WO2013161574A1 - Co2 recovery device, and co2 recovery method - Google Patents

Co2 recovery device, and co2 recovery method Download PDF

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Publication number
WO2013161574A1
WO2013161574A1 PCT/JP2013/060933 JP2013060933W WO2013161574A1 WO 2013161574 A1 WO2013161574 A1 WO 2013161574A1 JP 2013060933 W JP2013060933 W JP 2013060933W WO 2013161574 A1 WO2013161574 A1 WO 2013161574A1
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Prior art keywords
temperature
rich solution
solution
regeneration tower
rich
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PCT/JP2013/060933
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French (fr)
Japanese (ja)
Inventor
田中　裕士
長安　弘貢
琢也 平田
大石　剛司
上條　孝
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三菱重工業株式会社
関西電力株式会社
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Publication of WO2013161574A1 publication Critical patent/WO2013161574A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention relates to a CO 2 recovery apparatus and method for energy saving.
  • a step of removing and recovering CO 2 from the combustion exhaust gas using the above-mentioned CO 2 absorption liquid a step of bringing the combustion exhaust gas and the CO 2 absorption liquid into contact with each other in an absorption tower, an absorption liquid that has absorbed CO 2 is used. Heating is performed in a regeneration tower to liberate CO 2 and regenerate the absorption liquid, which is then recycled to the absorption tower and reused (Patent Document 1).
  • the regeneration step consumes a large amount of heat energy (water vapor) in order to release CO 2 from the CO 2 absorbing solution, so that it needs to be an energy saving process as much as possible.
  • Patent Document 2 there is a proposal to reduce the amount of water vapor used when CO 2 is released in the regeneration tower by heating the rich solution that has absorbed CO 2 supplied to the regeneration tower. 3).
  • Patent Document 2 as a means for heating the rich solution, a semi-rich solution that partially absorbs CO 2 in the absorption tower is used. Therefore, depending on the operating state of the CO 2 recovery device, stable energy saving is achieved. There is a problem that it cannot be planned. In addition, since the rich absorption liquid is heat-exchanged with the semi-rich solution, there is a problem that heat exchange is performed only with a temperature difference and stable energy saving cannot be achieved.
  • an object of the present invention is to provide a CO 2 recovery device and method that further improve energy efficiency while achieving stable energy saving.
  • the first aspect of the present invention to solve the above problems, and the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, the CO 2 An absorption liquid regeneration tower that separates CO 2 from the absorbed rich solution and regenerates the CO 2 absorption liquid to obtain a lean solution, and the lean solution from which CO 2 has been removed by the absorption liquid regeneration tower is converted into CO by the CO 2 absorption tower.
  • CO 2 CO 2 recovery device to be reused as an absorbing liquid, a part of the rich solution that has absorbed CO 2 in the CO 2 absorption tower is branched, and a preheating means for preheating the branched part of the rich solution;
  • a rich-lean solution heat exchanger that joins a portion of the rich solution preheated by the preheating means with the rich solution and exchanges heat between the joined rich solution and the lean solution that has released CO 2. It is in the CO 2 recovery device characterized by this.
  • a second invention is the CO 2 recovery apparatus according to the first invention, wherein the preheating temperature in the preheating means is equal to or lower than the temperature of the lean solution.
  • the concentration measuring means for measuring the concentration of the CO 2 absorbent in the absorbing solution of the rich solution, and the temperature of the rich solution immediately before being introduced into the absorbing solution regeneration tower are provided.
  • a temperature measuring means for measuring, a pressure measuring means for measuring the pressure in the absorption liquid regeneration tower, and an appropriate temperature of the rich solution to be introduced into the absorption liquid regeneration tower is obtained from these measurement results, and becomes the appropriate value.
  • a CO 2 recovery device comprising a control device for controlling the preheating temperature.
  • the control device controls the control to increase the preheating temperature in the preheating means.
  • the CO 2 recovery device is characterized in that it is executed in the above.
  • the control device controls the control to lower the preheating temperature in the preheating means.
  • the CO 2 recovery device is characterized in that it is executed in the above.
  • a sixth invention is the CO 2 recovery apparatus according to any one of the first to fifth inventions, wherein the CO 2 recovery device is provided with a plurality of water washing sections.
  • a seventh aspect of the present invention is separated and the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, the CO 2 from the CO 2 absorbent having absorbed CO 2 and by using the absorbent regenerator to regenerate the CO 2 absorbing solution, the lean solution from which CO 2 has been removed by the absorbing solution regeneration tower a CO 2 recovery method be reused in the CO 2 absorber, the CO branches the part of the rich solution that has absorbed CO 2 in 2 absorber, to preheat the rich solution part was the branched, the rich solution of a portion that is the preheating joins the rich solution, rich of flowing ⁇ In the CO 2 recovery method, heat exchange is performed between the solution and the lean solution from which CO 2 has been released, and then the solution is introduced into the absorption liquid regeneration tower.
  • An eighth invention is the CO 2 recovery method according to the seventh invention, wherein the preheating temperature in the preheating means is a temperature equal to or lower than the temperature of the lean solution.
  • the concentration of the CO 2 absorbent in the absorbent of the rich solution, the temperature of the rich solution immediately before being introduced into the absorbent regenerator, and the inside of the absorbent regenerator is characterized in that, from the measurement results, an appropriate temperature of the rich solution introduced into the absorption liquid regeneration tower is obtained, and the preheating temperature is controlled so as to be the appropriate value. It is in.
  • the present invention by efficiently using the low level residual heat of the CO 2 recovery device, it is possible to reduce the supply amount of heated steam in the regeneration tower, and further improve energy efficiency while achieving stable energy saving. Can be improved.
  • FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment.
  • FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment.
  • FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment.
  • FIG. 4 is a schematic diagram of a CO 2 recovery device according to the fourth embodiment.
  • FIG. 5 is a schematic diagram of a CO 2 recovery device according to the fifth embodiment.
  • FIG. 6 is a schematic diagram of a CO 2 recovery apparatus according to the sixth embodiment.
  • FIG. 7 is a flowchart of the rich solution branching amount control for carrying out the sixth embodiment.
  • FIG. 8 is a flowchart of the rich solution branching amount control for carrying out the sixth embodiment.
  • FIG. 9 is a graph comparing required heat amounts in the test example and the conventional example.
  • FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment.
  • CO 2 recovery apparatus 10A according to the present embodiment, CO 2 containing exhaust gas 11A and the CO 2 absorbing liquid containing CO 2 with (lean solution 12B) and contacting the removing CO 2 CO 2 an absorption tower (hereinafter referred to as “absorption tower”) 13, an absorption liquid regeneration tower 14 for regenerating a CO 2 absorption liquid (rich solution 12 A 0 ) that has absorbed CO 2 , and the absorption liquid regeneration tower (hereinafter “regeneration tower”).
  • absorption tower absorption tower
  • a part of the rich solution 12A 0 that has absorbed CO 2 in the absorption tower 13 is branched at the branching section X, and the part of the rich solution 12A 1 that is branched is removed from the temperature of the rich solution 12A 1 .
  • a first heat exchanger 23A which is a preheating means for exchanging heat with a fluid having a higher temperature and preheating to a temperature lower than the temperature of the lean solution 12B, and a part of the preheat rich solution preheated by the preheating means 12A 2 is combined with the rich solution 12A 0 at the junction Y, and the rich / lean solution heat exchanger 52 is provided for heat exchange between the merged rich solution 12A 3 and the lean solution 12B from which CO 2 has been released. is doing.
  • the CO 2 -containing exhaust gas 11 A is counterflowed with an amine-based CO 2 absorption liquid 12 based on, for example, an alkanolamine in a CO 2 absorption section 13 A provided on the lower side of the CO 2 absorption tower 13.
  • contact, CO 2 in the CO 2 containing exhaust gas 11A is absorbed by the CO 2 absorbing liquid 12 by a chemical reaction (R-NH 2 + H 2 O + CO 2 ⁇ R-NH 3 HCO 3).
  • R-NH 2 + H 2 O + CO 2 ⁇ R-NH 3 HCO 3 a chemical reaction
  • the CO 2 removal exhaust gas 11B rises to the water washing section 13B side via the chimney tray 16, contacts the washing water 20 supplied from the top side of the water washing section 13B, and accompanies the CO 2 removal exhaust gas 11B.
  • the CO 2 absorbent 12 to be recovered is recovered by circulation cleaning.
  • the washing water 20 stored in the liquid storage section 21 of the chimney tray 16 is circulated through the circulation line L 1 to perform circulation washing.
  • the circulation line L 1 of the cooling unit 22 is provided, it is cooled to a predetermined temperature (e.g., 40 ° C. or less).
  • Reference numeral 19 denotes a mist eliminator that captures mist in the gas.
  • the rich solution 12A 0 that has absorbed CO 2 in the absorption tower 13 is extracted from the bottom of the tower, and is pressurized by the rich solvent pump 51 interposed in the rich solution supply pipe L 11 , so that the top side of the absorption liquid regeneration tower 14 To be supplied.
  • the appropriate temperature refers to a temperature determined by, for example, the pressure in the regeneration tower 14, the amine concentration of the absorption liquid, the boiling point depending on the type of amine, and the CO 2 concentration in the absorption liquid.
  • the first heat exchanger 23 ⁇ / b> A that is a preheating means is interposed in a circulation line L 1 through which the cleaning water 20 circulates. Then, in the first heat exchanger 23A, a part of the rich solution 12A 1 branched from the mainstream rich solution 12A 0 is preheated using the heat of the wash water 20 to obtain a preheat rich solution 12A 2 .
  • the preheated rich solution 12A 2 is merged with the mainstream rich solution 12A 0 to form a merged rich solution 12A 3, and then the lean solution 12B from which CO 2 has been diffused in the regeneration tower 14 and the rich / lean solution heat exchanger 52.
  • the rich solution 12A 4 which has been subjected to heat exchange and has reached a high temperature is introduced into the regeneration tower 14.
  • the low temperature (for example, 30 to 50 ° C.) rich solution 12A 0 that has absorbed the CO 2 in the absorption tower 13 is effectively utilized by using the heat of the washing water 20 at a low level (for example, 50 to 60 ° C.).
  • the temperature of some of the rich solutions 12A 1 is increased.
  • the preheated rich solution 12A 2 whose temperature has been increased is merged with the main rich solution 12A 0 , and then the combined rich solution 12A 3 is heat-exchanged by the rich / lean solution heat exchanger 52 and supplied to the regeneration tower 14.
  • the temperature of the rich liquid 12A 4 can be increased to an appropriate temperature set value.
  • the reboiler required heat amount in the regeneration tower 14 can be reduced.
  • the rich solution 12A 4 released into the tower from the top side of the regeneration tower 14 releases most of the CO 2 by heating with water vapor from the bottom of the tower.
  • the CO 2 absorbent 12 that has released part or most of the CO 2 in the regeneration tower 14 is referred to as a “semi-lean solution”.
  • the semi-lean solution (not shown) flows down to the bottom of the regeneration tower 14, it becomes a lean solution 12B from which almost all of the CO 2 has been removed.
  • the lean solution 12B by saturated steam 62 in the regeneration heater 61 interposed in the circulation line L 20, is heated.
  • the saturated steam 62 after heating becomes steam condensed water 63.
  • CO 2 gas 41 accompanied by water vapor dissipated from the rich solution 12A 4 and a semi-lean solution (not shown) is released in the tower.
  • CO 2 gas 41 accompanied by water vapor is derived by the gas discharge line L 21
  • the water vapor is condensed by the cooling unit 42 interposed in the gas discharge line L 21
  • condensed water 44 is separated in the separation drum 43
  • the CO 2 gas 45 is released out of the system, and post-processing such as compression recovery is performed separately.
  • Condensed water 44 separated in the separation drum 43 is supplied to the upper portion of the absorbing solution regeneration tower 14 by the condensed water circulation pump 46 interposed in condensate line L 22.
