considered.
  • a biogas is passed through a tower filled with an adsorbent that supports a chemical adsorption component such as potassium carbonate or amine on a support such as activated carbon or porous resin, and only methane is exhausted.
  • a chemical adsorption component such as potassium carbonate or amine
  • a support such as activated carbon or porous resin
  • Carbon dioxide and water are adsorbed and desorbed using the difference in adsorption capacity with respect to the temperature of the agent.
  • a plurality of adsorption towers are prepared and the biogas is continuously processed.
  • an object of the present application is to provide a gas separation device that efficiently separates a specific component from a mixed gas while reducing the number of components compared to the conventional one.
  • a plurality of adsorption towers are prepared, and at the time of regeneration, regeneration is performed at a pressure lower than that at the time of adsorption and at an ambient temperature or lower, and the heat transfer tubes of the adsorption tower being adsorbed A heat medium is circulated between the heat transfer tubes of the adsorption tower being regenerated.
  • This heat medium effectively uses the heat of adsorption as the heat of desorption. Further, in order to compensate for the heat shortage necessary for heat radiation and desorption generated by adsorption, the adsorption tower being adsorbed and the adsorption tower being regenerated are exchanged with air outside the tower.
  • a gas separation device that separates a specific component from a mixed gas composed of a plurality of components, wherein the specific component in the mixed gas is adsorbed, a plurality of adsorption towers including heat transfer tubes, A heat medium circulation path for circulating a heat medium between the heat transfer pipe of the adsorption tower being adsorbed and the heat transfer pipe of the adsorption tower being regenerated among the plurality of adsorption towers, and the heat medium circulation path is at least outside
  • the adsorption heat of the adsorption tower that is higher than the temperature is transferred to the adsorption tower that is being regenerated by the heat medium, and the adsorption tower that is being regenerated is at least lower in pressure than the adsorption tower that is being adsorbed.
  • regeneration is performed at a temperature lower than the outside air temperature, and heat exchange is performed with the outside air outside the adsorption tower that is being regenerated.
  • the specific component to be separated by the gas separation device is a gas composed of components contained in a mixed gas, and is a gas composed of at least components that can be physically adsorbed by the adsorption tower.
  • the temperature of the adsorption tower during adsorption becomes higher than the outside air temperature, and the adsorption tower being regenerated is set to regenerate at least at a pressure lower than the adsorption tower during adsorption and below the outside air temperature. . Since the adsorption temperature is higher than the outside air temperature and the regeneration temperature is lower than the outside air temperature, the mixed gas provided from the upper process is continuously operated by operating the adsorption tower and the regeneration tower side by side.
  • the heat generated by the adsorption action can be used as the heat of the desorption action only by circulating the heat medium passing through the heat transfer tubes in the adsorption tower while realizing the typical treatment.
  • the heat medium circulating in the heat medium circulation path is a medium capable of transporting the heat of each adsorption tower, and examples thereof include water. Since the adsorption temperature is higher than the regeneration temperature, the heat of adsorption can be transferred by circulating a heat medium between the tower being adsorbed and the tower being regenerated. Further, since the regeneration temperature is lower than the outside air temperature, the heat corresponding to the temperature drop caused by the pressure drop when transitioning from the adsorption state to the regeneration state can be compensated by the heat exchange of the adsorption tower with the outside air. As a result, the heat of adsorption is used without leakage and a heat source is not required. Therefore, it is possible to efficiently separate the specific component from the mixed gas while reducing the number of components compared to the related art.
  • the adsorption tower during adsorption may adsorb at least at a temperature higher than the outside air temperature and exchange heat with the outside air outside the adsorption tower during adsorption. According to this, heat dissipation of adsorption heat is promoted, and adsorption performance can be enhanced.
  • the mixed gas is biogas
  • the specific component is carbon dioxide
  • the gas separation device removes impurities contained in the biogas upstream of the plurality of adsorption towers.
  • a pretreatment tower may be further provided.
  • Such a mixed gas may contain various impurity components.
  • carbon dioxide can be produced from biogas without complicating the components. It can be separated efficiently.
  • Specific components can be efficiently separated from the mixed gas while reducing the number of components.
