Patent Application
20130220122
This application is based upon and claims the benefit of priority from the prior Japanese Patent Application No. 2012-40288, filed on Feb. 27, 2012, the entire contents of which are incorporated herein by reference.
Embodiments described herein relate to a carbon dioxide separating and collecting system and a method of operating the same.
In recent years, importance of a problem of global warming has become increased due to the greenhouse effect of carbon dioxide (CO2) which is combustion products of fossil fuels. With such a background, studies are energetically made regarding a method of separating and collecting carbon dioxide in a combustion exhaust gas by bringing the combustion exhaust gas into contact with an amine-containing absorbing liquid, and a method of storing the collected carbon dioxide without emitting the carbon dioxide to the atmosphere, with regard to a thermal power station and the like which use a large amount of fossil fuels.
An example of the method of separating and collecting the carbon dioxide by using the absorbing liquid is a method which includes a step of bringing the combustion exhaust gas into contact with the absorbing liquid in an absorbing tower to cause the absorbing liquid to absorb the carbon dioxide in the combustion exhaust gas, and a step of heating the absorbing liquid which has absorbed the carbon dioxide in a regenerating tower to release the carbon dioxide from the absorbing liquid. The absorbing liquid which released the carbon dioxide and is regenerated is circulated to the absorbing tower again and is reused.
When this method is conducted, the amount of energy required in the step of releasing the carbon dioxide is enormous. Therefore, in this method, the amount of the energy is reduced by preheating a low-temperature absorbing liquid (rich liquid) which is discharged from the absorbing tower by using a high-temperature absorbing liquid (lean liquid) which is discharged from the regenerating tower and then supplying the preheated absorbing liquid to the regenerating tower. This preheating treatment is conducted by a regenerative heat exchanger which supplies heat quantity of the high-temperature absorbing liquid to the low-temperature absorbing liquid.
Embodiments will now be explained with reference to the accompanying drawings.
The high-temperature absorbing liquid and low-temperature absorbing liquid, however, usually circulate in a state of a liquid phase, so that the heat transfer characteristics between these absorbing liquids are low. Therefore, the regenerative heat exchanger is required to have a wide heat transfer area. As a result, the size of the regenerative heat exchanger becomes large.
Furthermore, when it is attempted to bring the temperature of the low-temperature absorbing liquid close to the operation temperature of the regenerating tower as much as possible by the regenerative heat exchanger, the temperature difference between the high-temperature absorbing liquid and the low-temperature absorbing liquid becomes very small in the vicinity of the outlet of the regenerative heat exchanger. Therefore, the heat transfer characteristics between these absorbing liquids become very low in the vicinity of the outlet of the regenerative heat exchanger. As a result, the size of the regenerative heat exchanger is required to be further large. On the other hand, if the low-temperature absorbing liquid is supplied to the regenerating tower in a state in which the above described temperature difference is large, the effect of reducing the energy consumption in the regenerating tower by the regenerative heat exchanger becomes small.
In one embodiment, a carbon dioxide separating and collecting system includes an absorbing tower configured to cause an absorbing liquid to absorb carbon dioxide, and discharge a rich liquid which is the absorbing liquid which has absorbed the carbon dioxide. The system further includes a regenerating tower configured to cause the absorbing liquid to release a gas containing the carbon dioxide, and discharge the released gas and a lean liquid which is the absorbing liquid having a dissolved carbon dioxide concentration lower than a dissolved carbon dioxide concentration of the rich liquid. The system further includes a regenerative heat exchanger configured to heat the rich liquid flowing between the absorbing tower and the regenerating tower by using heat of the lean liquid flowing between the regenerating tower and the absorbing tower. A discharge port of the rich liquid of the regenerative heat exchanger is disposed at a higher position than a supply port of the rich liquid of the regenerating tower so that the rich liquid discharged from the regenerative heat exchanger contains a descending flow by which a value of liquid head pressure loss in a path from the discharge port to the supply port becomes negative, and an absolute value of the liquid head pressure loss becomes larger than an absolute value of flow friction pressure loss in the path from the discharge port to the supply port.
