WO2005097299A1 - Ｃｏ2回収装置及び方法 - Google Patents

Ｃｏ2回収装置及び方法 Download PDF

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Publication number
WO2005097299A1
WO2005097299A1 PCT/JP2005/004473 JP2005004473W WO2005097299A1 WO 2005097299 A1 WO2005097299 A1 WO 2005097299A1 JP 2005004473 W JP2005004473 W JP 2005004473W WO 2005097299 A1 WO2005097299 A1 WO 2005097299A1
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WO
WIPO (PCT)
Prior art keywords
solution
semi
regeneration tower
lean solution
lean
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2005/004473
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English (en)
French (fr)
Japanese (ja)
Inventor
Masaki Iijima
Takashi Kamijo
Takahito Yonekawa
Tomio Mimura
Yasuyuki Yagi
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kansai Electric Power Co Inc
Mitsubishi Heavy Industries Ltd
Original Assignee
Kansai Electric Power Co Inc
Mitsubishi Heavy Industries Ltd
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Filing date
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First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=35080469&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2005097299(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority to CA2559744A priority Critical patent/CA2559744C/en
Priority to EP18175978.8A priority patent/EP3409344B1/en
Priority to US10/592,746 priority patent/US7918926B2/en
Priority to EP05720741.7A priority patent/EP1736231B2/en
Priority to DK05720741.7T priority patent/DK1736231T3/da
Priority to AU2005230300A priority patent/AU2005230300B2/en
Application filed by Kansai Electric Power Co Inc, Mitsubishi Heavy Industries Ltd filed Critical Kansai Electric Power Co Inc
Publication of WO2005097299A1 publication Critical patent/WO2005097299A1/ja
Anticipated expiration legal-status Critical
Priority to NO20064313A priority patent/NO344753B1/no
Priority to AU2008203827A priority patent/AU2008203827B2/en
Priority to US13/013,467 priority patent/US8535427B2/en
Priority to US13/013,419 priority patent/US8529678B2/en
Priority to US13/013,448 priority patent/US8409339B2/en
Priority to US13/962,754 priority patent/US8764884B2/en
Ceased legal-status Critical Current

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Classifications

    • 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
    • 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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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 an energy-saving CO recovery apparatus and method.
  • the sources of the second are all human activities that burn fossil fuels, and the demand for emission control tends to increase.
  • the boiler's combustion exhaust gas is brought into contact with amine-based CO absorbent to burn power generation equipment such as thermal power plants that use large amounts of fossil fuels.
  • the process involves contacting the flue gas with the CO absorbing solution in the absorption tower.
  • Patent Document 1 What is circulated and reused in an absorption tower is employed.
  • Patent Document 1 JP-A-7-51537
  • CO is absorbed from CO-containing gas such as combustion exhaust gas using the CO absorbing solution and the process.
  • the regenerating step consumes a large amount of heat energy, so that it is necessary to make the process as energy-saving as possible.
  • the present invention provides a CO recovery device with further improved energy efficiency.
  • a first invention of the present invention for solving the above-mentioned problem is that a gas containing CO and a CO
  • Regeneration tower and a CO recovery system that reuses the lean solution from which CO has been removed
  • the lean solution collected near the bottom of the regeneration tower is extracted to the outside, and the regeneration heater for exchanging heat with saturated steam and the rich solution supplied to the regeneration tower or withdrawn from the middle of the regeneration tower
  • the semi-lean solution from which CO was partially removed was passed through the regeneration heater.
  • a CO capture device characterized by comprising steam condensate heat exchange ⁇ ⁇ heated by residual heat of steam condensate.
  • the steam condensed water heat exchanger is interposed in a rich solution supply pipe for sending a rich solution having a capacity of the absorption tower.
  • a CO recovery device characterized by providing a flash drum on either the upstream side or downstream side of the exchanger.
  • a third invention is the second invention, wherein the rich solution is heated by providing a branch portion provided in a rich solution supply pipe for branching the rich solution and a first rich solution supply pipe branched therefrom.
  • a steam condensate heat exchanger, a flash drum provided on the downstream side of the steam condensate heat exchanger, and a branched second rich solution supply pipe are provided, and the flash drum partially removes CO.
  • Semi-lean solution heat that heats the rich solution with the residual heat of the semimilin solution
  • a CO capture device comprising:
  • a branch portion provided in the rich solution supply pipe for branching the rich solution and an end of the branched first rich solution supply pipe are provided.
  • the steam condensate heat exchange ⁇ is provided in the branched second rich solution supply pipe, and the residual heat of the semi-lean solution from which a part of CO has been removed by the steam condensate heat exchanger is used to recover.
  • a semi-lean solution heat exchanger for heating the tuchi solution is provided, and the end of the semi-lean solution supply pipe for supplying the semi-lean solution is connected to the middle part of the absorption tower. is there.
  • the steam condensed water heat exchange for flushing the rich solution comprises a flash drum provided with a flash portion for flushing the rich solution on an upper side, and the flash drum. And the lower part of the flash drum. And a steam supply unit for supplying steam from the steam condensed water.
  • the upper regeneration tower and the lower regeneration tower each formed by dividing the regeneration tower into upper and lower parts, and a branch part provided in a rich solution supply pipe for branching the rich solution,
  • a semi-condensed water heat exchanger interposed in the branched first rich solution supply pipe and a semi-condensed water in which the CO is partially removed by the upper regeneration tower are provided in the branched second rich solution supply pipe.
  • a semi-lean solution heat exchanger for heating the rich solution with the residual heat of the lean solution wherein the first rich solution supply pipe is connected to the lower regeneration tower, and the end of the second rich solution supply pipe is upper regeneration.
