Patent Application
20140219898
1. Field of the Invention
The present invention relates to a method of recovering carbon dioxide and recovery apparatus of carbon dioxide to return a clean gas into the air by separating and recovering carbon dioxide from a gas containing carbon dioxide such as a combustion gas.
2. Description of the Related Art
A large amount of fuel such as coal, heavy oil and extra heavy oil is used in facilities such as thermal power stations, ironworks and boilers. In regard to sulfur oxide, nitrogen oxide and carbon dioxide discharged by burning of the fuel, quantitative/concentration restriction on emissions has been required from the viewpoint of prevention of air pollution and global environmental protection. In recent years, carbon dioxide has been viewed as a problem as is a major contributor to global warming, and moves to suppress carbon dioxide emissions have been active worldwide. Therefore, various kinds of research have been vigorously conducted in order to enable recovery/storage of carbon dioxide from a combustion exhaust gas or a process exhaust gas instead of emitting carbon dioxide in the air. For example, a PSA (pressure swing adsorption) method, a membrane separation concentration method, and a chemical absorption technique using reaction absorption with a basic compound have been known as a method of recovering carbon dioxide.
In the chemical absorption technique, a basic compound that typically belongs to alkanolamines is mainly used as an absorbent, and the absorbing liquid is circulated in the treatment process thereof, generally, with use of an aqueous solution containing the absorbent as the absorbing liquid, by alternately repeating an absorption step of causing the absorbing liquid to absorb carbon dioxide contained in the gas and a regeneration step of regenerating the absorbing liquid by causing the absorbing liquid to release the absorbed carbon dioxide (see, for example, Publication document 1 described below). Heating for the release of carbon dioxide is needed in the regeneration step, and it becomes important to reduce energy required for heating/cooling for the regeneration, in order to reduce the operation cost of carbon dioxide recovery.
As disclosed in Publication Document 1, a high-temperature absorbing liquid from which carbon dioxide has been discharged (lean solution) in the regenerating step is subjected to heat exchange with an absorbing liquid in which carbon dioxide has been absorbed (rich solution) in the absorbing step. In this way, thermal energy is possibly recovered to reuse in the regenerating step.
In order to reduce the energy required for recovering carbon dioxide from the absorbing liquid, according to Publication Document 2 listed below, the following is used for heating the absorbing liquid: residual heat of steam-condensed water generated from a regenerating heater for pulling out the absorbing liquid in the regenerating step and then subjecting the absorbing liquid to heat exchange with high-temperature steam. Furthermore, Publication Document 3 listed below states that, in order to promote the discharge of absorbed carbon dioxide, a stripping gas is introduced to be accompanied with carbon dioxide.
Publication Document 1: Japanese Patent Application Laid-Open (JP-A) No. 2009-214089
Publication Document 2: JP-A 2005-254212
Publication Document 3: JP-A 2005-230808
Energy required for the regenerating step is classified into sensible heat required for a rise in the temperature of an absorbing liquid, reaction heat generated when carbon dioxide is discharged from the absorbing liquid, and latent heat compensating for heat loss based on vaporization of water from the absorbing liquid. However, the above-mentioned precedent techniques are techniques related to the sensible heat or reaction heat, and energy concerned with the latent heat is discharged together with water vapor contained in the collected carbon dioxide. Consequently, there has still remained a room for improving the efficiency of the energy.
In order to spread the recovering of carbon dioxide for environment preservation, it is desired from an economical viewpoint to make the energy efficiency as high as possible to reduce costs for the recovery. It is important for energy saving to heighten the efficiency of recovering thermal energy from an absorbing liquid. This can also act effectively onto the efficiency of recovering carbon dioxide.
An object of the present invention is to solve the above-mentioned problems to provide a carbon dioxide recovery method and recovery apparatus capable of reducing energy required for regenerating the absorbing liquid to decrease operating costs.
Another object of the present invention is to provide a carbon dioxide recovery method and recovery apparatus capable of decreasing burdens onto the apparatus and the absorbing liquid and reducing energy required for regenerating the absorbing liquid without lowering the recovery ratio of carbon dioxide, thereby decreasing costs for collecting carbon dioxide.
In order to solve the problems, the inventors have repeated eager researches to find out that the absorbing liquid is circulated by use of a two-part-divided circulation system in which each of the absorbing step and the regenerating step is divided into at least two stages, thereby carrying out two groups of a carbon-dioxide-absorbing/recovering cycle. Thus, the present invention has been achieved.
