Technical field
[0001]
　The present invention, CO which attained energy savings 2 recovery apparatus and a CO 2 for the return process.
BACKGROUND
[0002]
　In recent years, as one of the causes of the global warming phenomenon, CO 2 greenhouse effect has been pointed out by, international also the measures on protecting the global environment has become an urgent task. CO 2 as the source of Oyobi by any human activities combusting fossil fuels, there are increasing demands for its emissions. The target power generation facilities such as thermal power plants using large amounts of fossil fuels Accordingly, the flue gas of a boiler for example, an amine-based CO 2 is contacted with the absorption liquid, CO in the combustion exhaust gas 2 method removing, recovering and recovered CO 2 method of storing without the release to the atmosphere has been studied extensively.
[0003]
　CO from flue gas 2 CO with absorption liquid 2 as a method for removing and recovering, in the absorption tower combustion exhaust gas and CO 2 is brought into contact with absorption liquid, CO 2 is heated in the regeneration tower absorbing solution having absorbed CO 2 reproduces the absorbing liquid together to liberate, that the regenerated absorbing liquid is recirculated to the absorption tower for reuse is employed (Patent Document 1).
[0004]
　CO, such as flue gas 2 from gas containing CO 2 in the method of absorbing and removing and recovering, it is necessary to install by adding the absorption tower and the regeneration tower to the combustion equipment. Therefore, the cost of the non-installation costs, for example, must also be reduced as much as possible the operating costs. In particular, when reproducing the absorbing solution, CO 2 and CO 2 to be released from the absorbing solution, so consumes a large amount of heat energy (steam), it is required to be energy-saving process as much as possible in the process of reproduction.
[0005]
　Therefore, conventionally, the rich solution discharged from the absorption tower, and a first heat exchanger and the diversion device for diverting the second heat exchanger for cooling the carbon dioxide containing steam for cooling the lean solution, rich solution introduced into the first heat exchanger and the second heat exchanger, after exchanging lean solution and carbon dioxide containing steam and heat, respectively, CO 2 carbon dioxide as supplied to the regenerator to dissipate there are proposals for recovery device (Patent Document 2).
CITATION
Patent Document
[0006]
Patent Document 1: JP 2003-225537 Patent Publication
Patent Document 2: JP 2009-214089 JP
Summary of the Invention
Problems that the Invention is to Solve
[0007]
　However, the proposal of Patent Document 2, CO 2 branches the rich solution that has absorbed at the preceding stage of the lean-rich solution heat exchanger is a first heat exchanger, a branched rich solution, the top portion of the regenerator although it supplied to the regenerator while heating is heat exchanged with the carbon dioxide-containing steam exhausted from, branched rich solution is to be supplied to the upper than the rich solution, if heated bifurcated rich solution is insufficient can not satisfactory reproduction can not be achieved a stable energy-saving, there is a problem that. Further, the absorption liquid because they are recycled, when withdrawn branches a part of the rich solution in the preceding stage of the lean-rich solution heat exchanger, rich lean solution in the lean-rich solution heat exchanger cooling efficiency is deteriorated by a solution, there is a problem that. As a result, cooler installed in front of introducing into the absorber, it is necessary to increase the cooling capacity to cool the lean solution, there is a problem that.
[0008]
　In view of the above problems, while achieving a stable energy-saving, more CO with improved energy efficiency 2 recovery apparatus and a CO 2 and to provide a recovery method.
Means for Solving the Problems
[0009]
　According to a first aspect of the present invention, CO 2 CO containing 2 containing exhaust gas and CO 2 by contacting the absorption liquid, the CO 2 CO from exhaust gas containing 2 CO removing 2 and absorption tower, CO 2 and from absorbed rich solution CO 2 are separated, CO as lean solution 2 and absorbent regenerator to regenerate the absorbing solution, the rich solution the CO 2 rich from the bottom of the absorption tower of the top side of the absorbent regenerator between the solution supply unit to supply the rich solution supply line, and the rich-lean solution heat exchanger and said lean solution and the rich solution to heat exchange, and the rich lean solution heat exchanger and the absorbing solution regeneration tower the branches the part of the rich solution in the first branch portion of the rich solution supply line is provided, said bifurcated rich solution the absorbent regenerator than said top side bottom side first side wall of the provided in the supply position A first rich-solution branch line that is provided in the first rich-solution branch line, the first rich solution heat exchanger for preheating the rich solution that is branched by the first branching portion, the first provided between the rich solution the first branch portion and the first rich solution heat exchanger of the branch line, the so rich solution is preheated to a predetermined temperature in the first rich-solution heat exchanger , characterized by comprising, a first flow control device for controlling the flow rate of the rich solution that is branched by the first branching unit.
[0010]
　According to a second aspect of the present invention, CO 2 CO containing 2 containing exhaust gas and CO 2 by contacting the absorption liquid, the CO 2 CO from exhaust gas containing 2 CO removing 2 and absorption tower, CO 2 and absorbed CO 2 from the rich solution is absorbing liquid CO 2 separates CO 2 using the absorbent regenerator to regenerate the absorbing solution as a lean solution, wherein the absorbent regenerator CO at 2 CO has been removed 2 absorption the liquid wherein the CO 2 CO circulating reused in the absorption tower 2 to a recovery method, the CO 2 comprising the steps of heat exchange and a lean solution which is delivered with the rich solution sent from the absorption tower from the absorbent regenerator the rich solution supply portion of the absorbent regenerator the top side of, and in order to supply on the side wall located on the lower side of the rich solution supply unit, the steps of branching the heat exchanged rich solution, of the side wall preheating the rich solution supplied to the supply position It includes a floor, a, in the step of branching the heat exchanged rich solution, CO is supplied from the rich solution supply portion of the top side of the absorbent regenerator 2 and the temperature of the rich solution is partially removed, the temperature of the absorbing solution regeneration tower branched rich solution supplied from the side wall of the same, or CO 2 so that when the temperature is higher temperatures some removed rich solution, the rich solution to be heat exchanged and adjusting the branching amount.
Effect of the invention
[0011]
　According to the present invention, after preheating the branched rich solution, when supplying a first supply position of the absorption solution regeneration tower, CO of the absorbent regeneration tower 2 temperature of the rich solution is partly removed substantially the same, or CO and 2 so that the temperature is higher in the temperature of a portion removed rich solution, a branch of branched rich solution was adjusted at a flow rate adjusting device, to preheat the branched rich solution since the introduction, without occurs unevenness in temperature in the absorption liquid regenerator of the joined liquid, CO 2 was released efficiently, it is possible to obtain a high energy saving effect. As a result, the, CO can be reduced steam amount required reboiler 2 can be reduced the required amount of cooling water in the lean solution cooler for cooling the lean solution to be introduced into the absorption tower.
BRIEF DESCRIPTION OF THE DRAWINGS
[0012]
[1] Figure 1, CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device.
FIG. 2 is another CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device.
FIG. 3 is another CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device.
FIG. 4 is, CO according to the second embodiment 2 is a schematic diagram showing the structure of a recovery device.
FIG. 5 is, CO according to Example 3 2 is a schematic diagram showing the structure of a recovery device.
FIG. 6 is, CO according to Example 4 2 is a schematic diagram showing the structure of a recovery device.
