[go: up one dir, main page]

WO2012120370A2 - Système et procédé d'absorption physique du dioxyde de carbone contenu dans un flux de gaz de carneau - Google Patents

Système et procédé d'absorption physique du dioxyde de carbone contenu dans un flux de gaz de carneau Download PDF

Info

Publication number
WO2012120370A2
WO2012120370A2 PCT/IB2012/000449 IB2012000449W WO2012120370A2 WO 2012120370 A2 WO2012120370 A2 WO 2012120370A2 IB 2012000449 W IB2012000449 W IB 2012000449W WO 2012120370 A2 WO2012120370 A2 WO 2012120370A2
Authority
WO
WIPO (PCT)
Prior art keywords
carbon dioxide
flue gas
gas stream
solvent
stream
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/IB2012/000449
Other languages
English (en)
Other versions
WO2012120370A3 (fr
Inventor
Gianfranco Ludovico GUIDATI
Jean-Marc Gilbert AMANN
Viktoria VON ZEDTWITZ-NIKULSHYNA
Andre Burdet
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.)
GE Vernova GmbH
Original Assignee
Alstom Technology AG
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 Alstom Technology AG filed Critical Alstom Technology AG
Priority to CN2012800125472A priority Critical patent/CN103415332A/zh
Priority to EP12711448.6A priority patent/EP2683462A2/fr
Publication of WO2012120370A2 publication Critical patent/WO2012120370A2/fr
Publication of WO2012120370A3 publication Critical patent/WO2012120370A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • B01D53/1425—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
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2021—Methanol
    • 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
    • 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