  • the CO recovery device is characterized in that it is connected to the tower and the end of the semi-lean solution supply pipe for supplying the semi-lean solution is connected to the middle part of the absorption tower.
  • the lean solution heat exchanger for heating the rich solution with the residual heat of the lean solution from the regeneration tower is provided with a rich solution supply.
  • An eighth invention is the invention according to the first invention, wherein the regeneration tower is divided into upper, middle, and lower parts, an upper regeneration tower, a middle regeneration tower, and a lower regeneration tower; and a rich solution supply pipe for branching the rich solution.
  • a lean solution heat exchanger interposed in a branched first rich solution supply pipe and a branched second rich solution supply pipe.
  • the CO recovery device is characterized by being connected to the middle part of the CO.
  • the semi-lean solution in which the regeneration tower is divided into at least two parts, and the upper stage of the divided regeneration tower is also extracted with CO partially removed is provided by the stainless steel.
  • a steam condensate heat exchanger that heats with the residual heat of the steam condensate, and supplies the heated semi-lean solution to the lower stage of the regeneration tower.
  • the regeneration tower is divided into at least two parts.
  • the CO2 recovery system is characterized in that a lean solution heat exchanger is installed in a rich solution supply pipe.
  • An eleventh invention is directed to the semi-lean solution according to the first invention, wherein the regeneration tower is divided into at least two parts, and the upper stage side power of the divided regeneration tower is also extracted.
  • a steam condensate heat exchanger for heating by the residual heat of the condensed water is provided.
  • the heated semi-lean solution is supplied to the lower stage of the regeneration tower, and the lean solution is heated by the residual heat of the lean solution from the regeneration tower.
  • a solution heat exchanger is interposed in the rich solution supply pipe, and a first branch provided in the rich solution supply pipe for branching the rich solution and a first branch branched in the first branch are provided.
  • the first lean solution heat exchanger interposed in the rich solution supply pipe, and the second rich solution supply pipe branched at the first branch section, CO2 was partially removed by the upper regeneration tower Semi-lean solution heat exchange to heat rich solution with residual heat of semi-milin solution
  • the first rich solution supply pipe and the second rich solution supply pipe are joined to exchange heat.
  • a steam condensed water heat exchanger interposed in a second branch provided on the downstream side of the semi-lean solution heat exchanger and a first semi-lean solution supply pipe branched in the second branch ⁇
  • the end of the first semi-lean solution supply pipe is connected to the lower side of the regeneration tower, and the end of the second semi-lean solution supply pipe branched at the second branch is absorbed.
  • the CO capture device is characterized by being connected to the middle part of the tower.
  • the regenerator in a twelfth aspect, is divided into at least two parts, and the separated regenerator also has an upper-stage force.
  • the CO recovery system is provided with a lean solution heat exchanger that heats with the residual heat of a strong lean solution, and supplies the heated semi-mine solution to the lower side of the regeneration tower.
  • a thirteenth invention is directed to the first invention, wherein the semi-lean solution partially removed from the upper stage side of the divided regeneration tower is heated with the residual heat of the lean solution having the regeneration tower power.
  • a lean solution heat exchanger and a steam condensate heat exchanger are installed side by side.
  • the CO recovery device is characterized in that a second lean solution heat exchanger for heating the rich solution by the residual heat of the lean solution after heating the solution is provided in the rich solution supply pipe.
  • the upper regeneration tower, the middle regeneration tower, the lower regeneration tower, and the CO extracted from the upper regeneration tower, each of which is formed by dividing the regeneration tower into upper, middle, and lower parts, are separated by one. Part removal
  • the first lean solution heat exchanger which heats the semi-lean solution with the lean solution from the regeneration tower, and the semi-lean solution from which the power of the central regeneration tower is also partially removed to remove the CO
  • the first steam condensed water heat exchanger that heats with condensed water and the semi-solid solution heat exchange that is provided in the rich solution supply pipe and heats the rich solution with a part of the semi-lean solution from which the power of the central regeneration tower is also extracted ⁇
  • a second heat source provided at the downstream side of the semi-lean solution heat exchange of the rich solution supply pipe to heat the rich solution with residual heat of the lean solution after heating the semi-lean solution.
  • the absorption tower is divided into upper and lower two stages, and the semi-lean is supplied to a middle part of the absorption tower.
  • the CO recovery system is characterized in that the solution is combined with the semi-lean liquid from which the upper absorption tower was also withdrawn and supplied to the lower absorption tower.
  • the sixteenth invention removes CO by bringing a CO-containing gas into contact with a CO absorbing solution.
  • An absorption tower a regeneration tower that regenerates the rich solution that absorbed CO, and CO was removed by the regeneration tower
  • a CO recovery unit that reuses the lean solution in the absorption tower, which is collected at the bottom of the regeneration tower.
  • a seventeenth invention removes CO by bringing a CO-containing gas into contact with a CO absorbing solution.
  • An absorption tower a regeneration tower that regenerates the rich solution that absorbed CO, and CO was removed by the regeneration tower
  • a CO recovery unit that reuses the lean solution in the absorption tower, which is collected at the bottom of the regeneration tower.
  • Regenerative heater for exchanging heat with saturated steam and semi-lean solution partially removed from CO extracted from the middle of the regenerator with residual heat of steam condensate
  • a CO recovery device characterized by comprising steam condensate heat exchange ⁇ .
  • the eighteenth invention removes CO by bringing a CO-containing gas into contact with a CO absorbing solution.
  • An absorption tower a regeneration tower that regenerates the rich solution that absorbed CO, and CO was removed by the regeneration tower
  • the semi-lean solution from which some of the emitted CO has been removed is heated by the residual heat of the lean solution.
  • a CO recovery apparatus characterized by comprising a solution heat exchange.