FIG. 7 is, CO according to Example 5 2 is a schematic diagram showing the structure of a recovery device.
FIG. 8 is, CO according to Example 6 2 is a schematic diagram showing the structure of a recovery device.
[9] FIG. 9, CO according to Example 7 2 is a schematic diagram showing the structure of a recovery device.
[10] Figure 10, CO according to Example 8 2 is a schematic diagram showing the structure of a recovery device.
DESCRIPTION OF THE INVENTION
[0013]
　It will be described in detail with reference to the drawings the present invention. It should be understood that the present invention be limited by the following examples of the present invention. In addition, constituent elements in the embodiments, those skilled in the art can be easily assumed, of substantially the same, include those in the range of so-called equivalents. Furthermore, the components disclosed in the following examples can be appropriately combined.
Example 1
[0014]
　1, CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 1, CO according to the present embodiment 2 recovery apparatus 10A, CO 2 CO containing 2 containing exhaust gas (hereinafter "exhaust gas") 11 and CO 2 by contacting the absorption liquid 12, from the exhaust gas 11 CO 2 CO removing 2 and absorption tower (hereinafter referred to as "absorption column") 13, CO 2 CO from the rich solution 14 having absorbed 2 to separate, CO 2 and lean solution 15 to play the absorbing liquid 12 the absorbent regenerator (the "regenerator" hereinafter) 16, the rich solution 14 rich solution supplied to the rich solution supply portion 16c of top 16a side near the regeneration column 16 from the bottom 13b supply line L of the absorption column 13 to 11 and , the rich solution 14 and the lean solution 15 and the rich lean solution heat exchanger 21 for exchanging heat, the rich-solution supply line L is provided between the rich lean solution heat exchanger 21 and the regenerator 16 11 first of the branch portion A- In branches the part of the rich solution 14, the bifurcated fed by the first inlet portion 24 of the supply position B-1 of the side wall of the bottom portion 16b side from the rich solution supply portion 16c of the rich solution 14a regenerator 16 the first rich-solution branch line L to 13-1 and the first rich-solution branch line L 13-1 provided in the first rich preheating the rich solution 14a which is branched by the first branching unit a-1 a solution heat exchanger 22-1, the first rich-solution branch line L 13-1 provided between the first branch portion a-1 and the first rich solution heat exchanger 22-1 in the first of the rich solution heat exchanger 22-1 to the rich solution 14a is preheated to a predetermined temperature, the first flow rate control device for controlling the flow rate of the first rich solution 14a which is branched at the branch portion a-1 23- 1, comprises a.
[0015]
　The first CO 2 from the rich solution 14 that fall within the regenerator 16 at the supply position B-1 to introduce the rich solution 14a which is branched to the regenerator 16 2 temperature is rich solution 14 desorbed semi-lean solution 15a t 1 to conform to, by adjusting the first flow control device 23-1, while adjusting the branching ratio of branched rich solution 14a, and preheated in the first rich-solution heat exchanger 22-1 becomes, the temperature t is introduced in the preheated rich solution 14a 11 and the temperature t of the semi-lean solution 15a in the regeneration tower 16 1 is substantially the same and a.
[0016]
　Here, in FIG. 1, reference numeral L 12 is the lean-solution supply line for supplying the lean solution supply portion 13c of the absorption column 13 the lean solution 15 that was withdrawn from the bottom 16b of the regenerator 16, 30 lean-solution supply line L 12 is interposed, the lean solution cooler lean solution 15 introduced into the absorption tower 13 is cooled by cooling water (CW), 31 is provided to the regenerator 16, indirectly heated lean solution 15 by saturated steam 32 reboiler for introducing steam inside the regenerator 16 to 33 gas-liquid separator for separating the vapor condensate 34 from saturated steam 32 after heating, L 30 is the reboiler 31 is interposed, a portion of the lean solution 15 There lean solution circulation line for circulating, L 31 represents a saturated water vapor introduction line for introducing the saturated steam 32 in reboiler 31, L 32 each shown a feed line feeding Kyusuru steam condensate feed steam condensate 34 That.
[0017]
　The CO 2 CO using recovery device 10A 2 in the recovery process, first, for example CO from boilers and gas turbines, etc. 2 gas 11 containing is cooled in gas cooling device (not shown), it is fed to the absorption tower 13.
[0018]
　In the absorption tower 13, the exhaust gas 11 CO based, for example, an amine-based solution 2 in contact countercurrent with absorption liquid 12. Then, CO in the exhaust gas 11 two are, CO by a chemical reaction 2 is absorbed in the absorbing liquid 12. CO absorption tower within 13 2 is CO after absorption removed 2 removing exhaust gas, washing water and in liquid contact with water washing section of the absorption column 13 (not shown), CO 2 CO entrained in flue gas 2 absorbing liquid 12 is recovered, then CO 2 is CO removed 2 flue gas 11A is released from the top 13a to the outside of the system. Moreover, CO 2 CO was absorbed 2 rich solution 14 is absorption liquid 12 is pressurized by the rich solution pump (not shown), the rich-lean solution heat exchanger 21, CO reproduced by the reproducing tower 16 2 the lean solution 15 is absorbed fluid 12 is heated (one lean solution 15 is cooled by heat exchange.), it is supplied to the regenerator 16.
[0019]
　Rich solution 14 released from the rich solution supply portion 16c of the regenerator 16 therein is caused an endothermic reaction by steam supplied from the bottom 16b side, most of the CO 2 release was desorbed. CO some or most in the regeneration tower 16 2 CO were released 2 absorbing solution is called semi-lean solvent 15a. The semi-lean solution 15a is the time to reach the bottom 16b of the regenerator 16, almost all of the CO 2 CO has been removed 2 becomes lean solution 15 of the absorption liquid. The lean solution 15 is partially heated by saturated steam 32 at the reboiler 31 and supplies the steam to the internal regeneration column 16.
[0020]
　On the other hand, from the top 16a of the regeneration tower 16, CO accompanied by water vapor released from the rich solution 14 and the semi-lean solution 15a in the column 2 gas 41 is a gas discharge line L 25 is derived via. Thereafter, the water vapor is condensed by the condenser, the water is separated in the separation drum. CO separated by the separation drum 2 gas 41 is a gas discharge line L 25 is released out of the system via a compressed separately by the compressor, is recovered. CO The recovered 2 gas 41 is, for example enhanced oil recovery method (EOR: Enhanced Oil Recovery) or pressed into oil was used to stored in an aquifer, thereby achieving the warming.
[0021]
　CO played 2 lean solution 15 is absorbing fluid at the rich-lean solution heat exchanger 21, is cooled by the rich solution 14 and the heat exchanger is pressurized subsequently at the lean solution pumps (not shown), after being further cooled in the lean solution cooler 30, is supplied to the absorption tower 13, CO 2 is circulated reused as the absorption liquid 12.
[0022]
　In this embodiment, CO in absorption tower 13 2 branches the part of the rich solvent 14 that has absorbed by the first branch portion A-1 was placed on the downstream side of the rich-lean solution heat exchanger 21, the branch was rich solution 14a, the first rich solution heat exchanger 22-1 to preheat by heat exchange provided by the bifurcated high temperature of the heat medium than the temperature of the rich solution 14a was (e.g. water vapor, etc.) 29, and a branch after preheating the rich solution 14a, it is introduced in the middle near the regeneration column 16.
