WO2014185445A1 - 二酸化炭素濃縮装置及び二酸化炭素供給方法 - Google Patents
二酸化炭素濃縮装置及び二酸化炭素供給方法 Download PDFInfo
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- WO2014185445A1 WO2014185445A1 PCT/JP2014/062809 JP2014062809W WO2014185445A1 WO 2014185445 A1 WO2014185445 A1 WO 2014185445A1 JP 2014062809 W JP2014062809 W JP 2014062809W WO 2014185445 A1 WO2014185445 A1 WO 2014185445A1
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- 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
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- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01G—HORTICULTURE; CULTIVATION OF VEGETABLES, FLOWERS, RICE, FRUIT, VINES, HOPS OR SEAWEED; FORESTRY; WATERING
- A01G7/00—Botany in general
- A01G7/02—Treatment of plants with carbon dioxide
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- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01G—HORTICULTURE; CULTIVATION OF VEGETABLES, FLOWERS, RICE, FRUIT, VINES, HOPS OR SEAWEED; FORESTRY; WATERING
- A01G9/00—Cultivation in receptacles, forcing-frames or greenhouses; Edging for beds, lawn or the like
- A01G9/18—Greenhouses for treating plants with carbon dioxide or the like
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- 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
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- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
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- B01J20/16—Alumino-silicates
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- B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
- B01J20/28069—Pore volume, e.g. total pore volume, mesopore volume, micropore volume
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- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
- B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
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- 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
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- 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
- B01J20/3491—Regenerating or reactivating by pressure treatment
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- 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
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- 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
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/20—Reduction of greenhouse gas [GHG] emissions in agriculture, e.g. CO2
Definitions
- the present invention relates to a carbon dioxide concentrator and a carbon dioxide supply method using the same.
- Concentration of carbon dioxide generally increasing the concentration of carbon dioxide in the air, is beneficial in agriculture, horticulture, etc., for growing plants that use carbon dioxide for photosynthesis.
- the apparatus of the present invention is not limited to this and can be used for other purposes.
- Cultivated crops such as strawberries, melons and tomatoes are generally cultivated in facilities such as greenhouses from the viewpoint of temperature control. Since the greenhouse is a closed space, carbon dioxide in the greenhouse is consumed by photosynthesis during the daytime when sunlight is irradiated during the day, and as a result, there is a problem that the carbon dioxide concentration decreases. Therefore, it is known that the growth of plants is promoted by increasing the carbon dioxide concentration during the time when photosynthesis by sunlight during the day is active. Therefore, in greenhouse cultivation, the growth of the cultivated crop is increased, the yield is increased, and the quality is improved by setting the carbon dioxide concentration in the greenhouse to 1000 ppm or more.
- Patent Documents 1 and 2 As a method for supplying high-concentration carbon dioxide to a horticultural facility, there is conventionally known a method of using combustion exhaust gas containing a large amount of carbon dioxide generated from a combustion apparatus for atmosphere adjustment (Patent Documents 1 and 2). For example, when supplying carbon dioxide during the day, carbon dioxide is supplied by burning kerosene and LP gas using a combustion device that burns completely and does not generate carbon monoxide. In addition, there is a method to increase the carbon dioxide concentration in the house by introducing a part of the exhaust gas from the heater used for nighttime heating into the house. However, the carbon dioxide concentration decreases rapidly when photosynthesis starts, and the afternoon It seems to be lacking. Furthermore, when there are many harmful substances in the exhaust gas such as heavy oil, it is necessary to introduce carbon dioxide into the house after removing harmful substances such as sulfur oxides, nitrogen oxides and carbon monoxide.
- Patent Document 4 a method of concentrating carbon dioxide in the atmosphere has been developed. It is said that carbon dioxide in the atmosphere is concentrated by a pressure swing type adsorption device and carbon dioxide with a concentration of 500 to 2000 ppm is supplied into the house, but there is no problem if it is a small house within 10 m 3 for experiments. In the large house, there is a problem that the concentration of carbon dioxide hardly rises unless a large carbon dioxide concentrator is used and the supply amount of concentrated carbon dioxide is increased. Large-scale carbon dioxide concentrators are expensive to use because they are expensive.
