US20070221065A1 - Heat recovery gas absorption process - Google Patents

Heat recovery gas absorption process Download PDF

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Publication number
US20070221065A1
US20070221065A1 US11/386,824 US38682406A US2007221065A1 US 20070221065 A1 US20070221065 A1 US 20070221065A1 US 38682406 A US38682406 A US 38682406A US 2007221065 A1 US2007221065 A1 US 2007221065A1
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United States
Prior art keywords
absorption liquid
section
liquid solvent
solvent system
gas stream
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Abandoned
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US11/386,824
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English (en)
Inventor
Adisorn Aroonwilas
Amornvadee Veawab
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University of Regina
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University of Regina
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Priority to US11/386,824 priority Critical patent/US20070221065A1/en
Assigned to UNIVERSITY OF REGINA reassignment UNIVERSITY OF REGINA ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AROONWILAS, ADISORN, VEAWAB, AMORNVADEE
Priority to JP2009501794A priority patent/JP2009531163A/ja
Priority to US12/294,136 priority patent/US7906087B2/en
Priority to PCT/CA2007/000461 priority patent/WO2007107004A1/en
Priority to KR1020087026022A priority patent/KR20090008270A/ko
Priority to AU2007229238A priority patent/AU2007229238B2/en
Priority to EP07710781A priority patent/EP2004309A4/en
Priority to CN2007800179397A priority patent/CN101472662B/zh
Priority to CA2646443A priority patent/CA2646443C/en
Publication of US20070221065A1 publication Critical patent/US20070221065A1/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
    • B01D53/14—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
    • B01D53/1456—Removing acid components
    • 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S423/00—Chemistry of inorganic compounds
    • Y10S423/06—Temperature control
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S423/00—Chemistry of inorganic compounds
    • Y10S423/08—Corrosion or deposition inhibiting

Definitions

  • This invention relates to the removal of gaseous components from industrial gas streams. More particularly, this invention relates to apparatus and processes for separation and recovery of gaseous components from process gas streams and/or exhaust gas streams.
  • Gas absorption, separation and recovery processes have long been provided for both industrial and environmental purposes.
  • Industrial applications typically involve processes for separation and removal of at least one gaseous component from a process gas stream in order to enhance the quality of gas products produced and/or to prevent undesirable downstream operational problems that might subsequently occur in downstream processes. Examples are the removals of carbon dioxide (CO 2 ) and/or hydrogen sulfide (H 2 S) from natural gas and synthesis gas, and the removals and separations of volatile organic compounds (VOCs) and gases such as nitrogen (N 2 ), oxygen (O 2 ) and hydrogen (H 2 ) from industrial process gas streams.
  • CO 2 carbon dioxide
  • H 2 S hydrogen sulfide
  • VOCs volatile organic compounds
  • gases such as nitrogen (N 2 ), oxygen (O 2 ) and hydrogen (H 2 ) from industrial process gas streams.
  • Environmental applications typically involve the removal of at least one gaseous component such as sulfur dioxide (SO 2 ), CO 2 , oxides of nitrogen (NO x ), and mercury (Hg) from combustion flue gases or exhaust gas streams in order to reduce emissions of air pollutants to the atmosphere.
  • SO 2 sulfur dioxide
  • CO 2 CO 2
  • NO x oxides of nitrogen
  • Hg mercury
  • the exemplary embodiments of the present invention are directed to apparatus and processes for high-capacity energy-efficient: (a) removal of at least one gaseous component from a process gas stream or exhaust gas stream into a liquid solvent system configured to absorb and assimilate the gaseous component, followed by (b) separation and recovery of the gaseous component from the liquid solvent system.
  • an apparatus comprising an absorber device provided with a plurality of sequentially adjacent sections, said absorber device communicating with a conduit infrastructure conveying a liquid solvent system therein, said conduit infrastructure configured to ingress into and egress from each section of the absorber device.
  • the absorber comprises a vertically oriented column provided with a plurality of vertical sequentially positioned adjacent sections.
  • An inlet for a process gas stream is provided near the bottom of the absorber, while an outlet for the gas stream wherefrom a selected gaseous component has been removed, is provided at the top of the absorber.
  • a waste exhaust gas stream can be flowed through the absorber device for removing a selected gaseous component therefrom.
  • the gas stream travels sequentially through the adjacent sections of the absorber against a counter-current flow of the liquid solvent system.
  • the liquid solvent system is provided with at least one chemical component to absorb and/or assimilate and/or sequester the gaseous component from the gas stream.
  • a conduit infrastructure configured to ingress the absorber by communicating with the top portion of the first section, i.e., the section adjacent to the absorber gas stream outlet, and to egress from the bottom of the absorber device.
  • the conduit infrastructure is a piping infrastructure.
  • the piping infrastructure sequentially ingresses into the top portion and egresses from the bottom portion of each adjacent section of the absorber.
  • a lean heat transfer unit interposed a portion of the piping infrastructure that ingresses into the top portion of the first section of the absorber device.
  • the piping infrastructure is provided with a lean cooler unit interposed said lean heat transfer unit and the first section of the absorber.
  • the piping infrastructure ingresses a temperature-manipulated lean absorption liquid into the top portion of the first section of the absorber.
  • a heat transfer unit interposed a portion of said piping infrastructure which egresses from the bottom portion of the first section of the absorber and ingresses into the top portion of the adjacent section of the absorber.
  • said portion of piping infrastructure is provided, interposed said heat transfer unit and the top portion of the adjacent section of the absorber, an interconnection with a portion of piping infrastructure conveying therein a heated liquid solvent system.
  • a heat transfer unit interposed each portion of the piping infrastructure that egresses from the bottom portion of a section of the absorber and ingresses into the top portion of the adjacent section of the absorber.
  • each portion of the piping infrastructure is provided, interposed said heat transfer unit and the top portion of the adjacent section of the absorber, a cooling unit. It is preferred that the cooling unit is a pinched cooling unit.
  • a removal piping infrastructure communicating with the bottom of the absorber for removing therefrom an enriched absorption liquid, i.e., absorption liquid containing therein the gaseous component that has been removed from the process gas stream or the exhaust gas stream.
  • the removal piping infrastructure is interconnected with and cooperates with the heat exchange units provided for each portion of the liquid infrastructure communicating with the sections adjacent to the first section of the absorber whereby the heat energy removed by a heat exchange unit from absorption liquid withdrawn from the bottom portion of each section, is transferred to the enriched absorption liquid being conveyed through said heat exchange unit by the removal piping infrastructure.
  • the removal piping infrastructure is interconnected with and cooperates with the lean-rich heat exchange unit for transferring heat from the hot lean absorption liquid to the enriched absorption liquid being conveyed through said lean-rich heat exchange unit by the removal piping infrastructure.
  • the removal piping infrastructure is interconnected with and cooperates with a first plurality of equipment configured to: (a) separate from the enriched absorption liquid solvent, a stream containing the selected gaseous component removed from the gas stream, and (b) regenerate the enriched absorption liquid into a lean absorption liquid.
  • a second plurality of equipment is provided for recovering the separated stream of selected gaseous component, and further processing and/or purification said selected gaseous component prior to its use for other industrial processes.
  • the recovered and purified gaseous component may be conveyed to and stored in containers selected for that purpose.
  • a process for removing and recovering a selected gaseous component from a process gas stream or exhaust gas stream is flowed sequentially through a multi-sectioned absorber unit wherein the selected gaseous component is removed by repeatedly commingling and contacting the upward flowing gas stream with a counter-flowing temperature-manipulable and temperature-controllable liquid solvent system comprising at least one chemical constituent selected for its propensity to absorb and/or assimilate and/or sequester and/or react with said gaseous component.
  • the liquid solvent system is a lean absorption liquid that is controllably cooled before it is ingressed into the top, i.e., the first section of the absorber, wherein it counter-currently commingles with and contacts the gas stream thereby removing a portion of the selected gaseous component from the gas stream and partially loading the lean absorption liquid.
