Patent Application
20190255509
The present invention relates to an adsorbent, a method for removing carbon dioxide, an apparatus for removing carbon dioxide, and a system for removing carbon dioxide.
In recent years, global warming caused by emission of greenhouse effect gases has become a global problem. Examples of greenhouse effect gases may include carbon dioxide (CO2), methane (CH4), and fluorocarbons (CFCs and the like). Among the greenhouse effect gases, the effect of carbon dioxide is the greatest, and it is demanded to construct a method for removing carbon dioxide (for example, carbon dioxide discharged from a thermal power plant, a steelworks, and the like).
In addition, it is known that carbon dioxide affects the human body. For example, drowsiness, health damage, and the like are caused when a gas containing carbon dioxide at a high concentration is sucked. In a space with a high density of people (a building, a vehicle, or the like), the concentration of carbon dioxide (hereinafter referred to as the “CO2 concentration” in some cases) in the room is likely to rise due to the exhalation of people and the CO2 concentration is adjusted by ventilation in some cases.
It is required to operate an air blowing device such as a blower in order to quickly replace the indoor air with outdoor air. In addition, it is required to operate the cooling system in the summer and to operate the heating system in the winter since the temperature and humidity of the air (outdoor air) taken in from the outside are not adjusted. For these reasons, an increase in CO2 concentration in the room is a cause of an increase in power consumption associated with air conditioning.
The decrease amount of carbon dioxide (CO2 decrease amount) in the room due to ventilation is expressed by the following equation. In the following equation, the CO2 concentration can be constantly maintained when the CO2 decrease amount on the left side is equivalent to the CO2 increase amount due to the exhalation of people.
CO
2decrease amount=(CO2 concentration in room−CO2 concentration in outdoor air)×amount of ventilation
In recent years, however, the difference between CO2 concentration in the outdoor air and CO2 concentration in the room has decreased since the CO2 concentration in the outdoor air has increased. Hence, the amount of ventilation required for adjusting the CO2 concentration has also increased. In the future, it is considered that the power consumption for the adjustment of the CO2 concentration by ventilation will increase if the CO2 concentration in the outdoor air further increases.
The problem is caused by replacement of the indoor air with outdoor air. Hence, the amount of ventilation can be decreased if carbon dioxide can be selectively removed by a method other than ventilation, and as a result, there is a possibility that the power consumption associated with air conditioning can be decreased.
In addition, since it is difficult to replace the indoor air with outdoor air in a space (space station, submarine, or the like) shielded from the outdoor air in which air exists, it is required to selectively remove carbon dioxide by a method other than ventilation.
Examples of a solution to the above problem may include a method in which carbon dioxide is removed by a chemical absorption method, a physical absorption method, a membrane separation method, an adsorption separation method, a cryogenic separation method, or the like. Examples thereof may include a method (CO2 separation recovery method) in which carbon dioxide is separated and recovered using a CO2 adsorbent (hereinafter simply referred to as the “adsorbent”). As the adsorbent, for example, zeolite is known (see, for example, Patent Literature 1 below).
Patent Literature 1: Japanese Unexamined Patent Publication No. 2000-140549
Meanwhile, there is a case in which carbon dioxide is desorbed from the adsorbent by heating the adsorbent on which carbon dioxide is adsorbed at a high temperature (for example, 100° C. to 200° C.) from the viewpoint of repeatedly separating and recovering carbon dioxide. In this case, the labor for adsorption and desorption operations can be diminished if it is possible to adsorb and desorb a great amount of carbon dioxide.
The present invention has been made in view of the above circumstances, and an object thereof is to provide an adsorbent capable of improving the desorption amount of carbon dioxide in the case of being heated at a high temperature. In addition, an object of the present invention is to provide a method for removing carbon dioxide, an apparatus for removing carbon dioxide and a system for removing carbon dioxide in which the adsorbent is used.
An adsorbent according to the present invention is an adsorbent used for removing carbon dioxide from a gas containing carbon dioxide, the adsorbent containing cerium oxide containing cerium and a metallic element (excluding cerium) having an electronegativity of 1.00 or more.
According to the adsorbent of the present invention, it is possible to improve the desorption amount of carbon dioxide in the case of heating the adsorbent at a high temperature (for example, 100° C. to 200° C.). Such an adsorbent exhibits excellent CO2 adsorptivity (carbon dioxide adsorptivity, carbon dioxide trapping ability). In addition, according to the adsorbent of the present invention, it is possible to desorb carbon dioxide from the adsorbent even in the case of heating the adsorbent at a relatively low temperature (for example, 50° C. or more and less than 100° C.).
Meanwhile, in the method using a conventional adsorbent such as zeolite, the removal efficiency of carbon dioxide tends to decrease in a case in which the CO2 concentration in the gas is low. On the other hand, according to the adsorbent of the present invention, it is possible to improve the amount of carbon dioxide adsorbed on the adsorbent in a case in which the CO2 concentration in the gas is low. According to the adsorbent as described above, it is possible to efficiently remove carbon dioxide in a case in which the CO2 concentration in the gas is low.
The electronegativity of the metallic element may be 1.00 to 1.80. It is preferable that the metallic element includes at least one kind selected from the group consisting of lanthanum, neodymium, yttrium, magnesium, zirconium, aluminum, zinc, iron and copper. It is preferable that the metallic element includes neodymium. It is preferable that the metallic element includes aluminum. It is preferable that the metallic element includes zinc.
It is preferable that a specific surface area of the adsorbent according to the present invention is more than 130 m2/g.