  • a portion of the condensed water 44 is fed into the circulation line L 1 of the washing water 20, be used to absorb the CO 2 absorbing liquid 12 to be entrained in the CO 2 absorbing solution removed exhaust 11C Good.
  • the regenerated CO 2 absorbent (lean solution 12B) is sent to the CO 2 absorption tower 13 side by the lean solution pump 54 via the lean solution supply pipe L 12 and circulated and used as the CO 2 absorbent 12.
  • the lean solution 12B is cooled to a predetermined temperature by the cooling unit 55 and is supplied into the CO 2 absorbing unit 13A through the nozzle 56. Therefore, the CO 2 absorbing liquid 12 forms a closed path for circulating a CO 2 absorption tower 13 and the absorption solution regenerator 14 is reused in the CO 2 absorbing section 13A of the CO 2 absorber 13.
  • the CO 2 absorbent 12 is supplied from a replenishment line (not shown) as necessary, and the CO 2 absorbent 12 is regenerated by a reclaimer (not shown) as needed.
  • the CO 2 -containing exhaust gas 11A supplied to the CO 2 absorption tower 13 is cooled by the cooling water 71 in the cooling tower 70 provided on the upstream side thereof, and then introduced into the CO 2 absorption tower 13. Incidentally, is fed to the top of the washing unit 13B as wash water 20 also the CO 2 absorber 13 portion of the cooling water 71, is sometimes used for cleaning the CO 2 absorbing liquid 12 accompanying the CO 2 flue gas 11B.
  • Reference numeral 72 denotes a circulation pump
  • 73 denotes a cooler
  • 74 denotes a circulation line.
  • the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched
  • the first heat exchanger 23A preheats to a temperature of the solution 12B or lower (for example, 120 ° C.), and a portion of the rich solution 12A 2 preheated by the preheating means is merged with the rich solution 12A 0 and the merged rich Since the solution 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to form a higher temperature rich solution 12A 4 and introduced into the regeneration tower 14, the rich solution composition Therefore, the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
  • Example 1 of the present invention A test was conducted to confirm the effect of Example 1 of the present invention. That is, the amount of heat required for the reboiler in the regeneration tower 14 when the rich solution introduced into the regeneration tower 14 from the absorption tower 13 only using the rich lean solution heat exchanger 52 is set to 1, and a part of the rich solution is preheated. Then, the amount of heat of the reboiler in the regeneration tower 14 when further heated using the rich / lean solution heat exchanger 52 was compared. The result is shown in FIG. As shown in FIG. 9, it was confirmed that 6% energy saving was achieved as compared with the standard case.
  • FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
  • the CO 2 recovery apparatus 10B of the present example as a preheating means for preheating a part of the rich solution 12A 1 branched, the steam discharged from the top 14a of the regeneration tower 14 was accompanied by water vapor.
  • the second heat exchange unit 23B using the CO 2 gas 41 is used.
  • This second heat exchanging portion 23B is interposed in a gas discharge line L 21 through which CO 2 gas 41 accompanied by water vapor is discharged, and a part of the rich solution 12A 1 branched by the CO 2 gas 41 accompanied by water vapor. Is preheated to obtain a preheat rich solution 12A 2 . Since the temperature of the CO 2 gas 41 accompanied with the water vapor is 100 ° C. or lower (for example, 60 to 100 ° C.), a part of the rich solution 12A 1 branched can be preheated to the temperature of the lean solution 12B or lower. .
  • a part of the branched rich solution 12A 1 is preheated to a temperature (for example, 80 to 90 ° C.) or lower than the temperature of the lean solution 12B (for example, 120 ° C.).
  • a temperature for example, 80 to 90 ° C.
  • the temperature of the lean solution 12B for example, 120 ° C.
  • the second heat exchanger 23B is installed, by utilizing the heat of the CO 2 gas 41 accompanied by water vapor, a part of the rich solution 12A 1 by heat exchange, the CO 2 gas 41 accompanied by water vapor The temperature drops. As a result, it is possible to reduce the capacity of the cooling unit 42 interposed in the downstream gas discharge line L 21 of the second heat exchanger 23B and the amount of cooling water to be used.
  • the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in second heat exchanger 23B to a temperature of the temperature (e.g., 120 ° C.) the following solutions, preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, the rich solution flows ⁇ 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to obtain a higher-temperature rich solution 12A 4 and introduced into the regeneration tower 14.
  • the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
  • FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted. As shown in FIG. 3, in the CO 2 recovery apparatus 10C of the present embodiment, the third heat using the condensed water 63 in the regenerative heater 61 as preheating means for preheating a part of the branched rich solution 12A 1. The exchange unit 23C is used.
  • the third heat exchanging portion 23C is interposed in the condensed water discharge line L 23 and preheats a part of the rich solution 12A 1 branched by the condensed water 63 to obtain a preheated rich solution 12A 2 . Since the temperature of the condensed water 63 is, for example, 130 to 140 ° C., a part of the branched rich solution 12A 1 can be preheated to the temperature of the lean solution 12B or less.
  • CO 2 is absorbed by the absorption tower 13 and a part of the rich solution 12A introduced into the regeneration tower 14 is branched, and the part of the branched rich solution 12A 1 is used as the lean solution.
  • a temperature temperature e.g. 120 ° C.
  • preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, the rich solution flows ⁇ 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to obtain a higher-temperature rich solution 12A 4 and introduced into the regeneration tower 14.
  • the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
  • FIG. 4 is a schematic diagram of a CO 2 recovery device according to the fourth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted. As shown in FIG. 4, in the CO 2 recovery apparatus 10D of the present embodiment, a fourth heat exchanging unit 23D using the boiler exhaust gas 11 is used as preheating means for preheating a part of the branched rich solution 12A 1 .
  • the fourth heat exchanging portion 23D is interposed in a flue 1001a for discharging the boiler exhaust gas 11 from the boiler 1001, and preheats a part of the rich solution 12A 1 branched by the boiler exhaust gas 11 at the outlet of the air heater (not shown).
  • the preheated rich solution 12A 2 is used. Since the temperature of the boiler exhaust gas 11 at the outlet of the air heater is, for example, 90 to 140 ° C., a part of the branched rich solution 12A 1 can be preheated to the temperature of the lean solution 12B or less.
  • the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in the fourth heat exchanger 23D to a temperature temperature (e.g.
  • the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
  • FIG. 5 is a schematic diagram of a CO 2 recovery device according to the fifth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
  • the CO 2 recovery apparatus 10E of the present embodiment as a preheating means for preheating a part of the rich solution 12A 1 branched, a part of the semi-rich solution is extracted in the intermediate part of the regeneration tower 14, and a fifth heat exchanging unit 23E using the semi-rich solution 12B 0 of this portion.
  • the fifth heat exchanging unit 23E is interposed extraction line L 24 of the semi-rich solution 12B 0, preheating the rich solution 12A 1 part branching the semi-rich solution 12B 0, is set to preheat the rich solution 12A 2. Since the temperature of the semi-rich solution 12B 0 is, for example, 100 to 120 ° C., a part of the rich solution 12A 1 branched can be preheated to the temperature of the lean solution 12B or less.
  • the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in the fifth heat exchanger 23E to a temperature temperature (e.g.
  • the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
  • FIG. 6 is a schematic diagram of a CO 2 recovery apparatus according to the sixth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted. 7 and 8 are flowcharts of the rich solution branching amount control for carrying out the sixth embodiment. As shown in FIG.
  • a concentration measuring unit 81 that further measures the concentration of the CO 2 absorbent in the rich solution 12A 0 ;
  • a temperature measuring means 82 for measuring the temperature of the heated rich solution 12A 4 immediately before being introduced into the regeneration tower 14 and a pressure measuring means 83 for measuring the pressure in the regeneration tower 14 are provided. Accordingly, the flow rate of a part of the rich solution 12A 1 extracted from the rich solution 12A 0 is controlled by operating the flow rate adjustment valve 85 interposed in the rich solution branch / return pipe L 13 .
  • the concentration measuring means 81 for measuring the concentration of the CO 2 absorbent in the rich solution absorption liquid is interposed in the rich solution supply pipe L 11 from which the rich solution 12A 0 is extracted from the bottom of the absorption tower, and the temperature measuring means 82 is The pressure measuring means 83 is interposed in the gas discharge line L 21 and is interposed in the rich solution supply pipe L 11 immediately before introduction into the regeneration tower 14. Then, from these measurement results, an appropriate temperature of the rich solution 12A 4 introduced into the regeneration tower 14 is obtained, and the preheating temperature is controlled by the control device so as to be the appropriate value.
  • condition A the concentration of the absorbent in the rich solution increases (condition A), the CO 2 concentration in the rich solution decreases (condition B), and the regeneration tower pressure increases (condition C).
  • condition B the concentration of the absorbent in the rich solution increases
  • condition C the regeneration tower pressure increases (condition C).
  • S10 the temperature set value of the rich solution supplied to the regeneration tower 14
  • S11 control is performed to increase the branching amount of a part of the rich solution 12A 1 of the rich solution 12A 0 (S11).
  • S12 The supply temperature of the rich solution 12A 4 at the inlet of the regeneration tower 14 is confirmed (S12), and if it is appropriate (normal), the current operation is maintained (S13).
  • low temperature (low) again returns to S11, performs control to increase the branching of the rich solution 12A 0.
  • the temperature of the supply liquid at the inlet of the regeneration tower is appropriately maintained.
  • the concentration of the absorbent in the rich solution decreases (condition D), the CO 2 concentration in the rich solution increases (condition E), and the regeneration tower pressure decreases (condition F).
  • condition D concentration of the absorbent in the rich solution decreases
  • condition E concentration of the absorbent in the rich solution increases
  • condition F regeneration tower pressure decreases
  • the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 becomes too high. Therefore, control is performed to lower the temperature set value of the rich solution supplied to the regeneration tower 14. (S20). In such a case, control is performed to lower the branch amount of a part of the rich solution 12A 1 of the rich solution 12A 0 (S21).
  • S22 The supply temperature of the rich solution at the inlet of the regeneration tower 14 is confirmed (S22), and if it is appropriate (normal), the current operation is maintained (S23).
  • high temperatures (high) again returns to S21, performs control to lower the branching amount of the rich solution 12A 1. Thereby, the temperature of the supply liquid at the inlet of the regeneration tower is appropriately maintained
  • the rich fluid branch amount as to heat exchange hot fluid (wash water 20) than the rich solution 12A 0 By adjusting this, the supply temperature of the rich solution 12A 4 to the regeneration tower 14 can be properly maintained, and energy saving can be continuously achieved.
  • Tables 1 and 2 below show examples of operating conditions and set values of the supply temperature of the rich solution 12A 4 supplied to the regeneration tower 14.
  • Table 1 when “standard” is set when the temperature of the set temperature condition in the regeneration tower 14 is 90 ° C., the concentration of the absorbent in the rich solution 12A 4 increases (condition A: standard 1.05 times), when the CO 2 concentration in the rich solution decreases (condition B: 0.95 times the standard), and the regeneration tower pressure increases (condition C: 1.05 times the standard). Changes the temperature setting value of the rich solution 12A 4 supplied to the regeneration tower 14 to 100 ° C.
  • the regeneration tower inlet supply temperature of the rich solution 12A 4 can be maintained at a predetermined set value.
  • CO 2 recovery device 11A CO 2 -containing exhaust gas 12 CO 2 absorbent 12A rich solution 12B lean solution 13 CO 2 absorption tower (absorption tower) 13A CO 2 absorption part 13B Flushing part 14 Absorption liquid regeneration tower (regeneration tower) 20 Wash water

Abstract

A CO2 recovery device which recovers and removes CO2 in a CO2-containing discharge gas (11A) including CO2, in a CO2 absorption tower (13), using a CO2 absorbing solution (12) is provided with: a first heat exchanger (23A) serving as a preheating means for preheating, to a temperature equal to or less than the temperature of a lean solution, a rich solution portion (12A1) separated, at a separation section (X), from a rich solution (12A) which has absorbed CO2 in the absorption tower; and a rich/lean solution heat exchanger (52) for performing heat exchange between the lean solution (12B) which has had CO2 released therefrom, and a merged rich solution (12A3) obtained by merging a rich solution portion (12A2) preheated by the preheating means with the rich solution (12A0) at a merging section (Y).