  • This disclosure relates to a system and to a process for the physical absorption of carbon dioxide from a flue gas stream.
  • this disclosure relates to a method and system for the physical absorption of carbon dioxide (C0 2 ) from a process gas stream using a solvent.
  • a stream of hot flue gas (also sometimes known as process gas) is generated.
  • a hot flue gas contains, among other components, carbon dioxide (C0 2 ).
  • C0 2 carbon dioxide
  • a system comprising a first heat exchanger; the first heat exchanger being operative to reduce a temperature of a carbon dioxide rich flue gas stream to about -100 to about -60°C; an absorber; the absorber being located downstream of the first heat exchanger; wherein the absorber facilitates contact between the flue gas stream and a solvent to form a carbon dioxide rich solvent stream; the solvent being operative to selectively absorb carbon dioxide over other gases present in the flue gas stream; and a valve; the valve being located downstream of the absorber; the valve being operative to reduce a pressure on the carbon dioxide rich solvent stream to produce carbon dioxide and a lean carbon dioxide solvent stream.
  • a method for capture of carbon dioxide from a flue gas stream comprising receiving a carbon dioxide rich flue gas stream from an emitter; the carbon dioxide rich flue gas stream being at the pressure and temperature of the emitter; refrigerating the carbon dioxide rich flue gas stream to a pressure of greater than or equal to about 101.325 kPa and a temperature of about 0°C to about the melting point of carbon dioxide for a given molar concentration of carbon dioxide within the carbon dioxide rich flue gas stream; contacting the refrigerated carbon dioxide rich flue gas stream with a lean liquid carbon dioxide solvent stream; the lean liquid carbon dioxide solvent stream having a higher solubility for carbon dioxide than of other gases present in the carbon dioxide rich flue gas stream; absorbing carbon dioxide with a liquid solvent to provide a carbon dioxide rich solvent stream and a lean carbon dioxide flue gas stream; and decreasing pressure of the carbon dioxide rich solvent stream to provide the lean liquid carbon dioxide solvent stream and carbon dioxide gas.
  • Figure 1 depicts an exemplary system for capturing carbon dioxide from a flue gas stream
  • Figure 2 schematically depicts an exemplary multi-stage desorption system that may be used in the system of Figure 1.
  • the system advantageously comprises an absorber tower in fluid communication with a flash tank, and a valve or a turbine.
  • absorber tower hereinafter "absorber"
  • carbon dioxide is selectively absorbed from a carbon dioxide rich flue gas stream into a solvent in an absorber, while in the flash tank, the absorbed carbon dioxide is released from the solvent and then discharged into a pipeline from which it is then sequestered or used for other processes.
  • the method for capture of the carbon dioxide from a flue gas comprises refrigerating a carbon dioxide rich flue gas (RFG) stream at a pressure of greater than or equal to about 101.325 kPa and a temperature of about 0°C to about the melting point of carbon dioxide for the given molar concentration of carbon dioxide within the carbon dioxide rich flue gas stream.
  • the carbon dioxide rich flue gas stream emanating from the emitter has a pressure greater than or equal to about atmospheric pressure and a temperature of about 40 to about 60°C.
  • the pressure of the refrigerated carbon dioxide rich flue gas stream can be up to about 1000 kPa.
  • the method further comprises contacting the refrigerated carbon dioxide rich flue stream with a lean carbon dioxide solvent having a higher solubility for the carbon oxide (in the flue gas stream) than for nitrogen and oxygen at the carbon dioxide rich flue gas stream temperature.
  • the contact between the carbon dioxide rich flue gas stream and the solvent results in the extraction of carbon dioxide from the carbon dioxide rich flue gas stream to produce a lean carbon dioxide flue gas stream and a carbon dioxide rich solvent stream.
  • the carbon dioxide is desorbed along with the production of a lean carbon dioxide solvent stream. The desorbed carbon dioxide is separately sequestered.
  • This system has a number of advantages because the solvent selectively absorbs carbon dioxide from the flue gas, while not interacting with other flue gas constituents such as nitric oxides (NO x ), sulfur oxides (SO x ), and the like.
  • the other flue gas constituents such as NO x and SO x may be removed upstream of the system if desired. This means that the stream of carbon dioxide obtained after the separation from the solvent can be advantageously used for other chemical purposes (other than sequestration) if desired.
  • the Figure 1 depicts a system 100 for removing carbon dioxide from a carbon dioxide rich flue gas stream.
  • the system comprises a first heat exchanger 102 in fluid communication with a first active cooling loop 200, an absorption-desorption loop 300 and a second active cooling loop 400.
  • the absorption-desorption loop comprises an absorber 302, a valve 304, a flash tank 306, absorber 302, valve 304, a pump 314 and a compressor 308.
  • the first heat exchanger 102 lies downstream of a flue gas emitter 110 at which the flue gas stream (from which carbon dioxide is to be removed) is generated.
  • the flue gas stream may pass through other devices such as scrubbers (not shown) where other contaminants such as oxygen, nitrogen and particulate matter can be removed prior to entering the first heat exchanger 102.
