US20010004838A1 - Integrated heat exchanger system for producing carbon dioxide - Google Patents

Integrated heat exchanger system for producing carbon dioxide Download PDF

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Publication number
US20010004838A1
US20010004838A1 US09/756,167 US75616701A US2001004838A1 US 20010004838 A1 US20010004838 A1 US 20010004838A1 US 75616701 A US75616701 A US 75616701A US 2001004838 A1 US2001004838 A1 US 2001004838A1
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carbon dioxide
heat exchanger
stream
section
passing
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US09/756,167
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Kenneth Wong
Dante Bonaquist
Henry Howard
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Praxair Technology Inc
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Praxair Technology Inc
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Priority to US09/756,167 priority patent/US20010004838A1/en
Assigned to PRAXAIR TECHNOLOGY, INC. reassignment PRAXAIR TECHNOLOGY, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BONAQUIST, DANTE PATRICK, HOWARD, HENRY EDWARD, WONG, KENNETH KAI
Publication of US20010004838A1 publication Critical patent/US20010004838A1/en
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0295Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/02Processes or apparatus using separation by rectification in a single pressure main column system
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/70Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/74Refluxing the column with at least a part of the partially condensed overhead gas
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/02Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/60Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02Recycle of a stream in general, e.g. a by-pass stream
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/02Internal refrigeration with liquid vaporising loop
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/12External refrigeration with liquid vaporising loop
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/60Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/90External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02CCAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C10/00CO2 capture or storage
    • Y02C10/12Capture by rectification and condensation
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00Refrigeration
    • Y10S62/928Recovery of carbon dioxide

Abstract

A system for producing carbon dioxide wherein carbon dioxide feed fluid is first processed in a cooling section of an integrated heat exchanger before purification in a column, and wherein column bottom fluid operates within one of an evaporating section and desuperheating section of the heat exchanger and refrigerant fluid operates within the other of the evaporating section and desuperheating section of the heat exchanger.

Description

  • This application is a continuation-in-part of U.S. application Ser. No. 09/429,611, filed Oct. 29, 1999. [0001]
  • FIELD OF THE INVENTION
  • This invention generally relates to the recovery of carbon dioxide from a feed stream. [0002]
  • BACKGROUND ART
  • Large scale processing systems for recovering carbon dioxide from a feed stream are known in the art. Typically such systems are similar to systems which are used to carry out the cryogenic separation of air into its components and thus employ heat exchangers having relatively complicated structures as are typically required for the rigorous cryogenic separation of air. Such complicated structures are costly and it would be desirable to have a system for producing carbon dioxide which can employ a more advantageous heat exchanger arrangement. [0003]
  • Accordingly it is an object of this invention to provide a system for effectively producing carbon dioxide from a feed stream while employing an improved heat exchanger arrangment from that employed by conventional carbon dioxide recovery systems. [0004]
  • SUMMARY OF THE INVENTION
  • The above and other objects, which will become apparent to those skilled in the art upon a reading of this disclosure, are attained by the present invention, one aspect of which is: [0005]
  • A method for producing carbon dioxide comprising: [0006]
  • (A) passing carbon dioxide feed fluid through a cooling section of a heat exchanger having a cooling section, a desuperheating section and an evaporating section to produce cooled carbon dioxide feed fluid; [0007]
  • (B) passing cooled carbon dioxide feed fluid into a distillation column and producing carbon dioxide product fluid in the distillation column; [0008]
  • (C) recovering carbon dioxide product fluid from the lower portion of the distillation column as product carbon dioxide; and [0009]
  • (D) passing carbon dioxide product fluid through one of the evaporating section and the desuperheating section of the heat exchanger, and passing refrigerant fluid through one of the evaporating section and the desuperheating section of the heat exchanger. [0010]
  • Another aspect of the invention is: [0011]
  • Apparatus for producing carbon dioxide comprising: [0012]
  • (A) a heat exchanger having a cooling section, a desuperheating section and an evaporating section, and means for passing carbon dioxide feed fluid to the cooling section of the heat exchanger; [0013]
  • (B) a distillation column and means for passing carbon dioxide feed fluid from the cooling section of the heat exchanger to the distillation column; [0014]
  • (C) means for recovering carbon dioxide product fluid from the lower portion of the distillation column; [0015]
  • (D) means for passing carbon dioxide product fluid from the lower portion of the distillation column through one of the desuperheating section and evaporating section of the heat exchanger, and means for passing refrigerant fluid through one of the evaporating section and the desuperheating section of the heat exchanger. [0016]
  • As used herein the term “indirect heat exchange” means the bringing of two fluid streams into heat exchange relation without any physical contact or intermixing of the fluids with each other. [0017]
  • As used herein the terms “upper portion” and “lower portion” mean those sections of a column respectively above and below the mid point of the column. [0018]
  • As used herein the term “column” means a distillation or fractionation column or zone, i.e. a contacting column or zone, wherein liquid and vapor phases are countercurrently contacted to effect separation of a fluid mixture, as for example, by contacting of the vapor and liquid phases on a series of vertically spaced trays or plates mounted within the column and/or on packing elements such as structured or random packing. For a further discussion of distillation columns, see the Chemical Engineer's Handbook, fifth edition, edited by R. H. Perry and C. H. Chilton, McGraw-Hill Book Company, New York, Section 13[0019] , The Continuous Distillation Process.