It is preferable that a content of the cerium oxide is 90% by mass or more based on a total mass of the adsorbent. In this case, it is possible to further improve the adsorption amount and desorption amount of carbon dioxide.
A method for removing carbon dioxide according to the present invention includes a step of bringing the adsorbent described above into contact with a gas containing carbon dioxide to adsorb carbon dioxide on the adsorbent. According to the method for removing carbon dioxide of the present invention, it is possible to improve the desorption amount of carbon dioxide and the removal efficiency of carbon dioxide.
A CO2 concentration in the gas may be 5000 ppm or less or 1000 ppm or less.
An apparatus for removing carbon dioxide according to the present invention includes the adsorbent described above. According to the apparatus for removing carbon dioxide of the present invention, it is possible to improve the removal efficiency of carbon dioxide.
A system for removing carbon dioxide according to the present invention includes the adsorbent apparatus for removing carbon dioxide described above. According to the system for removing carbon dioxide of the present invention, it is possible to improve the removal efficiency of carbon dioxide.
According to the present invention, it is possible to improve the desorption amount of carbon dioxide in the case of heating the adsorbent at a high temperature. In addition, according to the present invention, it is possible to efficiently remove carbon dioxide in a case in which the CO2 concentration in the gas is low.
In the present specification, the numerical range expressed by using “to” indicates the range including the numerical values stated before and after “to” as the minimum value and the maximum value, respectively. In a numerical range stated in a stepwise manner in the present specification, the upper limit value or lower limit value in the numerical range at a certain stage may be replaced with the upper limit value or lower limit value in the numerical range at another stage. In addition, in a numerical range stated in the present specification, the upper limit value or lower limit value in the numerical range may be replaced with the values stated in Examples.
In the present specification, the term “step” includes not only an independent step but also a step by which the intended purpose of the step can be achieved even in a case in which the step cannot be clearly distinguished from other steps. The materials exemplified in the present specification can be used singly or in combination of two or more kinds thereof unless otherwise stated. In the present specification, the content of each component in the composition means the total amount of the plurality of substances present in the composition unless otherwise stated in a case in which a plurality of substances corresponding to each component are present in the composition.
Hereinafter, embodiments for carrying out the present invention will be described in detail. However, the present invention is not limited to the following embodiments.
<Adsorbent>
The adsorbent (carbon dioxide trapping agent) according to the present embodiment contains cerium oxide and the cerium oxide contains cerium and a metallic element having an electronegativity of 1.00 or more (excluding cerium; hereinafter referred to as the “specific metallic element” in some cases). The adsorbent according to the present embodiment is used for removing (for example, recovering) carbon dioxide from a gas (a gas to be a target of treatment) containing carbon dioxide.
As a result of intensive investigations, the inventors of the present invention have found out that it is possible to improve the desorption amount of carbon dioxide in the case of heating the adsorbent at a high temperature (for example, 100° C. to 200° C.) by using an adsorbent containing cerium oxide containing cerium and a metallic element (excluding cerium) having an electronegativity of 1.00 or more.
Meanwhile, carbon dioxide adsorbed on the adsorbent is desorbed from the adsorbent when the adsorbent according to the present embodiment is heated. Here, in the adsorbent according to the present embodiment, there is a tendency that a temperature (peak temperature) providing the maximum value (maximum peak) is observed in each of a high temperature region (for example, 100° C. to 200° C.) and a low temperature region (for example, 50° C. or more and less than 100°) in the curve (horizontal axis: temperature, vertical axis: desorption amount at each temperature) representing the temperature dependency of the desorption amount when a change in the CO2 desorption amount associated with an increase in the heating temperature is observed. In a case in which such a peak temperature can be lowered, it is possible to lower the heating temperature for desorption of carbon dioxide and to improve the removal efficiency of carbon dioxide. According to the adsorbent of the present embodiment, it is possible to lower the peak temperatures in a high temperature region (for example, 100° C. to 200° C.) and a low temperature region (for example, 50° C. or more and less than 100°).
The peak temperature in the high temperature region (for example, 100° C. to 200° C.) is preferably 150° C. or less, more preferably 140° C. or less, still more preferably 135° C. or less, particularly preferably 130° C. or less, extremely preferably 125° C. or less, and exceedingly preferably 120° C. or less from the viewpoint of improving the removal efficiency of carbon dioxide. The peak temperature in the low temperature region (for example, 50° C. or more and less than 1000) is preferably 75° C. or less, more preferably 60° C. or less, further preferably 55° C. or less, and particularly preferably 50° C. or less from the viewpoint of improving the removal efficiency of carbon dioxide.
The electronegativity of the specific metallic element is 1.00 or more from the viewpoint of improving the desorption amount of carbon dioxide in the case of heating the adsorbent at a high temperature. As the value of electronegativity, the Pauling's electronegativity can be used.
The electronegativity may be 1.05 or more, 1.10 or more, 1.12 or more, 1.15 or more, 1.20 or more, 1.25 or more, 1.30 or more, 1.35 or more, 1.40 or more, 1.50 or more, 1.60 or more, or 1.63 or more from the viewpoint of an excellent balance between the desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region.
The electronegativity of the specific metallic element may be 1.90 or less, 1.85 or less, 1.80 or less, 1.70 or less, or 1.65 or less from the viewpoint that the desorption amount of carbon dioxide is likely to be improved. For example, the electronegativity of the specific metallic element may be 1.00 to 1.80 from the viewpoint of an excellent balance between the desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region.