[0023]
　As the heat medium 29 in the first rich-solution heat exchanger 22-1, for example steam, the steam condensate 34 from reboiler 31 may be used boiler exhaust gas and indirect heat medium and the heat exchange and the like.
[0024]
　Here, the first rich-solution branch line L 13-1 , the base is connected to the first branch portion A-1, its tip is connected to the side wall of the regenerator 16.
[0025]
　In the internal regeneration tower 16, the rich solution supply line L 11 rich solution 14 supplied from the rich solution supply portion 16c by, when introduced into the regeneration column 16 rises from the bottom 16b of the regenerator 16 steam CO from the rich solution 14 by 2 is desorbed removed. Then, as the rich solution 14 falls in the column, more CO 2 content is less semi-lean solution 15a, CO 2 lean solution 15 becomes the is almost released, more toward the bottom 16b from the top 16a, and gradually absorbed heat temperature of the liquid has a temperature distribution increases.
[0026]
　In this embodiment, the first rich-solution branch line L 13-1 first supply position B-1 of the tip portion of, CO 2 is partially removed, introduced at the top 16a side of the rich solution supply unit 16c Temperature temperature t of the semi-lean solution 15a whose temperature has risen from 1 a, the first rich-solution branch line L 13-1 preheating the rich solution 14a which is branched by the first rich solution heat exchanger 22-1 interposed temperature t 11 and is substantially the same, or semi-lean solution 15a temperature t of 1 is set to it is a higher temperature location of.
[0027]
　In other words, the supply position B-1 of the first is identified during plant design, when specifying the heat distribution of the regenerator 16, the temperature t of the semi-lean solution 15a 1 and preheated temperature of the bifurcated rich solution 14a t 11 and is substantially the same as or semi-lean solution 15a temperature t of 1 towards is to be introduced into the high position. Therefore, the first rich-solution branch line L 13-1 to a temperature t of the rich solution 14a which branches 11 a thermometer T measures the 11 are installed, measures the preheated temperature of the bifurcated rich solution 14a doing. The temperature t of the semi-lean solution 15a in the regeneration tower 16 in a first supply position B-1 to introduce the rich solution 14a which is branched into the regenerator 16 1 thermometer T a 1 is measured by. Here, the liquid temperature of the rich solution 14 introduced into the rich solution supply portion 16c of the regenerator 16 is a thermometer T t measured by the liquid temperature of the bottom unit 16b thermometer T b are each measured by.
[0028]
　As a result, the temperature t of the semi-lean solution 15a for a particular point in the regeneration tower 16 1 is substantially the same or lower temperature t 11 at a position a, so introduced to preheat the branched rich solution 14a, the inside regenerator 16 without variation in temperature occurs, CO 2 was released efficiently, it is possible to obtain a high energy saving effect. As a result, it is possible to it is possible to reduce the amount of steam required for the reboiler 31, a reduction in the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0029]
　Figure 2 shows another CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 2, another CO of the embodiment 2 in recovery device 10B, as shown in FIG. 2, CO in the regenerator 16 2 first stage reproduction unit for reproducing the rich solution 14 is absorbing liquid 12 the second stage regeneration section located 16-1 and the lower side of the first stage regeneration unit 16-1 is intended to include 16-2. The regeneration column 16, the first liquid storage unit 18 a portion of the CO from the rich solution 14 from the first chimney tray 19a of the first stage regeneration unit 16-1 of the upper side of the regenerator 16 2 is We extracted the total amount of removed semi-lean solution 15a to the outside, first connected to the supply position C to supply the top of the second stage regeneration section 16-2 at the lower side of a position in which withdrawal of the semi-lean solution 15a which issued該抜the semi-lean solvent extraction line L 21-1 and the first semi-lean solution discharge line L of regeneration column 16 21-1 supply position C of the first rich-solution branch line L 13-1 first supply position B-1 and are the same height, and the first mixing section 24-1 for mixing with the rich solution 14a which is branched semi-lean solution 15a in the regeneration tower 16, are provided. Here, the first mixing portion 24-1, as long as the four directions of the position or the side wall opposite of the configuration can be supplied evenly semi-lean solution 15a, and is not particularly limited. For example, the first semi-lean solution discharge line L 21-1 and supply position C of the first rich-solution branch line L 13-1 and the first supply position B-1 of the same height, full a same need not be high, it may be any height and semi-lean solution 15a and the rich solution 14a can be mixed in a first mixing section 24-1.
[0030]
　Then, the first branch portion A-1 provided between a first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate control valve for controlling the flow rate of the branched rich solution 14a ) 23-1 to control. By controlling the first flow controller 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and the first semi-lean solution extraction line L 21-1 in is installed, a thermometer T measures the temperature of the semi-lean solution 15a for extracting the total amount 1 temperature t measured by 1 substantially the same and or semi-lean solution 15a temperature t of 1 higher in the (t 1 ≧ t 11 ) It is as to become.
[0031]
　The temperature of adjustment, temperature t 11 temperature t of the measured from the initial set temperature of 11 case when becomes low, using, for example, first and to for example flow control valve flow controller 23-1, the flow rate control diaphragm valves, to adjust the branching ratio, for example, from 90:10 initially set ratio 93: 7 and by changing the ratio, thermometer T 11 measured temperature t at 11 is raised so as to have a default setting temperature Te, thermometer T of semi-lean solution 15a 1 temperature t of the measurement by 1 adjusted to approximate the.
[0032]
　Further, the temperature adjusting method of the bifurcated rich solution 14a, as the non-adjustment of the first flow control device 23-1, when it is possible to vary the temperature of, for example, the heat medium 29, the temperature of the heat medium 29 or raised, and or increasing the heat exchange capacity, achieving an increase in the preheating amount of branched rich solution 14a, adjusted to approximate a predetermined set temperature.
[0033]
　As a result, the temperature t of a particular predetermined semi-lean solution 15a in the regeneration tower 16 1 is substantially the same temperature t 11 by introducing preheated rich solution 14a which is branched such that the temperature during both mixing of there is substantially the same, without variation of the temperature within the regeneration column 16 occurs, CO 2 was released efficiently, it is possible to obtain a high energy saving effect. As a result, it is possible to it is possible to reduce the amount of steam required for the reboiler 31, a reduction in the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0034]
　This adjustment, there are a case where the case where the pre-programmed process with a control device, the processing operation by the operator to determine sequentially using the instrument. Here, CO in the regenerator 16 2 and the temperature of the absorption liquid, for example tower pressure in the regeneration tower 16, the amine concentration of the absorbent, the boiling point due to the type of the amine, CO 2 CO absorption liquid 2 by concentration, It refers to a determined is temperature.
[0035]
　Thus, in this embodiment, CO in absorption tower 13 2 absorbs, first branch portion A of the subsequent stage of the rich-lean solution heat exchanger 21 a portion of the rich solution 14 to be introduced into the regeneration column 16 -1 is branched at the first rich-solution branch line L for supplying a rich solution 14a which was the branched 13-1 and, the first rich-solution branch line L 13-1 provided in the branched rich solution 14a a first rich-solution heat exchanger 22-1 for preheating, provided between the first branch portion a-1 and the first rich solution heat exchanger 22-1, the flow rate of the branched rich solution 14a and it includes a first flow controller 23-1 for controlling the. Then, one of the bottom 16b side of the top portion 16a of the regeneration tower 16 in (e.g. middle vicinity), the temperature t of the semi-lean solution 15a of the heat distribution of the regenerator 16 1 and the temperature of the rich solution 14a which is branched to be supplied to the middle stage t 11 by the supplies at a position that is substantially the same, it is possible to achieve energy saving of the reboiler 31 and the lean solution cooler 30.