  • a CO-containing gas is brought into contact with a CO absorbing solution in an absorption tower to obtain CO2
  • the CO-absorbed rich solution is regenerated in a regeneration tower, and then the regenerated CO
  • the CO recovery method is characterized in that the solution recovered in the section is subjected to heat exchange with steam, and the rich solution is heated by the residual heat of the steam condensate.
  • the CO-absorbed rich solution is regenerated in a regeneration tower, and then the regenerated CO
  • the solution recovered in the part is heat-exchanged with steam, and the semi-lean solution removed from the middle of the regenerator is removed.
  • the second method is a CO recovery method characterized by heating with the residual heat of steam condensate.
  • a CO-containing gas and a CO absorbing solution are brought into contact in an absorption tower to reduce CO
  • the CO-absorbed rich solution is regenerated in a regeneration tower, and then the regenerated CO
  • FIG. 1 is a schematic diagram of a CO recovery device that is powerful in a first embodiment.
  • FIG. 2 is a schematic diagram of a CO recovery device that works in a second embodiment.
  • FIG. 3 is a schematic diagram of a CO recovery device that is powerful in a third embodiment.
  • FIG. 4 is a schematic diagram of a CO recovery device that is powerful in a fourth embodiment.
  • FIG. 5 is a schematic diagram of a CO recovery device empowered in a fifth embodiment.
  • FIG. 6 is a schematic diagram of a CO recovery device that is powerful in a sixth embodiment.
  • FIG. 7 is a schematic diagram of a CO recovery device according to a seventh embodiment.
  • FIG. 8 is a schematic diagram of a CO recovery device according to an eighth embodiment.
  • FIG. 9 is a schematic diagram of a CO recovery device according to a ninth embodiment.
  • FIG. 10 is a schematic diagram of a CO recovery device that works in the first embodiment.
  • FIG. 11 is a schematic diagram of a CO recovery device that works in a second embodiment.
  • FIG. 12 is a schematic diagram of a CO recovery device that is powerful in a third embodiment.
  • FIG. 13 is a schematic diagram of a CO recovery device working in a fourth embodiment.
  • FIG. 14 is a schematic diagram of a CO recovery device that is powerful in a fifth embodiment.
  • FIG. 15 is a schematic diagram of a CO recovery device that is powerful in a sixth embodiment.
  • FIG. 16 is a schematic diagram of a CO recovery device that works in a seventh embodiment.
  • FIG. 17 is a schematic diagram of a CO recovery device that is powerful in an eighth embodiment.
  • FIG. 18 is a schematic diagram of a CO recovery device that is powerful in a ninth embodiment.
  • FIG. 19 is a schematic diagram of a CO recovery device that is powerful in a tenth embodiment.
  • FIG. 20 is a schematic view of a CO recovery device for the eleventh embodiment.
  • FIG. 21 is a schematic diagram of a CO recovery device that is powerful in a twelfth embodiment.
  • FIG. 22 is a schematic diagram of a CO recovery device that is powerful in a conventional example.
  • FIG. 1 is a schematic diagram of a CO capture device according to the first embodiment.
  • the CO recovery device that is used in the first embodiment of the present invention
  • 14 is provided in a rich solution supply pipe 20 for supplying It comprises a steam condensate heat exchanger 21 for heating the rich solution 14 by the residual heat of the steam condensate 19.
  • a lean solution 16 as a regenerating solution is supplied from the regenerating tower 15 to the absorption tower 13 through a lean solution supply pipe 22.
  • the rich solution supply pipe 20 is provided with a lean solution heat exchanger 23 for heating the rich solution 14 by the residual heat of the lean solution 16.
  • reference numeral 8 denotes a nozzle
  • 9 denotes a chimney tray
  • 10 denotes a CO-removing exhaust gas
  • 25a and 25 denoted in FIG. 1, reference numeral 8 denotes a nozzle, 9 denotes a chimney tray, 10 denotes a CO-removing exhaust gas, and 25a and 25.
  • b denotes a packed bed provided in the absorption tower 13
  • 26a and 26b show packed beds provided in the regeneration tower 15, respectively.
  • the type of heat exchange used in the present embodiment is not particularly limited, and a known heat exchanger such as a plate heat exchanger, a shell & tube heat exchanger, or the like may be used.
  • the CO absorbing solution that can be used in the present invention is not particularly limited.
  • Hindered amines having an alcoholic hydroxyl group can be exemplified.
  • alkanolamines include monoethanolamine, diethanolamine, triethanolamine, methyljetanolamine, diisopropanolamine, diglycolamine, and the like.
  • Normally monoethanolamine (MEA) Is preferably used.
  • hinderdamines having an alcoholic hydroxyl group include 2-amino-2-methyl-1 propanol (AMP), 2- (ethylamino) ethanol (EAE), 2- (methylamino) ethanol (MAE), and 2- (ethylamino) ethanol (DEAE). And the like.
  • the regenerative heater 18 By effectively utilizing the residual heat of the used steam condensate 19, the supply temperature of the rich solution 14 supplied to the regeneration tower 15 can be increased, and as a result, the amount of steam supplied to the regeneration tower 15 can be reduced. Can be.
  • the CO-containing gas 11 supplied to the CO removal device is supplied by a cooling device (not shown).
  • the rich solution 14 from the absorption tower 13 of the CO removal device is heated at about 50 ° C
  • the steam in the regeneration tower 15 is heated by the lean solution heat exchange and is sent at about 110 ° C.
  • the heat of the steam condensate 19 (for example, at 137 ° C) is exchanged with the rich solution 14 by steam condensation.
  • the temperature of the rich solution 14 can be raised by several degrees.
  • a flash drum for flushing the rich solution is provided either before or after the steam condensate heat exchanger 21, and the flash drum is used to regenerate the CO contained in the rich solution. Can be dissipated outside. As a result, the regeneration tower 15
  • the supply amount of steam used for removing CO in the regeneration tower 15 can be reduced.
