US20130234438A1 - Apparatus and method for recovering energy after carbon dioxide capture - Google Patents

Apparatus and method for recovering energy after carbon dioxide capture Download PDF

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Publication number
US20130234438A1
US20130234438A1 US13/531,862 US201213531862A US2013234438A1 US 20130234438 A1 US20130234438 A1 US 20130234438A1 US 201213531862 A US201213531862 A US 201213531862A US 2013234438 A1 US2013234438 A1 US 2013234438A1
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United States
Prior art keywords
carbon dioxide
energy
pressure
turbine
atm
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Abandoned
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US13/531,862
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English (en)
Inventor
Sang Jin Park
Ki Chun Lee
Sung Yeup Chung
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Hyundai Motor Co
Kia Corp
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Hyundai Motor Co
Kia Motors Corp
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Assigned to KIA MOTORS CORPORATION, HYUNDAI MOTOR COMPANY reassignment KIA MOTORS CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CHUNG, SUNG YEUP, LEE, KI CHUN, PARK, SANG JIN
Publication of US20130234438A1 publication Critical patent/US20130234438A1/en
Abandoned legal-status Critical Current

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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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • 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
    • 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
    • B01D53/343—Heat recovery
    • 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
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/02—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being an unheated pressurised gas
    • 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
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • 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 apparatus and method for recovering energy after carbon dioxide capture. More particularly, it relates to an apparatus and method for recovering energy after carbon dioxide capture, which can recover energy from a discharge pressure of captured carbon dioxide when the captured carbon dioxide is treated by a method such as fixation or conversion.
  • methods for capturing carbon dioxide include an absorption method, an adsorption method, and a separation membrane method.
  • Absorption methods can treat a large amount of exhaust gas compared to adsorption methods and separation membrane methods, and provides a high removal efficiency even in cases when the CO 2 concentration condition is about 7% to about 30%. Further, adsorption methods have a high economical efficiency and are easy to apply.
  • the carbon dioxide once captured, can then be stored, or can be treated by fixation and conversion methods.
  • the method of storing CO 2 in the ground or deep sea is easy even with a large amount of CO 2 , in contrast to the other treatment methods.
  • Such storage methods are currently available are have been commercialized.
  • the cost for storing CO 2 in the ground or deep sea is high, and the stored CO 2 cannot be fundamentally removed, making additional profit-making difficult.
  • a chemical absorption method is currently being most widely developed.
  • CO 2 is selectively separated from exhaust gas by a chemical reaction.
  • the amount of absorption is not significantly affected by the CO 2 partial pressure. Accordingly, there is an advantage in that the CO 2 removal efficiency is high even when the CO 2 partial pressure is low.
  • the chemical absorption method is limited because high energy consumption is required in a subsequent recovery process in which CO 2 is separated from an absorbent.
  • the energy cost for recovery accounts for about 60% or more of the total CO 2 recovery cost of a CO 2 capturing apparatus.
  • the energy cost for separating CO 2 from absorbent in a recovery tower accounts for about 80% of the energy cost for CO 2 recovery
  • the energy cost for maintaining process equipment such as a pump accounts for about 20% of the energy cost for CO 2 recovery.
  • an improved absorption technology is needed for capturing carbon dioxide wherein energy consumed in absorbent recovery is reduced, thereby reducing the cost for collecting carbon dioxide.
  • an exhaust gas containing CO 2 is supplied to an absorption tower 10 that has a wide surface area for smooth gas-liquid contact and which is filled with filling substances.
  • a liquid absorbent is supplied from an absorbent storage tank 12 to an upper part of the absorption tower 10 , and an exhaust gas is supplied to a lower part of the absorption tower 10 .
  • the exhaust gas contacts the liquid absorbent (absorption solution) at an atmospheric pressure in the upper end of the absorption tower 10 , allowing CO 2 in the exhaust gas to be absorbed into the absorption solution, generally within a temperature range of 40° C. to 70° C.
  • the absorbent that absorbs CO 2 is discharged from the absorption tower 10 and is supplied to a recovery tower 14 where it undergoes a recovery process in which the absorbent is heated to a temperature of 100° C. to 160° C. Thereafter, the absorbent is discharged from the lower part of the recovery tower 14 (“used CO 2 absorbent”) and it is resupplied to the absorption tower 10 through an absorbent supplying line 22 .
  • Absorbent that is resupplied to the absorption tower 10 is heated by passing through a heat exchanger 16 .
  • absorbent newly supplied to the recovery tower 14 from the absorbent storage tank 12 can be preheated by heat exchange with the heated absorbent that is resupplied from the lower part of the recovery tower 14 .
  • This combined heated absorbent is then supplied to the upper part of the recovery tower 14 .
  • CO 2 separated in the recovery tower 14 is discharged through a condenser to locations for storage, fixation, and conversion, and the evaporated absorbent is condensed in the condenser 20 then fed back to the recovery tower 14 .