Description

ＣＯ2回収装置およびＣＯ2回収方法CO2 recovery device and CO2 recovery method
　本発明は、省エネルギーを図ったＣＯ2回収装置及び方法に関する。 The present invention relates to a CO 2 recovery apparatus and method for energy saving.
　近年、地球の温暖化現象の原因の一つとして、ＣＯ2による温室効果が指摘され、地球環境を守る上で国際的にもその対策が急務となってきた。ＣＯ2の発生源としては化石燃料を燃焼させるあらゆる人間の活動分野に及び、その排出抑制への要求が一層強まる傾向にある。これに伴い大量の化石燃料を使用する火力発電所などの動力発生設備を対象に、ボイラの燃焼排ガスを例えばアミン系ＣＯ2吸収液と接触させ、燃焼排ガス中のＣＯ2を除去、回収する方法及び回収されたＣＯ2を大気へ放出することなく貯蔵する方法が精力的に研究されている。 In recent years, the greenhouse effect due to CO 2 has been pointed out as one of the causes of global warming, and countermeasures have become urgent internationally to protect the global environment. The source of CO 2 extends to all human activity fields that burn fossil fuels, and there is a tendency for the demand for emission control to become stronger. Along with this, for a power generation facility such as a thermal power plant that uses a large amount of fossil fuel, a method for removing and recovering CO 2 in the combustion exhaust gas by bringing the combustion exhaust gas of the boiler into contact with, for example, an amine-based CO 2 absorbent In addition, methods for storing the recovered CO 2 without releasing it to the atmosphere have been intensively studied.
　また前記のようなＣＯ2吸収液を用い、燃焼排ガスからＣＯ2を除去・回収する工程としては、吸収塔において燃焼排ガスとＣＯ2吸収液とを接触させる工程、ＣＯ2を吸収した吸収液を再生塔において加熱し、ＣＯ2を遊離させると共に吸収液を再生して再び吸収塔に循環して再使用するものが採用されている（特許文献１）。 Further, as a step of removing and recovering CO 2 from the combustion exhaust gas using the above-mentioned CO 2 absorption liquid, a step of bringing the combustion exhaust gas and the CO 2 absorption liquid into contact with each other in an absorption tower, an absorption liquid that has absorbed CO 2 is used. Heating is performed in a regeneration tower to liberate CO 2 and regenerate the absorption liquid, which is then recycled to the absorption tower and reused (Patent Document 1).
　前記ＣＯ2吸収液及び工程を用いて燃焼排ガスのようなＣＯ2含有ガスからＣＯ2を吸収除去・回収する方法においては、これらの工程は燃焼設備に付加して設置されるため、その操業費用もできるだけ低減させなければならない。特に前記工程の内、再生工程はＣＯ2をＣＯ2吸収液から放出させるために、多量の熱エネルギー（水蒸気）を消費するので、可能な限り省エネルギープロセスとする必要がある。 In the method of absorbing and removing and recovering CO 2 from a CO 2 -containing gas such as combustion exhaust gas using the CO 2 absorbing liquid and the process, since these processes are added to the combustion equipment, the operating cost is increased. Must be reduced as much as possible. In particular, among the above steps, the regeneration step consumes a large amount of heat energy (water vapor) in order to release CO 2 from the CO 2 absorbing solution, so that it needs to be an energy saving process as much as possible.
　従来においては、再生塔に供給するＣＯ2を吸収したリッチ溶液を加熱して、再生塔でのＣＯ2を放出される際に使用する水蒸気量の低減を図ることの提案がある（特許文献２、３）。 Conventionally, there is a proposal to reduce the amount of water vapor used when CO 2 is released in the regeneration tower by heating the rich solution that has absorbed CO 2 supplied to the regeneration tower (Patent Document 2). 3).
特開平７－５１５３７号公報Japanese Unexamined Patent Publication No. 7-51537 特表２００９－５３１１６３号公報Special table 2009-531163 gazette 特開２００９－２１４０８９号公報JP 2009-214089 A
　しかしながら、特許文献２の提案では、リッチ溶液を加熱する手段として、吸収塔における一部ＣＯ2を吸収したセミリッチ溶液を用いているので、ＣＯ2回収装置の運転状態に左右され、安定した省エネルギーを図ることができない、という問題がある。また、リッチ吸収液をセミリッチ溶液で熱交換するので、温度差のみの熱交換となり、安定した省エネルギーを図ることができない、という問題がある。 However, in the proposal of Patent Document 2, as a means for heating the rich solution, a semi-rich solution that partially absorbs CO 2 in the absorption tower is used. Therefore, depending on the operating state of the CO 2 recovery device, stable energy saving is achieved. There is a problem that it cannot be planned. In addition, since the rich absorption liquid is heat-exchanged with the semi-rich solution, there is a problem that heat exchange is performed only with a temperature difference and stable energy saving cannot be achieved.
　特許文献３の提案では、ＣＯ2を吸収したリッチ溶液を分岐し、一方を加熱しつつ再生塔に供給するものの、加熱したリッチ溶液と加熱しないリッチ溶液との２種類の異なる温度のリッチ溶液が、別々に再生塔内部に導入されるので、再生にバラつきが生じ、良好な再生ができず、安定した省エネルギーを図ることができない、という問題がある。 In the proposal of Patent Document 3, a rich solution that has absorbed CO 2 is branched, and one of them is supplied to the regeneration tower while being heated, but there are two types of rich solutions of different temperatures, a heated rich solution and a non-heated rich solution. However, since they are separately introduced into the regeneration tower, there is a problem in that the regeneration is uneven, the satisfactory regeneration cannot be performed, and stable energy saving cannot be achieved.
　本発明は、前記問題に鑑み、安定した省エネルギーを図りつつ、エネルギー効率を一層向上させたＣＯ2回収装置及び方法を提供することを課題とする。 In view of the above problems, an object of the present invention is to provide a CO 2 recovery device and method that further improve energy efficiency while achieving stable energy saving.
　上述した課題を解決するための本発明の第１の発明は、ＣＯ2を含有するＣＯ2含有排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去するＣＯ2吸収塔と、ＣＯ2を吸収したリッチ溶液からＣＯ2を分離してＣＯ2吸収液を再生してリーン溶液とする吸収液再生塔と、前記吸収液再生塔でＣＯ2が除去されたリーン溶液をＣＯ2吸収塔でＣＯ2吸収液として再利用するＣＯ2回収装置であって、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液の一部を分岐させ、該分岐した一部のリッチ溶液を予熱する予熱手段と、前記予熱手段で予熱された一部のリッチ溶液をリッチ溶液と合流し、該合流したリッチ溶液と、ＣＯ2を放出したリーン溶液とを熱交換するリッチ・リーン溶液熱交換器と、を具備することを特徴とするＣＯ2回収装置にある。 The first aspect of the present invention to solve the above problems, and the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, the CO 2 An absorption liquid regeneration tower that separates CO 2 from the absorbed rich solution and regenerates the CO 2 absorption liquid to obtain a lean solution, and the lean solution from which CO 2 has been removed by the absorption liquid regeneration tower is converted into CO by the CO 2 absorption tower. 2 CO 2 recovery device to be reused as an absorbing liquid, a part of the rich solution that has absorbed CO 2 in the CO 2 absorption tower is branched, and a preheating means for preheating the branched part of the rich solution; A rich-lean solution heat exchanger that joins a portion of the rich solution preheated by the preheating means with the rich solution and exchanges heat between the joined rich solution and the lean solution that has released CO 2. It is in the CO 2 recovery device characterized by this.
　第２の発明は、第１の発明において、前記予熱手段での予熱温度が、前記リーン溶液の温度以下の温度であることを特徴とするＣＯ2回収装置にある。 A second invention is the CO 2 recovery apparatus according to the first invention, wherein the preheating temperature in the preheating means is equal to or lower than the temperature of the lean solution.
　第３の発明は、第１又は２の発明において、前記リッチ溶液の吸収液のＣＯ2吸収剤の濃度を計測する濃度計測手段と、前記吸収液再生塔に導入する直前のリッチ溶液の温度を計測する温度計測手段と、前記吸収液再生塔内の圧力を計測する圧力計測手段と、これらの計測結果より、前記吸収液再生塔に導入するリッチ溶液の適正温度を求め、該適正値となるように、予熱温度を制御する制御装置とを具備することを特徴とするＣＯ2回収装置にある。 According to a third invention, in the first or second invention, the concentration measuring means for measuring the concentration of the CO 2 absorbent in the absorbing solution of the rich solution, and the temperature of the rich solution immediately before being introduced into the absorbing solution regeneration tower are provided. A temperature measuring means for measuring, a pressure measuring means for measuring the pressure in the absorption liquid regeneration tower, and an appropriate temperature of the rich solution to be introduced into the absorption liquid regeneration tower is obtained from these measurement results, and becomes the appropriate value. Thus, a CO 2 recovery device comprising a control device for controlling the preheating temperature.
　第４の発明は、第３の発明において、前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも低い場合に、前記予熱手段での予熱温度を上昇させる制御を制御装置で実行することを特徴とするＣＯ2回収装置にある。 According to a fourth invention, in the third invention, when the temperature of the rich solution introduced into the absorption liquid regeneration tower is lower than an appropriate temperature set value, the control device controls the control to increase the preheating temperature in the preheating means. The CO 2 recovery device is characterized in that it is executed in the above.
　第５の発明は、第３の発明において、前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも高い場合に、前記予熱手段での予熱温度を下降させる制御を制御装置で実行することを特徴とするＣＯ2回収装置にある。 According to a fifth invention, in the third invention, when the temperature of the rich solution introduced into the absorption liquid regeneration tower is higher than an appropriate temperature set value, the control device controls the control to lower the preheating temperature in the preheating means. The CO 2 recovery device is characterized in that it is executed in the above.
　第６の発明は、第１乃至５のいずれか一つの発明において、水洗部を複数段具備することを特徴とするＣＯ2回収装置にある。 A sixth invention is the CO 2 recovery apparatus according to any one of the first to fifth inventions, wherein the CO 2 recovery device is provided with a plurality of water washing sections.
　第７の発明は、ＣＯ2を含有するＣＯ2含有排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去するＣＯ2吸収塔と、ＣＯ2を吸収したＣＯ2吸収液からＣＯ2を分離してＣＯ2吸収液を再生する吸収液再生塔とを用い、前記吸収液再生塔でＣＯ2が除去されたリーン溶液をＣＯ2吸収塔で再利用するＣＯ2回収方法であって、前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液の一部を分岐させ、該分岐した一部のリッチ溶液を予熱し、前記予熱された一部のリッチ溶液をリッチ溶液と合流し、該合流したリッチ溶液と、ＣＯ2を放出したリーン溶液とを熱交換した後、前記吸収液再生塔内に導入することを特徴とするＣＯ2回収方法にある。 A seventh aspect of the present invention is separated and the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, the CO 2 from the CO 2 absorbent having absorbed CO 2 and by using the absorbent regenerator to regenerate the CO 2 absorbing solution, the lean solution from which CO 2 has been removed by the absorbing solution regeneration tower a CO 2 recovery method be reused in the CO 2 absorber, the CO branches the part of the rich solution that has absorbed CO 2 in 2 absorber, to preheat the rich solution part was the branched, the rich solution of a portion that is the preheating joins the rich solution, rich of flowing該合In the CO 2 recovery method, heat exchange is performed between the solution and the lean solution from which CO 2 has been released, and then the solution is introduced into the absorption liquid regeneration tower.