  • FIG. 2 is a schematic diagram of a CO recovery device according to the second embodiment.
  • the CO recovery apparatus As shown in FIG. 2, the CO recovery apparatus according to the second embodiment of the present invention
  • a branch part 24 provided in a rich solution supply pipe 20 for branching the rich solution 14 and a first rich solution supply pipe 20-1 branched in the branch part 24 are further provided.
  • a steam condensed water heat exchanger 21 for heating the rich solution 14 a flash drum 27 provided on the downstream side of the steam condensed water heat exchange, and a branched second rich solution supply pipe 20-2.
  • the second rich solution supply pipe 20-2 is connected near the upper stage of the regeneration tower 15, so that CO is removed and recovered in the regeneration tower 15.
  • a steam condensate heat exchanger 21 for heating the rich solution 14 by the residual heat of the steam condensed water 19 from the regenerative heater 18 is provided. Since the solution was heated, the steam condensate used in the regenerator 18 This effectively utilizes the residual heat. The rich solution 14 that has obtained residual heat is then introduced into the flash drum 27. By flushing the rich solution 14 in the flash drum 27, the efficiency of removing CO is improved. Also, the flash drum 27
  • the regeneration solution 28 does not need to be regenerated in regeneration tower 15 because most of the CO has been removed.
  • the CO removed by the flash drum 27 joins the CO from the regeneration tower 15 and
  • the division ratio of the rich solution 14 in the first rich solution supply pipe 20-1 and the second rich solution supply pipe 20-2 in the branch portion 24 is 30: 70-70: 30, preferably 50:70. : 50
  • the inside of the absorption tower 13 is further divided into two stages to form an upper packed bed 13-U and a lower packed bed 13-L, and the upper packed bed 13-U force absorbs CO to the outside.
  • the temperature is lowered to about 40-50 ° C.!
  • FIG. 3 is a schematic diagram of a CO recovery device according to the third embodiment.
  • the CO recovery apparatus As shown in FIG. 3, the CO recovery apparatus according to the third embodiment of the present invention
  • a branch portion 24 provided in a rich solution supply pipe 20 for further branching the rich solution 14 and an end portion of a branched first rich solution supply pipe 20-1 are provided to flush the rich solution 14.
  • a semi-lean solution heat exchange 29 for heating the rich solution 14 with the residual heat of the semi-lean solution 28 is provided.
  • the end of a semi-lean solution supply pipe 30 for supplying the semi-lean solution 28 is connected to the middle part of the absorption tower 13. It becomes.
  • the steam condensate heat exchange 31 does not use a heat exchanger such as the plate heat exchanger described above, as shown in FIG.
  • a first flash drum 33 provided with a part 32 on the upper side, a packed layer 34 provided in the flash drum 33, and a steam supply provided at the lower part of the flash drum and supplying steam 35 from steam condensate 19 And a section 36.
  • a second flash drum 37 is provided to make it into normal-pressure steam, and the steam 35 is supplied to the first flash drum 33. To remove CO from the rich solution 14.
  • the semi-lean solution 28 from which a part of CO has been removed in the first flash drum 33 is
  • the rich solution 14 is heated in the semi-lean heat exchanger 29 using the residual heat, and then supplied to the middle part of the absorption tower 13.
  • the steam condensed water heat that heats the rich solution 14 in the branched first rich solution supply pipe 20-1 by the residual heat of the steam condensed water 19 from the regeneration heater 18 Since the exchanger 31 is provided and the rich solution is heated by the steam 35, the residual heat of the steam condensed water 19 used in the regenerative heater 18 is effectively used.
  • the heat is exchanged in the semi-lean solution heat exchanger 29 interposed in the branched second rich solution supply pipe 20-2 by using the heat exchanger, so that the temperature of the rich solution 14 introduced into the regeneration tower 15 can be increased. As a result, the supply amount of steam used in the regeneration tower 15 can be reduced. Also, the CO removed by the first flash drum 33 joins with the CO from the regeneration tower 15
  • the first flash drum 33 functions as a sub-regeneration tower for the regeneration tower 14.
  • FIG. 4 is a schematic diagram of a CO capture device according to a fourth embodiment. It should be noted that the same members as those of the first to third embodiments have the same structure as the CO recovery device.
  • the CO recovery apparatus As shown in FIG. 4, the CO recovery apparatus according to the fourth embodiment of the present invention
  • the upper regeneration tower 15-U and the lower regeneration tower 15-L each of which is formed by dividing the inside of the regeneration tower 15 into upper and lower parts, and a rich solution supply pipe 20 for branching the rich solution 14 are provided. And a steam condensate heat exchanger 21 interposed in the branched first rich solution supply pipe 20-1 and a branched second rich solution supply pipe 20-2.
  • the semi-lean solution 28 from which part of the CO was removed was enriched with residual heat 14
  • a semi-lean solution heat exchanger 29 for heating the first rich solution supply pipe 201 The end of the first rich solution supply pipe 201 is connected to the lower regeneration tower 15-L, and the second rich solution supply pipe 20-2 The end is connected to the upper regeneration tower 15-U, and the end of the semi-lean solution supply pipe 30 for supplying the semi-lean solution 28 is connected to the middle part of the absorption tower 13.
  • a steam condensate heat exchanger 21 for heating the rich solution 14 by the residual heat of the steam condensed water 19 from the regenerative heater 18 is provided. Since the solution has been heated, the residual heat of the steam condensed water 19 used in the regenerative heater 18 is effectively used. Further, the rich solution 14 having obtained the residual heat is introduced into the lower regeneration tower 15L, where it is regenerated.
