US20140144178A1 - Optimized heat exchange in a co2 de-sublimation process - Google Patents

Optimized heat exchange in a co2 de-sublimation process Download PDF

Info

Publication number
US20140144178A1
US20140144178A1 US13/687,645 US201213687645A US2014144178A1 US 20140144178 A1 US20140144178 A1 US 20140144178A1 US 201213687645 A US201213687645 A US 201213687645A US 2014144178 A1 US2014144178 A1 US 2014144178A1
Authority
US
United States
Prior art keywords
carbon dioxide
stream
heat exchanger
solid carbon
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US13/687,645
Inventor
Paul TERRIEN
Pascal Tessier
Christopher Hoeger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Sustainable Energy Solutions Inc
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority to US13/687,645 priority Critical patent/US20140144178A1/en
Assigned to L'AIR LIQUIDE SOCIETE, ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE SOCIETE, ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AMERICAN AIR LIQUIDE, INC.
Assigned to SUSTAINABLE ENERGY SOLUTIONS, LLC reassignment SUSTAINABLE ENERGY SOLUTIONS, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: HOEGER, CHRISTOPHER
Assigned to AMERICAN AIR LIQUIDE, INC. reassignment AMERICAN AIR LIQUIDE, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TERRIEN, PAUL, TESSIER, PASCAL
Publication of US20140144178A1 publication Critical patent/US20140144178A1/en
Assigned to SUSTAINABLE ENERGY SOLUTIONS, LLC reassignment SUSTAINABLE ENERGY SOLUTIONS, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: HOEGER, CHRISTOPHER
Priority to US15/182,494 priority patent/US9766011B2/en
Assigned to NEWVISTAS CAPITAL, LLC reassignment NEWVISTAS CAPITAL, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AMERICAN AIR LIQUIDE, INC.
Assigned to SUSTAINABLE ENERGY SOLUTIONS, LLC reassignment SUSTAINABLE ENERGY SOLUTIONS, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: NEWVISTAS CAPITAL, LLC
Assigned to US DEPARTMENT OF ENERGY reassignment US DEPARTMENT OF ENERGY CONFIRMATORY LICENSE (SEE DOCUMENT FOR DETAILS). Assignors: SUSTAINABLE ENERGY SOLUTIONS, LLC
Abandoned legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • B01D53/002—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 condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/40—Control of freezing of components
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • Carbon dioxide emissions from fossil fuel combustion is a growing source of concern, and various technologies have been, and continue to be developed, for capturing CO2 from flue gas and other gas streams.
  • Major technologies include amine wash, physical adsorption technologies, cryogenic technologies (CO2 liquefaction). These technologies involve significant additional investment and operating costs for industrial plants. In the case of coal power plants for example, a resulting increase of the cost of electricity in the range of 4 to 5 US cents/kWh is expected.
  • One of the main challenges today is to reduce cost of carbon dioxide capture from flue gas through efficiency improvement and capital reduction.
  • anti-sublimation There are major drawbacks to all the existing systems.
  • the basic concept is to separate CO2 from a flue gas by cooling the flue gas to turn the CO2 into solid (de-sublimation or cryo-condensation of CO2). Indeed, at such low CO2 partial pressure ( ⁇ 5.11 atmosphere), the CO2 will be directly changed from gas phase to solid phase.