- the present invention has been made in view of the above circumstances, developed an adsorbent excellent in carbon dioxide adsorption, developed a compact device for concentrating carbon dioxide in the air by using this, and relied on a combustion system. Without the need to supply concentrated carbon dioxide.
- the present inventors have completed the carbon dioxide concentration device of the present invention and a carbon dioxide supply method using the same, and the feature of the device is that the adsorbent is in the device.
- the ferrierite is characterized in that the pore volume with a pore diameter of 0.01 to 1 ⁇ m is increased to 0.1 mL / g or more by an alkali treatment.
- carbon dioxide concentrated by the apparatus of claim 1 is supplied for plant growth.
- Ferrierite is a kind of zeolite and has a FER structure code at the International Zeolite Society. Ferrierite may be either natural or synthetic, but in order to fill the adsorption tower of the pressure swing type concentrator, a granular or cylindrical shape with a diameter of 0.5 mm to 5 mm is preferable, and 0.5 mm to 2 mm is more preferable. . If the size is 0.5 mm or less, the pressure loss of the adsorption tower is too large, and the efficiency of the air pump is poor. If it is 5 mm or more, the diffusion of the gas in the particles is slow and the inside of the particles is not utilized.
- this ferrierite adsorbent has a pore volume in the range of 0.01 ⁇ m to 1 ⁇ m in diameter of 0.1 mL / g or more when measured with a mercury intrusion pore distribution measuring device. Since natural ferrierite is produced as a hard rock, it has a dense structure and a small number of pores having a diameter of 0.01 ⁇ m or more. On the other hand, in order to increase the rate of gas adsorption and desorption, it is better that there are many pores having a diameter of 0.01 ⁇ m or more.
- the alkaline solution include an aqueous sodium hydroxide solution, an aqueous potassium hydroxide solution, an aqueous sodium carbonate solution, and an aqueous potassium carbonate solution.
- Sodium hydroxide is preferred from the viewpoint of alkalinity and cost.
- the concentration of the aqueous sodium hydroxide solution is preferably 1.5 mol / L or more.
- the adsorbent packed in the adsorption tower may not be all the ferrierite described above. That is, you may use what added the mordenite or other zeolite, or what replaced a part thereof. Of course, as a whole, the above ferrierite contains 50% or more by weight.
- the pressure swing type concentrator is already known and can be continuously concentrated by alternately using at least two adsorption towers. In the present invention, this need not be special and may be general. Briefly, two adsorbing towers are filled with an adsorbent, air containing carbon dioxide is supplied to the adsorbing towers, and the high pressure adsorption process and the low pressure recovery process are alternately repeated in the respective adsorption towers. It generates concentrated air.
- the operation cycle of the carbon dioxide concentrator is within the range of 3000 to 15000 ppm by adopting, for example, adsorption, pressure equalization, reflux, regeneration process and the like.
- the predetermined carbon dioxide-enriched gas can be efficiently taken out.
- the adsorption pressure in the adsorption step is usually 2.0 to 9.9 kgf / cm 2 G, preferably 2 to 5 kgf / cm 2 G, and most preferably 2 to 3 kgf / cm 2 G.
- the regeneration pressure in the recovery step is usually 1 kPa or less, or 0.5 kPa or less, and most preferably 0.2 kPa or less.
- the concentration of the concentrated carbon dioxide in the present invention exerts its effect in the range of 500 ppm to 15000 ppm, preferably 1000 ppm to 15000 ppm, and most preferably 3000 ppm to 15000 ppm. If the carbon dioxide concentration exceeds 15000 ppm, the required power of the carbon dioxide concentration pressure swing device (hereinafter abbreviated as PSA device), the efficiency of gas yield, etc., are lowered, and the economic efficiency is lowered. Further, when the carbon dioxide concentration is less than 500 ppm, the meaning and effect of concentration are generally small.
- An application for supplying or using carbon dioxide concentrated by the apparatus of the present invention is for agriculture.
- the high-concentration carbon dioxide produced by the carbon dioxide concentrator is usually supplied from a gas flow control valve. At this time, it is preferable to supply carbon dioxide to the leaf portion of each plant body by a tube.