  • Vapor and liquid contacting separation processes depend on the difference in vapor pressures for the components. The high vapor pressure (or more volatile or low boiling) component will tend to concentrate in the vapor phase whereas the low vapor pressure (or less volatile or high boiling) component will tend to concentrate in the liquid phase. Distillation is the separation process whereby heating of a liquid mixture can be used to concentrate the more volatile component(s) in the vapor phase and thereby the less volatile component(s) in the liquid phase. Partial condensation is the separation process whereby cooling of a vapor mixture can be used to concentrate the volatile component(s) in the vapor phase and thereby the less volatile component(s) in the liquid phase. Rectification, or continuous distillation, is the separation process that combines successive partial vaporizations and condensations as obtained by a countercurrent treatment of the vapor and liquid phases. The countercurrent contacting of the vapor and liquid phases can be adiabatic or nonadiabatic and can include integral (stagewise) or differential (continuous) contact between the phases. Separation process arrangements that utilize the principles of rectification to separate mixtures are often interchangeably termed rectification columns, distillation columns, or fractionation columns. [0020]
  • As used herein the term “cooling section” means a section of a heat exchanger wherein a fluid stream releases heat indirectly to one or more other fluid streams thereby cooling and/or condensing that stream. [0021]
  • As used herein the term “desuperheating section” means a section of a heat exchanger wherein a fluid stream is cooled with an accompanying decrease in temperature and the heat exchange is carried out without a phase change, i.e. boiling or condensation. [0022]
  • As used herein the term “evaporating section” means a section of a heat exchanger wherein a fluid stream absorbs heat and is at least partially vaporized. [0023]
  • As used herein the term “refrigerant fluid” means a fluid which absorbs heat and is subsequently compressed and condensed against another fluid. [0024]
  • BRIEF DESCRIPTION OF THE DRAWINGS
  • FIG. 1 is a schematic representation of a carbon dioxide recovery system as one preferred embodiment of the present invention. [0025]
  • FIG. 2 is a schematic representation of a carbon dioxide recovery system as another preferred embodiment of the present invention. [0026]
  • FIG. 3 is a schematic representation of a carbon dioxide recovery system incorporating another preferred embodiment of the present invention. [0027]
  • FIG. 4 is a schematic representation of a carbon dioxide recovery system incorporating yet another preferred embodiment of the present invention. [0028]
  • DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
  • A first preferred embodiment of the present invention will be discussed with reference to the single column carbon dioxide distillation system [0029] 130 shown in FIG. 1.
  • Feed stream [0030] 135, generally comprising at least 95 mole percent carbon dioxide as well as contaminants such as nitrogen, oxygen, water, argon, hydrogen, carbon monoxide and methane, enters a feed stream supply 136. Feed stream supply 136 compresses, cleans, dries and cools the feed stream using, for example, one or more compressors, phase separators and heat exchangers to prepare the feed stream for processing. Although not shown in FIG. 1, carbon adsorption beds may be used to extract hydrocarbons from the feed stream. A refrigeration system 160 circulates in streams 161 and 162 refrigerant fluid through feed stream supply 136 to assist in cooling the feed stream. Refrigeration system 160 may be a conventional refrigeration system. Examples of suitable refrigerant fluids include carbon dioxide, chlorodifluoromethane, ammonia and propane.
  • The cooled and dried feed stream exits feed stream supply [0031] 136 as stream 140 and enters a single integrated heat exchanger 145 with a temperature of about 40° F. to about 50° F. at a pressure of about 300 psia to about 350 psia. Heat exchanger 145 comprises a single module having two heat exchanger portions, each portion having a cooling section, a desuperheating section and an evaporating section. The feed stream is further cooled within heat exchanger 145 to a temperature of about −10° F. to about −20° F. in the cooling section of the first portion and is substantially liquefied in the cooling section of the second portion by transferring heat from the feed stream to stream 150 of carbon dioxide product fluid supplied from a column 165 and passing in the evaporating section of the first portion, and to stream 155 of refrigerant from refrigeration system 160 and passing in the desuperheating section of the first portion of heat exchanger 145.
  • The cooled carbon dioxide feed stream exits heat exchanger [0032] 145 as stream 170 and is introduced into the upper portion of column 165 to serve as the primary feed source to column 165. The carbon dioxide feed fluid flows down column 165 while being contacted with upwardly flowing stripping vapor such that the concentration of carbon dioxide in the feed fluid descending through column 165 becomes progressively enriched. Essentially pure liquid carbon dioxide is produced as carbon dioxide product fluid in the lower portion of column 165 and is withdrawn from the bottom of column 165. The stripping vapor is withdrawn from the upper portion of column 165.
  • To provide the stripping vapor, carbon dioxide product fluid is removed in stream [0033] 180 from the bottom of column 165 and is split into two streams. A first stream 150 is passed into heat exchanger 145 and is vaporized in an evaporating section of heat exchanger 145 at a temperature of about 0° F. to about 10° F. at a pressure of about 300 psia to about 350 psia as was previously described. The resulting carbon dioxide vapor is introduced into column 165 in the lower portion of column 165 and passes counter to the descending stream of liquid carbon dioxide. Thus, the carbon dioxide vapor resulting from warming the first stream 150 serves as the stripping vapor within column 165 to purify the descending feed stream.