  • the first heat exchanger 102 lies upstream of the first active cooling loop 200, the absorption-desorption loop 300 and the second active cooling loop 400.
  • the first heat exchanger 102 can comprise any type of heat exchanger or sequence of heat exchangers and serves to cool down the flue gas stream emanating from the flue gas stream emitter 1 10 to a temperature proximate to the melting point of carbon dioxide.
  • the carbon dioxide rich flue gas stream 101 emanating from flue gas stream emitter 110 is cooled in the first heat exchanger 102 by a counter current flow of a cooled lean carbon dioxide flue gas stream 107 that emanates from the absorber 302.
  • the carbon dioxide rich flue gas stream 101 generally contains about 3 to about 30 molar percent (mol%) carbon dioxide based on the total weight of the carbon dioxide rich flue gas stream 101.
  • the lean carbon dioxide flue gas stream 107 generally contains about 0 to about 10 mol% carbon dioxide based on the total weight of the lean carbon dioxide flue gas stream 107.
  • the first heat exchanger 102 reduces the temperature of the flue gas stream from a temperature of about 40 to about 100°C to a temperature of about -60° to about -100°C.
  • the first heat exchanger 102 reduces the temperature of the flue gas stream to a temperature slightly above the melting temperature of carbon dioxide. In an exemplary embodiment, it is desirable to reduce the temperature of the flue gas stream to a temperature of -78 to -60°C. In an exemplary embodiment, for a molar carbon dioxide concentration of 14% in the flue gas stream, it is desirable for the carbon dioxide rich flue gas temperature after emanating from the first heat exchanger 102 to be about -100 to -60°C.
  • the first heat exchanger 102 may not be a single unit but may instead optionally comprise a collection of elements with the purpose of cooling down the flue gas stream to the temperature above the melting point of carbon dioxide.
  • the first heat exchanger 102 may comprise one or more heat exchangers; direct contact cooling (DCC) towers including the capability of (i) removing SO x from the carbon dioxide rich flue gas (RFG) stream using a pH-control system and of (ii) sub-zero cooling using a brine solution; active cooling loops, auxiliary systems such as fluid pumps, fans, and the like; and the capability to dry the carbon dioxide rich flue gas through water removal in the DCC and heat exchangers.
  • DCC direct contact cooling
  • the first heat exchanger 102 can be one of a variety of heat exchangers.
  • suitable heat exchangers are a shell and tube heat exchanger, plate heat exchanger, regenerative heat exchanger, adiabatic wheel heat exchanger, plate fin heat exchanger, pillow plate heat exchanger, dynamic scraped surface heat exchanger or a phase- change heat exchanger.
  • One or more of these heat exchangers may be used if desired.
  • An exemplary first heat exchanger 102 is a plate-fin heat exchanger.
  • the carbon dioxide rich flue gas stream 103 is discharged to the first active cooling loop 200.
  • the first active cooling loop 200 is optional.
  • the first active cooling loop 200 is used only to further cool down the carbon dioxide rich flue gas stream 103 when it does not reach the low temperatures desired in the first heat exchanger 102.
  • the first active cooling loop 200 is used when the mass flow of the lean carbon dioxide flue gas stream 107 is substantially less than the mass flow of the carbon dioxide rich flue gas stream 101 and therefore cannot reduce the temperature of the rich flue gas stream 103 to the desired value of -60 to -100°C.
  • the representation of the active cooling system 200 is symbolic and in reality may be achieved using a standard low temperature, multistage cooling cascade.
  • the first active cooling loop 200 may include a heat exchanger 202 for exchanging heat from the carbon dioxide rich flue gas stream to a refrigerant 210, a compressor 204 for circulating the refrigerant 210 within the first active cooling loop 200, a heat exchanger 206 for removing heat from the refrigerant 210, and a throttle valve 208.
  • Exemplary refrigerants 210 that can be used in the first active cooling loop 200 are non-halogenated hydrocarbons such as methane, propane, propene, iso-butane, or the like, ammonia, sulfur dioxide, or the like, or a combination comprising at least one of the foregoing refrigerants. While chlorofluorocarbons may also be used as refrigerants, it is desirable to use environment-neutral refrigerants in the active cooling loops 200 and 400 respectively.
  • the carbon dioxide rich flue gas stream 105 emanating from the first active cooling loop 200 is then discharged to the absorption-desorption loop 300.
  • the absorption- desorption loop 300 comprises an absorber 302, a valve 304, a flash tank 306, an adiabatic compressor 308, a heat exchanger 310 and an intercooled compressor 312.
  • the valve 304, the flash tank 306, the adiabatic compressor 308, the heat exchanger 310 and the intercooled compressor 312 each lie successively downstream of the absorber 302 and are in fluid communication with one another.
  • the carbon dioxide rich flue gas stream 105 enters from the bottom.
  • the carbon dioxide rich flue gas stream 105 flows up from the bottom of the absorber and exits the absorber 302 from the top as the lean carbon dioxide flue gas stream 107.