It is preferable that the specific metallic element includes at least one kind selected from the group consisting of lanthanum (La), neodymium (Nd), yttrium (Y), magnesium (Mg), zirconium (Zr), aluminum (Al), zinc (Zn), iron (Fe) and copper (Cu) from the viewpoint of an excellent balance between the desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region. It is preferable that the specific metallic element includes at least one kind selected from the group consisting of neodymium, aluminum, and zinc from the viewpoint of an excellent desorption amount in the low temperature region (for example, 50° C. or more and less than 100°). In addition, it is preferable that the specific metallic element includes neodymium from the viewpoint of an excellent balance between the desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region. It is preferable that the specific metallic element includes aluminum from the viewpoint of an excellent balance between a high desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region. It is preferable that the specific metallic element includes zinc from the viewpoint of an excellent balance between a high desorption amount of carbon dioxide and the peak temperature of the desorption amount in the high temperature region.
As cerium oxide, a composite oxide in which the specific metallic element is added to CeOx (x=1.5 to 2.0) can be used. Specific examples of cerium oxide may include composite oxides in which the specific metallic element is added to CeO2, Ce2O3, and the like.
The specific surface area of the adsorbent according to the present embodiment is preferably more than 130 m2/g, more preferably 140 m2/g or more, still more preferably 150 m2/g or more, particularly preferably 160 m2/g or more, and extremely preferably 170 m2/g or more from the viewpoint of a tendency that the desorption amount of carbon dioxide is likely to increase. The specific surface area of the adsorbent according to the present embodiment may be 250 m2/g or less, 240 m2/g or less, 230 m2/g or less, 220 m2/g or less, 210 m2/g or less, 200 m2/g or less, 190 m2/g or less, or 180 m2/g or less. The specific surface area (for example, BET specific surface area) can be measured in conformity to the method described in Examples. The specific surface area can be adjusted by the kind of raw material which is for obtaining the adsorbent; the firing temperature and oxygen concentration when firing the raw material; and the like.
The content of cerium oxide in the adsorbent may be 30% by mass or more, 40% by mass or more, 45% by mass or more, 50% by mass or more, 70% by mass or more, or 90% by mass or more based on the total mass of the adsorbent. The adsorbent may consist of cerium oxide (the content of cerium oxide may be substantially 100% by mass based on the total mass of the adsorbent). The adsorption amount and desorption amount of carbon dioxide can be further improved as the content of cerium oxide increases. The content of cerium oxide can be adjusted by, for example, the content of a cerium compound in the raw material which is for obtaining the adsorbent.
Examples of the shape of the adsorbent may include a powdery shape, a pellet shape, a granular shape, and a honeycomb shape. The shape of the adsorbent may be determined in consideration of the required reaction rate, pressure loss, amount adsorbed on the adsorbent, purity (CO2 purity) of the gas (adsorbed gas) to adsorb on the adsorbent, and the like.
<Method for Producing Adsorbent>
The method for producing an adsorbent according to the present embodiment includes, for example, a firing step of firing a raw material containing a cerium compound containing the specific metallic element. The cerium compound containing the specific metallic element may be a composite salt. Examples of the cerium compound may include a carbonate of cerium, a hydrogencarbonate of cerium, an oxalate of cerium, and a hydroxide of cerium. In such a method for producing an adsorbent, the cerium compound is decomposed and cerium is oxidized as the raw material containing a cerium compound is fired. A raw material containing a cerium compound may be obtained by reacting a nitrate of cerium (ammonium cerium nitrate or the like) with a nitrate of the specific metallic element, and then the raw material may be fired. In addition, a raw material containing a cerium compound may be obtained by impregnating ceric oxide (CeO2) with an aqueous solution of a nitrate of the specific metallic element, and then the raw material may be fired.
The cerium compound may be, for example, a compound containing a cerium ion and at least one kind of ion selected from the group consisting of a carbonate ion and a hydrogencarbonate ion. A carbonate of cerium is, for example, a compound containing a cerium ion and a carbonate ion. A hydrogencarbonate of cerium is, for example, a compound containing a cerium ion and a hydrogencarbonate ion.
Examples of the carbonate of cerium may include cerium carbonate and cerium oxycarbonate. Examples of the hydrogencarbonate of cerium may include cerium hydrogencarbonate. The cerium compound may be at least one kind of salt selected from the group consisting of cerium carbonate, cerium hydrogencarbonate and cerium oxycarbonate from the viewpoint of further improving the adsorption amount and desorption amount of carbon dioxide.
The content of the cerium compound may be 40% by mass or more, 45% by mass or more, 50% by mass or more, 90% by mass or more, or 99% by mass or more based on the total mass of the raw material. The raw material containing the cerium compound may consist of a cerium compound (the content of the cerium compound may be substantially 100% by mass based on the total mass of the raw material). The adsorption amount and desorption amount of carbon dioxide can be further improved as the content of the cerium compound increases.
The firing temperature in the firing step is not particularly limited as long as it is a temperature at which the cerium compound can be decomposed. The firing temperature may be 150° C. or more, 175° C. or more, 200° C. or more, or 225° C. or more from the viewpoint that the decomposition of the cerium compound is likely to proceed and thus the production time of the adsorbent can be shortened. The firing temperature may be 600° C. or less, 500° C. or less, 400° C. or less, 350° C. or less, or 300° C. or less from the viewpoint that sintering of cerium oxide hardly occurs and thus the specific surface area of the adsorbent is likely to increase. From these viewpoints, the firing temperature may be 150° C. to 600° C., 175° C. to 500° C., 150° C. to 400° C., 200° C. to 400° C., 200° C. to 350° C., or 225° C. to 300° C.