[0036]
　CO of the present embodiment shown in FIG. 2 2 The recovery system 10B, when the internal regeneration column 16 first stage regeneration unit 16-1, and the second stage regeneration section 16-2 has been divided into two undivided in even, CO from the rich solution 14 that fall within the regeneration column 16 at the first supply position B-1 to introduce the rich solution 14a which is branched to the regenerator 16 2 semi-lean solution 15a temperature t of the desorbed 1 matches as to, by adjusting the first flow control device 23-1, while adjusting the branching ratio of branched rich solution 14a, by preheating at a first rich solution heat exchanger 22-1, thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and thermometer T measures the temperature of the semi-lean solution 15a is not drawn 1 temperature t measured by 1 substantially the same and or semi-lean solution, 15a temperature t of 1 It is high (T 1 ≧ T 11 can be).
[0037]
　Figure 3 shows another CO according to Example 1 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 3, another CO according to the embodiment 2 recovery apparatus 10C as the heat medium 29 used in the first rich-solution heat exchanger 22-1, a case of using the steam condensate 34. In this embodiment, the gas-liquid separator 33 by feeding the steam condensate 34 which is separated Kyusuru steam condensate feed line L 32 and is connected to the first rich solution heat exchanger 22-1, and branch and using steam condensate 34 to preheat the rich solution 14a. As a result, as the heat medium 29 used in the first rich-solution heat exchanger 22-1, because of the use of steam condensed water 34, it is possible to omit the supply of heat medium from the outside, the regeneration efficiency of the regenerator 16 it is possible to improve the.
Example 2
[0038]
　4, CO according to the second embodiment 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG 4, CO according to Example 2 recovery system 10D, the second liquid storage portion of the second chimney tray 19b withdrawing a lean solution 15 to the reboiler 31 at the bottom 16b of the regenerator 16 18- 2, the first rich-solution branch line L 13-1 tip of is connected and a branched rich solution 14a is supplied from the first supply position B-1.
[0039]
　Then, the first branch portion A-1 provided between a first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate control valve for controlling the flow rate of the branched rich solution 14a ) 23-1 to control. By controlling the first flow controller 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and lean solution 15 in the second liquid reservoir 18-2 thermometer T measures the temperature 1 temperature t measured by 1 and substantially the same or the temperature t of the lean solution 15, 1 it is high in (t 1 ≧ t 11 are the) so as.
[0040]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
[0041]
　As a result, certain predetermined temperature t in the regeneration tower 16 1 is substantially the same temperature t 11 by introducing preheated rich solution 14a which branches so that, occurs the temperature of the dispersion of within the regenerator 16 it is no, CO 2 was released efficiently, it is possible to obtain a high energy saving effect. As a result, it is possible to it is possible to reduce the amount of steam required for the reboiler 31, a reduction in the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13. Also, since the residence time in the absorbing solution regeneration tower within 16 decreases, it is possible to reduce the thermal degradation of the absorbent.
Example 3
[0042]
　5, CO according to Example 3 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 5, CO according to the present embodiment 2 recovery apparatus 10E is the EkiTome portion of the bottom portion 16b of the lean solution 15 that is heated by the reboiler 31 in the bottom 16b side of the regenerator 16 is introduced, first the rich solution branch line L 13-1 tip of is connected and a branched rich solution 14a is supplied from the first supply position B-1.
[0043]
　Then, the first branch portion A-1 provided between a first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate control valve for controlling the flow rate of the branched rich solution 14a ) 23-1 to control. By controlling the first flow controller 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and the temperature of the lean solvent 15 of EkiTome portion of the bottom portion 16b thermometer T measures b temperature t measured by the b and a substantially identical or the temperature t of the lean solution 15, b it is high in (t b ≧ t 11 are the) so as.
[0044]
　As a result, certain predetermined temperature t of the bottom 16b in the regeneration tower 16 b substantially the same temperature t 11 by introducing preheated rich solution 14a which branches so that, at a temperature of within the regenerator 16 without variation occurs, CO 2 was released efficiently, it is possible to obtain a high energy saving effect. As a result, it is possible to it is possible to reduce the amount of steam required for the reboiler 31, a reduction in the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13. Also, since the residence time in the absorbing solution regeneration tower within 16 decreases, it is possible to reduce the thermal degradation of the absorbent.
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
Example 4
[0045]
　6, CO according to Example 4 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 6, CO according to the present embodiment 2 recovery apparatus 10F includes, CO 1 2 in the recovery device 10A, the lean-solution supply line L 12 bottom 16b and the rich-lean solution heat exchanger of the regenerator 16 is provided between the vessel 21, the lean-solution supply line L 12 and the first semi-lean solution extraction line L 21-1 at the intersection of the first lean of the lean solution 15 and the semi-lean solution 15a to the heat exchanger the - semi-lean solution heat exchanger 25-1 are provided.
[0046]
　By providing the first lean-semi-lean solution heat exchanger 25-1, the semi-lean solution 15a by the lean solution 15 is preheated, thermometer T 1 by the measurement of the temperature of the extraction of the semi-lean solution 15a is (t 1 ) if it was a thermometer T 2 by the measurement of the temperature of introduction of the semi-lean solution 15a is (t 2 : t 1 rises to + alpha ° C.).
[0047]
　Then, the first branch portion A-1 provided between a first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate control valve for controlling the flow rate of the branched rich solution 14a ) 23-1 to control. By controlling the first flow controller 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and the first semi-lean solution extraction line L 21-1 in is installed, a thermometer T measures the preheated temperature of the semi-lean solution 15a for extracting the total amount 2 temperature t measured by 2 substantially identical and or semi-lean solution 15a temperature t of 2 it is high in (t 2 ≧ T 11 is on) so as.
[0048]
　According to this embodiment, since the semi-lean solution 15a which extracted to the outside heat exchanger by the lean solution 15, by which it is possible to heat the semi-lean solution 15a to re-charged into the regeneration tower 16, CO Example 1 2 recovery than device 10A can be achieved energy savings reboiler efficiency of the regenerator 16. Further, it is possible to reduce the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0049]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
Example 5
[0050]
　7, CO according to Example 5 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 7, CO according to the present embodiment 2 recovery apparatus 10G has, CO 1 2 unlike recovery device 10A, CO in the regenerator 16 2 first to play the rich solution 14 is absorbed liquid 1-stage regeneration unit 16-1, the second stage regeneration section 16-2 located below the first stage regeneration unit 16-1, and the third located on the lower side of the second stage regeneration section 16-2 it is intended to include stepped reproducing unit 16-3. The regeneration column 16, a part of CO from the rich solution 14 by the first stage regeneration unit 16-1 2 the total amount of the first semi-lean from the liquid reservoir 18-1 solution 15a for storing the semi-lean solution 15a which has been removed the extracted to the outside, the first semi-lean solution discharge line L connected to the supply position C to supply the top of the second stage regeneration section 16-2 at the lower side of a position in which withdrawal of the semi-lean solution 15a which issued該抜 21 -1 a first semi-lean solution discharge line L 21-1 and supply position C, the first rich-solution branch line L 13-1 and the first supply position B-1 of the same height, a first mixing section 24-1 for mixing with the rich solution 14a which is branched semi-lean solution 15a in the regeneration tower 16, a portion of the CO from the semi-lean solution 15a by the second-stage regeneration unit 16-2 2 is further removed semi-lean solution 15b was Third chimney from the third liquid reservoir 18-3 of the tray 19c withdrawn semi-lean solution 15b to the outside, the semi-lean solution 15b a third stage regeneration unit 16-3 in the lower side of a position where withdrawn that issued該抜for storing the second semi-lean solution discharge line L that is the connection to the supply position D to be supplied to the upper 21-2 and is intended to include a.