The carbon dioxide separating and collecting system of
The combustion exhaust gas sent from a thermal power station and the like is introduced into the lower part of the absorbing tower 1 through the combustion exhaust gas supply port 3. The absorbing tower 1 brings the combustion exhaust gas in contact with an absorbing liquid, and causes the absorbing liquid to absorb carbon dioxide in the combustion exhaust gas. The absorbing liquid is introduced from the upper part of the absorbing tower 1, passes through the absorbing-tower packed bed 2 which has been filled with a filler for enhancing the efficiency of gas-liquid contact, and flows down the inside of the absorbing tower 1. In the present embodiment, a mixture of an amine compound and water, for instance, is used as the absorbing liquid.
Most of the carbon dioxide in the combustion exhaust gas is absorbed by the absorbing liquid, and an exhaust gas in which the carbon dioxide content has been decreased is discharged from the top of the absorbing tower 1. This exhaust gas is cooled by the absorbing-tower reflux condenser 14, its moisture is condensed, then the moisture is separated from the exhaust gas by the gas-liquid separator 15, and the resultant exhaust gas is discharged to the outside of the system. On the other hand, the separated moisture contains a component of the absorbing liquid, and accordingly is returned to the absorbing tower 1.
The rich liquid which is the absorbing liquid that has absorbed the carbon dioxide is accumulated in the bottom part of the absorbing tower 1. The rich liquid which has been accumulated in the bottom part of the absorbing tower 1 is discharged from the bottom part of the absorbing tower 1, and is supplied into the regenerating tower 6 through the regenerative heat exchanger 5 by the rich-liquid transferring pump 4. This rich liquid is introduced from the upper part of the regenerating tower 6, passes through the regenerating-tower packed bed 7 which has been filled with a filler for enhancing the efficiency of gas-liquid contact, and flows down the inside of the regenerating tower 6.
As a result, the absorbing liquid is accumulated in the bottom part of the regenerating tower 6. A part of the absorbing liquid which has been accumulated in the bottom part of the regenerating tower 6 is discharged from the bottom part of the regenerating tower 6, and is circulated between the regenerating tower 6 and the regenerating tower reboiler 8. On this occasion, this absorbing liquid is heated by a reboiler heating medium which has been supplied from the reboiler-heating medium supply port 9, and generates its vapor. The generated vapor is returned to the inside of the regenerating tower 6, passes and rises through the regenerating-tower packed bed 7, and heats the flowing-down absorbing liquid. As a result, the carbon dioxide gas and water vapor are released from the absorbing liquid in the regenerating tower 6.
The exhaust gas containing the released carbon dioxide gas and water vapor is discharged from the top of the regenerating tower 6. This exhaust gas is cooled by the regenerating-tower reflux condenser 16, its moisture is condensed, and the moisture is separated from the exhaust gas by the gas-liquid separator 17, and the exhaust gas becomes a gas containing only the carbon dioxide and is discharged to the outside of the system from the collected CO2 discharge line 18. On the other hand, the separated moisture contains the component of the absorbing liquid, and accordingly is returned to the regenerating tower 6.
On the other hand, the lean liquid which is an absorbing liquid having a dissolved CO2 concentration lower than that of the rich liquid is accumulated in the bottom part of the regenerating tower 6. The lean liquid which has been accumulated in the bottom part of the regenerating tower 6 is discharged from the bottom part of the regenerating tower 6, and is pooled in the lean liquid tank 11 through the regenerative heat exchanger 5 by the lean-liquid transferring pump 10. The pooled lean liquid is supplied into the absorbing tower 1 through the lean liquid cooler 13 by the lean-liquid returning pump 12. This lean liquid is introduced from the upper part of the absorbing tower 1, and is reused for collecting the carbon dioxide.