  • the partially loaded absorption liquid is egressed from the bottom portion of the first section by the piping infrastructure and is conveyed through at least one heat exchange unit wherein the partially loaded absorption liquid is heated to an elevated temperature before it is ingressed into the top portion of the underlying, i.e., the second section.
  • the temperature of the heated partially loaded absorption liquid is adjusted by controllably intermixing with a hot lean absorption liquid.
  • the partially loaded absorption liquid counter-flows through the second section against the gas stream flowing therethrough and removes an additional portion of the selected gaseous component from the gas stream thereby becoming an increasingly loaded absorption liquid.
  • the increasingly loaded absorption liquid is egressed from the bottom portion of the second section by the piping infrastructure and is conveyed through at least one heat exchange unit and one cooling unit configured for cooling and controlling the temperature of the increasingly loaded absorption liquid before it is ingressed into the top portion of the underlying, i.e., the third section.
  • the increasingly loaded absorption liquid counter-flows through the third section against the gas stream flowing therethrough and removes an additional portion of the selected gaseous component from the gas stream thereby becoming a highly loaded absorption liquid.
  • the highly loaded absorption liquid is withdrawn from the bottom portion of the third section by the piping infrastructure, and is conveyed through at least one heat exchange unit and one cooling unit configured for cooling and controlling the temperature of the absorption liquid before it is returned to the top of the bottom, i.e., the last section.
  • the highly loaded absorption liquid counter-flows through the last section against the gas stream flowing therethrough and removes a final portion of the selected gaseous component from the gas stream thereby becoming an enriched absorption liquid.
  • the enriched absorption liquid is removed from the bottom portion of the absorber by a removal piping infrastructure for conveyance to a plurality of equipment selected and configured for recovering the absorbed gaseous component contained within the absorption liquid and for regenerating the absorption liquid into a lean absorption liquid before recycling it to the absorber device.
  • a liquid solvent system for communicating with the absorber device by conveyance therethrough in communication with the piping infrastructure.
  • the liquid solvent system comprises an aqueous solution configured for absorbing and/or assimilating and/or sequestering and/or reacting with a selected gaseous component from a process gas stream, or alternatively, from an exhaust gas stream flowing through the absorber.
  • the aqueous solution is considered a lean absorption liquid when it ingresses the top portion of the first section adjacent the absorber gas stream outlet, and becomes increasing enriched with the selected gaseous component as the aqueous solution counterflows through the adjacent sections against the flow of the gas stream through the absorber thereby becoming a rich absorption liquid when it egresses from the bottom of the absorber.
  • the absorption liquid comprises an aqueous solution provided with at least one chemical component selected for absorbing and/or assimilating and/or sequestering and/or reacting with a selected gaseous component present in the process gas stream or exhaust gas stream or a refining gas stream.
  • the selected gaseous component includes a gas selected from the group comprising CO 2 , H 2 S, SO 2 , and NO x .
  • the absorption liquid comprises: (a) an aqueous solution provided with at least one chemical component selected for absorbing and/or assimilating and/or sequestering and/or reacting with a selected gaseous component present in the process gas stream or exhaust gas stream, and (b) at least one chemical component selected from the group comprising kinetic enhancers, corrosion inhibitors, anti-foam chemicals, oxygen scavengers, salt neutralizers, and anti-degradation chemicals.
  • the lean absorption liquid is controllably cooled and adjusted to a selected temperature prior to its ingress into the first section of the absorber device.
  • a plurality of equipment for cooling and controlling the temperature of said lean absorption liquid.
  • at least one heat transfer unit such as lean-rich heat exchanger for cooling the lean absorption liquid and at least one heat transfer unit for adjusting and refining the temperature of the cooled liquid solvent.
  • the liquid solvent system is configured to remove CO 2 from a combustion exhaust gas stream using the apparatus of the present invention.
  • the liquid solvent system provides an aqueous solution comprising an absorption liquid containing therein at least one chemical compound selected from the group comprising monoethanolamine (MEA), diglycolamine (DGA), diethanolamine (DEA), methyldiethanolamine (MDEA), 2-amino-2-methyl-1-propanol (AMP), piperazine (PZ), other chemical solvents and/or mixtures thereof.
  • the liquid solvent system may further comprise at least one chemical component selected from the group comprising kinetic enhancers, corrosion inhibitors, anti-foam chemicals, oxygen scavengers, salt neutralizers, and anti-degradation chemicals.
  • enriched absorption liquid egressing from the bottom of the absorber device is conveyed into a regenerator wherein the enriched absorption liquid is separated into: (a) a stream of hot lean absorption liquid which is egressed from the bottom of the regenerator and subsequently conveyed to a reboiler unit, and (b) a stream of hot vapor mixtures egressing from the top of the regenerator.
  • a process for reducing vapor loss of water and absorption liquid through the treated gas exiting from the top of the absorber involves two-step vapor reduction.
  • the first step of vapor reduction takes place in the first section of the absorber into which the controllably cooled lean absorption liquid is ingressed, thereby reducing the temperature of treated gas stream and knocking off the water vapor and absorption liquid vapor.
  • the second step of vapor reduction takes place in the treated gas condenser operated at a low temperature.
  • FIG. 1 is a schematic diagram illustrating one embodiment of the present invention
  • FIG. 2 is a graph illustrating the temperature profiles of an absorption liquid passing through a multi-sectioned absorber of the present invention.
  • FIG. 3 is a graph illustrating the effects of temperature manipulation on operating and equilibrium curves of the absorber.
  • the present invention provides apparatus and processes for energy-efficient removal and recovery of at least one gaseous component from process gas streams or exhaust gas streams emanating from chemical processes and/or combustion processes.
  • the invention provides an apparatus comprising an absorber device configured with a plurality of sequentially adjacent sections, said absorber device communicating with a multi-sectioned piping infrastructure conveying a liquid solvent system therein, said piping infrastructure configured to ingress into and egress from each section of the absorber device.
  • the gas stream travels sequentially through the adjacent sections of the absorber against a counter-current flow of the liquid solvent system.
  • the liquid solvent system is provided with at least one chemical component to absorb and/or assimilate and/or sequester and/or react with the gaseous component from the gas stream.
  • the multi-sectioned piping infrastructure is provided with: (a) at least two heat-exchange units configured for cooling absorption liquid flowing therethrough, (b) at least one heat-exchange unit configured for heating liquid solvent system flowing therethrough, each of said heat exchange units for cooling in item (a) cooperating with at least one dedicated cooling unit for precise temperature control of the liquid solvent system flowing through the piping infrastructure into the different sections of the absorber.
  • the multi-sectioned piping infrastructure is configured to: (1) ingress into the top portion and egress from the bottom portion of each section provided within the absorber, and (2) to cooperate with a heat exchange unit and/or a cooling unit interposed between each section of the absorber, said units configured to modulate, manipulate and control the temperature of the liquid solvent system flowing therethrough.
  • the absorber is configured to receive near its bottom end a process gas stream or an exhaust gas stream containing at least one gaseous component to be removed, and to release from the opposite end of the absorber a stream of treated gas containing a reduced concentration of said gaseous component.
  • the piping infrastructure cooperates with at least one reboiler unit for regenerating the liquid solvent system, at least two heat exchange units configured for cooling the liquid solvent system flowing therethrough and at least one cooling unit for precise temperature control of the cooled liquid solvent system to be delivered to the first section of the absorber.
  • the delivery side of the piping infrastructure communicates with a first section of the absorber adjacent to the end wherefrom the treated gas stream is released.
  • the absorber device is provided with a second section adjacent the first section.