The firing time in the firing step may be, for example, 10 minutes or more. The firing time may be, for example, 10 hours or less, 3 hours or less, or 1 hour or less.
The firing step may be performed by one stage or multi stages of two or more stages. Incidentally, it is preferable that at least one stage is the above described firing temperature and/or the above described firing time in the case of performing the firing by multi stages. The firing step can be performed in, for example, an air atmosphere, an oxygen atmosphere or reducing atmosphere.
In the firing step, a dried raw material may be fired. In addition, in the firing step, the raw material may be fired as well as the solvent may be removed by heating a solution containing the raw material (for example, a solution in which a cerium compound is dissolved).
The method for producing an adsorbent according to the present embodiment may include a step of molding the raw material before being subjected to firing into a predetermined shape (for example, the shape of the adsorbent to be described later) or a step of molding the raw material after being subjected to firing into a predetermined shape.
<Method for Removing Carbon Dioxide>
The method for removing carbon dioxide according to the present embodiment includes an adsorption step of bringing the adsorbent according to the present embodiment into contact with a gas containing carbon dioxide to adsorb carbon dioxide on the adsorbent.
The CO2 concentration in the gas may be 5000 ppm or less (0.5% by volume or less) based on the total volume of the gas. According to the method for removing carbon dioxide of the present embodiment, carbon dioxide can be efficiently removed in a case in which the CO2 concentration is 5000 ppm or less. The reason why such an effect is exerted is not clear, but the inventors of the present invention presume as follows. It is considered that carbon dioxide adsorbs on the adsorbent as carbon dioxide does not physically adsorb on the surface of cerium oxide but chemically bonds to the surface of cerium oxide in the adsorption step. In this case, in the method for removing carbon dioxide according to the present embodiment, it is presumed that the partial pressure dependency of carbon dioxide at the time of adsorption on the adsorbent is minor and thus carbon dioxide can be efficiently removed even when the CO2 concentration in the gas is 5000 ppm or less.
From the viewpoint that the effect of efficiently removing carbon dioxide is likely to be confirmed even in a case in which the CO2 concentration is low, the CO2 concentration may be 2000 ppm or less, 1500 ppm or less, 1000 ppm or less, or 800 ppm or less based on the total volume of the gas. From the viewpoint that the amount of carbon dioxide removed is likely to increase, the CO2 concentration may be 100 ppm or more, 200 ppm or more, or 400 ppm or more based on the total volume of the gas. From these viewpoints, the CO2 concentration may be 100 ppm to 5000 ppm, 100 ppm to 2000 ppm, 100 ppm to 1500 ppm, 100 ppm to 1000 ppm, 200 ppm to 1000 ppm, 400 ppm to 1000 ppm, or 400 ppm to 800 ppm based on the total volume of the gas. Incidentally, it is stipulated in the Ordinance on Health Standards in Office of the Occupational Safety and Health Act that the CO2 concentration in the room should be adjusted to 5000 ppm or less. In addition, it is known that drowsiness is induced in a case in which the CO2 concentration exceeds 1000 ppm and it is stipulated in the Management Standard of Environmental Sanitation for Buildings that the CO2 concentration should be adjusted to 1000 ppm or less. Hence, there is a case in which the CO2 concentration is adjusted by ventilation so as not to exceed 5000 ppm or 1000 ppm. The CO2 concentration in the gas is not limited to the above range, and it may be 500 ppm to 5000 ppm or 750 ppm to 5000 ppm.
The gas is not particularly limited as long as it is a gas containing carbon dioxide, and it may contain a gas component other than carbon dioxide. Examples of the gas component other than carbon dioxide may include water (water vapor, H2O), oxygen (O2), nitrogen (N2), carbon monoxide (CO), SOx, NOx, and volatile organic compounds (VOC). Specific examples of the gas may include air in the room of a building, a vehicle, and the like. In the adsorption step, in a case in which the gas contains water, carbon monoxide, SOx, NOx, volatile organic compounds, and the like, these gas components adsorb on the adsorbent in some cases.
Meanwhile, the CO2 adsorptivity of a conventional adsorbent such as zeolite tends to significantly decrease in a case in which the gas contains water. Hence, in order to improve the CO2 adsorptivity of the adsorbent in the method using a conventional adsorbent, it is required to perform a dehumidifying step of removing moisture from the gas before bringing the gas into contact with the adsorbent. The dehumidifying step is performed by using, for example, a dehumidifying device, and this thus leads to an increase in facility and an increase in energy consumption. On the other hand, the adsorbent according to the present embodiment exhibits superior CO2 adsorptivity as compared with a conventional adsorbent even in a case in which the gas contains water. Hence, in the method for removing carbon dioxide according to the present embodiment, the dehumidifying step is not required and carbon dioxide can be efficiently removed even in a case in which the gas contains water.
The dew point of the gas may be 0° C. or more. The relative humidity of the gas may be 30% or more, 50% or more, or 80% or more.
The adsorption amount of carbon dioxide can be adjusted by adjusting the temperature T1 of the adsorbent when bringing the gas into contact with the adsorbent in the adsorption step. The amount of CO2 adsorbed on the adsorbent tends to decrease as the temperature T1 is higher. The temperature T1 may be −20° C. to 100° C. or 10° C. to 40° C.