- carbon dioxide is concentrated from the atmosphere, it is difficult to increase the carbon dioxide concentration in the entire plant growing room because the production amount of high-concentration carbon dioxide-containing gas is small. For this reason, it is preferable to supply carbon dioxide locally to the leaf portion where carbon dioxide is required by photosynthesis. Of course, the supply amount of high-concentration carbon dioxide may be increased and introduced as a whole.
- the carbon dioxide concentrator of the present invention can supply high-concentration carbon dioxide directly to various facilities by using ferrierite with increased pores as an adsorbent. This is particularly effective for agriculture. For example, the sugar content of strawberries has been greatly improved.
- FIG. 1 is a schematic view showing an example of a carbon dioxide concentrator according to the present invention.
- the raw material air is pressurized by the blower (1) and flows through the air dryer (2), the inlet pipe (21), the on-off valve (10) (or (10A)), and the adsorption tower (3) (or (3A)).
- the pressurized air is supplied to the adsorption tower (3), carbon dioxide is adsorbed by the adsorbent in the adsorption tower (3), and other gases are opened and closed valves (12), exhaust pipes (22, 23), It passes through the on-off valve (14) and is discharged out of the system.
- the time required for the adsorption step is 300 to 900 seconds, preferably 300 to 600 seconds.
- the adsorption process is terminated, and the on-off valves (10), (12), and (14) are closed.
- a pressure equalizing step following the adsorption step.
- the on-off valves (11 or 11A) and (15) are opened, and high pressure air is discharged from the adsorption tower (3) using the lines (25) and (27).
- a recovery process is performed.
- the time required for this recovery step is 300 to 900 seconds, preferably 300 to 600 seconds, similar to the time required for the adsorption step.
- the on-off valves (11) and (16) are opened, and the adsorption tower (3) is depressurized by the vacuum pump (4), so that the carbon dioxide adsorbed on the adsorbent in the adsorption tower (3) is removed.
- the desorption is collected and supplied to the reservoir tank (5).
- the product carbon dioxide enriched gas in the reservoir tank (5) is taken out by the gas flow control valve (7) through the carbon dioxide enriched gas supply pipe (6).
- the purge process may be performed before or after the pressure equalization process.
- the product carbon dioxide enriched gas in the reservoir tank (5) flows from the bottom of the adsorption tower (3) to the top and is discharged out of the adsorption tower (3), or flows from the top to the bottom of the adsorption tower. (3) Discharge outside.
- the on-off valves (11), (12), (14), and (17) are opened, and the recovered carbon dioxide-concentrated gas in the reservoir tank (5) is circulated from the return line (26) to the adsorption tower (3).
- (14) may be opened and discharged out of the system, or the on-off valves (11), (17), (12), and (12A) may be opened and supplied to the adsorption tower (3A). Thereby, the purity of the carbon dioxide concentrated gas to be recovered can be improved.
- a reflux process may be inserted.
- the carbon dioxide-concentrated gas recovered in the reservoir tank (5) is caused to flow from the top of the adsorption tower (3) to the bottom through the line (24) and the valve (13) to desorb the adsorbed carbon dioxide.
- the product carbon dioxide-enriched gas is also recovered in the reservoir tank (5) through the on-off valves (11) and (16) and the vacuum pump (4).
- Adsorbent example 2 The same treatment was performed as in Adsorbent Example 1 except that the added sodium hydroxide was changed to 0.225 mol. As a result, the pore volume in the pore diameter range of 0.01 to 1.0 ⁇ m was 0.1086 mL / g.
- Adsorbent example 3 The same treatment was performed except that 0.15 mol of potassium hydroxide was added instead of sodium hydroxide in Example 1 of the adsorbent. As a result, the pore volume in the pore diameter range of 0.01 to 1.0 ⁇ m was 0.1042 mL / g.
- Adsorbent example 4 The same treatment was performed except that 0.225 mol of potassium hydroxide was added instead of sodium hydroxide in the adsorbent example 1. As a result, the pore volume in the pore diameter range of 0.01 to 1.0 ⁇ m was 0.1055 mL / g.