  • A second stream [0034] 185 of the carbon dioxide product fluid removed from the bottom of column 165 is passed through flow control valve 190 and into heat exchanger 145. The second stream 185 is subcooled in a desuperheating section of heat exchanger 145 to a temperature of about −10° F. to about −20° F. in heat exchanger 145 by transferring heat to a refrigerant stream 195 supplied from refrigeration system 160 across a valve 200 and passing in an evaporating section of heat exchanger 145.
  • After exiting heat exchanger [0035] 145, a subcooled second stream 205 is split into two streams. A first stream 210 of the subcooled second stream 205 recovered as product carbon dioxide having a carbon dioxide concentration of up to 99.9 mole percent or more.
  • A second stream [0036] 215 of the subcooled second stream 205 is passed through valve 220 and is sent as 255 to a condenser 225 at a temperature of about −65° F. to about −55° F. at a pressure of about 80 psia to about 115 psia. Additionally, stripping vapor is fed as stream 230 to condenser 225 from the top of column 165 at a temperature of about −50° F. to about −15° F. The second stream 215 partially condenses the stripping vapor to a temperature of about −-50° F. to about −60° F. The partially condensed stripping vapor is then passed as stream 235 from condenser 225 to a phase separator 240. Condensed impure liquid carbon dioxide from the bottom of phase separator 240 is returned as stream 245 to the top of column 165 for further processing. Waste gas from the top of phase separator 240 is vented as stream 250 to the atmosphere. The liquid carbon dioxide fed as stream 255 to vent condenser 225 to cool and condense the stripping vapor exits reflux condenser 225 as stream 260 and is passed through valve 265 and returned as stream 270 to feed stream supply 136.
  • Heat exchanger [0037] 145 in the first preferred embodiment illustrated in FIG. 1 is a single, integrated brazed aluminum plate-fin type heat exchanger. By way of explanation, a plate-fin type heat exchanger includes at least three heat conductive plates separated by predetermined distances. The separations between adjacent plates provide passages through which fluids flow. These passages may be filled with heat conductive structures, such as metal fins, to facilitate heat transfer from one passage to another. Thus, a warm fluid flowing in one passage may efficiently transfer heat to a colder fluid flowing in an adjacent channel.
  • A relatively large number of passages may be easily created in a plate-fin type heat exchanger to allow a relatively large number of fluids to participate in heat transfer operations. For example, heat exchanger [0038] 145 of the present invention includes sufficient passages to allow heat exchanger 145 to cool and liquefy the entering feed stream from about 45° F. to about −20° F., vaporize a refrigerant stream at about −25° F., subcool a portion of a product stream from about 0° F. to about −20° F., and partially vaporize a remaining portion of the column bottoms. Heat exchanger 145 thus provides the advantage of replacing multiple heat exchangers with a single integrated unit. Further, within heat exchanger 145 of the present invention unfavorable temperature differences are minimized. Less piping and related structures are required because the above-noted heat exchange operations are performed within a single integrated core.
  • Another preferred embodiment of the carbon dioxide recovery system of the present invention is illustrated in FIG. 2. This preferred embodiment provides, among other features, a carbon dioxide distillation system [0039] 570 having a single unit incorporating a heat exchanger into a distillation column.
  • The preferred embodiment illustrated in FIG. 2 uses a feed stream supply [0040] 575 for receiving a carbon dioxide feed stream 580 and compressing, cleaning, drying and cooling the feed stream.
  • The carbon dioxide feed stream exits feed stream supply [0041] 575 as stream 585 and enters a brazed aluminum plate-fin type main heat exchanger 590 located below a distillation unit 595 of a distillation column 600. At this stage, the feed stream has a temperature of about 40° F. to about 50° F. and a pressure of about 300 psia to about 350 psia. Main heat exchanger 590 includes a first heat exchanger portion 605 and a second heat exchanger portion 610 separated by a partition 615. The feed stream 585 entering first heat exchanger portion 605 is cooled by passage through the cooling section of heat exchanger portion 605 to a temperature of about 5° F. to about 15° F. by exchanging heat with column bottoms contained in the evaporating section of heat exchanger 605. Liquid refrigerant 625 from refrigeration supply 620 is subcooled in the desuperheating section of heat exchanger 605 and also against boiling carbon dioxide product fluid.
  • The carbon dioxide feed stream and the carbon dioxide product fluid surrounding first heat exchanger [0042] 605 pass through partition 615 and into second heat exchanger portion 610. Within second heat exchanger 610 the feed stream is substantially condensed by passing through the cooling section of second heat exchanger 610. The latent heat of feed condensation is imported to the refrigerant in the evaporating section of second heat exchanger 610. After condensation in second heat exchanger 610, the feed stream has a temperature of about −20° F.
  • To provide refrigerant to the evaporating section of second heat exchanger [0043] 610, the refrigerant leaves first heat exchanger 605, passes in stream 630 across a valve 635 and is re-introduced into distillation column shell 600 at a location below partition 615. The refrigerant then collects at the bottom of column 600 and surrounds second heat exchanger 610 at a temperature of about −25° F.