  • the present invention is a process for removing carbon dioxide from a compressed gas stream including cooling the compressed gas in a first heat exchanger, introducing the cooled gas into a de-sublimating heat exchanger, thereby producing a first solid carbon dioxide stream and a first carbon dioxide poor gas stream, expanding the carbon dioxide poor gas stream, thereby producing a second solid carbon dioxide stream and a second carbon dioxide poor gas stream, combining the first solid carbon dioxide stream and the second solid carbon dioxide stream, thereby producing a combined solid carbon dioxide stream, and indirectly exchanging heat between the combined solid carbon dioxide stream and the compressed gas in the first heat exchanger.
  • This invention relates to a specific process embodiment where the heat exchange is optimized in order to maximize efficiency in a realistic and cost-effective way.
  • the compressed flue gas stream 101 is first cooled down to above frosting point temperature in a multi-fluid heat exchanger 102 which may be a brazed aluminium heat exchanger (such as is a typical cryogenic heat exchanger used in Air Separation Units).
  • a multi-fluid heat exchanger 102 which may be a brazed aluminium heat exchanger (such as is a typical cryogenic heat exchanger used in Air Separation Units).
  • the refrigerated flue gas 103 is sent to a de-sublimating heat exchanger 104 where part of the CO2 is de-sublimated 113 .
  • the partially CO2 depleted flue gas 105 is sent to an expansion turbine 106 where it is expanded to almost atmospheric pressure 107 and the remainder of the CO2 to be captured is recovered as solids 109 in solids separator 108 , (i.e., achieving 90 % capture of the incoming CO2 flow rate when streams 113 and 109 are combined).
  • the solid CO2 streams 113 and 109 are mixed together 114 and pumped to a high pressure 116 in solids pressurizer 115 . This pressure should be high enough to not vaporize at ambient temperature. Then the high pressure CO2 stream 116 is sent to a melting heat exchanger 117 where most of the sensible heat plus the latent heat of fusion is recovered by the condensing refrigerant 123 . The liquefied CO2 118 is then sent to the multi-fluid heat exchanger 102 to recover the sensible heat of the liquid, after which the warmed fluid 119 exits the system. The 002 -depleted cold gas 110 is sent to the de-sublimating heat exchanger 104 and then to the multi-fluid heat exchanger 102 to recover all the cold. It is then pumped to the final pressure (not shown).
  • the refrigerant cycle is an inversed rankine cycle, the condensation happens in the melting heat exchanger 117 , close to CO2 triple point temperature, and vaporization happens in the de-sublimating heat exchanger 104 , below the outlet temperature of the de-sublimating heat exchanger. However, all other heat recovery involved will happen in the multi-fluid heat exchanger 102 .
  • FIG. 1 is a schematic representation of one embodiment of the present invention.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The present invention is a process for removing carbon dioxide from a compressed gas stream including cooling the compressed gas in a first heat exchanger, introducing the cooled gas into a de-sublimating heat exchanger, thereby producing a first solid carbon dioxide stream and a first carbon dioxide poor gas stream, expanding the carbon dioxide poor gas stream, thereby producing a second solid carbon dioxide stream and a second carbon dioxide poor gas stream, combining the first solid carbon dioxide stream and the second solid carbon dioxide stream, thereby producing a combined solid carbon dioxide stream, and indirectly exchanging heat between the combined solid carbon dioxide stream and the compressed gas in the first heat exchanger.