- Comparative adsorbent 1 As a result of measuring the pore volume of an untreated natural ferrierite in the pore diameter range of 0.01 to 1.0 ⁇ m, it was 0.0654 mL / g.
- Comparative adsorbent 2 The same treatment as in Adsorbent Example 1 was performed except that the added sodium hydroxide was changed to 0.075 mol. As a result, the pore volume in the pore diameter range of 0.01 to 1.0 ⁇ m was 0.0831 mL / g.
- Comparative adsorbent 3 The same treatment was performed except that 0.225 mol of sodium carbonate was added instead of sodium hydroxide in the adsorbent example 1. As a result, the pore volume in the pore diameter range of 0.01 to 1.0 ⁇ m was 0.0892 mL / g.
- Example 1 A carbon dioxide adsorption device similar to that shown in FIG. 1 was manufactured, and 1 L of the ferrierite of the adsorbent example 1 was packed in the adsorption tower. An adsorption pressure of 2 kgf / cm 2 G, a desorption pressure of 300 Pa, an adsorption / desorption cycle of 10 minutes, and a purge process from the reservoir tank to the adsorption tower were performed. The carbon dioxide concentration at the carbon dioxide supply port was about 10,000 ppm. At this time, the concentration ratio from the carbon dioxide concentration in the atmosphere was about 27 times.
- Example 2 The same procedure as in Example 1 was performed except that 1 L of the ferrierite of the adsorbent example 2 was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 9,500 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 25.7 times.
- Example 3 The same procedure as in Example 1 was performed except that 1 L of the ferrierite of the adsorbent example 3 was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 9,800 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 26.5 times.
- Example 4 The same operation as in Example 1 was performed except that 1 L of the ferrierite of the adsorbent example 4 was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 9,500 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 25.7 times.
- Comparative Example 1 The same operation as in Example 1 was performed except that 1 L of untreated natural ferrierite (comparative adsorbent 1) was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 4,000 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 10.8 times.
- Comparative Example 2 The same operation as in Example 1 was performed except that 1 L of the comparative adsorbent 2 was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 5,000 ppm. At this time, the concentration ratio from the carbon dioxide concentration in the atmosphere was about 13.5 times.
- Comparative Example 3 The same operation as in Example 1 was performed except that 1 L of the comparative adsorbent 3 was packed in the adsorption tower.
- the carbon dioxide concentration at the carbon dioxide supply port was about 6,800 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 18.3 times.
- Example 5 In Example 1, the same operation was performed except that 0.5 L of the ferrierite of Adsorbent Example 1 and 0.5 L of natural mordenite were filled.
- the carbon dioxide concentration at the carbon dioxide supply port was about 8,000 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 21.6 times.
- Comparative Example 4 The same operation as in Example 1 was performed except that 0.3 L of the ferrierite of Adsorbent Example 1 and 0.7 L of natural mordenite were filled.
- the carbon dioxide concentration at the carbon dioxide supply port was about 6,200 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 16.8 times.
- Comparative Example 5 The same operation was performed in Example 1, except that 0.4 L of the ferrierite of Adsorbent Example 1 and 0.6 L of natural mordenite were filled.
- the carbon dioxide concentration at the carbon dioxide supply port was about 7,000 ppm.
- the concentration ratio from the carbon dioxide concentration in the atmosphere at this time was about 18.9 times.
- Example 6 Plant Growth Test
- strawberry was cultivated by supplying carbon dioxide with a concentration of 10,000 ppm to the leaves of strawberry seedlings from 8:00 to 17:00 with a tube. Carbon dioxide around the leaves was 2,000 ppm. Cultivated from November to March while supplying carbon dioxide. The result of measuring the sugar content of the cultivated strawberry fruit was 10.2%.
- Example 7 Plant growth test By using the adsorbent of Example 1 and the operation, carbon dioxide with a concentration of 10000 ppm was supplied to the leaves of 60 strawberry seedlings through a tube from 8:00 to 17:00. A breeding test was conducted. The first flowering was 42 days after planting. The total yield of strawberries was 13.57 kg. Comparative Example 7 A strawberry growth test was conducted in the same manner except that carbon dioxide was not supplied in Example 7. The first flowering was 57 days after planting, 15 days later than when carbon dioxide was supplied. The total yield of strawberries was 10.15 kg, 35% less than when carbon dioxide was supplied.