  • FIG. 1 is a configuration diagram of a biogas separation and recovery system 1 (corresponding to a gas separation device in the present invention) 1 according to an embodiment.
  • the biogas separation / recovery system 1 according to the present embodiment separates and recovers methane, carbon dioxide, water, and the like from so-called biogas generated in a sewage treatment plant, livestock manure, garbage, a fermenter that produces alcoholic beverages, and the like. Then, the separated methane is sent out as various fuel gases, and the separated carbon dioxide is sent out as a raw material for industrial gas such as food additives.
  • the biogas processed by the biogas separation and recovery system 1 according to the present embodiment is assumed to have a methane content of approximately 55 to 65% and a carbon dioxide content of approximately 35 to 45%. .
  • biogas separation system 1 is not applied only to such biogas separation.
  • the present invention can be applied to a case where carbon dioxide, water, etc. are separated and recovered from combustion exhaust gas such as factory exhaust gas. Further, carbon dioxide separated from biogas does not necessarily need to be effectively used as a raw material for industrial gas, and may be discarded, for example.
  • Biogas is produced by fermenting with fungi after transitioning high molecular organic substances contained in organic waste or the like to low molecular organic substances.
  • the biogas generated in the fermenter for the purpose of reducing organic waste is recovered by the biogas separation and recovery system 1 and the methane and carbon dioxide contained in the biogas are separated, thereby reducing the waste energy and the biomass energy. Effective commercialization and commercialization of gas for various uses are planned.
  • the biogas separation and recovery system 1 is a two-system adsorption tower 2A filled with an adsorbent such as molecular sieve or activated carbon in order to continuously separate impurities such as methane, carbon dioxide and water in the biogas. , B.
  • the tower may be filled with an adsorbent that adsorbs carbon dioxide or water, or an adsorbent that adsorbs water on the upstream side of the tower and adsorbs carbon dioxide on the downstream side. It may be a two-layer structure filled with an adsorbent.
  • strain here is called adsorption tower 2A, B
  • strain is not limited to what is single body, It divides
  • the biogas separation and recovery system 1 is based on the PSA method, and performs heat exchange between the adsorption side and the regeneration side to improve the adsorption / desorption performance. That is, the biogas separation / recovery system 1 uses a circulating water tank, a circulating water pump, or the like to effectively use the heat generated when adsorbing carbon dioxide as heat when desorbing and regenerating carbon dioxide.
  • a device 3 is provided. By this water circulation device 3, the adsorption temperature is in the range of approximately 0 to 60 ° C., and the regeneration temperature is in the relatively low temperature range of approximately ⁇ 10 to 50 ° C.
  • the circulation route only needs to be able to transfer the heat of adsorption as circulating water as an intermediate heat medium, and may circulate the adsorption towers in parallel or in series, or may switch the flow direction as necessary.
  • an intermediate heat medium for example, a medium excellent in heat transport such as Freon gas or ammonia gas can be applied.
  • Freon gas or ammonia gas can be used as the intermediate heat medium.
  • the adsorption heat is removed on the adsorption side so as to suppress a decrease in adsorption performance due to a temperature rise.
  • heat lost by regeneration and pressure swing is compensated to suppress a decrease in desorption performance, and the adsorption / desorption performance is improved.
  • the concentration of carbon dioxide in the gas to be processed is relatively high, such as the biogas processed by the biogas separation and recovery system 1 according to the present embodiment, a lot of heat of adsorption is generated. For this reason, if there is no heat exchange function such as an adsorption tower structure equipped with heat transfer tubes and a water circulation device 3, it is difficult to treat the adsorption heat by the adsorption process alone. A combination with a pretreatment process capable of treating 1 to 2% is required. In the present biogas separation and recovery system 1, not only can the adsorption process be performed alone, but also the effective utilization of the heat of adsorption by the water circulation device 3 for the regeneration heat can be realized. For this reason, thermal energy is utilized very effectively.
  • each process value is in the order of adsorption temperature, outside air temperature (ambient temperature), and desorption temperature in descending order of temperature.
  • the heat of adsorption can be used as the heat of desorption without performing special control. That is, by setting the regeneration temperature lower than the adsorption temperature, the heat of adsorption can be used as heat for regeneration only by transferring the heat of adsorption using a heat medium.