[0051]
　Further, in the present embodiment, the lean-solution supply line L 12 disposed between the bottom 16b and the rich-lean solution heat exchanger 21 of the regenerator 16, the lean-solution supply line L 12 and the first semi-lean solution extraction line L 21-1 at the intersection of the lean solution 15 and the semi-lean solution 15a and the first lean-semi-lean solution heat exchanger 25-1 for heat exchange, the lean-solution supply line L 12 and the second semi-lean solution extraction line L 21-2 at the intersection of the, and the lean solution 15 and the semi-lean solution 15b includes a second lean-semi-lean solution heat exchanger 25-2 for heat exchange, a.
[0052]
　The first lean-semi-lean solution heat exchanger 25-1, by providing each of the second lean-semi-lean solution heat exchanger 25-2, semi-lean solution 15a is preheated respectively by the lean solution 15, a thermometer T 1 temperature of extraction of semi-lean solution 15a by the measurement of t 1 if a thermometer T 2 temperature of introduction of the semi-lean solution 15a is t by the measurement of 2 rises. Further, a thermometer T 3 temperature of extraction of semi-lean solution 15b are t by the measurement of the 3 cases were, thermometer T 4 by the measurement of the temperature of introduction of the semi-lean solution 15b are t 4 rises.
[0053]
　Then, the first branch portion A-1 provided between a first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate control valve for controlling the flow rate of the branched rich solution 14a ) 23-1 to control. By controlling the first flow control device 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and the first semi-lean solution extraction line L 21-1 in is installed, a thermometer T measures the temperature of the semi-lean solution 15a for extracting the total amount 2 temperature t measured by 2 substantially identical and or semi-lean solution 15a temperature t of 2 higher in the (t 2 ≧ t 11 ) It is as to become.
[0054]
　According to this embodiment, divided into three parts inside of the regenerator 16, so replacing each heat the semi-lean solution 15a which extracted twice outside the lean solution 15, the semi-lean solution 15a to re-charged into the regeneration tower 16 heated by being able to, CO example 1 2 than the recovery device 10A can be achieved energy savings reboiler efficiency of the regenerator 16. Further, it is possible to reduce the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0055]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
Example 6
[0056]
　8, CO according to Example 6 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 8, CO according to the present embodiment 2 recovery apparatus 10H is, CO in the regenerator 16 2 first stage regeneration unit 16-1 for reproducing the rich solution 14 is absorbing liquid, the first stage regeneration the second stage regeneration unit 16-2 located on the lower side of the part 16-1, and is intended to include third-stage regeneration unit 16-3 located on the lower side of the second stage regeneration section 16-2. The regeneration column 16, a part of CO from the rich solution 14 by the first stage regeneration unit 16-1 2 the total amount of the first semi-lean from the liquid reservoir 18-1 solution 15a for storing the semi-lean solution 15a which has been removed the extracted to the outside, the first semi-lean solution discharge line L connected to the supply position C to supply the top of the second stage regeneration section 16-2 at the lower side of a position in which withdrawal of the semi-lean solution 15a which issued該抜 21 -1 and a part of CO from the semi-lean solution 15a by the second-stage regeneration unit 16-2 2 extracted from the third liquid reservoir 18-3 for storing the semi-lean solution 15b which is further removed semi-lean solution 15b to the outside ,該抜out semi-lean solution 15b of the second supply to the supply position D to be supplied to the upper portion of the third stage regeneration unit 16-3 lower stage of a position where withdrawn semi-lean solution discharge line L 21- 2 and, second semi-lean solution discharge line L 21-2 and supply position D, the first rich-solution branch line L 13-1 and the first supply position B-1 of the same height, reproduction it is intended to includes a second mixing section 24-2 for mixing with the rich solution 14a is branched semi-lean solution 15b within the tower 16.
[0057]
　In this embodiment, unlike the fifth embodiment, it is provided between the first branch portion A-1 and the first rich solution heat exchanger 22-1, first to control the flow rate of the branched rich solution 14a 1 controlling the flow control devices (e.g. flow control valve) 23-1. By controlling the first flow controller 23-1, a thermometer T 11 temperature t is preheated rich solution 14a branching is measured in 11 and, second semi-lean solution extraction line L 21-2 in installed, thermometer T measures the temperature of the semi-lean solution 15b for extracting the total amount 4 temperature t measured by 4 substantially the same and or semi-lean solution temperature 15b (t, 4 ) it is high in (t 4 ≧ t 11 are in) so as.
[0058]
　According to this embodiment, divided into three parts the interior of the regenerator 16, the semi-lean solutions 15a which extracted twice outside, the lean solution 15 to 15b, the first lean-semi-lean solution heat exchanger 25-1, second since the exchange of each heat with the lean-semi-lean solution heat exchanger 25-2, the semi-lean solution 15a to re-charged into the regenerator 16, by which can be heated respectively 15b, CO example 1 2 recovering apparatus it is possible to achieve energy saving in the reboiler efficiency of the regenerator 16 than 10A. Further, it is possible to reduce the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0059]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
Example 7
[0060]
　9, CO according to Example 7 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 9, CO according to the present embodiment 2 recovery apparatus 10I is, CO Example 1 2 in the recovery device 10A, the rich-solution supply line L 11 and the first branch portion A-1 and the regenerator 16 the second branch section a-2 is provided between the, in the second branch portion a-2, and further branches part of the rich solution 14, the bifurcated rich solution 14a-2 of the top portion 16a of the regeneration tower 16 at the bottom 16b side from the rich solution supply unit 16c, the first rich-solution branch line L 13-1 at the supply position B-2 from the first side wall of the supply position B-1 top 16a side than in the second the second rich solution branch line L supply 13-2 and the second rich-solution branch line L 13-2 provided, first to preheat the rich solution 14a-2 that is branched by the second branching section a-2 2 rich solution heat exchanger 22-2, the second rich-solution branch line L 13-2 of the second It provided between the branch portion A-2 and a second rich solution heat exchanger 22-2, a second flow rate control for controlling the flow rate of the rich solution 14a-2 that is branched by the second branching section A-2 and the device 23-2, including a.
[0061]
　According to this embodiment, respectively branched by rich lean solution heat exchanger 21 the rich solution 14 to the first and second branches of the two A-1, A-2, which has exchanged heat with and that branch rich solution 14a-1 and 14a-2 respectively first rich solution heat exchanger 22-1, and preheated in the second rich solution heat exchanger 22-2, a first supply position of the regenerator 16 B- 1, are introduced into the second supply position B-2.