  • the second section is configured to: (a) communicate with a first portion of the piping infrastructure cooperating with said heat exchange unit configured for heating the liquid solvent system egressing from the bottom portion of the first section prior to the return of the absorption liquid to the top portion of the second section of the absorber, and (b) communicate with a second portion of the piping infrastructure that egresses the absorption liquid from the bottom portion of the second section and ingresses into the top portion of an underlying third section.
  • At least one heat exchange unit and a cooling unit are interposed the second portion of the piping infrastructure for controllably cooling and manipulating the temperature of absorption liquid solvent flowing therethrough from the second to the third section of the absorber.
  • the absorber device is provided with a third section adjacent the second section.
  • the third section is configured to: (a) communicate with a first portion of the piping infrastructure cooperating with at least one heat exchange unit and a cooling unit configured for controllably cooling and manipulating the temperature of absorption liquid solvent system egressing from bottom portion of the second section prior to the return of the absorption liquid to the top portion of the third section of the absorber, and (b) communicate with a second portion of the piping infrastructure that egresses the absorption liquid from the bottom portion of the third section and ingresses into the top portion of an underlying forth section.
  • At least one heat exchange unit and a cooling unit are interposed the second portion of the piping infrastructure for controllably cooling and manipulating the temperature of absorption liquid solvent flowing therethrough from the third to the fourth section of the absorber.
  • the absorber may be provided with a plurality of the sections configured similarly to the third section to communicate with a corresponding portion of the piping infrastructure cooperating with at least one dedicated heat exchange unit configured for cooling absorption liquid solvent flowing therethrough and a dedicated cooling unit for precise temperature control of absorption liquid solvent flowing from the bottom portion of one section before it ingresses the top portion of the adjacent underlying section of the absorber.
  • the exit side of the piping infrastructure i.e., the portion of piping infrastructure configured to remove the liquid solvent system from the last section of the absorber, is interconnected with the bottom end of the absorber adjacent the inlet for the gas stream.
  • the piping infrastructure communicates with at least one heat exchange unit configured for heating the liquid solvent system flowing through the piping infrastructure on the exit side of the absorber, while at the same time cooling the liquid solvent system flowing through the piping infrastructure interposed the second section and bottom section of the absorber, then communicates with at least one heat exchange unit configured for cooling the liquid solvent system flowing through the piping infrastructure into the absorber, and then is interconnected with a series of equipment selected and configured for: (a) separating and recovering the absorbed gaseous component contained within the liquid solvent system thereby stripping and regenerating the liquid solvent system, and (b) for bringing the stripped liquid solvent system to its boiling point thereby completing the regeneration process.
  • Suitable equipment may include condensers, phase separators, regenerators and reboilers commonly used in heating and cooling infrastructure installations.
  • Suitable regenerator units may be configured as packed-type or trayed-type, or spray-type or membrane-type units.
  • the configuration of the apparatus of the present invention may include one regenerator unit or alternatively, a plurality of cooperating units.
  • the reboiler unit may be a standard reboiler unit known in the art and may be operable by steam, combustion, electricity or other suitable heating source.
  • the invention also provides processes for removing at least one selected gaseous component from gas streams emanating from chemical and/or combustion processes by flowing a gas stream containing at least one gaseous component to be removed through said multi-sectioned absorber, and commingling and contacting the gas stream with a temperature-manipulable and temperature-controllable lean absorption liquid solvent system configured to absorb and/or sequester and/or react with said gaseous component, through a sequential series of temperature adjustments to the absorption liquid solvent system while the gas stream is flowing upward through said absorber.
  • a lean absorption liquid is an absorption liquid comprising at least one chemical compound selected to react with and/or sequester and/or absorb a selected gaseous component but actually contains very little of the certain gaseous component, and that an enriched absorption liquid is an absorption liquid solvent that has been saturated with the selected gaseous component removed from the gas stream.
  • the absorption liquid may optionally further comprise additives such as kinetic enhancers, corrosion inhibitors, anti-foam chemicals, oxygen scavengers, anti-degradation chemicals, salt neutralizers and other selected additives.
  • scrubbing can be used to describe the reaction and/or sequestering and/or absorption of a selected gaseous component by an absorption liquid configured to react with and/or sequester and/or absorb said gaseous component
  • treated can be used to describe a gas stream from which said gaseous component has been removed by reaction and/or sequestering and/or absorption with an absorption liquid configured for that purpose.
  • sinrubbed can be used to describe said gaseous component that has been removed by the absorption liquid from the gas stream.
  • the process comprises flowing a gas stream through an absorber provided with a plurality of sequentially adjacent sections wherein the incoming gas stream is commingled with a temperature-manipulable and temperature-controllable absorption liquid solvent system intercalating within and throughout the sections whereby a gaseous component present in the gas stream is increasingly scrubbed out by the absorption liquid solvent system as gas stream flows through the sequentially adjacent sections of the absorber.
  • the temperature-manipulable and temperature-controllable absorption liquid counter-flows through each section of the absorber against the flow of gas stream.
  • the temperature of the absorption liquid is adjusted to a relatively cool temperature prior to delivery and ingress of the cooled absorption liquid into the top portion of the first section of the absorber.
  • the cooled absorption liquid then flows downward against the upward flow of gas stream in the first section thereby commingling and contacting with said gas stream which results in the scrubbing and removal of the gaseous component into the absorption liquid, which is then considered to be a partially loaded absorption liquid.
  • the commingling and contacting of the cooled absorption liquid with the gas stream generates heat energy within the absorption liquid.
  • the heated partially loaded absorption liquid solvent egresses the first section at its bottom portion and passes through a heat exchange unit wherein the temperature of said partially loaded absorption liquid is further raised after which, the heated and temperature-manipulated partially loaded absorption liquid is ingressed to the top portion of the second section of the absorber.
  • the temperature-adjusted partially-loaded absorption liquid then flows downward against the upward flow of gas stream in the second section thereby commingling and contacting with said gas stream which results in additional heat generation and scrubbing and removal of the gaseous component into the absorption liquid solvent, which is then considered to be a heated increasingly loaded absorption liquid solvent.
  • the heated increasingly loaded absorption liquid solvent then egresses the second section at its bottom portion and flows into a heat exchange unit wherein the temperature of said increasingly loaded absorption liquid is lowered after which, the temperature-manipulated increasingly loaded absorption liquid flows through a cooling unit wherein the temperature of said absorption liquid is further cooled to a selected value, after which the cooled and temperature-adjusted increasingly-loaded absorption liquid solvent ingresses into the top portion of the third section of the absorber.
  • the temperature-adjusted increasingly-loaded absorption liquid then flows downward against the upward flow of gas stream in third section of the absorber thereby commingling and contacting with said gas stream which results in additional heat generation and further scrubbing and removal of the gaseous component into the absorption liquid, which is then considered to be a heated highly loaded absorption liquid.
  • the heated highly loaded absorption liquid solvent then egresses the third section at its bottom portion and flows into a heat exchange unit wherein the temperature of said highly loaded absorption liquid solvent is cooled after which, the temperature-manipulated highly loaded absorption liquid flows through a cooling unit wherein the temperature of said absorption liquid is adjusted further cooled to a selected value, after which the cooled temperature-adjusted highly loaded absorption liquid solvent ingresses into the top portion of the fourth section of the absorber.
  • the cooled temperature-adjusted highly-loaded absorption liquid then flows downward against the upward flow of gas stream in fourth section of the absorber thereby commingling and contacting with said gas stream as it enters the absorber and begins to flow upward which results in additional heat generation and scrubbing and removal of the gaseous component into the highly loaded absorption liquid, which is then considered to be a heated enriched absorption liquid.
  • an enriched absorption liquid is a lean absorption liquid that has been saturated with the gaseous component removed from the gas stream.
  • the gas stream containing the selected gaseous component is increasingly stripped of the gaseous component as the gas stream flows upward through the fourth, then third, then second, then first sections in the absorber while the lean absorption liquid becomes increasingly loaded with the scrubbed gaseous component as the absorption liquid flows downward through the first, then the second, then the third, then the fourth sections of the absorber.
