WO2007073201A1 - Procede energetiquement efficace d’elimination et de sequestration de co2 dans un gaz d’echappement d’unites de traitement d’energie - Google Patents

Procede energetiquement efficace d’elimination et de sequestration de co2 dans un gaz d’echappement d’unites de traitement d’energie Download PDF

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Publication number
WO2007073201A1
WO2007073201A1 PCT/NO2006/000485 NO2006000485W WO2007073201A1 WO 2007073201 A1 WO2007073201 A1 WO 2007073201A1 NO 2006000485 W NO2006000485 W NO 2006000485W WO 2007073201 A1 WO2007073201 A1 WO 2007073201A1
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WO
WIPO (PCT)
Prior art keywords
stream
absorbent
desorber
exhaust gas
energy
Prior art date
Application number
PCT/NO2006/000485
Other languages
English (en)
Inventor
Dag Arne Eimer
Knut Ingvar ÅSEN
Original Assignee
Norsk Hydro Asa
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Norsk Hydro Asa filed Critical Norsk Hydro Asa
Publication of WO2007073201A1 publication Critical patent/WO2007073201A1/fr

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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
    • 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
    • B01D53/14—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
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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 efficient process for removing and sequestering CO 2 from energy process plants exhaust gas.
  • Carbon dioxide recovery demands that the temperature of the exhaust gas is reduced to lower levels than the typical gas turbine exhaust gas temperature of 500 0 C.
  • Highest temperature allowable for separating carbon dioxide from gas with today's technology is in the region of 100-150 0 C, but more typical for exhaust gas treatment would be 20-50 0 C.
  • droplets When treating the exhaust gas with liquid based methods (e.g. absorption), droplets will usually become present in the gas phase. Droplets may also arise when condensation occurs. Thus it is desirable to remove such droplets either to recover the liquid or to avoid an extra effluent to the atmosphere.
  • liquid based methods e.g. absorption
  • a conventional design for a plant to achieve heat recovery, cooling, and carbon dioxide removal from exhaust gas will embrace a separate boiler, followed by a cooler for the gas before the carbon dioxide is removed in an absorption column with a demister unit downstream, and probably a blower to overcome the ensuing pressure drop.
  • These process units are bulky and require instrumentation and control, in addition to a complex piping system to connect the various units.
  • the main objective of the present invention was to arrive at a more energy efficient process for removing and sequestering CO 2 from energy process plants exhaust gas.
  • the present invention relates to how desorption of CO 2 can be done with reduced energy consumption relative to the state of the art. It is observed that the overhead stream from the desorber contains a large amount of water vapour that is subsequently condensed to recover the water, and the latent heat in this vapour is in known processes wasted in the condensation step. When, in the conventional process as illustrated in Figure 1 , CO 2 is recovered for the purpose of carbon sequestration, the CO 2 in the desorber overhead stream has to be compressed before it can be deposited in whatever way that is available to the plant, but the application of a condenser to remove the bulk of the water is practised in conventional plants. In the new method the overhead stream is compressed without prior treatment to alter its temperature or condense water.
  • Vapour recompression as such is not normally profitable, but in this case the compression step is combined with the compression of the CO 2 that is needed anyway, and the compressor is now an extension in capacity of a machine that is already required.
  • the compressed gas mixture can be used directly to provide heat for the reboiler in the desorption plant or it can be used to raise steam from BFW (boiler feed water), and this steam can subsequently be used as heat medium in the reboiler. It is obvious that the heat thus recovered could also be used for other heating purposes if present on site. And in the case of practicing the invention in the form where steam is raised, then the raised steam could be incorporated in local steam nets if desirable.
  • Figure 1 shows a flowsheet of an embodiment of a conventional desorption process.
  • Figure 2 shows a flowsheet of an embodiment of the process according to the present invention.
  • Figure 3 shows a flowsheet of another embodiment of the process according to the present invention.
  • desorption column (desorber) overhead stream 1 is compressed 53 with the compressed stream 2 being cooled by boiler feed water (BFW) 20 in heat exchanger 54 before the cooled overhead stream 3 is further compressed 55 rendering a hot stream 4 that is used to partially evaporate the heated BFW 22 in heat exchanger 56 thus partially condensing the overhead stream that as stream 5 enters the separator 57 where essentially condensed water leaves the bottom as stream 12 that is let down in pressure by valve 66 before it is mixed with stream 15 to be explained below and the mixed stream 13 is returned to the desorber 51 preferably mixed with stream 40 the rich amine stream to be stripped thus aiding pre-flashing of its CO 2 content.
  • BFW boiler feed water