[0062]
　Then, provided between the second branch portion A-2 and a second rich solution heat exchanger 22-2, the second flow control device (e.g., flow rate for controlling the flow rate of branched rich solution 14a-2 controlling the control valve) 23-2. By controlling the second flow control device 23-2, a thermometer T 12 temperature t preheated rich solution 14a-2 branching is measured in 12 and the first semi-lean solution discharge line L 21- 1 is installed in, a thermometer T measures the temperature of the semi-lean solution 15a for extracting the total amount 1 temperature t measured by 1 substantially the same and or semi-lean solution 15a temperature t of 1 higher in the (t 1 ≧ t 12 are in) so as.
[0063]
　Further, provided between the first branch portion A-1 and the first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate for controlling the flow rate of the rich solution 14a-1 that branches to control the control valve) 23-1. By controlling the first flow control device 23-1, a thermometer T 11 temperature t preheated rich solution 14a-1 that branches are measured at 11 and the lean withdrawn into the reboiler 31 of the regenerator 16 solution thermometer T measures the temperature of 15 2 temperature t measured by 2 substantially identical and or semi-lean solution 15a temperature t of 2 towards the high (t 2 ≧ t 11 is set to be).
[0064]
　As in this embodiment, by the two at the branching part of the rich solution 14, it is possible to achieve energy saving in reboiler efficiency. Further, it is possible to reduce the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0065]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
[0066]
　Further, as the second heat medium 29 for heat exchange is supplied to the rich solution heat exchanger 22-2, and to use a steam condensate 34 after the heat exchange in the second rich solution heat exchanger 22-2 it may be.
Example 8
[0067]
　10, CO according to Example 8 2 is a schematic diagram showing the structure of a recovery device. As shown in FIG. 10, CO according to the present embodiment 2 recovery unit 10J includes, CO Example 6 2 in the recovery apparatus 10H, the rich-solution supply line L 11 and the first branch portion A-1 and the regenerator 16 the second branch section a-2 is provided between the, in the second branch portion a-2, and further branches part of the rich solution 14, the bifurcated portion rich solution 14a-2 of the regeneration column 16 the rich solution supply unit 16c first rich-solution branch line L also on the bottom 16b side from 13-1 or a second supply side walls of the first first supply position B-1 top 16a side than in the second rich solution branch line L is supplied to the position B-2 13-2 , a second rich-solution branch line L 13-2 provided, the rich solution branched at the second branch portion a-2 14a- a second rich solution heat exchanger 22-2 for preheating the 2, second rich-solution branch line L 13 -2 and the second branch portion A-2 of the disposed between the second rich solution heat exchanger 22-2, controls the flow rate of the rich solution 14a-2 that is branched by the second branching section A-2 a second flow control device 23-2 to the first semi-lean solution discharge line L 21-1 and supply position C, the second rich-solution branch line L 13-2 second supply position B-2 of Doo is substantially the same position, comprising a first mixing section 24-1 for mixing with the rich solution 14a-2 which is branched semi-lean solution 15a in the regeneration tower 16, a.
[0068]
　According to this embodiment, respectively branched by rich lean solution heat exchanger 21 the rich solution 14 to the first and second branches of the two A-1, A-2, which has exchanged heat with and that branch rich solution 14a-1 and 14a-2 respectively first rich solution heat exchanger 22-1, and preheated in the second rich solution heat exchanger 22-2, a first supply position of the regenerator 16 B- 1, are introduced into the second supply position B-2.
[0069]
　Then, provided between the second branch portion A-2 and a second rich solution heat exchanger 22-2, the second flow control device (e.g., flow rate for controlling the flow rate of branched rich solution 14a-2 controlling the control valve) 23-2. By controlling the second flow control device 23-2, a thermometer T 12 temperature t preheated rich solution 14a-2 branching is measured in 12 and the first semi-lean solution discharge line L 21- 1 is installed in, the total amount withdrawn semi-lean thermometer T measures the temperature of the solution 15a 2 temperature t measured by 2 substantially identical and or semi-lean solution 15a temperature t of 2 it is high in (t 2 ≧ t 12 ) is set to be.
[0070]
　Further, provided between the first branch portion A-1 and the first rich solution heat exchanger 22-1, the first flow control device (e.g., flow rate for controlling the flow rate of the rich solution 14a-1 that branches to control the control valve) 23-1. By controlling the first flow controller 23-1, a thermometer T 11 temperature t preheated rich solution 14a-1 that branches are measured at 11 and a second semi-lean solution discharge line L 21- 2 is installed in, the total amount withdrawn semi-lean solution 15b thermometer T measures the temperature of 4 temperature t measured by 4 substantially the same and or semi-lean solution 15b temperature t of 4 higher in the (t 4 ≧ t 11 ) is set to be.
[0071]
　A branch portion of the rich solution 14 With two places, it is possible to achieve energy saving in reboiler efficiency. Further, it is possible to reduce the required amount of cooling water in the lean solution cooler 30 for cooling the lean solution 15 introduced into the absorption tower 13.
[0072]
　In the present embodiment, as the heat medium 29 for heat exchange is supplied to the first rich solution heat exchanger 22-1, likewise vapor condensate feed line L as in Example 1 32 by the gas-liquid separator steam condensate 34 separated by 33 may be used.
[0073]
　Further, as the second heat medium 29 for heat exchange is supplied to the rich solution heat exchanger 22-2, and to use a steam condensate 34 after the heat exchange in the second rich solution heat exchanger 22-2 it may be.
[0074]
[Test Example 1-8]
　were tested to confirm the effect of Examples 1-8 of the present invention.
　That is, as in the prior art, from the absorption tower 13, 1 to heat requirements of the reboiler 31 in the regeneration tower 16 when the rich solution 14 to be introduced into the regeneration tower 16 using only the rich-lean solution heat exchanger 21, the lean the necessary cooling of the solution cooler 30 and 1, CO of the embodiment shown in FIGS. 3-10 2 using the apparatus shown in recovery apparatus 10C ~ 10J, the first second-stage rich lean solution heat exchanger 21 in the branch unit a-1, branches a part of the rich solvent 14, after preheating in the first rich-solution heat exchanger 22-1, when introduced to the same temperature and the semi-lean solution 15a of the regenerator 16 heat of reboiler 31 in and compared the cooling efficiency of the lean solution cooler 30.
[0075]
　Incidentally, with steam condensate 34 as a heat medium 29 used in the first rich-solution heat exchanger 22-1. The results are shown in Table 1.