  • additional sections may be added sequentially adjacent underneath the third section to provide more scrubbing of a gas stream flowing through the absorber to ensure energy-efficient removal of the selected gaseous component from the gas stream.
  • the process of the present invention provides an inverse temperature profile in the absorber device which is opposite to the profiles of the prior art conventional processes.
  • the temperature of absorber top is much lower than that of absorber bottom due to the release of heat energy from gas absorption.
  • the process of the present invention provides higher temperatures at the second section near the absorber top than at the gas inlet end of the absorber by the use of heat transfer equipment to: (a) heat partially loaded absorption liquid solvents at the second section of the absorber, and (b) to cool the absorption liquid solvents as they become increasingly enriched as they proceed toward the gas inlet end of the absorber device.
  • the heat captured during the cooling of the increasingly enriched liquid solvents is used for heating the rich absorption liquid solvent egressing the bottom of the absorber device.
  • the absorption capacity of the increasingly enriched absorption liquid solvent is increased by the use of pinched coolers cooperating with the heat transfer equipment to control the temperature of the enriched liquid solvent re-entering the absorber.
  • the invention also provides processes for recovering the selected gaseous component from the heated enriched absorption liquid.
  • the heated enriched liquid is fed into a regenerator, wherein it is processed to provide a stream of hot lean absorption liquid withdrawn from a reboiler unit at the bottom of the regenerator and a stream of hot vapor mixtures exiting the top of the regenerator.
  • the waste heat energy in the hot vapor stream is recovered by a heat-recovery condenser to produce a stream of heated condensate being delivered to the reboiler unit wherein the recovered heat energy is utilized for liquid regeneration, thus reducing the energy consumption of the absorption process.
  • the present invention provides a process for reducing the loss of water and absorption liquid from the top of absorber in the gas stream egressing through the gas outlet.
  • the process involves two-step water balance control wherein the first-step uses the cool-lean absorption liquid from lean cooler to reduce the temperature of treated gas and to knock off the vapor of water and absorption liquid.
  • the second-step water control uses the treated gas condenser operated at low temperature for final vapor loss reduction before the gas stream egresses out of the apparatus.
  • FIG. 1 An exemplary embodiment of the heat recovery gas absorption apparatus of the present invention is shown in the accompanying FIG. 1 and comprises a vertically orientated absorber 20 configured with a gas inlet 25 near the bottom of the absorber, a gas outlet 26 at the top of the absorber, and a plurality of sequentially stacked first section 21 , second section 22 , third section 23 and fourth section 24 , said sections sequentially interposed the outlet 26 and inlet 25 .
  • a process gas stream or exhaust gas stream 100 containing at least one gaseous component, e.g., CO 2 enters the absorber 20 at inlet 25 and flows upward through sections 24 , 23 , 22 , and 21 , and then exits the absorber through the outlet 26 .
  • the treated gas then passes through the treated gas condenser 27 which serves to remove any entrainment, i.e. water vapor and liquid solvent vapor.
  • an absorption liquid solvent system may be configured to react with and/or sequester and/or assimilate and/or absorb CO 2 from the gas stream, by the preparation of an aqueous solution containing single or blended alkanolamines such as monoethanolamine, diglycolamine, diethanolamine, methyldiethanolamine, 2-amino-2-methyl-1-propanol, piperazine and their mixtures.
  • the absorption liquid solvent system is heated to boiling in a reboiler 95 , which may occur at a temperature from the range of 105° C. to 125° C. depending on the alkanolamine composition of the absorption liquid solvent system.
  • the absorption liquid solvent system at said boiling point is considered to be a “lean” absorption liquid because its CO 2 content will be low.
  • the lean absorption liquid is withdrawn from the reboiler 95 into pipeline 110 by lean-liquid pump 51 and then is transferred through firstly, the hot side of a lean-rich heat exchange unit 34 where the temperature of the lean absorption liquid is reduced through transfer of its heat to the enriched absorption liquid passing through the cold side of said heat exchange unit 34 (explained in more detail below), then secondly passes through the hot side of a first heat-recovery heat exchange unit 31 where the temperature of the lean absorption liquid is further reduced by transfer of its heat to the partially loaded absorption liquid passing through the cold side of said heat exchange unit 31 , and thirdly through a cooling unit 41 wherein the temperature of the lean absorption liquid is further reduced to a final temperature in the range of 30° C. to 40° C. after which it is into the top portion of the first section 21 of the absorber 20 .
  • Such temperature is
  • the lean absorption liquid then counterflows downward against and commingles and contacts with the upward flowing gas stream thereby absorbing CO 2 and retaining heat generated by the exothermic reaction of CO 2 with the one or more alkanolamines provided in the absorption liquid.
  • the heated and partially loaded absorption liquid egresses from the bottom of the first section 21 through pipeline 111 which flows through the cold side of a first heat-recovery heat exchange unit 31 wherein heat is transferred from the lean absorption liquid passing through the hot side of said heat exchange unit 31 to the partially loaded absorption liquid thereby further heating the partially loaded absorption liquid to a selected temperature from the range of 40° C. to 70° C.
  • the hot partially loaded absorption liquid exits the heat exchange unit 31 via pipeline 112 .
  • the temperature of the partially loaded absorption liquid may be further adjusted in pipeline 112 by controllably diverting through a three-way valve or splitter 35 a portion of the lean absorption liquid exiting the lean-rich heat exchange unit 34 in pipeline 113 so that the diverted lean absorption liquid intermixes with the hot partially loaded absorption liquid in pipeline 112 .
  • An important consequence of intermixing the partially loaded absorption liquid with the lean absorption liquid is that the absorption capacity of the hot partially loaded absorption liquid for CO 2 is increased before it ingresses into the top portion of the second section 22 of the absorber 20 .
  • the hot partially loaded absorption liquid then counterflows downward against and commingles with and contacts the upward flowing gas stream thereby further absorbing CO 2 and retaining heat released by the exothermic reaction between CO 2 and the absorption liquid.
  • the increasingly heated and increasingly loaded absorption liquid egresses from the bottom of the second section 22 through pipeline 121 which enters the hot side of a second heat-recovery heat exchange unit 32 wherein heat is transferred from the heated increasingly loaded absorption liquid to the enriched absorption liquid passing through the cold side of said heat-recovery heat exchange unit 32 , thereby cooling said increasingly loaded absorption liquid which then exits the hot side of the heat exchange unit 32 in pipeline 122 and then passes through a first pinched cooling unit 42 to further cool the increasingly loaded absorption liquid to a selected temperature from the range of 30° C. to 40° C.
  • the cooled increasingly loaded liquid solvent then ingresses the top portion of the third section 23 of the absorber 20 .
  • the cooled increasingly loaded absorption liquid then counterflows downward against and commingles and contacts with the upward flowing gas stream thereby yet further absorbing CO 2 and retaining heat released by the exothermic reaction between CO 2 and the absorption liquid.
  • the heated highly loaded liquid solvent egresses from the bottom of the third section 23 through pipeline 131 which enters the hot side of a third heat-recovery heat exchange unit 33 wherein heat is transferred from the heated highly loaded absorption liquid thereby cooling said highly loaded absorption liquid which then exits the heat exchange unit 33 in pipeline 132 and then passes through a second pinched cooling unit 43 to further cool the highly loaded absorption liquid to a selected temperature from the range of 20° C. to 40° C.
  • the cooled highly loaded liquid solvent then ingresses the top portion of the fourth section 24 of the absorber 20 .
  • the cooled highly loaded absorption liquid then counterflows downward against and commingles and contacts with the incoming and upward flowing gas stream thereby even further absorbing CO 2 and retaining heat released by the exothermic reaction between CO 2 and the absorption liquid, thereby becoming a heated rich absorption liquid.