  • the carbon dioxide rich flue gas stream 105 contacts a solvent that selectively absorbs carbon dioxide from the carbon dioxide rich flue gas stream 105.
  • the solvent can be any solvent that selectively absorbs carbon dioxide from the flue gas stream 105 in preference to other contaminants in the flue gas stream such as nitrogen, oxygen, nitrogen oxides, sulfur oxides, particulate matter, and the like. It is desirable for the solvent to have a low melting point and a low vapor pressure at the operating (sub-zero) temperatures. It is also desirable for the solvent to display a minimal viscosity at operating (sub-zero) temperatures.
  • Suitable solvents for use in absorbing the carbon dioxide in the absorber are alcohols.
  • the alcohols can be monohydric, polyhydric, aliphatic, alicyclic alcohols, or the like, or a combination comprising at least one of the foregoing alcohols.
  • alcohols are methanol, ethanol, propanol, butanol, pentanol, hexadecan-l-ol, ethane- 1,2-diol, propane- 1, 2,3 -triol, butane-l,2,3,4-tetraol, pentane-l,2,3,4,5-pentol, hexane- 1,2,3, 4,5,6- hexol, heptane- 1,2,3,4,5,6,7-heptol, prop-2-ene-l -ol, 3,7-dimethylocta-2,6-dien-l-ol, prop-2- in-l-ol, cyclohexane-l,2,3,4,5,6-hexol, (2-propyl)-5-methyl-cyclohexane-l-ol, or the like, or a combination comprising at least one of the foregoing alcohols.
  • Exemplary alcohols are methanol, ethanol, propan
  • the carbon dioxide rich flue gas stream 105 enters the absorber tower 302 from the bottom, flows upwards during which it contacts the solvent and leaves the absorber 302 at the top.
  • the solvent enters the absorber 302 from the top as a lean carbon dioxide solvent stream 309 and leaves the absorber 302 from the bottom as a carbon dioxide rich solvent stream 301.
  • the pressure within the absorber is maintained at proximately atmospheric pressure during the contact between the solvent and the carbon dioxide rich glue gas stream 105.
  • carbon dioxide and heat from the flue gas stream is absorbed by the solvent.
  • Carbon dioxide from the flue gas stream 105 is absorbed by the solvent via physical absorption.
  • the heat of absorption is mainly extracted by the solvent that warms up during the process of absorption.
  • the lean carbon dioxide flue gas stream 107 which leaves the absorber 302 at the top is used to pre-cool the incoming carbon dioxide rich glue gas stream 101 in the aforementioned first heat exchanger 102.
  • the carbon dioxide rich solvent stream 301 is collected at the bottom of the absorber tower 2 and is passed to the desorption portion of the absorption-desorption loop 300.
  • the desorption portion of the absorption-desorption loop 300 comprises a valve 304, the flash tank 306, a pump 314 and an adiabatic compressor 308.
  • the valve 304 is effective to the pressure of the carbon dioxide rich solvent stream 301 to a level at which the carbon dioxide extracted from the carbon dioxide rich flue gas stream 105 can be desorbed from the solvent and returns into gas phase within the flash tank 306.
  • the solvent enters the absorber 302 from the top and leaves the absorber 302 from the bottom as a carbon dioxide rich solvent stream 301.
  • the valve 304 can be replaced with a turbine to effect the same decrease in pressure which causes the absorbed carbon dioxide to being desorbed from the solvent.
  • the turbine can be used when it is desirable to improve the cooling effect of the expansion and produce power.
  • the reduced pressure is about 5 to about 500 times lower (for a 90% carbon dioxide capture rate) than the original partial pressure of the carbon dioxide in the carbon dioxide rich flue gas stream 105.
  • the pressure in the absorber 302 is around atmospheric pressure.
  • the pressure of the carbon dioxide rich solvent stream after the valve is therefore about l/5 th atmosphere to about 1/500 th atmosphere.
  • the pressure after the valve 304 would be about 0.010 bar. Depending on the operating conditions, this pressure may also be lower or higher.
  • the carbon dioxide lean solvent stream 303 and the carbon dioxide released from the solvent is collected in the flash tank 306.
  • the lean solvent which is in liquid form is extracted from the flash tank by a lean solvent pump 314 and discharged back to the top of the absorber 302.
  • the lean solvent pump 314 increases the pressure of the solvent to the level that is desired at the top of the absorber 314.
  • the pressure at the top of the absorber 302 is about 1 atmosphere or greater. In an exemplary embodiment, the pressure of the solvent at the top of the absorber 302 is about 1 atmosphere.
  • the carbon dioxide gas desorbed from the solvent is drawn from the flash tank 306 by an adiabatic compressor 308.
  • the adiabatic compressor 308 increases the pressure of the carbon gas from about 0.010 bar to a level where the temperature of the gas is above the temperature of available cooling water.
  • the exhaust pressure of the adiabatic carbon dioxide compressor 308 may be up to about 1 bar, specifically about 0.001 to about 1 bar.
  • the carbon dioxide gas leaving the adiabatic carbon dioxide compressor 308 may be cooled using cooling water in a heat exchanger 310.
  • the pressure of the carbon dioxide gas is raised in several steps in an intercooled compressor 312 to a desired pipeline pressure, where the carbon dioxide gas may be transported for use or sequestration.
  • this compression of the carbon dioxide gas may be similar to that used in post-combustion carbon dioxide capture processes based on chemical absorption and oxy-fuel processes.