[0076]
　As shown in Table 1, Test Example 1 (CO of the first embodiment of FIG 2 in the collecting device 10C), it is confirmed to achieve 6% energy savings as compared with the case of Comparative Example 1 does not branch a reference It was. Test Example 2 (CO Example 2 of FIG. 4 2 In recovery device 10D), as compared with the case of Comparative Example 1 does not branch a reference be made 6% energy saving has been confirmed. Test Example 3 (CO Example 3 of FIG. 5 2 In recovery device 10E), as compared with the case of Comparative Example 1 does not branch a reference be made 6% energy saving has been confirmed. Test Example 4 (CO Example 4 6 2 In recovery apparatus 10F), as compared with the case of Comparative Example 1 does not branch a reference be made 14% of energy saving has been confirmed. Test Example 5 (CO embodiment 5 of FIG. 7 2 In recovery device 10G), as compared with the case of Comparative Example 1 does not branch a reference be made 16% of energy saving has been confirmed. Test Example 6 (CO Example 6 8 2 In recovery unit 10H), compared with the case of Comparative Example 1 does not branch a reference be made 17% energy saving has been confirmed. Test Example 7 (CO embodiment 7 of FIG 2 in the collecting device 10I), as compared with the case of Comparative Example 1 does not branch a reference be made 6% energy saving has been confirmed. Test Example 8 (CO of Example 8 10 2 In recovery device 10J), as compared with the case of Comparative Example 1 does not branch a reference be made 6% energy saving has been confirmed. Test Example 9 (CO of Example 8 10 2 in the recovery device 10J), the heating medium of the second rich solution heat exchanger 22-2, does not branch case, the reference using the water vapor from the outside compared possible to 7% energy savings as compared with the case of example 1 was confirmed. Further, in Test Example 4-6, also improves cooling efficiency of the lean solution cooler 30, it was confirmed that reduced amount of cooling water.
[0077]
[Table 1]

DESCRIPTION OF SYMBOLS
[0078]
　10A ~ 10J CO 2 recovery device
　11 CO 2 containing exhaust gas
　12 CO 2 absorbing solution
　13 CO 2 absorption tower
　14 rich solution
　14a branched rich solution
　15 lean solution
　15a semi-lean solution
　16 absorbent regenerator
　L 11　rich solution supply line
　L 12　lean solution supply line
　L 13-1　first rich-solution branch line
　L 13-2　second rich-solution branch line
　21 rich lean solution heat exchanger
　22-1 first rich solution heat exchanger
　22-2 second rich solution heat exchanger
　23-1 first flow control device
　23-2 second flow control device
　a-1 first branch portion
　a-2 the second branch portion
　B-1 first supply position
　B-2 second supply position

　
The scope of the claims
[Requested item 1]
　CO 2 CO containing 2 containing exhaust gas and CO 2 by contacting the absorption liquid, the CO 2 CO from exhaust gas containing 2 CO removing 2 and absorption
　tower, CO 2 CO from the rich solution that has absorbed 2 separates Te, CO as lean solution 2 and absorbent regenerator to regenerate the absorbing solution,
　the rich solution the CO 2 rich solution supply line for supplying the bottom of the absorption column to the rich solution supply portion of the top side of the absorbent regenerator When,
　the rich solution and the lean solution and the rich-lean solution heat exchanger for heat exchange,
　first of the rich solution supply line provided between the rich-lean solution heat exchanger wherein the absorbing solution regeneration tower branches the part of the rich solution in the first branch portion, the branch to the first rich solvent supplying the rich solution in the first supply position of the side wall of the absorbing solution regeneration tower the bottom side than the top side of the branch La And down,
　is provided on the first rich-solution branch line, the first rich solution heat exchanger for preheating the rich solution that is branched by the first branching portion,
　said first rich-solution branch line first provided between the one of the bifurcation first rich solution heat exchanger, said in the first rich-solution heat exchanger so rich solution is preheated to a predetermined temperature, said first branch portion in branched CO characterized by comprising a first and a flow control device for controlling the flow rate of the rich solution, was 2 recovery device.
[Requested item 2]
　According to claim 1,
　wherein the first heat exchange medium of the rich solution heat exchanger, CO, characterized in that steam condensate from the reboiler provided in the absorbent regenerator 2 recovery apparatus.
[Requested item 3]
　According to claim 1,
　wherein the CO in the absorbing solution regeneration tower 2 includes a second stage regeneration section located below the first stage regeneration section and the first stage regeneration unit for reproducing the absorption liquid,
　the first stage some of CO from the rich solution by the reproduction unit 2 extracted from the first liquid storage unit for storing the semi-lean solution is removed semi-lean solution to the outside, the lower stage side of a position in which withdrawal of the semi-lean solution which issued該抜a first semi-lean solution discharge line which is connected to a supply position for supplying to the top of the second stage regeneration section,
　and the supply position of the first semi-lean solution discharge line of the absorbent regenerator, the first a supply position and the same height of the rich-solution branch line, characterized in that the rich solution the branch and the semi-lean solution to the absorption liquid regeneration tower is the first mixing portion for mixing comprises CO 2 recovery apparatus.
[Requested item 4]
　In claim 3,
　the lean solution from the bottom of the absorbing solution regeneration tower the CO 2 has a lean-solution supply line for supplying the lean rich solution supply portion of the top side of the absorption tower,
　the absorbing of the lean-solution supply line heat in between the bottom of the liquid regenerator and the rich lean solution heat exchanger, the intersections of the lean-solution supply line and the first semi-lean solution discharge line, and said lean solution wherein the semi-lean solution CO and providing a first lean-semi-lean solution heat exchanger to exchange 2 recovery apparatus.
[Requested item 5]
　According to claim 1,
　wherein the CO in the absorbing solution regeneration tower 2 first stage reproduction unit for reproducing the absorption liquid, the second stage regeneration section located below the first stage regeneration unit, and the second stage regeneration includes a third stage regeneration unit positioned on the lower side of the part,
　the part of CO from the rich solution by the first stage regeneration unit 2 from the first liquid storage unit for storing the semi-lean solution is removal of the semi-lean solution withdrawn the whole amount to the outside, a first semi-lean solution discharge line which is connected to a supply position for supplying the upper part of the second stage regeneration section at the lower side of a position where withdrawn said semi-lean solution that issued該抜,
　the first and supply position of one of the semi-lean solution discharge line, wherein the supply position of the first rich-solution branch line are identical height, the rich solution described above and the semi-lean-solution branch to the absorbing solution regeneration tower is mixed a first mixing unit for,
　the second Some of CO from the semi-lean solution by stepped reproducing unit 2 extracted from the second liquid reservoir for storing the semi-lean solution is further removed semi-lean solution to the outside, lower than the position withdrawn said semi-lean solution which issued該抜CO characterized by comprising a second semi-lean solution discharge line which is connected to a supply position for supplying the upper portion of the third stage regeneration section on the side, a 2 recovery apparatus.
[Requested item 6]
　According to claim 1,
　wherein the CO in the absorbing solution regeneration tower 2 first stage reproduction unit for reproducing the absorption liquid, the second stage regeneration section located below the first stage regeneration unit, and the second stage regeneration includes a third stage regeneration unit positioned on the lower side of the part,
　the part of CO from the rich solution by the first stage regeneration unit 2 from the first liquid storage unit for storing the semi-lean solution is removal of the semi-lean solution withdrawn the whole amount to the outside, a first semi-lean solution discharge line which is connected to a supply position for supplying the upper part of the second stage regeneration section at the lower side of a position where withdrawn said semi-lean solution that issued該抜,
　the first some of CO from the semi-lean solution by two-stage regeneration unit 2 extracted from the second liquid reservoir for storing the semi-lean solution is further removed semi-lean solution to the outside, from the position withdrawn said semi-lean solution which issued該抜before in the lower side A second semi-lean solution extraction line for supplying the supply position for supplying to the upper portion of the third stage and reproducing unit,
　a supply position of the second semi-lean solution discharge line, the supply position of the first rich-solution branch line DOO are identical height, the absorbing liquid CO characterized by comprising a second mixing unit for mixing with the rich solution, the branched and the semi-lean solution in the regeneration tower in 2 recovery apparatus.