　第８の発明は、第７の発明において、前記予熱手段での予熱温度が、前記リーン溶液の温度以下の温度であることを特徴とするＣＯ2回収方法にある。 An eighth invention is the CO 2 recovery method according to the seventh invention, wherein the preheating temperature in the preheating means is a temperature equal to or lower than the temperature of the lean solution.
　第９の発明は、第７又は８の発明において、前記リッチ溶液の吸収液のＣＯ2吸収剤の濃度、前記吸収液再生塔に導入する直前のリッチ溶液の温度、及び前記吸収液再生塔内の圧力を計測し、これらの計測結果より、前記吸収液再生塔に導入するリッチ溶液の適正温度を求め、該適正値となるように、予熱温度を制御することを特徴とするＣＯ2回収方法にある。 According to a ninth invention, in the seventh or eighth invention, the concentration of the CO 2 absorbent in the absorbent of the rich solution, the temperature of the rich solution immediately before being introduced into the absorbent regenerator, and the inside of the absorbent regenerator The CO 2 recovery method is characterized in that, from the measurement results, an appropriate temperature of the rich solution introduced into the absorption liquid regeneration tower is obtained, and the preheating temperature is controlled so as to be the appropriate value. It is in.
　第１０の発明は、第９の発明において、前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも低い場合に、前記予熱手段での予熱温度を上昇させる制御を実行することを特徴とするＣＯ2回収方法にある。 In a tenth aspect based on the ninth aspect, when the temperature of the rich solution introduced into the absorption liquid regeneration tower is lower than an appropriate temperature set value, control for increasing the preheating temperature in the preheating means is executed. The CO 2 recovery method is characterized by the above.
　第１１の発明は、第９の発明において、前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも高い場合に、前記予熱手段での予熱温度を下降させる制御を実行することを特徴とするＣＯ2回収方法にある。 In an eleventh aspect based on the ninth aspect, when the temperature of the rich solution introduced into the absorption liquid regeneration tower is higher than an appropriate temperature setting value, control is performed to lower the preheating temperature in the preheating means. The CO 2 recovery method is characterized by the above.
　本発明によれば、ＣＯ2回収装置の低レベルの余熱を効率的に用いることで、再生塔における加熱水蒸気の供給量を低減させることができると共に、安定した省エネルギーを図りつつ、エネルギー効率を一層向上させることができる。 According to the present invention, by efficiently using the low level residual heat of the CO 2 recovery device, it is possible to reduce the supply amount of heated steam in the regeneration tower, and further improve energy efficiency while achieving stable energy saving. Can be improved.
図１は、実施例１に係るＣＯ2回収装置の概略図である。FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment. 図２は、実施例２に係るＣＯ2回収装置の概略図である。FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment. 図３は、実施例３に係るＣＯ2回収装置の概略図である。FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment. 図４は、実施例４に係るＣＯ2回収装置の概略図である。FIG. 4 is a schematic diagram of a CO 2 recovery device according to the fourth embodiment. 図５は、実施例５に係るＣＯ2回収装置の概略図である。FIG. 5 is a schematic diagram of a CO 2 recovery device according to the fifth embodiment. 図６は、実施例６に係るＣＯ2回収装置の概略図である。FIG. 6 is a schematic diagram of a CO 2 recovery apparatus according to the sixth embodiment. 図７は、実施例６を実施するリッチ溶液分岐量制御の流れ図である。FIG. 7 is a flowchart of the rich solution branching amount control for carrying out the sixth embodiment. 図８は、実施例６を実施するリッチ溶液分岐量制御の流れ図である。FIG. 8 is a flowchart of the rich solution branching amount control for carrying out the sixth embodiment. 図９は、試験例と従来例とにおける必要熱量を対比したグラフである。FIG. 9 is a graph comparing required heat amounts in the test example and the conventional example.
　以下、この発明につき図面を参照しつつ詳細に説明する。なお、この実施例により本発明が限定されるものではなく、また、実施例が複数ある場合には、各実施例を組み合わせて構成するものも含むものである。また、下記実施例における構成要素には、当業者が容易に想定できるもの、あるいは実質的に同一のものが含まれる。 Hereinafter, the present invention will be described in detail with reference to the drawings. In addition, this invention is not limited by this Example, Moreover, when there exists multiple Example, what comprises combining each Example is also included. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art or those that are substantially the same.
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図１は、実施例１に係るＣＯ2回収装置の概略図である。
　図１に示すように、本実施例に係るＣＯ2回収装置１０Ａは、ＣＯ2を含有するＣＯ2含有排ガス１１ＡとＣＯ2吸収液（リーン溶液１２Ｂ）とを接触させてＣＯ2を除去するＣＯ2吸収塔（以下「吸収塔」という）１３と、ＣＯ2を吸収したＣＯ2吸収液（リッチ溶液１２Ａ0）を再生する吸収液再生塔１４と、前記吸収液再生塔（以下「再生塔」という）１４でＣＯ2が除去されたリーン溶液１２ＢをＣＯ2吸収塔１３で再利用するＣＯ2回収装置であって、前記ＣＯ2吸収塔１３が、ＣＯ2吸収液によりＣＯ2含有排ガス中のＣＯ2を吸収するＣＯ2吸収部１３Ａと、前記ＣＯ2吸収部１３Ａのガス流れ後流側に設けられ、洗浄水２０によりＣＯ2除去排ガス１１Ｂを冷却すると共に、同伴するＣＯ2吸収液１２を前記洗浄水２０により回収する水洗部１３Ｂと、前記水洗部１３Ｂの液貯留部２１で回収されたＣＯ2吸収液を含む洗浄水２０を前記水洗部１３Ｂの頂部側から供給して循環する循環ラインＬ1とを具備してなる。図１中、符号Ｌ11はリッチ溶液供給管、リーン溶液供給管、Ｌ13はリッチ溶液分岐・返送管を各々図示する。 A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment.
As shown in FIG. 1, CO 2 recovery apparatus 10A according to the present embodiment, CO 2 containing exhaust gas 11A and the CO 2 absorbing liquid containing CO 2 with (lean solution 12B) and contacting the removing CO 2 CO 2 an absorption tower (hereinafter referred to as “absorption tower”) 13, an absorption liquid regeneration tower 14 for regenerating a CO 2 absorption liquid (rich solution 12 A 0 ) that has absorbed CO 2 , and the absorption liquid regeneration tower (hereinafter “regeneration tower”). the lean solution 12B which CO 2 has been removed by) 14 that a CO 2 reused in the CO 2 absorber 13, the CO 2 absorption tower 13, the CO 2 absorbent at a CO 2 content in the flue gas A CO 2 absorbing portion 13A that absorbs CO 2 and a gas downstream side of the CO 2 absorbing portion 13A that cools the CO 2 removal exhaust gas 11B with the wash water 20 and also supplies the accompanying CO 2 absorbing liquid 12 Water recovered by the washing water 20 And parts 13B, is formed by and a circulation line L 1 which circulates and supplies the washing water 20 containing the CO 2 absorbing liquid that has been recovered by the liquid reservoir 21 of the washing unit 13B from the top side of the washing unit 13B . In FIG. 1, symbol L 11 indicates a rich solution supply tube and lean solution supply tube, and L 13 indicates a rich solution branch / return tube.
　本実施例では、前記吸収塔１３でＣＯ2を吸収したリッチ溶液１２Ａ0の一部を分岐部Ｘで分岐させ、該分岐した一部のリッチ溶液１２Ａ1を、該リッチ溶液１２Ａ1の温度よりも高い温度である流体で熱交換して、前記リーン溶液１２Ｂの温度以下の温度まで予熱する予熱手段である第１の熱交換器２３Ａと、前記予熱手段で予熱された一部の予熱リッチ溶液１２Ａ2を、合流部Ｙでリッチ溶液１２Ａ0と合流し、該合流した合流リッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとを熱交換するリッチ・リーン溶液熱交換器５２とを具備している。 In this embodiment, a part of the rich solution 12A 0 that has absorbed CO 2 in the absorption tower 13 is branched at the branching section X, and the part of the rich solution 12A 1 that is branched is removed from the temperature of the rich solution 12A 1 . A first heat exchanger 23A, which is a preheating means for exchanging heat with a fluid having a higher temperature and preheating to a temperature lower than the temperature of the lean solution 12B, and a part of the preheat rich solution preheated by the preheating means 12A 2 is combined with the rich solution 12A 0 at the junction Y, and the rich / lean solution heat exchanger 52 is provided for heat exchange between the merged rich solution 12A 3 and the lean solution 12B from which CO 2 has been released. is doing.
　前記吸収塔１３では、ＣＯ2含有排ガス１１Ａは、ＣＯ2吸収塔１３の下部側に設けられたＣＯ2吸収部１３Ａにおいて、例えばアルカノールアミンをベースとするアミン系のＣＯ2吸収液１２と対向流接触し、ＣＯ2含有排ガス１１Ａ中のＣＯ2は、化学反応（Ｒ－ＮＨ2＋Ｈ2Ｏ＋ＣＯ2→Ｒ－ＮＨ3ＨＣＯ3）によりＣＯ2吸収液１２に吸収される。
　この結果、ＣＯ2吸収部１３Ａを通過して、ＣＯ2吸収塔１３の内部を上昇するＣＯ2除去排ガス１１Ｂには、ＣＯ2が殆ど残存しないものとなる。 In the absorption tower 13, the CO 2 -containing exhaust gas 11 A is counterflowed with an amine-based CO 2 absorption liquid 12 based on, for example, an alkanolamine in a CO 2 absorption section 13 A provided on the lower side of the CO 2 absorption tower 13. contact, CO 2 in the CO 2 containing exhaust gas 11A is absorbed by the CO 2 absorbing liquid 12 by a chemical reaction (R-NH 2 + H 2 O + CO 2 → R-NH 3 HCO 3).
As a result, almost no CO 2 remains in the CO 2 removal exhaust gas 11B passing through the CO 2 absorption section 13A and rising inside the CO 2 absorption tower 13.
　その後、ＣＯ2除去排ガス１１Ｂは、チムニートレイ１６を介して水洗部１３Ｂ側へ上昇し、水洗部１３Ｂの頂部側から供給される洗浄水２０と気液接触して、ＣＯ2除去排ガス１１Ｂに同伴するＣＯ2吸収液１２を循環洗浄により回収する。 Thereafter, the CO 2 removal exhaust gas 11B rises to the water washing section 13B side via the chimney tray 16, contacts the washing water 20 supplied from the top side of the water washing section 13B, and accompanies the CO 2 removal exhaust gas 11B. The CO 2 absorbent 12 to be recovered is recovered by circulation cleaning.
　水洗部１３Ｂでは、チムニートレイ１６の液貯留部２１で貯留した洗浄水２０を循環ラインＬ1で循環させて、循環洗浄するようにしている。
　なお、循環ラインＬ1には冷却部２２を設け、所定の温度（例えば４０℃以下）まで冷却している。
　この循環する洗浄水２０による洗浄によって、ＣＯ2除去排ガス１１Ｂに同伴するＣＯ2吸収液１２を回収・除去することができる。 In the water washing section 13B, the washing water 20 stored in the liquid storage section 21 of the chimney tray 16 is circulated through the circulation line L 1 to perform circulation washing.
Note that the circulation line L 1 of the cooling unit 22 is provided, it is cooled to a predetermined temperature (e.g., 40 ° C. or less).
By washing with washing water 20 to the circulation, the CO 2 absorbing liquid 12 accompanying the CO 2 removing exhaust gas 11B can be collected and removed.
　その後、ＣＯ2吸収液１２が除去されたＣＯ2吸収液除去排ガス１１Ｃは、ＣＯ2吸収塔１３の頂部１３ａから外部へ排出される。なお、符号１９はガス中のミストを捕捉するミストエリミネータを図示する。 Thereafter, the CO 2 absorbent-removed exhaust gas 11C from which the CO 2 absorbent 12 has been removed is discharged from the top portion 13a of the CO 2 absorber 13 to the outside. Reference numeral 19 denotes a mist eliminator that captures mist in the gas.
