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WO2025009184A1 - Dispositif de concentration de gaz - Google Patents

Dispositif de concentration de gaz Download PDF

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Publication number
WO2025009184A1
WO2025009184A1 PCT/JP2023/030032 JP2023030032W WO2025009184A1 WO 2025009184 A1 WO2025009184 A1 WO 2025009184A1 JP 2023030032 W JP2023030032 W JP 2023030032W WO 2025009184 A1 WO2025009184 A1 WO 2025009184A1
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WO
WIPO (PCT)
Prior art keywords
gas
zone
regeneration
oxygen
passed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/JP2023/030032
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English (en)
Japanese (ja)
Inventor
酒井春菜
井上宏志
古木啓明
児玉昭雄
大坂侑吾
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Seibu Giken Co Ltd
Kanazawa University NUC
Original Assignee
Seibu Giken Co Ltd
Kanazawa University NUC
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Filing date
Publication date
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Publication of WO2025009184A1 publication Critical patent/WO2025009184A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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Classifications

    • 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
    • B01D53/06—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 moving adsorbents, e.g. rotating beds
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide

Definitions

  • the present invention relates to a gas concentrator that is used for oxygen-enriched combustion, etc., and uses air as a raw material to adsorb and concentrate oxygen by temperature swing adsorption.
  • Oxygen-enriched combustion is a type of combustion technology.
  • oxygen-enriched combustion in industrial furnaces is expected to have an energy-saving effect by increasing the flame temperature and reducing exhaust gas losses.
  • cryogenic separation separates oxygen by compressing and cooling the air
  • PSA method concentrates oxygen by adsorbing and removing nitrogen from the air. Both cryogenic separation and PSA methods require large amounts of electricity to compress and cool the air.
  • the cryogenic separation method can produce high-purity oxygen, it requires large equipment and is difficult to install near a furnace, for example, where air with a high oxygen concentration (hereafter referred to as "oxygen-enriched air”) is required.
  • oxygen-enriched air air with a high oxygen concentration
  • the PSA method can produce relatively high-purity oxygen and can be made compact, but because it is used under reduced pressure/high pressure, the equipment needs to be airtight, necessitating the use of expensive materials such as thick steel plates and highly airtight valves.
  • the temperature swing adsorption method (hereafter referred to as the "TSA method") operates at normal pressure, so general-purpose materials can be used, which helps keep initial costs down.
  • an oxygen concentration of around 30% is sufficient, and even if the oxygen concentration is increased beyond that, the effect remains almost the same and the energy saving effect can also be fully achieved. If the oxygen concentration is too high, the temperature inside the furnace will rise and the furnace material will not be able to withstand it.
  • Patent documents 1 and 2 have proposed an economical oxygen concentrator that uses the TSA method to continuously extract oxygen-enriched air with a high oxygen concentration, can be installed in areas of demand according to the amount of demand, and has a low unit power source for separation.
  • the methods of concentrating oxygen in the air using the TSA method include a method of adsorbing nitrogen onto an adsorbent and a method of adsorbing oxygen onto an adsorbent.
  • Zeolite, activated carbon, etc. are used as adsorbents.
  • the oxygen concentrator (adsorption/desorption treatment device) described in Patent Document 1 is manufactured by manufacturing an adsorbent using Ca-X zeolite as an adsorbent, dividing the adsorption area into two, the first adsorption area and the second adsorption area, and the area that has completed regeneration passes through the first and second adsorption areas in sequence, while the outlet gas of the first adsorption area is circulated to the inlet side of the first adsorption area via a cooling device, while the gas that has passed through the second adsorption area is merged into this circulation system, and furthermore, a portion of the circulating gas is recovered from an arbitrary position in this circulation system to obtain oxygen-enriched gas, and in an experimental example, the oxygen concentration in the oxygen-enriched gas is said to be 30%.
  • nitrogen-adsorbing zeolites such as Li-LSX and Ca-A are used as adsorbents and have been put to practical use.
  • Carbon molecular sieve (hereafter referred to as "CMS") is a speed-separation type adsorbent that adsorbs both oxygen and nitrogen, but has the characteristic that the difference in adsorption speed between oxygen and nitrogen is very large, so by utilizing this difference in adsorption speed between oxygen and nitrogen, oxygen and nitrogen can be separated.
  • CMS is also used in the PSA method, but in the TSA method, oxygen-enriched air can be supplied by temperature swinging a honeycomb rotor carrying CMS.
  • CMS has a small oxygen adsorption capacity, it is more efficient than the method of obtaining oxygen-enriched air by adsorbing and removing nitrogen, which accounts for about 80% of the feed air, and the amount of adsorbent required can be reduced.