  • The refrigerant surrounding second heat exchanger [0044] 610 is vaporized by the condensing carbon dioxide feed stream. At this stage, the refrigerant vapor has a temperature of about −25° F. The refrigerant vapor passes through a demister 640 to remove liquid droplets and exits column 600 to be recycled as stream 627 through refrigeration supply system 620. The refrigerant also provides product subcooling of stream 650.
  • The cooled and liquefied feed stream exits second heat exchanger [0045] 610 as stream 645 and is fed to the upper portion of distillation unit 595. The liquid feed stream thus becomes the primary feed stream descending through distillation unit 595 for purification. The liquid cooled carbon dioxide feed stream is enriched in distillation unit 595 by contacting a counterflowing stripping vapor to become almost pure carbon dioxide product fluid. After flowing down distillation column 595, the liquid carbon dioxide product fluid collects above partition 615 and surrounds first heat exchanger 605 in the evaporating section of heat exchanger 605. The carbon dioxide product fluid surrounding first heat exchanger 605 contributes to cooling the carbon dioxide feed stream passing through the cooling section of first heat exchanger 605, and a portion of the carbon dioxide product fluid passes through partition 615 through a pipe and through second heat exchanger 610, as previously discussed. After passing through second heat exchanger 610, the carbon dioxide product fluid exits column 600 as stream 650 and passes through valve 655 for recovery as product carbon dioxide.
  • A portion of the carbon dioxide product fluid surrounding first heat exchanger [0046] 605 is vaporized by indirect heat exchange with the carbon dioxide feed stream passing through the cooling section of first heat exchanger 605. The resulting carbon dioxide vapor passes into distillation unit 595.
  • The stripping vapor collects at the top of distillation column [0047] 600 after passing countercurrently to the descending carbon dioxide feed fluid in distillation unit 595. The stripping vapor is then fed as stream 660 from the top of the distillation column 600 into a secondary heat exchanger 665 at a temperature of about −10° F. to about −20° F. Secondary heat exchanger 665 cools and partially condenses the stripping vapor to a temperature of about −40° F. to about −60° F. The partially condensed stripping vapor drains as stream 670 directly into a phase separator 675 by way of piping. Waste gas from the top of phase separator 675 passes as stream 680 through secondary heat exchanger 665, across a valve 685 and is vented directly to the atmosphere. Impure carbon dioxide liquid is withdrawn as stream 690 from the bottom of phase separator 675, passes through valve 695 and through secondary heat exchanger 665. The carbon dioxide liquid is subsequently passed through valve 700 and as stream 701 is passed into feed compression and prepurification unit 575.
  • The preferred embodiment illustrated in FIG. 2 provides many advantages. For example, incorporating most of the heat transfer and mass transfer functions of a carbon dioxide distillation system into a single unit reduces the necessary piping and equipment for producing essentially pure carbon dioxide from a feed stream. Thus, this embodiment of the present invention reduces the complexities and costs of producing carbon dioxide from a feed stream. [0048]
  • Additional preferred embodiments are shown in FIGS. 3 and 4 and are described below. [0049]
  • One such embodiment comprises recovering a vapor stream containing carbon dioxide from the top of the distillation column, passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream, separating said partially condensed stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, and passing said carbon dioxide enriched liquid condensate stream into said distillation column. [0050]
  • With reference to FIG. 3, overhead gas stream [0051] 660 is directed to an additional pass through heat exchanger 610. The stream is cooled and partially condensed to −15 to −20° F. and exits as stream 700. Stream 700 is phase separated in vessel 701. Condensate stream 702 which is enriched in carbon dioxide is directed to a mechanical pump 703 where it is pressurized to a pressure greater than the presure in column 595. The pressurized condensate stream is then directed to the upper section of column 704. Alternatively, stream 704 can be directed into column feed pipe 645. The vapor derived from vessel 701 contains residual light gas contaminants and is directed to an atmospheric vent through pipe 705, valve 706 and pipe 707.
  • The advantage posed by the arrangement shown in FIG. 3 stems from the fact that a separate heat exchanger is not required to obtain an increased fraction of carbon dioxide from the feed stream. This arrangement reduces total package height and eliminates the separate vent exchanger, refrigerant, piping and controls. [0052]
  • Another embodiment comprises recovering a vapor stream containing carbon dioxide from the top of the distillation column, passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream thereby forming a vapor component and a liquid component, passing the vapor component and the liquid component together or separately into a second heat exchanger to further cool said liquid component and further partially condense said vapor component, recovering from said second heat exchanger a combined stream comprising said further cooled liquid component and said further partially condensed vapor component, separating said combined stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, passing said carbon dioxide depleted vapor stream and said carbon dioxide enriched liquid condensate stream through said second heat exchanger to vaporize said carbon dioxide enriched liquid into a carbon dioxide enriched vapor and to warm said carbon dioxide depleted vapor stream by heat exchange therein from said partially condensed vapor stream, and recycling said carbon dioxide enriched vapor to step (A) for passing through said cooling section. [0053]
  • With reference to FIG. 4, a carbon dioxide refrigerated vent condenser is incorporated into the process. In this arrangement, condensate stream [0054] 702 is directed through valve 800 and through pipe 801 into vent condenser 802. Vapor stream 705 is directed through valve 706 and through stream 707 and is rejoined with stream 801. Alternatively, stream 700 could be introduced into exchanger 802 directly. However, phase separator 701 is included in order to provide separate liquid and vapor streams which can be distributed individually within exchanger 802. If this were not done it is possible that maldistribution of liquid and vapor could occur within exchanger 802 reducing its overall efficiency. The combined stream emerges further cooled and further partially condensed as stream 803. Stream 803 is then phase separated in vessel 804. Condensate stream 805 is pressure reduced in valve 806 and directed to exchanger 802 via pipe 807. Stream 807 is substantially vaporized and emerges as gas stream 808 which can be recycled to feed compression train 575 (as previously noted in regard to FIGS. 1 and 2) for compression and subsequent additional carbon dioxide recovery. A residual vent gas stream 809 is taken from vessel 804 and warmed in exchanger 802 and vented to atmosphere through pipe 810, valve 811 and pipe 812.