  • the moist CO 2 stream 6 leaving the top of the separator 57 is compressed 58 giving a hot stream 7 that is producing more steam in stream 21 that left the heat exchanger 59.
  • the mainly CO 2 stream with condensed water 8 is further cooled in heat exchanger 60 by a cooling stream 30/31 to condense more water out off the stream 8 that enters separator 61 as a 2-phase stream.
  • the bottom stream 15 from the separator is flashed over valve 65 and mixed with stream 12 as explained already.
  • the separator 61 overhead stream 10 is essentially CO 2 that is further compressed 62 before being dried 63 rendering a CO 2 stream 11 that can be compressed or pumped to whatever pressure that is required for sequestration purposes.
  • the steam need for the process is balanced by fresh steam in stream 25.
  • the desorber overhead stream 201 is compressed 253 rendering a warm stream 202 that is used to reboil 250 the desorption column 51 leaving a 2-phase stream 203 that is separated in separator 257.
  • the bottom stream 205 from 257 is flashed to the pressure of the desorption column 251 over valve 206 giving a 2-phase stream 207 that is separated in separator 260.
  • This separator's bottom stream is lead to column 51 as shown.
  • the overhead stream 208 from separator 260 is used to reboil 251 the desorption column 51 before the cooled stream 210 is pumped to the separator 257 (pump not shown).
  • the overhead stream from separator 257 is compressed 255 giving a warm stream 211 that is used to raise steam 215 in heat exchanger 256 before the cooled stream 212, that is essentially CO 2 , is dried before being "sequestered" as stream 213.
  • Vapour stream 1 at 0.55 barg is compressed to 3.3 barg in a compressor 53.
  • Vapour 2 at 3.3 barg and 233 0 C is cooled to 140 0 C in a boiler 54 and further compressed to 8 barg in a compressor 55.
  • Vapour 4 at about 233 0 C enters a boiler/condenser 56 where about 73% of the water vapour is condensed.
  • Vapour/liquid mixture 5 enters a separator vessel 57 containing a demister and is separated in one vapour stream 6 containing about 23 wt% H 2 O and 77wt% CO 2 and one liquid stream 12 containing mainly water and any MEA entrainments.
  • vapour stream 6 is further compressed to 19.6 bar in compressor 58 and cooled to 140 0 C in boiler/condenser 59 and further cooled to about 25 0 C in a water cooled condenser 60.
  • vapour stream 6 is cooled to about 25 0 C in a separate condenser (not shown). Vapour and liquid are separated in a vessel containing a demister (not shown) before being compressed to about 20 bar in compressor 58. Unit 59 is by-passed in this case.
  • Stream 9 is separated in a vapour stream 10 containing more than 99% CO 2 and a liquid stream 15 containing mainly water.
  • the vapour stream 10 is compressed to about 75 bar and is further liquefied (not shown) and dried in a unit 63.
  • Condensed water stream 13 at 140 0 C is mixed with rich amine solution stream 40.
  • Cold condensate stream 15 is recycled to the top of the stripper column.
  • Boiler feed water 20 is fed to boiler 54, boiler/condenser 56 and boiler condenser 60.
  • Generated steam at about 2 barg and 133 0 C enters reboiler 50 (section a). About 75% of required heat is supplied by steam generated in said boilers. About 25% of the steam is supplied to reboiler 50 (section b) from other sources.
  • Vapour stream 103 is compressed to 75 bar in 4 compressor stages 156, 159, 162 and 165 with intermediate coolers 157, 160 and 163 and intermediate vapour/condensate separators 158, 161 and 164.
  • the compressed CO 2 stream 113 is further liquefied (not shown) and dried in a unit 166.
  • the advantage of the present invention is exemplified by the following difference in energy consumption between the conventional process ( Figure 1) and the novel process ( Figure 2).
  • the heat consumption is 4 MJ/kg CO 2 recovered in both cases.
  • Steam to electric power efficiency is estimated to 28% using low pressure steam to generate electric power in a condensation steam turbine assuming a turbine efficiency of 90% and exit pressure of 0.025 bar.
  • the present invention can increase the power plant efficiency with about 1.3 %-points.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

La présente invention concerne un procédé énergétiquement efficace d’élimination et de séquestration de CO2 dans un gaz d’échappement d’unités de traitement d’énergie respectivement par absorption et désorption chimiques, ledit gaz d’échappement étant introduit dans un absorbeur contenant un absorbant chimique, le CO2 étant absorbé dans ledit absorbant et un courant de gaz d’échappement appauvri en CO2 étant formé, l’absorbant riche en CO2 étant ensuite introduit dans un désorbeur au niveau duquel le CO2 est éliminé de l’absorbant, l’absorbant sensiblement exempt de CO2 étant remis en circulation vers l’absorbeur et le CO2 gazeux désorbé étant déchargé, ledit courant de CO2 déchargé étant comprimé et le courant comprimé et chaud étant utilisé directement pour le rebouillage du désorbeur ou pour obtenir de la vapeur à partir de l’eau d’alimentation du bouilleur, ladite vapeur pouvant être utilisée en tant que moyen de chauffage pour le rebouillage dudit désorbeur.
PCT/NO2006/000485 2005-12-21 2006-12-18 Procede energetiquement efficace d’elimination et de sequestration de co2 dans un gaz d’echappement d’unites de traitement d’energie WO2007073201A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO20056112 2005-12-21
NO20056112 2005-12-21