According to an aspect of the present invention, a subject matter of a recovery apparatus of carbon dioxide resides in comprising: an absorption column configured to bring a gas into contact with an absorbing liquid and to allow the absorbing liquid to absorb carbon dioxide contained in the gas, the absorption column having a first absorbing section and a second absorbing section which are arranged to supply the gas through the first absorbing section into the second absorbing section; a regeneration column that regenerate the absorbing liquid, configured to heat the absorbing liquid having carbon dioxide absorbed in the absorption column to cause the absorbing liquid to release the carbon dioxide, the regeneration column having a first regenerating section having an external heating implement and a second regenerating section arranged to be heated by heat from gas discharged from the first regenerating section; and a circulation system having a first circulating path configured to circulate the absorbing liquid between the first absorbing section and the second regenerating section, and a second circulating path configured to circulate the absorbing liquid between the second absorbing section and the first regenerating section.
According to another aspect of the present invention, a subject matter of the carbon dioxide recovery method resides in comprising: an absorption treatment of bringing a gas into contact with an absorbing liquid to cause carbon dioxide contained in the gas to be absorbed into the absorbing liquid, the absorption treatment having a first absorbing step and a second absorbing step, and the gas being supplied through the first absorbing step to the second absorbing step; a regeneration treatment of heating the absorbing liquid in which carbon dioxide is absorbed in the absorption treatment to discharge carbon dioxide, thereby regenerating the absorbing liquid, the regeneration treatment having a first regenerating step and a second regenerating step, the absorbing liquid being heated in the first regenerating step with use of an external heating implement, and the absorbing liquid being heated in the second regenerating step with use of heat from the gas discharged in the first regenerating step; and a first circulating step of circulating the absorbing liquid between the first absorbing step and the second regenerating step, and a second circulating step of circulating the absorbing liquid between the second absorbing step and the first regenerating step.
According to the present invention, in the process of recovering carbon dioxide contained in the gas, an improvement is made in the efficiency of recovering heat used for regenerating the absorbing liquid, so that thermal energy required for the regeneration is possibly reduced without lowering the recovery ratio of carbon dioxide. Thus, the provided carbon dioxide recovery method and recovery apparatus are useful for reducing driving costs. Two absorbing liquids different from each other in composition are usable, and respective properties of the absorbing liquids can be specialized correspondingly to the respective absorbing/regenerating conditions of the absorbing liquids. Using their properties, the recovery of carbon dioxide and the regeneration of the absorbing liquids can be efficiently attained, so that loads onto the absorbing liquids are reduced when the absorbing liquids are regenerated. Thus, the absorbing liquids can be efficiently and stably used, and it is useful for decreasing operating costs and facility-maintaining costs. Since the present invention can easily be performed using ordinary facilities without requiring special equipment or expensive apparatus, it is economically favorable.
The features and advantages of the carbon dioxide recovery method and recovery apparatus according to the present invention will more clearly understood from the following description of the conjunction with the accompanying drawings in which identical reference letters designate the same or similar elements or cases throughout the figures and in which:
In an absorption process of carbon dioxide according to the chemical absorption method, an absorption treatment in which an absorbing liquid at low temperature is caused to absorb carbon dioxide contained in a gas and a regeneration treatment in which the absorbing liquid is regenerated by causing the absorbing liquid to release the absorbed carbon dioxide are alternately repeated by circulating the absorbing liquid between the absorption treatment and the regeneration treatment. The regeneration degree of the absorbing liquid in the regeneration treatment depends on the heating temperature of the absorbing liquid. As the temperature is higher, the absorbing liquid discharges a larger volume of carbon dioxide so that the remaining carbon dioxide concentration in the absorbing liquid becomes lower (see: Jong I. Lee, Federick D. Otto and Alan E. Mather, “Equilibrium Between Carbon Dioxide and Aqueous Monoethanolamine Solutions”, J. appl. Chem. Biotechnol. 1976, 26, pp. 541-549). Thus, the absorbing liquid in the regeneration treatment is kept at a temperature near to the boiling point thereof by an external heating implement using thermal energy supplied from an external heat source. The absorbing liquid from which carbon dioxide has been discharged (lean solution) in the regeneration treatment, which is high in temperature, is subjected to heat exchange with the absorbing liquid in which carbon dioxide has been absorbed (rich solution) in the absorption treatment, and the heated rich solution is supplied to the regeneration treatment. Thus, thermal energy is recovered and reused. However, carbon-dioxide-containing gas discharged from the absorbing liquid in the regeneration treatment is discharged in a high-temperature state that the gas contains the heat. The heat quantity contained in the discharged gas is wasted. The temperature of the discharged gas, that is, the column-top temperature of the regeneration column can be made low by lowering the heat exchange ratio between the rich solution and the lean solution. However, it does not contribute to a reduction in the heat quantity because sensible heat recovered in the heat exchange is reduced.