  • the desorption portion of the absorption-desorption loop 300 may comprise a plurality of valves, flash tanks and adiabatic carbon dioxide
  • a multistage desorption system 500 comprises a first valve 502 in fluid communication with a first flash tank 504, a second valve 506, a second flash tank 508, a third valve 510, a third flash tank 512, a first adiabatic compressor 514, a second adiabatic compressor 516 and a third adiabatic compressor 518.
  • the adiabatic compressors 514, 516 and 518 are in mechanical communication with a motor.
  • a first stage desorption system comprises the first valve 502, a first flash tank 504 and the first adiabatic compressor 514 is in fluid communication with a second stage desorption system comprising the second valve 506, the second flash tank 508 and the second adiabatic compressor 516 and a third desorption system comprising the third valve 510, the third flash tank 512 and the third adiabatic compressor 518.
  • the pressure PI of the carbon dioxide in the first stage desorption system after the first valve 502 is higher than the pressure P2 of the carbon dioxide in the second stage desorption system after the second valve 506, which is in turn greater than the pressure P3 of the carbon dioxide in the third stage desorption system after the third valve 510.
  • the carbon dioxide released by the multistage desorption system 500 is pressurized (as detailed above) in the intercooled compressor 312.
  • the carbon dioxide may also be cooled using cooling water in a heat exchanger 310 that lies upstream of the intercooled compressor 312.
  • This multi-stage arrangement allows the system to collect as much carbon dioxide as possible at a pressure greater than the aforementioned minimum pressure of about 0.010 bar. This arrangement also reduces the power consumption and the size and costs of the adiabatic carbon dioxide compressor. While the Figure 2 shows a possible arrangement with three pressure level stages, it is contemplated that the number of pressure level stages may be greater than 3 or less than 3 but greater than or equal to 1.
  • a second active cooling system 400 may optionally be used on the lean solvent as well.
  • the second active cooling system 400 is optional and functions in much the same manner as the first active cooling system 200.
  • the second active cooling loop 400 may include a second heat exchanger 402 for exchanging heat from the lean solvent stream 307 to a refrigerant 410, a compressor 404 for circulating the refrigerant 410 within the second active cooling loop 400, a heat exchanger 406 for removing heat from the refrigerant 410, and a throttle valve 408.
  • the second active loop 400 may be used to cool down the lean carbon dioxide solvent stream 309 to temperatures where it will most selectively extract carbon dioxide from the carbon dioxide rich flue gas stream 105.
  • the disclosed process is advantageous in a variety of ways.
  • the power consumption of the current method of system 100 is estimated to be low compared to other carbon dioxide capture systems that use solvents which selectively extract carbon dioxide from flue gas streams. This is because the carbon dioxide rich flue gas stream 105 is at about atmospheric pressure during the absorption stage (within absorber 302) no flue gas compression is needed, and since the solvent is regenerated via expansion by valve(s) 304 and flash tank(s) 306, the main power consuming element of system 100 are the carbon dioxide compressors 308 and 312. Use of a high-efficiency axial compressor as carbon dioxide compressor 308 can thus lead to low power consumption. Such a compressor could be based on technology used in gas turbines.
  • the solvent losses in the method of system 100 are expected to be very low because of the low operation temperature (e.g., a carbon dioxide rich flue gas stream temperature of about -100 to -60°C in the absorber 302.
  • the system 100 may be installed with minimal changes to an existing carbon dioxide recovery system (e.g., no need to install compressors to increase the pressure of the rich flue gas stream), the system 10 can be installed on an existing power plant without a long shut-down period.
  • relative terms such as “lower” or “bottom” and “upper” or “top,” may be used herein to describe one element's relationship to other elements as illustrated in the Figures. It will be understood that relative terms are intended to encompass different orientations of the device in addition to the orientation depicted in the Figures. For example, if the device in one of the figures is turned over, elements described as being on the “lower” side of other elements would then be oriented on “upper” sides of the other elements. The exemplary term “lower,” can therefore, encompasses both an orientation of “lower” and “upper,” depending on the particular orientation of the figure.
  • Exemplary embodiments are described herein with reference to cross section illustrations that are schematic illustrations of idealized embodiments. As such, variations from the shapes of the illustrations as a result, for example, of manufacturing techniques and/or tolerances, are to be expected. Thus, embodiments described herein should not be construed as limited to the particular shapes of regions as illustrated herein but are to include deviations in shapes that result, for example, from manufacturing. For example, a region illustrated or described as flat may, typically, have rough and/or nonlinear features.