(1) Details of Regenerative Heat Exchanger 5
Details of the regenerative heat exchanger 5 will be described below with reference to
The regenerative heat exchanger 5 is arranged in a point at which a rich liquid line that extends from the absorbing tower 1 toward the regenerating tower 6 intersects with a lean liquid line that extends from the regenerating tower 6 toward the absorbing tower 1. This lean liquid has a remaining heat which the lean liquid has acquired when having been heated by the regenerating tower reboller 8, and the regenerative heat exchanger 5 heats a rich liquid flowing through the rich liquid line by using the heat of this lean liquid.
Reference character A1 illustrated in
In the present embodiment, the discharge port A3 of the rich liquid of the regenerative heat exchanger 5 is disposed at a higher position than the supply port A4 of the rich liquid of the regenerating tower 6. As a result, at least a part of the pipe T1 forms a down corner (descending pipe), so that the rich liquid flowing in the pipe T1 contains a descending flow.
The reason why the discharge port A3 is disposed at a higher position than the supply port A4 will be described below.
Suppose that a pressure at the discharge port A3 of the regenerative heat exchanger 5 is represented by “PEXO”, and an operation pressure of the regenerating tower 6 is represented by “PRG”. Then, the relationship of Expression (1) holds between these pressures.
P
EXO
=ΔP
F
+ΔP
H
+P
RG (1)
Here, “ΔPF” and “ΔPH” respectively represent flow friction pressure loss and liquid head pressure loss which are generated in a path from the discharge port A3 of the regenerative heat exchanger 5 and to the supply port A4 of the regenerating tower 6.
The value of “ΔPF” can be calculated from a computation expression of a flow friction loss in a pipe, which is described in a handbook concerning mechanical engineering and the like. On the other hand, “ΔPH” is expressed by the following Expression (2).
ΔPH=−ρmgH (2)
Here, “ρm” represents an average density of a fluid flowing through the pipe T1. In addition, “H” represents a height difference obtained by subtracting the height of the supply port A4 from the height of the discharge port A3. In addition, “g” represents gravitational acceleration.
Therefore, if the discharge port A3 has been provided at a lower position than the supply port A4, the value of “ΔPH” becomes positive, but as in the present embodiment, when the discharge port A3 is provided at a higher position than the supply port A4, the value of “ΔPH” becomes negative. Therefore, in the present embodiment, when an absolute value of “ΔPH” is larger than an absolute value of “ΔPF”, the value of “PEXO” results in being smaller than the value of “PRG”. In other words, the pressure “PEXO” at the discharge port A3 of the regenerative heat exchanger 5 becomes lower than the operation pressure “PRG” of the regenerating tower 6.
Therefore, according to the present embodiment, it becomes possible to lower the pressure in the regenerative heat exchanger 5 by structuring the system so that the absolute value of “ΔPH” becomes larger than the absolute value of “ΔPF”.
As a result of having made an extensive investigation, the present inventors have found out that when the pressure in the regenerative heat exchanger 5 is lowered, the following phenomena occur.
Firstly, it has been found that when the pressure in the regenerative heat exchanger 5 is set at a certain value or lower, the carbon dioxide gas is dissociated from the rich liquid and moisture evaporates while the rich liquid is heated in the regenerative heat exchanger 5. In this case, the rich liquid in the regenerative heat exchanger 5 and the rich liquid which is discharged from the discharge port A3 form a gas-liquid two-phase flow which contains gases of the liquids.
Secondly, it has been found that when the rich liquid becomes the gas-liquid two-phase flow in the regenerative heat exchanger 5, the heat transfer characteristics in the regenerative heat exchanger 5 become high. The reason is because the heat of the lean liquid can be recovered not only as a sensible heat of the rich liquid but also as a latent heat such as a dissociation heat of the carbon dioxide gas and the heat of vaporization of water. As a result, even when a temperature difference between the rich liquid and the lean liquid is not decreased so much, the recovered heat quantity in the regenerative heat exchanger 5 can be increased.