In the present invention, each of an absorption treatment and a regeneration treatment is divided into at least two stages, so as to constitute two groups of an absorbing step and a regenerating step. The circulating path for circulating the absorbing liquid is also separated into two independent paths, and the absorbing liquid is circulated between the absorbing step and the regenerating step in each of the groups to constitute the recovery method of the present invention. In one of the regenerating steps, the absorbing liquid is positively heated by an external heating implement using an external energy source, and a high-temperature gas discharged in this step is supplied to the other regenerating step to function as a heat source, whereby the absorbing liquid is heated and regenerated. In short, heat discharged and recovered from the gas is directly used to regenerate the absorbing liquid. In this configuration, the absorbing liquid that is circulated in the two paths can be separately selected for each path so that each of the absorbing liquids can be adjusted to have a property suitable for treatment conditions in the path concerned. As a result, two kinds of absorbing liquids prepared to have different compositions are also usable. It is generally difficult for the absorbent contained in the absorbing liquid to develop such an absorbent as to be excellent in both of absorption performance and regeneration property, and general absorbents are excellent in either one of the above two items. Thus, according to the structure in which absorbing liquids different from each other in concentration or composition are usable, an absorbing liquid specialized for treatment conditions in the absorbing step and the regenerating step is possibly selected to use for each circulation system, so that a decrease can be favorably advanced in energy required for the regeneration while a lowering in the efficiency of the absorption and that of the regeneration is avoided.
Hereinafter, referring to the drawings, a detailed description will be made about the carbon dioxide recovery method and carbon dioxide recovery apparatus of the present invention.
The gas G containing carbon dioxide is supplied through a lower portion of the absorption column 10. The inside of the absorption column 10 is partitioned into a first absorbing section 12a at the lower side in which a filler 11a is held, and a second absorbing section 12b at the upper side in which a filler 11b is held. Between the first and second absorbing sections 12a and 12b, a partitioning member 13 is interposed such that a cylindrical wall stands on the circumferential edge of a central hole formed in a horizontal circular plate, and a lamp-shade-like member covers over the upper end hole of the cylindrical wall of the partitioning member 13, and it is configured so that a liquid reservoir is formed on the horizontal circular plate between the inner wall of the absorption column 10 and the cylindrical wall of the partitioning member 13. The gas G supplied through the lower portion of the absorption column 10 rises in the column to pass through the filler 11a in the first absorbing section 12a, and then passes through the inner bore of the cylindrical wall of the partitioning member 13 to pass through the filler 11b in the second absorbing section 12b. The absorbing liquid is separated into first and second absorbing liquids. The first absorbing liquid is supplied through an upper portion of the first absorbing section 12a of the absorption column 10 to flow down through the filler 11a, and then stored on the bottom portion of the absorption column 10. The second absorbing liquid is supplied through an upper portion of the second absorbing section 12b of the absorption column 10 to flow down through the filler 11b, and then stored in the liquid reservoir of the partitioning member 13. It is configured to discharge the second absorbing liquid to the outside of the column without flowing down to the first absorbing section. While the gas G passes through the fillers 11a and 11b, the gas is brought into gas-liquid contact with the two absorbing liquids successively, so that carbon dioxide in the gas G is absorbed into the absorbing liquids. Since the gas after passing through the first absorbing section has been lowered in carbon dioxide concentration, the second absorbing liquid contacts a gas lower in carbon dioxide concentration than the gas G which the first absorbing liquid contacts. The first absorbing liquid A1′ in which carbon dioxide has been absorbed (rich solution) in the first absorbing section 12a is stored on the bottom of the absorption column 10 and then supplied, by means of a pump 14, to the regeneration column 20 through a first supplying path 15 through which the bottom of the absorption column 10 is connected to an upper portion of the regeneration column 20. The second absorbing liquid A2′ in which carbon dioxide has been absorbed (rich solution) in the second absorbing section 12b is stored in the liquid reservoir of the partitioning member 13 and then supplied, by means of a pump 16, to the regeneration column 20 through a second supplying path 17 through which the center portion of the absorption column 10 is connected to the center portion of the regeneration column 20. The gas G′ from which carbon dioxide has been removed is discharged from the absorption column 10 through the top thereof.