  • the adsorption selectivity of CMS for oxygen can be increased and desorption can be performed successfully, high concentration is also possible.
  • the oxygen concentrator (adsorption device) disclosed in Patent Document 2 indicates that it is desirable to use CMS as the adsorbent for the adsorption rotor, and in Figure 1, the adsorption rotor 1 is arranged across the air path 2 and the regeneration path 3, and a common fan 5 is provided upstream of the air path 2 and the regeneration path 3 via flow control valves 4 and 13, respectively, so that air is introduced into the adsorption rotor 1 in parallel flows. In the regeneration path 3, heated air e at 100°C or higher is passed through the adsorption rotor 1 to regenerate the adsorption rotor 1.
  • the inventors conducted an experiment using an adsorption rotor carrying CMS, with a treatment (adsorption) zone: regeneration zone ratio of 1:1, one-pass regeneration (without circulation), and countercurrent flow as described in Patent Document 2. It was found that the oxygen concentration in the oxygen-enriched air at the regeneration outlet was almost the same as that of the feed air, and the oxygen concentration performance was very low (Comparative Example 1 described below). This is because the adsorbent moves to the treatment zone while still in an elevated temperature after leaving the regeneration zone, so the adsorption capacity of the adsorbent is low and the amount of oxygen adsorbed is extremely small.
  • the main objective of the present invention is to provide a gas concentrator that can utilize the adsorption capacity of the adsorbent with high efficiency and continuously supply the desired enriched gas with a high gas concentration.
  • the present invention divides an adsorption rotor equipped with an adsorbent that preferentially adsorbs oxygen over nitrogen into at least a treatment zone, a regeneration zone, and a purge zone, which rotate in that order; raw air is passed through the treatment zone to adsorb oxygen into the adsorbent, the air that has passed through the treatment zone is sent to a supply destination or released into the atmosphere, heated air is passed through the regeneration zone to desorb the oxygen adsorbed into the adsorbent, a portion of the air that has passed through the regeneration zone is extracted as oxygen-enriched air, and the remainder is returned to the inlet side of the regeneration zone for regeneration circulation; and air is passed through the purge zone to purge the oxygen-enriched air remaining in the adsorption rotor.
  • the running cost for oxygen concentration can be significantly reduced.
  • a power consumption rate of 0.11 kWh/Nm 3 -25% O 2 (2.2 yen/Nm 3 -25% O 2 ) is required as the power for compressing the raw air or reducing the pressure for regenerating the adsorbent.
  • a power consumption rate of 0.10 kWh/Nm 3 -25% O 2 (2.1 yen/Nm 3 -25% O 2 ) is required as the power for the blower.
  • the power consumption rate can be reduced to 0.04 kWh/Nm 3 -25% O 2 (0.8 yen/Nm 3 -25% O 2 ), which is less than half that of the PSA method, by increasing the cell size of the honeycomb to reduce the size of the blower and further increasing the adsorption capacity of the CMS.
  • FIG. 1 is a diagram showing an example of the configuration of a gas concentrating apparatus according to the present invention.
  • FIG. 2 is a flow diagram of the gas concentrating apparatus according to the first embodiment of the present invention.
  • FIG. 3 is a flow diagram of a gas concentrating apparatus according to a second embodiment of the present invention.
  • FIG. 4 is a diagram showing the influence of the moisture concentration in the gas concentrating device according to the second embodiment of the present invention.
  • a CMS suitable for TSA operation of an adsorption rotor is used as an adsorbent that preferentially adsorbs a first gas over a second gas.
  • a gas with a high concentration of the first gas is referred to as a "first gas enriched gas.”
  • the first gas will be described as oxygen and the second gas as nitrogen.
  • CMS can precisely control the pores formed in the carbon body to sift (separate) gases with slightly different molecular diameters.
  • the CMS used in the present invention is designed to match the speed separation of oxygen and nitrogen to the rotor rotation and temperature.
  • FIG. 1 shows an example of the configuration of the gas concentrator of the present invention.
  • an adsorption rotor 1 equipped with an adsorbent that preferentially adsorbs oxygen over nitrogen is divided into at least a processing zone 2, a regeneration zone 3, and a purge zone 4, which rotate in this order; raw gas (e.g., air) is passed through the processing zone 2 to adsorb oxygen to the adsorbent; the gas that has passed through the processing zone 2 is sent to a supply destination or released to the atmosphere; heated gas that has passed through a regeneration heater 5 is passed through the regeneration zone 3 to desorb the oxygen adsorbed to the adsorbent; a portion of the gas that has passed through the regeneration zone 3 is taken out and recovered as oxygen-enriched gas; the remainder is returned to the inlet of the regeneration heater 5 (the inlet side of the regeneration zone 3) for regeneration circulation; and gas is passed through the purge zone 4 to purge the oxygen-enriched gas remaining in the adsorption rotor 1.