Therefore, in the present embodiment, the discharge port A3 of the rich liquid of the regenerative heat exchanger 5 is disposed at a higher position than the supply port A4 of the rich liquid of the regenerating tower 6. Specifically, a height difference between the discharge port A3 and the supply port A4 is set at a value so that the rich liquid which is discharged from the regenerative heat exchanger 5 becomes a gas-liquid two-phase flow. As a result, in the present embodiment, the recovered heat quantity in the regenerative heat exchanger 5 can be increased by such a simple structure that the discharge port A3 is set at a higher position than the supply port A4.
A height difference at which the rich liquid that is discharged from the regenerative heat exchanger 5 becomes the gas-liquid two-phase flow varies depending on the shape of the pipe T1. It is considered that as the pipe T1 becomes longer, the flow friction pressure loss “ΔPF” becomes larger in many cases and accordingly a necessary height difference becomes larger.
In addition, when the pressure in the regenerative heat exchanger 5 is lowered, a temperature is lowered at which the dissociation of the carbon dioxide gas and the evaporation of the moisture start. Therefore, in the present embodiment, such a design is adopted that the pressure in the regenerative heat exchanger 5 becomes lower, and thereby it becomes possible to lower the above described starting temperature and more surely make the rich liquid shift to a gas-liquid two-phase state.
According to the present embodiment, the regenerative heat exchanger 5 can recover a sufficient heat quantity even though a temperature difference between the rich liquid and the lean liquid in its inside is large, and accordingly the regenerative heat exchanger 5 can get smaller. Alternatively, the system of the present embodiment can reduce a temperature difference between the rich liquid and the lean liquid without increasing the size of the regenerative heat exchanger 5, and accordingly can recover a sufficient heat quantity by a compact regenerative heat exchanger 5.
As a result, the system of the present embodiment can reduce the amount of energy which is input from the outside for releasing carbon dioxide from the absorbing liquid in the regenerating tower 6.
(2) Measurement Results of Pressure Loss
Measurement results of pressure loss will be described below with reference to
A horizontal axis X of
It is understood from
When the fluid flowing through the pipe T1 becomes only a liquid phase, a liquid density of the above described an average density “ρm” equals to a liquid density “ρL”. On the other hand, when the fluid flowing through the pipe T1 is the gas-liquid two-phase flow, the average density “ρm” of this fluid is represented by the following Expression (3).
ρm=αmρG+(1−αm)ρL (3)
Here, “ρG” represents a density of a mixed gas containing carbon dioxide gas and a water vapor. In addition, “αm” is an average value of an area ratio of a gas phase which occupies in the cross section of the pipe T1. The value of “αm” largely varies depending on the weight flow rate percentage X, the diameter of the pipe and the like.
(3) Effects of First Embodiment
Effects of the first embodiment will be described below.
As has been described above, in the present embodiment, the discharge port A3 of the rich liquid of the regenerative heat exchanger 5 is disposed at a higher position than the supply port A4 of the rich liquid of the regenerating tower 6 so that the rich liquid which is discharged from the regenerative heat exchanger 5 becomes the gas-liquid two-phase flow.
Therefore, according to the present embodiment, the recovered heat quantity in the regenerative heat exchanger 5 can be increased by such a simple structure that the discharge port A3 is set at a higher position than the supply port A4. As a result, the system of the present embodiment can reduce the amount of energy which is input from the outside for releasing carbon dioxide from the absorbing liquid in the regenerating tower 6.
The carbon dioxide separating and collecting system of
The first gas-liquid separator 21 is disposed between the regenerative heat exchanger 5 and the regenerating tower 6, and separates the rich liquid which has been discharged from the regenerative heat exchanger 5 into a gas and a liquid. Reference characters B1, B2 and B3 denote a supply port of the rich liquid, a discharge port of the liquid and a discharge port of the gas, respectively, in the first gas-liquid separator 21. The liquid and the gas which have been discharged from the discharge ports B2 and B3 are supplied into the regenerating tower 6 from the supply ports A4 and B4, respectively. This liquid (semi-lean liquid) is transferred to the regenerating tower 6 by the first semi-lean liquid transferring pump 22.