Publications (1)

Publication Number Publication Date
WO2007073201A1 true WO2007073201A1 (fr) 2007-06-28

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008063082A3 (fr) * 2006-11-24 2008-07-31 Aker Clean Carbon As Améliorations apportées à la régénération d'un absorbant
WO2010129856A1 (fr) * 2009-05-08 2010-11-11 Alstom Technology Ltd Récupération de chaleur à partir d'un procédé de capture de dioxyde de carbone, et procédé de compression pour traitement de combustible
WO2010145732A1 (fr) * 2009-05-14 2010-12-23 Linde-Kca-Dresden Gmbh Procédé et dispositif pour le traitement de gaz de fumées
WO2011029814A1 (fr) * 2009-09-11 2011-03-17 Siemens Vai Metals Technologies Gmbh Procédé d'élimination de co2 contenu dans des effluents gazeux, tels que des effluents gazeux provenant d'installations pour la fabrication de fonte brute ou des effluents gazeux provenant d'installations de production de gaz de synthèse
EP2305364A1 (fr) 2009-09-29 2011-04-06 Alstom Technology Ltd Centrale électrique dotée pour capture de CO2
EP2305363A1 (fr) 2009-09-29 2011-04-06 Alstom Technology Ltd Centrale électrique dotée pour capture de CO2
WO2011003892A3 (fr) * 2009-07-10 2011-06-23 Hitachi Power Europe Gmbh Centrale thermique au charbon avec lavage des fumées et récupération de chaleur
EP2444141A1 (fr) * 2010-10-21 2012-04-25 Kabushiki Kaisha Toshiba Procédé de récupération de dioxyde de carbone et système de génération d'énergie de vapeur de type à récupération de dioxyde de carbone
EP2511001A1 (fr) * 2011-04-14 2012-10-17 Mitsubishi Heavy Industries, Ltd. Système de récupération de CO2 et procédé de récupération de CO2 gazeux contenant de l'humidité
US8321056B2 (en) 2008-01-11 2012-11-27 Alstom Technology Ltd Power plant with CO2 capture and compression
US8346394B2 (en) 2008-01-11 2013-01-01 Alstom Technology Ltd Power plant with CO2 capture and compression
WO2013040094A1 (fr) * 2011-09-12 2013-03-21 E. I. Du Pont De Nemours And Company Procédés et appareil pour la capture de dioxyde de carbone
US8721770B2 (en) 2008-12-04 2014-05-13 E I Du Pont De Nemours And Company Carbon dioxide removal and ionic liquid compounds useful therein
US9017455B2 (en) 2010-06-03 2015-04-28 E I Du Pont De Nemours And Company Sulfur compounds for carbon dioxide and sulfur dioxide removal
US9067953B2 (en) 2010-03-12 2015-06-30 E I Du Pont De Nemours And Company Systems for carbon dioxide and sulfur dioxide removal

Citations (4)

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Publication number Priority date Publication date Assignee Title
US4384875A (en) * 1980-03-31 1983-05-24 Societe Nationale Elf Aquitaine Process and installation for regenerating an absorbent solution containing gaseous compounds
US4444571A (en) * 1983-03-07 1984-04-24 Bend Research, Inc. Energy-efficient process for the stripping of gases from liquids
EP0551876A2 (fr) * 1992-01-17 1993-07-21 The Kansai Electric Power Co., Inc. Procédé pour éliminer de dioxyde de carbone de gaz de combustion
WO2004080573A1 (fr) * 2003-03-10 2004-09-23 Board Of Regents - The University Of Texas System Regeneration d'une solution aqueuse a partir d'un procede d'absorption de gaz acide par un flashage et un strippage multietage

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4384875A (en) * 1980-03-31 1983-05-24 Societe Nationale Elf Aquitaine Process and installation for regenerating an absorbent solution containing gaseous compounds
US4444571A (en) * 1983-03-07 1984-04-24 Bend Research, Inc. Energy-efficient process for the stripping of gases from liquids
EP0551876A2 (fr) * 1992-01-17 1993-07-21 The Kansai Electric Power Co., Inc. Procédé pour éliminer de dioxyde de carbone de gaz de combustion
WO2004080573A1 (fr) * 2003-03-10 2004-09-23 Board Of Regents - The University Of Texas System Regeneration d'une solution aqueuse a partir d'un procede d'absorption de gaz acide par un flashage et un strippage multietage