  • raw gas e
  • the adsorption rotor 1 is made by corrugating inorganic and/or non-flammable sheets such as ceramic fiber paper or glass fiber paper, metal sheets, plastic sheets, heat-resistant fiber nonwoven fabric, etc., and then laminating them into a block shape or winding them into a cylindrical (rotor) shape.
  • the cross section of the adsorption rotor 1 is honeycomb-shaped, and is not limited to corrugations like the cross section of cardboard, but can be any shape such as a triangle, trapezoid, or hexagon, as long as it does not cause any problems in allowing gas to pass through.
  • the honeycomb adsorption rotor has a wide contact area, low pressure loss, and is lightweight yet strong, so it can be easily made large.
  • Either method may be used: a method of corrugating paper containing a powdered or fibrous adsorbent or a sheet coated with a powdered adsorbent, laminating or winding it to form a honeycomb, or a method of corrugating a base sheet not containing an adsorbent, laminating or winding it to form a honeycomb, and then immersing it in a slurry of a mixture of adsorbent powder and a binder, and drying it.
  • CMS Since CMS has a small oxygen adsorption capacity, it is desirable to increase the loading rate on the adsorption rotor as much as possible, and a loading amount of 50 to 500 kg/ m3 is preferable. If the loading rate is low, the adsorption amount is small and the adsorption performance is low. On the other hand, if the loading rate is too high, the pressure loss becomes excessive, gas flowability deteriorates, and adsorption performance decreases. Therefore, in order to maximize the adsorption performance of CMS, the honeycomb cell size and loading amount are optimized.
  • raw gas e.g. air
  • oxygen is adsorbed by utilizing the difference in adsorption speed between oxygen and nitrogen in the CMS.
  • gas is passed through processing zone 2 only for the time that oxygen can be adsorbed.
  • the rotor rotation speed and processing air volume are optimized.
  • the adsorption capacity of oxygen and nitrogen also changes depending on the temperature of the CMS, and the processing air volume also serves as cooling, so the processing air volume and rotor rotation speed are adjusted to be optimal.
  • regeneration zone 3 heated gas that has passed through regeneration heater 5 is passed through adsorption rotor 1 carrying CMS to swing the temperature, which causes the adsorbed oxygen to be desorbed by heat and generate oxygen-enriched gas. Furthermore, the gas that has passed through regeneration zone 3 is returned to the inlet of regeneration heater 5 (the inlet side of regeneration zone 3) and circulated for regeneration, increasing the oxygen concentration.
  • purge zone 4 a purge zone wall is created between treatment zone 2 and regeneration zone 3 to prevent gas from the treatment side from leaking between zones or being carried over by the rotation of the adsorption rotor 1 into the regeneration side. This prevents the oxygen concentration in the regeneration circulation from being diluted. Gas is also passed through the purge zone to purge the oxygen-enriched gas remaining in the adsorption rotor. If necessary, the gas introduced into the purge zone is heated to desorb oxygen that was not desorbed in the regeneration zone and remains in the adsorbent. Alternatively, gas is passed through purge zone 4 to cool the adsorption rotor 1. Air, a portion of the gas that has passed through treatment zone 2 or before entering treatment zone 2, purge circulation gas, a portion of the regeneration circulation gas, etc. are introduced into purge zone 4.
  • Example 1 two-stage regeneration flow of the gas concentrating apparatus of the present invention with reference to the flow diagram of FIG. 2.
  • an adsorption rotor 1 was manufactured with a honeycomb cell size of 200 cells/ inch2 , a loading rate of 60% (loading amount of 250 kg/ m3 ), a diameter of ⁇ 200 mm, and a height of H400 mm.
  • the treatment zone was divided into three zones, a first treatment zone 21, a second treatment zone 22, and a third treatment zone 23.
  • the regeneration zone was also divided into two zones, a first regeneration zone 31 and a second regeneration zone 32.
  • the treatment zone or regeneration zone is divided into a plurality of zones, it is written as "first, second, ".
  • the angles of each zone were the same, and the ratio of treatment zone: regeneration zone: purge zone was 3:2:1.
  • the adsorption rotor 1 is rotated by a geared motor (not shown) or the like to pass through the first treatment zone 21, the second treatment zone 22, the third treatment zone 23, the first regeneration zone 31, the second regeneration zone 32, and the purge zone 4 in that order.
  • the raw gas that has passed through the blower 6 is branched and introduced into the first processing zone 21, the second processing zone 22, and the third processing zone 23, respectively.
  • the gas that has passed through each processing zone is joined and sent to the supply destination by the blower 7, or released into the atmosphere.
  • the gas is made to flow at a high surface wind speed to quickly and reliably cool the adsorption rotor 1 and ensure the adsorption time of oxygen in the second processing zone 22 and the third processing zone 23.