  • the liquid 28 is taken out to the outside by the semi-lean supply pipe 30, and the residual heat causes heat exchange in the semi-lean solution heat exchange 29 interposed in the branched second rich solution supply pipe 20-2.
  • the temperature of the rich solution 14 to be introduced can be increased, and as a result, the supply amount of steam used in the regeneration tower 15 can be reduced.
  • the first rich solution supply pipe 20-1 and the second rich solution supply pipe 20 in the branch section 24 are connected to the first rich solution supply pipe 20-1 and the second rich solution supply pipe 20 in the branch section 24
  • the split ratio of the rich solution 14 of 2 should be 25: 75—75: 25! ⁇ .
  • FIG. 5 is a schematic diagram of a CO recovery device according to a fifth embodiment.
  • a CO recovery apparatus As shown in FIG. 5, a CO recovery apparatus according to a fifth embodiment of the present invention is
  • An upper regeneration tower 15-U, a middle regeneration tower 15-M, and a lower regeneration tower 15-L, in which the regeneration tower 15 is divided into upper, middle, and lower sections, and a rich solution supply pipe 20 for branching the rich solution 14 are provided.
  • the steam condensed water heat exchanger 21 for heating the semi-lean solution 28 extracted by the extraction pipe 41 is provided, and the semi-lean solution 28 is heated by the residual heat of the steam condensed water 19.
  • the residual heat of the steam condensed water 19 used in the regenerative heater 18 is effectively used, and as a result, the supply amount of steam used in the regenerator 15 can be reduced.
  • the rich solution 14 is regenerated by the lean solution 16 regenerated in the regenerator 15, and the rich solution 14 is heat-exchanged by the lean solution heat exchange 23 interposed in the branched first rich solution supply pipe 20-1. Since the obtained rich solution 14 is introduced into the central regeneration tower 15 ⁇ , the supply amount of steam used in the regeneration tower can be reduced.
  • the liquid 28 is taken out to the outside by the semi-lean supply pipe 30, and heat is exchanged by the semi-lean solution heat exchange 29 interposed in the branched second rich solution supply pipe 20-2 by the residual heat.
  • the temperature of the rich solution 14 introduced into U can be increased, and as a result, the amount of steam supplied to the regeneration tower 15 can be reduced.
  • the first rich solution supply pipe 20-1 and the second rich solution supply pipe 20 in the branch portion 24 The split ratio of the rich solution 14 of -2 should be 25: 75-75: 25! ⁇ .
  • FIG. 6 is a schematic diagram of a CO recovery device according to a sixth embodiment.
  • the CO recovery apparatus As shown in FIG. 6, the CO recovery apparatus according to the sixth embodiment of the present invention
  • the regeneration tower is divided into at least two parts, the upper regeneration tower 15-U and the lower regeneration tower 15-L, and the divided upper regeneration tower 15—U power is also removed from the semi-reely that partially removes the CO extracted through the extraction pipe 41.
  • a steam condensed water heat exchange 21 for heating the semi-lean solution 28 extracted by the extraction pipe 41 by the residual heat of the steam condensed water 19 from the regeneration heater 18 is provided. Since the semi-lean solution 28 was heated by the residual heat of the condensed water, the residual heat of the steam condensed water 19 used in the regeneration heater 18 was effectively used, and as a result, the amount of steam supplied to the regeneration tower 15 was reduced. can do.
  • FIG. 7 is a schematic diagram of a CO recovery device according to a seventh embodiment.
  • a first branch portion 24-1 provided in a rich solution supply tube 20 for branching a rich solution 14, and a first rich solution supply tube branched at a first branch portion 24-1
  • the end is connected to the lower regeneration tower 15-L, and the end of the second semi-lean solution supply pipe 30-2 branched at the second branch 24-2 is connected to the middle part of the absorption tower 13. It is made to become.
  • the residual heat of the semi-lean solution 28 from which the upper regeneration tower 14 U power has also been extracted is used in the semi-lean solution heat exchange ⁇ 29 to effectively use the residual heat of the semi-lean solution 28 by heating the rich solution 14. ing.
  • the steam condensate heat exchanger 21 is provided.
  • the semi-lean solution 28 can be heated by the residual heat of the steam condensate 19, and the residual heat of the steam condensate 19 used in the regeneration heater 18 is effectively used. As a result, the steam used in the regeneration tower 15 is used. The amount of supply can be reduced.
  • the rich solution 14 is once branched and heat-exchanged by the semi-lean solution heat exchange 29, and the other branched rich solution is also heat-exchanged by the first lean solution heat exchanger 23-1.
  • these rich solutions were merged at the merging section 42 and further heat-exchanged in the second lean solution heat exchange 23-2, they were supplied to the upper regeneration tower 15-U.
  • the temperature of the rich solution 14 introduced into the tower rises, and as a result, the amount of steam supply used in the regeneration tower 15 can be reduced.
  • FIG. 8 is a schematic diagram of a CO recovery device according to an eighth embodiment.
  • a CO recovery device As shown in FIG. 8, a CO recovery device according to an eighth embodiment of the present invention
  • the regeneration tower is divided into at least two parts, the upper regeneration tower 15-U and the lower regeneration tower 15-L, and the split upper regeneration tower 15-U also has a semi-lean solution 28 from which CO has been partially removed.
  • the semi-lean solution 28 flows through the lean solution supply pipe 22 into the lean solution.
  • the first lean solution heat exchanger 23-1 which is heated by the residual heat of the liquid 16, and the first lean solution heat exchange of the extraction pipe 41, which is provided on the downstream side of the
  • a second condensate heat exchanger 21 for heating the rich solution 14 with the residual heat of the lean solution after heating the semi-lean solution 28 is provided together with a steam condensate heat exchanger 21 for heating again with the steam condensate 19.
  • Ver. 23-2 is provided in the rich solution supply pipe 20.