　吸収塔１３でＣＯ2を吸収したリッチ溶液１２Ａ0は、その塔底部から抜き出され、リッチ溶液供給管Ｌ11に介装されたリッチソルベントポンプ５１により昇圧され、吸収液再生塔１４の頂部側に供給される。 The rich solution 12A 0 that has absorbed CO 2 in the absorption tower 13 is extracted from the bottom of the tower, and is pressurized by the rich solvent pump 51 interposed in the rich solution supply pipe L 11 , so that the top side of the absorption liquid regeneration tower 14 To be supplied.
　本実施例では、このリッチ溶液１２Ａ0が再生塔１４に導入する間において、予熱をして、再生塔１４に導入する加熱リッチ溶液１２Ａ4の温度が適正温度となるようにしている。
　ここで、適正温度とは、例えば再生塔１４内の塔内圧力、吸収液のアミン濃度、アミンの種類による沸点、吸収液中のＣＯ2濃度により、決定される温度のことをいう。 In this embodiment, while the rich solution 12A 0 is introduced into the regeneration tower 14, preheating is performed so that the temperature of the heated rich solution 12A 4 introduced into the regeneration tower 14 becomes an appropriate temperature.
Here, the appropriate temperature refers to a temperature determined by, for example, the pressure in the regeneration tower 14, the amine concentration of the absorption liquid, the boiling point depending on the type of amine, and the CO 2 concentration in the absorption liquid.
　本実施例においては、図１に示すように、予熱手段である第１の熱交換器２３Ａは、洗浄水２０が循環する循環ラインＬ1に介装されている。そして、第１の熱交換器２３Ａにおいて、洗浄水２０の熱を利用して、主流のリッチ溶液１２Ａ0から分岐した一部のリッチ溶液１２Ａ1を予熱し、予熱リッチ溶液１２Ａ2としている。 In the present embodiment, as shown in FIG. 1, the first heat exchanger 23 </ b> A that is a preheating means is interposed in a circulation line L 1 through which the cleaning water 20 circulates. Then, in the first heat exchanger 23A, a part of the rich solution 12A 1 branched from the mainstream rich solution 12A 0 is preheated using the heat of the wash water 20 to obtain a preheat rich solution 12A 2 .
　その後、予熱リッチ溶液１２Ａ2を、主流のリッチ溶液１２Ａ0と合流させて合流リッチ溶液１２Ａ3とし、その後、再生塔１４においてＣＯ2が放散されたリーン溶液１２Ｂとリッチ・リーン溶液熱交換器５２において熱交換し、高温となったリッチ溶液１２Ａ4を再生塔１４に導入している。 Thereafter, the preheated rich solution 12A 2 is merged with the mainstream rich solution 12A 0 to form a merged rich solution 12A 3, and then the lean solution 12B from which CO 2 has been diffused in the regeneration tower 14 and the rich / lean solution heat exchanger 52. The rich solution 12A 4 which has been subjected to heat exchange and has reached a high temperature is introduced into the regeneration tower 14.
　この結果、吸収塔１３でＣＯ2を吸収した低温（例えば３０～５０℃）のリッチ溶液１２Ａ0を、低レベルの温度（例えば５０～６０℃）である洗浄水２０の熱を有効利用して、一部のリッチ溶液１２Ａ1の温度を上昇させている。その後、温度が上昇した予熱リッチ溶液１２Ａ2を本流のリッチ溶液１２Ａ0に合流させた後に、合流リッチ溶液１２Ａ3をリッチ・リーン溶液熱交換器５２で熱交換させて、再生塔１４に供給されるリッチ液１２Ａ4の温度を、適性温度設定値まで高めることができる。 As a result, the low temperature (for example, 30 to 50 ° C.) rich solution 12A 0 that has absorbed the CO 2 in the absorption tower 13 is effectively utilized by using the heat of the washing water 20 at a low level (for example, 50 to 60 ° C.). The temperature of some of the rich solutions 12A 1 is increased. Thereafter, the preheated rich solution 12A 2 whose temperature has been increased is merged with the main rich solution 12A 0 , and then the combined rich solution 12A 3 is heat-exchanged by the rich / lean solution heat exchanger 52 and supplied to the regeneration tower 14. The temperature of the rich liquid 12A 4 can be increased to an appropriate temperature set value.
　この結果、再生塔１４内でのリボイラ必要熱量の低減を図ることができる。また、低レベルの循環水の熱の有効利用を図ることができ、システム全体としての省エネルギー化を図ることができる。 As a result, the reboiler required heat amount in the regeneration tower 14 can be reduced. In addition, it is possible to effectively use the heat of the low-level circulating water, and to save energy as the entire system.
　なお、前記再生塔１４の頂部側から塔内部に放出されたリッチ溶液１２Ａ4は、その塔底部からの水蒸気による加熱により、大部分のＣＯ2を放出する。再生塔１４内で一部または大部分のＣＯ2を放出したＣＯ2吸収液１２は「セミリーン溶液」と呼称される。この図示しないセミリーン溶液は、再生塔１４底部に流下する頃には、ほぼ全てのＣＯ2が除去されたリーン溶液１２Ｂとなる。このリーン溶液１２Ｂは循環ラインＬ20に介装された再生加熱器６１で飽和水蒸気６２により、加熱される。加熱後の飽和水蒸気６２は水蒸気凝縮水６３となる。 The rich solution 12A 4 released into the tower from the top side of the regeneration tower 14 releases most of the CO 2 by heating with water vapor from the bottom of the tower. The CO 2 absorbent 12 that has released part or most of the CO 2 in the regeneration tower 14 is referred to as a “semi-lean solution”. When the semi-lean solution (not shown) flows down to the bottom of the regeneration tower 14, it becomes a lean solution 12B from which almost all of the CO 2 has been removed. The lean solution 12B by saturated steam 62 in the regeneration heater 61 interposed in the circulation line L 20, is heated. The saturated steam 62 after heating becomes steam condensed water 63.
　一方、再生塔１４の塔頂部１４ａからは塔内においてリッチ溶液１２Ａ4及び図示しないセミリーン溶液から逸散された水蒸気を伴ったＣＯ2ガス４１が放出される。
　そして、水蒸気を伴ったＣＯ2ガス４１がガス排出ラインＬ21により導出され、ガス排出ラインＬ21に介装された冷却部４２により水蒸気が凝縮され、分離ドラム４３にて凝縮水４４が分離され、ＣＯ2ガス４５が系外に放出されて、別途圧縮回収等の後処理がなされる。
　分離ドラム４３にて分離された凝縮水４４は凝縮水ラインＬ22に介装された凝縮水循環ポンプ４６にて吸収液再生塔１４の上部に供給される。
　なお、図示していないが、一部の凝縮水４４は洗浄水２０の循環ラインＬ1に供給され、ＣＯ2吸収液除去排ガス１１Ｃに同伴するＣＯ2吸収液１２の吸収に用いるようにしてもよい。 On the other hand, from the top 14a of the regeneration tower 14, CO 2 gas 41 accompanied by water vapor dissipated from the rich solution 12A 4 and a semi-lean solution (not shown) is released in the tower.
Then, CO 2 gas 41 accompanied by water vapor is derived by the gas discharge line L 21, the water vapor is condensed by the cooling unit 42 interposed in the gas discharge line L 21, condensed water 44 is separated in the separation drum 43 The CO 2 gas 45 is released out of the system, and post-processing such as compression recovery is performed separately.
Condensed water 44 separated in the separation drum 43 is supplied to the upper portion of the absorbing solution regeneration tower 14 by the condensed water circulation pump 46 interposed in condensate line L 22.
Although not shown, a portion of the condensed water 44 is fed into the circulation line L 1 of the washing water 20, be used to absorb the CO 2 absorbing liquid 12 to be entrained in the CO 2 absorbing solution removed exhaust 11C Good.
　再生されたＣＯ2吸収液（リーン溶液１２Ｂ）はリーン溶液供給管Ｌ12を介してリーン溶液ポンプ５４によりＣＯ2吸収塔１３側に送られ、ＣＯ2吸収液１２として循環利用される。この際、リーン溶液１２Ｂは、冷却部５５により所定の温度まで冷却して、ＣＯ2吸収部１３Ａ内にノズル５６を介して、供給されている。
　よって、ＣＯ2吸収液１２は、ＣＯ2吸収塔１３と吸収液再生塔１４とを循環する閉鎖経路を形成し、ＣＯ2吸収塔１３のＣＯ2吸収部１３Ａで再利用される。なお、必要に応じて図示しない補給ラインによりＣＯ2吸収液１２は供給され、また必要に応じて図示しないリクレーマによりＣＯ2吸収液１２を再生するようにしている。 The regenerated CO 2 absorbent (lean solution 12B) is sent to the CO 2 absorption tower 13 side by the lean solution pump 54 via the lean solution supply pipe L 12 and circulated and used as the CO 2 absorbent 12. At this time, the lean solution 12B is cooled to a predetermined temperature by the cooling unit 55 and is supplied into the CO 2 absorbing unit 13A through the nozzle 56.
Therefore, the CO 2 absorbing liquid 12 forms a closed path for circulating a CO 2 absorption tower 13 and the absorption solution regenerator 14 is reused in the CO 2 absorbing section 13A of the CO 2 absorber 13. Note that the CO 2 absorbent 12 is supplied from a replenishment line (not shown) as necessary, and the CO 2 absorbent 12 is regenerated by a reclaimer (not shown) as needed.
　なお、ＣＯ2吸収塔１３に供給されるＣＯ2含有排ガス１１Ａは、その前段側に設けられた冷却塔７０において、冷却水７１により冷却され、その後ＣＯ2吸収塔１３内に導入される。なお、冷却水７１の一部もＣＯ2吸収塔１３の洗浄水２０として水洗部１３Ｂの頂部に供給され、ＣＯ2除去排ガス１１Ｂに同伴するＣＯ2吸収液１２の洗浄に用いる場合もある。なお、符号７２は循環ポンプ、７３は冷却器、７４は循環ラインを図示する。 Note that the CO 2 -containing exhaust gas 11A supplied to the CO 2 absorption tower 13 is cooled by the cooling water 71 in the cooling tower 70 provided on the upstream side thereof, and then introduced into the CO 2 absorption tower 13. Incidentally, is fed to the top of the washing unit 13B as wash water 20 also the CO 2 absorber 13 portion of the cooling water 71, is sometimes used for cleaning the CO 2 absorbing liquid 12 accompanying the CO 2 flue gas 11B. Reference numeral 72 denotes a circulation pump, 73 denotes a cooler, and 74 denotes a circulation line.
　このように、本実施例では、前記吸収塔１３でＣＯ2を吸収し、再生塔１４へ導入するリッチ溶液１２Ａ0の一部を分岐させ、該分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液１２Ｂの温度（例えば１２０℃）以下の温度まで第１の熱交換器２３Ａで予熱し、予熱手段で予熱された一部のリッチ溶液１２Ａ2をリッチ溶液１２Ａ0と合流し、該合流したリッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとをリッチ・リーン溶液熱交換器５２で熱交換して、さらに高温のリッチ溶液１２Ａ4とし、再生塔１４内に導入するので、リッチ溶液組成と再生塔圧力に基づく適性温度まで高めることができ、省エネルギー化を図ることができる。 Thus, in this embodiment, the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched The first heat exchanger 23A preheats to a temperature of the solution 12B or lower (for example, 120 ° C.), and a portion of the rich solution 12A 2 preheated by the preheating means is merged with the rich solution 12A 0 and the merged rich Since the solution 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to form a higher temperature rich solution 12A 4 and introduced into the regeneration tower 14, the rich solution composition Therefore, the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
［試験例］
　本発明の実施例１の効果を確認する試験を行った。
　即ち、吸収塔１３から、再生塔１４に導入するリッチ溶液をリッチ・リーン溶液熱交換器５２のみを用いた場合の再生塔１４におけるリボイラの必要熱量を１とし、リッチ溶液の一部を予熱した後、リッチ・リーン溶液熱交換器５２を用いてさらに加熱した場合の再生塔１４におけるリボイラの熱量を較べた。この結果を図９に示す。図９に示すように、基準である場合に較べて６％の省エネルギー化を図ることが確認された。 [Test example]
A test was conducted to confirm the effect of Example 1 of the present invention.