Abstract
Description
簡単に述べると、2塔の吸着塔に吸着材を充填し、この吸着塔に二酸化炭素を含む空気を供給し、高圧吸着工程と低圧回収工程とをそれぞれの吸着塔において交互に繰り返し、二酸化炭素濃縮空気を発生するものである。
例えば、植物育成用の温室やビニールハウス、温度とは関係のない密閉空間(二酸化炭素濃度を高めるための)への濃縮二酸化炭素の導入、さらには密閉しない場所での植物への濃縮二酸化炭素の供給等である。
原料空気は、ブロア(1)により加圧されエアードライヤ(2)、流入路パイプ(21)、開閉弁(10)(または(10A))を流通し吸着塔(3)(または(3A))に供給される。
ここでは、吸着塔(3)で吸着が行われる場合について説明する。加圧空気が吸着塔(3)に供給された後、吸着塔(3)内の吸着材によって二酸化炭素は吸着され、他のガスは開閉弁(12)、排気路パイプ(22、23)、開閉弁(14)を通過し系外に排出される。吸着工程に要する時間は、300~900秒間、好ましくは300~600秒間である。該吸着材が飽和する前に吸着工程を終了し、開閉弁(10)、(12)、(14)は、閉止される。この際、吸着工程に引続き均圧工程を挿入することが望ましい。均圧工程は、開閉弁(11又は11A)、(15)を開放し、ライン(25)、(27)を使用して、吸着塔(3)から高圧空気を排出する。均圧工程が終了すると回収工程が行われる。この回収工程に要する時間は、吸着工程に要する時間と同様、300~900秒間、好ましくは300~600秒間である。この回収工程は、開閉弁(11)、(16)を開放し真空ポンプ(4)により吸着塔(3)を減圧することにより吸着塔(3)内の吸着材に吸着されていた二酸化炭素を脱着回収しリザーバータンク(5)に供給する。リザーバータンク(5)内の製品二酸化炭素濃縮ガスは、二酸化炭素濃縮ガス供給パイプ(6)を通してガス流量調節弁(7)により取り出される。
フェリエライトのアルカリ処理
島根県産天然フェリエライトを2~5mmに整粒し、10gを100gの純水に入れ、水酸化ナトリウムを0.15mol添加して、室温で1晩振とうさせた。この天然フェリエライトを純水で洗浄し、その後、120℃で乾燥した。このアルカリで処理した天然フェリエライトをカンタクローム社製の水銀圧入式細孔分布測定装置で細孔分布を測定した。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.1056mL/gであった。
吸着材例1で、添加した水酸化ナトリウムを0.225molとした以外は同様の処理をおこなった。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.1086mL/gであった。
吸着材例1で、水酸化ナトリウムの代わりに水酸化カリウムを0.15mol添加した以外は同様の処理をおこなった。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.1042mL/gであった。
吸着材例1で、水酸化ナトリウムの代わりに水酸化カリウムを0.225mol添加した以外は同様の処理をおこなった。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.1055mL/gであった。
無処理の天然フェリエライトの細孔直径0.01~1.0μmの範囲の細孔容積を測定した結果、0.0654mL/gであった。
吸着材例1で、添加した水酸化ナトリウムを0.075molとした以外は同様の処理をおこなった。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.0831mL/gであった。
吸着材例1で、水酸化ナトリウムの代わりに炭酸ナトリウムを0.225mol添加した以外は同様の処理をおこなった。その結果、細孔直径0.01~1.0μmの範囲の細孔容積が0.0892mL/gであった。
図1と同様の二酸化炭素吸着装置を製作し、吸着塔に吸着材例1のフェリエライトを1L充填した。吸着圧力2kgf/cm2G、脱着圧力300Pa、吸着・脱着サイクル10分、およびリザーバータンクから吸着塔へのパージ処理をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約10,000ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約27倍であった。
吸着塔に吸着材例2のフェリエライトを1L充填した以外は、実施例1と同様におこなった。二酸化炭素供給口の二酸化炭素濃度は、約9,500ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約25.7倍であった。
吸着塔に吸着材例3のフェリエライトを1L充填した以外は、実施例1と同様におこなった。二酸化炭素供給口の二酸化炭素濃度は、約9,800ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約26.5倍であった。
吸着塔に吸着材例4のフェリエライトを1L充填した以外は、実施例1と同様におこなった。二酸化炭素供給口の二酸化炭素濃度は、約9,500ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約25.7倍であった。