Description

    BACKGROUND
  • Carbon dioxide emissions from fossil fuel combustion is a growing source of concern, and various technologies have been, and continue to be developed, for capturing CO2 from flue gas and other gas streams. Major technologies include amine wash, physical adsorption technologies, cryogenic technologies (CO2 liquefaction). These technologies involve significant additional investment and operating costs for industrial plants. In the case of coal power plants for example, a resulting increase of the cost of electricity in the range of 4 to 5 US cents/kWh is expected. One of the main challenges today is to reduce cost of carbon dioxide capture from flue gas through efficiency improvement and capital reduction.
  • There are major drawbacks to all the existing systems. One possible alternative to traditional capture solutions is called anti-sublimation. The basic concept is to separate CO2 from a flue gas by cooling the flue gas to turn the CO2 into solid (de-sublimation or cryo-condensation of CO2). Indeed, at such low CO2 partial pressure (<5.11 atmosphere), the CO2 will be directly changed from gas phase to solid phase. There are two main schemes to implement such a process. The first is de-sublimation at atmospheric or very low pressure. For this scheme, a significant external refrigeration loop is required to perform such a cooling. This is known as indirect de-sublimation. The second is de-sublimation at higher pressure by expansion with solid formation. This is known as direct de-sublimation.
  • However, in any case, the efficiency of the process is strongly related to the ability to integrate the heat exchange. This is to say that without heat exchangers to recover energy from the flue gas notably, the efficiency of the process would be drastically decreased. Hence, there is a need in the industry for an optimized heat exchange in a carbon dioxide de-sublimation process.
    • SUMMARY
  • The present invention is a process for removing carbon dioxide from a compressed gas stream including cooling the compressed gas in a first heat exchanger, introducing the cooled gas into a de-sublimating heat exchanger, thereby producing a first solid carbon dioxide stream and a first carbon dioxide poor gas stream, expanding the carbon dioxide poor gas stream, thereby producing a second solid carbon dioxide stream and a second carbon dioxide poor gas stream, combining the first solid carbon dioxide stream and the second solid carbon dioxide stream, thereby producing a combined solid carbon dioxide stream, and indirectly exchanging heat between the combined solid carbon dioxide stream and the compressed gas in the first heat exchanger.
    • DESCRIPTION OF PREFERRED EMBODIMENTS
  • Illustrative embodiments of the invention are described below. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and are herein described in detail. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
  • It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another. Moreover, it will be appreciated that such a development effort might be complex and time-consuming, but would nevertheless be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.
  • This invention relates to a specific process embodiment where the heat exchange is optimized in order to maximize efficiency in a realistic and cost-effective way.
  • The compressed flue gas stream 101 is first cooled down to above frosting point temperature in a multi-fluid heat exchanger 102 which may be a brazed aluminium heat exchanger (such as is a typical cryogenic heat exchanger used in Air Separation Units).
  • After multi-fluid heat exchanger 102, the refrigerated flue gas 103 is sent to a de-sublimating heat exchanger 104 where part of the CO2 is de-sublimated 113.
  • After the de-sublimating heat exchanger 104, the partially CO2 depleted flue gas 105 is sent to an expansion turbine 106 where it is expanded to almost atmospheric pressure 107 and the remainder of the CO2 to be captured is recovered as solids 109 in solids separator 108, (i.e., achieving 90% capture of the incoming CO2 flow rate when streams 113 and 109 are combined).
  • The solid CO2 streams 113 and 109 are mixed together 114 and pumped to a high pressure 116 in solids pressurizer 115. This pressure should be high enough to not vaporize at ambient temperature. Then the high pressure CO2 stream 116 is sent to a melting heat exchanger 117 where most of the sensible heat plus the latent heat of fusion is recovered by the condensing refrigerant 123. The liquefied CO2 118 is then sent to the multi-fluid heat exchanger 102 to recover the sensible heat of the liquid, after which the warmed fluid 119 exits the system. The 002-depleted cold gas 110 is sent to the de-sublimating heat exchanger 104 and then to the multi-fluid heat exchanger 102 to recover all the cold. It is then pumped to the final pressure (not shown).
  • A small refrigeration loop is required in this configuration. The refrigerant cycle is an inversed rankine cycle, the condensation happens in the melting heat exchanger 117, close to CO2 triple point temperature, and vaporization happens in the de-sublimating heat exchanger 104, below the outlet temperature of the de-sublimating heat exchanger. However, all other heat recovery involved will happen in the multi-fluid heat exchanger 102.
  • The following points are important in order to achieve a high efficiency. There needs to be partial de-sublimation of the flue gas prior to the turbine, thus allowing less temperature difference between the inlet and the outlet of the turbine. This also allows the pressure required for the flue gas to be as low as approximately 6 bar absolute. There needs to be an inversed rankine cycle of the refrigerant with condensation happening at CO2 melting temperature There needs to be heat recovery of all fluids not involving solid CO2 in the multi-fluid heat exchanger (aluminium brazed in particular). The heat integration between flue gas lines, CO2 lines and refrigerant lines allows lowering the average temperature difference. Furthermore, a very low temperature approach (down to 2 C or below) would be achievable whereas typically 5 C is a reasonable limit in other types of heat exchanger.
    • A BRIEF DESCRIPTION OF THE DRAWINGS
  • FIG. 1 is a schematic representation of one embodiment of the present invention.