That is, the amount of heat required for the reboiler in the regeneration tower 14 when the rich solution introduced into the regeneration tower 14 from the absorption tower 13 only using the rich lean solution heat exchanger 52 is set to 1, and a part of the rich solution is preheated. Then, the amount of heat of the reboiler in the regeneration tower 14 when further heated using the rich / lean solution heat exchanger 52 was compared. The result is shown in FIG. As shown in FIG. 9, it was confirmed that 6% energy saving was achieved as compared with the standard case.
＜再生塔１４上部放出ＣＯ2ガス４１の利用＞
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図２は、実施例２に係るＣＯ2回収装置の概略図である。なお、図１に示す実施例１に係るＣＯ2回収装置１０Ａと同一の構成については、同一符号を付して重複した説明は省略する。
　図２に示すように、本実施例のＣＯ2回収装置１０Ｂでは、分岐した一部のリッチ溶液１２Ａ1を予熱する予熱手段として、再生塔１４の塔頂部１４ａから排出される、水蒸気を伴ったＣＯ2ガス４１を用いた第２の熱交換部２３Ｂとしている。
　この第２の熱交換部２３Ｂは、水蒸気を伴ったＣＯ2ガス４１が排出されるガス排出ラインＬ21に介装され、水蒸気を伴ったＣＯ2ガス４１で分岐した一部のリッチ溶液１２Ａ1を予熱し、予熱リッチ溶液１２Ａ2としている。
　この水蒸気を伴ったＣＯ2ガス４１の温度は、１００℃以下（例えば６０～１００℃）であるので、分岐した一部のリッチ溶液１２Ａ1をリーン溶液１２Ｂの温度以下まで、予熱することができる。 <Use of CO 2 gas 41 released from regeneration tower 14>
A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
As shown in FIG. 2, in the CO 2 recovery apparatus 10B of the present example, as a preheating means for preheating a part of the rich solution 12A 1 branched, the steam discharged from the top 14a of the regeneration tower 14 was accompanied by water vapor. The second heat exchange unit 23B using the CO 2 gas 41 is used.
This second heat exchanging portion 23B is interposed in a gas discharge line L 21 through which CO 2 gas 41 accompanied by water vapor is discharged, and a part of the rich solution 12A 1 branched by the CO 2 gas 41 accompanied by water vapor. Is preheated to obtain a preheat rich solution 12A 2 .
Since the temperature of the CO 2 gas 41 accompanied with the water vapor is 100 ° C. or lower (for example, 60 to 100 ° C.), a part of the rich solution 12A 1 branched can be preheated to the temperature of the lean solution 12B or lower. .
　ここで、第２の熱交換器２３Ｂでは、分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液１２Ｂの温度（例えば１２０℃）以下の温度（例えば８０～９０℃）まで予熱するのが好ましい。
　これは、予熱リッチ溶液１２Ａ2の温度が高いような場合には、主流のリッチ溶液１２Ａ0と合流した後の合流リッチ溶液１２Ａ3の温度が高くなり、再生塔１４上部での過度の水分フラッシュによる再生塔出口ガスに同伴する水分量の増加のため、冷却部４２での廃熱が増大してしまうからである。 Here, in the second heat exchanger 23B, it is preferable that a part of the branched rich solution 12A 1 is preheated to a temperature (for example, 80 to 90 ° C.) or lower than the temperature of the lean solution 12B (for example, 120 ° C.).
This is because, when the temperature of the preheated rich solution 12A 2 is high, the temperature of the combined rich solution 12A 3 after being combined with the mainstream rich solution 12A 0 becomes high, and excessive moisture flashes in the upper part of the regeneration tower 14 This is because waste heat in the cooling section 42 increases due to an increase in the amount of water accompanying the regeneration tower outlet gas.
　この第２の熱交換器２３Ｂを設置し、水蒸気を伴ったＣＯ2ガス４１の熱を利用して、一部のリッチ溶液１２Ａ1を熱交換することで、水蒸気を伴ったＣＯ2ガス４１の温度は低下する。この結果、第２の熱交換器２３Ｂの後流側のガス排出ラインＬ21に介装される冷却部４２の容量及び使用する冷却水の量の低減を図ることができる。 The second heat exchanger 23B is installed, by utilizing the heat of the CO 2 gas 41 accompanied by water vapor, a part of the rich solution 12A 1 by heat exchange, the CO 2 gas 41 accompanied by water vapor The temperature drops. As a result, it is possible to reduce the capacity of the cooling unit 42 interposed in the downstream gas discharge line L 21 of the second heat exchanger 23B and the amount of cooling water to be used.
　このように、本実施例では、前記吸収塔１３でＣＯ2を吸収し、再生塔１４へ導入するリッチ溶液１２Ａ0の一部を分岐させ、該分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液の温度（例えば１２０℃）以下の温度まで第２の熱交換器２３Ｂで予熱し、予熱手段で予熱された一部のリッチ溶液１２Ａ2をリッチ溶液１２Ａ0と合流し、該合流したリッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとをリッチ・リーン溶液熱交換器５２で熱交換して、さらに高温のリッチ溶液１２Ａ4とし、再生塔１４内に導入するので、リッチ溶液組成と再生塔圧力に基づく適性温度まで高めることができ、省エネルギー化を図ることができる。 Thus, in this embodiment, the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in second heat exchanger 23B to a temperature of the temperature (e.g., 120 ° C.) the following solutions, preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, the rich solution flows該合12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to obtain a higher-temperature rich solution 12A 4 and introduced into the regeneration tower 14. The temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
　実施例１と同様に、１００℃以下の低レベルの流体の熱の有効利用を図ることができる。 As in the first embodiment, it is possible to effectively use the heat of a low level fluid of 100 ° C. or lower.
＜リボイラ凝縮水６３の利用＞
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図３は、実施例３に係るＣＯ2回収装置の概略図である。なお、図１に示す実施例１に係るＣＯ2回収装置１０Ａと同一の構成については、同一符号を付して重複した説明は省略する。
　図３に示すように、本実施例のＣＯ2回収装置１０Ｃでは、分岐した一部のリッチ溶液１２Ａ1を予熱する予熱手段として、再生加熱器６１での凝縮水６３を用いた第３の熱交換部２３Ｃとしている。
　この第３の熱交換部２３Ｃは、凝縮水排出ラインＬ23に介装され、凝縮水６３により分岐した一部のリッチ溶液１２Ａ1を予熱し、予熱リッチ溶液１２Ａ2としている。
　この凝縮水６３の温度は、例えば１３０～１４０℃であるので、分岐した一部のリッチ溶液１２Ａ1をリーン溶液１２Ｂの温度以下まで、予熱することができる。 <Use of reboiler condensate 63>
A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
As shown in FIG. 3, in the CO 2 recovery apparatus 10C of the present embodiment, the third heat using the condensed water 63 in the regenerative heater 61 as preheating means for preheating a part of the branched rich solution 12A 1. The exchange unit 23C is used.
The third heat exchanging portion 23C is interposed in the condensed water discharge line L 23 and preheats a part of the rich solution 12A 1 branched by the condensed water 63 to obtain a preheated rich solution 12A 2 .
Since the temperature of the condensed water 63 is, for example, 130 to 140 ° C., a part of the branched rich solution 12A 1 can be preheated to the temperature of the lean solution 12B or less.
　このように、本実施例では、前記吸収塔１３でＣＯ2を吸収し、再生塔１４へ導入するリッチ溶液１２Ａの一部を分岐させ、該分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液１２Ｂの温度（例えば１２０℃）以下の温度まで第３の熱交換器２３Ｃで予熱し、予熱手段で予熱された一部のリッチ溶液１２Ａ2をリッチ溶液１２Ａ0と合流し、該合流したリッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとをリッチ・リーン溶液熱交換器５２で熱交換して、さらに高温のリッチ溶液１２Ａ4とし、再生塔１４内に導入するので、リッチ溶液組成と再生塔圧力に基づく適性温度まで高めることができ、省エネルギー化を図ることができる。 Thus, in the present embodiment, CO 2 is absorbed by the absorption tower 13 and a part of the rich solution 12A introduced into the regeneration tower 14 is branched, and the part of the branched rich solution 12A 1 is used as the lean solution. preheated in the third heat exchanger 23C to a temperature temperature (e.g. 120 ° C.) of less 12B, preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, the rich solution flows該合12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to obtain a higher-temperature rich solution 12A 4 and introduced into the regeneration tower 14. The temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
＜ボイラ排ガス１１の利用＞
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図４は、実施例４に係るＣＯ2回収装置の概略図である。なお、図１に示す実施例１に係るＣＯ2回収装置１０Ａと同一の構成については、同一符号を付して重複した説明は省略する。
　図４に示すように、本実施例のＣＯ2回収装置１０Ｄでは、分岐した一部のリッチ溶液１２Ａ1を予熱する予熱手段として、ボイラ排ガス１１を用いた第４の熱交換部２３Ｄとしている。
　この第４の熱交換部２３Ｄは、ボイラ１００１からボイラ排ガス１１を排出する煙道１００１ａに介装され、エアヒータ（図示せず）出口のボイラ排ガス１１により分岐した一部のリッチ溶液１２Ａ1を予熱し、予熱リッチ溶液１２Ａ2としている。
　このエアヒータ出口のボイラ排ガス１１の温度は、例えば９０～１４０℃であるので、分岐した一部のリッチ溶液１２Ａ1をリーン溶液１２Ｂの温度以下まで、予熱することができる。 <Use of boiler exhaust gas 11>
A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 4 is a schematic diagram of a CO 2 recovery device according to the fourth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
As shown in FIG. 4, in the CO 2 recovery apparatus 10D of the present embodiment, a fourth heat exchanging unit 23D using the boiler exhaust gas 11 is used as preheating means for preheating a part of the branched rich solution 12A 1 .
The fourth heat exchanging portion 23D is interposed in a flue 1001a for discharging the boiler exhaust gas 11 from the boiler 1001, and preheats a part of the rich solution 12A 1 branched by the boiler exhaust gas 11 at the outlet of the air heater (not shown). The preheated rich solution 12A 2 is used.
Since the temperature of the boiler exhaust gas 11 at the outlet of the air heater is, for example, 90 to 140 ° C., a part of the branched rich solution 12A 1 can be preheated to the temperature of the lean solution 12B or less.