吸着塔に無処理の天然フェリエライト(比較吸着材1)を1L充填した以外は、実施例1と同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約4,000ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約10.8倍であった。
吸着塔に比較吸着材2を1L充填した以外は、実施例1と同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約5,000ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約13.5倍であった。
吸着塔に比較吸着材3を1L充填した以外は、実施例1と同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約6,800ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約18.3倍であった。
実施例1で、吸着材例1のフェリエライトを0.5Lと、天然モルデナイト0.5Lを充填した以外は、同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約8,000ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約21.6倍であった。
実施例1で、吸着材例1のフェリエライトを0.3Lと、天然モルデナイト0.7Lを充填した以外は、同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約6,200ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約16.8倍であった。
実施例1で、吸着材例1のフェリエライトを0.4Lと、天然モルデナイト0.6Lを充填した以外は、同様の操作をおこなった。二酸化炭素供給口の二酸化炭素濃度は、約7,000ppmであった。このときの大気中の二酸化炭素濃度からの濃縮倍率は、約18.9倍であった。
植物体の育成試験
実施例1の吸着材および運転操作により、濃度10000ppmの二酸化炭素をチューブでイチゴ苗の葉部分に8時から17時まで供給してイチゴを栽培した。葉の周辺の二酸化炭素は2,000ppmであった。二酸化炭素を供給しながら11月から3月まで栽培した。栽培したイチゴ果実の糖度を測定した結果は、10.2%であった。
二酸化炭素を供給せずに栽培したイチゴでは、イチゴ果実の糖度を測定した結果は、8.1%であった。
植物体の育成試験
実施例1の吸着材および運転操作により、濃度10000ppmの二酸化炭素をチューブによりイチゴ苗60株の葉の部分に8時から17時まで供給し、10月から4月までイチゴの育成試験を行った。最初の開花は、植え付け後42日目であった。また、イチゴの総収穫量は13.57kgであった。
比較例7
実施例7で二酸化炭素を供給しなかった以外は、同様にイチゴの育成試験を行った。最初の開花は、植え付け後57日目であり、二酸化炭素を供給した場合より15日遅かった。また、イチゴの総収穫量は10.15kgであり、二酸化炭素を供給した場合より35%少なかった。
以上、実施例6、7及び比較例6、7より、本発明の二酸化炭素供給装置により二酸化炭素を供給することで、イチゴの生育が良くなり、糖度の向上だけでなく収穫量も増大し、ハウス栽培での植物育成の効果が高いことが確認できた。
2 エアードライヤ
3、3A 吸着塔
4 真空ポンプ
5 リザーバータンク
6 二酸化炭素濃縮ガス供給パイプ
7 ガス流量調節弁
10、10A,11、11A、12、12A 開閉弁
13、14、15、16、17 開閉弁
21 流入路パイプ
22 排気路パイプ
23 排気路パイプ
24、25 ライン
26 リターンライン
27 ライン
Claims (3)
- 吸着材としてフェリエライトを使用する圧力スイング式濃縮装置であって、該フェリエライトは、アルカリ処理によって細孔径が0.01~1μmの細孔容量が0.1mL/g以上にしたものであることを特徴とする二酸化炭素濃縮装置。
- 大気中の二酸化炭素を20倍以上に濃縮するものである請求項1記載の二酸化炭素濃縮装置。
- 請求項1の装置により濃縮された二酸化炭素を植物育成用に供給する二酸化炭素供給方法。
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US14/890,988 US20160101383A1 (en) | 2013-05-16 | 2014-05-14 | Carbon dioxide concentration apparatus and carbon dioxide supply method |
US15/900,156 US20180169564A1 (en) | 2013-05-16 | 2018-02-20 | Apparatus for Concentrating Carbon Dioxide and a Method of Supplying Carbon Dioxide |
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