  • the surface wind speed of the gas to be flowed into the first processing zone 21 is made to be higher than the maximum surface wind speed among the surface wind speeds of the other zones (the second processing zone 22, the third processing zone 23, the first regeneration zone 31, the second regeneration zone 32, and the purge zone 4). However, if it exceeds 6 m/s, the adsorption rotor is sufficiently cooled, the oxygen-enriched gas concentration in the regeneration circulation path reaches a plateau, and the power of the blower is also increased, so 6 m/s is set as the upper limit.
  • a cooler may be provided on the inlet side of the processing zone to lower the temperature of the raw material gas.
  • processing side blowers (blowers 6 and 7) are provided on the inlet side and outlet side, respectively, only one may be provided on either side.
  • the gas that has passed through the processing zone has a relatively high nitrogen concentration (nitrogen-enriched gas), so it may be supplied to a destination for use as needed.
  • gas heated by a regeneration heater 51 is introduced into the first regeneration zone 31, where the oxygen adsorbed by the adsorbent is desorbed to increase the oxygen concentration.
  • the gas that has passed through the first regeneration zone 31 is introduced into the second regeneration zone 32 via a regeneration heater 52 by a blower 8.
  • oxygen is desorbed, and the oxygen concentration is further increased.
  • the gas that has passed through the second regeneration zone 32 is again passed through the regeneration heater 51 by a blower and introduced into the first regeneration zone 31.
  • the oxygen-enriched gas is regenerated and circulated in two stages, passing through the first regeneration zone 31 and the second regeneration zone 32, and the oxygen is concentrated.
  • the gas with an increased oxygen concentration that has passed through the second regeneration zone 32 is taken out as oxygen-enriched gas.
  • purge zone 4 gas heated by heater 10 is passed to purge the oxygen-enriched gas remaining in the honeycomb voids of the adsorption rotor 1 and to desorb the oxygen remaining in the pores of the adsorbent that was not desorbed in the regeneration zone.
  • the gas leaving purge zone 4 is introduced again into purge zone 10 by blower 11 and circulated. By circulating through purge zone 4 alone, a loop wall of the purge zone is created between the treatment zone and the regeneration zone, preventing dilution of the oxygen concentration of the oxygen-enriched gas in the regeneration circuit.
  • the gases introduced into all zones, the treatment zone, regeneration zone, and purge zone are parallel flow, introduced in the same direction.
  • parallel flow the positive pressure difference between the zones is small, reducing the amount of leakage and enabling the oxygen concentration of the oxygen-enriched gas to be kept high.
  • the oxygen concentration test was performed with a treatment inlet temperature of 22°C, a regeneration inlet temperature of 120°C, a purge inlet temperature of 100°C, and dehumidified air with a dew point of -30°C or less as the raw gas, with a surface wind speed of 5 m/s in the first treatment zone 21 and 1.5 m/s in the other zones (second treatment zone 22, third treatment zone 23, first regeneration zone 31, second regeneration zone 32, purge zone 4).
  • the rotation speed was 15 rph.
  • the oxygen concentration in the oxygen-enriched gas was 24.9% (oxygen concentration in the raw gas was 20.9%), and the oxygen concentration in the purge circulation path was 22.0%.
  • the second embodiment parallel regeneration flow of the gas concentration device of the present invention will be described with reference to the flow diagram of FIG. 3. Explanations of parts that overlap with the first embodiment will be omitted.
  • the flow of the first embodiment is simplified, and the regeneration circulation gas is branched and introduced in parallel to the first regeneration zone 31 and the second regeneration zone 32. That is, a part of the regeneration circulation gas is heated by the regeneration heater 51 and introduced into the first regeneration zone 31, and the rest of the regeneration circulation gas is heated by the regeneration heater 52 and introduced into the second regeneration zone 32.
  • the gas that has passed through each regeneration zone is merged and circulated again to the inlet side of the regeneration zone.
  • the number of blowers on the regeneration outlet side is two (blowers 8 and 9) in the first embodiment, but only one (blower 12) is required in the second embodiment.
  • the other configurations are the same as those in the first embodiment.
  • the regeneration heaters 51 and 52 are provided at the inlet side of each of the first regeneration zone 31 and the second regeneration zone 32, it is also possible to combine the regeneration heaters into one and branch the gas that has passed through the regeneration heater and introduce it into each regeneration zone. The gas with an increased oxygen concentration that circulates through the regeneration zone is extracted and recovered as oxygen-enriched gas.
  • Example 2 In the flow of this Example 2, an oxygen concentration test was conducted under the same conditions as in Example 1. As a result, the oxygen concentration in the oxygen-enriched gas was 24.9% (oxygen concentration in the raw gas: 20.9%), and the oxygen concentration in the purge circulation path was 22.1%. It was found that the flows of Example 1 and Example 2 have equivalent performance when the gas input flow rate is the same, and there is no problem even if the flow is simplified.