The temperature T1 of the adsorbent may be adjusted by heating or cooling the adsorbent, and heating and cooling may be used in combination. In addition, the temperature T1 of the adsorbent may be indirectly adjusted by heating or cooling the gas. Examples of a method for heating the adsorbent may include: a method in which a heat medium (for example, a heated gas or liquid) is brought into direct contact with the adsorbent; a method in which a heat medium (for example, a heated gas or liquid) is circulated through a heat transfer pipe or the like and the adsorbent is heated by heat conduction from the heat transfer surface; and a method in which the adsorbent is heated by using an electric furnace which has been electrically heated or the like. Examples of a method for cooling the adsorbent may include: a method in which a refrigerant (for example, a cooled gas or liquid) is brought into direct contact with the adsorbent; and a method in which a refrigerant (for example, a cooled gas or liquid) is circulated through a heat transfer pipe or the like and the adsorbent is cooled by heat conduction from the heat transfer surface.
In the adsorption step, the adsorption amount of carbon dioxide can be adjusted by adjusting the total pressure (for example, the total pressure in the vessel containing the adsorbent) of the atmosphere in which the adsorbent is present. The amount of CO2 adsorbed on the adsorbent tends to increase as the total pressure is higher. The total pressure is preferably 1 atm or more from the viewpoint of further improving the removal efficiency of carbon dioxide. The total pressure may be 10 atm or less, 2 atm or less, or 1.3 atm or less from the viewpoint of energy saving. The total pressure may be 5 atm or more.
The total pressure of the atmosphere in which the adsorbent is present may be adjusted by pressurization or depressurization, and pressurization and depressurization may be used in combination. Examples of a method for adjusting the total pressure may include: a method in which the pressure is mechanically adjusted by using a pump, a compressor or the like; and a method in which of a gas having a pressure different from the pressure of the atmosphere surrounding the adsorbent is introduced.
In the method for removing carbon dioxide according to the present embodiment, the adsorbent may be used by being supported on a honeycomb-shaped substrate or by being filled in a vessel. The method for using the adsorbent may be determined in consideration of the required reaction rate, pressure loss, amount adsorbed on the adsorbent, purity (CO2 purity) of the gas (adsorbed gas) to adsorb on the adsorbent, and the like.
In the case of using the adsorbent by being filled in a vessel, it is more preferable as the void fraction is smaller in the case of increasing the purity of carbon dioxide in the adsorbed gas. In this case, the amount of gas remaining in the voids other than carbon dioxide decreases and thus the purity of carbon dioxide in the adsorbed gas can be increased. On the other hand, it is more preferable as the void fraction is greater in the case of diminishing the pressure loss.
The method for removing carbon dioxide according to the present embodiment may further include a desorption step of desorbing (detaching) carbon dioxide from the adsorbent after the adsorption step.
Examples of a method for desorbing carbon dioxide from the adsorbent may include: a method utilizing the temperature dependency of the adsorption amount (temperature swing method. A method utilizing a difference in the amount adsorbed on the adsorbent associated with a change in temperature); a method utilizing the pressure dependency of the adsorption amount (pressure swing method. A method utilizing a difference in the amount adsorbed on the adsorbent associated with a change in pressure), and these methods may be used in combination (temperature and pressure swing method).
In the method utilizing the temperature dependency of the adsorption amount, for example, the temperature of the adsorbent in the desorption step is set to be higher than that in the adsorption step. Examples of a method for heating the adsorbent may include: the same methods as the methods for heating the adsorbent in the adsorption step described above; and a method utilizing surrounding waste heat. It is preferable to utilize surrounding waste heat from the viewpoint of diminishing energy required for heating.
The temperature difference (T2−T1) between the temperature T1 of the adsorbent in the adsorption step and the temperature T2 of the adsorbent in the desorption step may be 200° C. or less, 100° C. or less, or 50° C. or less from the viewpoint of energy saving. The temperature difference (T2−T1) may be 10° C. or more, 20° C. or more, or 30° C. or more from the viewpoint that the carbon dioxide which has adsorbed on the adsorbent is likely to desorb. The temperature T2 of the adsorbent in the desorption step may be, for example, 40° C. to 300° C., 50° C. to 200° C., or 80° C. to 120° C.
In the method utilizing the pressure dependency of the adsorption amount, it is preferable to change total pressure so that the total pressure in the desorption step is lower than the total pressure in the adsorption step since the CO2 adsorption amount is greater as the total pressure of the atmosphere in which the adsorbent is present (for example, the total pressure in the vessel containing the adsorbent) is higher. The total pressure may be adjusted by pressurization or depressurization, and pressurization and depressurization may be used in combination. Examples of a method for adjusting the total pressure may include the same methods as those in the adsorption step described above. The total pressure in the desorption step may be the pressure of the surrounding air (for example, 1 atm) or less than 1 atm from the viewpoint of increasing the CO2 desorption amount.
The carbon dioxide desorbed and recovered through the desorption step may be discharged to the outdoor air as it is, but it may be reused in the field using carbon dioxide. For example, in greenhouse cultivation houses and the like, there is a case in which the CO2 concentration is increased to a 1000 ppm level since the growth of plants is promoted by increasing the CO2 concentration, and thus the recovered carbon dioxide may be reused for increasing the CO2 concentration.
It is preferable that the gas does not contain SOx, NOx, dust and the like since there is a possibility that the CO2 adsorptivity of the adsorbent in the adsorption step decreases in a case in which SOx, NOx, dust and the like are adsorbed on the adsorbent. In a case in which the gas contains SOx, NOx, dust and the like (for example, a case in which the gas is exhaust gas discharged from a coal fired power plant or the like), it is preferable that the method for removing carbon dioxide according to the present embodiment further includes an impurity removing step of removing impurities such as SOx, NOx, and dust from the gas before the adsorption step from the viewpoint that the CO2 adsorptivity of the adsorbent is likely to be maintained. In the impurity removing step, impurities adsorbed on the adsorbent can be removed by heating the adsorbent. The impurity removing step can be performed by using a removal apparatus such as a denitrification apparatus, a desulfurization apparatus, or a dust removing apparatus, and the gas can be brought into contact with the adsorbent on the downstream side of these apparatuses.