  • each process value of the whole system will shift naturally according to the change of outside temperature, without performing special operation.
  • ⁇ Adsorption heat and desorption heat are theoretically equivalent, but the temperature drops due to pressure swing.
  • a part of the regenerative heat including the temperature drop is obtained from the outside air by actively exchanging heat with the outside air. Can compensate for heat.
  • the desorption temperature is set lower than the outside air temperature, regeneration by suppressing the temperature drop of the gas generated at the time of depressurization during regeneration by active heat exchange between the outer surface of the adsorption tower and the outside air. Reduction in rate is prevented. For this reason, compared with the case where a separate heat source is provided, the apparatus can be simplified and configured compactly, and heat dissipation loss can be eliminated.
  • the biogas separation / recovery system 1 includes a pressure equalizing buffer tank 4 for stabilizing gas components and pressure to flow in a downstream process, a vacuum pump 5 used for regeneration of the adsorption towers 2A and B, and a drain separator as others. 6, an off-gas KO drum (a steam separator) 7, and various valves.
  • the adsorption towers 2A and 2B are in the form of a fixed tube plate type heat exchanger in order to realize heat transport by the water circulation device 3.
  • the biogas which is the raw material gas, passes through the cylinder side filled with the adsorbent, and a heat medium such as water or an aqueous ethylene glycol solution flows through the pipe side connected to the water circulation device 3.
  • the heat insulating material is not attached to the shell outer surfaces of the adsorption towers 2A and 2B, and heat exchange with the outside air is performed. Vertical or brim-shaped heat transfer fins are provided as necessary.
  • the adsorption towers 2A and 2B having such a structure, in order to adsorb carbon dioxide and water, an appropriate amount of adsorbent is filled to secure a channel area in the tower for ensuring a certain contact time. It is required to secure a heat transfer area for efficient heat exchange of heat of adsorption / desorption with the medium.
  • the flow path area in the tower is uniquely determined by the gas flow rate, and the heat transfer area is uniquely determined by the amount of gas, the amount of gas components to be adsorbed and desorbed, and the pressure operation conditions.
  • the biogas separation and recovery system 1 is designed so that the gas flow rate in the adsorption towers 2A and B is operated at 1 m / s or less, as in the case of a general adsorption tower. Has been.
  • the gas side film heat transfer coefficient remains at about 10 to 100 W / m 2 K, which is a large difference from the pipe side film heat transfer coefficient.
  • the adsorption towers 2A and 2B according to the present embodiment employ a fin tube as a heat transfer tube to ensure a large heat transfer area. In order to make the filling of the adsorbent relatively easy, it is preferable to employ a low fin tube.
  • the biogas separation and recovery system 1 configured as described above operates as follows.
  • FIG. 1 shows a state where the adsorption tower 2A is in the adsorption process and the adsorption tower 2B is in the regeneration process.
  • a valve V1A that can open and close a pipe path that leads from the drain separator 6 to the adsorption tower 2A, and a pipe that leads from the adsorption tower 2A to the pressure equalization buffer tank 4 By opening the valve 4A capable of opening and closing the path, the biogas sent from the upper process is vented.
  • the ventilation of the biogas is stopped by closing the valve 1B and the valve 4B, and the pipe connecting the adsorption tower 2B to the vacuum pump 5
  • the vacuum pump 5 evacuates the adsorption tower 2B.
  • the adsorption heat generated in the adsorption tower 2A is transferred to the adsorption tower 2B by the water circulation device 3 and used as desorption heat in the adsorption tower 2B. Further, heat for compensating for the temperature drop due to the pressure swing (decompression) is taken in from the ambient outside air.
  • the carbon dioxide desorbed in the adsorption tower 2B passes through the vacuum pump 5 and the off-gas KO drum 7, and can be used as product CO 2 gas by being treated as off-gas by a carbon dioxide purification facility outside the system. is there.
  • the adsorption process is performed under atmospheric pressure to a low pressure of about 0.06 MPa (G) (more preferably 0.02 MPa (G ) And the like, and the regeneration step is basically based on regeneration using a vacuum pump 5 under a vacuum of 100 torr or less (under negative pressure).