  • the CO 2 separated in the recovery tower 14 is a high concentration of gaseous CO 2 (90% to 100%), and is discharged from the recovery tower 14 at a pressure range of 1.9 atm to 6 atm to be finally treated by a storage, fixation, or conversion method.
  • the pressure of a high concentration of CO 2 discharged from the upper end of the recovery tower 14 must be increased to a high pressure of about 70 atm to about 100 atm. For this pressure increase, additional energy is required.
  • the captured CO 2 when captured CO 2 is directly treated by fixation or conversion instead of storage, the captured CO 2 can be treated by a pressure of just 1.2 atm or less and, thus, a process of increasing the pressure of CO 2 with a compressor is unnecessary.
  • the present invention provides an apparatus and method for recovering energy after carbon dioxide capture, which reduces a discharge pressure of captured CO 2 to a pressure necessary for fixation or conversion.
  • the apparatus and method further simultaneously generates energy (e.g. in a generator connected to a turbine), wherein the energy is generated by fixation or conversion of the captured CO 2 instead of storing the captured CO 2 in the ground or deep sea.
  • This generated energy can be supplied to process operating units of the present apparatus and, thus, can be used by any of the operating units to capture CO 2 .
  • the present invention provides an apparatus for recovering energy after carbon dioxide capture, including an energy recovery unit at a carbon dioxide discharge part of a carbon dioxide capturing apparatus, wherein the energy recovery unit reduces a discharge pressure of the carbon dioxide to a pressure level suitable for a fixation or conversion treatment.
  • energy generated during the pressure reduction can be simultaneously recovered by the energy recovery unit.
  • the energy recovery unit may be in connection with one or more process operating units of the carbon dioxide capturing apparatus to supply the recovered electrical energy to the desired process operating units.
  • the energy recovery unit may include: a turbine disposed at an outlet of a condenser, wherein the outlet is a discharge part of the carbon dioxide capturing apparatus; and a generator connected to the turbine.
  • the present invention provides a method for recovering energy after carbon dioxide capture, including: capturing, by a carbon dioxide capturing apparatus, carbon dioxide from an exhaust gas; discharging, by the carbon dioxide capturing apparatus, the captured carbon dioxide; reducing a discharge pressure of the discharged carbon dioxide to a pressure level suitable for a fixation or conversion treatment; and recovering energy generated during the pressure reduction.
  • the method may further include supplying the recovered energy to one or more desired process operating units of the carbon dioxide capturing apparatus to utilize the recovered energy.
  • the energy recovery may include: rotating a turbine using the discharge pressure of the carbon dioxide captured by the carbon dioxide capturing apparatus; continually reducing a final discharge pressure of the carbon dioxide that has passed the turbine to the pressure level suitable for the fixation or conversion treatment; and delivering a rotary force of the turbine to a generator connected to the turbine to enable generation of energy by the generator.
  • the final discharge pressure of the carbon dioxide that has passed the turbine may be reduced to a pressure of less than about 1.8 atm, less than about 1.6 atm, less than about 1.4 atm, or a pressure of about 1.2 atm which is suitable for the fixation or conversion treatment.
  • FIG. 1 is a diagram illustrating an apparatus for recovering energy after carbon dioxide capture according to an embodiment of the present invention.
  • FIG. 2 is a diagram illustrating a typical carbon dioxide capturing apparatus.
  • vehicle or “vehicular” or other similar term as used herein is inclusive of motor vehicles in general such as passenger automobiles including sports utility vehicles (SUV), buses, trucks, various commercial vehicles, watercraft including a variety of boats and ships, aircraft, and the like, and includes hybrid vehicles, electric vehicles, plug-in hybrid electric vehicles, hydrogen-powered vehicles and other alternative fuel vehicles (e.g., fuels derived from resources other than petroleum).
  • a hybrid vehicle is a vehicle that has two or more sources of power, for example both gasoline-powered and electric-powered vehicles.
  • the present invention provides an apparatus and method that improves the economical efficiency of CO 2 capture by reducing the CO 2 absorption cost, particularly by reducing energy costs.
  • a CO 2 capturing apparatus is designed to discharge captured CO 2 for conversion or fixation after reducing the discharge pressure of the CO 2 to a pressure level suitable for fixation or conversion treatment, wherein energy is recovered during the pressure reduction, and the recovered energy is supplied to one or more of process units of the CO 2 capturing apparatus.
  • an energy recovery unit 30 may be disposed around a location where CO 2 captured by the CO 2 capturing apparatus is discharged.
  • the energy recovery unit 30 may be disposed at the side of an outlet of a condenser 20 connected to a recovery tower 14 of the CO2 capturing apparatus.
  • the energy recovery unit 30 may be configured and arranged to reduce the discharge pressure of CO 2 to a pressure level suitable for fixation or conversion treatment, and to recover energy generated during the pressure reduction.
  • the energy recovery unit 30 may include a turbine 32 disposed at an outlet of the condenser 20 that is a discharge part of the CO 2 capturing apparatus.
  • a generator 34 can be provided in connection with the turbine 32 , for example, by concentrically connecting the generator 34 to the turbine 32 or by other suitable arrangements.
  • the generator 34 of the energy recovery unit 30 may be connected to one or more process operating units (e.g., pump and blower disposed in each capture process, which are typically driven by electrical energy) of the CO 2 capturing apparatus so as to supply generated electrical energy to the respective process operating units.