Landscapes

  • 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)
  • Gas Separation By Absorption (AREA)

Abstract

Le système ci-décrit comprend un premier échangeur thermique, ledit premier échangeur thermique servant à abaisser une température d'un flux de gaz de carneau riche en dioxyde de carbone à environ -100/environ -60°C ; un absorbeur, ledit absorbeur se trouvant en aval du premier échangeur thermique et servant à faciliter le contact entre le flux de gaz de carneau et un solvant pour former un flux de solvant riche en dioxyde de carbone, le solvant servant à absorber sélectivement le dioxyde de carbone par rapport aux autres gaz présents dans le flux de gaz de carneau ; et une soupape, la soupape se trouvant en aval de l'absorbeur et servant à réduire une pression sur le flux de solvant riche en dioxyde de carbone pour obtenir du dioxyde de carbone et un flux de solvant pauvre en dioxyde de carbone.
PCT/IB2012/000449 2011-03-10 2012-03-08 Système et procédé d'absorption physique du dioxyde de carbone contenu dans un flux de gaz de carneau Ceased WO2012120370A2 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN2012800125472A CN103415332A (zh) 2011-03-10 2012-03-08 物理吸收来自烟道气流的二氧化碳的系统和工艺
EP12711448.6A EP2683462A2 (fr) 2011-03-10 2012-03-08 Système et procédé d'absorption physique du dioxyde de carbone contenu dans un flux de gaz de carneau

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201161451278P 2011-03-10 2011-03-10
US61/451,278 2011-03-10
US13/414,132 2012-03-07
US13/414,132 US20120227440A1 (en) 2011-03-10 2012-03-07 System And Process For The Physical Absorption of Carbon Dioxide From a Flue Gas Stream

Publications (2)