　このように、本実施例では、前記吸収塔１３でＣＯ2を吸収し、再生塔１４へ導入するリッチ溶液１２Ａ0の一部を分岐させ、該分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液１２Ｂの温度（例えば１２０℃）以下の温度まで第４の熱交換器２３Ｄで予熱し、予熱手段で予熱された一部のリッチ溶液１２Ａ2をリッチ溶液１２Ａ0と合流し、該合流したリッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとをリッチ・リーン溶液熱交換器５２で熱交換して、さらに高温のリッチ溶液１２Ａ4とし、再生塔１４内に導入するので、リッチ溶液組成と再生塔圧力に基づく適性温度まで高めることができ、省エネルギー化を図ることができる。 Thus, in this embodiment, the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in the fourth heat exchanger 23D to a temperature temperature (e.g. 120 ° C.) of the following solutions 12B, preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, rich of flowing該合Since the solution 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to form a higher temperature rich solution 12A 4 and introduced into the regeneration tower 14, the rich solution composition Therefore, the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
＜セミリッチ溶液＞
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図５は、実施例５に係るＣＯ2回収装置の概略図である。なお、図１に示す実施例１に係るＣＯ2回収装置１０Ａと同一の構成については、同一符号を付して重複した説明は省略する。
　図５に示すように、本実施例のＣＯ2回収装置１０Ｅでは、分岐した一部のリッチ溶液１２Ａ1を予熱する予熱手段として、再生塔１４の中間部分において、セミリッチ溶液の一部を抜き出し、この一部のセミリッチ溶液１２Ｂ0を用いた第５の熱交換部２３Ｅとしている。
　この第５の熱交換部２３Ｅは、セミリッチ溶液１２Ｂ0の抜き出しラインＬ24に介装され、セミリッチ溶液１２Ｂ0により分岐した一部のリッチ溶液１２Ａ1を予熱し、予熱リッチ溶液１２Ａ2としている。
　このセミリッチ溶液１２Ｂ0の温度は、例えば１００～１２０℃であるので、分岐した一部のリッチ溶液１２Ａ1をリーン溶液１２Ｂの温度以下まで、予熱することができる。 <Semi-rich solution>
A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 5 is a schematic diagram of a CO 2 recovery device according to the fifth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
As shown in FIG. 5, in the CO 2 recovery apparatus 10E of the present embodiment, as a preheating means for preheating a part of the rich solution 12A 1 branched, a part of the semi-rich solution is extracted in the intermediate part of the regeneration tower 14, and a fifth heat exchanging unit 23E using the semi-rich solution 12B 0 of this portion.
The fifth heat exchanging unit 23E is interposed extraction line L 24 of the semi-rich solution 12B 0, preheating the rich solution 12A 1 part branching the semi-rich solution 12B 0, is set to preheat the rich solution 12A 2.
Since the temperature of the semi-rich solution 12B 0 is, for example, 100 to 120 ° C., a part of the rich solution 12A 1 branched can be preheated to the temperature of the lean solution 12B or less.
　このように、本実施例では、前記吸収塔１３でＣＯ2を吸収し、再生塔１４へ導入するリッチ溶液１２Ａ0の一部を分岐させ、該分岐した一部のリッチ溶液１２Ａ1を前記リーン溶液１２Ｂの温度（例えば１２０℃）以下の温度まで第５の熱交換器２３Ｅで予熱し、予熱手段で予熱された一部のリッチ溶液１２Ａ2をリッチ溶液１２Ａ0と合流し、該合流したリッチ溶液１２Ａ3と、ＣＯ2を放出したリーン溶液１２Ｂとをリッチ・リーン溶液熱交換器５２で熱交換して、さらに高温のリッチ溶液１２Ａ4とし、再生塔１４内に導入するので、リッチ溶液組成と再生塔圧力に基づく適性温度まで高めることができ、省エネルギー化を図ることができる。 Thus, in this embodiment, the absorbs CO 2 in the absorption tower 13 branches the part of the rich solution 12A 0 to be introduced into the regeneration tower 14, the lean and rich solution 12A 1 part of the said branched preheated in the fifth heat exchanger 23E to a temperature temperature (e.g. 120 ° C.) of the following solutions 12B, preheated part of the rich solution 12A 2 in the preheating unit joins the rich solution 12A 0, rich of flowing該合Since the solution 12A 3 and the lean solution 12B from which CO 2 has been released are heat-exchanged by the rich / lean solution heat exchanger 52 to form a higher temperature rich solution 12A 4 and introduced into the regeneration tower 14, the rich solution composition Therefore, the temperature can be increased to an appropriate temperature based on the regeneration tower pressure, and energy saving can be achieved.
　本発明による実施例に係るＣＯ2回収装置について、図面を参照して説明する。図６は、実施例６に係るＣＯ2回収装置の概略図である。なお、図１に示す実施例１に係るＣＯ2回収装置１０Ａと同一の構成については、同一符号を付して重複した説明は省略する。また、図７及び８は、実施例６を実施するリッチ溶液分岐量制御の流れ図である。
　図６に示すように、本実施例のＣＯ2回収装置１０Ｆでは、実施例１のＣＯ2回収装置１０Ａにおいて、さらにリッチ溶液１２Ａ0のＣＯ2吸収剤の濃度を計測する濃度計測手段８１と、再生塔１４に導入する直前の加熱リッチ溶液１２Ａ4の温度を計測する温度計測手段８２と、再生塔１４内の圧力を測定する圧力計測手段８３とを具備し、それらの情報を制御手段８４で判断して、リッチ溶液１２Ａ0から抜き出す一部のリッチ溶液１２Ａ1の流量の制御を、リッチ溶液分岐・返送管Ｌ13に介装した流量調整弁８５の操作により行うようにしている。 A CO 2 recovery apparatus according to an embodiment of the present invention will be described with reference to the drawings. FIG. 6 is a schematic diagram of a CO 2 recovery apparatus according to the sixth embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted. 7 and 8 are flowcharts of the rich solution branching amount control for carrying out the sixth embodiment.
As shown in FIG. 6, in the CO 2 recovery device 10F of the present embodiment, in the CO 2 recovery device 10A of the first embodiment, a concentration measuring unit 81 that further measures the concentration of the CO 2 absorbent in the rich solution 12A 0 ; A temperature measuring means 82 for measuring the temperature of the heated rich solution 12A 4 immediately before being introduced into the regeneration tower 14 and a pressure measuring means 83 for measuring the pressure in the regeneration tower 14 are provided. Accordingly, the flow rate of a part of the rich solution 12A 1 extracted from the rich solution 12A 0 is controlled by operating the flow rate adjustment valve 85 interposed in the rich solution branch / return pipe L 13 .
　リッチ溶液の吸収液のＣＯ2吸収剤の濃度を計測する濃度計測手段８１は、吸収塔底部からリッチ溶液１２Ａ0が抜き出されるリッチ溶液供給管Ｌ11に介装され、温度計測手段８２は、再生塔１４への導入直前のリッチ溶液供給管Ｌ11に介装され、圧力計測手段８３は、ガス排出ラインＬ21に介装されている。そして、これらの計測結果より、再生塔１４に導入するリッチ溶液１２Ａ4の適正温度を求め、該適正値となるように、予熱温度を制御装置により制御するようにしている。 The concentration measuring means 81 for measuring the concentration of the CO 2 absorbent in the rich solution absorption liquid is interposed in the rich solution supply pipe L 11 from which the rich solution 12A 0 is extracted from the bottom of the absorption tower, and the temperature measuring means 82 is The pressure measuring means 83 is interposed in the gas discharge line L 21 and is interposed in the rich solution supply pipe L 11 immediately before introduction into the regeneration tower 14. Then, from these measurement results, an appropriate temperature of the rich solution 12A 4 introduced into the regeneration tower 14 is obtained, and the preheating temperature is controlled by the control device so as to be the appropriate value.
　そして、図７に示すように、リッチ溶液中の吸収剤の濃度が上昇する（条件Ａ）、リッチ溶液中のＣＯ2濃度が低下する（条件Ｂ）、再生塔圧力が上昇する（条件Ｃ）の少なくとも一つが変動した場合、再生塔１４に供給されるリッチ溶液１２Ａ4の温度が、低すぎることとなるので、再生塔１４に供給するリッチ溶液の温度設定値を上昇させる制御を実施する（Ｓ１０）。
　このような場合、リッチ溶液１２Ａ0の一部のリッチ溶液１２Ａ1の分岐量を上昇させる制御を行う（Ｓ１１）。
　再生塔１４入口のリッチ溶液１２Ａ4の供給温度を確認して（Ｓ１２）、適切（正常）であれば、現状の運転を維持する（Ｓ１３）。
　これに対し、温度が低ければ（低い）、再度、Ｓ１１に戻り、リッチ溶液１２Ａ0の分岐量を上昇させる制御を行う。
　これにより、再生塔入口供給液の温度を適切に維持するようにしている。 As shown in FIG. 7, the concentration of the absorbent in the rich solution increases (condition A), the CO 2 concentration in the rich solution decreases (condition B), and the regeneration tower pressure increases (condition C). When at least one of these changes, the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 is too low, and therefore, control is performed to increase the temperature set value of the rich solution supplied to the regeneration tower 14 ( S10).
In such a case, control is performed to increase the branching amount of a part of the rich solution 12A 1 of the rich solution 12A 0 (S11).
The supply temperature of the rich solution 12A 4 at the inlet of the regeneration tower 14 is confirmed (S12), and if it is appropriate (normal), the current operation is maintained (S13).
In contrast, low temperature (low) again returns to S11, performs control to increase the branching of the rich solution 12A 0.
Thereby, the temperature of the supply liquid at the inlet of the regeneration tower is appropriately maintained.
　この結果、再生塔１４での加熱によるＣＯ2放散に余分な熱エネルギーが必要とならず、再生塔１４に供給されるリッチ溶液１２Ａ0温度の不適正な条件となることを防止することにより、省エネ化が図れる。 As a result, extra heat energy is not required for CO 2 emission due to heating in the regeneration tower 14, thereby preventing an inappropriate condition of the temperature of the rich solution 12A 0 supplied to the regeneration tower 14. Energy saving can be achieved.
　また、図８に示すように、リッチ溶液中の吸収剤の濃度が低下する（条件Ｄ）、リッチ溶液中のＣＯ2濃度が上昇する（条件Ｅ）、再生塔圧力が低下する（条件Ｆ）の少なくとも一つが変動した場合、再生塔１４に供給されるリッチ溶液１２Ａ4の温度が、高くなりすぎることとなるので、再生塔１４に供給するリッチ溶液の温度設定値を下降させる制御を実施する（Ｓ２０）。
　このような場合、リッチ溶液１２Ａ0の一部のリッチ溶液１２Ａ1の分岐量を下降させる制御を行う（Ｓ２１）。
　再生塔１４入口のリッチ溶液の供給温度を確認して（Ｓ２２）、適切（正常）であれば、現状の運転を維持する（Ｓ２３）。
　これに対し、温度が高ければ（高い）、再度、Ｓ２１に戻り、リッチ溶液１２Ａ1の分岐量を下降させる制御を行う。
　これにより、再生塔入口供給液の温度を適切に維持するようにしている。 Further, as shown in FIG. 8, the concentration of the absorbent in the rich solution decreases (condition D), the CO 2 concentration in the rich solution increases (condition E), and the regeneration tower pressure decreases (condition F). When at least one of the above changes, the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 becomes too high. Therefore, control is performed to lower the temperature set value of the rich solution supplied to the regeneration tower 14. (S20).
In such a case, control is performed to lower the branch amount of a part of the rich solution 12A 1 of the rich solution 12A 0 (S21).
The supply temperature of the rich solution at the inlet of the regeneration tower 14 is confirmed (S22), and if it is appropriate (normal), the current operation is maintained (S23).
In contrast, high temperatures (high) again returns to S21, performs control to lower the branching amount of the rich solution 12A 1.
Thereby, the temperature of the supply liquid at the inlet of the regeneration tower is appropriately maintained.
　この結果、再生塔１４上部での過度の水分フラッシュによる再生塔出口ガスに同伴する水分量の増加を防ぎ、冷却部４２での廃熱の増大を防止することができる。 As a result, it is possible to prevent an increase in the amount of moisture accompanying the regeneration tower outlet gas due to excessive moisture flushing at the top of the regeneration tower 14 and to prevent an increase in waste heat in the cooling section 42.
　また、本実施例では、リッチ溶液の組成と再生塔供給部での温度を連続的に検知することで、リッチ溶液１２Ａ0よりも高温の流体（洗浄水２０）と熱交換させるリッチ液分岐量を調節することにより、リッチ溶液１２Ａ4の再生塔１４への供給温度を適正に維持し、連続的に省エネルギー化を図ることができる。 Further, in this embodiment, by continuously sensing the temperature of the composition and regenerator supply of rich solution, the rich fluid branch amount as to heat exchange hot fluid (wash water 20) than the rich solution 12A 0 By adjusting this, the supply temperature of the rich solution 12A 4 to the regeneration tower 14 can be properly maintained, and energy saving can be continuously achieved.