  • the heated rich absorption liquid is withdrawn from the bottom of the absorber 20 via a pipeline 140 by a rich liquid pump 52 which transfers the CO 2 -rich liquid through the cold side of the third heat exchange unit 33 wherein the heated CO 2 -rich liquid is further heated by the heated highly loaded absorption liquid, and exits the third heat exchange unit 33 into pipeline 141 which enters the cold side of the second heat exchange unit 32 wherein the CO 2 rich liquid is yet further heated by the heated increasingly loaded absorption liquid, and exits the second heat exchange unit 32 into pipeline 142 which enters the lean-rich exchange unit 34 where more heat is transferred to the rich absorption liquid from the hot lean absorption liquid in pipeline 110 .
  • the CO 2 -rich absorption liquid As the CO 2 -rich absorption liquid is increasingly heated as it passes through firstly the third heat exchange unit 33 and secondly, the second heat exchange unit 32 and thirdly, the lean-rich heat exchange unit 34 , some of the CO 2 contained within the rich absorption liquid is “stripped”, i.e., is released from the absorption liquid back into the gas phase, thus forming two-phase fluid.
  • the two-phase CO 2 -rich fluid stream then exits the lean-rich heat exchange unit 34 via pipeline 143 and is delivered to a phase separator 60 wherein the gaseous CO 2 stripped out of the rich liquid during its passage sequentially through heat exchange units 33 , 32 , and 34 , is separated and extracted through pipeline 145 for further processing, storage, or utilization while the rich absorption liquid with a reduced CO 2 content is transferred through pipeline 150 into a regenerator 65 into a section just underneath the reflux section 66 .
  • the rich absorption liquid then travels downward through the regenerator 65 against an upward flow of steam vapor which is generated from the reboiler 95 , and serves to further strip the absorbed CO 2 from the absorption liquid thereby making it increasingly “leaner”.
  • the leaner absorption liquid is transferred from the regenerator 65 through pipeline 152 to the reboiler unit 95 .
  • the gaseous stream containing the stripped CO 2 and water vapor exits the upper end of the regenerator 65 through pipeline 151 .
  • the water vapor is condensed in two stages by firstly, transfer through the hot side of a heat-recovery condenser 70 and then secondly, through a reflux condenser 75 .
  • Such a two-stage condensation produces a steam of two-phase fluid which is then flowed through a phase separator 80 wherefrom the high purity CO 2 gas stream is then removed through pipeline 155 for further processing, storage, or utilization.
  • the condensate in the phase separator 80 is withdrawn via pipeline 160 by condensate pump 85 and split into two streams by a three-way valve or splitter 90 .
  • the first stream is delivered to the cold side of heat-recovery condenser 70 by pipeline 161 wherein it is significantly heated by heat removed from the hot vapor stream exiting the reflux section 66 of the regenerator 65 .
  • the heated condensate is then delivered through pipeline 162 to the reboiler unit 95 wherein the recovered heat energy from the heat-recovery condenser is utilized to heat and regenerate the absorption liquid.
  • the second stream of condensate is delivered through pipeline 165 over the top portion of the reflux section 66 of the regenerator 65 .
  • the heat recovered from the hot vapor stream exiting the regenerator 65 by heat-recovery condenser 70 and subsequently delivered to the reboiler unit 95 by pipeline 162 results in a reduction in the quantity of heating medium required by the reboiler unit 95 through pipeline 175 in order to bring the absorption liquid to its boiling point thereby consuming less energy while maximizing the performance of CO 2 stripping and liquid regeneration.
  • the regenerated or lean absorption liquid is then recycled through pipeline 110 back to the absorber 20 for continued scrubbing of CO 2 from the gas stream entering the absorber 20 via pipeline 100 .
  • the hot vapor stream generated in the reboiler unit 95 is transferred through pipeline 170 into the bottom of the regenerator 65 and flows upwards against the downward flow of the rich absorption liquid to strip CO 2 from the rich absorption liquid.
  • CO 2 present in the gas stream delivered to the absorber 20 via pipeline 100 is increasingly scrubbed from the gas stream as it flows sequentially upward through sections 24 , 23 , 22 , and 21 .
  • the relatively low temperature of absorption liquid controls the temperature of treated gas so as to remove any entrainment of water vapor and liquid solvent vapor that may have exited the absorber with the treated gas.
  • the treated gas stream containing a reduced concentration of CO 2 exits the absorber through the outlet 26 .
  • the treated gas stream then passes through a treated gas condenser 27 which serves to further remove any entrainment of water vapor and liquid solvent vapor, after which, the vapor-eliminated gas stream is released from the apparatus through pipeline 101 .
  • the lean absorption liquid is introduced at the top of the absorber so that it flows downward against and repeatedly commingles and contacts with the gas stream in each of the sections 21 , 22 , 23 and 24 of the absorber 20 .
  • the apparatus of the present invention is configured so that the absorption liquid ingresses the top portion and egresses the bottom portion of each section so that the temperature of the absorption liquid solvent can be precisely manipulated and adjusted between each section of the absorber 20 , as illustrated in FIG. 2 , in order to provide optimal and maximal scrubbing of CO 2 from the gas stream while requiring low energy for solvent regeneration.
  • the temperature profile 221 of the lean absorption liquid in the first section 21 of the absorber 20 compares the increase in the temperature 210 of the feed liquid with the temperature 211 a of the egressing partially loaded liquid from about 32° C. to about 40° C., and then shows the manipulation and adjustment of the egressing partially loaded absorption liquid to increase its temperature 211 b to about 70° C.
  • the temperature profile 222 of the partially loaded absorption liquid in the second section 22 of the absorber 20 compares the increase in the temperature 221 of the ingressing partially loaded absorption liquid with the temperature 222 a of the egressing increasingly loaded absorption liquid from about 70° C.
  • the temperature profile 223 of the increasingly loaded liquid solvent in the third section 23 of the absorber 20 compares the increase in the temperature 231 of the ingressing cold increasingly loaded absorption liquid with the temperature 232 a of the egressing loaded absorption liquid from about 35° C. to about 52° C., and then shows the manipulation and adjustment of the egressing highly loaded absorption liquid to further reduce its temperature 232 b to about 25° C.
  • the temperature profile 224 of the highly loaded absorption liquid in the fourth section 24 of the absorber 20 (as illustrated in FIG.
  • FIG. 3 shows a typical McCabe-Thiele diagram for the absorber devices configured and operated as described herein.
  • the relationship between the concentration of specific gaseous component in gas phase (referred to as partial pressure of gaseous component) and the concentration of the said gaseous component in absorption liquid (referred to as liquid mole fraction of gaseous component) is represented by lines 300 and 311 .
  • Line 300 is commonly known by those skilled in these arts as the operating line, and illustrates the relationship between the partial pressure of the gaseous component and the liquid mole fraction of the gaseous component that actually prevails inside the absorber device.
  • Line 311 is commonly known by those skilled in these arts as the equilibrium line presenting the partial pressure of gaseous component in equilibrium with the said liquid mole fraction of gaseous component.
  • the operating line In the gas absorption operation, the operating line must lie above the equilibrium line in order to facilitate the transfer of gaseous component from gas stream to absorption liquid. It should be noted that the operating line shows that the partial pressure of gaseous component increases as the liquid mole fraction increases. In a typical gas absorption process, the partial pressure of gaseous component in the equilibrium line also increases with the liquid mole fraction. The equilibrium partial pressure of gaseous component, however, increases at a much higher rate compared to the operating partial pressure of gaseous component. This will result in an early crossing between the operating and equilibrium lines, thus limiting the gas absorption capacity.
  • the temperature of the absorption liquid passing through the absorber is manipulated and controlled by pinch coolers thereby preventing the early crossing between the operating and equilibrium lines, but instead establishing pinch regions shown as 305 , 306 , and 307 between the two lines, thereby providing a significant enhancement in gas absorption capacity.