  • the semi-lean solution 28 from which the upper regeneration tower 15-U power is also extracted is heated by the first lean solution heat exchange 1 and further heated by the steam condensed water heat exchange 21 to perform regeneration.
  • the residual heat of the steam condensed water 19 used in the heater 18 is effectively used, and as a result, the supply amount of steam used in the regeneration tower 15 can be reduced.
  • the inside of the regenerator is divided into a plurality of stages, and the divided semi-lean solutions 28 from which the respective regenerative tower powers are also extracted are returned to the lower regenerator, the lean solution heat exchanger and the steam condensate water heat are returned.
  • the temperature of the semimilin solution 28 to be regenerated in the regenerator 15 can be increased, and as a result, the steam supply amount used in the regenerator 15 can be reduced.
  • FIG. 9 is a schematic diagram of a CO recovery device according to the ninth embodiment.
  • a CO recovery device As shown in FIG. 9, a CO recovery device according to a ninth embodiment according to the present invention
  • the upper regeneration tower 15-U, the middle regeneration tower 15-M, and the lower regeneration tower 15L, which are divided into upper, middle, and lower sections of the regeneration tower 15, and the upper regeneration tower 15-U also have the first extraction pipe 41 1
  • the semi-lean solution 28 from which CO was partially removed is heated with the lean solution from the regeneration tower.
  • the lean solution heat exchanger 23-1 and the central regeneration tower 15- The semi-lean solution 28 from which a part of the CO is removed through the second extraction pipe 412 is also heated with steam condensed water.
  • a semi-lean solution heat exchanger provided in the steam condensate heat exchanger 21 and the rich solution supply pipe 20 and heating the rich solution 14 with a part of the semi-lean solution 28 extracted from the central regeneration tower 15-M. 29 and the semi-lean solution heat exchanger 29 of the rich solution supply pipe 20 And a second lean solution heat exchanger 23-2 for heating the rich solution 14 with the residual heat of the lean solution 16 after heating the semi-lean solution 28, and regenerating the heated semi-lean solutions respectively.
  • the semi-lean solution 28 after the heat exchange in the semi-lean solution heat exchange 29 is supplied to the middle part of the absorption tower 13 via the semi-lean solution supply pipe 30 while being supplied to the lower side of the column.
  • the semi-lean solution 28 extracted from the upper regeneration tower 15-U and the middle regeneration tower 15-M, respectively, is converted into the first lean solution heat exchange 23-1 or the steam condensed water heat exchanger 21.
  • the residual heat of the lean solution 16 and the steam condensed water 19 is effectively used, and as a result, the supply amount of steam used in the regeneration tower 15 can be reduced.
  • the residual heat of the semi-lean solution 28 after heat exchange in the steam condensate heat exchange 21 is used for heating the rich solution, and the residual heat of the lean solution heat-exchanged in the first lean
  • the lean solution heat exchange ⁇ 23-2 to heat the rich solution, the temperature of the rich solution 14 supplied to the regeneration tower 15 can be increased, and as a result, the steam supply amount used in the regeneration tower 15 can be reduced. Can be reduced.
  • FIG. 10 is a conceptual diagram illustrating the CO capture device according to the first embodiment.
  • the counterpart is brought into countercurrent contact with the absorption liquid 12 of a predetermined concentration supplied from the charging section, and CO in the flue gas is absorbed and removed by the CO absorption liquid 12, and the remaining CO removal and exhaust gas from which CO is absorbed and removed is removed.
  • the absorption liquid 12 supplied to the CO absorption tower 13 absorbs CO and
  • the temperature usually becomes higher than the temperature
  • the liquid 2 is sent to the lean solution heat exchanger 23 and the steam condensate heat exchanger 21 as the rich solution 14 by the absorbing solution discharge pump 51 that has absorbed 2 and is heated and guided to the regeneration tower 15.
  • the absorbent is regenerated by heating by the regeneration heater 18 by the steam 17,
  • the lean solution 16 is cooled by the lean solution heat exchange 23 and the cooler 52 provided as necessary and returned to the CO absorption tower 13.
  • the regenerator 15 At the top of the regenerator 15
  • the separated CO is cooled by the regenerator reflux condenser 53, and the CO
  • the water vapor entrained in 222 is separated from the condensed reflux water, and is taken out of the system through the recovered CO discharge line 55.
  • the reflux water 56 is returned to the regeneration tower 15 by a reflux water pump 57.
  • the steam used in the regenerative heater 18 is led to the CO separator 54 and flashed.
  • FIG. 22 shows a case where the steam condensate heat exchanger 21 was not provided.
  • the temperature (° C) is surrounded by a square
  • the flow rate (tZh) is surrounded by a parallelogram
  • the calorific value (MMkcl / h) is indicated by a squeeze. The same applies to FIGS. 11 to 21 below.
  • the steam consumption of the comparative example in FIG. 22 was 98.77 MMkclZh. If the comparative example is set to 100, it is 99.2%, so the reduction rate of steam intensity (improvement effect) was 0.8%.
  • FIG. 11 is a conceptual diagram illustrating a CO recovery device according to the second embodiment. Note that the same as in Example 1
  • a flash drum 61 is provided on the downstream side of the steam condensed water heat exchanger 21 for heating the rich solution 14. Since the rich solution 14 is heated by the steam condensed water heat exchange 21 on the upstream side of the flash drum 61, the CO in the rich solution 14 can be removed by the flash drum 61.
  • the temperature of the rich solution from the flash drum 61 was 103.9. Part of CO that is C Since the water is removed, lowering the inlet temperature of the regeneration tower 15 is preferable because it reduces the amount of water vapor taken out from the top of the tower.