  • process operating units e.g., pump and blower disposed in each capture process, which are typically driven by electrical energy
  • exhaust gas containing CO 2 may be supplied into an absorption tower 10 , and absorbent, typically liquid absorbent, may be supplied from an absorbent storage tank 12 to an upper part of the absorption tower 10 .
  • absorbent typically liquid absorbent
  • the exhaust gas supplied into the absorption tower 10 may contact liquid absorbent (absorption solution), typically at an atmospheric pressure, in the absorption tower 10 (e.g. in the upper part of the absorption tower 10 ), and CO 2 within the exhaust gas may be absorbed by the absorbent.
  • liquid absorbent absorption solution
  • the absorbent that absorbs CO 2 (“used CO 2 absorbent”) is discharged from the absorption tower 10 , and is supplied to a recovery tower 14 where it may then undergo a recovery process.
  • the absorbent is heated to a suitable temperature (such as a temperature of about 100° C. to about 160° C.) in the recovery tower 14 .
  • the absorbent recovered in the recovery process is discharged from the lower part of the recover tower 14 , and may then be resupplied to the absorption tower 10 via an absorbent supplying line 22 which connects the absorbent storage tank 12 and the absorption tower 10 .
  • the resupplied absorbent passes through a heat exchanger 16 , and thereafter combines with CO 2 absorbent newly supplied from the absorption tower 10 .
  • the newly supplied CO 2 absorbent may be preheated by heat exchange with the heated resupplied absorbent, and the combined absorbent (newly supplied absorbent and resupplied absorbent) may then be supplied to the upper part of the recovery tower 14 .
  • evaporated absorbent with CO 2 may be discharged from the upper part of the recovery tower 14 .
  • liquid absorbent with CO 2 may be discharged from the lower part of the recovery tower 14 , may pass through a heater 18 (e.g. a boiler or the like) where it is heated to a suitable temperature range, such as a temperature of about 100° C. to about 160° C., so as to separate CO 2 from the absorbent.
  • a heater 18 e.g. a boiler or the like
  • CO 2 separated in the recovery tower 14 i.e., CO 2 with evaporated absorbent
  • CO 2 with evaporated absorbent may be discharged to a condenser 20 .
  • condensed absorbent may be resupplied to the recovery tower 14 , while separated CO 2 may be discharged to a location for fixation or conversion treatment.
  • the pressure of CO 2 may range from about 1.8 atm to about 6 atm.
  • a suitable discharge pressure of CO 2 necessary for the fixation or conversion treatment may be less than this discharge pressure, and, for example, may be less than 1.8 atm, less than 1.6 atm, less than 1.4 atm, and in some embodiments, may be about 1.2 atm.
  • separated CO 2 discharged from the condenser 20 at a pressure of about 1.8 atm to about 6 atm is passes through the turbine 32 of the energy recovery apparatus 30 .
  • the turbine 32 may be rotated, and the rotary force of the turbine 32 may be delivered to the generator 34 .
  • the pressure of CO 2 may be reduced to a suitable pressure level for the fixation or conversion treatment.
  • separated CO 2 is discharged from the condenser 20 at a pressure of about 1.8 atm to about 6 atm, and passes through the turbine 32 where the pressure of the CO 2 is constantly or continuously reduced as needed to a suitable pressure level for fixation or conversion treatment.
  • the final discharge pressure of CO 2 that has passed through the turbine 32 may be reduced to a pressure of about 1.2 atm, which is a suitable pressure for the subsequent fixation or conversion treatment.
  • the rotary force of the turbine 32 may be delivered to the generator 34 , enabling the generation of energy by the generator 34 .
  • Electrical energy generated in the generator 34 may be supplied to and consumed in one or more of the process operating units (e.g., pump and blower disposed in each capture process and driven by electrical energy) of the CO 2 capturing apparatus.
  • the amount of energy that must be supplied (i.e. external energy) to operate the CO 2 capturing apparatus can be significantly reduced, and costs can be saved by utilizing electrical energy generated in the generator 34 of the energy recovery unit 30 as energy for powering one or more of the process operating units of the CO 2 capturing apparatus.
  • the consumed energy kW of a reboiler (e.g., heater 18 connected to the lower part of the recovery tower 14 ) for each gas-liquid flow ratio and the flow rate of CO 2 gas discharged from the condenser are shown in Table 2 below.
  • the pressure of CO 2 inputted into the turbine ranged from about 4.12 atm to about 4.41 atm regardless of a wet or dry flow, and the pressure of CO 2 discharged into a fixation or conversion treatment unit through the turbine is constantly reduced to about 1.20 atm. Also, as energy generated by the generator increased according to the turbine efficiency, energy used in the absorbent pump of the CO 2 capturing apparatus was reduced.
  • the discharge pressure of CO 2 captured by the CO 2 capturing apparatus can be reduced to a pressure necessary for the fixation or conversion treatment.
  • An energy recovery unit can be provided to generate energy from the pressure reduction, particularly wherein a turbine is positioned through which captured CO 2 passes such that the rotary force of the turbine can be delivered to a generator to obtain an energy recovery effect in which electrical energy is produced.
  • electrical energy produced in the generator can be utilized as energy for driving various process operating units (e.g., pump and blower) of the CO 2 capturing apparatus, energy (i.e., externally supplied energy) necessary for operating the apparatus to capture CO 2 can be significantly saved.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
US13/531,862 2012-03-09 2012-06-25 Apparatus and method for recovering energy after carbon dioxide capture Abandoned US20130234438A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2012-0024182 2012-03-09
KR1020120024182A KR20130102950A (ko) 2012-03-09 2012-03-09 이산화탄소 포집후 에너지 회수 장치 및 방법