  • The advantage posed by the embodiment of FIG. 4 stems from the fact that it is more suitable for lean feed streams (lower carbon dioxide content, <97% CO[0055] 2). Stream 803 is cooled/condensed to −60° F. and consequently significant additional carbon dioxide can be recovered as product.
  • In addition, the embodiment of FIG. 4 offers the option of eliminating the additional mechanical pump [0056] 703 shown in FIG. 3. This saves cost and increases process reliability.
  • While the present invention has been described with respect to what is considered to be the preferred embodiments, the invention is not limited to the disclosed embodiments. To the contrary, the invention is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims. The scope of the following claims is to be accorded the broadest interpretation so as to encompass all such modifications and equivalent structures and functions. [0057]

Claims (14)

1. A method for producing carbon dioxide comprising:
(A) passing carbon dioxide feed fluid through a cooling section of a heat exchanger having a cooling section, a desuperheating section and an evaporating section to produce cooled carbon dioxide feed fluid;
(B) passing cooled carbon dioxide feed fluid into a distillation column and producing carbon dioxide product fluid in the distillation column;
(C) recovering carbon dioxide product fluid from the lower portion of the distillation column as product carbon dioxide; and
(D) passing carbon dioxide product fluid through one of the evaporating section and the desuperheating section of the heat exchanger, and passing refrigerant fluid through one of the evaporating section and the desuperheating section of the heat exchanger.
2. The method of
claim 1
wherein carbon dioxide product fluid is passed through the evaporating section of heat exchanger and refrigerant fluid is passed through the desuperheating section of the heat exchanger.
3. The method of
claim 1
wherein carbon dioxide product fluid is passed through the desuperheating section of the heat exchanger and refrigerant fluid is passed through the evaporating section of the heat exchanger.
4. The method of
claim 1
wherein the heat exchanger comprises a first portion and a second portion with each portion having a cooling section, a desuperheating section and an evaporating section, and wherein the carbon dioxide feed fluid passes through the cooling sections of each of the first and second portions, carbon dioxide product fluid passes through the evaporating section of the first portion and the desuperheating section of the second portion, and refrigerant fluid passes through the desuperheating section of the first portion and the evaporating section of the second portion.
5. The method of
claim 4
further comprising recovering a vapor stream containing carbon dioxide from the top of the distillation column, passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream, separating said partially condensed stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, and passing said carbon dioxide enriched liquid condensate stream into said distillation column.
6. The method of
claim 4
further comprising recovering a vapor stream containing carbon dioxide from the top of the distillation column, passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream thereby forming a vapor component and a liquid component, passing the vapor component and the liquid component together or separately into a second heat exchanger to further cool said liquid component and further partially condense said vapor component, recovering from said second heat exchanger a combined stream comprising said further cooled liquid component and said further partially condensed vapor component, separating said combined stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, passing said carbon dioxide depleted vapor stream and said carbon dioxide enriched liquid condensate stream through said second heat exchanger to vaporize said carbon dioxide enriched liquid into a carbon dioxide enriched vapor and to warm said carbon dioxide depleted vapor stream by heat exchange therein from said partially condensed vapor stream, and recycling said carbon dioxide enriched vapor to step (A) for passing through said cooling section.
7. Apparatus for producing carbon dioxide comprising:
(A) a heat exchanger having a cooling section, a desuperheating section and an evaporating section, and means for passing carbon dioxide feed fluid to the cooling section of the heat exchanger;
(B) a distillation column and means for passing carbon dioxide feed fluid from the cooling section of the heat exchanger to the distillation column;
(C) means for recovering carbon dioxide product fluid from the lower portion of the distillation column;
(D) means for passing carbon dioxide product fluid from the lower portion of the distillation column through one of the desuperheating section and evaporating section of the heat exchanger, and means for passing refrigerant fluid through one of the evaporating section and the desuperheating section of the heat exchanger.
8. The apparatus of
claim 7
comprising means for passing carbon dioxide product fluid through the evaporating section of the heat exchanger, and means for passing refrigerant fluid through the desuperheating section of the heat exchanger.
9. The apparatus of
claim 7
comprising means for passing carbon dioxide product fluid through the desuperheating section of the heat exchanger, and means for passing refrigerant fluid through the evaporating section of the heat exchanger.