  • FIG. 4(a) shows the change over time of the dew point in the oxygen-enriched gas in the regeneration circulation path
  • FIG. 4(b) shows the change over time of the oxygen concentration in the oxygen-enriched gas in the regeneration circulation path.
  • the processing side is a one-pass, but some or all of the gas that has passed through the processing zone may be returned to the inlet side of the processing zone and circulated.
  • the purge path is a circulation path, but it may be a one-pass, and a heater may not be provided on the purge inlet side (in this case, the oxygen concentration in the oxygen-enriched gas was 24.4% (oxygen concentration in the raw gas was 20.9%), and the oxygen concentration in the purge circulation path was 20.8%).
  • An air volume adjustment device such as a damper that takes in outside air into the regeneration circulation path and the purge circulation path may be provided. Furthermore, in this embodiment, parallel flow is used in all zones, but this is not limited to this, and counterflow is expected to improve performance by improving the heat exchange rate, so some zones may be counterflow as appropriate.
  • the adsorption rotor is preferably a honeycomb adsorption rotor in which the adsorbent is supported on a honeycomb, but it may also be an adsorption rotor composed of an adsorption tower filled with bead-shaped or pellet-shaped adsorbent.
  • the adsorbent may be formed into a cylindrical shape and gas may be circulated in the radial direction.
  • CMS is used as the adsorbent, but any adsorbent that can separate nitrogen and oxygen based on the difference in adsorption speed like CMS or that preferentially adsorbs oxygen over nitrogen may also be used.
  • the heated gas introduced into the regeneration zone is not limited to a regeneration heater, and if heated gas that has been heat exchanged with the combustion exhaust gas is used, running costs can be reduced.
  • Comparative Example 2 Next, a test was performed with regeneration circulation under the same conditions as in Comparative Example 1.
  • the oxygen concentration at the regeneration inlet was 20.9%, while the oxygen concentration at the regeneration outlet was 21.7%. This shows that the oxygen concentration does not increase with one-pass regeneration, and that regeneration circulation is necessary for oxygen concentration. However, the increase was only 0.8 points, and optimization of the flow is necessary to further increase the oxygen concentration.
  • Example 1 a honeycomb adsorption rotor with 200 cells/ inch2 was used, but by reducing the number of cells to, for example, 50 cells/ inch2 and setting the loading amount to 250 kg/ m3 as in this example, the pressure loss can be reduced by up to 75% while maintaining the oxygen concentration performance, and the blower size can be reduced. Since the main energy consumed in the oxygen-enriched TSA method is the electricity required for blowing air, the operating costs can be significantly reduced. In the oxygen-enriched PSA method, an electric power consumption rate of 0.11 kWh/ Nm3 -25% O2 (2.2 yen/ Nm3 -25% O2 ) is required as the pressure reduction power for compressing the feed air or regenerating the adsorbent.
  • the oxygen-enriched TSA method of the present invention when a honeycomb adsorption rotor with 200 cells/inch 2 is used, a power consumption rate of 0.10 kWh/Nm 3 -25% O 2 (2.1 yen/Nm 3 -25% O 2 ) is required as the power source for the blower, and the operating cost is equivalent to that of the oxygen-enriched PSA method. Furthermore, when the number of cells is reduced to, for example, 50 cells/inch 2 , the power consumption rate can be reduced to 0.08 kWh/Nm 3 -25% O 2 (1.6 yen/Nm 3 -25% O 2 ) while maintaining the oxygen concentration performance.
  • the adsorption capacity of CMS can be doubled, and in this case, it is estimated that the power consumption rate can be reduced to 0.04 kWh/Nm 3 -25% O 2 (0.8 yen/Nm 3 -25% O 2 ), which is less than half that of the oxygen-enriched PSA method.
  • the first gas is oxygen and the second gas is nitrogen, but this is not limited thereto.
  • the first gas and the second gas may be changed as appropriate depending on the type of gas, for example, the first gas may be carbon dioxide and the second gas may be methane.
  • the gas concentrator of the present invention is expected to be applied to industrial furnaces. It is compatible with various combustion equipment that is sensitive to pressure loss, and it is relatively easy to scale up, making it easy to introduce, and further energy-saving effects can be expected.
  • Oxygen-enriched combustion which increases the oxygen concentration to around 25-30%, is excellent for energy saving, such as reducing fuel consumption by about 10-30%, and contributes to reducing fuel consumption in industrial furnaces, etc.
  • SOFCs solid oxide fuel cells
  • the present invention is the speed separation of oxygen and nitrogen, but as long as the gas can be separated at different adsorption speeds using CMS, it is also possible to separate methane and carbon dioxide, hydrogen and other substances, propane gas and propylene, etc., and the flow of the present invention can be used to separate components from several types of mixed gases.
  • Adsorption rotor 2 Treatment zone 3 Regeneration zone 4 Purge zone 5 Regeneration heater 6, 7, 8, 9, 11, 12 Blower 10 Heater 21 First treatment zone 22 Second treatment zone 23 Third treatment zone 31 First regeneration zone 32 Second regeneration zone 51, 52 Regeneration heater