  • the biogas supplied from the upper process is already pressurized, and a certain pressure (for example, 0.2 MPa (G) or more) is already applied, and the biogas is adsorbed at that pressure.
  • the regeneration pressure may be any pressure from a vacuum of ⁇ 0.1 MPa to a normal pressure region of about 0.01 MPa.
  • the vacuum pump 5 can be omitted.
  • the adsorption towers 2A and B perform the adsorption process and the regeneration process alternately in this way, so that the biogas supplied from the upper process is continuously processed.
  • the valves 1A (B) and 4A (B) are closed from the state where both towers are in the adsorption process, and then the valve 2A (B) is opened and the vacuum pump 5 is turned on. to start.
  • the period from when the vacuum pump 5 is started until the pressure drop in the adsorption tower settles can be regarded as a depressurization process from the adsorption process to the regeneration process.
  • valve 2A (B) is closed and the vacuum pump 5 is stopped, and then the valves 1A (B) and 4A (B) are opened.
  • the pressure in the adsorption tower 2A (B) becomes equal to the pressure in the adsorption tower 2B (A)
  • a part of the purified biogas flowing downstream of the adsorption tower 2B (A) is absorbed in the adsorption tower. It will flow into 2A (B).
  • the pressure equalization buffer tank 4 suppresses fluctuations in the flow rate of the gas flowing in the flow paths downstream of the adsorption towers 2A and 2B.
  • valve 3A (B) is opened to equalize the pressure in both towers, and then the valve 1A (B) and the valve 4A (B) are opened to close the valve 3A (B).
  • a pressure equalization step may be performed between the regeneration step and the transition to the adsorption step. Operations of the series of valves and pumps are sequentially controlled by control devices (not shown).
  • the biogas separation and recovery system 1 can directly receive high-concentration carbon dioxide gas, eliminates the need for a large pretreatment facility such as a high-pressure water washing process, and can greatly reduce the number of components.
  • the recovery rate of methane gas is about 65 to 85% due to loss outside the system in the prior art, whereas it is 95% or more in this embodiment.
  • the recovered methane gas has a purity of 95% or more. Therefore, even if it does not perform a large-scale process in the downstream process, it can be used as various industrial raw materials such as food additives for the purpose of adding impurities and other refining processes.
  • the biogas separation / recovery system 1 since the adsorption / desorption heat and the outside air heat are effectively used by the water circulation device 3 and a separate heat source is not necessary, the power energy used for driving the circulation pumps and the control power source is sufficient. Sufficient and energy saving. In particular, since the biogas separation and recovery system 1 is a low-pressure process, power consumption of a rotating machine or the like is suppressed.
  • the biogas separation and recovery system 1 can save energy while reducing the number of components, the recovery cost of methane and carbon dioxide contained in the biogas can be greatly reduced. . In trial calculation, it can be reduced to at least one third of the conventional method. In addition, since the gas that can be effectively used can be recovered even though it is an energy saving and resource saving type system, it can directly contribute to the reduction of environmental load.
  • the biogas separation / recovery system 1 In the biogas separation / recovery system 1 according to the above embodiment, a blower that covers the pressure loss in the system is not provided in the path through which the biogas flows.
  • the biogas separation / recovery system 1 is based on a low pressure, and the biogas supplied from the higher-level process may be sent at a very low pressure from atmospheric pressure to a slight positive pressure. Therefore, in such a case, in order to compensate for the pressure loss in the system, as shown in FIG. 2, pressures such as the raw material gas blower 8 and the gas compressor 9 are provided upstream and downstream of the adsorption towers 2A and 2B. You may provide the equipment which compensates for loss as needed.
  • the pressure equalization buffer tank 4 is branched from the main path (that is, the branch returning to the adsorption towers 2A and B downstream of the gas compressor 9). If it is provided in the path), it is possible to effectively suppress flow rate fluctuations during pressure equalization.
  • the biogas separation and recovery system 1 employs a configuration in which the exhaust from the vacuum pump 5 is directly sent to a lower process.
  • the biogas separation and recovery system 1 may adopt a configuration in which a part of the exhaust of the vacuum pump 5 returns to the adsorption tower being regenerated. In this case, since the regeneration of the adsorption tower is promoted, the carbon dioxide recovery efficiency can be increased.