10. The apparatus of
claim 7
wherein the heat exchanger comprises a first portion and a second portion with each portion having a cooling section, a desuperheating section and an evaporating section, comprising means for passing carbon dioxide feed fluid to the cooling sections of each of the first and second portions, means for passing carbon dioxide product fluid to the evaporating section of the first portion and the desuperheating section of the second portion, and means for passing refrigerant fluid to the desuperheating section of the first portion and to the evaporating section of the second portion.
11. The apparatus of
claim 10
wherein the first and second portions are contained in a single heat exchanger module.
12. The apparatus of
claim 10
wherein the first and second portions are contained in separate heat exchanger modules.
13. The apparatus of
claim 10
further comprising means for recovering a vapor stream containing carbon dioxide from the top of the distillation column, means for passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream, means for separating said partially condensed stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, and means for passing said carbon dioxide enriched liquid condensate stream into said distillation column.
14. The apparatus of
claim 10
further comprising means for recovering a vapor stream containing carbon dioxide from the top of the distillation column, means for passing said vapor stream through one or both cooling sections of the heat exchanger to cool and partially condense said stream thereby forming a vapor component and a liquid component, means for passing the vapor component and the liquid component together or separately into a second heat exchanger to further cool said liquid component and further partially condense said vapor component, means for recovering from said second heat exchanger a combined stream comprising said further cooled liquid component and said further partially condensed vapor component, means for separating said combined stream into a liquid condensate stream enriched in carbon dioxide and a carbon dioxide depleted vapor stream, means for passing said carbon dioxide depleted vapor stream and said carbon dioxide enriched liquid condensate stream through said second heat exchanger to vaporize said carbon dioxide enriched liquid into a carbon dioxide enriched vapor and to warm said carbon dioxide depleted vapor stream by heat exchange therein from said partially condensed vapor stream, and means for recycling said carbon dioxide enriched vapor to step (A) for passing through said cooling section.
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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1398586A2 (en) * 2002-08-23 2004-03-17 The Boc Group, Inc. Method and apparatus for producing a purified liquid
EP2545977A1 (en) * 2011-07-11 2013-01-16 Alstom Technology Ltd Heat integration for cryogenic CO2 separation
WO2013039464A2 (en) * 2011-09-15 2013-03-21 Horowitz Alan Mark A system and method for recycling energy from ice remnants
CN103459815A (en) * 2011-03-22 2013-12-18 埃克森美孚上游研究公司 Methods of varying low emission turbine gas recycle circuits and systems and apparatus related thereto
CN103797228A (en) * 2011-03-22 2014-05-14 埃克森美孚上游研究公司 Low emission turbine systems incorporating inlet compressor oxidant control apparatus and methods related thereto
US20140196499A1 (en) * 2013-01-14 2014-07-17 Alstom Technology Ltd. Stripper overhead heat integration system for reduction of energy consumption

Families Citing this family (80)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070087401A1 (en) * 2003-10-17 2007-04-19 Andy Neilson Analysis of metabolic activity in cells using extracellular flux rate measurements
US7210312B2 (en) 2004-08-03 2007-05-01 Sunpower, Inc. Energy efficient, inexpensive extraction of oxygen from ambient air for portable and home use
US7666251B2 (en) * 2006-04-03 2010-02-23 Praxair Technology, Inc. Carbon dioxide purification method
US7819951B2 (en) * 2007-01-23 2010-10-26 Air Products And Chemicals, Inc. Purification of carbon dioxide
US8088196B2 (en) * 2007-01-23 2012-01-03 Air Products And Chemicals, Inc. Purification of carbon dioxide
US7850763B2 (en) * 2007-01-23 2010-12-14 Air Products And Chemicals, Inc. Purification of carbon dioxide
DE102007007581A1 (en) * 2007-02-15 2008-08-21 Linde Ag Carbon dioxide product producing method for gas analysis process, involves producing two-phase material-mixture by releasing fluid phase by throttle element, and vaporizing and heating fluid phase against application gas
WO2009121008A2 (en) 2008-03-28 2009-10-01 Exxonmobil Upstream Research Company Low emission power generation and hydrocarbon recovery systems and methods
AU2009228283B2 (en) 2008-03-28 2015-02-05 Exxonmobil Upstream Research Company Low emission power generation and hydrocarbon recovery systems and methods
US8535417B2 (en) * 2008-07-29 2013-09-17 Praxair Technology, Inc. Recovery of carbon dioxide from flue gas
US7927572B2 (en) * 2008-09-26 2011-04-19 Praxair Technology, Inc. Purifying carbon dioxide and producing acid
US8202702B2 (en) * 2008-10-14 2012-06-19 Seahorse Bioscience Method and device for measuring extracellular acidification and oxygen consumption rate with higher precision
JP5580320B2 (en) 2008-10-14 2014-08-27 エクソンモービル アップストリーム リサーチ カンパニー Method and system for controlling the combustion products
EP2438281B1 (en) 2009-06-05 2016-11-02 Exxonmobil Upstream Research Company Combustor system
FR2947329A1 (en) * 2009-06-24 2010-12-31 Air Liquide Device for cooling gas flow e.g. during combustion of fossil fuels, has two refrigeration units comprising exchangers with brazed aluminum plates, where one of refrigeration units is located downstream of other refrigeration unit
EA023673B1 (en) 2009-11-12 2016-06-30 Эксонмобил Апстрим Рисерч Компани Low emission power generation and hydrocarbon recovery system and method
FR2956900B1 (en) * 2010-03-01 2012-06-01 Air Liquide An apparatus and process for separating a mixture containing distilled carbon dioxide
CA2801499C (en) 2010-07-02 2017-01-03 Exxonmobil Upstream Research Company Low emission power generation systems and methods
BR112012031505A2 (en) 2010-07-02 2016-11-01 Exxonmobil Upstream Res Co stoichiometric combustion enriched air with exhaust gas recirculation
MX341981B (en) 2010-07-02 2016-09-08 Exxonmobil Upstream Res Company * Stoichiometric combustion with exhaust gas recirculation and direct contact cooler.