Claims (9)

What is claimed is:
1. A process for removing carbon dioxide from a compressed gas stream comprising:
a) cooling the compressed gas (101) in a first heat exchanger (102),
b) introducing the cooled gas (103) into a de-sublimating heat exchanger (104), thereby producing a first solid carbon dioxide stream (113) and a first carbon dioxide poor gas stream (105),
c) expanding the carbon dioxide poor gas stream, thereby producing a second solid carbon dioxide stream (109) and a second carbon dioxide poor gas stream (110),
d) combining the first solid carbon dioxide stream and the second solid carbon dioxide stream, thereby producing a combined solid carbon dioxide stream (114), and
e) indirectly exchanging heat between the combined solid carbon dioxide stream and the compressed gas in the first heat exchanger.
2. The process of claim 1, wherein the compressed gas is flue gas.
3. The process of claim 1, wherein the compressed gas is cooled to a temperature higher than the carbon dioxide de-sublimation temperature.
4. The process of claim 1, wherein the second carbon dioxide poor gas stream (110) is introduced into the de-sublimating heat exchanger (104) to indirectly exchange heat with the cooled gas (103).
5. The process of claim 1, wherein after the second carbon dioxide poor gas stream exits the de-sublimating heat exchanger, it (111) is introduced into the first heat exchanger (102) to indirectly exchange heat with the compressed gas (101).
6. The process of claim 1, further comprising introducing the combined solid carbon dioxide stream (114) into a second heat exchanger (117), after step d) and before step e), wherein the combined solid carbon dioxide stream indirectly exchanges heat with an external refrigeration loop (123).
7. The process of claim 6, wherein the external refrigeration loop comprises:
vaporizing a compressed refrigeration stream (125/127) in the de-sublimating heat exchanger (104), thereby producing a warmed refrigeration stream (129/130/120),
compressing the warmed refrigeration fluid (120), thereby producing a compressed refrigeration stream (122), and
condensing the compressed refrigeration stream in a second heat exchanger (117) by indirectly transferring heat with the combined solid carbon dioxide stream (114/116), thereby producing a cooled refrigeration stream (124).
8. The process of claim 6, wherein the compressed refrigeration stream (122) is further warmed (123) in the first heat exchanger (102) before indirectly transferring heat with the combined solid carbon dioxide stream.
9. The process of claim 6, wherein the cooled refrigeration stream (124) is further cooled (125) in the first heat exchanger (102), before being compressed.
US13/687,645 2012-11-28 2012-11-28 Optimized heat exchange in a co2 de-sublimation process Abandoned US20140144178A1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US13/687,645 US20140144178A1 (en) 2012-11-28 2012-11-28 Optimized heat exchange in a co2 de-sublimation process
US15/182,494 US9766011B2 (en) 2012-11-28 2016-06-14 Optimized heat exchange in a CO2 de-sublimation process

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US13/687,645 US20140144178A1 (en) 2012-11-28 2012-11-28 Optimized heat exchange in a co2 de-sublimation process

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US15/182,494 Continuation US9766011B2 (en) 2012-11-28 2016-06-14 Optimized heat exchange in a CO2 de-sublimation process
US15/182,494 Continuation-In-Part US9766011B2 (en) 2012-11-28 2016-06-14 Optimized heat exchange in a CO2 de-sublimation process

Publications (1)

Publication Number Publication Date
US20140144178A1 true US20140144178A1 (en) 2014-05-29

Family

ID=50772078

Family Applications (2)

Application Number Title Priority Date Filing Date
US13/687,645 Abandoned US20140144178A1 (en) 2012-11-28 2012-11-28 Optimized heat exchange in a co2 de-sublimation process
US15/182,494 Active US9766011B2 (en) 2012-11-28 2016-06-14 Optimized heat exchange in a CO2 de-sublimation process

Family Applications After (1)

Application Number Title Priority Date Filing Date
US15/182,494 Active US9766011B2 (en) 2012-11-28 2016-06-14 Optimized heat exchange in a CO2 de-sublimation process

Country Status (1)

Country Link
US (2) US20140144178A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10677524B2 (en) 2016-04-11 2020-06-09 Geoff ROWE System and method for liquefying production gas from a gas source
US11384962B2 (en) 2016-06-13 2022-07-12 Geoff ROWE System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic system
US11486638B2 (en) 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20180187972A1 (en) * 2017-01-05 2018-07-05 Larry Baxter Device for Separating Solid Carbon Dioxide from a Suspension
US20190168175A1 (en) * 2017-12-06 2019-06-06 Larry Baxter Solids-Producing Siphoning Exchanger
CN108854423B (en) * 2018-07-09 2020-12-29 哈尔滨工业大学 Flue gas waste heat driven desulfurization, denitration and carbon capture coupled flue gas purification system and flue gas treatment method
US20230134621A1 (en) 2021-11-02 2023-05-04 Chart Energy & Chemicals, Inc. Carbon Capture System and Method with Exhaust Gas Recirculation