[Requested item 7]
　According to claim 1,
　wherein further comprising a second branch portion provided with the first branch portion between the absorbent regenerator,
　in the second branch portion, further a part of the rich-solution branch It is allowed, in the branched rich solution the absorbent regenerator the top side of the rich solution supply unit bottom side than in, and at a second feed position of the first rich-solution branch line sidewall of the top side of the a second rich-solution branch line that supplies,
　provided in the second rich-solution branch line, a second rich solution heat exchanger for preheating the rich solution that is branched by the second branching part,
　the second the rich solution is provided between the second branch portion of the branch line and the second rich solution heat exchanger, a second flow rate control for controlling the flow rate of branched rich solution in the second branch portion CO, characterized in that it comprises apparatus and a 2 times Apparatus.
[Requested item 8]
　According to claim 6,
　wherein further comprising a second branch portion provided with the first branch portion between the absorbent regenerator,
　in the second branch portion, further a part of the rich-solution branch is, the supplies the branched rich solution to one of the side walls of said at absorbent regenerator the top side of the rich solution supply unit bottom side than the, and the first rich-solution branch top side than the line and 2 rich solution branch line,
　wherein provided in the second rich-solution branch line, a second rich solution heat exchanger for preheating the rich solution that is branched by the second branching part,
　the second rich-solution branch provided between the second branch of the line and the second rich solution heat exchanger, the second flow control device for controlling the flow rate of the rich solution branched at the second branch portion,
　said the first semi-lean solution extraction feed position of the line When a supply position and the same height of the second rich-solution branch line comprises a first mixing portion and a rich solution which is branched to the semi-lean solution to the absorption liquid regeneration tower are mixed, the CO wherein the 2 recovery apparatus.
[Requested item 9]
　According to claim 1,
　wherein the CO in the absorbing solution regeneration tower 2 first stage reproduction unit for reproducing the absorption liquid, the second stage regeneration section located below the first stage regeneration unit, and the second stage regeneration includes a third stage regeneration unit positioned on the lower side of the part,
　the part of CO from the rich solution by the first stage regeneration unit 2 from the first liquid storage unit for storing the semi-lean solution is removal of the semi-lean solution withdrawn the whole amount to the outside, a first semi-lean solution discharge line which is connected to a supply position for supplying the upper part of the second stage regeneration section at the lower side of a position where withdrawn said semi-lean solution that issued該抜,
　the first and supply position of one of the semi-lean solution discharge line, wherein the supply position of the first rich-solution branch line are identical height, the rich solution described above and the semi-lean-solution branch to the absorbing solution regeneration tower is mixed a first mixing unit for,
　the second Some of CO from the semi-lean solution by stepped reproducing unit 2 extracted from the second liquid reservoir for storing the semi-lean solution is further removed semi-lean solution to the outside, lower than the position withdrawn said semi-lean solution which issued該抜a second semi-lean solution discharge line which is connected to a supply position for supplying the upper portion of the third stage regeneration section on the side,
　the lean solution the CO from the bottom of the absorbing solution regeneration tower 2 on the top side of the absorption tower a lean-solution supply line for supplying the lean solution the absorbent regenerator at the bottom of the supply line and disposed between the rich lean solution heat exchanger, the said lean-solution supply line first semi-lean the intersection of the solution extraction line, a first lean-semi-lean solution heat exchanger for the heat exchange lean solution and the semi-lean solvent,
　wherein the lean-solution supply line The intersection of emission and said second semi-lean solution discharge line, characterized by comprising: a second lean-semi-lean solution heat exchanger for exchanging heat between said lean solution wherein the semi-lean solution CO 2 recovery system.
[Requested item 10]
　According to claim 1,
　wherein the CO in the absorbing solution regeneration tower 2 first stage reproduction unit for reproducing the absorption liquid, the second stage regeneration section located below the first stage regeneration unit, and the second stage regeneration includes a third stage regeneration unit positioned on the lower side of the part,
　the part of CO from the rich solution by the first stage regeneration unit 2 from the first liquid storage unit for storing the semi-lean solution is removal of the semi-lean solution withdrawn the whole amount to the outside, a first semi-lean solution discharge line which is connected to a supply position for supplying the upper part of the second stage regeneration section at the lower side of a position where withdrawn said semi-lean solution that issued該抜,
　the first some of CO from the semi-lean solution by two-stage regeneration unit 2 extracted from the second liquid reservoir for storing the semi-lean solution is further removed semi-lean solution to the outside, from the position withdrawn said semi-lean solution which issued該抜before in the lower side A second semi-lean solution extraction line for supplying the supply position for supplying to the upper portion of the third stage and reproducing unit,
　a supply position of the second semi-lean solution discharge line, the supply position of the first rich-solution branch line DOO are identical height, the second mixing section and the rich solution which branches the semi-lean solution to the absorption liquid regeneration tower is mixed,
　the CO said lean solution from the bottom of the absorbing solution regeneration tower 2 absorption a lean-solution supply line supplying the top side of the column, is provided between the lean solution the absorbent regenerator at the bottom of the supply line and the rich lean solution heat exchanger, and the lean-solution supply line the intersections of the first semi-lean solution discharge line, a first lean-semi-lean solution heat exchanger for the heat exchange lean solution and the semi-lean solvent,
　wherein the lean-solution supply line before An intersection of the serial second semi-lean solution discharge line, the lean solution and the semi-lean solution and the CO is characterized by comprising a second lean-semi-lean solution heat exchanger for exchanging heat, a 2 recovery apparatus.
[Requested item 11]
　CO 2 CO containing 2 containing exhaust gas and CO 2 by contacting the absorption liquid, the CO 2 CO from exhaust gas containing 2 CO removing 2 and absorption tower, CO 2 CO absorbed 2 is an absorption solution rich solution CO from 2 to separate the CO 2 using the absorbent regenerator to regenerate the absorbing solution as a lean solution, wherein the absorbent regenerator CO at 2 CO has been removed 2 the absorbing solution the CO 2 circulation again in the absorption tower CO utilizing 2 a recovery method,
　the CO 2 comprising the steps of heat exchange and a lean solution which is delivered with the rich solution sent from the absorption tower from the absorbent regenerator,
　the top side of the absorbent regenerator rich solution supply unit, and to feed the side wall located on the lower side of the rich solution supply unit, the steps of branching the heat exchanged rich solution,
　to preheat the rich solution supplied to the supply position of the side wall It has a step, a
　the heat exchanger of And in the step of branching the rich solution, the absorbing solution is supplied from the rich solution supply portion of the regenerator the top side of the CO 2 and the temperature of the rich solution is partially removed, is supplied from the side wall of the absorbing solution regeneration tower temperature of branched rich solution is identical, or CO 2 CO is characterized by so that towards the temperature of a portion removed rich solution becomes high temperature, adjusting the branching amount of the rich solution to be heat exchanged 2 recovery method.
[Requested item 12]
　According to claim 11,
　CO and wherein the heating medium to preheat the rich solution, a vapor condensate from the absorbent regenerator to be supplied to the side wall 2 recovery method.