  • Example 2 as a result, the steam consumption in the regeneration tower 15 was 97.64 MMkcl Zh. Assuming that the comparative example is 100, it is 98.1%, so the steam intensity reduction rate (improvement effect) was 1.1%.
  • FIG. 12 is a conceptual diagram illustrating a CO capture device according to the third embodiment. Note that the same as in Example 1
  • a flash drum 61 is provided on the upstream side of the steam condensate heat exchanger 21 for heating the rich solution 14.
  • the rich solution 14 is heated by the steam condensed water heat exchanger 21, so that the temperature of the rich solution 14 supplied to the regeneration tower 15 is increased.
  • Example 3 as a result, the steam consumption in the regeneration tower 15 was 97.27 MMkcl Zh. Assuming that the comparative example is 100, it is 98.5%, so the reduction rate of steam intensity (improvement effect) was 1.5%.
  • FIG. 13 is a conceptual diagram illustrating a CO capture device according to the fourth embodiment. Note that the same as in Example 1
  • Example 4 the rich solution 14 was branched and a part thereof was sent to a flash drum type heat exchanger 31 where heat was exchanged with steam from steam condensed water to remove CO in the rich solution 14. .
  • the other rich solution 14 branched in the exchanger 29 was subjected to heat exchange so that the temperature of the rich solution 14 supplied to the regeneration tower 15 was raised.
  • Example 4 As a result, the steam consumption in the regeneration tower 15 was 97.56 MMkcl Zh. Assuming that the comparative example is 100, it is 98.8%, so the steam intensity reduction rate (improvement effect) was 1.2%.
  • Example 5 As a result, the steam consumption in the regeneration tower 15 was 97.56 MMkcl Zh. Assuming that the comparative example is 100, it is 98.8%, so the steam intensity reduction rate (improvement effect) was 1.2%.
  • Example 5 Example 5
  • FIG. 14 is a conceptual diagram illustrating a CO capture device according to the fifth embodiment. Note that the same as in Example 1
  • the rich solution 14 is branched, and a part of the branched solution is sent to a flash drum type heat exchanger 31. 31, improved CO removal efficiency in rich solution 14
  • Example 5 as a result, the steam consumption in the regeneration tower 15 was 95.52 MMkcl Zh. If the comparative example is set to 100, it is 96.7%, so the reduction rate of steam intensity (improvement effect) was 3.3%.
  • FIG. 15 is a conceptual diagram illustrating a CO recovery device according to the sixth embodiment. Note that the same as in Example 1
  • Example 6 the regeneration tower 15 was divided into two parts, and the semi-lean solution 28 from which the upper regeneration tower 15-U power was also extracted was heat-exchanged with the residual heat of the steam condensate 19 by the steam condensate heat exchanger 21. Returned to 15-L. As a result, the temperature of the semi-clean solution supplied to the lower portion of the regeneration tower 15 was increased.
  • Example 6 as a result, the steam consumption in the regeneration tower 15 was 93.65 MMkcl Zh. Assuming that the comparative example is 100, it is 94.8%, so the reduction rate of steam intensity (improvement effect) was 5.2%.
  • FIG. 16 is a conceptual diagram illustrating a CO capture device according to the seventh embodiment. Note that the same as in Example 1
  • Example 7 the regeneration tower is divided into two stages.
  • the rich solution 14 is branched, a lean solution heat exchange 23 is provided in the branched first rich solution supply pipe 20-1, and then a steam condensate heat exchanger 21 is provided on the downstream side, and the lower regeneration tower is provided.
  • the temperature of the rich solution 14 supplied to 15-L is increased.
  • the upper regeneration tower 15-U is supplied to the upper regeneration tower 15-U by installing a semi-lean solution heat exchanger 29 by the residual heat of the semi-lean solution 28 as much as possible in the branched second rich solution supply pipe 20-2.
  • the temperature of the rich solution was increased.
  • the branching ratio was 70% for the first rich solution and 30% for the second rich solution.
  • Example 7 as a result, the steam consumption in the regeneration tower 15 was 93.58 MMkcl Zh. Assuming that the comparative example is 100, it is 94.8%, so the reduction rate of steam intensity (improvement effect) was 5.2%.
  • FIG. 17 is a conceptual diagram illustrating a CO recovery device according to the eighth embodiment. Note that the same as in Example 1
  • Example 8 the semi-lean solution 28 from which the regeneration tower 15 was divided into two parts and the upper regeneration tower 15-U power was also extracted was first heat-exchanged in the first lean solution heat exchange 23-1, and then steam condensed. The heat was exchanged with the residual heat of the steam condensate 19 by the water heat exchanger 21 and returned to the lower regeneration tower 15-L. As a result, the temperature of the semi-lean solution supplied to the lower portion of the regeneration tower 15 was increased.
  • Example 8 as a result, the steam consumption in the regeneration tower 15 was 91. IMMkcl / h. If the comparative example is set to 100, it will be 92.3%, so the reduction rate of steam intensity (improvement effect) was 7.7%.
  • FIG. 18 is a conceptual diagram illustrating a CO recovery device according to the ninth embodiment. Note that the same as in Example 1
  • Example 9 the regeneration tower 15 was divided into four sections, and the first regeneration tower 15-1, the second regeneration tower 15-2, the third regeneration tower 15-3, and the fourth regeneration tower 15-4. Then, the first regeneration tower 15-1 and the third regeneration tower 15
  • the semi-lean solution 28 extracted from —3 was heat-exchanged in the first steam condensate heat exchanger 21-1 and the second steam condensate heat exchanger 21-2 by the residual heat of the steam condensate, respectively. Since the temperature on the lower side of the regeneration tower was high, the residual heat of the steam condensate 19 was used efficiently.
  • the semi-lean solution extracted from the second regeneration tower 15-2 was subjected to heat exchange by the first lean solution heat exchange 1 by the residual heat of the lean solution 16.