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008063082A3 (fr) * 2006-11-24 2008-07-31 Aker Clean Carbon As Améliorations apportées à la régénération d'un absorbant
US8321056B2 (en) 2008-01-11 2012-11-27 Alstom Technology Ltd Power plant with CO2 capture and compression
US8346394B2 (en) 2008-01-11 2013-01-01 Alstom Technology Ltd Power plant with CO2 capture and compression
US8721770B2 (en) 2008-12-04 2014-05-13 E I Du Pont De Nemours And Company Carbon dioxide removal and ionic liquid compounds useful therein
WO2010129856A1 (fr) * 2009-05-08 2010-11-11 Alstom Technology Ltd Récupération de chaleur à partir d'un procédé de capture de dioxyde de carbone, et procédé de compression pour traitement de combustible
AU2010245778B2 (en) * 2009-05-08 2016-05-12 General Electric Technology Gmbh Heat recovery from a carbon dioxide capture and compression process for fuel treatment
US8500891B2 (en) 2009-05-08 2013-08-06 Alstom Technology Ltd Waste heat recovery from a carbon capture process
WO2010145732A1 (fr) * 2009-05-14 2010-12-23 Linde-Kca-Dresden Gmbh Procédé et dispositif pour le traitement de gaz de fumées
WO2011003892A3 (fr) * 2009-07-10 2011-06-23 Hitachi Power Europe Gmbh Centrale thermique au charbon avec lavage des fumées et récupération de chaleur
WO2011029814A1 (fr) * 2009-09-11 2011-03-17 Siemens Vai Metals Technologies Gmbh Procédé d'élimination de co2 contenu dans des effluents gazeux, tels que des effluents gazeux provenant d'installations pour la fabrication de fonte brute ou des effluents gazeux provenant d'installations de production de gaz de synthèse
WO2011039263A1 (fr) 2009-09-29 2011-04-07 Alstom Technology Ltd. Centrale électrique à capture de co2
EP2305364A1 (fr) 2009-09-29 2011-04-06 Alstom Technology Ltd Centrale électrique dotée pour capture de CO2
EP2305363A1 (fr) 2009-09-29 2011-04-06 Alstom Technology Ltd Centrale électrique dotée pour capture de CO2
US9067953B2 (en) 2010-03-12 2015-06-30 E I Du Pont De Nemours And Company Systems for carbon dioxide and sulfur dioxide removal
US9017455B2 (en) 2010-06-03 2015-04-28 E I Du Pont De Nemours And Company Sulfur compounds for carbon dioxide and sulfur dioxide removal
CN102451605B (zh) * 2010-10-21 2015-03-11 株式会社东芝 二氧化碳回收方法及二氧化碳回收型火力发电系统
CN102451605A (zh) * 2010-10-21 2012-05-16 株式会社东芝 二氧化碳回收方法及二氧化碳回收型火力发电系统
EP2444141A1 (fr) * 2010-10-21 2012-04-25 Kabushiki Kaisha Toshiba Procédé de récupération de dioxyde de carbone et système de génération d'énergie de vapeur de type à récupération de dioxyde de carbone
AU2011239264B2 (en) * 2010-10-21 2013-11-14 Kabushiki Kaisha Toshiba Carbon dioxide recovery method and carbon-dioxide-recovery-type steam power generation system
US8720203B2 (en) 2010-10-21 2014-05-13 Kabushiki Kaisha Toshiba Carbon dioxide recovery method and carbon-dioxide-recovery-type steam power generation system
AU2012201488B2 (en) * 2011-04-14 2014-02-20 Mitsubishi Heavy Industries, Ltd. CO2 recovery system and recovery method for moisture containing CO2 gas
JP2012223661A (ja) * 2011-04-14 2012-11-15 Mitsubishi Heavy Ind Ltd Ｃｏ２回収システム及びｃｏ２ガス含有水分の回収方法
US9050555B2 (en) 2011-04-14 2015-06-09 Mitsubishi Heavy Industries, Ltd. CO2 recovery system and recovery method for moisture containing CO2 gas
EP2511001A1 (fr) * 2011-04-14 2012-10-17 Mitsubishi Heavy Industries, Ltd. Système de récupération de CO2 et procédé de récupération de CO2 gazeux contenant de l'humidité
US9400106B2 (en) 2011-04-14 2016-07-26 Mitsubishi Heavy Industries, Ltd. CO2 recovery system and recovery method for moisture containing CO2 gas
WO2013040094A1 (fr) * 2011-09-12 2013-03-21 E. I. Du Pont De Nemours And Company Procédés et appareil pour la capture de dioxyde de carbone

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