When the absorbing liquid absorbs carbon dioxide, heat is generated so that the temperature of the liquid is raised. Thus, as the need arises, a cooling condenser section 18 is provided at the top of the absorption column 10 to condense water vapor and others contained in the gas G′. This section enables to restrain the water vapor and the others to some degree from leaking outside the column. In order to further ensure the restraint, the recovery apparatus has a cooler 31 and a pump 32 located outside the absorption column. A part of condensed water stored under the cooling condenser section 18 (the condensed water part being permissible to contain the gas G′ in the column) is circulated between the cooling condenser section 18 and the cooler 31 by means of the pump 32. The condensed water and others that have been cooled by the cooler 31 to be supplied to the column top portion cause the cooling condenser section 18 to be kept at a low temperature, and causes the gas G′ passing through the cooling condenser section 18 to be certainly cooled. The driving of the pump 32 is controlled in such a manner that the temperature of the gas G′ discharged outside the column is preferably about 60° C. or lower, more preferably 45° C. or lower. In the structure in
The inside of the regeneration column 20 is partitioned into a first regenerating section 22a at the lower side in which a filler 21a is held, and a second regenerating section 22b at the upper side in which a filler 12b is held. Between the first and second regenerating sections 22a and 22b, a partitioning member 23 is interposed which has the same structure as the partitioning member 13 to form a liquid reservoir. The first absorbing liquid A1′ supplied from the bottom of the absorption column 10 through the first supplying path 15 is introduced to the upper portion of the second regenerating section 22b of the regeneration column 20 to flow down through the filler 21b, and then stored in the liquid reservoir of the partitioning member 23. It is configured that the first absorbing liquid part A1′ is discharged to the outside of the column without flowing down to the first regenerating section. The second absorbing liquid A2′ supplied from the second absorbing section 12b of the absorption column 10 through the second supplying path 17 is supplied to the upper portion of the first regenerating section 22a to flow down through the filler 21a, and then stored on the bottom of the regeneration column 20.
A reboiler is fitted, as an external heating implement for heating the absorbing liquid positively by use of energy supplied from the outside, to the bottom of the regeneration column 20. Specifically, a steam heater 24 located outside the regeneration column 20, and a circulating path 25 for circulating, through the steam heater 24, a second absorbing liquid A2 stored on the column bottom are equipped. The second absorbing liquid A2 on the column bottom is partially branched through the circulating path 25 into the steam heater 24, and it is continuously heated by heat exchange with high-temperature steam to flow back into the column. In this manner, the second absorbing liquid A2 on the bottom is positively heated to discharge carbon dioxide sufficiently, and the filler 21a is also heated indirectly to promote the discharge of carbon dioxide by gas-liquid contact on the filler 21a. A high-temperature gas containing carbon dioxide and water vapor discharged from the second absorbing liquid rises to pass through the filler 21a in the first regenerating section 22a. Thereafter, it passes through the inner hole surrounded by the cylindrical wall of the partitioning member 23 to pass through the filler 21b in the second regenerating section 22b. During this period, the second absorbing liquid A2′ flowing down through the filler 21a and the first absorbing liquid A1′ flowing down through the filler 21b are heated so that carbon dioxide in the absorbing liquids A1′ and A2′ is discharged. The first absorbing liquid A1′ supplied into the second regenerating section 22b does not receive any positive heating by the external heating implement, so as to be heated only by heat of gas discharged from the first regenerating section 22a. Thus the temperature thereof is lower than that of the second absorbing liquid A2′. Consequently, when the first and second absorbing liquids are identical with each other in composition, the regeneration degree of the first absorbing liquid A1 in the liquid reservoir of the partitioning member 23 becomes lower than that of the second absorbing liquid A2 on the column bottom, so as to become a semi-lean solution. The first absorbing liquid A1 from which carbon dioxide has been discharged is caused to flow back, by a pump 26, from the liquid reservoir of the partitioning member 23 to the upper region of the first absorbing section 12a of the absorption column 10 through a first return path 27 through which the center portion of the regeneration column 20 is connected to center portion of the absorption column 10. The second absorbing liquid A2 from which carbon dioxide has been sufficiently discharged (lean solution part) while being stored on the bottom of the regeneration column 20 is caused to flow back, by a pump 28, to the upper portion of the second absorbing section 12b of the absorption column 10 through the second return path 29 through which the upper portion of the absorption column 10 is connected to the bottom of the regeneration column 20. As a result, the first absorbing liquid A1, A1′ are reciprocated between the first absorbing section 12a and the second regenerating section 22b through the first supplying path 15 and the first return path 27, so as to constitute a first circulation system. The second absorbing liquid A2, A2′ are reciprocated between the second absorbing section 12b and the first regenerating section 22a through the second supplying path 17 and the second return path 29, so as to constitute a second circulation system. A carbon-dioxide-containing gas discharged from the absorbing liquid in the regeneration column 20 is discharged from the regeneration column 20 through the top thereof.