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040011039A1 (en) * 2002-07-22 2004-01-22 Stinger Daniel Harry Cascading closed loop cycle (CCLC)
US20080173585A1 (en) * 2007-01-23 2008-07-24 Vincent White Purification of carbon dioxide
US20080302133A1 (en) * 2005-12-21 2008-12-11 Gaz De France Method and Device for Recovering Carbon Dioxide from Fumes
US20100107634A1 (en) * 2008-11-06 2010-05-06 Air Products And Chemicals, Inc. Rankine Cycle For LNG Vaporization/Power Generation Process
WO2010076467A1 (en) * 2008-12-19 2010-07-08 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Co2 recovery and cold water production method
US20120006022A1 (en) * 2010-07-09 2012-01-12 Purdue Research Foundation Organic rankine cycle with flooded expansion and internal regeneration
US20120137728A1 (en) * 2010-04-16 2012-06-07 Kourosh Zanganeh Auto-refrigerated gas separation system for carbon dioxide capture and compression
US20120297821A1 (en) * 2011-05-26 2012-11-29 Brigham Young University Systems and methods for separating condensable vapors from light gases or liquids by recruperative cryogenic processes
US20130025317A1 (en) * 2011-06-15 2013-01-31 L'Air Liguide Societe Anonyme Pour L' Etude Et L' Exploitation Des Procedes Georges Claude Process for Removing Carbon Dioxide From a Gas Stream using Desublimation
US20130081426A1 (en) * 2011-09-30 2013-04-04 Vitali Victor Lissianski Low temperature heat exchanger system and method

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012075266A2 (en) * 2010-12-01 2012-06-07 Black & Veatch Corporation Ngl recovery from natural gas using a mixed refrigerant

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040011039A1 (en) * 2002-07-22 2004-01-22 Stinger Daniel Harry Cascading closed loop cycle (CCLC)
US20080302133A1 (en) * 2005-12-21 2008-12-11 Gaz De France Method and Device for Recovering Carbon Dioxide from Fumes
US20080173585A1 (en) * 2007-01-23 2008-07-24 Vincent White Purification of carbon dioxide
US20100107634A1 (en) * 2008-11-06 2010-05-06 Air Products And Chemicals, Inc. Rankine Cycle For LNG Vaporization/Power Generation Process
WO2010076467A1 (en) * 2008-12-19 2010-07-08 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Co2 recovery and cold water production method
US20110252827A1 (en) * 2008-12-19 2011-10-20 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude CO2 Recovery And Cold Water Production Method
US20120137728A1 (en) * 2010-04-16 2012-06-07 Kourosh Zanganeh Auto-refrigerated gas separation system for carbon dioxide capture and compression
US20120006022A1 (en) * 2010-07-09 2012-01-12 Purdue Research Foundation Organic rankine cycle with flooded expansion and internal regeneration
US20120297821A1 (en) * 2011-05-26 2012-11-29 Brigham Young University Systems and methods for separating condensable vapors from light gases or liquids by recruperative cryogenic processes
US20130025317A1 (en) * 2011-06-15 2013-01-31 L'Air Liguide Societe Anonyme Pour L' Etude Et L' Exploitation Des Procedes Georges Claude Process for Removing Carbon Dioxide From a Gas Stream using Desublimation
US20130081426A1 (en) * 2011-09-30 2013-04-04 Vitali Victor Lissianski Low temperature heat exchanger system and method

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10677524B2 (en) 2016-04-11 2020-06-09 Geoff ROWE System and method for liquefying production gas from a gas source
US11408671B2 (en) 2016-04-11 2022-08-09 Geoff ROWE System and method for liquefying production gas from a gas source
US11384962B2 (en) 2016-06-13 2022-07-12 Geoff ROWE System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic system
US11486638B2 (en) 2019-03-29 2022-11-01 Carbon Capture America, Inc. CO2 separation and liquefaction system and method