Publication Number Publication Date
WO2012120370A2 true WO2012120370A2 (fr) 2012-09-13
WO2012120370A3 WO2012120370A3 (fr) 2012-12-20

Family

ID=46794271

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2012/000449 Ceased WO2012120370A2 (fr) 2011-03-10 2012-03-08 Système et procédé d'absorption physique du dioxyde de carbone contenu dans un flux de gaz de carneau

Country Status (5)

Country Link
US (1) US20120227440A1 (fr)
EP (1) EP2683462A2 (fr)
CN (1) CN103415332A (fr)
TW (1) TW201247308A (fr)
WO (1) WO2012120370A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016081074A1 (fr) * 2014-11-21 2016-05-26 Gas Technology Institute Procédé de régénération de solvant écoénergétique pour la capture de dioxyde de carbone

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8696804B2 (en) 2010-12-29 2014-04-15 Delphi Technologies, Inc. Carbon dioxide absorbent fluid for a carbon dioxide sequestering system on a vehicle
US9267415B2 (en) 2010-12-29 2016-02-23 Delphi Technologies, Inc. Heat exchanger equipped with thermal electric device for engine exhaust carbon dioxide collection system
IN2013MU03192A (fr) * 2013-10-09 2015-07-03 Reliance Ind Ltd
US10508568B2 (en) 2018-03-16 2019-12-17 Uop Llc Process improvement through the addition of power recovery turbine equipment in existing processes
US10745631B2 (en) 2018-03-16 2020-08-18 Uop Llc Hydroprocessing unit with power recovery turbines
US11131218B2 (en) 2018-03-16 2021-09-28 Uop Llc Processes for adjusting at least one process condition of a chemical processing unit with a turbine
US11507031B2 (en) 2018-03-16 2022-11-22 Uop Llc Recovered electric power measuring system and method for collecting data from a recovered electric power measuring system
US11194301B2 (en) 2018-03-16 2021-12-07 Uop Llc System for power recovery from quench and dilution vapor streams
US10811884B2 (en) 2018-03-16 2020-10-20 Uop Llc Consolidation and use of power recovered from a turbine in a process unit
US10829698B2 (en) 2018-03-16 2020-11-10 Uop Llc Power recovery from quench and dilution vapor streams
US10753235B2 (en) 2018-03-16 2020-08-25 Uop Llc Use of recovered power in a process
US10690010B2 (en) 2018-03-16 2020-06-23 Uop Llc Steam reboiler with turbine
US10794225B2 (en) 2018-03-16 2020-10-06 Uop Llc Turbine with supersonic separation
US10871085B2 (en) 2018-03-16 2020-12-22 Uop Llc Energy-recovery turbines for gas streams
US10920624B2 (en) 2018-06-27 2021-02-16 Uop Llc Energy-recovery turbines for gas streams
CN113813744B (zh) * 2021-09-26 2022-10-25 西安交通大学 一种提升燃煤锅炉烟气中co2捕集经济性的系统和方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2863527A (en) * 1949-09-15 1958-12-09 Metallgesellschaft Ag Process for the purification of gases
DE2312754C3 (de) * 1973-03-14 1980-06-26 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Rückgewinnung von wertvollen Bestandteilen bei einer physikalischen Gaswäsche
FR2863910B1 (fr) * 2003-12-23 2006-01-27 Inst Francais Du Petrole Procede de capture du dioxyde de carbone contenu dans des fumees
US7976803B2 (en) * 2005-08-16 2011-07-12 Co2Crc Technologies Pty Ltd. Plant and process for removing carbon dioxide from gas streams
JP2011525860A (ja) * 2008-06-26 2011-09-29 ユーオーピー エルエルシー セミリーン物理溶媒を冷却するための二酸化炭素吸収剤の部分的ポンプアラウンド
DE102008057937A1 (de) * 2008-11-19 2010-05-20 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Waschmittelregenerierung in physikalischen Gaswäschen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016081074A1 (fr) * 2014-11-21 2016-05-26 Gas Technology Institute Procédé de régénération de solvant écoénergétique pour la capture de dioxyde de carbone
JP2018501947A (ja) * 2014-11-21 2018-01-25 ガス テクノロジー インスティテュート 二酸化炭素回収のためのエネルギー効率のよい溶媒再生プロセス
US9901846B2 (en) 2014-11-21 2018-02-27 Gas Technology Institute Energy efficient solvent regeneration process for carbon dioxide capture
RU2660881C1 (ru) * 2014-11-21 2018-07-10 Гэз Текнолоджи Инститьют Энергосберегающий способ регенерации растворителя для улавливания диоксида углерода