The first absorbing liquid A1, from which carbon dioxide has been discharged in the second regenerating section 22b, passes through a first heat exchanger 33 while flowing back in the first return path 27, so that heat exchange is performed between the first supplying path 15 and the first return path 27 in the first heat exchanger 33. Consequently, the first absorbing liquid A1 is cooled with the first absorbing liquid part A1′ in the first supplying path 15, and further sufficiently cooled to a temperature suitable for the absorption of carbon dioxide by a cooler 35 using cooling water. Thereafter, the first absorbing liquid A1 is introduced into the upper portion of the first absorbing section 12a. Moreover, the second absorbing liquid A2, from which carbon dioxide has been discharged in the first regenerating section 22a, passes through a second heat exchanger 34 while flowing in the second return path 29, so that heat exchange is performed between the second supplying path 17 and the second return path 29 in the second heat exchanger 34. Consequently, the second absorbing liquid A2 is cooled with the second absorbing liquid A2′ in the second supplying path 17, and further sufficiently cooled in the same manner by a cooler 36 using cooling water. Thereafter, the second absorbing liquid A2 is introduced into the upper portion of the second absorbing section 12b. Heat exchangers can be classified into various types such as spiral, plate, double-tube, multi-cylinder, circular multi-tube, eddy tube, eddy plate, tank coil, tank jacket, and direct contacting liquid types. Each of the first and second heat exchangers 33 and 34 used in the present invention may be any one of these types. From the viewpoint of the simplification of the exchangers and easiness of the disassembly and cleaning thereof, plate type exchangers are excellent.
A carbon-dioxide-containing gas discharged from the absorbing liquid by heating in the regeneration column 20 passes through a condensing section 37 at an upper portion of the regeneration column 20, and then discharged through an exhaust pipe 38 from the top thereof. The gas is sufficiently cooled by a cooler 39 using cooling water, so that water vapor and others contained therein are condensed as much as possible. The resultant condensed water is removed by a gas-liquid separator 40, and then recovered as a recovery gas C. The condensing section 37 condenses water vapor contained in the gas to restrain the discharge thereof, and further restrains the discharge of the absorbent. By injecting carbon dioxide contained in the recovery gas C into, for example, the earth or an oil well, carbon dioxide gas is possibly fixed in the earth and re-organized. The condensed water separated in the gas-liquid separator 40 is supplied at a predetermined flow rate through a flow path 42 into an upper portion of the condensing section 37 of the regeneration column 20 by a pump 41 so that the water functions as cooling water.
In the regeneration column 20, an expression of T1>T2 is satisfied in which T1 represents the temperature of the second absorbing liquid A2 heated on the bottom of the first regenerating section 22a, and T2 represents the temperature of the second absorbing liquid A2′ introduced from the second heat exchanger 34 into the upper portion of the first regenerating section 22a. Expressions of t1>T3>T4 and t1>t2 are also satisfied in which T3 represents the temperature of the first absorbing liquid A1 in the liquid reservoir that has been heated in the second regenerating section 22b by the gas discharged from the first regenerating section 22a, T4 represents the temperature of the first absorbing liquid A1′ introduced from the first heat exchanger 33 into the second regenerating section 22b, t1 represents the temperature of the gas discharged from the first regenerating section 22a into the second regenerating section 22b, and t2 represents the temperature of the gas discharged from the second regenerating section 22b. In general, the absorbing liquid in the regeneration column is heated to a temperature close to the boiling point of the absorbing liquid in order to heighten the regeneration degree thereof. When a heat exchanger being high in heat exchanging performance is used to heighten the recovery ratio of heat to make the temperature difference (T1−T2) small, the temperature t1 of the gas discharged from the first regenerating section 22a also becomes high. If the gas is discharged from the regeneration column 20 as it is, a large quantity of energy corresponding to the latent heat is also discharged, together with water vapor, as well as energy corresponding to the sensible heat. In the present invention, the heat quantity of the gas discharged from the first regenerating section 22a is recovered in the second regenerating section 22b to be used for the regeneration of the absorbing liquid, so that the temperature of the gas is lowered from t1 to t2 to reduce the quantity of the discharge of the sensible heat to the outside. Following the lowering in the gas temperature, the condensation of water vapor also advances, so that the water vapor and latent heat contained in the gas discharged from the second regenerating section 22b are also decreased. In the above-mentioned structure, condensed water from water vapor vaporized from the absorbing liquid is, in the absorption column 10, supplied to the second absorbing liquid A2, A2′ in the second absorbing section 12b while the condensed water is supplied, in the regeneration column 20, to the first absorbing liquid A1, A1′ in the second regenerating section 22b. However, if the vaporized amount from the second absorbing liquid A2 in the first regenerating section 22a is more than the amount of the condensed water supplemented in the second absorbing section 12b, the structure may be changed so that the condensed water in the gas-liquid separator 40 is used as dilution water for restraining a rise in the concentration of the second absorbing liquid. In a case where the first and second absorbing liquids having the same composition are used, a part of the first absorbing liquid may be mixed into the second absorbing liquid or a part of the second absorbing liquid may be mixed into the first absorbing liquid part, in order to equalize the respective concentrations of the first and second absorbing liquids that are varied by vaporization. In this case, an energy loss caused by the partial mixing of the absorbing liquids can be reduced by adjusting conditions (such as the circulating quantity of the absorbing liquid) for the driving. It is appropriate to mix the absorbing liquids with each other while the driving conditions are adjusted so as to make the first absorbing liquid A1 after regenerated and the second absorbing liquid A2′ after absorbing equivalent in the carbon dioxide concentration to each other.