The adsorbent after being subjected to the desorption step can be used again in the adsorption step. In the method for removing carbon dioxide according to the present embodiment, the adsorption step and the desorption step may be repeatedly performed after the desorption step. The adsorbent may be cooled by the method described above and used in the adsorption step in a case in which the adsorbent is heated in the desorption step. The adsorbent may be cooled by bringing a gas containing carbon dioxide (for example, a gas containing carbon dioxide) into contact with the adsorbent.
The method for removing carbon dioxide according to the present embodiment can be suitably implemented in a sealed space which requires management of CO2 concentration. Examples of the space which requires management of CO2 concentration may include a building; a vehicle; an automobile; a space station; a submarine; a manufacturing plant for a food or a chemical product. The method for removing carbon dioxide according to the present embodiment can be suitably implemented particularly in a space (for example, a space with a high density of people such as a building and a vehicle) in which the CO2 concentration is limited to 5000 ppm or less. In addition, the method for removing carbon dioxide according to the present embodiment can be suitably implemented in a manufacturing plant for a food or a chemical product and the like since there is a possibility that carbon dioxide adversely affects at the time of manufacture of a food or a chemical product.
<Apparatus for Removing Carbon Dioxide and System for Removing Carbon Dioxide>
The system for removing carbon dioxide according to the present embodiment is equipped with an apparatus for removing carbon dioxide according to the present embodiment. For example, the system for removing carbon dioxide according to the present embodiment is equipped with the apparatus for removing carbon dioxide according to the present embodiment and a control means for comprehensively controlling the apparatus for removing carbon dioxide. The system for removing carbon dioxide (air conditioning system or the like) according to the present embodiment may be equipped with a plurality of apparatuses for removing carbon dioxide (air conditioners and the like) according to the present embodiment. The system for removing carbon dioxide according to the present embodiment may be equipped with a control section for comprehensively controlling the operation of a plurality of apparatuses for removing carbon dioxide. The apparatus for removing carbon dioxide according to the present embodiment is equipped with the adsorbent according to the present embodiment.
In the system for removing carbon dioxide and the apparatus for removing carbon dioxide according to the present embodiment, for example, carbon dioxide adsorbs on the adsorbent as the gas, which has been introduced into the reaction vessel, comes into contact with the adsorbent disposed in the reaction vessel. The system for removing carbon dioxide and apparatus for removing carbon dioxide according to the present embodiment may be used for decreasing the concentration of carbon dioxide in the space to be air-conditioned or for decreasing the concentration of carbon dioxide in the gas to be discharged to the outdoor air from a plant or the like. The space to be air-conditioned may be, for example, a building; a vehicle; an automobile; a space station; a submarine; a manufacturing plant for a food or a chemical product; or the like.
The apparatus for removing carbon dioxide according to the present embodiment may be an air conditioner. The air conditioner according to the present embodiment is an air conditioner used in a space containing a gas containing carbon dioxide. The air conditioner according to the present embodiment is equipped with a flow path connected to the space, and a removal section (a carbon dioxide removing section) for removing carbon dioxide contained in the gas is disposed in the flow path. In the air conditioner according to the present embodiment, the adsorbent according to the present embodiment is disposed in the removal section, and carbon dioxide adsorbs on the adsorbent as the adsorbent comes into contact with the gas. According to the present embodiment, there is provided an air conditioning method including an adsorption step of bringing a gas in a space to be air-conditioned into contact with an adsorbent to adsorb carbon dioxide on the adsorbent. Incidentally, the details of the gas containing carbon dioxide are the same as those of the gas in the method for removing carbon dioxide described above.
Hereinafter, an air conditioning system and an air conditioner will be described as examples of a system for removing carbon dioxide and an apparatus for removing carbon dioxide with reference to
As illustrated in
The flow path 10 is connected to a space R to be air-conditioned containing a gas (indoor gas) containing carbon dioxide. The flow path 10 includes a flow path section 10a, a flow path section 10b, a removal section (a flow path section, a carbon dioxide removing section) 10c, a flow path section 10d, a flow path section (circulation flow path) 10e, and a flow path section (exhaust flow path) 10f, and the removal section 10c is disposed in the flow path 10. The air conditioner 100 is equipped with the removal section 10c as a reaction vessel. In the flow path 10, a valve 70a for adjusting the presence or absence of inflow of the gas in the removal section 10c and a valve 70b for adjusting the flow direction of the gas are disposed.
The upstream end of the flow path section 10a is connected to the space R and the downstream end of the flow path section 10a is connected to the upstream end of the flow path section 10b via the valve 70a. The upstream end of the removal section 10c is connected to the downstream end of the flow path section 10b. The downstream end of the removal section 10c is connected to the upstream end of the flow path section 10d. The downstream side of the flow path section 10d in the flow path 10 is branched into the flow path section 10e and the flow path section 10f. The downstream end of the flow path section 10d is connected to the upstream end of the flow path section 10e and the upstream end of the flow path section 10f via the valve 70b. The downstream end of the flow path section 10e is connected to the space R. The downstream end of the flow path section 10f is connected to the outdoor air.