TWI564475B (en) 2010-07-02 2017-01-01 Exxonmobil Upstream Res Co Low emission triple-cycle power generation systems and methods
US8585802B2 (en) 2010-07-09 2013-11-19 Arnold Keller Carbon dioxide capture and liquefaction
US9903279B2 (en) 2010-08-06 2018-02-27 Exxonmobil Upstream Research Company Systems and methods for optimizing stoichiometric combustion
WO2012018458A1 (en) 2010-08-06 2012-02-09 Exxonmobil Upstream Research Company System and method for exhaust gas extraction
FR2969746B1 (en) 2010-12-23 2014-12-05 Air Liquide Condensation of a first fluid with the aid of a second fluid
TWI563166B (en) 2011-03-22 2016-12-21 Exxonmobil Upstream Res Co Integrated generation systems and methods for generating power
TWI563165B (en) 2011-03-22 2016-12-21 Exxonmobil Upstream Res Co Power generation system and method for generating power
TWI564474B (en) 2011-03-22 2017-01-01 Exxonmobil Upstream Res Co Integrated systems for controlling stoichiometric combustion in turbine systems and methods of generating power using the same
EP2505948B1 (en) * 2011-03-30 2018-10-10 General Electric Technology GmbH Cryogenic CO2 separation using a refrigeration system
FR2982168B1 (en) 2011-11-04 2015-05-01 Air Liquide Method and apparatus for separation of a gas rich in carbon dioxide by distillation
US9810050B2 (en) 2011-12-20 2017-11-07 Exxonmobil Upstream Research Company Enhanced coal-bed methane production
FR2988167B1 (en) 2012-03-13 2018-06-15 Air Liquide Method and apparatus separation of a mixture containing distilled carbon dioxide
US9353682B2 (en) 2012-04-12 2016-05-31 General Electric Company Methods, systems and apparatus relating to combustion turbine power plants with exhaust gas recirculation
US10273880B2 (en) 2012-04-26 2019-04-30 General Electric Company System and method of recirculating exhaust gas for use in a plurality of flow paths in a gas turbine engine
US9784185B2 (en) 2012-04-26 2017-10-10 General Electric Company System and method for cooling a gas turbine with an exhaust gas provided by the gas turbine
FR2993352B1 (en) * 2012-07-13 2018-07-13 Air Liquide Method and apparatus for separation of a gas rich in carbon dioxide
US10100741B2 (en) 2012-11-02 2018-10-16 General Electric Company System and method for diffusion combustion with oxidant-diluent mixing in a stoichiometric exhaust gas recirculation gas turbine system
US10107495B2 (en) 2012-11-02 2018-10-23 General Electric Company Gas turbine combustor control system for stoichiometric combustion in the presence of a diluent
US9611756B2 (en) 2012-11-02 2017-04-04 General Electric Company System and method for protecting components in a gas turbine engine with exhaust gas recirculation
US10215412B2 (en) 2012-11-02 2019-02-26 General Electric Company System and method for load control with diffusion combustion in a stoichiometric exhaust gas recirculation gas turbine system
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US9599070B2 (en) 2012-11-02 2017-03-21 General Electric Company System and method for oxidant compression in a stoichiometric exhaust gas recirculation gas turbine system
US9803865B2 (en) 2012-12-28 2017-10-31 General Electric Company System and method for a turbine combustor
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US20140250945A1 (en) 2013-03-08 2014-09-11 Richard A. Huntington Carbon Dioxide Recovery
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US20140332405A1 (en) * 2013-05-08 2014-11-13 Satish S. Tamhankar Hydrogen production process with carbon dioxide recovery
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US9915200B2 (en) 2014-01-21 2018-03-13 General Electric Company System and method for controlling the combustion process in a gas turbine operating with exhaust gas recirculation
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US10079564B2 (en) 2014-01-27 2018-09-18 General Electric Company System and method for a stoichiometric exhaust gas recirculation gas turbine system
US10047633B2 (en) 2014-05-16 2018-08-14 General Electric Company Bearing housing
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US10060359B2 (en) 2014-06-30 2018-08-28 General Electric Company Method and system for combustion control for gas turbine system with exhaust gas recirculation
US9819292B2 (en) 2014-12-31 2017-11-14 General Electric Company Systems and methods to respond to grid overfrequency events for a stoichiometric exhaust recirculation gas turbine
US9869247B2 (en) 2014-12-31 2018-01-16 General Electric Company Systems and methods of estimating a combustion equivalence ratio in a gas turbine with exhaust gas recirculation