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Families Citing this family (5)

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Publication number Priority date Publication date Assignee Title
JP6107695B2 (ja) * 2014-02-10 2017-04-05 日立化成株式会社 二酸化炭素回収装置及び二酸化炭素回収方法
CN107983089B (zh) * 2017-11-29 2019-09-13 苏州绿碳环保科技有限公司 一种工厂电厂炼厂烟气捕获、转化和应用全量资源化系统
CN108679682B (zh) * 2018-03-13 2019-07-30 东南大学 回收火力发电厂干法捕集co2过程余热并用于供热的系统
CN115350574B (zh) * 2022-08-03 2023-08-04 大连理工大学 气体热功能量回收及碳捕获综合利用方法和装置
CN116154241A (zh) * 2023-02-17 2023-05-23 中国华能集团清洁能源技术研究院有限公司 与电厂碳捕集耦合的金属-二氧化碳电池电力系统及其运行方法

Citations (3)

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Publication number Priority date Publication date Assignee Title
US6209307B1 (en) * 1999-05-05 2001-04-03 Fpl Energy, Inc. Thermodynamic process for generating work using absorption and regeneration
US6497852B2 (en) * 2000-12-22 2002-12-24 Shrikar Chakravarti Carbon dioxide recovery at high pressure
US20110068585A1 (en) * 2009-09-24 2011-03-24 Alstom Technology Ltd Method and system for capturing and utilizing energy generated in a flue gas stream processing system

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6209307B1 (en) * 1999-05-05 2001-04-03 Fpl Energy, Inc. Thermodynamic process for generating work using absorption and regeneration
US6497852B2 (en) * 2000-12-22 2002-12-24 Shrikar Chakravarti Carbon dioxide recovery at high pressure
US20110068585A1 (en) * 2009-09-24 2011-03-24 Alstom Technology Ltd Method and system for capturing and utilizing energy generated in a flue gas stream processing system

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