  • Another exemplary embodiment of the present embodiment provides an absorber device in the form of a vertically oriented absorption column configured with a plurality of vertical sequentially stacked sections interposed a process gas inlet near the bottom of the column and a treated process gas outlet at the top of the column.
  • the plurality of sections may optionally be filled with either random-type or structured-type packing known to those skilled in these arts.
  • the absorber device may comprise other types of gas-liquid contacting devices known to those skilled in these arts as exemplified by trayed-type absorbers, spray-type absorbers, and membrane gas absorbers.
  • the apparatus of the present invention as exemplified in this example, is configured to provide means for:
  • the present invention provides a process to operate the apparatus of the present invention to minimize heat waste while achieving high gas absorption performance during removal and recovery of selected gaseous components from process or exhaust gas streams.
  • the absorber device is operated under two modes, i.e.: (a) thermodynamic-driven mass transfer at the front end of the absorber device, i.e. wherein the gas stream enters the absorber device, and (b) kinetic-driven mass transfer at the back end of the absorber device, i.e., wherein the gas stream exits the absorber device.
  • the kinetic-driven mass transfer is facilitated by performing gas absorption with an appropriately configured lean absorption liquid solvent system at an elevated temperature in the second section of the absorber device, i.e., the section next to the first section adjacent the gas stream outlet from the absorber device.
  • the thermodynamic-driven mass transfer is facilitated by performing gas absorption with liquid solution having relatively high gas content at a low temperature.
  • the process of the present invention provides an inverse temperature profile. In typical operation of conventional processes, the temperatures at the back end of the absorber devices are much lower than those at the front end of the absorber devices due to the exothermic release of heat energy during absorption of gaseous components by the liquid solvent systems. In contrast, the process of the present invention provides higher temperatures at the back end of the absorber device compared cooler temperatures provided at the front end of the absorber device.
  • a coal-fired power plant removes CO 2 from combustion flue gas with 95% removal efficiency by using a gas absorption unit provided with a 30% aqueous solution of monoethanolamine (MEA).
  • the flue gas is produced at a rate of 5,000,000 m 3 /day and contains 16.2% CO 2 (1,400 tonnes/day).
  • the temperature of the flue gas entering the absorber is 40° C.
  • the absorber pressure is 1 atm.
  • the reboiler temperature is 116° C.
  • An in-house process simulator was used for: (a) simulating the operations of the CO 2 absorption using the apparatus, methods and process configurations according to the present invention, and (b) comparisons of said operations with those of prior art systems.
  • Table 1 shows the simulation results and demonstrates that, compared to conventional and other processes, the present invention provides a lower temperature of rich absorption liquid at the bottom of the absorber, thus facilitating a rich-pinch operation, thereby achieving a greater CO 2 loading of rich absorption liquid and reducing circulating rate of absorption liquid.
  • the present invention also provides greater % CO 2 flashing before the regenerator than the prior art, thereby saving the energy used for solvent regeneration.
  • Case-A i.e.

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CA2646443A CA2646443C (en) 2006-03-23 2007-03-23 Heat recovery gas absorption process
KR1020087026022A KR20090008270A (ko) 2006-03-23 2007-03-23 열 복구 가스 흡수 프로세스
US12/294,136 US7906087B2 (en) 2006-03-23 2007-03-23 Heat recovery gas absorption process
PCT/CA2007/000461 WO2007107004A1 (en) 2006-03-23 2007-03-23 Heat recovery gas absorption process
JP2009501794A JP2009531163A (ja) 2006-03-23 2007-03-23 熱回収ガス吸収プロセス
AU2007229238A AU2007229238B2 (en) 2006-03-23 2007-03-23 Heat recovery gas absorption process
EP07710781A EP2004309A4 (en) 2006-03-23 2007-03-23 GAS ABSORPTION PROCESS WITH HEAT RECOVERY
CN2007800179397A CN101472662B (zh) 2006-03-23 2007-03-23 热回收气体的吸收方法

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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100031817A1 (en) * 2006-09-25 2010-02-11 Dais Analytic Corporation Enhanced hvac system and method
US20100083696A1 (en) * 2007-01-19 2010-04-08 Total S.A. Method for purifying a gas mixture containing acid gases
US20110174156A1 (en) * 2008-07-31 2011-07-21 Novozymes A/S Modular Reactor and Process for Carbon-Dioxide Extraction
US20120101767A1 (en) * 2010-10-22 2012-04-26 Kabushiki Kaisha Toshiba Carbon dioxide separation recovery system and method of measuring amount of reboiler input heat
US20130098126A1 (en) * 2010-04-23 2013-04-25 Co2Crc Technologies Pty Ltd. Process and plant for removing acid gases
US20130193373A1 (en) * 2007-05-29 2013-08-01 University Of Regina Method and absorbent compositions for recovering a gaseous component from a gas stream
US20130220122A1 (en) * 2012-02-27 2013-08-29 Kabushiki Kaisha Toshiba Carbon dioxide separating and collecting system and method of operating same
US20140112855A1 (en) * 2012-10-22 2014-04-24 Bp Alternative Energy International Limited Separation of Components from a Gas Mixture
WO2014109742A1 (en) * 2013-01-09 2014-07-17 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
JP2014156392A (ja) * 2008-02-22 2014-08-28 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置及びｃｏ２回収方法
US9314732B2 (en) 2013-01-09 2016-04-19 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
US20160236139A1 (en) * 2015-02-16 2016-08-18 Korea Institute Of Energy Research Absorption tower having absorption separator
CN112169541A (zh) * 2020-09-23 2021-01-05 怀化市恒渝新材料有限公司 一种光引发剂生产用尾气处理装置
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US11446603B2 (en) * 2017-07-06 2022-09-20 Qatar Foundation For Education, Science, Andcommunity Development Acid gas removal system for removing acidic gases from gaseous hydrocarbons
US11628392B2 (en) * 2017-08-07 2023-04-18 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claide Absorption column having external heat exchange circuit
GB2625299A (en) * 2022-12-13 2024-06-19 Rolls Royce Plc Improvements to energy performance in CO² capture

Families Citing this family (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2014347A1 (en) * 2007-07-03 2009-01-14 ALSTOM Technology Ltd Removal of carbon dioxide from flue gas
US7708801B2 (en) * 2007-11-09 2010-05-04 General Electric Company System and methods for treating transient process gas
US7862788B2 (en) * 2007-12-05 2011-01-04 Alstom Technology Ltd Promoter enhanced chilled ammonia based system and method for removal of CO2 from flue gas stream