US10094566B2 (en) 2015-02-04 2018-10-09 General Electric Company Systems and methods for high volumetric oxidant flow in gas turbine engine with exhaust gas recirculation
US10253690B2 (en) 2015-02-04 2019-04-09 General Electric Company Turbine system with exhaust gas recirculation, separation and extraction
US10316746B2 (en) 2015-02-04 2019-06-11 General Electric Company Turbine system with exhaust gas recirculation, separation and extraction
US10267270B2 (en) 2015-02-06 2019-04-23 General Electric Company Systems and methods for carbon black production with a gas turbine engine having exhaust gas recirculation
US10145269B2 (en) 2015-03-04 2018-12-04 General Electric Company System and method for cooling discharge flow

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4952223A (en) 1989-08-21 1990-08-28 The Boc Group, Inc. Method and apparatus of producing carbon dioxide in high yields from low concentration carbon dioxide feeds
JP3072766B2 (en) * 1990-03-16 2000-08-07 富士通株式会社 Scalar data processing system
JP2585874B2 (en) * 1991-03-18 1997-02-26 富士通株式会社 Color image of the edge detection method
US5275004A (en) 1992-07-21 1994-01-04 Air Products And Chemicals, Inc. Consolidated heat exchanger air separation process
US5815596A (en) * 1994-04-14 1998-09-29 Narendra Ahuja Multiscale image edge and region detection method and apparatus
GB9503592D0 (en) 1995-02-23 1995-04-12 Boc Group Plc Separation of gas mixtures
EP0771107B1 (en) * 1995-05-12 2002-12-11 Sony Corporation Key signal generating device, picture producing device, key signal generating method, and picture producing method
US5596883A (en) 1995-10-03 1997-01-28 Air Products And Chemicals, Inc. Light component stripping in plate-fin heat exchangers
US5592832A (en) 1995-10-03 1997-01-14 Air Products And Chemicals, Inc. Process and apparatus for the production of moderate purity oxygen
JP3679512B2 (en) * 1996-07-05 2005-08-03 キヤノン株式会社 Image extraction apparatus and method
US6798834B1 (en) * 1996-08-15 2004-09-28 Mitsubishi Denki Kabushiki Kaisha Image coding apparatus with segment classification and segmentation-type motion prediction circuit
US5927103A (en) 1998-06-17 1999-07-27 Praxair Technology, Inc. Carbon dioxide production system with integral vent gas condenser
US6697497B1 (en) * 1998-12-22 2004-02-24 Novell, Inc. Boundary identification and characterization through density differencing
JP2000293696A (en) * 1999-04-07 2000-10-20 Matsushita Electric Ind Co Ltd Picture recognizing device

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4694116B2 (en) * 2002-08-23 2011-06-08 ザ・ビーオーシー・グループ・インコーポレーテッドThe Boc Group Incorporated Method of manufacturing a purified fluid and equipment
JP2004085192A (en) * 2002-08-23 2004-03-18 Boc Group Inc:The Method and apparatus for producing purified liquid
EP1398586A3 (en) * 2002-08-23 2004-10-20 The Boc Group, Inc. Method and apparatus for producing a purified liquid
US6912872B2 (en) 2002-08-23 2005-07-05 The Boc Group, Inc. Method and apparatus for producing a purified liquid
US20050217315A1 (en) * 2002-08-23 2005-10-06 Walter Whitlock Method and apparatus for producing a purified liquid
US7263858B2 (en) * 2002-08-23 2007-09-04 The Boc Group, Inc. Method and apparatus for producing a purified liquid
EP1398586A2 (en) * 2002-08-23 2004-03-17 The Boc Group, Inc. Method and apparatus for producing a purified liquid
CN103797228A (en) * 2011-03-22 2014-05-14 埃克森美孚上游研究公司 Low emission turbine systems incorporating inlet compressor oxidant control apparatus and methods related thereto
CN103459815A (en) * 2011-03-22 2013-12-18 埃克森美孚上游研究公司 Methods of varying low emission turbine gas recycle circuits and systems and apparatus related thereto
WO2013008067A1 (en) * 2011-07-11 2013-01-17 Alstom Technology Ltd Heat integration for cryogenic co2 separation
EP2545977A1 (en) * 2011-07-11 2013-01-16 Alstom Technology Ltd Heat integration for cryogenic CO2 separation
CN103687659A (en) * 2011-07-11 2014-03-26 阿尔斯通技术有限公司 Heat integration for cryogenic co2 separation
AU2012282201B2 (en) * 2011-07-11 2015-09-17 General Electric Technology Gmbh Heat integration for cryogenic CO2 separation
WO2013039464A3 (en) * 2011-09-15 2014-04-03 Horowitz Alan Mark A system and method for recycling energy from ice remnants
WO2013039464A2 (en) * 2011-09-15 2013-03-21 Horowitz Alan Mark A system and method for recycling energy from ice remnants
US20140196499A1 (en) * 2013-01-14 2014-07-17 Alstom Technology Ltd. Stripper overhead heat integration system for reduction of energy consumption

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