An adsorbent 80 which is the adsorbent according to the present embodiment is disposed in the removal section 10c. The adsorbent 80 is filled in the central portion of the removal section 10c. Two spaces are formed in the removal section 10c via the adsorbent 80, and the removal section 10c includes a space S1 on the upstream side, a central portion S2 filled with the adsorbent 80, and a space S3 on the downstream side. The space S1 is connected to the space R via the flow path sections 10a and 10b and the valve 70a, and the gas containing carbon dioxide is supplied from the space R to the space S1 of the removal section 10c. The gas which has been supplied to the removal section 10c moves from the space SI to the space S3 through the central portion S2 and then is discharged from the removal section 10c.
At least a part of carbon dioxide in the gas which has been discharged from the space R is removed in the removal section 10c. The gas from which carbon dioxide has been removed may be returned to the space R by adjusting the valve 70b or discharged to the outdoor air present outside the air conditioner 100. For example, the gas which has been discharged from the space R can flow into the space R from the upstream to the downstream through the flow path section 10a, the flow path section 10b, the removal section 10c, the flow path section 10d, and the flow path section 10e. In addition, the gas which has been discharged from the space R may be discharged to the outdoor air from the upstream to the downstream through the flow path section 10a, the flow path section 10b, the removal section 10c, the flow path section 10d, and the flow path section 10f.
The exhaust fan 20 is disposed at the discharge position of the gas in the space R. The exhaust fan 20 discharges the gas from the space R and supplies the gas to the removal section 10c.
The device for measuring concentration 30 measures the concentration of carbon dioxide in the space R. The device for measuring concentration 30 is disposed in the space R.
The electric furnace 40 is disposed outside the removal section 10c of the air conditioner 100 and can raise the temperature of the adsorbent 80. The compressor 50 is connected to the removal section 10c of the air conditioner 100 and can adjust the pressure inside the removal section 10c.
The control apparatus 110 can perform overall operation control of the air conditioner 100, and for example, it can control the presence or absence of inflow of the gas in the removal section 10c based on the concentration of carbon dioxide measured by the device for measuring concentration 30. More specifically, the concentration information is transmitted from the device for measuring concentration 30 to the control apparatus 110 in a case in which the device for measuring concentration 30 detects that the concentration of carbon dioxide in the space R has increased by exhalation or the like and reached a predetermined concentration. The control apparatus 110, which has received the concentration information, opens the valve 70a and also adjusts so that the gas discharged from the removal section 10c flows into the space R via the flow path section 10d and the flow path section 10e. Thereafter, the control apparatus 110 operates the exhaust fan 20 to supply the gas from the space R to the removal section 10c. Furthermore, the control apparatus 110 operates the electric furnace 40 and/or the compressor 50 if necessary to adjust the temperature of the adsorbent 80, the pressure in the removal section 10c, and the like.
The gas comes into contact with the adsorbent 80 and carbon dioxide in the gas adsorbs on the adsorbent 80 as the gas supplied to the removal section 10c moves from the space S1 to the space S3 via the central portion S2. By this, carbon dioxide is removed from the gas. In this case, the gas from which carbon dioxide has been removed is supplied to the space R via the flow path section 10d and the flow path section 10e.
Carbon dioxide adsorbed on the adsorbent 80 may be recovered in a state of being adsorbed on the adsorbent 80 without being desorbed from the adsorbent 80 or may be desorbed from the adsorbent 80 and recovered. In the desorption step, carbon dioxide can be desorbed from the adsorbent 80 by the temperature swing method, pressure swing method and the like described above as the temperature of the adsorbent 80, the pressure inside the removal section 10c, and the like are adjusted by operating the electric furnace 40 and/or the compressor 50. In this case, for example, the valve 70b is adjusted so that the gas (gas containing the desorbed carbon dioxide) discharged from the removal section 10c is discharged to the outdoor air via the flow path section 10f, and discharged carbon dioxide can be recovered if necessary.
As illustrated in
The apparatus for removing carbon dioxide and the system for removing carbon dioxide are not limited to the embodiment described above and may be appropriately changed without departing from the gist thereof. For example, the contents of control by the control section of the apparatus for removing carbon dioxide are not limited to control of the presence or absence of inflow of the gas in the reaction vessel, and the control section may adjust the inflow amount of the gas in the reaction vessel.
In the air conditioner, a gas may be supplied to the reaction vessel by using a blower instead of the exhaust fan, and the exhaust means may not be used in a case in which the gas is supplied to the reaction vessel by natural convection. In addition, the temperature control means and the pressure control means are not limited to the electric furnace and the compressor, and various means described in the adsorption step and the desorption step can be used. The temperature control means is not limited to the heating means, and it may be a cooling means.
In the air conditioner, each of the space to be air-conditioned, the carbon dioxide removing section, the exhaust means, the temperature control means, the pressure control means, the concentration measuring section, and the like is not limited to one, and a plurality of these may be disposed. The air conditioner may be equipped with a humidity adjuster for adjusting the dew point and relative humidity of the gas; a humidity measuring device for measuring the humidity of the space to be air-conditioned; a removal apparatus such as a denitrification apparatus, a desulfurization apparatus, or a dust removing apparatus.
Hereinafter, the contents of the present invention will be described in more detail with reference to Examples and Comparative Examples, but the present invention is not limited to the following Examples.
A solution obtained by dissolving 0.32 g of sodium carbonate in 2.0 g of purified water was added to 5.16 g of a commercially available ceric oxide (CeO2) powder. Thereafter, the mixture was dried at 120° C. in the air and then fired at 300° C. for 1 hour in the air, thereby obtaining an adsorbent (Ce:Na=5:1 (molar ratio)).