In the present embodiment, the discharge port A3 of the rich liquid of the regenerative heat exchanger 5 is disposed at a higher position than the supply port B1 of the rich liquid of the first gas-liquid separator 21. As a result, at least a part of the pipe T1 which extends from the discharge port A3 toward the supply port B1 forms a down corner (descending pipe), so that the rich liquid flowing in the pipe T1 contains a descending flow. On the other hand, the discharge port B2 of the semi-lean liquid of the first gas-liquid separator 21 may be disposed at a lower position than the supply port A4 of the semi-lean liquid of the regenerating tower 6.
Next, subsequently with reference to
Suppose that a pressure in the gas discharge port B3 of the first gas-liquid separator 21 is represented by “PSP”, and an operation pressure of the regenerating tower 6 is represented by “PRG”. Then, the relationship of Expression (4) holds between these pressures.
P
SP
=ΔP
FG
+P
RG (4)
Here, “ΔPFG” represents flow friction pressure loss in a pipe T2 which extends from the discharge port B3 toward the supply port B4.
In this way, “PSP” becomes higher than “PRG” only by “ΔPFG”. However, if the diameter of the pipe T2 has been set to be large to some extent, “ΔPFG” is suppressed to a small value because the flow rate of the gas is small. Therefore, as in the following Expression (5), the pressure “PSP” of the first gas-liquid separator 21 is considered to be approximately equal to the operation pressure “PRG” of the regenerating tower 6.
P
SP
≈P
RG (5)
Therefore, a relationship between the pressure “PEXO” of the regenerative heat exchanger 5 and the pressure “PSP” of the first gas-liquid separator 21 in the present embodiment becomes similar to the relationship between the pressure “PEXO” of the regenerative heat exchanger 5 and the pressure “PRG” of the regenerating tower 6 in the first embodiment.
Therefore, in the present embodiment, the discharge port A3 of the rich liquid of the regenerative heat exchanger 5 is disposed at a higher position than the supply port B1 of the rich liquid of the first gas-liquid separator 21. Specifically, a height difference between the discharge port A3 and the supply port B1 is set at such a value that the rich liquid which is discharged from the regenerative heat exchanger 5 becomes a gas-liquid two-phase flow.
As a result, in the present embodiment, the recovered heat quantity in the regenerative heat exchanger 5 can be increased with such a simple structure that the discharge port A3 is set at a higher position than the supply port B1. Thereby, in the present embodiment, the system can reduce the amount of energy which is input from the outside for releasing carbon dioxide from the absorbing liquid in the regenerating tower 6.
The method of separately introducing the gas and the liquid into the regenerating tower 6 as in the present embodiment has such an advantage as to be capable of reducing the collision of the droplet entrained in the gas with the inner wall of the regenerating tower 6 and suppressing the corrosion of the inner wall of the regenerating tower 6, as compared to the method of introducing the gas-liquid two-phase flow into the regenerating tower 6 as in the first embodiment.
The carbon dioxide separating and collecting system of
The flow splitting apparatus 31 is disposed between the absorbing tower 1 and the regenerative heat exchanger 5, and splits the rich liquid flowing between the tower and the heat exchanger into first and second rich liquids. Then, the first rich liquid is supplied to the regenerative heat exchanger 5, and the second rich liquid is supplied to the CO2 emitter 32. A distribution ratio of the first and second rich liquids is 85 to 90% to 10 to 15%, for instance.