　下記表１及び２に運転条件と再生塔１４に供給するリッチ溶液１２Ａ4の供給温度の設定値の例を示す。
　表１に示すように、再生塔１４での設定温度条件の温度が９０℃の場合を「標準」と設定した場合、リッチ溶液１２Ａ4中の吸収剤の濃度が上昇する（条件Ａ:標準の１．０５倍）、リッチ溶液中のＣＯ2濃度が低下する（条件Ｂ：標準の０．９５倍）、再生塔圧力が上昇する（条件Ｃ：標準の１．０５倍）となった場合には、再生塔１４に供給するリッチ溶液１２Ａ4の温度の設定値を１００℃に変更する。そして、リッチ溶液の一部を分岐して予熱手段で予熱し、再生塔１４に供給するリッチ溶液１２Ａ4の温度が１００℃になるように、流量調整弁８５を操作する制御を行う。
　これにより、リッチ溶液１２Ａ4の再生塔入口供給温度を所定の設定値に維持することができる。 Tables 1 and 2 below show examples of operating conditions and set values of the supply temperature of the rich solution 12A 4 supplied to the regeneration tower 14.
As shown in Table 1, when “standard” is set when the temperature of the set temperature condition in the regeneration tower 14 is 90 ° C., the concentration of the absorbent in the rich solution 12A 4 increases (condition A: standard 1.05 times), when the CO 2 concentration in the rich solution decreases (condition B: 0.95 times the standard), and the regeneration tower pressure increases (condition C: 1.05 times the standard). Changes the temperature setting value of the rich solution 12A 4 supplied to the regeneration tower 14 to 100 ° C. Then, a part of the rich solution is branched and preheated by the preheating means, and the flow rate adjusting valve 85 is controlled so that the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 becomes 100 ° C.
Thereby, the regeneration tower inlet supply temperature of the rich solution 12A 4 can be maintained at a predetermined set value.
Figure JPOXMLDOC01-appb-T000001
  
Figure JPOXMLDOC01-appb-T000001
  
　また、表２に示すように、再生塔での設定温度条件の温度が９０℃の場合を「標準」と設定した場合、リッチ溶液中の吸収剤の濃度が低下する（条件Ｄ:標準の０．９５倍）、リッチ溶液中のＣＯ2濃度が上昇する（条件Ｅ：標準の１．０５倍）、再生塔圧力が低下する（条件Ｆ：標準の０．９５倍）となった場合には、再生塔１４に供給するリッチ溶液１２Ａ4の温度の設定値を７５℃に変更する。そして、リッチ溶液の一部を分岐して予熱手段で予熱し、再生塔１４に供給するリッチ溶液１２Ａ4の温度が７５℃になるように、流量調整弁８５を操作する制御を行う。
　これにより、リッチ溶液１２Ａ4の再生塔入口供給温度を所定の設定値に維持することができる。 Further, as shown in Table 2, when “standard” is set when the temperature of the set temperature condition in the regeneration tower is 90 ° C., the concentration of the absorbent in the rich solution decreases (Condition D: Standard 0) .95 times), when the CO 2 concentration in the rich solution increases (condition E: 1.05 times the standard) and the regeneration tower pressure decreases (condition F: 0.95 times the standard) Then, the set value of the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 is changed to 75 ° C. Then, a part of the rich solution is branched and preheated by the preheating means, and the flow rate adjusting valve 85 is controlled so that the temperature of the rich solution 12A 4 supplied to the regeneration tower 14 becomes 75 ° C.
Thereby, the regeneration tower inlet supply temperature of the rich solution 12A 4 can be maintained at a predetermined set value.
Figure JPOXMLDOC01-appb-T000002
  
Figure JPOXMLDOC01-appb-T000002
  
　１０Ａ～１０Ｆ　ＣＯ2回収装置
　１１Ａ　ＣＯ2含有排ガス
　１２　ＣＯ2吸収液
　１２Ａ　リッチ溶液
　１２Ｂ　リーン溶液
　１３　ＣＯ2吸収塔（吸収塔）
　１３Ａ　ＣＯ2吸収部
　１３Ｂ　水洗部
　１４　吸収液再生塔（再生塔）
　２０　洗浄水 10A to 10F CO 2 recovery device 11A CO 2 -containing exhaust gas 12 CO 2 absorbent 12A rich solution 12B lean solution 13 CO 2 absorption tower (absorption tower)
13A CO 2 absorption part 13B Flushing part 14 Absorption liquid regeneration tower (regeneration tower)
20 Wash water

Claims (11)

  1. 　ＣＯ2を含有するＣＯ2含有排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去するＣＯ2吸収塔と、
    　ＣＯ2を吸収したリッチ溶液からＣＯ2を分離してＣＯ2吸収液を再生してリーン溶液とする吸収液再生塔と、
    　前記吸収液再生塔でＣＯ2が除去されたリーン溶液をＣＯ2吸収塔でＣＯ2吸収液として再利用するＣＯ2回収装置であって、
    　前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液の一部を分岐させ、該分岐した一部のリッチ溶液を予熱する予熱手段と、
    　前記予熱手段で予熱された一部のリッチ溶液をリッチ溶液と合流し、該合流したリッチ溶液と、ＣＯ2を放出したリーン溶液とを熱交換するリッチ・リーン溶液熱交換器と、を具備することを特徴とするＣＯ2回収装置。     And the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2,
    And absorbing solution regeneration tower to lean solution to separate the CO 2 to play the CO 2 absorbing solution from the rich solution that has absorbed CO 2,
    Wherein the absorption liquid lean solution from which CO 2 has been removed in the regeneration tower a CO 2 is reused as a CO 2 absorbing solution in a CO 2 absorption tower,
    A preheating means for branching a part of the rich solution that has absorbed CO 2 in the CO 2 absorption tower and preheating the branched rich solution;
    A rich-lean solution heat exchanger that joins a portion of the rich solution preheated by the preheating means with the rich solution and exchanges heat between the joined rich solution and the lean solution that has released CO 2. A CO 2 recovery device characterized by that.
  2. 　請求項１において、
    　前記予熱手段での予熱温度が、前記リーン溶液の温度以下の温度であることを特徴とするＣＯ2回収装置。     In claim 1,
    The CO 2 recovery apparatus, wherein the preheating temperature in the preheating means is a temperature equal to or lower than the temperature of the lean solution.
  3. 　請求項１又は２において、
    　前記リッチ溶液の吸収液のＣＯ2吸収剤の濃度を計測する濃度計測手段と、前記吸収液再生塔に導入する直前のリッチ溶液の温度を計測する温度計測手段と、前記吸収液再生塔内の圧力を計測する圧力計測手段と、
    　これらの計測結果より、前記吸収液再生塔に導入するリッチ溶液の適正温度を求め、該適正値となるように、予熱温度を制御する制御装置とを具備することを特徴とするＣＯ2回収装置。     In claim 1 or 2,
    A concentration measuring means for measuring the concentration of the CO 2 absorbent in the rich solution absorption liquid; a temperature measuring means for measuring the temperature of the rich solution immediately before being introduced into the absorption liquid regeneration tower; Pressure measuring means for measuring pressure;
    From these measurement results, a CO 2 recovery device is provided, which comprises a control device for determining an appropriate temperature of the rich solution to be introduced into the absorption liquid regeneration tower and controlling the preheating temperature so as to be the appropriate value. .
  4. 　請求項３において、
    　前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも低い場合に、前記予熱手段での予熱温度を上昇させる制御を制御装置で実行することを特徴とするＣＯ2回収装置。     In claim 3,
    A CO 2 recovery device, wherein a control device executes control to increase the preheating temperature in the preheating means when the temperature of the rich solution introduced into the absorption liquid regeneration tower is lower than an appropriate temperature set value. .
  5. 　請求項３において、
    　前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも高い場合に、前記予熱手段での予熱温度を下降させる制御を制御装置で実行することを特徴とするＣＯ2回収装置。     In claim 3,
    A CO 2 recovery device, characterized in that, when the temperature of the rich solution introduced into the absorption liquid regeneration tower is higher than an appropriate temperature set value, the control device executes control for lowering the preheating temperature in the preheating means. .
  6. 　請求項１乃至５のいずれか一つにおいて、
    　水洗部を複数段具備することを特徴とするＣＯ2回収装置。     In any one of Claims 1 thru | or 5,
    A CO 2 recovery device comprising a plurality of water washing sections.
  7. 　ＣＯ2を含有するＣＯ2含有排ガスとＣＯ2吸収液とを接触させてＣＯ2を除去するＣＯ2吸収塔と、ＣＯ2を吸収したＣＯ2吸収液からＣＯ2を分離してＣＯ2吸収液を再生する吸収液再生塔とを用い、前記吸収液再生塔でＣＯ2が除去されたリーン溶液をＣＯ2吸収塔で再利用するＣＯ2回収方法であって、
    　前記ＣＯ2吸収塔でＣＯ2を吸収したリッチ溶液の一部を分岐させ、該分岐した一部のリッチ溶液を予熱し、前記予熱された一部のリッチ溶液をリッチ溶液と合流し、該合流したリッチ溶液と、ＣＯ2を放出したリーン溶液とを熱交換した後、前記吸収液再生塔内に導入することを特徴とするＣＯ2回収方法。     And the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, to separate the CO 2 from the CO 2 absorbent having absorbed CO 2 CO 2 absorbing solution A CO 2 recovery method in which a lean solution from which CO 2 has been removed in the absorption liquid regeneration tower is reused in a CO 2 absorption tower.
    A part of the rich solution that has absorbed CO 2 in the CO 2 absorption tower is branched, the part of the branched rich solution is preheated, the part of the preheated rich solution is merged with the rich solution, and the merged The CO 2 recovery method, wherein the rich solution and the lean solution from which CO 2 has been released are heat-exchanged and then introduced into the absorption liquid regeneration tower.
  8. 　請求項７において、
    　前記予熱手段での予熱温度が、前記リーン溶液の温度以下の温度であることを特徴とするＣＯ2回収方法。     In claim 7,
    A CO 2 recovery method, wherein a preheating temperature in the preheating means is a temperature equal to or lower than a temperature of the lean solution.
  9. 　請求項７又は８において、
    　前記リッチ溶液の吸収液のＣＯ2吸収剤の濃度、前記吸収液再生塔に導入する直前のリッチ溶液の温度、及び前記吸収液再生塔内の圧力を計測し、
    　これらの計測結果より、前記吸収液再生塔に導入するリッチ溶液の適正温度を求め、該適正値となるように、予熱温度を制御することを特徴とするＣＯ2回収方法。     In claim 7 or 8,
    Measure the concentration of the CO 2 absorbent in the rich solution absorption liquid, the temperature of the rich solution immediately before being introduced into the absorption liquid regeneration tower, and the pressure in the absorption liquid regeneration tower,
    A CO 2 recovery method characterized in that, from these measurement results, an appropriate temperature of the rich solution introduced into the absorption liquid regeneration tower is obtained, and the preheating temperature is controlled so as to be the appropriate value.
  10. 　請求項９において、
    　前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも低い場合に、前記予熱手段での予熱温度を上昇させる制御を実行することを特徴とするＣＯ2回収方法。     In claim 9,
    A CO 2 recovery method, wherein control for increasing the preheating temperature in the preheating means is executed when the temperature of the rich solution introduced into the absorption liquid regeneration tower is lower than an appropriate temperature set value.
  11. 　請求項９において、
    　前記吸収液再生塔に導入するリッチ溶液の温度が、適正温度設定値よりも高い場合に、前記予熱手段での予熱温度を下降させる制御を実行することを特徴とするＣＯ2回収方法。     In claim 9,
    A CO 2 recovery method, wherein control is performed to lower the preheating temperature in the preheating means when the temperature of the rich solution introduced into the absorption liquid regeneration tower is higher than an appropriate temperature set value.
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