  • the semi-lean solution 28 extracted from the first regeneration tower 15-1 is recovered by the residual heat of the lean solution 16 heat-exchanged in the first lean solution heat exchange-1. Heat was exchanged in the second lean solution heat exchanger 23-2 for heat exchange.
  • the rich solution 14 from the absorption tower was heat-exchanged in the third lean solution heat exchanger 23-3.
  • Example 9 as a result, the steam consumption in the regeneration tower 15 was 85.49 MMkcl Zh. If the comparative example is set to 100, it is 86.6%, so the reduction rate of steam intensity (improvement effect) was 13.4%.
  • FIG. 19 is a conceptual diagram illustrating a CO capture device according to the tenth embodiment. The same as in Example 1
  • Example 10 the regeneration tower 15 was divided into three parts, an upper regeneration tower 15-U, a middle regeneration tower 15-M, and a lower regeneration tower 15-L. Then, the semi-lean solution 28 from which the central regeneration tower 15-M power was also extracted was subjected to heat exchange by steam condensate heat exchange using residual heat of the steam condensate. A part of the extracted semi-lean solution 28 was supplied to a semi-lean solution heat exchanger 29 for heating the rich solution 14, and efficiently used the residual heat of the semi-lean solution.
  • the semi-lean solution from which the upper regeneration tower 15-U power was also extracted was subjected to heat exchange in the first lean solution heat exchange 23-1 by the residual heat of the lean solution 16.
  • the rich solution 14 heat-exchanged in the semi-lean solution heat exchange 29 is converted into the second lean solution heat exchange 23-2 in which heat exchange is performed with the residual heat of the lean solution 16 heat-exchanged in the first lean solution heat exchange 1 Heat exchanged.
  • Example 10 as a result, the steam consumption in the regeneration tower 15 was 91.9 MMkcl. Zh. If the comparative example is set to 100, it will be 93.0%, so the reduction rate of steam intensity (improvement effect) is 7%.
  • FIG. 20 is a conceptual diagram illustrating a CO capture device according to the eleventh embodiment. The same as in Example 1
  • Example 11 the regeneration tower 15 was divided into two parts, the upper regeneration tower 15-U and the lower regeneration tower 15-. Then, the semi-lean solution 28 from which the upper regeneration tower 15-U power is also extracted is heated at the same time as the rich solution in the second rich solution supply pipe 20-2 branched by the semi-lean solution heat exchange 29, and then branched off to the lower part. Before supplying to the regeneration tower 15-L, heat was exchanged by the steam condensate heat exchange 21 by the residual heat of the steam condensate.
  • the rich solution in the first rich solution supply pipe 20-1 is supplied to the first lean solution heat exchanger 23—
  • Heat exchange was carried out at 1 and then the rich solutions were combined, heat-exchanged at the second lean solution heat exchange 23-2 by the residual heat of the lean solution 16, and supplied to the regeneration tower 15.
  • Example 11 as a result, the steam consumption in the regeneration tower 15 was 93.96 MMkclZh. Assuming that the comparative example is 100, it is 95.1%, so the reduction rate of steam intensity (improvement effect) was 4.9%.
  • FIG. 21 is a conceptual diagram illustrating a CO capture device according to Embodiment 12. The same as in Example 1
  • Example 12 the regeneration tower 15 was divided into three parts, an upper regeneration tower 15-U, a middle regeneration tower 15-M, and a lower regeneration tower 15-L. Then, the semi-lean solution 28 from which the central regeneration tower 15-M power was also extracted was subjected to heat exchange by steam condensate heat exchange using residual heat of the steam condensate. Further, the rich solution 14 was divided, and a lean solution heat exchanger 23 was provided in the first rich solution supply pipe 20-1. In the second rich solution supply pipe 20-2, heat is exchanged using a lean solution heat exchange 29 using a semi-lean solution 28 extracted from the upper regeneration tower 15-U, and the residual heat of the semi-lean solution is Was used efficiently. In Example 12, as a result, the steam consumption in the regeneration tower 15 was 91.14 MMkclZh. If the comparative example is set to 100, it is 92.3%, so the reduction rate of steam intensity (improvement effect) was 7.7%.
  • the CO recovery system according to the present invention is capable of

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CA2559744A CA2559744C (en) 2004-03-15 2005-03-14 Co2 recovery system and method
EP18175978.8A EP3409344B1 (en) 2004-03-15 2005-03-14 Co2 recovery system and method
US10/592,746 US7918926B2 (en) 2004-03-15 2005-03-14 CO2 recovery system and method
EP05720741.7A EP1736231B2 (en) 2004-03-15 2005-03-14 Apparatus and method for recovering co2
DK05720741.7T DK1736231T3 (da) 2004-03-15 2005-03-14 Apparat og fremgangsmåde til genvinding af co2
AU2005230300A AU2005230300B2 (en) 2004-03-15 2005-03-14 Apparatus and method for recovering CO2
NO20064313A NO344753B1 (no) 2004-03-15 2006-09-22 System og fremgangsmåte til gjenvinning av CO2
AU2008203827A AU2008203827B2 (en) 2004-03-15 2008-08-11 Apparatus and method for recovering CO2
US13/013,448 US8409339B2 (en) 2004-03-15 2011-01-25 CO2 recovery system and method
US13/013,419 US8529678B2 (en) 2004-03-15 2011-01-25 CO2 recovery system and method
US13/013,467 US8535427B2 (en) 2004-03-15 2011-01-25 CO2 recovery system and method
US13/962,754 US8764884B2 (en) 2004-03-15 2013-08-08 CO2 recovery system and method

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US13/013,419 Division US8529678B2 (en) 2004-03-15 2011-01-25 CO2 recovery system and method
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