The CO2 emitter 32 is disposed between the flow splitting apparatus 31 and the regenerating tower 6, heats the second rich liquid by the heat of the exhaust gas which has been discharged from the regenerating tower 6, and causes the second rich liquid to release the carbon dioxide. The CO2 emitter 32 discharges a third rich liquid which is an absorbing liquid having a dissolved CO2 concentration lower than that of the second rich liquid, and supplies the third rich liquid into the regenerating tower 6. The carbon dioxide which has been emitted in the CO2 emitter 32 is sent to the regenerating tower 6 together with the third rich liquid, and is discharged from the regenerating tower 6 together with the above described exhaust gas.
Reference characters C1 and C2 illustrated in
In the present embodiment, the discharge port C2 of the CO2 emitter 32 is disposed at a higher position than the supply port C3 of the regenerating tower 6. Specifically, a height difference between the discharge port C2 and the supply port C3 is set at such a value that the third rich liquid which is discharged from the CO2 emitter 32 becomes a gas-liquid two-phase flow.
As a result, in the present embodiment, the recovered heat quantity in the CO2 emitter 32 can be increased with such a simple structure that the discharge port C2 is set at a higher position than the supply port C3. Thereby, in the present embodiment, the system can reduce the amount of energy which is input from the outside for releasing carbon dioxide from the absorbing liquid in the regenerating tower 6.
As has been described above, in the present embodiment, the system recovers a remaining heat of the lean liquid by the regenerative heat exchanger 5, and simultaneously recovers a remaining heat of the exhaust gas by the CO2 emitter 32. Furthermore, in the present embodiment, the discharge port A3 of the regenerative heat exchanger 5 and the discharge port C2 of the CO2 emitter 32 are disposed at higher positions than the supply ports A4 and C3 of the regenerating tower 6, respectively so that both of the first rich liquid which is discharged from the regenerative heat exchanger 5 and the third rich liquid which is discharged from the CO2 emitter 32 form a gas-liquid two-phase flow.
An effect of disposing the discharge port A3 of the regenerative heat exchanger 5 at a higher position than the supply port A4 of the regenerating tower 6 will be described below, which is shown when the CO2 emitter 32 is disposed.
In the case in which the rich liquid is split as in the present embodiment, if a conventional regenerative heat exchanger 5 has been used which recovers the heat of the lean liquid only by a sensible heat of the rich liquid, the heat quantity which is recovered in the regenerative heat exchanger 5 results in decreasing by an amount of decrease in the flow rate of the rich liquid which is supplied to the regenerative heat exchanger 5.
However, the regenerative heat exchanger 5 of the present embodiment recovers the heat of the lean liquid by the sensible heat and the latent heat of the rich liquid, and accordingly does not decrease the heat quantity to be recovered even when the flow rate of the rich liquid decreases, by controlling the pressure in the regenerative heat exchanger 5. Therefore, according to the embodiment, the recovered heat quantity of the whole system can be increased by the amount of the heat quantity which has been recovered by the CO2 emitter 32.
Therefore, in the present embodiment, when the regenerative heat exchanger 5 and the CO2 emitter 32 are disposed, the discharge port A3 of the regenerative heat exchanger 5 is disposed at a higher position than the supply port A4 of the regenerating tower 6 so that the first rich liquid which is discharged from the regenerative heat exchanger 5 becomes a gas-liquid two-phase flow. Therefore, according to the present embodiment, the recovered heat quantity of the whole system can be more increased than that of the case in which only the regenerative heat exchanger 5 is disposed.
Furthermore, in the present embodiment, when the regenerative heat exchanger 5 and the CO2 emitter 32 are disposed, the discharge port C2 of the CO2 emitter 32 is disposed at a higher position than the supply port C3 of the regenerating tower 6 so that the third rich liquid which is discharged from the CO2 emitter 32 becomes the gas-liquid two-phase flow. Therefore, according to the present embodiment, the recovered heat quantity in the CO2 emitter 32 can be increased, and the heat quantity to be recovered in the whole system can be further increased.
As a result, according to the present embodiment, the amount of energy can be reduced which is input from the outside for releasing the carbon dioxide from the absorbing liquid in the regenerating tower 6.