Into a beaker, 300 mL of pure water and 60.0 g of urea were added, and the mixture was stirred until to be uniform. Next, 16.45 g of diammonium cerium(IV) nitrate was added thereto, and the mixture was stirred at 30° C. for 10 minutes. Thereafter, 2.60 g of lanthanum(III) nitrate⋅hexahydrate was added thereto, and the mixture was stirred at 30° C. for 10 minutes. Thereafter, the temperature of the mixture was raised to 95° C. over 30 minutes while continuously performing stirring, and the temperature was maintained at 95° C. for 3 hours, thereby causing precipitation. The pH when the precipitation occurred was 5 to 6. The solution was cooled to room temperature (25° C.), and then the solid was separated by suction filtration and washed with water. Thereafter, the washed solid was dried at 120° C. for 1 hour and then fired at 300° C. for 1 hour, thereby obtaining an adsorbent (Ce:La=5:1 (molar ratio)).
An adsorbent (Ce:Nd=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 2.63 g of neodymium nitrate⋅hexahydrate.
An adsorbent (Ce:Y=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 2.30 g of yttrium nitrate⋅hexahydrate.
An adsorbent (Ce:Mg=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 1.54 g of magnesium nitrate⋅hexahydrate.
An adsorbent (Ce:Zr=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 1.60 g of zirconyl nitrate⋅dihydrate.
An adsorbent (Ce:AI=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 2.25 g of aluminum nitrate⋅nonahydrate.
An adsorbent (Ce:Zn=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 1.78 g of zinc nitrate⋅hexahydrate.
An adsorbent (Ce:Fe=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 2.42 g of iron(III) nitrate⋅nonahydrate.
An adsorbent (Ce:Cu=5:1 (molar ratio)) was obtained in the same manner as in Example 1 except that 2.60 g of lanthanum(III) nitrate⋅hexahydrate was changed to 1.45 g of copper(II) nitrate⋅trihydrate.
An adsorbent was obtained in the same manner as in Example 1 except that lanthanum(III) nitrate⋅hexahydrate was not used.
<Measurement of BET Specific Surface Area of Adsorbent>
The BET specific surface area of the respective adsorbents was measured. First, as a pretreatment, the adsorbent was heated at 200° C. while performing vacuum drawing. Subsequently, the adsorption isotherm of nitrogen at −196° C. was measured. Subsequently, the BET specific surface area was measured by the Bnmauer-Emmett-Teller (BET) method. The measurement results are presented in Table 1.
<Adsorption Desorption Test of Carbon Dioxide>
The CO2 desorption amount at each temperature was measured using the adsorbents of Examples and Comparative Examples by the temperature programmed desorption measurement (TPD) according to the following procedure.
First, the adsorbent was pelletized at 500 kgf by using a pressing machine and a mold having a diameter of 40 mm. Subsequently, the pellet was pulverized and then adjusted into a granular shape (particle size: 0.5 mm to 1.0 mm) by using a sieve. Thereafter, the adsorbent was weighed by 1.0 mL and fixed in a reaction tube. Subsequently, the adsorbent was dried at 120° C. in the air.
Subsequently, as the adsorption step, a mixed gas containing CO2 at 800 ppm, He (balance gas), and moisture (H2O) at 2.3% by volume was circulated through the reaction tube at a flow rate of 60 cm3/min (total pressure in the reaction tube: 1 atm) while adjusting the temperature of the adsorbent to 20° C. Incidentally, moisture was introduced by circulating the gas through a bubbler. The CO2 concentration in the outlet gas of the reaction tube was analyzed by gas chromatography and the mixed gas was circulated until adsorption saturation was achieved.
Subsequently, as a desorption step, the temperature of the adsorbent was raised from 20° C. to 200° C. at 2° C./min by using an electric furnace (total pressure in the reaction tube: 1 atm) while circulating the same mixed gas as that in the adsorption step through the reaction tube at a flow rate of 60 cm3/min as a circulating gas. The CO2 desorption amount (accumulated amount) until the temperature reached 50° C. and the CO2 desorption amount (accumulated amount) until the temperature reached 200° C. were calculated by measuring the CO2 concentration in the outlet gas of the reaction tube. The CO2 desorption amount was calculated by excluding the CO2 concentration in the mixed gas from the CO2 concentration in the outlet gas (CO2 concentration in outlet gas—800 ppm). The measurement results are presented in Table 1.
In addition, the peak temperature of the peak appearing in the region of 50° C. or more and less than 100° C. and the peak temperature of the peak appearing in the region of 100° C. to 200° C. were calculated based on a change in the CO desorption amount associated with an increase in the heating temperature. The measurement results are presented in Table 1.
As presented in Table 1, it can be seen that the CO2 desorption amount until the temperature reached 200° C. is superior in each Example as compared with Comparative Examples. In each Example in which the CO2 desorption amount is excellent at a high temperature as described above, carbon dioxide can also be desorbed at a low temperature (a desorption amount of 0.80 g/L or more can be obtained). Furthermore, it can be seen that the peak temperature in the high temperature region can be lowered in each Example as compared with Comparative Example 1 in the case of using cerium and another metallic element in combination.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2016-098200 | May 2016 | JP | national |
| 2016-098203 | May 2016 | JP | national |
| 2016-129064 | Jun 2016 | JP | national |
| 2016-167643 | Aug 2016 | JP | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2017/013677 | 3/31/2017 | WO | 00 |