Also Published As

Publication number Publication date
TW201247308A (en) 2012-12-01
EP2683462A2 (fr) 2014-01-15
US20120227440A1 (en) 2012-09-13
CN103415332A (zh) 2013-11-27
WO2012120370A3 (fr) 2012-12-20

Similar Documents

Publication Publication Date Title
US20120227440A1 (en) System And Process For The Physical Absorption of Carbon Dioxide From a Flue Gas Stream
KR102311531B1 (ko) 이동 오염원의 내연 기관으로부터 co2 포획 및 화력 생산 사이클에서 사용을 위한 통합 공정
Wolsky et al. CO2 capture from the flue gas of conventional fossil‐fuel‐fired power plants
Song et al. Energy analysis of the cryogenic CO2 capture process based on Stirling coolers
Clodic et al. CO2 capture by anti-sublimation Thermo-economic process evaluation
US20110265512A1 (en) Carbon dioxide capture from power or process plant gases
US9447996B2 (en) Carbon dioxide removal system using absorption refrigeration
EP2668994A1 (fr) Changement de phase de CO2 intégré absorbant pour système de séparation de CO2
TW201248099A (en) Cryogenic CO2 separation using a refrigeration system
CN105268283A (zh) 一种联合吸收的二氧化碳捕集与压缩处理工艺
CN102895860A (zh) 化学吸收co2捕获流程的降耗方法及系统
CN110152453B (zh) 使用溶剂吸收法捕集气体混合物中酸性气体的方法和设备
EP2563499B1 (fr) Procédé de réduction des émissions de co2 dans un flux de combustion et installations industrielles mettant en oeuvre ce procédé
CN107741103A (zh) 一种氨水吸收式制冷联合碳捕集装置
CN103463955A (zh) 一种从工业尾气中分离回收二氧化碳的工艺
ES2981913T3 (es) Procedimiento y aparato para tratar un gas rico en dióxido de carbono que contiene agua
CN112221327A (zh) 一种燃煤电厂二氧化碳氨法捕集及低温液化系统及方法
CN107073388A (zh) 用于二氧化碳捕集的节能溶剂的再生方法
CN108854423A (zh) 一种烟气余热驱动的脱硫、脱硝与碳捕集耦合的烟气净化系统及烟气处理的方法
Malekli et al. CO2 capture and sequestration from a mixture of direct air and industrial exhaust gases using MDEA/PZ: Optimal design by process integration with organic rankine cycle
CN103687659A (zh) 用于低温二氧化碳分离的热综合利用
CN205481067U (zh) 独立太阳能相变梯级蓄热间接热力驱动脱除二氧化碳的系统
CN104791031B (zh) 一种与机组汽水系统整合的二氧化碳捕集再生系统
CN213556279U (zh) 一种燃煤电厂二氧化碳氨法捕集及低温液化系统
US12251658B2 (en) System, apparatus, and method for capture of multi-pollutants from industrial gases and/or exhausts

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12711448

Country of ref document: EP

Kind code of ref document: A2

NENP Non-entry into the national phase

Ref country code: DE

REEP Request for entry into the european phase

Ref document number: 2012711448

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2012711448

Country of ref document: EP