Also Published As

Publication number Publication date
US20160290714A1 (en) 2016-10-06
US9766011B2 (en) 2017-09-19

Similar Documents

Publication Publication Date Title
US9766011B2 (en) Optimized heat exchange in a CO2 de-sublimation process
Xu et al. A novel CO2 cryogenic liquefaction and separation system
AU2012258510B2 (en) Systems and methods for separating condensable vapors from light gases or liquids by recuperative cryogenic processes
CN101231131B (en) Purification of carbon dioxide
CN102753252B (en) The method of carbon dioxide is obtained by carbon dioxide containing gas mixture
CA2588540C (en) Method to condense and recover carbon dioxide (co2) from co2 containing gas streams
US20130025317A1 (en) Process for Removing Carbon Dioxide From a Gas Stream using Desublimation
US20130111948A1 (en) Purification of Carbon Dioxide
CA2805336C (en) Energy efficient production of co2 using single stage expansion and pumps for elevated evaporation
CN101231130A (en) Purification of carbon dioxide
Clodic et al. A new method for CO2 capture: frosting CO2 at atmospheric pressure
CN101285573A (en) Purification of carbon dioxide
US10197328B2 (en) Method and apparatus for purifying a carbon dioxide-rich mixture at a low temperature
US10317135B2 (en) Separation at sub-ambient temperature of a gaseous mixture containing carbon dioxide and a lighter contaminant
TW201144703A (en) Method and installation for liquefying flue gas from combustion installations
US9746233B2 (en) Process for the separation of a gas rich in carbon dioxide
US10281208B2 (en) Method and apparatus for separating a carbon dioxide-rich gas
CN102917771A (en) Method and apparatus for producing liquid carbon dioxide
Fu et al. Reducing the power penalty related to CO2 conditioning in oxy-coal combustion plants by pinch analysis
US9797653B2 (en) Method and device for condensing a carbon dioxide-rich gas stream
Patil et al. Innovations in cryogenic carbon capture
US9995530B2 (en) Method for the capture of carbon dioxide through cryogenically processing gaseous emissions from fossil-fuel power generation
CN102853633B (en) Air-separating plant and include the system of this air-separating plant
US20230375266A1 (en) Process and apparatus for the cooling of a co2-rich flow
EP3271671B1 (en) Plant for the liquefaction of nitrogen using the recovery of cold energy deriving from the evaporation of liquefied natural gas

Legal Events

Date Code Title Description
AS Assignment

Owner name: L'AIR LIQUIDE SOCIETE, ANONYME POUR L'ETUDE ET L'E

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:AMERICAN AIR LIQUIDE, INC.;REEL/FRAME:029885/0660

Effective date: 20130123

Owner name: AMERICAN AIR LIQUIDE, INC., CALIFORNIA

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:TERRIEN, PAUL;TESSIER, PASCAL;SIGNING DATES FROM 20130115 TO 20130226;REEL/FRAME:029885/0473

Owner name: SUSTAINABLE ENERGY SOLUTIONS, LLC, UTAH

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:HOEGER, CHRISTOPHER;REEL/FRAME:029885/0527

Effective date: 20130221

AS Assignment

Owner name: SUSTAINABLE ENERGY SOLUTIONS, LLC, UTAH

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:HOEGER, CHRISTOPHER;REEL/FRAME:038815/0296

Effective date: 20130221

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO PAY ISSUE FEE

AS Assignment

Owner name: NEWVISTAS CAPITAL, LLC, UTAH

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:AMERICAN AIR LIQUIDE, INC.;REEL/FRAME:042882/0860

Effective date: 20170623

AS Assignment

Owner name: SUSTAINABLE ENERGY SOLUTIONS, LLC, UTAH

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:NEWVISTAS CAPITAL, LLC;REEL/FRAME:050961/0605

Effective date: 20191108

AS Assignment

Owner name: US DEPARTMENT OF ENERGY, DISTRICT OF COLUMBIA

Free format text: CONFIRMATORY LICENSE;ASSIGNOR:SUSTAINABLE ENERGY SOLUTIONS, LLC;REEL/FRAME:067046/0240

Effective date: 20200220