  • a specific configuration for returning a part of the exhaust of the vacuum pump 5 to the regenerating adsorption tower for example, a path between the adsorption tower 2A (B) and the valve V3A (B), the off-gas KO drum 7, A route having a valve in the middle is provided. By opening and closing the valve together with the valve V1A (B), a path for returning a part of the exhaust of the vacuum pump 5 to the adsorption tower is formed.
  • biogas contains a trace amount of impurity components such as nitrogen, oxygen, moisture, siloxane, hydrogen sulfide, and ammonia.
  • impurity components such as nitrogen, oxygen, moisture, siloxane, hydrogen sulfide, and ammonia.
  • Siloxane, hydrogen sulfide, ammonia, and the like are harmful components for use in fuels and food additives, and thus need to be removed. Therefore, when directly receiving and processing biogas, as shown in FIG. 2, depending on the necessity of the product, a pretreatment tower 10 filled with an adsorbent such as activated carbon is installed in front of the adsorption towers 2A and 2B. By adsorbing and removing these components in advance, impurities can be contained in the carbon dioxide gas separated and recovered in addition to the purified biogas, and a high value-added gas can be provided.
  • the adsorption temperature and the regeneration temperature are set so as to sandwich the outside air temperature.
  • the heat medium circulating in the water circulation device 3 is fixed by a heater or a cooler.
  • the temperature may be controlled within a temperature range (for example, 35 to 40 ° C.), and the adsorption temperature may be set higher than this temperature range, and the regeneration temperature may be set lower than this temperature range.
  • each adsorption tower may be provided with a heat insulating material for preventing heat exchange with the outside air. Even if the biogas separation and recovery system 1 according to the above-described embodiment is configured in this way, at least the heat of adsorption can be used as the desorption heat, so that the heat energy can be used effectively.

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Abstract

L'appareil permettant de séparer des gaz ci-décrit est conçu pour réduire le nombre de dispositifs par rapport au passé et pour séparer efficacement des composants spécifiques contenus dans un mélange gazeux. L'appareil permettant de séparer des gaz (1) selon l'invention, qui sépare des composants spécifiques contenus dans un mélange gazeux qui comprend de multiples composants, est constitué d'une pluralité de tours d'adsorption (2A et 2B) qui adsorbent des composants spécifiques contenus dans le mélange gazeux et renferment des tuyaux de transfert thermique, et d'un circuit de circulation de milieu caloporteur (3) qui fait circuler ledit milieu caloporteur entre le tuyau de transfert thermique de la tour d'adsorption (2A) de la pluralité de tours d'adsorption (2A et 2B) qui adsorbe et le tuyau de transfert thermique de la tour d'adsorption (2B) en cours de régénération. A l'aide du milieu caloporteur, le circuit de circulation de milieu caloporteur (3) transfère la chaleur d'adsorption de la tour d'adsorption (2A) qui adsorbe et dont la température s'accroît au moins au-dessus de la température externe, vers la tour d'adsorption (2B) en cours de régénération. La tour d'adsorption (2B) en cours de régénération est régénérée à une pression qui est inférieure à celle de la tour d'adsorption (2A) qui adsorbe et à une température inférieure à la température externe et échange également de la chaleur avec l'air à l'extérieur de la tour d'adsorption (2B) en cours de régénération.