US8192530B2 (en) * 2007-12-13 2012-06-05 Alstom Technology Ltd System and method for regeneration of an absorbent solution
FR2936165B1 (fr) * 2008-09-23 2011-04-08 Inst Francais Du Petrole Procede de desacidification d'un gaz par solution absorbante avec controle de la demixtion
DE102008050816B4 (de) * 2008-10-08 2013-09-05 Alstom Technology Ltd. Verfahren und Anordnung zur Abscheidung von CO2 aus Verbrennungsabgas
US8292989B2 (en) * 2009-10-30 2012-10-23 Alstom Technology Ltd Gas stream processing
JP5383338B2 (ja) 2009-06-17 2014-01-08 三菱重工業株式会社 Ｃｏ２回収装置及びｃｏ２回収方法
US8523979B2 (en) * 2009-06-22 2013-09-03 Basf Se Removal of acid gases by means of an absorbent comprising a stripping aid
JP4803470B2 (ja) * 2009-10-05 2011-10-26 独立行政法人産業技術総合研究所 熱交換型蒸留装置
DE102009052640A1 (de) * 2009-11-10 2011-05-12 Linde-Lkca-Dresden Gmbh Verfahren und Vorrichtung zur Gaswäsche
US8460436B2 (en) * 2009-11-24 2013-06-11 Alstom Technology Ltd Advanced intercooling and recycling in CO2 absorption
US9314734B2 (en) 2010-01-14 2016-04-19 Alstom Technology Ltd Wash water method and system for a carbon dioxide capture process
EA201300013A1 (ru) * 2010-07-28 2013-07-30 Саргас Ас Реактивная двигательная установка с улавливанием углерода
US8940261B2 (en) 2010-09-30 2015-01-27 The University Of Kentucky Research Foundation Contaminant-tolerant solvent and stripping chemical and process for using same for carbon capture from combustion gases
JP5637809B2 (ja) * 2010-10-21 2014-12-10 株式会社東芝 二酸化炭素回収方法及び二酸化炭素回収型汽力発電システム
JP5737916B2 (ja) * 2010-12-01 2015-06-17 三菱重工業株式会社 Ｃｏ２回収システム
CN102151456A (zh) * 2011-01-28 2011-08-17 北京化工大学 化学试剂法脱除沼气及类似气源中co2和h2s的方法及装置
US9133407B2 (en) 2011-02-25 2015-09-15 Alstom Technology Ltd Systems and processes for removing volatile degradation products produced in gas purification
CN102258928B (zh) * 2011-05-18 2013-12-25 成都华西工业气体有限公司 溶剂循环吸收法烟气脱硫中脱硫溶剂的加压热再生流程
WO2012163847A1 (de) * 2011-05-27 2012-12-06 Evonik Industries Ag Verfahren und vorrichtung zur abtrennung von kohlendioxid aus gasströmen
JP2013000729A (ja) * 2011-06-21 2013-01-07 Toshiba Corp 二酸化炭素回収装置および二酸化炭素回収方法
US8864878B2 (en) 2011-09-23 2014-10-21 Alstom Technology Ltd Heat integration of a cement manufacturing plant with an absorption based carbon dioxide capture process
US8911538B2 (en) 2011-12-22 2014-12-16 Alstom Technology Ltd Method and system for treating an effluent stream generated by a carbon capture system
US9028654B2 (en) 2012-02-29 2015-05-12 Alstom Technology Ltd Method of treatment of amine waste water and a system for accomplishing the same
US9101912B2 (en) 2012-11-05 2015-08-11 Alstom Technology Ltd Method for regeneration of solid amine CO2 capture beds
CN103100299B (zh) * 2013-01-31 2015-01-28 安徽淮化股份有限公司 用于处理乙二醇生产中产生的废气和废液的方法和装置
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KR101491521B1 (ko) * 2013-11-21 2015-02-11 한국에너지기술연구원 응축수를 활용한 에너지 절감형 산성 가스 포집 시스템 및 방법
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CN104826472B (zh) * 2015-04-23 2017-03-01 中石化石油工程设计有限公司 烟气二氧化碳捕集回收系统
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JP6656843B2 (ja) * 2015-08-21 2020-03-04 株式会社神戸製鋼所 ガス処理システム及びガス処理方法
ES2697300B2 (es) 2017-07-21 2019-05-24 Univ Sevilla Composicion acuosa para la separacion de co2 y/o gases acidos
CN109432952A (zh) * 2018-10-09 2019-03-08 四川亚联高科技股份有限公司 新型酸性气体吸收方法
JP2022109656A (ja) * 2021-01-15 2022-07-28 株式会社東芝 二酸化炭素回収システムおよび二酸化炭素回収システムの運転方法
WO2024019960A1 (en) * 2022-07-18 2024-01-25 Evoqua Water Technologies Llc Vertical flow quad-bed dry media scrubber for odor control
GB2622087A (en) * 2022-09-02 2024-03-06 Johnson Matthey Plc Carbon dioxide removal unit

Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4271132A (en) * 1966-02-01 1981-06-02 Eickmeyer Allen Garland Method and compositions for removing acid gases from gaseous mixtures
US4405577A (en) * 1981-11-13 1983-09-20 Exxon Research And Engineering Co. Non-sterically hindered-sterically hindered amine co-promoted acid gas scrubbing solution and process for using same
US4577642A (en) * 1985-02-27 1986-03-25 Medtronic, Inc. Drug dispensing body implantable lead employing molecular sieves and methods of fabrication
US5096150A (en) * 1984-11-29 1992-03-17 Westwood Samuel M Clamp device
US5358517A (en) * 1993-01-14 1994-10-25 Medtronic, Inc. Electrical medical lead with textured stylet guide
US5562689A (en) * 1993-08-20 1996-10-08 United States Surgical Corporation Apparatus and method for applying and adjusting an anchoring device
US5660166A (en) * 1993-05-21 1997-08-26 Aradigm Corporation Systems for the intrapulmonary delivery of aerosolized aqueous formulations
US6318101B1 (en) * 2000-03-15 2001-11-20 Carrier Corporation Method for controlling an electronic expansion valve based on cooler pinch and discharge superheat
US6500154B1 (en) * 2000-01-11 2002-12-31 Canox International Ltd. Intravascular access device positioning system
US6645446B1 (en) * 1998-11-23 2003-11-11 Floor Corporation Split-flow process and apparatus
US6781026B2 (en) * 2000-04-28 2004-08-24 Gtc Technology Inc. Aromatics purification from petroleum streams
US20040204592A1 (en) * 2003-03-24 2004-10-14 Manzer Leo Ernest Production of 5-methyl-N-(methyl aryl)-2-pyrrolidone, 5-methyl-N-(methyl cycloalkyl)-2-pyrrolidone and 5-methyl-N-alkyl-2-pyrrolidone by reductive amination of levulinic acid with cyano compounds
US20050033367A1 (en) * 2002-08-09 2005-02-10 Leung Jeffrey C. Suture anchor and method
US20050263452A1 (en) * 1999-12-08 2005-12-01 Jacobson James D Microporous filter membrane, method of making microporous filter membrane and separator employing microporous filter membranes
US6979236B1 (en) * 2004-07-07 2005-12-27 Fci Americas Technology, Inc. Wedge connector assembly
US20070179581A1 (en) * 2006-01-30 2007-08-02 Dennis Charles L Intravascular medical device
US20080033260A1 (en) * 2006-08-03 2008-02-07 Microchips, Inc. Cardiac Biosensor Devices and Methods
US7450993B2 (en) * 2004-09-08 2008-11-11 Spinal Modulation, Inc. Methods for selective stimulation of a ganglion
US7493174B2 (en) * 2004-09-23 2009-02-17 Medtronic, Inc. Implantable medical lead
US7515968B2 (en) * 2006-04-28 2009-04-07 Medtronic, Inc. Assembly method for spinal cord stimulation lead
US7519432B2 (en) * 2004-10-21 2009-04-14 Medtronic, Inc. Implantable medical lead with helical reinforcement
US20090248028A1 (en) * 2008-03-26 2009-10-01 Anthony Alexander Systems and Methods of Anchoring Surgical Wires, Catheters, and other Medical Objects

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1589231A (en) * 1977-04-21 1981-05-07 Shell Int Research Process for the removal of acidic gases
JPS5956584A (ja) * 1982-07-14 1984-04-02 エクソン・リサーチ・アンド・エンヂニアリング・コムパニー アルカリ系における腐食防止方法
US4702898A (en) * 1986-10-17 1987-10-27 Union Carbide Corporation Process for the removal of acid gases from gas mixtures
NO302454B1 (no) * 1996-07-31 1998-03-09 Kvaerner Asa Fremgangsmåte til fjerning av karbondioksid fra gasser
JP3416443B2 (ja) * 1997-01-27 2003-06-16 三菱重工業株式会社 脱炭酸塔内のアミンミストの減少方法