When a heat exchanger high in heat exchanging performance is used as the second heat exchanger 34, in the second absorbing liquid part A2′ (rich solution part) in the second supplying path 17 extended from the second heat exchanger 34 to the first regenerating section 22a, bubbles of carbon dioxide are easily generated by a rise in the temperature. Thus, a case may occur where the bubbles hinder the conduction of heat so that a decrease in the temperature difference (T1−T2) is disturbed. In this case, the bubbles can be restrained by pouring the rich solution part into the second heat exchanger 34 in the state that the solution part is pressurized, so that the disturbance of the temperature rise of the rich solution part is cancelled. Consequently, the heat exchanging performance is projected onto the temperature difference between the heat exchanger inlet temperature of the lean solution part and the heat exchanger outlet temperature of the rich solution part, so that this temperature difference is reduced. Thus, thermal energy given by the heat exchanger is efficiently supplied into the regeneration stage. The above-described temperature difference at the heat exchange can be generally set to a temperature lower than 10° C., preferably about 3° C. In regard to the pressure applied to the absorbing liquid, it also works effective for promoting the discharge of carbon dioxide if it is released when the absorbing liquid part is charged into the regeneration treatment. For pouring the absorbing liquid into the second heat exchanger 34 in the state that the absorbing liquid is pressurized, for example, a back pressure valve is fitted onto the second supplying path 17 (for example, in the vicinity of an introduction port into the regenerating section 22a) between the second heat exchanger 34 and the regeneration column 20, whereby it is made possible to use the driving force of the pump 16 for pressurizing the absorbing liquid. In this case, the pressure can also be adjusted, using a pressure sensor. Similarly, it is also possible, for the absorbing liquid passing through the first heat exchanger 33, to restrain the bubbling by means of pressurization so that a rise in the temperature of the first absorbing liquid A1′ supplied into the second regenerating section 22b can easily be attained. If the pressure of the absorbing liquid in the pressurized state is released when the absorbing liquid is introduced into the regeneration column, the discharge of carbon dioxide is promoted. At this time, latent heat is consumed to produce a further advantageous effect of contributing to a lowering in the temperature of the discharged gas.
The recovery method performed in the recovery apparatus 1 in
In the absorption column 10, the gas G which contains carbon dioxide, such as a combustion exhaust gas or process exhaust gas, is supplied thereto through the bottom. The first and second absorbing liquids A1 and A2 are supplied to the first and second absorbing sections 12a and 12b, respectively, through the respective upper portions thereof. As a result, the gas G is brought into gas-liquid contact on the fillers 11a and 11b with the first and second absorbing liquids A1 and A2, so that carbon dioxide is absorbed into the absorbing liquids. Since carbon dioxide is satisfactorily absorbed at a low temperature, the liquid temperature of the absorbing liquids A1 and A2 or the temperature of the absorption column 10 (in particular, the fillers 11a and 11b) is generally adjusted to about 50° C. or lower, preferably 40° C. or lower. Since the absorbing liquids absorb carbon dioxide with generating heat, it is desired to pay attention to a matter that the liquid temperature should not be over 60° C., considering a rise in the liquid temperature by this heat generation. It is also appropriate, in regard to the gas G supplied into the absorption column 10, to use a cooling column to adjust the temperature thereof beforehand to an appropriate temperature, considering the above. For the first and second absorbing liquids A1 and A2, an aqueous liquid containing, as an absorbent, a compound having affinity with carbon dioxide is possibly used, respectively. For the absorbent, alkanolamines, hindered amines having an alcoholic hydroxyl group, and the like can be mentioned, and specific examples thereof include monoethanolamine, diethanolamine, triethanolamine, N-methyldietanolamine (MDEA), diisopropanolamine, and diglycolamine, which belong to alkanolamines; and 2-amino-2-methyl-1-propanol (AMP), 2-(ethylamino)ethanol (EAE), and 2-(methylamino)ethanol (MAE), which belong to hindered amines each having an alcoholic hydroxyl group. It is allowed to combine two or more kinds of the compounds as mentioned above to use in a mixture form. The absorbent concentration in each of the absorbing liquids may be appropriately set in accordance with the quantity of carbon dioxide contained in the gas which is a target to be treated, and the treating speed, the fluidity of the absorbing liquid, a consumption loss restraint thereof, and others. The absorbent is generally used in a concentration of about 10 to 50% by mass. For treatment of the gas G in which the content by percentage of carbon dioxide is, for example, about 20%, an absorbing liquid having the concentration of about 30% by mass is favorably used.