PCT/JP2010/059931 2010-06-11 2010-06-11 Appareil permettant de séparer des gaz Ceased WO2011155058A1 (fr)

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JP2012519187A JP5669835B2 (ja) 2010-06-11 2010-06-11 ガス分離装置
PCT/JP2010/059931 WO2011155058A1 (fr) 2010-06-11 2010-06-11 Appareil permettant de séparer des gaz

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PCT/JP2010/059931 WO2011155058A1 (fr) 2010-06-11 2010-06-11 Appareil permettant de séparer des gaz

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JP2014077060A (ja) * 2012-10-10 2014-05-01 Metawater Co Ltd メタン発酵ガスの精製方法および精製システム
JP2014077065A (ja) * 2012-10-10 2014-05-01 Metawater Co Ltd 都市ガスの製造方法および製造システム
CN104128074A (zh) * 2014-07-28 2014-11-05 王新建 一种压缩空气干燥吸附系统
CN104368220A (zh) * 2014-05-20 2015-02-25 常州大学 一种新型高效的有机废气吸附塔
JP2016052285A (ja) * 2014-09-04 2016-04-14 本田技研工業株式会社 二酸化炭素回収装置
CN110527571A (zh) * 2019-09-11 2019-12-03 张家港富瑞特种装备股份有限公司 一种天然气过滤计量脱水脱汞模块
CN114225631A (zh) * 2022-01-06 2022-03-25 江西微碳能源科技有限公司 一种恒温吸附解析脱碳系统及脱碳方法
CN114504935A (zh) * 2020-11-16 2022-05-17 巴特尔纪念研究院 用于以最小能耗进行除湿和大气水提取的方法和系统
WO2022122472A1 (fr) * 2020-12-11 2022-06-16 Thyssenkrupp Marine Systems Gmbh Sous-marin ayant un absorbeur de co2
DE102024102529B3 (de) 2024-01-30 2025-01-09 Elke Münch Vorrichtung und Verfahren für die reversible Adsorption und Desorption des Kohlendioxids in Verbrennungsabgasen
WO2025203345A1 (fr) * 2024-03-27 2025-10-02 本田技研工業株式会社 Dispositif de récupération de dioxyde de carbone
DE102024114508A1 (de) * 2024-05-23 2025-11-27 Elke Hildegard Münch Vorrichtung zur Kühlung von sehr heißen Gasen auf Temperaturen S50° C mithilfe von temperaturoptimierten Wärmerohren und ihre Verwendung bei der Kohledioxidabscheidung

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CN119435162A (zh) * 2025-01-09 2025-02-14 东方电气集团东方汽轮机有限公司 煤电排烟碳捕集与二氧化碳储能一体化系统及其控制方法

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JPS60129116A (ja) * 1983-12-16 1985-07-10 Kobe Steel Ltd 非加熱再生型吸着装置
JPS6391120A (ja) * 1986-10-01 1988-04-21 ザ・ビ−オ−シ−・グル−プ・インコ−ポレ−テッド 圧力切換装置
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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2014077060A (ja) * 2012-10-10 2014-05-01 Metawater Co Ltd メタン発酵ガスの精製方法および精製システム
JP2014077065A (ja) * 2012-10-10 2014-05-01 Metawater Co Ltd 都市ガスの製造方法および製造システム
CN104368220A (zh) * 2014-05-20 2015-02-25 常州大学 一种新型高效的有机废气吸附塔
CN104128074A (zh) * 2014-07-28 2014-11-05 王新建 一种压缩空气干燥吸附系统
CN104128074B (zh) * 2014-07-28 2015-12-09 王新建 一种压缩空气干燥吸附系统
JP2016052285A (ja) * 2014-09-04 2016-04-14 本田技研工業株式会社 二酸化炭素回収装置
CN110527571A (zh) * 2019-09-11 2019-12-03 张家港富瑞特种装备股份有限公司 一种天然气过滤计量脱水脱汞模块
CN114504935A (zh) * 2020-11-16 2022-05-17 巴特尔纪念研究院 用于以最小能耗进行除湿和大气水提取的方法和系统
WO2022122472A1 (fr) * 2020-12-11 2022-06-16 Thyssenkrupp Marine Systems Gmbh Sous-marin ayant un absorbeur de co2
CN114225631A (zh) * 2022-01-06 2022-03-25 江西微碳能源科技有限公司 一种恒温吸附解析脱碳系统及脱碳方法
DE102024102529B3 (de) 2024-01-30 2025-01-09 Elke Münch Vorrichtung und Verfahren für die reversible Adsorption und Desorption des Kohlendioxids in Verbrennungsabgasen
WO2025203345A1 (fr) * 2024-03-27 2025-10-02 本田技研工業株式会社 Dispositif de récupération de dioxyde de carbone
DE102024114508A1 (de) * 2024-05-23 2025-11-27 Elke Hildegard Münch Vorrichtung zur Kühlung von sehr heißen Gasen auf Temperaturen S50° C mithilfe von temperaturoptimierten Wärmerohren und ihre Verwendung bei der Kohledioxidabscheidung

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