DE19753903C2 (de) * 1997-12-05 2002-04-25 Krupp Uhde Gmbh Verfahren zur Entfernung von CO¶2¶ und Schwefelverbindungen aus technischen Gasen, insbesondere aus Erdgas und Roh-Synthesegas
US6800120B1 (en) * 1998-11-23 2004-10-05 Fluor Corporation Split-flow process and apparatus
AU2003251783B2 (en) 2002-07-03 2007-08-09 Fluor Technologies Corporation Improved split flow process and apparatus
ATE473796T1 (de) * 2002-09-17 2010-07-15 Fluor Corp Konfigurationen und verfahren zur entfernung von sauren gasen
WO2004073838A1 (en) * 2003-02-18 2004-09-02 Union Engineering A/S Method for recovery of carbon dioxide from a gaseous source
DK1601445T3 (da) * 2003-03-10 2010-08-02 Univ Texas Regenerering af en vandig opløsning fra en syregasabsorptionsfremgangsmåde ved multitrins-flashing og stripping

Patent Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4271132A (en) * 1966-02-01 1981-06-02 Eickmeyer Allen Garland Method and compositions for removing acid gases from gaseous mixtures
US4405577A (en) * 1981-11-13 1983-09-20 Exxon Research And Engineering Co. Non-sterically hindered-sterically hindered amine co-promoted acid gas scrubbing solution and process for using same
US5096150A (en) * 1984-11-29 1992-03-17 Westwood Samuel M Clamp device
US4577642A (en) * 1985-02-27 1986-03-25 Medtronic, Inc. Drug dispensing body implantable lead employing molecular sieves and methods of fabrication
US5358517A (en) * 1993-01-14 1994-10-25 Medtronic, Inc. Electrical medical lead with textured stylet guide
US5660166A (en) * 1993-05-21 1997-08-26 Aradigm Corporation Systems for the intrapulmonary delivery of aerosolized aqueous formulations
US5562689A (en) * 1993-08-20 1996-10-08 United States Surgical Corporation Apparatus and method for applying and adjusting an anchoring device
US6645446B1 (en) * 1998-11-23 2003-11-11 Floor Corporation Split-flow process and apparatus
US20050263452A1 (en) * 1999-12-08 2005-12-01 Jacobson James D Microporous filter membrane, method of making microporous filter membrane and separator employing microporous filter membranes
US6500154B1 (en) * 2000-01-11 2002-12-31 Canox International Ltd. Intravascular access device positioning system
US6318101B1 (en) * 2000-03-15 2001-11-20 Carrier Corporation Method for controlling an electronic expansion valve based on cooler pinch and discharge superheat
US6781026B2 (en) * 2000-04-28 2004-08-24 Gtc Technology Inc. Aromatics purification from petroleum streams
US20050033367A1 (en) * 2002-08-09 2005-02-10 Leung Jeffrey C. Suture anchor and method
US20040204592A1 (en) * 2003-03-24 2004-10-14 Manzer Leo Ernest Production of 5-methyl-N-(methyl aryl)-2-pyrrolidone, 5-methyl-N-(methyl cycloalkyl)-2-pyrrolidone and 5-methyl-N-alkyl-2-pyrrolidone by reductive amination of levulinic acid with cyano compounds
US6979236B1 (en) * 2004-07-07 2005-12-27 Fci Americas Technology, Inc. Wedge connector assembly
US7450993B2 (en) * 2004-09-08 2008-11-11 Spinal Modulation, Inc. Methods for selective stimulation of a ganglion
US7493174B2 (en) * 2004-09-23 2009-02-17 Medtronic, Inc. Implantable medical lead
US7519432B2 (en) * 2004-10-21 2009-04-14 Medtronic, Inc. Implantable medical lead with helical reinforcement
US20070179581A1 (en) * 2006-01-30 2007-08-02 Dennis Charles L Intravascular medical device
US7515968B2 (en) * 2006-04-28 2009-04-07 Medtronic, Inc. Assembly method for spinal cord stimulation lead
US20080033260A1 (en) * 2006-08-03 2008-02-07 Microchips, Inc. Cardiac Biosensor Devices and Methods
US20090248028A1 (en) * 2008-03-26 2009-10-01 Anthony Alexander Systems and Methods of Anchoring Surgical Wires, Catheters, and other Medical Objects

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8470071B2 (en) * 2006-09-25 2013-06-25 Dais Analytic Corporation Enhanced HVAC system and method
US20100031817A1 (en) * 2006-09-25 2010-02-11 Dais Analytic Corporation Enhanced hvac system and method
US20100083696A1 (en) * 2007-01-19 2010-04-08 Total S.A. Method for purifying a gas mixture containing acid gases
US8287626B2 (en) * 2007-01-19 2012-10-16 Total S.A. Method for purifying a gas mixture containing acid gases
US20130193373A1 (en) * 2007-05-29 2013-08-01 University Of Regina Method and absorbent compositions for recovering a gaseous component from a gas stream
US9028593B2 (en) * 2007-05-29 2015-05-12 University Of Regina Method and absorbent compositions for recovering a gaseous component from a gas stream
JP2014156392A (ja) * 2008-02-22 2014-08-28 Mitsubishi Heavy Ind Ltd Ｃｏ２回収装置及びｃｏ２回収方法
US20110174156A1 (en) * 2008-07-31 2011-07-21 Novozymes A/S Modular Reactor and Process for Carbon-Dioxide Extraction
US9757682B2 (en) * 2010-04-23 2017-09-12 Uno Technology Pty Ltd Process and plant for removing acid gases
US20130098126A1 (en) * 2010-04-23 2013-04-25 Co2Crc Technologies Pty Ltd. Process and plant for removing acid gases
US8983791B2 (en) * 2010-10-22 2015-03-17 Kabushiki Kaisha Toshiba Carbon dioxide separation recovery system and method of measuring amount of reboiler input heat
US20120101767A1 (en) * 2010-10-22 2012-04-26 Kabushiki Kaisha Toshiba Carbon dioxide separation recovery system and method of measuring amount of reboiler input heat
US20130220122A1 (en) * 2012-02-27 2013-08-29 Kabushiki Kaisha Toshiba Carbon dioxide separating and collecting system and method of operating same
US20140112855A1 (en) * 2012-10-22 2014-04-24 Bp Alternative Energy International Limited Separation of Components from a Gas Mixture
US9242209B2 (en) * 2012-10-22 2016-01-26 Bp Alternative Energy International Limited Separation of components from a gas mixture
US9314732B2 (en) 2013-01-09 2016-04-19 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
US20160193561A1 (en) * 2013-01-09 2016-07-07 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
WO2014109742A1 (en) * 2013-01-09 2014-07-17 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
US10569215B2 (en) * 2013-01-09 2020-02-25 Fluor Technologies Corporation Systems and methods for reducing the energy requirements of a carbon dioxide capture plant
US20160236139A1 (en) * 2015-02-16 2016-08-18 Korea Institute Of Energy Research Absorption tower having absorption separator
CN105879586A (zh) * 2015-02-16 2016-08-24 现代自动车株式会社 具有吸收分离器的吸收塔
US9868085B2 (en) * 2015-02-16 2018-01-16 Hyundai Motor Company Absorption tower having absorption separator
US11446603B2 (en) * 2017-07-06 2022-09-20 Qatar Foundation For Education, Science, Andcommunity Development Acid gas removal system for removing acidic gases from gaseous hydrocarbons
US11628392B2 (en) * 2017-08-07 2023-04-18 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claide Absorption column having external heat exchange circuit
CN112169541A (zh) * 2020-09-23 2021-01-05 怀化市恒渝新材料有限公司 一种光引发剂生产用尾气处理装置
CN114832599A (zh) * 2022-04-02 2022-08-02 江苏爱尚环境科技有限公司 一种生产工艺尾气清洁处理装置
GB2625299A (en) * 2022-12-13 2024-06-19 Rolls Royce Plc Improvements to energy performance in CO² capture

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US7906087B2 (en) 2011-03-15
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