In the present invention, the first and second absorbing liquids A1 and A2 may be absorbing liquids identical with each other; or may be 1) absorbing liquids being different in absorbent concentration from each other, or 2) absorbing liquids being different in absorbent species or absorbent-contained composition from each other. For example, in regard to the embodiment of 1), when the absorbent concentration in the second absorbing liquid A2, which is relatively high in the temperature heated in the regeneration column 20, is set to be lower than that in the first absorbing liquid, the second absorbing liquid A2 can be restrained from thermal denaturation and be made high in heat resistance while the first absorbing liquid A1 can be made high in absorption capacity. Thus it becomes possible to select, among absorbents poor in heat resistance, an absorbent good in absorption performance and regeneration property (regeneration easiness) to use. In regard to the embodiment of 2), since the first absorbing section 12a has a condition that the carbon dioxide concentration in a gas to be treated is higher than that in the second absorbing section 12b so that the absorption of carbon dioxide is easy, selection of the absorbing liquids is made by giving priority to regeneration property of the absorbing liquid for the first absorbing liquid A1, while giving priority to absorption performance for the second absorbing liquid A2 that is brought into contact in the second absorbing section 12b in which the carbon dioxide concentration in the gas is relatively low. In accordance with this construction, it is made possible to make easy the regeneration of the absorbing liquids without lowering the absorbing efficiency as a whole, so as to reduce the energy required for the regeneration. By using an absorbing liquid good in regeneration property as the first absorbing liquid A1, the regeneration degree thereof at low temperature in the second regenerating section 22b is made high, so that the absorbing liquid flowing back into the first absorbing section 12a can be brought near to a lean solution. Monoethanolamine (MEA), which is favorably usable in general, is an absorbent of high absorption performance while AMP and MDEA are good in regeneration property. In order to improve AMP or MDEA in absorption performance, an absorbing liquid is frequently prepared by blending MEA into them, and the absorption performance and the regeneration property can be adjusted to some degree in accordance with the blend ratio. Therefore, when the first and second absorbing liquids in the present invention are prepared using this method, it is possible to perform the absorption and the regeneration are efficiently while taking advantage of properties of each of the absorbing liquids. For example, it is preferred for reducing regeneration energy to use, as the first absorbing liquid A1, an absorbing liquid which is relatively high in concentration of MDEA or AMP and good in regeneration property and use, as the second absorbing liquid A2, an absorbing liquid which is relatively high in MEA concentration and high in absorption performance.
The supplying rate of the gas G, and the circulating rates of the first and second absorbing liquids are appropriately set, respectively, so that the absorption is advanced satisfactorily, in view of the amount of carbon dioxide contained in the gas G, the carbon dioxide absorption capacity of the absorbing liquids, the gas-liquid contact efficiency in the filler, and others. By circulating each of the absorbing liquids, an absorption treatment and a regeneration treatment are repeatedly performed.
The second absorbing liquid A2′ in which carbon dioxide has been absorbed is supplied through the second supplying path 17 to the first regenerating section 22a. During this period, the second absorbing liquid A2′ is subjected to heat exchange with the second absorbing liquid A2 flowing back from regeneration column 20, so as to be heated. The temperature T1 of the second absorbing liquid A2 heated by external heat in the first regenerating section 22a is varied in accordance with composition of the used absorbing liquid and regenerating conditions. The temperature T1 is generally set into the range of about 100 to 130° C. (the boiling point or thereabout). On the basis of this, the heat exchanger outlet temperature of the second absorbing liquid A2′, that is, the introduction temperature T2 thereof into the second regenerating section 22a can be set into the range of about 95 to 125° C. The temperature t1 of the gas discharged from the first regenerating section 22a to the second regenerating section 22b turns into the range of about 85 to 115° C. The temperature T3 of the first absorbing liquid A1 heated in the second regenerating section 22b by the gas discharged from the first regenerating section 22a turns into the range of about 85 to 115° C. The heat exchange in the first heat exchanger 33 makes it possible to set, into the range of about 80 to 110° C., the temperature T4 of the first absorbing liquid A1′ introduced into the second regenerating section 22b. The temperature t2 of the gas discharged from the second regenerating section 22b is possibly lowered to 100° C. or lower.
In the case of pressurizing at least one of the first and second absorbing liquids A1′ and A2′ flowing in the first and second heat exchangers 33 and 34, respectively, it is appropriate to render the pressure a constant pressure of 150 kPaG or more, preferably 200 kPaG or more, more preferably 250 kPaG or more (provided that the pressure is about 900 kPaG or less, in view of the pressure resistance of the apparatus and others).