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  • Chemical Kinetics & Catalysis (AREA)
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  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)

Abstract

Le problème décrit par la présente invention est de fournir un dispositif de concentration de gaz capable de fournir en continu de l'air enrichi en oxygène ayant une concentration élevée en oxygène en permettant à un adsorbant de démontrer une capacité d'adsorption avec une efficacité élevée. Un rotor d'adsorption comprenant un adsorbant qui adsorbe préférentiellement de l'oxygène sur de l'azote est divisé en au moins une zone de traitement, une zone de régénération et une zone de purge et est configuré de telle sorte que les zones tournent en séquence dans l'ordre indiqué. De l'air de matière première est passé à travers la zone de traitement de telle sorte que l'oxygène est adsorbé sur l'adsorbant. L'air qui a traversé la zone de traitement est envoyé à une destination d'alimentation ou est évacué vers l'atmosphère. L'air chauffé qui a traversé un dispositif de chauffage de régénération est passé à travers la zone de régénération pour désorber l'oxygène adsorbé sur l'adsorbant, et une partie de l'air qui a traversé la zone de régénération est prise en tant qu'air enrichi en oxygène. Le reste est renvoyé vers le côté d'entrée du dispositif de chauffage de régénération pour la circulation de régénération. De l'air est passé à travers la zone de purge pour purger l'air enrichi en oxygène restant dans le rotor d'adsorption.
PCT/JP2023/030032 2023-07-03 2023-08-21 Dispositif de concentration de gaz Pending WO2025009184A1 (fr)

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JP2023-108986 2023-07-03
JP2023108986A JP2025007529A (ja) 2023-07-03 2023-07-03 ガス濃縮装置

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Citations (9)

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