The result of
The carbon dioxide separating and collecting system of
The second gas-liquid separator 41 is disposed between the CO2 emitter 32 and the regenerating tower 6, and separates the third rich liquid which has been discharged from the CO2 emitter 32 into a gas and a liquid. Reference characters D1, D2 and D3 denote a supply port of the third rich liquid, a discharge port of the liquid, and a discharge port of the gas in the second gas-liquid separator 41, respectively. The liquid which has been discharged from the discharge port D2 is supplied into the regenerating tower 6 from the supply port C3. This liquid (semi-lean liquid) is transferred to the regenerating tower 6 by the second semi-lean liquid transferring pump 42.
In the present embodiment, the discharge port C2 of the third rich liquid of the CO2 emitter 32 is disposed at a higher position than the supply port D1 of the third rich liquid of the second gas-liquid separator 41. As a result, at least a part of the pipe T3 which extends from the discharge port C2 toward the supply port D1 forms a down corner (descending pipe), so that the third rich liquid flowing in the pipe T3 contains a descending flow. On the other hand, the discharge port D2 of the semi-lean liquid of the second gas-liquid separator 41 may be disposed at a lower position than the supply port C3 of the semi-lean liquid of the regenerating tower 6.
In addition, the flow joining apparatus 43 causes the exhaust gas which has been discharged from the regenerating tower 6 to join a gas which has been discharged from the first gas-liquid separator 21 and a gas which has been discharged from the second gas-liquid separator 41 therein, and supplies the joined gas to the CO2 emitter 32. Reference characters T2 and T4 denote pipes which extend from the discharge ports B3 and D3 toward the CO2 emitter 32, respectively. In this way, in the present embodiment, not only a remaining heat of the exhaust gas but also a remaining heat of the gas after the gas-liquid separation can be recovered.
In the present embodiment, at least any one of these gases may be supplied into the regenerating tower 6, in a similar way to that in the second embodiment. The method of separately introducing the gas and the liquid into the regenerating tower 6 has such an advantage as to be capable of reducing the collision of the droplet entrained in the gas with the inner wall of the regenerating tower 6 and suppressing the corrosion of the inner wall of the regenerating tower 6, as compared to the method of introducing the gas-liquid two-phase flow into the regenerating tower 6.
Next, subsequently with reference to
The above described relationships of Expression (4) and Expression (5) hold also for the pipe T4, similarly to the pipe T2. Therefore, a relationship between the pressure of the CO2 emitter 32 and the pressure of the second gas-liquid separator 41 in the present embodiment becomes similar to the relationship between the pressure of the CO2 emitter 32 and the pressure of the regenerating tower 6 in the third embodiment.
Therefore, in the present embodiment, the discharge port C2 of the third rich liquid of the CO2 emitter 32 is disposed at a higher position than the supply port D1 of the third rich liquid of the second gas-liquid separator 41. Specifically, a height difference between the discharge port C2 and the supply port D1 is set at such a value that the third rich liquid which is discharged from the CO2 emitter 32 becomes a gas-liquid two-phase flow.
As a result, in the present embodiment, the heat quantity to be recovered in the CO2 emitter 32 can be increased with such a simple structure that the discharge port C2 is set at a higher position than the supply port D1. Thereby, in the present embodiment, the system can reduce the amount of energy which is input from the outside for releasing carbon dioxide from the absorbing liquid in the regenerating tower 6.
The carbon dioxide separating and collecting system and the method of operating the same in at least one of the above described embodiments can increase the recovered heat quantity in the regenerative heat exchanger.
While certain embodiments have been described, these embodiments have been presented by way of example only, and are not intended to limit the scope of the inventions. Indeed, the novel systems and methods described herein may be embodied in a variety of other forms; furthermore, various omissions, substitutions and changes in the form of the systems and methods described herein may be made without departing from the spirit of the inventions. The accompanying claims and their equivalents are intended to cover such forms or modifications as would fall within the scope and spirit of the inventions.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2012-040288 | Feb 2012 | JP | national |