The second absorbing liquid A2 stored in the bottom of the regeneration column 20 is heated to the boiling point or thereabout by partial circulation heating. At this time, the boiling point of the absorbing liquid depends on the composition (absorbent concentration) and the pressure in the regeneration column 20. For the heating, necessary is the supply of vaporization latent heat of water, which is lost from the absorbing liquid, and sensible heat of the absorbing liquid, and, if the vaporization is restrained by increasing the pressure, the sensible heat is increased by a rise in the boiling point. Therefore, in view of the balance between them, it is preferred for energy efficiency to use the condition setting that the pressure in the regeneration column 20 is increased to about 100 kPaG and the absorbing liquid is heated into the range of 120 to 130° C. The increase in the pressure in the regeneration column 20 is adjustable by fitting a pressure regulating valve to an outlet of the exhaust pipe 38 and controlling the pressure.
In the second regenerating section 22b, the regeneration is performed at a temperature lower than that of the first regenerating section 22a, thereby making it possible to lower the temperature t2 of the upper portion of the regeneration column 20 to a temperature close to the temperature T4 of the poured first absorbing liquid A1′ (t2<t1, and T4<T3<t1). Consequently, the water vapor and the latent heat contained in the recovered gas passing through the condensing section 37 are decreased so that a loss of heat energy is reduced. In order to promote the regeneration of the absorbing liquid at a low temperature, it is important that the carbon dioxide content in the absorbing liquid is high. In this regard, the first absorbing liquid contacting the gas high in carbon dioxide concentration in the first absorbing section 12a easily becomes to have a relatively high content of carbon dioxide, and thus the first absorbing liquid is suitable for performing the regeneration with use of heat recovered in the second regenerating section 22b.
In this way, the first and second absorbing liquids A1 and A2 are circulated independently of each other between the absorption column 10 and the regeneration column 20, and the second regenerating section 22b for performing the regeneration at a lower temperature than that of the first regenerating section 22a is used to perform the regeneration treatment having two stages, thus improving the efficiency of energy in the regeneration column. It is also possible to regard the first and second absorbing liquids A1 and A2 that the first absorbing liquid A1 is an assistant absorbing liquid and the second absorbing liquid A2 is a main absorbing liquid. In this case, the function of the first absorbing liquid A1 includes the recovery and reuse of thermal energy in the regeneration column, as well as a decrease in absorption load which is given to the second absorbing liquid A2 by a gas of high carbon dioxide concentration. In short, the apparatus structure in
In a recovery apparatus having a conventional type of absorption column and regeneration column, an effect of the heat-exchanging efficiency of its heat exchanger is evaluated on the supposition that, in a simulating test for calculating regeneration energy required for the recovery of carbon dioxide, a 30% MEA solution in water is used as an absorbing liquid to treat a carbon-dioxide-containing gas into a carbon dioxide recovery ratio of 90%. In that case, when increasing the heat exchange performance (represented by a difference between the heat exchange inlet temperature of its return path and the heat exchange outlet temperature of its supplying path) of the heat exchanger from 10° C. to 3° C., the rich solution introduction temperature of the regeneration column is raised by 7° C. (the temperature is presumed to be 118° C.) and the regeneration energy is lowered from about 4.1 GJ/t-CO2 to about 3.9 GJ/t-CO2 by decrease of a sensible heat required for the temperature rise. In order to evaluate the structure of the present invention, an absorbing section and a regenerating section to be added for changing the recovery apparatus to the apparatus structure illustrated in
In the regeneration column 20′, expressions of t2>T5>T6, and t2>t3 are satisfied in which: T5 represents the temperature of the first absorbing liquid A1c heated, in the third regenerating section 22c, by the gas discharged from the first and second regenerating sections 22a and 22b; T6 represents that of the first absorbing liquid part A1′ introduced from the third heat exchanger 33′ into the upper portion of the third regenerating section 22c; and t3 represents that of the gas discharged from the third regenerating section 22c. Consequently, if the temperatures of T1 to T4 and t1 and t2 of the recovery apparatus in
In regard to the recovery apparatus 2 in
In the recovery apparatus 2 in
The present invention is usable for a treatment or some other operation of carbon-dioxide-containing gas discharged from thermal power plants, ironworks, boilers and other facilities, and is useful for reducing the amount of discharged carbon dioxide from them, the effect thereof onto the environment, and others. The invention provides a carbon dioxide recovery apparatus capable of reducing costs required for carbon dioxide collecting process, and contributing to energy saving and environmental protection.
As there are many apparently widely different embodiments of the present invention that may be made without departing from the spirit and scope thereof, it is to be understood that the invention is not limited to the specific embodiments thereof, except as defined in the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2011-236829 | Oct 2011 | JP | national |
This application is a continuation application of International Application No. PCT/JP2012/076073, filed on Oct. 9, 2012, which claims priority of Japanese Patent Application No. 2011-236829, filed on Oct. 28, 2011, the entire contents of which are incorporated by references herein.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/JP2012/076073 | Oct 2012 | US |
| Child | 14248764 | US |
